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    • 专利摘要:
      RETROGRADED SOLUBLE SOLUTE RECOVERY FOR TREATMENTOF WATER BY DIRECT OSMOSISImproved systems and processes for water purification by direct osmosis or desalination are revealed here. According to one embodiment a process for purifying contaminated water is provided in which a flow of contaminated feed solution comprising water and with a first osmotic pressure is passed through a semipermeable membrane to an extraction side having a flow of extraction solution one second osmotic pressure on an extraction side of the semipermeable membrane. The diluted extraction solution stream is heated, agglomerated and cooled to produce a cooled, single phase water-rich stream, which is purified to produce a stream of water product.
    公开号:BR112013025175A2
    申请号:R112013025175-1
    申请日:2012-04-23
    公开日:2020-09-01
    发明作者:Gary Carmignani；Steve Sitkiewitz；John Wilfred Webley
    申请人:Trevi Systems Inc.；
    IPC主号:
    专利说明:

    "RETROGRADED SOLUBLE SOLUTE RECOVERY FOR WATER TREATMENT BY DIRECT OSMOSIS" Reference to related orders This order claims priority for United States Provisional Order No. 61/517. 687, entitled "REGENERATION OF RETROGRADE SOLUBLE SOLUTES FOR FORWARD OSMOSIS WATER TREATMENT", filed on April 25, 2011 and United States Provisional Application No. 61 / 572,394, entitled "RETROGRADE SOLUBLE SOLUTE FOR FORWARD OSMOSIS WATER TREATMENT", filed on 15 of 15 July 2011 both, hereby incorporated by reference in their entirety, for all purposes.
    Technology field This description refers to the desalination of sea water, brackish water, waste water and / or contaminated water.
    More specifically, the present description refers to desalination by direct osmosis.
    Background Direct osmosis is known in the art and has been the subject of recent study, due to the likelihood of future water scarcity and the corresponding increase in demand for cost-effective desalination and water purification technologies.
    Sea water, brackish water or, otherwise, contaminated water can be purified by extracting water (the solvent) through a semipermeable membrane, which rejects salts and other contaminants (the solutes). This approach to natural or direct osmosis is different from the widely used reverse osmosis process where water is forced to pass through a semipermeable membrane, acting similarly under pressure.
    In direct osmosis processes, water is extracted through the semipermeable membrane, using an extraction solution.
    The direct osmosis process does not purify water.
    Direct osmosis simply moves water from one set of solutes to another set of solutes.
    An analysis and summary of direct osmosis technology is provided by Miller and Evens, Forward Osmosis: A new approach to water purification and desalination, Sandia Report SAND2006-4634, July 2006, in which the concept of using soluble polymer extraction solutes retrograde is discussed.
    The process for carrying out the separation of solutes from water is not described.
    A direct osmosis system based on carbon dioxide-ammonia is described in US Patent Nos. 7,560,029 and 6,393,295 to McGinnis, where solubility as a function of solute temperature is used for partial solute separation from the water.
    The precipitated solutes revealed are solid salts and the equilibrium of the separation is achieved with distillation.
    United States Patent Application Serial No. 11 / 632,994 by Collins also describes the use of solubility as a function of the temperature of salts to separate extraction solute from water.
    United States patent application Serial No. 11 / 796,118 describes another direct osmosis system, which uses coated magnetic nanoparticles as an extraction solute.
    PCT WO / 2010/107804 describes the use of magnetic particles as a controllable osmotic agent.
    United States Patent No. 5,679,254 to Chakrabarti describes the use of solubility as a function of the temperature of polymers in water to perform desalination, although not by direct osmosis.
    United States Patent No. 8,021,553 to Iyer describes a system using solutes of retrograde soluble polymer and a nano filter for the separation and recovery of the solute micelles resulting from the product water.
    Iyer specifies extraction solutes with both a hydrophobic and hydrophilic component.
    Iyer also reveals the recovery of the solutes in semi-batch by collecting the precipitated extraction solute (or separate phase) in a nano filter and recovery of the solute by retrograde washing of the nano filter.
    Improved systems and processes for water purification by direct osmosis or desalination are disclosed here.
    Summary Improved systems and processes for water purification by direct osmosis or desalination are disclosed here.
    According to one embodiment, a process for purifying contaminated water is provided.
    The process includes providing a feed stream of the contaminated solution comprising water and having a first osmotic pressure on a feed side of a semipermeable membrane, and providing a stream of extraction solution comprising an extraction solute and having a second - osmotic pressure on one side extraction of the semipermeable membrane.
    Water is passed through the semipermeable membrane to the extraction side to produce a flow of diluted extraction solution.
    The extraction solute in the diluted extraction solution stream to produce a two-phase effluent stream.
    The extraction solute in the two-phase effluent stream is agglomerated to produce an agglomerated effluent stream.
    The agglomerated extraction solute is separated from the agglomerated effluent flow to produce a water-rich flow comprising water and residual extraction solute and a solute-rich flow comprising agglomerated extraction solute and water.
    The water-rich stream is cooled to dissolve the residual extraction solute and to produce a rich stream of cooling water.
    The residual extraction solute is separated from the cooled, single-phase water-rich flow to produce a flow of residual extraction solute and a product flow of purified water.
    The previous objectives, characteristics and advantages, and others, of the present disclosure will become more easily evident from the following detailed description of the exemplary modalities, as disclosed here.
    Brief description of the drawings The modalities of the present application are described, by way of example only, with reference to the attached figures, in which: FIG. 1 illustrates an exemplary direct osmosis process according to a modality; FIG. 2 illustrates an exemplary direct osmosis process according to another modality; FIG. 3 illustrates an exemplary direct osmosis process according to another modality; and FIG. 4 illustrates an exemplary process flow diagram of an exemplary direct osmosis system according to an embodiment.
    Detailed description It should be noted that, for simplicity and clarity of illustration, where considered appropriate, reference numerals can be repeated within the figures to indicate corresponding or similar elements.
    In addition, numerous specific details are established to provide a complete understanding of the examples of modalities described herein.
    However, it will be understood by those skilled in the art that the examples of modalities described here can be practiced without these specific details.
    In other cases, the methods, procedures and components have not been described in detail so as not to obscure the modalities described here.
    The present disclosure relates to improved extraction solution systems and processes for water purification by direct osmosis or desalination.
    The extraction solution systems and processes include a device for separating solutes from extraction solutions from a water solvent and concentrating the solutes of extraction solutions as part of a water purification system by direct osmosis.
    The extraction solutes disclosed here exhibit retrograde solubility.
    The solubility of the extraction solutes disclosed here decreases significantly with temperature, but has sufficient solubility under ambient conditions to provide a useful working osmotic pressure.
    The extraction solutes disclosed herein are preferably polymers specifically designed for use in a soluble retrograde direct osmosis water purification system and process.
    In an exemplary embodiment, the extraction solute is a random or sequential copolymer of low molecular weight diols, such as 1,2 propanediol, 1,3 propanediol and / or 1,2 ethanediol.
    The extraction solutes have an acceptable osmotic pressure for the specific application of purification with a cloud mist temperature between 40ºC to 90ºC and a molecular weight high enough to allow the refined filtration of the dissolved polymer using a nano filter and / or reverse osmosis membrane.
    In an exemplary embodiment, the extraction solute is a polyglycolic copolymer for use with an extraction solute recovery process including a cooler / separator for the recovery of large amounts of solute and a nano filter for the final recovery of the redissolved solute.
    The extraction solute copolymers disclosed herein consist of various numbers and orders of diols, which confer the necessary solution properties.
    Osmotic pressure, mist point temperature, molecular weight and molecular structure are adjusted by adding or subtracting the various monomer units.
    In an exemplary embodiment, units of 1.2 ethanediol are added to the extraction solute cup-polymer to increase the molecular weight and cloud point temperature of the resulting extraction solute polymer.
    On the other hand, the addition of 1,2 propanediol units to the extraction solute polymer results in a lower cloud point temperature and higher molecular weight of the resulting extraction solute polymer.
    In another exemplary embodiment, monomers of 1.3 propanediol or 1.2 ethanediol are replaced by a portion of higher molecular weight polypropylene glycol polymer monomers of 1.2 propanedioles to increase solubility and decrease the temperature of fog point of the resulting polymer.
    The osmotic pressure of the exemplary extraction solutes depends on the application and the desired recovery.
    Exemplary extraction solutes require greater osmotic pressure for high recovery in applications with process flows containing high concentrations of dissolved solids.
    The osmotic pressure of extraction solution required for systems and exemplary processes for desalination of water by direct osmosis of seawater is generally greater than ~ 30.99 kg / cm2 at a minimum, with more than ~ 41.32 kg / cm2 being preferred to allow reasonable product flow and recovery.
    In an exemplary embodiment, the solubility of the extraction solute decreases at a temperature sufficiently (~ 10ºC) above room temperature and sufficiently (~ 10ºC) below the temperature of the bubble formation point.
    In other words, the solubility of the extraction solute changes significantly and the dependence on solubility in temperature increases between temperatures of 40ºC to 90ºC.
    Examples of extraction solutes with a strong dependence on solubility in the lower temperature range (for example, closer to 40 ° C) are preferred to minimize the operating temperature of the regeneration steps in the process and to minimize the resulting energy loss.
    Within the limitations of osmotic pressure and mist point temperature, the chemistry of the exemplary extraction solute polymers is selected in order to control the molecular weight and / or the physical structure of the polymer, resulting in high (> 90% and preferably> 99%) rejection of the extraction solute through filtration.
    In addition, the chemistry of exemplary extraction solute polymers is selected to minimize the diffusion of solute through a direct osmosis membrane.
    Preferably, for the desalination of salt water, the osmotic pressure of an exemplary extraction solution containing 40% cup-polymer of extraction solute in water is greater than 30.99 kg / cm2, preferably greater than 41.32 kg / cm2, and more preferably greater than 51.66 kg / cm2, while the molecular weight of the extraction solute copolymer is greater than 500, preferably greater than 1000 and more preferably greater than 2000. Exemplary Compositions of Extraction Solute The following non-limiting examples are provided to illustrate exemplary modalities and are not intended to limit the scope of this disclosure.
    Polymeric compositions of extraction solute including a random polyoxy copolymer were formulated in concentrations of 30-70% by weight of extraction solute in solution.
    The effect of the concentration of the extraction solution under osmotic pressure at a typical direct osmosis operating temperature of 25ºC is shown in Table 1. Osmotic pressure was measured directly against a NaCl reference standard using equilibrium dialysis Table 1: Solute concentration Extraction versus Osmotic Pressure Extraction Solute Concentration (%) Osmotic Pressure (kg / cm2) 30 41.32 40 46.49 50 61.99 70 98.15 Figure 1 illustrates an exemplary direct osmosis process according to an modality.
    A stream of brackish water source 1 is fed to a feed side of a semipermeable membrane, in a direct osmosis module 3. A stream of extraction solution 18 is fed to an extraction side of a semipermeable membrane in the module of direct osmosis 3. The osmotic pressure of the flow of brackish water source 1 is less than the osmotic pressure of the flow of extraction solution 18. This differential pressure causes water from the flow of brackish water source 1 to permeate through of the semipermeable membrane, resulting in a flow of diluted extraction solution 5 and a flow of saline solution 2. The flow of diluted extraction solution 5 is passed through a network of heat exchangers 4, where the temperature is sufficiently increased to initiate phase separation.
    The network of heat exchangers 4 may include one or more heat exchangers configured in series or in parallel to increase the temperature of the diluted extraction solution 5. The temperature of the diluted extraction solution stream 19 that comes out as effluent from the network of heat exchangers 4 is sufficient to create a two-phase effluent.
    The two-phase extraction solution effluent stream 19 leaving the heat exchanger network 4 is fed to a temperature controlled coalescer 6 to agglomerate small solute-rich droplets into the heat exchanger network 4. The cooler 6 is designed to aggregate droplets rich in solute large enough to be separated in the subsequent phase separation process 8. In an exemplary embodiment, coalescer 6 is designed to aggregate droplets rich in solute, greater than 10 µm, from pre - transfer greater than 25 µm, and more preferably greater than 50 µm.
    The pressure drop caused by two-phase flows that passed through coalescer 6 is significantly less than the pressure drop caused by two-phase flows that passed through a nano filter.
    The use of coalescer 6 eliminates the added complexity and backwash required in semi-batch operations.
    Coalescer 6 can also be segregated into an upper section that comprises hydrophobic coalescent elements to agglomerate the extraction solute and a lower section that comprises hydrophilic coalescent elements to aggregate water.
    The degree of hydrophobicity of the hydrophobic coalescent elements and the degree of hydrophilicity of the hydrophilic coalescent elements are selected to achieve a certain degree of agglomeration of the extraction solute to greater than 10 µm.
    In an exemplary embodiment, the degree of hydrophobicity of the hydrophobic coalescent elements and the degree of hydrophilicity of the hydrophilic coalescent elements are selected to agglomerate the extraction solute to greater than 10 µm.
    The coalescent effluent stream 7 is fed to a controlled temperature gravity separator 8, centrifuge, hydro-cyclone or a similar device, in which the solute-rich drops of the coalescer are accumulated.
    The gravity phase separator 8 is designed to separate solute from water and produce a continuous flow rich in solute 10 and a continuous flow rich in water 9. In an exemplary embodiment, the operating temperature of coalescer 6 and phase separator by gravity 8 it is maintained at less than 150 ° C, preferably less than 100 ° C and more preferably less than 80 ° C to establish a specific concentration of the solute and osmotic pressure of the water-rich flow 9 leaving as effluent from the separator 8. In an exemplary embodiment, the operating temperature of the coalescer 6 and phase separator by gravity 8 is selected to establish a solute concentration in the water-rich flow 9 of less than 5%, preferably less than 2% and more preferably less than 1% by weight of solution solute.
    In an exemplary embodiment, the gravity phase separator 8 is designed to concentrate the solute in the solute-rich flow 10 at a concentration greater than 60%, preferably greater than 80% and more preferably greater than 90%, by weight, of solute in solution.
    The solute-rich stream 10 which leaves the phase separator 8 as an effluent is cooled in a heat exchanger 16. The water-rich stream 9 which leaves as the phase 8 separator effluent is also cooled by a heat exchanger 11 to allow residual solute to be dissolved again and to create a single phase, water-rich, cooled flow
    12. The cooled water-rich flow 12 is a single-phase flow fed to a nano filter 13, ultrafilter, or reverse osmosis module, including a semipermeable membrane, or a device similar to that used to separate the residual solute from the product water .
    Nano filter 13 is selected to reject solute molecules based on size or structure and, ideally, passes most of the dissolved salt.
    The final filtration step in the nano filter 13, ultrafilter, reverse osmosis module, or similar device, is used only for the recovery of the residual solutes in the cool, single-phase water flow, cooled 12. The solutes are dissolved again in a flow rich in single-phase water, cooled 12 to minimize the pressure drop through the nano filter 13 and to simplify the operation.
    A solute-free water filter permeation product 14 is the product of the process.
    The solute-rich flow 15 from the nano filter 13 is combined in a mixer 17 with the cooled, solute-rich flow 10 from the heat exchanger 16, to create a combined solute-rich flow 18. Mixer 17 is used to completely dissolve the solute in the resulting combined solute-rich flow 18. The combined solute-rich flow 18 is fed to the direct osmosis module 3 to purify or desalinate the source flow continuously.
    The solute-rich flow 10 leaving the phase separator 8 as an effluent is cooled in the heat exchanger 16 to a specific temperature that keeps the temperature of the combined solute-rich flow 18 low enough, and provides complete solubility in the flow rich in combined solute 18 entering the direct osmosis module 3. In an exemplary embodiment of FIG. 1, coalescer 6 and / or phase separator 8 can be heated to operating temperature with an additional external heat source (not shown). In another exemplary embodiment of FIG. 1, coalescer 6 and phase separator 8 are combined in one physical device.
    Alternatively, the interior surface area of the heat exchanger network 4 and the piping between the heat exchanger network 4 and 8, the phase separator can be used in place of coalescer 6. In another exemplary embodiment of FIG. 1, instead of maintaining the temperature based on the solute concentration, the temperature of the coalescer 6 and the phase separator 8 is controlled to maintain the osmotic pressure of the rich water flow 9 in less than 50 mOsm, preferably less than 25 mOsm and more preferably less than 15 mOsm.
    In another exemplary embodiment of FIG. 1, the solute concentration in the diluted extraction solution flow 5 is controlled using the diluted extraction solution flow rate 5 or the combined solute rich flow 18. The target concentration in the diluted extraction solution 5 is controlled to maintain a minimum flow in the direct osmosis module 3, of at least 4 L / (m2 * h).
    In another exemplary embodiment of FIG. 1, the concentration of microorganisms in the diluted extraction solution stream 5 is controlled by a UV sterilizer or by the addition of a biocide.
    In another exemplary embodiment of FIG. 1, an advanced oxidation process or adsorption system is used to remove the residual extraction solute from the filter permeation product 14. In another exemplary embodiment of FIG. 1, the nano filter 13, ultrafilter or reverse osmosis filter is selected to obtain a cut of molecular weight less than 2000, preferably less than 1000 and more preferably less than 500; a rejection of NaCl less than 50%, preferably less than 25% and more preferably less than 10%, and a solute rejection greater than 95%, preferably greater than 99% and more preferably greater than 99.9 % by weight of solute in solution.
    Exemplary Coalescer Operating Conditions The effect of the coalescer operating temperature on the process flow concentration and osmotic pressure in the direct osmosis process, illustrated in FIG. 1, was investigated.
    A preferred extraction solution comprising a random polyoxy copolymer was used in the process.
    Under heating in coalescer 6, the osmotic pressure of the diluted extraction solution flow 5 decreased and the solution separated into a solute-rich phase and a water-rich phase.
    The coalescer effluent 7 was fed to a gravity separator at a controlled temperature 8, where the gravity phase separator 8 separated the solute from the water to produce a continuous flow rich in solute 10 and a continuous flow rich in water 9 The osmotic pressure of the water-rich flow 9 (which defines or restricts the final energy consumption of the filter 13) and the solute composition of the solute-rich flow 10 (which defines or restricts the membrane flow and maximum brine concentration). processed in the direct osmosis module) were measured as a function of the coalescer's operating temperature.
    The results are shown in Table 2. Table 2: Effects of Coalescer Operating Temperature Operating Temperature Effluent Osmotic Pressure Effluent Concentration of Coalescer Coalescer Rich in Water Coalescer Solute Rich (ºC) (mOsm) (% by weight) ) 75 27 50 80 22 55 85 20 63 90 17 72 95 13 80 The operating temperature of coalescer 6 has been controlled to establish a specific osmotic pressure in the water-rich flow 9 that comes out as effluent from the separator 8. The operating temperature Coalescer 6 was also controlled to establish a solute concentration in the solute-rich flow 10. As described in Table 2, increasing the operating temperature of coalescer 6 decreases the osmotic pressure of the water-rich flow 9, thereby reducing the energy required for filtration in the final filtration step 13. Increasing the operating temperature of coalescer 6 also results in an increase in the concentration of solute in the effluent of solute-rich coalescer, thus allowing an increase in membrane flow and maximum concentration of brine processed in the direct osmosis module 3. FIG. 2 illustrates an exemplary direct osmosis process according to another model. A stream of brackish water source 200 is fed to a feed side of a semipermeable membrane, in a direct osmosis module 202. A stream of extraction solution 240 is fed to an extraction side of a semipermeable membrane, in the feed module. direct osmosis 202. The osmotic flow pressure of the brackish water source 200 is less than the osmotic pressure of the extraction solution flow 240. This pressure differential causes the water in the flow of the brackish water source 200 to permeate through the mem - semi-permeable white, resulting in a flow of diluted extraction solution 206 and a flow of brine 204. The flow of diluted extraction solution 206 can be divided into two flows of diluted extraction solution 206 and transmitted to a network of heat exchangers comprising two, or more, heat exchangers, 208, 210, and 214. One flow of diluted extraction solution 206 is fed to one solute-rich heat exchanger 208 and the other flow of diluted extraction solution 206 is fed to a water-rich heat exchanger 210. Both streams of diluted extraction solution 206 are heated in the respective heat exchangers 208, 210 and the resulting heated extraction solution streams are recombined to form a combined flow of diluted extraction solution
    212. The proportion of the flow rate of the diluted extraction solution streams 206 is adjusted so that the temperature difference between the two diluted extraction solution streams 206, which leave the heat exchangers 208, 210 in the heat exchanger network heat, is less than 5 ° C, preferably less than 3 ° C and preferably less than 1 ° C. The combined diluted extraction solution stream 212 can be passed through an additional heat exchanger 214 where the external heat, from a residual heat source, a solar thermal source, or a Heat source of burnt fuel (not shown) is added to adjust the temperature and accounts for heat losses from the process. The diluted extraction solution streams 206 and the combined extraction solution stream 212 are heated in the network of heat exchangers 208, 210 and 214 sufficiently to initiate phase separation. The temperature of the combined flow of diluted extraction solution 212 leaving the effluent of the composition heat exchanger 214 is sufficient to create a two-phase effluent 212. The flow of effluent from the two-phase extraction solution 5 exiting the heat exchanger Composition heat 214 is fed to a temperature-controlled coalescer 216 to agglomerate small solute-rich droplets into the network of heat exchangers 208, 210, 214. Coalescer 216 is designed to aggregate large enough, solute-rich droplets to be separated into the subsequent phase separation process 218. In an exemplary embodiment, coalescer 216 is designed to aggregate solute-rich drops greater than 10 µm, preferably greater than 25 µm and more preferably greater than 50 µm.
    The pressure drop caused by two-phase flows that passed through the 216 coalescer is significantly less than the pressure drop caused by two-phase flows that passed through a nano filter.
    The use of coalescer 216 eliminates the added complexity and backwash required in semi-batch operations.
    Coalescer 216 can also be segregated into an upper section that comprises hydrophobic coalescent elements to agglomerate the extraction solute and a lower section that comprises hydrophilic coalescent elements for water aggregation.
    The degree of hydrophobicity of the hydrophobic coalescent elements and the degree of hydrophilicity of the hydrophilic coalescent elements are selected to obtain a specific degree of agglomeration of the extraction solute greater than 10 µm.
    In an exemplary embodiment, the degree of hydrophobicity of the hydrophobic coalescent elements and the degree of hydrophilicity of the hydrophilic coalescent elements are selected to agglomerate the extraction solute to more than 10 µm.
    The coalescent effluent flow 220 is fed to a temperature controlled gravity separator 218, centrifuge, hydro-cyclone or similar device in which the solute-rich drops from the coalescer are accumulated.
    The gravity phase separator 218 is designed to separate solute from water and produce a continuous flow rich in water 222 and a continuous flow rich in solute 224. In an exemplary embodiment, the operating temperature of coalescer 216 and of the gravity phase separator 218 is maintained at less than 150 ° C, preferably less than 100 ° C and more preferably less than 80 ° C to establish a specific solute concentration and osmotic pressure of the water-rich flow 222 leaving as an effluent from separator 218. In an exemplary embodiment, the operating temperature of coalescer 216 and gravity phase separator 218 is selected to establish a solute concentration in water-rich flow 222 of less than 5%, preferably less than than 2% and more preferably less than 1% by weight of solute in the solution.
    In an exemplary embodiment, the gravity phase separator 218 is designed to concentrate the solute in the solute-rich flow 224 to a concentration greater than 60%, preferably greater than 80% and more preferably greater than 90% in solute weight in the solution.
    The water-rich flow 222 leaving the effluent from the separator 218 is passed through the water-rich heat exchanger 210 where it is cooled by the diluted extraction solution flow 206 and the diluted extraction solution flow 206 is in turn heated by the water-rich flow 222. The solute-rich flow 224 exiting as an effluent from the separator 218 is passed through the solute-rich heat exchanger 218 where it is cooled by the diluted extraction solution flow 206 and the flow of diluted extraction solution 206 in turn is heated by the flow rich in solute 224. Therefore, the network of heat exchangers 208, 210, 214 purifies / recovers mainly the sensitive heat from the gravity phase separator effluents 218 including water-rich continuous flow 222 and solute-rich continuous flow 224. Water-rich flow 222 and solute-rich flow 224 are cooled to a few degrees from the operating temperature of direct osmosis module 202, while the diluted extraction solution streams 206 are correspondingly heated.
    The water-rich stream 222 exiting as an effluent from the phase separator 218 is cooled by the water-rich heat exchanger 210 to allow the residual solute to be dissolved again and to create a single-phase cooled water-rich stream 226. The chilled water-rich flow 226 is a single-phase flow fed to a 228 nano filter, ultrafilter, reverse osmosis module including a semipermeable membrane, or similar device, used to separate the residual solute from the drinking water. product.
    Nano filter 228 is selected to reject solute molecules based on size or structure and ideally passes most of the dissolved salt.
    The final filtration step in the nano filter 228, ultrafilter, reverse osmosis module or similar device is used only for the recovery of the residual solutes in the 226 single-phase cooled water-rich stream. The solutes are again dissolved in the rich-stream. 226 single phase cooled water to minimize pressure drop through nano filter 228 and to simplify operation.
    A solute free water filter permeation product 230 is the process product.
    The solute-rich stream 232 from the nano filter 228 is combined in a mixer 234 with the cooled-solute-rich stream 224 from the solute-rich heat exchanger 208 to create a solute-rich combined stream 240. The mixer 234 is used to completely dissolve the solute in the resulting solute-rich combined flow 240. The solute-rich combined flow 240 is fed to the direct osmosis module 202 to purify or desalinate the source flow 200 in a continuous manner.
    The solute-rich flow 224 exiting the phase separator 218 as an effluent is cooled in the solute-rich heat exchanger 208 to a specific temperature that keeps the temperature of the solute-rich combined flow 240 low enough and provides complete solubility in the solute. solute-rich combined flow 240 entering direct osmosis module 202. In an exemplary embodiment of Figure 2, coalescer 216 and / or phase separator 218 can be heated to operating temperature with an additional external heat source (no shown). In another exemplary embodiment of Figure 2, coalescer 216 and phase separator 218 are combined in one physical device.
    In another exemplary embodiment of Figure 2, instead of maintaining the temperature based on the solute solution, the temperature of the coalescer 216 and phase separator 218 is controlled to maintain the osmotic pressure of the water-rich flow 222 in less than 50 mOsm, preferably less than 25 mOsm and more preferably less than 15 mOsm.
    In another exemplary embodiment of Figure 2, the solute concentration in the diluted extraction solution flows 206 is controlled using the flow rate of the diluted extraction solution flow 216 or the combined solute-rich flow 240. The target concentration in the diluted extraction solution 206 is controlled to maintain a minimum flow in the direct osmosis module 202 of at least 4 L / (m2 * h). In another exemplary embodiment of Figure 2, the concentration of microorganisms in the diluted extraction solution streams 206 is controlled with a UV sterilizer or the addition of a biocide.
    In another exemplary embodiment of Figure 2, an advanced oxidation process or adsorption system is used to remove residual extraction solute from filter permeation product 228. In another exemplary embodiment of Figure 2, nano filter 228, ultra filter or reverse osmosis filter is selected to obtain a cut of molecular weight less than 2,000, preferably less than 1,000 and more preferably less than 500; a rejection of NaCl less than 50%, preferably less than 25% and more preferably less than 10%; and a solute rejection greater than 95%, preferably greater than 99% and more preferably greater than 99.9% by weight of solute in the solution.
    Figure 3 illustrates an exemplary direct osmosis process according to another modality.
    A stream of brackish water source 300 is fed to a feed side of a semipermeable membrane in a direct osmosis module 304. The flow of extraction solution 318 is fed to a feed side of a semipermeable membrane in the direct osmosis module 304. The osmotic pressure of the brackish water source stream 300 is less than the osmotic pressure of the extraction solution stream 318. This pressure differential causes water from the brackish water source stream 300 to permeate through the membrane semipermeable resulting in a flow of diluted extraction solution 306 and a flow of brine 302. The flow of diluted extraction solution 306 is passed through a network of heat exchangers 308 where the temperature is raised sufficiently to start drying. phase stop.
    The heat exchanger network 308 can include one or more heat exchangers
    heaters configured in series or in parallel to increase the temperature of the diluted extraction solution stream 306. The temperature of the diluted extraction solution stream 300 exiting the effluent from the network of heat exchangers 308 is sufficient to create an effluent two-phase. The effluent stream of two-phase extraction solution 340 leaving the heat exchanger network 308 is fed to a main temperature controlled coalescer 310 to agglomerate small droplets rich in solute into the heat exchanger network
    308. The main coalescer 310 is designed to aggregate the solute-rich drops, large enough to be separated in the subsequent phase separation process
    312. In an exemplary embodiment, the main coalescer 310 is designed to aggregate drops rich in solute for more than 10 µm, preferably greater than 25 µm, more preferably greater than 50 µm. The pressure drop caused by the two-phase flows that passed through the main coalescer 310 is significantly less than the pressure drop caused by the two-phase flows, which passed through a nano filter. The use of coalescer 310 eliminates the added complexity and backwash required in semi-batch operations. The main coalescent effluent stream 314 is fed to a temperature controlled gravity separator 312, centrifuge, hydro-cyclone or similar device in which the solute-rich droplets from the main coalescer 310 are accumulated. The gravity phase separator 312 is designed to separate the solute from the water and provide a continuous flow rich in solute 316 and a continuous flow rich in water 342. In an exemplary embodiment, the operating temperature of the main coalescer 310 and the gravity phase separator 312 can be kept at less than 150 ° C, preferably less than 100 ° C and more preferably less than 80 ° C to establish a specific concentration of the solute in the water-rich flow 342 leaving as an effluent from the separator 312. The operating temperature of the main coalescer 310 and the gravity phase separator 312 can also be maintained to establish a solute concentration in the water-rich flow 342 of less than 5%, preferably less than 2% and more preferably less than 1% by weight of solute in solution. In an exemplary embodiment, the gravity phase separator 312 can be designed and operated to concentrate the solute in the flow rich in solute 316 to a concentration greater than 60%, preferably greater than 80% and more preferably greater than 90% by weight of solute in solution. The solute-rich stream 316 exiting the phase separator 312 as an effluent is cooled in a heat exchanger 320. The water-rich stream 342 exiting as an effluent from the separator 312 can be passed through a designed temperature controlled secondary coalescer 322 for a dispersed phase of low concentration solute. The secondary coalescer 322 is designed to aggregate solute-rich drops into the water-rich flow 342 and produce a solute-rich flow 324 leaving as an effluent from the secondary coalescer 322. Due to the flooding of the coalescer caused by high solute concentrations, or use of a dense coalescence matrix is not feasible within or before main coalescer 310. As a result, small drops of solute-rich phase may persist dispersed in the main coalescent effluent stream 314. These small dispersed solute-rich droplets will increase the osmotic pressure of the coalescent effluent 314 and correspondingly require a high pressure and energy consumption for the final stage of filter 330. The water-rich flow 342 feeding the secondary coalescer 322 will have a low concentration of solute allowing the use of a more dense coalescer matrix with minor elements in the secondary coalescer 322 resulting in the smaller droplets to be aggregated and separated before the water-rich flow 342 before it is sent to the final filter stage 330. The coalescer matrix model, material and configuration are selected based on the chemical properties of the solute, the concentration of the solute and the size of the scattered drops.
    The solute-rich stream 324 leaving as effluent from the secondary coalescer 322 is recycled and added to the two-phase extraction solution effluent stream 240 exiting the heat exchanger network 308 upstream of the main coalescer 310. The flow rich in water 338 leaving as effluent from the secondary coalescer 322 is cooled by a heat exchanger 326 to allow the residual solute to be dissolved again and to produce a single-phase cooled water rich flow 328. secondary coalescer 322 is independently controlled as required to establish the solute concentration in the chilled single-phase water-rich stream 328 in less than 5%, preferably less than 2% and more preferably less than 1% by weight of solute in solution.
    The 328 single stage cooled water flow is fed to a nano filter 330, ultrafilter, reverse osmosis module including a semipermeable membrane, or similar device, to separate the residual solute from the product water.
    Nano filter 330 is selected to reject solute molecules based on size or structure and ideally passes most of the dissolved salt.
    The final filtration step in the nano filter 330, ultrafilter, reverse osmosis module or similar device is used only for the recovery of the residual solutes in the 328 single-phase cooled water-rich stream. The solutes are again dissolved in the rich stream in 328 single phase cooled water to minimize pressure drop through nano filter 330 and to simplify operation.
    The solute free water filter permeation product 332 is the process product.
    The solute-rich flow 334 from nano filter 330 is combined in a mixer 336 with the cooled solute-rich flow 316 to create a combined solute-rich flow
    318. The mixer 336 is used to completely dissolve the solute in the resulting solute-rich combined flow 318. The solute-rich combined flow 318 is fed to the direct osmosis module 304 to purify or desalinate the source flow 300 in a continuous manner.
    The solute-rich stream 316 leaving the phase separator 312 as effluent is cooled in the heat exchanger 320 to a specific temperature that keeps the temperature of the solute-rich combined stream 318 low enough to provide complete solubility of the solute in water entering the direct osmosis module 304. In an exemplary embodiment of Figure 2, coalescers 310, 322 and / or phase separator 312 can be heated to operating temperature with an additional external heat source ( not shown). In another exemplary embodiment of Figure 3, primary coalescer 310 and phase separator 312 are combined in one physical device.
    Alternatively, the surface area within the heat exchanger network 308 and the conduit between the heat exchanger network 308 and the phase separator 312 can be used to replace the main coalescer 310 and its operation.
    In another exemplary embodiment of Figure 3, instead of maintaining the temperature based on the solute solution, the temperature of main coalescer 310, secondary coalescer 322 and phase separator 312 is controlled to maintain the osmotic pressure of the water-rich flow 338 in less than 50 mOsm, preferably less than 25 mOsm and more preferably less than 15 mOsm.
    In another exemplary embodiment of Figure 3, the solute concentration in the diluted extraction solution flow 306 is adjusted by controlling the flow rate of the diluted extraction solution flow 306 or the combined solute-rich flow 318. The target concentration in the flow diluted extraction solution 306 is adjusted to maintain a minimum flow in the direct osmosis module 304 of at least 4 L / (m2 * h). In another exemplary embodiment of Figure 3, the concentration of microorganisms in the diluted extraction solution stream 306 is controlled with a UV stabilizer or by the addition of a biocide.
    In another exemplary embodiment of Figure 3, an advanced oxidation process or adsorption system is used to remove residual extraction solute from filter permeation product 332. In another exemplary embodiment of Figure 3, the nano filter 330, ultra filter or reverse osmosis filter is selected to obtain a cut of molecular weight less than 2,000, preferably less than 1,000 and more preferably less than 500; a rejection of NaCl less than 50%, preferably less than 25% and more preferably less than 10%; and a solute rejection greater than 95%, preferably greater than 99% and more preferably greater than 99.9% by weight of solute in solution.
    The systems and processes for water purification of direct osmosis, or desalination, present here, revealed the initial phase separation by heating, the resulting two-phase dispersed system is aggregated using the coalescer and the volume of the solute is recovered using a phase separator.
    Finally, the resulting water-rich flow is cooled to dissolve any remaining dispersed solute and a single phase, low solute flow is sent to a filter (eg nano filter) for final, continuous filtration processing.
    The nano filter or similar device is used to separate a two-phase system in the final filtration step.
    Figure 4 illustrates an exemplary process flow diagram of an exemplary direct osmosis system according to an embodiment.
    In step 401, a stream of contaminated feed solution comprising water and having a first osmotic pressure is provided on a feed side of the semipermeable membrane and a stream of extraction solution comprising an extraction solute and having a second pressure osmotic is provided on an extraction side of the semipermeable membrane.
    In step 402, water from the contaminated feed solution is allowed to pass through the semipermeable membrane to the extraction side to produce a flow of diluted extraction solution comprising water and the extraction solute on the extraction side of the membrane. - mipermeable.
    In step 403, the diluted extraction solution stream is heated sufficiently to produce a two-phase effluent stream.
    In step 405, the extraction solute in the two-phase effluent stream is agglomerated to produce an agglomerated effluent stream.
    In step 406, the agglomerated extraction solute is separated from the agglomerated effluent flow to produce a water-rich flow comprising water and residual extraction solute and a solute-rich flow comprising agglomerated extraction solute and water.
    In step 407, the water-rich flow is cooled to dissolve the residual extraction solute and to produce a cooled, single-phase water-rich flow.
    In step 408, the residual extraction solution is separated from the cooled single-phase water-rich flow to produce a flow of residual extraction solute and a flow of purified water product.
    The process may also include the steps to reconstitute and recycle the extraction solution.
    In step 409, the solute-rich flow is cooled to produce a cooled-solute flow comprising extraction solute and water.
    In step 410, the residual extraction solute flow is combined with the cooled solute flow to produce a reconstituted extraction solution.
    In step 411, the reconstituted extraction solution is recycled to the extraction side of the semipermeable membrane.
    Exemplary modalities have been described above with respect to improved systems and processes for water purification by direct osmosis or desalination.
    Various modifications and departures from the exemplary modalities revealed will occur to those of ordinary knowledge in the art.
    The study material that must be understood in the essence of this revelation is presented in the following claims.
    权利要求:
    Claims (23)
    [1]
    1. Process for purifying contaminated water CHARACTERIZED by understanding: providing a flow of contaminated feed solution comprising water and having a first osmotic pressure on a feeding side of a semipermeable membrane; providing a flow of extraction solution comprising an extraction solute and having a second osmotic pressure on an extraction side of the semipermeable membrane; passing the water through the semipermeable membrane to the extraction side to produce a flow of diluted extraction solution; heating the flow of diluted extraction solution to initiate the separation phase and producing a two-phase effluent flow comprising a liquid phase of extraction solute and a liquid phase of water; agglomerating the extraction solute in the two-stage effluent stream to produce a sintered two-phase effluent stream comprising a liquid agglomerated extraction solute phase and a liquid water phase; separating the agglomerated extraction solute from the agglomerated two-phase effluent flow to produce a water-rich flow comprising water and residual extraction solute and a solute-rich flow comprising agglomerated extraction solute and water; cooling the water-rich flow to produce a cooled, single-phase water-rich flow; and separating the residual extraction solute from the cooled, single phase water rich stream to produce a flow of residual extraction solute and a stream of purified water product.
    [2]
    2. Process, according to claim 1, CHARACTERIZED by further comprising: cooling the solute-rich flow to produce a cooled-solute-rich flow comprising extraction solute and water; combining the flow of residual extraction solute with the flow rich in chilled solute to produce a reconstituted extraction solution; and recycling the reconstituted extraction solution to the extraction side of the semipermeable membrane.
    [3]
    3. Process, according to claim 1, CHARACTERIZED by the fact that heating the diluted extraction solution comprises heating the diluted extraction solution in a network of heat exchangers.
    [4]
    4. Process according to claim 1, CHARACTERIZED by the fact that the agglomeration of the extraction solute comprises agglomerating the extraction solute in a coalescer.
    [5]
    5. Process according to claim 1, CHARACTERIZED by the fact that the separation of the agglomerated extraction solute from the agglomerated two-phase effluent stream comprises separating the agglomerated extraction solute from the two-phase effluent stream phases agglomerated in a gravity phase separator.
    [6]
    6. Process according to claim 1, CHARACTERIZED by the fact that the cooling of the water-rich flow comprises cooling the water-rich flow in a network of heat exchangers.
    [7]
    7. Process according to claim 1, CHARACTERIZED by the fact that the separation of the residual extraction solute from the cooled water-rich single-phase flow comprises separating the residual extraction solute from the water-rich flow single-phase cooled in a nano filter, ultrafilter or in a reverse osmosis module.
    [8]
    8. Process according to claim 2, CHARACTERIZED by the fact that the cooling of the solute-rich flow comprises cooling the solute-rich flow in a network of heat exchangers.
    [9]
    9. Process, according to claim 4, CHARACTERIZED by the fact that the mobile station of mist point of the extraction solute is between 40ºC and 90ºC and the coalescer's operating temperature is less than 150ºC.
    [10]
    10. Process according to claim 1, CHARACTERIZED by the fact that the concentration of the residual extraction solute in the water-rich flow is less than 5% by weight of solute in solution.
    [11]
    11. Process, according to claim 1, CHARACTERIZED by the fact that the osmotic pressure of the single-phase cooled water-rich flow is less than 50 mOsm.
    [12]
    12. Process according to claim 1, CHARACTERIZED by the fact that the concentration of the solute in the solute-rich flow is greater than 60% by weight of solute in solution.
    [13]
    13. Process, according to claim 1, CHARACTERIZED by the fact that the extraction solute is a random or sequential copolymer of low molecular weight diols.
    [14]
    14. Process according to claim 13, CHARACTERIZED by the fact that the molecular weight of the random or sequential copolymer is greater than 500, and the osmotic pressure of 40% by weight of solute in solution, is greater than 30.99 kg / cm2.
    [15]
    15. Process, according to claim 13, CHARACTERIZED by the fact that the low molecular weight diols are ethane diol and propane diol and the temperature of mist point, solubility and osmotic pressure of the extraction solute are controlled less before adjusting the proportion of ethanol diol / propane diol and adjusting the molecular weight of the extraction solute.
    [16]
    16. Process according to claim 1, CHARACTERIZED by the fact that it also comprises measuring the concentration or osmotic pressure of the residual extraction solute in the water-rich flow and controlling the concentration or osmotic pressure of the residual extraction solute by adjusting the coalescer operating temperature.
    [17]
    17. Process, according to claim 1, CHARACTERIZED by the fact that it also comprises controlling the flow rate of the extraction solution flow to maintain a predetermined concentration of extraction solute in the diluted extraction solution flow.
    [18]
    18. Process, according to claim 4, CHARACTERIZED by the fact that the coalescer is segregated in an upper section comprising hydrophobic coalescent elements to agglomerate the extraction solute and a lower section comprising hydrophilic coalescent elements for water aggregation , in which the degree of hydrophobicity of the hydrophobic coalescent elements and the degree of hydrophilicity of the hydrophilic coalescent elements are selected to agglomerate the extraction solute to more than 10 µm.
    [19]
    19. Process, according to claim 3, CHARACTERIZED by the fact that the network of heat exchangers comprises at least two heat exchangers.
    [20]
    20. Process, according to claim 7, CHARACTERIZED by the fact that the nano-filter, ultra-filter or reverse osmosis module comprises a cut of molecular weight less than 2,000, a rejection of NaCl less than 50% by weight of solute in solution and an extraction solute rejection greater than 95% by weight of solution solute.
    [21]
    21. Process according to claim 1, CHARACTERIZED by the fact that a concentration of microorganisms from the extraction solute in the process is controlled with a UV sterilizer or a biocide.
    [22]
    22. Process according to claim 7, CHARACTERIZED by the fact that an oxidation process or adsorption system is used to remove residual extraction solute from the filter permeation product of the nano filter, ultrafilter or module reverse osmosis.
    [23]
    23. System for purifying contaminated water, FEATURED for understanding: a semipermeable membrane comprising a feed side to receive a stream of contaminated feed solution comprising water and having a first osmotic pressure and an extraction side to receive a solution stream extraction system comprising an extraction solute and having a second osmotic pressure, in which the semipermeable membrane is configured to pass water from the contaminated feed solution stream to the extraction side to produce a flow of extraction solution diluted; a first heat exchanger configured to heat the flow of diluted extraction solution to initiate phase separation and produce a two-phase effluent flow comprising a liquid phase of extraction solute and a liquid phase of water; a coalescer configured to agglomerate the extraction solute in the diluted extraction solution stream to produce an agglomerated two-phase effluent stream, comprising a liquid agglomerated extraction solute phase and a liquid water phase; a gravity phase separator configured to separate the agglomerated extraction solute from the agglomerated two-phase effluent stream to produce a water-rich stream comprising water and residual extraction solute and a solute-rich stream comprising agglomerated extraction solute and Water; a second heat exchanger configured to cool the water-rich flow to produce a cooled, single-phase water-rich flow; and a reverse osmosis module configured to separate the residual extraction solute from the cooled single-phase water-rich flow to produce a flow of residual extraction solute and a product flow of purified water.
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    同族专利:
    公开号 | 公开日
    ZA201306937B|2015-03-25|
    CN105712436A|2016-06-29|
    US9676639B2|2017-06-13|
    JP5985609B2|2016-09-06|
    KR20160014791A|2016-02-11|
    RU2556662C2|2015-07-10|
    CN103492038B|2016-01-20|
    AU2015282372A1|2016-01-28|
    US20120267308A1|2012-10-25|
    MX2013011840A|2014-02-27|
    SG194156A1|2013-11-29|
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    RU2013145560A|2015-05-27|
    JP6495207B2|2019-04-03|
    CA2830390C|2018-01-16|
    US9216917B2|2015-12-22|
    EP2686081A1|2014-01-22|
    IL228533A|2016-07-31|
    US20160039685A1|2016-02-11|
    WO2012148864A1|2012-11-01|
    AU2015282372B2|2017-10-12|
    IL228533D0|2013-12-31|
    JP2017018952A|2017-01-26|
    CL2013002899A1|2014-04-11|
    KR101591318B1|2016-02-18|
    KR101861024B1|2018-05-24|
    AU2012249944A1|2013-10-10|
    CN103492038A|2014-01-01|
    CA2830390A1|2012-11-01|
    JP2014512951A|2014-05-29|
    CN105712436B|2018-11-30|
    EP2686081A4|2014-12-10|
    AU2012249944B2|2015-10-08|
    KR20130137022A|2013-12-13|
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    法律状态:
    2020-09-15| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2020-09-29| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|
    2020-10-27| B08F| Application dismissed because of non-payment of annual fees [chapter 8.6 patent gazette]|Free format text: REFERENTE A 8A ANUIDADE. |
    2021-01-12| B11B| Dismissal acc. art. 36, par 1 of ipl - no reply within 90 days to fullfil the necessary requirements|
    2021-11-23| B350| Update of information on the portal [chapter 15.35 patent gazette]|
    优先权:
    申请号 | 申请日 | 专利标题
    US201161517687P| true| 2011-04-25|2011-04-25|
    US61/517,687|2011-04-25|
    US201161572394P| true| 2011-07-15|2011-07-15|
    US61/572,394|2011-07-15|
    PCT/US2012/034723|WO2012148864A1|2011-04-25|2012-04-23|Recovery of retrograde soluble solute for forward osmosis water treatment|
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