CN111867705A - Solvent separation - Google Patents
Solvent separation Download PDFInfo
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- CN111867705A CN111867705A CN201880081420.3A CN201880081420A CN111867705A CN 111867705 A CN111867705 A CN 111867705A CN 201880081420 A CN201880081420 A CN 201880081420A CN 111867705 A CN111867705 A CN 111867705A
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- 239000002904 solvent Substances 0.000 title claims abstract description 31
- 238000000926 separation method Methods 0.000 title description 3
- 239000012528 membrane Substances 0.000 claims abstract description 240
- 239000000243 solution Substances 0.000 claims abstract description 199
- 239000012466 permeate Substances 0.000 claims abstract description 91
- 239000012527 feed solution Substances 0.000 claims abstract description 73
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 63
- 238000000034 method Methods 0.000 claims abstract description 57
- 238000009292 forward osmosis Methods 0.000 claims description 15
- 230000003204 osmotic effect Effects 0.000 claims description 12
- 239000002243 precursor Substances 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 25
- 150000003839 salts Chemical class 0.000 description 19
- 239000002351 wastewater Substances 0.000 description 9
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 8
- 239000002357 osmotic agent Substances 0.000 description 7
- -1 alkali metal (e.g. Chemical class 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 239000013535 sea water Substances 0.000 description 6
- 239000000654 additive Substances 0.000 description 5
- 239000011780 sodium chloride Substances 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- 239000012267 brine Substances 0.000 description 4
- 239000000835 fiber Substances 0.000 description 4
- 239000003673 groundwater Substances 0.000 description 4
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 4
- 239000002440 industrial waste Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 239000012266 salt solution Substances 0.000 description 4
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 4
- 230000003373 anti-fouling effect Effects 0.000 description 3
- 210000000416 exudates and transudate Anatomy 0.000 description 3
- 239000010842 industrial wastewater Substances 0.000 description 3
- 238000001728 nano-filtration Methods 0.000 description 3
- 239000002455 scale inhibitor Substances 0.000 description 3
- 239000002352 surface water Substances 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 2
- BTBUEUYNUDRHOZ-UHFFFAOYSA-N Borate Chemical compound [O-]B([O-])[O-] BTBUEUYNUDRHOZ-UHFFFAOYSA-N 0.000 description 2
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 229920002284 Cellulose triacetate Polymers 0.000 description 2
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 2
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 2
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 2
- 239000004952 Polyamide Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- NNLVGZFZQQXQNW-ADJNRHBOSA-N [(2r,3r,4s,5r,6s)-4,5-diacetyloxy-3-[(2s,3r,4s,5r,6r)-3,4,5-triacetyloxy-6-(acetyloxymethyl)oxan-2-yl]oxy-6-[(2r,3r,4s,5r,6s)-4,5,6-triacetyloxy-2-(acetyloxymethyl)oxan-3-yl]oxyoxan-2-yl]methyl acetate Chemical compound O([C@@H]1O[C@@H]([C@H]([C@H](OC(C)=O)[C@H]1OC(C)=O)O[C@H]1[C@@H]([C@@H](OC(C)=O)[C@H](OC(C)=O)[C@@H](COC(C)=O)O1)OC(C)=O)COC(=O)C)[C@@H]1[C@@H](COC(C)=O)O[C@@H](OC(C)=O)[C@H](OC(C)=O)[C@H]1OC(C)=O NNLVGZFZQQXQNW-ADJNRHBOSA-N 0.000 description 2
- 230000000996 additive effect Effects 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 2
- 150000001342 alkaline earth metals Chemical class 0.000 description 2
- 150000004645 aluminates Chemical class 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- SXDBWCPKPHAZSM-UHFFFAOYSA-M bromate Inorganic materials [O-]Br(=O)=O SXDBWCPKPHAZSM-UHFFFAOYSA-M 0.000 description 2
- SXDBWCPKPHAZSM-UHFFFAOYSA-N bromic acid Chemical compound OBr(=O)=O SXDBWCPKPHAZSM-UHFFFAOYSA-N 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 229920002301 cellulose acetate Polymers 0.000 description 2
- ZCDOYSPFYFSLEW-UHFFFAOYSA-N chromate(2-) Chemical compound [O-][Cr]([O-])(=O)=O ZCDOYSPFYFSLEW-UHFFFAOYSA-N 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- XLJMAIOERFSOGZ-UHFFFAOYSA-M cyanate Chemical compound [O-]C#N XLJMAIOERFSOGZ-UHFFFAOYSA-M 0.000 description 2
- 229940104869 fluorosilicate Drugs 0.000 description 2
- UQSQSQZYBQSBJZ-UHFFFAOYSA-M fluorosulfonate Chemical compound [O-]S(F)(=O)=O UQSQSQZYBQSBJZ-UHFFFAOYSA-M 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 239000012510 hollow fiber Substances 0.000 description 2
- XMBWDFGMSWQBCA-UHFFFAOYSA-N hydrogen iodide Chemical compound I XMBWDFGMSWQBCA-UHFFFAOYSA-N 0.000 description 2
- 229910052744 lithium Inorganic materials 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 229910052751 metal Chemical class 0.000 description 2
- 239000002184 metal Chemical class 0.000 description 2
- 150000004767 nitrides Chemical class 0.000 description 2
- VLTRZXGMWDSKGL-UHFFFAOYSA-M perchlorate Inorganic materials [O-]Cl(=O)(=O)=O VLTRZXGMWDSKGL-UHFFFAOYSA-M 0.000 description 2
- VLTRZXGMWDSKGL-UHFFFAOYSA-N perchloric acid Chemical compound OCl(=O)(=O)=O VLTRZXGMWDSKGL-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
- 239000010452 phosphate Substances 0.000 description 2
- 229920002647 polyamide Polymers 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical class [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 235000012206 bottled water Nutrition 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000000065 osmolyte Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000012465 retentate Substances 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
- B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
- B01D2311/252—Recirculation of concentrate
- B01D2311/2521—Recirculation of concentrate to permeate side
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
- B01D2311/253—Bypassing of feed
- B01D2311/2531—Bypassing of feed to permeate side
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
Abstract
A process for separating a solvent from a feed solution, the process comprising contacting the feed solution with one side of a first semi-permeable membrane; applying hydraulic pressure to the feed solution such that solvent from the feed solution flows through the first semi-permeable membrane by reverse osmosis to provide a permeate solution on a permeate side of the first semi-permeable membrane and a residual solution on a feed side of the first semi-permeable membrane; and feeding a portion of the feed solution or a portion of the residual solution to the permeate side of the first semi-permeable membrane.
Description
Background
The present invention relates to a process for separating a solvent, such as water, from a feed solution.
In the water purification process, water is separated from an impure solution, such as a brine solution. Various methods of water purification are known. An example of such a method is reverse osmosis. In reverse osmosis, water is forced through a semi-permeable membrane from a region of high solute concentration to a region of low solute concentration by applying a hydraulic pressure (hydraulic pressure) that exceeds the osmotic pressure of the solution of high solute concentration. For example, reverse osmosis is commonly used to obtain potable water from seawater. Reverse osmosis is also used to separate water from, for example, industrial waste streams (industrial waste streams). By treating an industrial waste stream using reverse osmosis, relatively clean water can be produced from the industrial waste while reducing the volume of undesirable waste that needs to be disposed of or further treated.
Reverse osmosis requires the application of relatively high pressures on the high solute concentration side of the membrane. For example, to desalinate seawater by conventional reverse osmosis techniques, pressures of up to 82barg are typically used to increase the recovery of product water. This places a significant energy burden on desalination processes that rely on conventional reverse osmosis. Furthermore, a stream with a higher solute concentration than seawater may require the application of even higher hydraulic pressure. Many commercially available reverse osmosis membranes are not adapted to withstand hydraulic pressures greater than 82 barg. This may therefore impose a limit on the concentration of feed solution that can be treated using commercially available reverse osmosis membranes, which effectively limits the maximum concentration of the concentrated feed stream to an osmotic pressure equal to the maximum hydraulic rating of the reverse osmosis membrane and the pressure vessel.
Brief Description of Drawings
Embodiments of the invention are further described below with reference to the accompanying drawings, in which:
fig. 1 is a schematic illustration of a system for implementing a process according to a first example of the present disclosure;
fig. 2 is a schematic illustration of a system for implementing a process according to a second example of the present disclosure;
FIG. 3 is a schematic illustration of a system for implementing a process according to a third example of the present disclosure;
Fig. 4 is a schematic illustration of a system for implementing a process according to a fourth example of the present disclosure;
fig. 5 is a schematic illustration of a system for implementing a process according to a fifth example of the present disclosure;
fig. 6 is a schematic illustration of a system for implementing a process according to a sixth example of the present disclosure;
fig. 7 is a schematic illustration of a system for implementing a process according to a seventh example of the present disclosure;
fig. 8 is a schematic illustration of a system for implementing a process according to an eighth example of the present disclosure;
fig. 9 is a schematic illustration of a system for implementing a process according to a ninth example of the present disclosure;
fig. 10 is a schematic illustration of a system for implementing a process according to a tenth example of the present disclosure; and
fig. 11 is a schematic illustration of a system for implementing a process according to an eleventh example of the present disclosure.
Detailed description of the invention
Throughout the description and claims of this specification, the words "comprise" and variations of the words "comprise" and "comprising" mean "including but not limited to", and they are not intended to (and do not) exclude other moieties, additives, components, integers or steps. Throughout the description and claims of this specification, the singular encompasses the plural unless the context otherwise requires. In particular, where the indefinite article is used, the specification is to be understood as contemplating plurality as well as singularity, unless the context requires otherwise.
Features, integers, characteristics and compounds in combination with a particular aspect, embodiment or example of the invention are to be understood to be applicable to any other aspect, embodiment or example described herein unless incompatible therewith. All of the features disclosed in this specification (including any accompanying claims, abstract and drawings), and/or all of the steps of any method or process so disclosed, may be combined in any combination, except combinations where at least some of such features and/or steps are mutually exclusive. The invention is not limited to the details of any of the foregoing embodiments. The invention extends to any novel one, or any novel combination, of the features disclosed in this specification (including any accompanying claims, abstract and drawings), or to any novel one, or any novel combination, of the steps of any method or process so disclosed.
According to the present invention there is provided a process for separating a solvent from a feed solution, the process comprising:
contacting the feed solution with one side of a first semi-permeable membrane (first semi-permeable membrane);
applying hydraulic pressure to the feed solution such that solvent from the feed solution flows through the first semi-permeable membrane by reverse osmosis to provide a permeate solution on a permeate-side of the first semi-permeable membrane and a residual solution on a feed side of the first semi-permeable membrane; and
A portion of the feed solution or a portion of the residual solution is fed to the permeate side of the first semi-permeable membrane.
Preferably, the solvent is water. The feed solution may be a salt solution, such as a brine solution. The feed solution may be an impure water stream, such as saline ground water (saline ground water) or surface water, brine and seawater. Other examples include wastewater streams, lake water, river water, and pond water. Examples of wastewater streams include industrial wastewater streams or agricultural wastewater streams. Alternatively, the feed solution may be a salt solution prepared by dissolving a penetrant (osmotic agent) in water.
The inventors have found that by feeding a portion of the feed solution or a portion of the residual solution to the permeate side of the first semi-permeable membrane, the osmotic pressure differential across the first semi-permeable membrane can be reduced. Thus, the hydraulic pressure required to induce solvent flow from the feed solution by reverse osmosis can be reduced. Thus, the reverse osmosis step may become osmosis-assisted (i.e., osmosis-assisted reverse osmosis or "OARO"). Thus, the flux across the semi-permeable membrane is higher than that obtained using reverse osmosis operating alone under the same hydraulic limitations. In other words, to achieve the same level of flux across the semi-permeable membrane, a lower hydraulic pressure may be used. An important advantage of the present invention is that it allows for the treatment of highly concentrated feed solutions at hydraulic pressures within the hydraulic rating of conventional reverse osmosis membranes (e.g., 82barg or less). In the case of conventional reverse osmosis technology, such highly concentrated feed solutions would require hydraulic pressures in excess of the maximum hydraulic rating of most conventional reverse osmosis membranes (e.g., above 82 barg).
In one embodiment, it is a portion of the feed solution that is fed to the permeate side of the first semi-permeable membrane.
Alternatively or additionally, it is a portion of the residual solution that is fed to the permeate side of the first semi-permeable membrane. Due to the concentrated nature of the residual solution, it may be advantageous to utilize a portion of the residual solution to feed to the permeate side of the first semi-permeable membrane. For example, to provide the same brine concentration, a lower flow of residual solution to the permeate side of the first semi-permeable membrane may be required compared to the flow of feed solution. This may be caused by the higher osmotic pressure of the residual solution. Furthermore, for a given hydraulic pressure, a more concentrated residual solution can be obtained. In one embodiment, where the first semi-permeable membrane is a hollow fiber membrane and where the draw solution (draw solution) is on the fiber pores (fiber bore), a portion of the feed residual solution may be more energy efficient than a portion of the feed, e.g., feed solution. A lower pressure drop along the fiber pores may mean less energy is required.
Preferably, the feed solution to the first semi-permeable membrane may be produced by contacting the initial solution with one side of the initial semi-permeable membrane. A hydraulic pressure may be applied to the initial solution such that solvent from the initial solution may flow through the initial semi-permeable membrane by reverse osmosis to provide an initial permeate solution on the permeate side of the initial semi-permeable membrane and an initial residual solution on the feed side of the initial semi-permeable membrane. The initial residual solution may be used as a feed solution to the first semi-permeable membrane. The initial permeate solution may be withdrawn, e.g., for use or further purification. Withdrawing the initial permeate solution for use after the initial reverse osmosis stage may advantageously result in a higher quality permeate than feeding the initial permeate solution to a further reverse osmosis step. This may be due to the lower concentration on the feed/concentrate side of the initial semipermeable membrane. Furthermore, the inclusion of an initial reverse osmosis step may provide economic benefits as conventional, widely used reverse osmosis may be employed. In one embodiment, a portion of the permeate solution on the permeate side of the first semi-permeable membrane may be recycled as feed to the initial semi-permeable membrane.
In one embodiment, the hydraulic pressure applied to the initial solution may be used at least in part to apply hydraulic pressure to the feed solution in contact with the first semi-permeable membrane. For example, a pump may be used to apply hydraulic pressure to drive the initial solution across the initial semi-permeable membrane. The hydraulic pressure may also be used, in whole or in part, to drive a downstream membrane separation step.
In one embodiment, the process may further comprise withdrawing at least a portion of the residual solution on the feed side of the first semi-permeable membrane and contacting the withdrawn solution as additional feed solution with one side of the additional semi-permeable membrane. Hydraulic pressure may be applied to the further feed solution in contact with the further semi-permeable membrane to flow solvent from the further feed solution through the further semi-permeable membrane by reverse osmosis to provide a further permeate solution on the permeate side of the further semi-permeable membrane and a further residual solution on the feed side of the further semi-permeable membrane. A portion of the additional feed solution or a portion of the additional residual solution may be fed to the permeate side of the additional semipermeable membrane. As explained above, this may reduce the osmotic pressure difference across the additional semi-permeable membrane. Thus, the hydraulic pressure required to induce solvent flow from the additional feed solution by reverse osmosis may be reduced.
Although a dedicated pump may be used to apply the hydraulic pressure, a pump used to apply the hydraulic pressure to the initial solution in the initial reverse osmosis step may also be used to apply the hydraulic pressure for one or more of any subsequent osmosis assisted reverse osmosis steps.
In some embodiments, a series of additional semi-permeable membranes may be disposed downstream of the first semi-permeable membrane. The residual solution from any of these membranes can be withdrawn and contacted with the downstream membrane as a feed solution for the downstream membrane. A portion of the feed solution to the downstream membrane or a portion of the residual solution on the feed side of the downstream membrane may be fed to the permeate side of the downstream membrane.
Where the process includes the use of an initial semipermeable membrane as described above, a portion of the additional permeate solution on the permeate side of the additional semipermeable membrane may be recycled as feed to the initial semipermeable membrane or as a portion of the feed to the initial semipermeable membrane.
In another embodiment, the feed solution to the first semi-permeable membrane is produced by contacting the initial solution with one side of the initial semi-permeable membrane. Hydraulic pressure may be applied to the initial solution such that solvent from the initial solution flows through the initial semi-permeable membrane by reverse osmosis to provide an initial permeate solution on the permeate side of the initial semi-permeable membrane and an initial residual solution on the feed side of the initial semi-permeable membrane. The initial residual solution may then be contacted with one side of the additional semi-permeable membrane. Hydraulic pressure may be applied to the initial residual solution such that solvent from the initial residual solution flows through the additional semipermeable membrane by reverse osmosis to provide an additional permeate solution on the permeate side of the additional semipermeable membrane and an additional residual solution on the feed side of the additional semipermeable membrane. This additional residual solution can then be used as feed to the first semi-permeable membrane.
In some embodiments, the initial residual solution may flow through a series of additional semi-permeable membranes, each additional semi-permeable membrane producing its respective permeate solution and residual solution. At least one of these residual solutions may be used as feed to the first semi-permeable membrane.
In some embodiments, at least a portion of the additional residual solution from the additional semipermeable membrane (or one of the additional semipermeable membranes) is withdrawn and fed to the permeate side of the first semipermeable membrane.
In some embodiments, at least a portion of the first permeate solution from the first semi-permeable membrane is recycled as feed to the initial semi-permeable membrane.
In some embodiments, the hydraulic pressure applied to the initial solution is used at least in part to apply hydraulic pressure to the feed solution in contact with the first semi-permeable membrane and/or the additional feed solution in contact with the additional semi-permeable membrane or at least one of the additional semi-permeable membranes.
The feed solution and/or the initial solution may be any solution, such as an aqueous solution. The feed solution and/or the initial solution may be a salt solution, such as an aqueous salt solution. In some embodiments, the feed solution and/or the initial solution may comprise more than one dissolved salt. In some embodiments, the feed solution and/or the initial solution is an aqueous solution of sodium chloride. Examples of suitable feed solutions and/or initial solutions include brackish ground or surface water, salt water and sea water. Other examples include wastewater streams, lake water, river water, and pond water. Examples of wastewater streams include industrial wastewater streams or agricultural wastewater streams.
The feed solution and/or the initial solution may be a solution of one or more osmolytes. Suitable osmotic agents include salts, such as inorganic salts. Suitable salts include ammonium and metal salts, such as alkali metal (e.g., Li, Na, K) and alkaline earth metal (e.g., Mg and Ca) salts. The salt may be fluoride, chloride, bromide, iodide, sulfate, sulfite, sulfide, carbonate, bicarbonate, nitrate, nitrite, nitride, phosphate, aluminate, borate, bromate, carbide, chloride, perchlorate, hypochlorite (hypochlorate), chromate, fluorosilicate, fluorosulfate, silicate, cyanide, and cyanate. One or more salts may be present. An example may be sodium chloride.
The total dissolved salt concentration of the feed solution and/or the initial solution may be at least 5,000mg/l, for example 5,000mg/l to 250,000 mg/l. In one example, the total dissolved salt concentration of the feed solution and/or the initial solution to the first semi-permeable membrane is at least 30,000 mg/l. The osmotic pressure of the feed may be at least 4barg, for example 4barg to 320 barg.
In some examples, the starting solution may be produced by contacting an impure solution with one side of a forward osmosis membrane (forward osmosismembrane) and contacting the opposite side of the forward osmosis membrane with a starting solution precursor. The osmotic pressure (solute concentration) of the initial solution precursor may be higher than the osmotic pressure (solute concentration) of the impure solution such that solvent from the impure solution flows across the forward osmosis membrane by forward osmosis to dilute the initial solution precursor to produce the initial solution.
The impure solution may be brackish ground or surface water, salt water and sea water. Other examples include wastewater streams, lake water, river water, and pond water. Examples of wastewater streams include industrial wastewater streams or agricultural wastewater streams.
The initial solution and/or initial solution precursors may be formed by dissolving the osmotic agent in a solvent, such as water.
Suitable osmotic agents include salts, such as sodium chloride. Other examples of salts include ammonium salts and metal salts, such as alkali metal (e.g., Li, Na, K) salts and alkaline earth metal (e.g., Mg and Ca) salts. The salt may be fluoride, chloride, bromide, iodide, sulfate, sulfite, sulfide, carbonate, bicarbonate, nitrate, nitrite, nitride, phosphate, aluminate, borate, bromate, carbide, chloride, perchlorate, hypochlorite, chromate, fluorosilicate, fluorosulfate, silicate, cyanide, and cyanate. One or more salts may be used.
The semipermeable membrane used in the present invention may be a nanofiltration membrane or a reverse osmosis membrane. Preferably, the semi-permeable membrane is a reverse osmosis membrane. Where more than two membranes are used, the membranes may be the same or different. In one embodiment, the semi-permeable membrane is entirely a reverse osmosis membrane. In another embodiment, the semi-permeable membrane is entirely a nanofiltration membrane. In yet another embodiment, both nanofiltration and reverse osmosis membranes are used as semipermeable membranes.
Any suitable reverse osmosis membrane may be used in the present invention. For example, a reverse osmosis membrane can have an average (e.g., mean) pore size of 0.5 angstroms to 80 angstroms, preferably 2 angstroms to 50 angstroms. In a preferred embodiment, the membrane has an average (e.g., mean) pore size of from 3 angstroms to 30 angstroms. Pore size (e.g., average pore size) can be measured using any suitable technique. For example, a differential flow method (Japan Membrane Journal, Vol.29; No. 4; pp.227-.
Suitable reverse osmosis membranes include integral membranes (integral membranes) and composite membranes. Specific examples of suitable membranes include membranes formed from Cellulose Acetate (CA) and/or Cellulose Triacetate (CTA), such as or similar to those used in the studies of McCutcheon et al decontamination 174(2005)1-11, and membranes formed from Polyamide (PA). An array of membranes may be used.
Reverse osmosis membranes may be planar or may take the form of tubular or hollow fibers. For example, a tubular configuration of hollow fine fiber membranes may be used. If desired, the membrane may be supported on a support structure, such as a mesh support. When a planar membrane is used, the sheet may be rolled such that it defines a spiral in cross-section. When tubular membranes are employed, one or more of the tubular membranes may be contained within a housing or shell.
Reverse osmosis membranes can be operated at elevated pressures to drive a (liquid) solution through the membrane. For example, the reverse osmosis step may be carried out at a pressure of from 25 bar to 120 bar, preferably from 50 bar to 100 bar, more preferably from 60 bar to 80 bar.
Optionally, scale inhibitors (scale inhibitors), anti-fouling additives or anti-fouling additives may be added to any of the solutions that come into contact with any of the membranes. Preferably, the scale inhibitor, scale control additive or anti-fouling additive may be recycled between the retentate side of one membrane and the permeate side of the other membrane, or vice versa.
These and other aspects of the invention will now be described with reference to the drawings. Referring to fig. 1, this represents a schematic illustration of a system for implementing a process according to a first example of the present disclosure. The system 10 includes a reverse osmosis unit 12, the reverse osmosis unit 12 including a first semi-permeable membrane 14. Feed solution 16 is in contact with one side of membrane 14 and hydraulic pressure is applied such that solvent (e.g., water) from feed solution 16 flows through membrane 14 by reverse osmosis to provide permeate solution 18 on permeate side 14b of the first semi-permeable membrane and residual solution 20 on feed side 14a of the first semi-permeable membrane. A portion 16a of feed solution 16 is fed to permeate side 14b of membrane 14. This may reduce the osmotic pressure differential across the membrane 14. Thus, the hydraulic pressure required to induce solvent flow from the feed solution by reverse osmosis can be reduced.
The residual solution 20 may be removed, for example, as a concentrated waste product, e.g., for disposal or further processing or use.
Fig. 2 depicts a schematic illustration of a system for implementing a process according to a second example of the present disclosure. The system 10 of fig. 2 is similar to the system of fig. 1 and like components have been labeled with like numerals. However, unlike the system 10 of FIG. 1, it is a portion 20a of the residual solution 20 that is recycled to the permeate side 14b of the membrane 14 to reduce the osmotic pressure differential across the membrane 14.
Fig. 3 depicts a schematic illustration of a system for implementing a process according to a third example of the present disclosure. The system 10 of fig. 3 is similar to the system 10 of fig. 1, and like components have been labeled with like numerals. However, the apparatus of FIG. 3 also includes an initial reverse osmosis unit 22, the initial reverse osmosis unit 22 including an initial semi-permeable membrane 24. A pump 26 is also provided.
When the process is operated using the system 10 of fig. 3, the feed solution 16 is produced by contacting the initial solution 28 with one side of the initial semipermeable membrane 24. Using a pump 26, hydraulic pressure is applied to the initial solution 28 such that solvent from the initial solution 28 flows through the initial semi-permeable membrane 24 by reverse osmosis to provide an initial permeate solution 30 on the permeate side of the initial semi-permeable membrane and an initial residual solution 32 on the feed side of the initial semi-permeable membrane. The initial residual solution 32 is used as feed solution 16 to the first semi-permeable membrane 14. The initial permeate solution 30 may be withdrawn and used or further purified. The pump 26 may be used to deliver the hydraulic pressure required by the downstream reverse osmosis unit.
The permeate solution 18 on the permeate side of the first semi-permeable membrane 14 may be recycled for use as part of the initial solution 28.
Fig. 4 depicts a schematic illustration of a system for implementing a process according to a fourth example of the present disclosure. The system 10 of fig. 4 is similar to the system of fig. 3 and like components have been labeled with like numerals. However, rather than feeding a portion 16a of feed solution 16 to permeate side 14b of first semi-permeable membrane 14, a portion 20a of residual solution 20 on feed side 14a of first semi-permeable membrane 14 is fed to permeate side 14b of first semi-permeable membrane 14.
Fig. 5 depicts a schematic illustration of a system for implementing a process according to a fifth example of the present disclosure. The system 10 of fig. 5 is similar to the system 10 of fig. 3, and like components have been labeled with like numerals. However, in the system 10 of fig. 5, residual solution 20 from the feed side 14a of the first semi-permeable membrane is withdrawn and contacted as additional feed solution with one side of an additional semi-permeable membrane 34.
Hydraulic pressure delivered by pump 26 or other means is applied to the additional feed solution in contact with the additional semi-permeable membrane 34 such that solvent from the additional feed solution flows through the additional semi-permeable membrane 34 by reverse osmosis. This provides an additional permeate solution 36 on the permeate side of the additional semipermeable membrane and an additional residual solution 38 on the feed side of the additional semipermeable membrane 34. A portion of the additional feed solution 20b is fed to the permeate side of the second semi-permeable membrane. Additional residual solution 38 may be disposed of or further concentrated for disposal. At least a portion of the additional permeate solution 36 may be recycled as at least a portion of the initial solution 28.
Fig. 6 depicts a schematic illustration of a system for implementing a process according to a sixth example of the present disclosure. The system 10 of fig. 6 is similar to the system 10 of fig. 5, and like components have been labeled with like numerals. However, in fig. 6, recycled to permeate side 14b of first semi-permeable membrane 14 to reduce the permeation difference across membrane 14 is a portion 20a of residual solution 20. Recycled to the permeate side of the further semipermeable membrane is a portion 38a of the further residual solution 38 also on the feed side of the further semipermeable membrane 34.
Fig. 7 depicts a schematic illustration of a system for implementing a process according to a seventh example of the present disclosure. The system 10 of fig. 7 is similar to the system 10 of fig. 1, and like components have been labeled with like numerals. However, in FIG. 7, the feed solution 16 is produced by contacting the initial solution 100 with one side of an initial semipermeable membrane 110. Hydraulic pressure may be applied to the initial solution, for example via pump 112, such that solvent from the initial solution 100 flows through the initial semipermeable membrane 110 by reverse osmosis to provide an initial residual solution 114 on the feed side of the initial semipermeable membrane and an initial permeate solution 116 on the permeate side of the initial semipermeable membrane. The initial permeate solution 116 may be removed for use or further purification. The initial residual solution 114 is brought into contact with one side of an additional semi-permeable membrane 118. Hydraulic pressure may be applied to the initial residual solution 114, for example, using pump 112 to the initial residual solution 114, such that solvent from the initial residual solution 114 flows through the additional semi-permeable membrane 118 by reverse osmosis. This flow of solvent provides an additional permeate solution 120 on the permeate side of the additional semipermeable membrane 118 and an additional residual solution 122 on the feed side of the additional semipermeable membrane 118. Additional residual solution 122 may be used as feed to the first semi-permeable membrane 14.
Fig. 8 depicts a schematic illustration of a system for implementing a process according to an eighth example of the present disclosure. The system 10 of fig. 8 is similar to the system 10 of fig. 7, and like components have been labeled with like numerals. However, in fig. 6, recycled to permeate side 14b of first semi-permeable membrane 14 to reduce the permeation difference across membrane 14 is a portion 20a of residual solution 20.
Fig. 9 depicts a schematic illustration of a system for implementing a process according to a ninth example of the present disclosure. The system 10 of fig. 9 is similar to the system 10 of fig. 8, and like components have been labeled with like numerals. However, rather than the permeate solution 18 from the first semi-permeable membrane 14 being fed to the permeate side of the additional semi-permeable membrane 118, a portion 20c of the residual solution 20 from the feed side 14a of the first semi-permeable membrane 14 is fed to the permeate side of the additional semi-permeable membrane 118. Permeate solution 18 from first semi-permeable membrane 14 may be recycled for use as part of initial solution 100.
Fig. 10 depicts a schematic illustration of a system for implementing a process according to a tenth example of the present disclosure. The system 10 of fig. 10 is similar to the system 10 of fig. 9, and like components have been labeled with like numerals. However, in FIG. 10, the initial solution 100 is produced by contacting impure solution 200 with one side of a forward osmosis membrane 210. An opposite side of the forward osmosis membrane 210 is brought into contact with a starting solution precursor 212, wherein the starting solution precursor 212 has a higher solute concentration than the impure solution, such that solvent from the impure solution flows across the forward osmosis membrane by forward osmosis to dilute the starting solution precursor to produce a starting solution 100. The initial solution 100 may be stored, for example, in the storage vessel 216 prior to contact with the initial semipermeable membrane 110. The concentrated impure solution 214 on the feed side of the forward osmosis membrane 210 may be withdrawn and optionally discarded or further concentrated.
The initial solution precursor 212 may be formed by dissolving the osmotic agent 218 in water. The initial solution precursor 212 may be formed by recycling at least a portion of the residual solution 20 from the first semi-permeable membrane 14 to the permeate side of the forward osmosis membrane 210. Recycled residual solution 20 exudate (bleed) may be removed and discarded via line 220 if desired.
Fig. 11 depicts a schematic illustration of a system for implementing a process according to an eleventh example of the present disclosure. In fig. 11, a pump is used to apply hydraulic pressure to drive the initial feed 300 through the reverse osmosis membrane 310 under reverse osmosis conditions. Permeate 312 is withdrawn as product while residual solution 314 is in contact with semi-permeable membrane 316. The residual pressure from the pump is used to drive the residual solution through the membrane. However, draw solution 318, containing added osmotic agent 328, is brought into contact with the opposite side of semi-permeable membrane 316 in order to reduce the osmotic pressure differential across membrane 316. This assists the reverse osmosis step across membrane 316 in osmosis. The permeate through membrane 316 is withdrawn as a dilute draw solution and stored in tank 322, while the residual solution 324 from membrane 316 is withdrawn as a concentrate.
To regenerate the diluted draw solution in tank 322, a portion of the draw solution is withdrawn and pumped 325 through reverse osmosis membrane 326. This produces a permeate 328 and a residual solution 330 that can be withdrawn as product. The residual solution 330 is brought into contact with a semi-permeable membrane 332. The pressure applied using pump 325 for the previous reverse osmosis step may be used to drive residual solution 330 through membrane 332 to produce permeate, which is recycled to tank 322. However, a portion 336 of residual solution 334 is fed to the permeate side of membrane 332 to osmotically assist in reverse osmosis across membrane 332. The remainder of the residual solution 334 is recycled to the membrane 316 as regenerated draw solution. An osmotic agent 328 may be added to the regenerated draw solution. The exudate 338 may also be used to withdraw some of the regenerated draw solution, e.g., as an exudate for disposal or treatment, e.g., to reduce the risk of accumulation of unwanted impurities in the circulating draw solution.
The reader's attention is directed to all papers and documents which are filed concurrently with or previous to this specification in connection with this application and which are open to public inspection with this specification, and the contents of all such papers and documents are incorporated herein by reference.
Claims (17)
1. A process for separating a solvent from a feed solution, the process comprising
Contacting the feed solution with one side of a first semi-permeable membrane;
applying hydraulic pressure to the feed solution such that solvent from the feed solution flows through the first semi-permeable membrane by reverse osmosis to provide a permeate solution on a permeate side of the first semi-permeable membrane and a residual solution on a feed side of the first semi-permeable membrane; and
feeding a portion of the feed solution or a portion of the residual solution to the permeate side of the first semi-permeable membrane.
2. The process of claim 1, wherein fed to the permeate side of the first semi-permeable membrane is a portion of the feed solution.
3. The process of claim 1, wherein fed to the permeate side of the first semi-permeable membrane is a portion of the residual solution.
4. The process of any one of the preceding claims, wherein the feed solution to the first semi-permeable membrane is produced by:
contacting the initial solution with one side of the initial semipermeable membrane;
applying hydraulic pressure to the initial solution such that solvent from the initial solution flows through the initial semi-permeable membrane by reverse osmosis to provide an initial permeate solution on a permeate side of the initial semi-permeable membrane and an initial residual solution on a feed side of the initial semi-permeable membrane; wherein the initial residual solution is used as the feed solution.
5. The process of claim 4, wherein a portion of the permeate solution on the permeate side of the first semi-permeable membrane is recycled as feed to the initial semi-permeable membrane.
6. The process of claim 4 or 5, wherein the hydraulic pressure applied to the initial solution is used at least in part to apply hydraulic pressure to the feed solution in contact with the first semi-permeable membrane.
7. The process of any one of claims 4 to 6, further comprising withdrawing at least a portion of the residual solution from the feed side of the first semi-permeable membrane and contacting the withdrawn solution as an additional feed solution with one side of an additional semi-permeable membrane.
8. The process of claim 7, further comprising applying hydraulic pressure to the additional feed solution in contact with the additional semipermeable membrane such that solvent from the additional feed solution flows through the additional semipermeable membrane by reverse osmosis to provide an additional permeate solution on a permeate side of the additional semipermeable membrane and an additional residual solution on a feed side of the additional semipermeable membrane; and
feeding a portion of the additional feed solution or a portion of the additional residual solution to the permeate side of the second semi-permeable membrane.
9. The process of claim 8, wherein a portion of the additional permeate solution on the permeate side of the additional semipermeable membrane is recycled as feed to the initial semipermeable membrane.
10. The process of any one of claims 7 to 9, wherein the hydraulic pressure applied to the initial solution is used at least in part to apply hydraulic pressure to the feed solution in contact with the first semi-permeable membrane and the feed solution in contact with the additional semi-permeable membrane.
11. The process of claim 1, wherein the feed solution to the first semi-permeable membrane is produced by:
Contacting the initial solution with one side of the initial semipermeable membrane;
applying hydraulic pressure to the initial solution such that solvent from the initial solution flows through the initial semi-permeable membrane by reverse osmosis to provide an initial permeate solution on a permeate side of the initial semi-permeable membrane and an initial residual solution on a feed side of the initial semi-permeable membrane;
contacting the initial residual solution with one side of an additional semi-permeable membrane;
applying hydraulic pressure to the initial residual solution such that solvent from the initial residual solution flows through the additional semipermeable membrane by reverse osmosis to provide an additional permeate solution on a permeate side of the additional semipermeable membrane and an additional residual solution on a feed side of the additional semipermeable membrane; and
using the additional residual solution as a feed to the first semi-permeable membrane.
12. The process of claim 11, wherein at least a portion of the first permeate solution from the first semi-permeable membrane is withdrawn and fed to the permeate side of the additional semi-permeable membrane.
13. The process of claim 11, wherein at least a portion of the additional residual solution from the additional semi-permeable membrane is withdrawn and fed to the permeate side of the first semi-permeable membrane.
14. The process of claim 11 or 13, wherein at least a portion of the first permeate solution from the first semi-permeable membrane is recycled as a feed to the initial semi-permeable membrane.
15. The process of any one of claims 11 to 13, wherein the hydraulic pressure applied to the initial solution is used at least in part to apply hydraulic pressure to the feed solution in contact with the first semi-permeable membrane and/or the further feed solution in contact with the further semi-permeable membrane.
16. The process of any one of claims 4 to 15, wherein the initial solution is produced by:
contacting the impure solution with one side of the forward osmosis membrane,
contacting an opposite side of the forward osmosis membrane with a starting solution precursor, wherein the starting solution precursor has a lower osmotic potential than the impure solution, such that solvent from the impure solution flows across the forward osmosis membrane by forward osmosis to dilute the starting solution precursor to produce the starting solution.
17. The process of claim 16, wherein a portion of the residual solution from the first or additional selective membranes is recycled to the opposite side of the forward osmosis membrane.
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| GBGB1719153.7A GB201719153D0 (en) | 2017-11-20 | 2017-11-20 | Solvent separation |
| GB1719153.7 | 2017-11-20 | ||
| PCT/GB2018/053347 WO2019097261A1 (en) | 2017-11-20 | 2018-11-19 | Solvent separation |
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| CN111867705A true CN111867705A (en) | 2020-10-30 |
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| EP3328522A4 (en) | 2015-07-29 | 2019-04-24 | Gradiant Corporation | Osmotic desalination methods and associated systems |
| US11629072B2 (en) | 2018-08-22 | 2023-04-18 | Gradiant Corporation | Liquid solution concentration system comprising isolated subsystem and related methods |
| WO2021061343A1 (en) * | 2019-09-25 | 2021-04-01 | Veolia Water Solutions & Technologies Support | Energy efficient process for concentrating and recovering lithium from a lithium containing brine |
| JP7020512B2 (en) * | 2020-06-30 | 2022-02-16 | 東洋紡株式会社 | Membrane separation device and concentration method |
| EP4247522A1 (en) | 2020-11-17 | 2023-09-27 | Gradiant Corporation | Osmotic methods and systems involving energy recovery |
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| ZA202003213B (en) | 2023-11-29 |
| GB201719153D0 (en) | 2018-01-03 |
| WO2019097261A1 (en) | 2019-05-23 |
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