WO2016025716A1 - Procédés sur membrane à entraînement osmotique ainsi que systèmes et procédés pour la récupération de soluté d'extraction - Google Patents

Procédés sur membrane à entraînement osmotique ainsi que systèmes et procédés pour la récupération de soluté d'extraction Download PDF

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Publication number
WO2016025716A1
WO2016025716A1 PCT/US2015/045059 US2015045059W WO2016025716A1 WO 2016025716 A1 WO2016025716 A1 WO 2016025716A1 US 2015045059 W US2015045059 W US 2015045059W WO 2016025716 A1 WO2016025716 A1 WO 2016025716A1
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Prior art keywords
draw solution
distillation apparatus
solution
eductor
draw
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PCT/US2015/045059
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English (en)
Inventor
Zachary W. GOODMAN
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Oasys Water, Inc.
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Publication of WO2016025716A1 publication Critical patent/WO2016025716A1/fr

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    • 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
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/10—Vacuum distillation
    • B01D3/105—Vacuum distillation with the use of an ejector for creating the vacuum, the ejector being placed between evaporator or distillation devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
    • 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
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/001—Upstream control, i.e. monitoring for predictive control
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/005—Processes using a programmable logic controller [PLC]
    • C02F2209/006—Processes using a programmable logic controller [PLC] comprising a software program or a logic diagram
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/02—Temperature
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/03—Pressure
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/05—Conductivity or salinity
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/40—Liquid flow rate
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/16—Regeneration of sorbents, filters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/18—Removal of treatment agents after treatment

Definitions

  • the invention relates to osmotically driven membrane processes and more particularly to draw solute recovery techniques for osmotically driven membrane processes.
  • osmotically driven membrane processes involve two solutions separated by a semi-permeable membrane.
  • One solution may be, for example, seawater, while the other solution is a concentrated solution that generates a concentration gradient between the seawater and the concentrated solution.
  • This gradient draws water from the seawater across the membrane, which selectively permits water to pass, but not salts, into the concentrated solution.
  • the water entering the concentrated solution dilutes the solution.
  • the solutes then need to be removed from the dilute solution to generate potable water.
  • the potable water was obtained, for example, via distillation; however, the solutes were typically not recovered and recycled.
  • the invention generally relates to osmotically driven membrane systems and methods, for example, forward osmosis (FO), pressure retarded osmosis (PRO), osmotic dilution (OD), direct osmotic concentration (DOC), and the like, and to systems and methods for draw solute recovery in the osmotically driven membrane systems/processes.
  • FO forward osmosis
  • PRO pressure retarded osmosis
  • OD osmotic dilution
  • DOC direct osmotic concentration
  • the separation operation includes using an absorber configured to condense the draw solutes into the concentrated draw solution.
  • the solvent stream, dilute draw solution, or concentrated draw solution may be used as an absorbent in the absorber. Cooling may be used with the absorber.
  • the process may further include the step of compressing a gas stream resulting from separation of the draw solutes from the dilute draw solution using a gas compressor or a steam eductor driven by hydraulic pressure on an absorbing liquid stream to promote reabsorption of draw solutes into the concentrated draw solution.
  • low grade thermal energy is used to assist in the recovery of the draw solutes.
  • the recovery system uses a distillation apparatus (e.g., a packed column or a membrane device) to thermally separate the draw solutes out of a dilute draw solution using the low grade thermal energy.
  • An eductor is used to draw a vacuum on the distillation apparatus to lower the temperature of vaporization and draw the draw solute vapors into the eductor driving fluid.
  • the driving fluid i.e., the vacuum inducing medium
  • the absorption medium in one embodiment, is a portion of the dilute draw solution, which allows for the absorption of the vaporized draw solutes and eliminates the need for the separate absorption process required by the prior art.
  • the use of a portion of the dilute draw solution as the driving medium allows two otherwise separate processes to occur in a single unit: First, the media traveling through the nozzle induces a vacuum on the system, and second, the absorbent and vaporized draw solutes are mixed within the nozzle.
  • An additional advantage of this arrangement is that it also eliminates the introduction of non-condensable gases into the system.
  • the mixture of absorbent and draw solute vapors can be directed to an additional mixer, if necessary, and then to a heat exchanger/condenser to assist in condensing the draw solute vapors into the absorbent, thereby creating a new source of concentrated draw solution.
  • This new concentrated draw solution can be returned to the FO system or sent for further processing (e.g., additional condensation or separation processes or adjustment of the solutions chemical composition) prior to being returned to the FO system.
  • the invention relates to a system for concentrating a dilute draw solution from an osmotically driven membrane system.
  • the source of dilute draw solution can be available as part of the overall system or supplied by others from a remote osmotically driven membrane system.
  • the system includes a valve arrangement in fluid communication with a source of the dilute draw solution, where the valve arrangement is configured to apportion the dilute draw solution (e.g., via a 3- way valve or combination of valves manually or automatically actuated via a control system and any necessary sensors); a distillation apparatus disposed downstream of and in fluid communication with the valve arrangement, where the distillation apparatus is configured for receiving a first portion of the dilute draw solution; a source of thermal energy in communication with the distillation apparatus for vaporizing at least a portion of any draw solutes out of the first portion of the dilute draw solution within the distillation apparatus; an eductor disposed downstream of and in fluid communication with the valve arrangement and in parallel with and in fluid communication with the distillation apparatus, where the eductor is configured for receiving a second portion of the dilute draw solution and the vaporized portion of draw solutes via a vacuum generated by the educator (e.g., via any necessary plumbing, valves, sensors, etc.
  • a valve arrangement in fluid communication with a source
  • the condenser is configured for receiving a gas-liquid mixture of the dilute draw solution and the vaporized draw solutes from the eductor and a cooling fluid (e.g., water).
  • the condenser outputs a concentrated draw solution (i.e., the vaporized draw solutes condensed and absorbed by the second portion of the dilute draw solution) that can be recycled to the osmotically driven membrane system and the now hot fluid.
  • the hot fluid exiting the condenser can be reused elsewhere in the system (e.g., for preheating a feed solution or as the thermal energy to the distillation apparatus).
  • the system further includes a second recovery system that can be used in conjunction with the first system to, for example, recover draw solutes that reverse fluxed through a membrane within the osmotically driven membrane system.
  • the system includes a second distillation apparatus in fluid communication with a source of a concentrated feed solution from the osmotically driven membrane system and a source of thermal energy in communication with the second distillation apparatus for vaporizing at least a portion of any draw solute out of the concentrated feed solution within the second distillation apparatus.
  • This can be a second source of thermal energy or the same source as used in the first distillation apparatus (e.g., introduced in parallel to the different distillation apparatus).
  • the system also includes a second eductor disposed downstream of and in fluid communication with the valve arrangement and in parallel with and in fluid communication with the second distillation apparatus, where the second eductor is configured for receiving a third portion of the dilute draw solution and the vaporized at least one draw solute from the second distillation apparatus via a vacuum generated by the second eductor; and a second condenser disposed downstream of and in fluid communication with the second eductor.
  • the second condenser is configured for receiving a gas-liquid mixture of the dilute draw solution and the vaporized draw solutes from the second eductor and a cooling fluid (e.g., water).
  • the condenser outputs a second concentrated draw solution and the now hot fluid, which can be reused as previously described.
  • Additional embodiments of the system can include one or more knock-out pots disposed downstream of and in fluid communication with either of the condensers and configured for receiving the concentrated draw solution output and any remaining vapors.
  • a knock-out pot is disposed downstream of each condenser, in other embodiments, a single knock-out pot is used with both condensers.
  • the distillation apparatus can include at least one distillation column and/or a membrane distillation module. The distillation apparatus is also configured to output a product solvent.
  • the first portion of dilute draw solution is significantly larger than the second portion of dilute draw solution, for example, a ratio of about 3:1 to about 10:1.
  • the portions can be divided as necessary.
  • a portion of the dilute draw solution is siphoned off of the main source of dilute draw solution sufficient to create the necessary vacuum within the eductor(s) based, in part, on the available fluid flow rates and pressures, fluid temperatures, specific gravity, and viscosities, and vapor pressures.
  • the system includes a second distillation apparatus in fluid communication with a source of a concentrated feed solution from the osmotically driven membrane system, a second source of thermal energy in communication with the second distillation apparatus for vaporizing at least a portion of any draw solutes out of the concentrated feed solution within the second distillation apparatus, and a second eductor disposed downstream of and in fluid communication with the valve arrangement and in fluid communication with the first distillation apparatus and the second distillation apparatus.
  • the second eductor is configured for receiving the first portion of the dilute draw solution and the vaporized portion of draw solutes from the second distillation apparatus via a vacuum generated by the second eductor and outputting a mixture of vaporized draw solutes and the first portion of the dilute draw solution to the first distillation column.
  • the invention in another aspect, relates to an apparatus for recovering a product solvent from a feed solution and concentrating a dilute draw solution.
  • the apparatus includes an osmotically driven membrane system having a source of a concentrated draw solution including thermally removable solutes, where the osmotically driven membrane system is configured to introduce the feed solution to one side of a membrane and the concentrated draw solution to an opposite side of the membrane, thereby causing the solvent to diffuse across the membrane and dilute the concentrated draw solution, and a separation system in fluid communication with the osmotically driven membrane system.
  • the separation system is configured to receive the dilute draw solution and includes a valve arrangement configured to receive and apportion the dilute draw solution and a distillation apparatus disposed downstream of and in fluid communication with the valve arrangement, where the distillation apparatus is configured for receiving a first portion of the dilute draw solution and outputting vaporized draw solutes and the product solvent in response to the introduction of a source of thermal energy.
  • the system also includes an eductor disposed downstream of and in fluid communication with the valve arrangement and in parallel with and in fluid communication with the distillation apparatus, where the eductor is configured for receiving a second portion of the dilute draw solution and the vaporized draw solutes via a vacuum generated by the eductor, and a condenser disposed downstream of and in fluid communication with the eductor.
  • the condenser is configured for receiving a gas-liquid mixture of dilute draw solution and vaporized draw solutes from the eductor and a cooling fluid.
  • the condenser outputs a concentrated draw solution (i.e., the vaporized draw solutes condensed and absorbed by the second portion of the dilute draw solution) and the now hot fluid.
  • the invention relates to a method of recovering draw solutes from an osmotically driven membrane system.
  • the method includes the steps of providing a source of dilute draw solution from the osmotically driven membrane system, wherein the dilute draw solution includes thermally removable solutes; introducing the dilute draw solution to a valve arrangement; apportioning the dilute draw solution into at least a first portion and a second portion; introducing the first portion of dilute draw solution to a distillation apparatus;
  • introducing a source of thermal energy to the distillation apparatus vaporizing at least a portion of the dilute draw solution solutes out of the first portion of the dilute draw solution; introducing the second portion of dilute draw solution to an eductor such that the eductor generates a vacuum on the distillation apparatus to remove the vaporized dilute draw solution solutes; mixing the vaporized dilute draw solution solutes with the second portion of the dilute draw solution;
  • the method also includes the steps of recovering a product solvent from the distillation apparatus and additional separation and condensation steps to remove and/or absorb additional draw solute and/or solvent vapors.
  • FIG. 1 is a schematic representation of an exemplary osmotically driven membrane system/process using a solute recovery system in accordance with one or more embodiments of the invention
  • FIG. 2A is a schematic representation of an alternative osmotically driven membrane system/process including a draw solute recovery system using an eductor in accordance with one or more embodiments of the invention
  • FIG. 2B is a schematic representation of an alternative embodiment of the system/process of FIG.2A.
  • FIG. 3 is a schematic representation of an alternative osmotically driven membrane system/process using a compressor and eductor for draw solute recovery in accordance with one or more embodiments of the invention.
  • Various embodiments of the invention may be used in any osmotically driven membrane process, such as FO, PRO, OD, DOC, etc.
  • An osmotically driven membrane process for extracting a solvent from solution may generally involve exposing the solution to a first surface of a forward osmosis membrane.
  • the first solution (known as a process or feed solution) may be seawater, brackish water, wastewater, contaminated water, a process stream, or other aqueous solution.
  • the solvent is water; however, other embodiments may use non-aqueous solvents.
  • a second solution (known as a draw solution) with an increased concentration of solute(s) relative to that of the first solution may be exposed to a second, opposed surface of the forward osmosis membrane.
  • Solvent for example water, may then be drawn from the first solution through the forward osmosis membrane and into the second solution generating a solvent-enriched solution via forward osmosis.
  • Forward osmosis generally utilizes fluid transfer properties involving movement of solvent from a less concentrated solution to a more concentrated solution. Osmotic pressure generally promotes transport of solvent across a forward osmosis membrane from feed to draw solutions.
  • the solvent-enriched solution also referred to as a dilute draw solution, may be collected at a first outlet and undergo a further separation process.
  • purified water may be produced as a product from the solvent-enriched solution.
  • a second product stream i.e., a depleted or concentrated process solution, may be collected at a second outlet for discharge or further treatment.
  • the concentrated process solution may contain one or more target compounds which it may be desirable to concentrate or otherwise isolate for downstream use.
  • FIG. 1 depicts one exemplary osmotically driven membrane system/process 10 utilizing a draw solute recovery system 22 in accordance with one or more embodiments of the invention.
  • the system/process 10 includes a forward osmosis module 12, such as those described in U.S. Patent Nos. 6,391,205 and 7,560,029; and PCT Publication Nos. WO2009/155596, WO2011/059751, and WO2011/053794; and U.S. Patent Publication No. 2014/0224716; the disclosures of which are hereby incorporated by reference herein in their entireties.
  • the module 12 is in fluid communication with a feed solution source or stream 14 and a draw solution source or stream 16.
  • the draw solution source 16 can include, for example, a saline stream, such as sea water, or another solution as described herein that can act as an osmotic agent to dewater the feed source 14 by osmosis through a forward osmosis membrane within the module 12. Examples of draw solutions and draw solute recovery schemes are described in PCT Publication No. WO2014/078415, the disclosure of which is hereby incorporated by reference herein in its entirety.
  • the module 12 outputs a stream of concentrated solution 18 from the feed stream 14 that can be further processed, for example via the draw solute recovery system 22 as described later herein.
  • the module 12 also outputs a dilute draw solution 20 that can be further processed via the recovery system 22, examples of which are described and/or incorporated herein, where draw solutes and a target solvent can be recovered.
  • draw solutes are recovered for reuse.
  • FIGS. 2-3 Various osmotically driven membrane systems/processes are described with respect to FIGS. 2-3.
  • FIG. 2A depicts an embodiment of an osmotically driven membrane system 110 that generally includes one or more FO membrane modules 112 and one or more solute recovery/separation subsystems 122.
  • the basic operation of the FO module(s) 112 is as previously described, where a feed stream 114 and a concentrated draw solution (CDS) 116 are introduced to the module 112 and a concentrated feed stream 118 and a dilute draw solution (DDS) 120 are output from the module 112.
  • CDS concentrated draw solution
  • DDS dilute draw solution
  • the DDS 120 is directed to a recovery/separation system 122a where the draw solutes are recovered from the DDS and new CDS 116 is generated.
  • the DDS 120 is first introduced to one or more valves 128 (manually or automatically actuated via a control system, actuators, sensors, etc., as necessary) to apportion the DDS 120 to different devices within the system 122a.
  • a first portion of the DDS 120a is directed to a distillation apparatus 124a, while a second, typically much smaller portion (e.g., 75% to 90% for the first portion versus 25% to 10% for the second portion) of DDS 120b is directed to an eductor 126a.
  • the second portion 120b can be transported to the eductor via a pump 130a or other pressure transfer device.
  • the flow of the DDS 120b through the eductor creates a vacuum on the distillation apparatus 124a.
  • thermal energy e.g., low grade or waste heat
  • thermal energy 136a is introduced to the distillation apparatus 124a to volatilize the draw solutes within the DDS 120a.
  • the vacuum created by the flow of the DDS 120b through the eductor 126a allows the draw solutes to volatilize at a lower temperature and draws the draw solute vapors 121a out of the distillation apparatus 124a and into the DDS 120b within the eductor 126a.
  • the absorbent i.e., DDS 120b
  • draw solute mixture 123a is directed to a condenser 138a.
  • the mixture 123a may be directed to a an external mixing device (e.g., a static mixer) to ensure that the draw solute vapor 121a is well mixed within the solution 123a prior to being sent to the condenser or other heat exchange device.
  • a static mixer e.g., a static mixer
  • the mixture 123a may be condensed within the distillation apparatus 124a reboiler to capture additional waste heat.
  • a cooling fluid 137a e.g., plant water or other cooling medium
  • a heated fluid 139a exits the condenser 138a.
  • the heated fluid 139a can be recycled within the system 110 (e.g., used to preheat the feed 114 or the DDS 120 prior to introduction to the distillation apparatus 124a).
  • the condenser 138a outputs a regenerated draw solution 116' that may be directed back to the FO module(s) 112 or further processed prior to reuse in the FO module(s) 112.
  • the regenerated draw solution 116' can be directed to a knock-out pot 134a, or similar device, to remove and/or further condense any non-condensed vapors remaining in the mixture. In some cases, a minor amount of remaining, non-condensed vapors 144a may be vented to atmosphere. However, with this arrangement, virtually all of the vapors/draw solutes will be condensed and recovered. Additionally or alternatively, the draw solution 116' can, for example, have additional draw solutes added thereto to change its osmotic concentration (e.g., via a brine maker).
  • FIG. 2A also depicts a second, optional recovery/separation subsystem 122b that is similar to the first subsystem 122a, insofar as it includes a second distillation apparatus 124b, a second eductor 126b, a second pump 130b, and a second condenser 138b.
  • the distillation apparatus 124b is in fluid communication with the feed side of the osmotically driven membrane system 112 and configured to receive at least a portion of the concentrated feed solution 118. Typically, a small portion of draw solutes will reverse flux through the membrane and be carried away by the concentrated feed solution 118.
  • a source of thermal energy 136b is directed to the distillation apparatus 124b. In some embodiments, this may be the same source of thermal energy directed to the first distillation apparatus 124a or a completely separate source.
  • a third portion of DDS 120c is directed to the second eductor 126b, which is in fluid communication with the valve arrangement 128 and the second distillation apparatus 124b.
  • the second eductor 126b is configured to draw a vacuum on the second distillation apparatus 124b and thereby draw the vaporized solutes out of the apparatus 124b and into the absorbent (i.e., DDS 120c).
  • This mixture 123b can directed to the second condenser 138b, which operates the same as described with respect to the first condenser 138a.
  • FIG. 2A depicts the condensed/re-concentrated draw solution passing through a second knock-out pot 134b prior to being returned to the osmotically driven membrane system; however, this draw solution could be recombined with the re-concentrated draw solution from the first condenser 138a prior to being returned to the osmotically driven membrane system 112 or sent through any additional process (e.g., knock-out pot 134a).
  • FIG. 2B depicts an alternative version of the system 110 of FIG. 2A.
  • this system no longer includes the second condenser and has relocated the second eductor 126b, so that the additional draw solutes recovered from the concentrated feed solution 118 are directly input to the first distillation apparatus 124a for recovery via recovery/separation subsystem 122a.
  • the second distillation apparatus 124b is configured for receiving the concentrated feed 118 and source of thermal energy 136b as previously described.
  • the second eductor 126b is disposed in the DDS 120a input line to the first distillation apparatus 124a so that the flow of DDS through the second eductor 126b draws a vacuum on the second distillation apparatus 124b, thereby drawing the draw solute vapors 121b out of the feed and into the DDS stream 120a and creating a slightly more concentrated DDS stream 120c.
  • the more concentrated DDS stream 120c is further processed as described above with respect to FIG.2A.
  • FIG. 3 is a simplified schematic of an osmotically driven membrane system and related subsystem for recovering draw solutes similar to those systems described with respect to FIGS. 2A and 2B.
  • the system 200 includes one or more FO modules 212 in fluid
  • the system 200 also includes one or more compressors 270 and one or more steam eductors 226, along with any necessary condensers, pumps, valves, plumbing, etc., as described elsewhere herein.
  • the system 200 also operates similar to those described above; however, with a slightly different arrangement of the components and corresponding change in operation. Generally, the arrangement depicted in FIG. 3 utilizes low grade heat sources as the driving force to recover the draw solutes, while maintaining a vacuum on one or more of the distillation apparatus 224.
  • the concentrated feed stream (i.e., brine) 218 from the FO module(s) 212 is directed to the second distillation apparatus 224b, where any draw solutes that may have reverse fluxed through the FO membranes are vaporized.
  • Low grade heat or other source of thermal energy is introduced via the reboiler 268b.
  • the distillate (i.e., draw solute vapors) 221b from the brine distillation apparatus 224b are directed to one or more mechanical compressors 270, where the compressor(s) 270 pull a vacuum on the brine distillation apparatus 224b, lowering the boiling point of the draw solutes therein.
  • the condensate from the reboiler 268b can exit the distillation apparatus 224b along with the bottoms product, which is a further concentrated feed stream 218' .
  • This feed stream 218' can be recycled to the initial feed stream 214 for further processing, disposed of, or sent for additional concentration/processing (e.g., to a crystallizer).
  • the compressed draw solute vapors 221b which are now in the form of steam at a high pressure, is directed to an eductor 226 located at the top of the first distillation apparatus 224a (i.e., the dilute draw solution distillation apparatus) that pulls a vacuum on the apparatus 224a.
  • the vacuum created by the vaporized draw solutes 121b forced through the eductor 226 allows the dilute draw solution distillation apparatus 224a to operate at a lower boiling point, which in turn lowers the required temperature for separation of the draw solutes.
  • the exact amount of vacuum pulled on the apparatus 224a may vary, but will typically be in the range of about 50-150 Torr, preferably about 100 Torr.
  • the vaporized draw solutes 221b exiting the eductor 226, along with the vaporized draw solutes 221a pulled from the dilute draw solution distillation apparatus 224a, can be directed to a condenser (e.g., condenser 138 described above) to form the concentrated draw solution 216, which in turn can be recycled back to the FO module(s) 212.
  • a condenser e.g., condenser 138 described above
  • the apparatus 224a includes a reboiler 268a for introducing the low grade heat/thermal energy to the first distillation apparatus 224a.
  • the bottoms product 242 of the first distillation apparatus 224a is the product solvent, e.g., water, and may be combined with the reboiler condensate.
  • the product solvent e.g., water
  • the product solvent 242 can be used as is or sent for further processing to suit a particular application.
  • the devices, systems and methods described herein may generally include a controller for adjusting or regulating at least one operating parameter of a device or a component of the systems, such as, but not limited to, actuating valves and pumps, as well as adjusting a property or characteristic of one or more fluid flow streams through an osmotically driven membrane module, or other module in a particular system.
  • a controller may be in electronic communication with at least one sensor configured to detect at least one operational parameter of the system, such as a concentration, flow rate, pressure, pH level, or temperature.
  • the controller may be generally configured to generate a control signal to adjust one or more operational parameters in response to a signal generated by a sensor.
  • the controller can be configured to receive a representation of a condition, property, or state of any stream, component, or subsystem of the osmotically driven membrane systems and associated recovery systems.
  • the controller typically includes an algorithm that facilitates generation of at least one output signal that is typically based on one or more of any of the representation and a target or desired value such as a set point.
  • the controller can be configured to receive a representation of any measured property of any stream, and generate a control, drive or output signal to any of the system components, to reduce any deviation of the measured property from a target value.
  • process control systems and methods may monitor various concentration levels, such as may be based on detected parameters including pH and conductivity.
  • Process stream flow rates and tank levels may also be controlled. Temperature and pressure may be monitored, along with other operational parameters and maintenance issues.
  • Various process efficiencies may be monitored, such as by measuring product water flow rate and quality, heat flow and electrical energy consumption.
  • Cleaning protocols for biological fouling mitigation may be controlled such as by measuring flux decline as determined by flow rates of feed and draw solutions at specific points in a membrane system.
  • a sensor on a brine stream may indicate when treatment is needed, such as with distillation, ion exchange, breakpoint chlorination or like protocols.
  • FTIR Fourier Transform Infrared Spectrometry
  • a draw solution condition may be monitored and tracked for makeup addition and/or replacement of solutes.
  • product water quality may be monitored by conventional means or with a probe such as an ammonium or ammonia probe.
  • FTIR may be implemented to detect species present providing information which may be useful to, for example, ensure proper plant operation, and for identifying behavior such as membrane ion exchange effects.

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

La présente invention concerne des procédés sur membrane à entraînement osmotique ainsi que des systèmes et des procédés de récupération de solutés d'extraction dans le cadre de procédés sur membrane à entraînement osmotique. Les procédés sur membrane à entraînement osmotique comprennent l'extraction d'un solvant à partir d'une première solution en utilisant une seconde solution concentrée pour extraire le solvant de la première solution à travers une membrane semi-perméable. La récupération de soluté d'extraction peut être réalisée par différents moyens pour récupérer et recycler des solutés d'extraction contenus à l'intérieur d'une seconde solution diluée et obtenir un produit de type solvant.
PCT/US2015/045059 2014-08-15 2015-08-13 Procédés sur membrane à entraînement osmotique ainsi que systèmes et procédés pour la récupération de soluté d'extraction WO2016025716A1 (fr)

Applications Claiming Priority (4)

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US201462037921P 2014-08-15 2014-08-15
US62/037,921 2014-08-15
US201562118834P 2015-02-20 2015-02-20
US62/118,834 2015-02-20

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018064129A1 (fr) * 2016-09-27 2018-04-05 Oasys Water, Inc. Procédés sur membrane à entraînement osmotique et systèmes et procédés pour la récupération de soluté d'extraction

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3181797A (en) * 1963-04-03 1965-05-04 Hayes Spray Gun Company Mixing apparatus having plural eductors
US20060231377A1 (en) * 2003-08-01 2006-10-19 Costa Sergio M Desalination machine
US20140124443A1 (en) * 2012-11-07 2014-05-08 Robert L. McGinnis Systems and Methods for Integrated Heat Recovery in Thermally Separable Draw Solute Recycling in Osmotically Driven Membrane Processes
US20140224718A1 (en) * 2013-02-08 2014-08-14 Oasys Water, Inc. Osmotic separation systems and methods

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3181797A (en) * 1963-04-03 1965-05-04 Hayes Spray Gun Company Mixing apparatus having plural eductors
US20060231377A1 (en) * 2003-08-01 2006-10-19 Costa Sergio M Desalination machine
US20140124443A1 (en) * 2012-11-07 2014-05-08 Robert L. McGinnis Systems and Methods for Integrated Heat Recovery in Thermally Separable Draw Solute Recycling in Osmotically Driven Membrane Processes
US20140224718A1 (en) * 2013-02-08 2014-08-14 Oasys Water, Inc. Osmotic separation systems and methods

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018064129A1 (fr) * 2016-09-27 2018-04-05 Oasys Water, Inc. Procédés sur membrane à entraînement osmotique et systèmes et procédés pour la récupération de soluté d'extraction

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