US20050161343A1 - Apparatus and method for brine separation and reuse - Google Patents
Apparatus and method for brine separation and reuse Download PDFInfo
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- US20050161343A1 US20050161343A1 US10/763,691 US76369104A US2005161343A1 US 20050161343 A1 US20050161343 A1 US 20050161343A1 US 76369104 A US76369104 A US 76369104A US 2005161343 A1 US2005161343 A1 US 2005161343A1
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- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 95
- 238000000926 separation method Methods 0.000 title claims abstract description 28
- 239000012267 brine Substances 0.000 title claims description 73
- 238000000034 method Methods 0.000 title claims description 35
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- 239000012535 impurity Substances 0.000 claims abstract description 61
- 239000012528 membrane Substances 0.000 claims abstract description 45
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 21
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 21
- 230000001172 regenerating effect Effects 0.000 claims abstract description 3
- 230000008569 process Effects 0.000 claims description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 17
- 150000002500 ions Chemical class 0.000 claims description 12
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- 229910001385 heavy metal Inorganic materials 0.000 claims description 10
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- 238000005342 ion exchange Methods 0.000 claims description 7
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- 239000012141 concentrate Substances 0.000 abstract description 2
- 125000006850 spacer group Chemical group 0.000 description 17
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- VLTRZXGMWDSKGL-UHFFFAOYSA-M perchlorate Inorganic materials [O-]Cl(=O)(=O)=O VLTRZXGMWDSKGL-UHFFFAOYSA-M 0.000 description 10
- VLTRZXGMWDSKGL-UHFFFAOYSA-N perchloric acid Chemical compound OCl(=O)(=O)=O VLTRZXGMWDSKGL-UHFFFAOYSA-N 0.000 description 10
- 238000000909 electrodialysis Methods 0.000 description 9
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- DJHGAFSJWGLOIV-UHFFFAOYSA-K Arsenate3- Chemical compound [O-][As]([O-])([O-])=O DJHGAFSJWGLOIV-UHFFFAOYSA-K 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 4
- 229940000489 arsenate Drugs 0.000 description 4
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- 238000010612 desalination reaction Methods 0.000 description 4
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- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
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- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 229910052785 arsenic Inorganic materials 0.000 description 3
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 3
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- 229910001220 stainless steel Inorganic materials 0.000 description 2
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- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- 239000002033 PVDF binder Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
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- 229910052793 cadmium Inorganic materials 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
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- HTXDPTMKBJXEOW-UHFFFAOYSA-N dioxoiridium Chemical compound O=[Ir]=O HTXDPTMKBJXEOW-UHFFFAOYSA-N 0.000 description 1
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- 229910000457 iridium oxide Inorganic materials 0.000 description 1
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- 229910052749 magnesium Inorganic materials 0.000 description 1
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- 238000005325 percolation Methods 0.000 description 1
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- 229920001155 polypropylene Polymers 0.000 description 1
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- 229910052712 strontium Inorganic materials 0.000 description 1
- CIOAGBVUUVVLOB-UHFFFAOYSA-N strontium atom Chemical compound [Sr] CIOAGBVUUVVLOB-UHFFFAOYSA-N 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
- C02F1/4695—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis electrodeionisation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/103—Arsenic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/46115—Electrolytic cell with membranes or diaphragms
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4618—Supplying or removing reactants or electrolyte
- C02F2201/46185—Recycling the cathodic or anodic feed
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/22—Eliminating or preventing deposits, scale removal, scale prevention
Definitions
- the invention relates to the field of electrolytic membrane separation systems.
- ion exchange systems are configured with resins to extract impurities from a feed liquid such as groundwater and/or potable water. These impurities are accumulated until the ion exchange resin has been exhausted, namely all of the replacement ions coated on the resin are gone. Thereafter, the ion exchange resin must be either disposed of as a hazardous material or regenerated.
- the brine solution is an aqueous solution, perhaps with an elevated level of minerals, such as replacement ions for ion exchange resin regeneration.
- the brine solution causes the impurities to be released.
- contaminated brine solution a large volume of brine solution, perhaps a thousand or more gallons of brine solution in some cases, is contaminated with the released impurities (hereinafter referred to as “contaminated brine solution”).
- the contaminated brine solution needs to be transported to an off-site waste treatment facility. Such removal of the contaminated brine solution poses a substantial cost.
- membrane separation systems are designed with a membrane to separate different ionic material from water.
- nano-filtration uses a porous membrane that is partially permeable to perform such separation.
- the separated ionic materials are as part of the reject solution that is output along with the filtered water. Since the composition of the reject solution is substantially water, and only a small amount of separated ionic material, it is not cost effective to merely dispose of the reject solution.
- FIG. 1 is an exemplary embodiment of a process system that not only reduces the volume of waste required for treatment or disposal, but also recycles the brine solution for reuse.
- FIG. 2 is an exemplary embodiment of a membrane electrolysis (ME) unit associated with the EMS subsystem of FIG. 1 .
- ME membrane electrolysis
- FIG. 3 is a first detailed embodiment of the ME unit of FIG. 2 associated with the EMS subsystem of FIG. 1 .
- FIG. 4 is an embodiment of a cell frame of FIG. 3 .
- FIG. 5 is a detailed embodiment of the ME unit of FIG. 3 implemented with a clamping unit.
- FIG. 6 is an exemplary embodiment of an expanded metal screen cathode of the ME unit of FIG. 3 .
- FIG. 7 is a second detailed embodiment of the ME unit of FIG. 2 .
- FIG. 8 is a third detailed embodiment of the ME unit having multiple cells.
- FIG. 9 is an exemplary embodiment of a flowchart of the operations of an EMS subsystem to recover the brine solution and remove an impurity such as perchlorate.
- FIG. 10 is an exemplary embodiment of a flowchart of the operations of the EMS subsystem to recover the brine solution and remove an impurity, such as heavy metals for example.
- FIG. 11 is an exemplary embodiment of an EMS subsystem for reducing hardness in drinking water and recycling the brine solution for reuse.
- FIG. 12 is an exemplary embodiment of a flowchart of the operations of the EMS subsystem to increase the concentration of the decontaminated brine solution for reuse.
- FIG. 13 is an exemplary embodiment of EMS subsystem for water desalination and recycling of the brine solution for reuse.
- FIG. 14 is an exemplary embodiment of a flowchart of the operations of the EMS subsystem to recover the brine solution and remove an impurity, such as a bivalent anion (arsenic) for example.
- an impurity such as a bivalent anion (arsenic) for example.
- an exemplary embodiment of the invention relates to an electrolytic membrane separation (EMS) subsystem and improved operations thereof.
- the EMS subsystem is configured to remove one or more impurities from a contaminated brine solution and to recycle the reusable brine solution for subsequent use in regenerating ion exchange resins.
- the EMS subsystem is configured to concentrate the impurities recovered from the contaminated brine solution for subsequent disposal or treatment.
- brine solution is water combined with certain minerals at an elevated level.
- concentrated minerals include, but are not limited or restricted to the targeted impurities.
- the brine solution may be a non-aqueous, conductive solution with an elevated level of certain minerals.
- a “spacer” is generally defined as a device that provides a defined distance between either adjacent membranes or a membrane and electrode for liquid to flow or move therebetween. Normally, the spacer is non-conductive.
- a “membrane” is generally defined as a thin section of material that allows ions of a certain chemical composition to migrate from one side to another, while ions of another chemical composition are precluded from passing through the material.
- a “solution” is a liquid of any chosen chemical composition.
- the process system 10 comprises an impurity separation subsystem 20 and an electrolytic membrane separation (EMS) subsystem 100 .
- the impurity separation subsystem 20 may be either a membrane separation system (e.g., micro-filter, ultra-filter, nano-filter, Reverse Osmosis unit) or an ion exchange unit.
- the membrane separation system would accumulate impurities migrating through one or more membranes and output a reject solution featuring these accumulated impurities.
- the ion exchange unit would accumulate impurities on the ion exchange resin and such impurities would be released in the regenerate brine solution applied to the resin.
- the impurity separation subsystem 20 accumulates and releases targeted impurities that have migrated through one or more selected membranes.
- a process solution 30 e.g., an aqueous solution such as groundwater and/or potable water
- a process solution 30 e.g., an aqueous solution such as groundwater and/or potable water
- removes selected impurities such as monovalent ions (e.g., perchlorate), anions (e.g., arsenate), heavy metals (e.g., Nickel “Ni”, Copper “Cu”, Cadmium “Cd”, lead “Pb”, etc.) and the like.
- a solution 40 such as a filtrate that is substantially free from the targeted impurities, is produced.
- a reject solution 60 perhaps brine solution used for regeneration purposes, is supplied to the EMS subsystem 100 .
- a brine (regenerate) solution 50 is directed to flow through the ion exchange resin. This causes the captured impurities to be released into the brine solution.
- the brine solution, now with a higher concentration of the selected impurities (hereinafter referred to as the “contaminated brine solution”) 60 is routed as the reject solution to the EMS subsystem 100 .
- the impurity separation system 20 When the impurity separation system 20 is deployed as a membrane separation system, impurities from the process solution 30 are captured by the membrane and directly released as part of the reject solution 60 .
- the reject solution 60 now with the impurities, is routed to the EMS subsystem 100 .
- the EMS subsystem 100 comprises an anode 110 and a cathode 120 being a part of a reject process unit 130 .
- the reject process unit 130 is a membrane electrolysis (ME) unit.
- the reject process unit 130 is an electrodialysis (ED) unit.
- the reject process unit 130 receives and processes the contaminated brine solution 60 to produce either a reusable brine solution 70 or diluate 80 , which is sufficiently free from targeted impurities to be supplied to the second solution 40 .
- the optional production of reusable brine solution 70 or diluate 80 is represented by dashed lines.
- a maintenance solution 90 namely a selected electrically conductive solution, is supplied to the reject process unit 130 to receive the impurities. Therefore, the maintenance solution 95 with an elevated level of impurities is waste for subsequent storage or treatment.
- the ME unit 130 comprises at least one cell formed by a plurality of cell frames 200 and 210 , which are separated by a membrane 220 and at least two screen spacers 230 and 240 .
- a first screen spacer 230 is interposed between cell frame 200 and membrane 220 while a second screen spacer 240 is interposed between cell frame 210 and membrane 220 .
- each cell frame 200 and 210 is made of a material that mitigates corrosive effects caused by the process and brine solutions as well as harmful effects caused by temperature variations.
- Examples of the type of material forming the cell frames 200 and 210 include, but are not limited or restricted to PVC, polypropylene and PVDF.
- each cell frame 200 and 210 is polygon shaped with a thickness (D 1 , D 2 ) approximately ranging between one-half of an inch (1 ⁇ 2′′) to one inch (1′′).
- the thickness of each cell frame 200 or 210 may vary for industrial applications. This thickness may affect the overall system performance as well as provide appropriate mechanical stability.
- each cell frame 200 and 210 features a perimeter 201 and 211 and a compartment 202 and 212 , respectively.
- the collective depth of the compartments 202 and 212 is sufficient to house, at a minimum, anode and cathode components, at least one membrane 220 and optional screen spacers 230 and 240 .
- a first cell frame 200 is configured with the anolyte compartment 202 to contain an anode 260 adapted with a positive voltage (referred to as an “anode cell frame”).
- the anode cell frame 200 comprises an in-flow port 204 positioned along its perimeter 201 .
- an in-flow port 204 may be positioned at a first side edge 205 near a top edge 207 of the anode cell frame 200 .
- This allows fluid (e.g., conductive solution in one embodiment) to flow into the anode cell frame 200 .
- An out-flow port (not shown) is positioned at a second side edge 206 near a bottom edge 208 of the anode cell frame 200 .
- These ports allow fluid (e.g., conductive solution with an elevated level of impurities) to flow into and out of the anode cell frame 200 .
- At least one sidewall 209 of the anode cell frame 200 is either transparent or perhaps translucent. This provides an ability to view internal components and operations within the anode cell frame 200 .
- the sidewall 209 is made of a clear PVC material, a person can shine a light into the anode cell frame 200 for inspection purposes during maintenance of the ME unit 130 .
- a second cell frame 210 is configured with the catholyte compartment 212 to contain a cathode 400 (hereinafter referred to as a “cathode cell frame”).
- the cathode 400 receives a negative voltage from an external source (e.g., rectifier).
- an in-flow port 214 is positioned along a perimeter (e.g., side edge 211 1 ) of the cathode cell frame 210 near a bottom edge 213 of the cell frame 210 as shown in FIG. 4 .
- the in-flow port 214 allows fluid (e.g., contaminated brine solution) to flow into the cathode cell frame 210 .
- An out-flow port 216 is positioned at a side edge 211 2 near a top edge 215 of the cathode cell frame 210 , which allows fluid (e.g., reusable brine solution) to flow out therefrom.
- the positioning of out-flow port 216 above the in-flow port 214 is designed to substantially mitigate air bubbles.
- At least one sidewall 218 of cathode cell frame 210 is either transparent or perhaps translucent. This provides an ability to view internal components and operations within the cathode cell frame 210 .
- the sidewall 218 is made of a clear PVC material, a person can shine a light into the cathode cell frame 210 for inspection purposes for maintenance of the ME unit 130 . For example, one can check whether electrodes of the cell frame 210 are corroded.
- the positioning of in-flow ports and out-flow ports along side edges may alternate between neighboring cell frames.
- the cathode cell frame 210 features out-flow port 216 positioned near the top edge 215 of the cathode cell frame 210 .
- the out-flow port (not shown) is positioned near the bottom edge 208 while the in-flow port 204 is positioned near the top edge 207 . This provides a cross flow condition for the fluid being processed.
- the ME unit 130 may be physically stabilized using two end frames as a clamping unit 300 .
- clamping unit 300 comprises two clamping frames 310 and 311 , perhaps made of a metal such as stainless steel, placed adjacent to and generally flush against cell frames 200 and 210 .
- each of the clamping frames 310 and 311 features a center opening 312 and 313 , respectively. These openings 312 and 313 are situated over the transparent or translucent sidewalls 209 and 218 , respectively.
- Each of the clamping frames 310 and 311 also features apertures.
- Each aperture of the clamping frame 310 is aligned with an aperture of the clamping frame 311 .
- the apertures of the clamping frames 310 and 311 may be predrilled or may be made at the time of assembly.
- Fastening rods 320 , 325 , 330 , 335 are inserted through the apertures with fastening components 340 placed at each end or at least one end of the fastening rods 320 , 325 , 330 and 335 .
- the fastening components 340 may are rotated in a clockwise direction so that clamping frames 310 and 311 are forced closer together and sandwich cell frames 200 , 210 , spacers 230 , 240 and membranes 220 until the ME cell is sealed and stabilized. It is contemplated, however, that the clamping frames 310 and 311 may be forced closer together by hydraulic equipment in lieu of fastening components.
- each rod (e.g., rod 330 ) comprises a body portion 331 , a first end 332 and a second end 333 .
- a first end 332 is sized with a diameter less than the diameter of one of the apertures formed within the clamping frame 310 . Inserted through this aperture, the first end 332 of rod 330 may be threaded to receive the fastening component 340 .
- a “fastening component” include, but are not limited or restricted to different types of hardware such as a threaded nut, wing nut, lock nut or the like.
- the fastening component 340 is used to tighten and pull together the clamping frames 310 and 320 .
- the fastening component 340 may be a fastener that does not require threaded ends of rods 320 , 325 , 330 and 335 .
- a force is applied to a front surfaces 316 and 317 of the clamping frames 310 and 311 , where the fastening components 340 are slid on the rods 320 , 325 , 330 and 335 and secured by soldering, contraction of an opening within the fastening components 340 or the like.
- the second end 333 of rod 330 may be sized with a diameter greater than the diameter of its corresponding aperture placed in the second clamping frame 311 .
- the first end 332 and the body portion 331 of rod 330 is inserted through the aperture until the second end 333 engages with the wall forming the aperture.
- the second end 333 may be sized with a diameter less than the diameter of its corresponding aperture. Hence, another fastening component would be placed thereon.
- cathode 400 comprises a material formed as a mesh screen 410 .
- the material is referred to as “expanded metal,” such as, for example, platinum, stainless steel or a base material electroplated or cladded with a conductive material (e.g., platinum plated titanium, iridium plated titanium, iridium oxide coated titanium, etc.).
- the cathode 400 may be deployed in a variety of embodiments besides as an expanded metal screen cathode, such as a filling (e.g., negatively charged metal or carbon beads) for example.
- cathode 400 comprises a plurality of electrical connectors (electrodes) 420 and 430 , a portion 421 , 431 of which are made of expanded metal. These electrodes 420 and 430 protrude from the mesh screen 410 for coupling with a bus bar 250 on a top edge 215 of the cell frame 210 as shown in FIG. 3 .
- the bus bar 250 includes connectors 251 and 252 sized to receive connectors 420 and 430 for attachment thereto.
- anode cell frame 200 comprises the anode 260 , which is configured as a self-supporting screen and placed between screen spacer 230 and housed within the anolyte compartment 202 of anode cell frame 200 .
- the screen is self-supporting by the inclusion of a frame 261 bordering a perimeter of screening material 262 .
- a bus bar 270 is attached to the anode 260 via connectors as used for attachment of the cathode 400 .
- the connectors may need to be of greater length than connectors 420 and 430 of FIG. 6 .
- the cell frames 200 and 210 of the ME unit 130 are completely closed, but may be coupled to an external tank with ventilation. This coupling allows off-gassing when the electrodes are energized and electrochemical reactions occur in the inside of the cell frames 200 and 210 at the electrodes.
- Each spacer 230 and 240 includes a gasket structure, a one-piece structure according to one embodiment, and is made from a material that provides good mechanical and stability properties at the interface between the gasket and a cell frame.
- the spacers 230 and 240 provide a pressurized seal between the cell frames 200 and 210 and the membrane 220 .
- a second exemplary embodiment of the ME unit 130 is shown.
- the ME unit 130 comprises the anode cell frame 200 and the cathode cell frame 210 separated by a third non-conductive frame (referred to as “PVC frame”) 500 .
- the anode cell frame 200 neighbors a first screen spacer 510 .
- a first membrane 520 is interposed between the first screen spacer 510 and a second screen spacer 530 , which neighbors PVC frame 500 .
- PVC frame 500 is similar in construction to cell frames 200 and 210 but does not include electrodes.
- This multiple membrane configuration with additional components may be repeated to support an additional membrane between PVC frame 500 and cathode cell frame 210 . It is noted that these additional components may be repeated for additional cell frames or cells.
- a first cell 600 comprises an anode cell frame 605 , a cathode cell frame 610 , and a first membrane 615 .
- Spacers 620 and/or 625 may be optionally provided between the first membrane 615 and the respective cell frames 605 and 610 .
- a second cell 630 comprises an anode cell frame 635 , a cathode cell frame 640 , a second membrane 645 and optional spacers 650 and/or 655 .
- a PVC frame 660 is interposed between the cells 600 and 630 so that fluid may be exchanged between the cell frames and the cells themselves in a cross flow orientation as described in FIG. 3 .
- an ED unit When an ED unit is utilized such as in desalination as described below, it has a similar construction to an ME unit as shown in FIGS. 5 and 6 .
- the ED unit would feature multiple cell frames alternating between anode and cathode cell frames with an inert frame placed between each anode and cathode cell frame pair.
- the ED unit would further feature clamping frames at each end of the ED unit and secured together through hydraulics for example.
- FIG. 9 an exemplary embodiment of a flowchart of the operations of an EMS subsystem to recover the brine solution and remove an impurity, such as a monovalent anion (perchlorate) for example, from the ME unit 130 is shown.
- a brine solution being a high volume in order of magnitude of a thousand gallons or more, is feed into an in-flow port of a cathode cell frame in order to flow through the catholyte compartment of the ME unit (block 700 ).
- a conductive maintenance solution having a volume substantially less in magnitude than the brine solution, is applied to the anolyte compartment of the ME unit via an in-flow port of an anode cell frame (block 710 ).
- the electrodes associated with these compartments are energized to generate a current that forces monovalent anions to migrate from the catholyte compartment through the membrane to the anolyte compartment (block 720 ). Since perchlorate is a monovalent ion, depending on the adjusted current density in the EMS subsystem, it migrates into the anolyte compartment of the EMS subsystem.
- the perchlorate accumulates in the anolyte compartment of the ME unit (block 730 ). This migration causes a significant reduction in the perchlorate concentration in the contaminated brine solution. Moreover, an electro-chemical decomposition (off-gassing) of water during processing of the contaminated brine solution causes an increased concentration of the reusable brine solution (block 740 ).
- the reusable brine solution substantially free of the perchlorate, is output from an out-flow port of the cathode cell frame and can be used for further regeneration of the ion exchange resins (block 750 ). This avoids unnecessary disposal of the brine solution.
- the maintenance solution with an elevated level of perchlorate is output from an out-flow port of the anode cell frame for waste treatment or storage (block 760 ).
- nitrate may be treated in a manner similar to perchlorate. This will be facilitated when nitrate is removed from an ion exchange resin bed with a brine solution.
- nitrate is contaminant of an aqueous solution (surface water, groundwater, potable water, etc.)
- an alternative treatment process can be applied. Such treatment would be conducted within an ED unit, not an ME unit.
- the process solution e.g., surface, potable or ground water
- the maintenance solution is feed into the anolyte compartment. Once the electrodes associated with these compartments are energized, the nitrate migrates into the anolyte compartment and outputs the same as reject.
- FIG. 10 an exemplary embodiment of a flowchart of the operations of the EMS subsystem 100 to recover the brine solution and remove an impurity, such as heavy metals for example, from the ME unit 130 is shown.
- the operations are substantially equivalent to the operations for removing perchlorate as described in FIG. 9 ; however, the contaminated brine solution is fed into the in-flow port of the anode cell frame while a negatively conductive maintenance solution is fed into the in-flow port of the cathode cell frame (blocks 800 and 810 ).
- the electrodes associated with these compartments are energized (block 820 ).
- the amount of current is adjusted so that the current density forces any of the heavy metals to migrate from the anolyte compartment through the membrane to the catholyte compartment (block 830 ).
- the heavy metals accumulate in the catholyte compartment of the ME unit (block 840 ), while off-gassing of the water forming a portion of the contaminated brine solution causes an increased concentration of the reusable brine solution (block 850 ).
- the reusable brine solution substantially free of heavy metals, is output from an out-flow port of the anode cell frame (block 860 ).
- the maintenance solution with an elevated level of heavy metals is output from an out-flow port of the cathode cell frame for waste treatment or storage (block 860 ).
- Hardness in drinking water is removed by an ion exchange softening system 900 .
- these ion exchange resin beds are regenerated with a combination of brine solution 910 and surface water 920 that removes the hardness (e.g., calcium, magnesium, barium, strontium, iron and manganese) from the ion exchange resin beds.
- the contaminated brine solution 930 now containing the hardness was discharged into a wastewater treatment plant or into percolation ponds, if available, as illustrated by dashed arrow 940 .
- the ion exchange softening system 900 is in fluid communications with a membrane separation system 950 , such as a nano-filter for example, to remove hardness from the contaminated brine solution 930 that has been further diluted by the softening system 900 .
- the EMS subsystem 100 receives a filtered brine solution 960 , which has been diluted so as to have a lower concentration than the brine solution 910 .
- the EMS subsystem 100 operates by increasing the concentration of the brine solution for reuse.
- FIG. 12 an exemplary embodiment of a flowchart of the operations of the EMS subsystem 100 to increase the concentration of the decontaminated brine solution for reuse is shown.
- the filtered brine solution is directed to flow into an anolyte compartment of a first cell frame of the ME unit via an in-flow port (block 1000 ).
- the electrodes associated with these compartments are energized to generate a current that forces the metals associated with hardness to migrate from the anolyte compartment through the membrane to the catholyte compartment (blocks 1020 and 1030 ).
- the filtered brine solution substantially free of the hardness, can be reused for further regeneration of the ion exchange resin beds without disposal or further treatment (block 1050 ).
- feed water 1100 with low overall quality e.g., ground water, potable water, etc.
- pre-filtration system 1110 e.g., micro-filter, ultra-filter, etc.
- the pre-filtration system 1110 is designed to remove suspended solids and other organic material from the feed water 1100 .
- the filtrate 1120 namely the filtered feed water, is supplied to a membrane separation system 1130 (e.g., nano-filter, Reverse Osmosis, etc.) in order to remove one or more selected impurities (e.g., total dissolved solids).
- the membrane separation system 1130 produces a permeate 1140 , which undergoes disinfection 1150 (e.g., ultraviolet light radiation, chlorination, etc.). This results in purified water 1160 .
- disinfection 1150 e.g., ultraviolet light radiation, chlorination, etc.
- a first reject solution 1170 and a second reject solution 1175 are provided to the EMS subsystem 100 from systems 1110 and 1130 , respectively.
- the EMS subsystem 100 removes the impurities associated with the reject solutions 1170 and 1175 and provides a diluate 1180 (e.g., a solution generally equivalent in composition to the filtrate 1120 ) to the membrane separation system 1130 for further processing. Additionally, the EMS subsystem 100 provides a filtered, concentrated reject solution 1190 for disposal or recycling.
- FIG. 14 an exemplary embodiment of a flowchart of the operations of the EMS subsystem 100 to recover the brine solution and remove an impurity, such as a bivalent anion (arsenic) for example, is shown.
- the brine solution is based on a monovalent aqueous salt solution, so that arsenate can be separated from the brine solution using selective membranes.
- the EMS subsystem 100 is configured with an ED unit (block 1200 ).
- a contaminated brine solution with an elevated level of arsenate is feed into an anolyte compartment of the anode cell frame via an in-flow port of an anode cell frame (block 1210 ).
- a negatively conductive maintenance solution having a volume substantially less in magnitude than the contaminated brine solution, is applied to an catholyte compartment of the ME unit via an in-flow port of an cathode cell frame (block 1220 ).
- the electrodes associated with these compartments are energized to generate a current that forces monovalent salt ions of the brine solution to accumulate within the catholyte compartment through membrane migration (blocks 1230 and 1240 ). Since arsenate is a bivalent ion, it will remain in the anolyte compartment and be output with the maintenance solution for waste treatment and/or disposal (block 1250 ). This filters the contaminated brine solution, and in combination with out-gassing, produces a filtered, concentrated brine solution for regeneration of ion exchange resin beds (block 1260 ).
Abstract
According to one embodiment, an electrolytic membrane separation (EMS) subsystem is configured to remove one or more impurities from a contaminated reject solution and to recycle the reusable reject solution for subsequent use in regenerating ion exchange resins. According to another embodiment of the invention, the EMS subsystem is configured to concentrate the impurities recovered from the contaminated brine solution for subsequent disposal or treatment.
Description
- The invention relates to the field of electrolytic membrane separation systems.
- Currently, there exist a number of conventional systems for separating impurities from a feed solution. For example, ion exchange systems are configured with resins to extract impurities from a feed liquid such as groundwater and/or potable water. These impurities are accumulated until the ion exchange resin has been exhausted, namely all of the replacement ions coated on the resin are gone. Thereafter, the ion exchange resin must be either disposed of as a hazardous material or regenerated.
- In order to regenerate the ion exchange resin, a large volume of brine solution is applied thereto. In most cases, the brine solution is an aqueous solution, perhaps with an elevated level of minerals, such as replacement ions for ion exchange resin regeneration.
- During regeneration of the resin, the brine solution causes the impurities to be released. As a result, a large volume of brine solution, perhaps a thousand or more gallons of brine solution in some cases, is contaminated with the released impurities (hereinafter referred to as “contaminated brine solution”). Usually, the contaminated brine solution needs to be transported to an off-site waste treatment facility. Such removal of the contaminated brine solution poses a substantial cost.
- Similarly, membrane separation systems are designed with a membrane to separate different ionic material from water. For example, nano-filtration uses a porous membrane that is partially permeable to perform such separation. The separated ionic materials are as part of the reject solution that is output along with the filtered water. Since the composition of the reject solution is substantially water, and only a small amount of separated ionic material, it is not cost effective to merely dispose of the reject solution.
- Clearly, it would be advantageous from a cost standpoint to recycle the contaminated brine solution or reject solution as well as reduce the volume of materials that need to be treated as waste.
- The features and advantages of the invention will become apparent from the following detailed description of the invention in which:
-
FIG. 1 is an exemplary embodiment of a process system that not only reduces the volume of waste required for treatment or disposal, but also recycles the brine solution for reuse. -
FIG. 2 is an exemplary embodiment of a membrane electrolysis (ME) unit associated with the EMS subsystem ofFIG. 1 . -
FIG. 3 is a first detailed embodiment of the ME unit ofFIG. 2 associated with the EMS subsystem ofFIG. 1 . -
FIG. 4 is an embodiment of a cell frame ofFIG. 3 . -
FIG. 5 is a detailed embodiment of the ME unit ofFIG. 3 implemented with a clamping unit. -
FIG. 6 is an exemplary embodiment of an expanded metal screen cathode of the ME unit ofFIG. 3 . -
FIG. 7 is a second detailed embodiment of the ME unit ofFIG. 2 . -
FIG. 8 is a third detailed embodiment of the ME unit having multiple cells. -
FIG. 9 is an exemplary embodiment of a flowchart of the operations of an EMS subsystem to recover the brine solution and remove an impurity such as perchlorate. -
FIG. 10 is an exemplary embodiment of a flowchart of the operations of the EMS subsystem to recover the brine solution and remove an impurity, such as heavy metals for example. -
FIG. 11 is an exemplary embodiment of an EMS subsystem for reducing hardness in drinking water and recycling the brine solution for reuse. -
FIG. 12 is an exemplary embodiment of a flowchart of the operations of the EMS subsystem to increase the concentration of the decontaminated brine solution for reuse. -
FIG. 13 is an exemplary embodiment of EMS subsystem for water desalination and recycling of the brine solution for reuse. -
FIG. 14 is an exemplary embodiment of a flowchart of the operations of the EMS subsystem to recover the brine solution and remove an impurity, such as a bivalent anion (arsenic) for example. - Herein, an exemplary embodiment of the invention relates to an electrolytic membrane separation (EMS) subsystem and improved operations thereof. According to one embodiment, the EMS subsystem is configured to remove one or more impurities from a contaminated brine solution and to recycle the reusable brine solution for subsequent use in regenerating ion exchange resins. According to another embodiment of the invention, the EMS subsystem is configured to concentrate the impurities recovered from the contaminated brine solution for subsequent disposal or treatment.
- Herein, the embodiments of the invention described are not exclusive; rather, they merely provide a thorough understanding of the invention. Also, well-known chemicals, reactions and elements are not set forth in detail in order to avoid unnecessarily obscuring the invention.
- In the following description, certain terminology is used to describe features of the invention. For example, the term “brine solution” is water combined with certain minerals at an elevated level. Examples of the concentrated minerals include, but are not limited or restricted to the targeted impurities. Of course, for certain systems, it is contemplated that the brine solution may be a non-aqueous, conductive solution with an elevated level of certain minerals.
- A “spacer” is generally defined as a device that provides a defined distance between either adjacent membranes or a membrane and electrode for liquid to flow or move therebetween. Normally, the spacer is non-conductive. A “membrane” is generally defined as a thin section of material that allows ions of a certain chemical composition to migrate from one side to another, while ions of another chemical composition are precluded from passing through the material. A “solution” is a liquid of any chosen chemical composition.
- I. General Architecture of the Process System
- Referring to
FIG. 1 , an exemplary embodiment of aprocess system 10 is shown that not only reduces the volume of waste required for treatment or disposal, but also recycles the brine solution for reuse. Theprocess system 10 comprises animpurity separation subsystem 20 and an electrolytic membrane separation (EMS)subsystem 100. It is contemplated that theimpurity separation subsystem 20 may be either a membrane separation system (e.g., micro-filter, ultra-filter, nano-filter, Reverse Osmosis unit) or an ion exchange unit. The membrane separation system would accumulate impurities migrating through one or more membranes and output a reject solution featuring these accumulated impurities. The ion exchange unit would accumulate impurities on the ion exchange resin and such impurities would be released in the regenerate brine solution applied to the resin. - Herein, the
impurity separation subsystem 20 accumulates and releases targeted impurities that have migrated through one or more selected membranes. For instance, for this embodiment of the invention, a process solution 30 (e.g., an aqueous solution such as groundwater and/or potable water) is fed into theimpurity separation subsystem 20, which removes selected impurities such as monovalent ions (e.g., perchlorate), anions (e.g., arsenate), heavy metals (e.g., Nickel “Ni”, Copper “Cu”, Cadmium “Cd”, lead “Pb”, etc.) and the like. Asolution 40, such as a filtrate that is substantially free from the targeted impurities, is produced. Moreover, areject solution 60, perhaps brine solution used for regeneration purposes, is supplied to theEMS subsystem 100. - For instance, when the
impurity separation system 20 is deployed as an ion exchange unit and the ion exchange resin is exhausted, a brine (regenerate)solution 50 is directed to flow through the ion exchange resin. This causes the captured impurities to be released into the brine solution. The brine solution, now with a higher concentration of the selected impurities (hereinafter referred to as the “contaminated brine solution”) 60 is routed as the reject solution to theEMS subsystem 100. - When the
impurity separation system 20 is deployed as a membrane separation system, impurities from theprocess solution 30 are captured by the membrane and directly released as part of thereject solution 60. Thereject solution 60, now with the impurities, is routed to theEMS subsystem 100. - II. General Architecture of the EMS Subsystem
- Referring now to
FIGS. 1 and 2 , theEMS subsystem 100 comprises ananode 110 and acathode 120 being a part of areject process unit 130. According to one embodiment, thereject process unit 130 is a membrane electrolysis (ME) unit. According to another embodiment of the invention, thereject process unit 130 is an electrodialysis (ED) unit. Thereject process unit 130 receives and processes the contaminatedbrine solution 60 to produce either areusable brine solution 70 ordiluate 80, which is sufficiently free from targeted impurities to be supplied to thesecond solution 40. The optional production ofreusable brine solution 70 ordiluate 80 is represented by dashed lines. - As described below, a
maintenance solution 90, namely a selected electrically conductive solution, is supplied to thereject process unit 130 to receive the impurities. Therefore, themaintenance solution 95 with an elevated level of impurities is waste for subsequent storage or treatment. - III. Exemplary Architectures of the ME Unit & ED Unit
- Referring now to
FIG. 3 , an exemplary embodiment of thereject process unit 130 configured as an ME unit is shown. Being implemented with a “closed frame” design for this embodiment, theME unit 130 comprises at least one cell formed by a plurality of cell frames 200 and 210, which are separated by amembrane 220 and at least twoscreen spacers first screen spacer 230 is interposed betweencell frame 200 andmembrane 220 while asecond screen spacer 240 is interposed betweencell frame 210 andmembrane 220. - For this embodiment, each
cell frame - Moreover, each
cell frame cell frame - As further shown in
FIG. 3 , eachcell frame perimeter compartment compartments membrane 220 andoptional screen spacers - For this embodiment of the invention, a
first cell frame 200 is configured with theanolyte compartment 202 to contain ananode 260 adapted with a positive voltage (referred to as an “anode cell frame”). Theanode cell frame 200 comprises an in-flow port 204 positioned along itsperimeter 201. For example, an in-flow port 204 may be positioned at afirst side edge 205 near atop edge 207 of theanode cell frame 200. This allows fluid (e.g., conductive solution in one embodiment) to flow into theanode cell frame 200. An out-flow port (not shown) is positioned at asecond side edge 206 near abottom edge 208 of theanode cell frame 200. These ports allow fluid (e.g., conductive solution with an elevated level of impurities) to flow into and out of theanode cell frame 200. - For this embodiment of the invention, at least one
sidewall 209 of theanode cell frame 200 is either transparent or perhaps translucent. This provides an ability to view internal components and operations within theanode cell frame 200. For instance, where thesidewall 209 is made of a clear PVC material, a person can shine a light into theanode cell frame 200 for inspection purposes during maintenance of theME unit 130. - As further shown in
FIG. 4 , asecond cell frame 210 is configured with thecatholyte compartment 212 to contain a cathode 400 (hereinafter referred to as a “cathode cell frame”). Thecathode 400 receives a negative voltage from an external source (e.g., rectifier). - With respect to
cathode cell frame 210, as shown inFIGS. 3 and 4 , an in-flow port 214 is positioned along a perimeter (e.g., side edge 211 1) of thecathode cell frame 210 near abottom edge 213 of thecell frame 210 as shown inFIG. 4 . The in-flow port 214 allows fluid (e.g., contaminated brine solution) to flow into thecathode cell frame 210. An out-flow port 216 is positioned at aside edge 211 2 near atop edge 215 of thecathode cell frame 210, which allows fluid (e.g., reusable brine solution) to flow out therefrom. The positioning of out-flow port 216 above the in-flow port 214 is designed to substantially mitigate air bubbles. - For this embodiment of the invention, at least one
sidewall 218 ofcathode cell frame 210 is either transparent or perhaps translucent. This provides an ability to view internal components and operations within thecathode cell frame 210. For instance, where thesidewall 218 is made of a clear PVC material, a person can shine a light into thecathode cell frame 210 for inspection purposes for maintenance of theME unit 130. For example, one can check whether electrodes of thecell frame 210 are corroded. - It is contemplated that the positioning of in-flow ports and out-flow ports along side edges may alternate between neighboring cell frames. For instance, the
cathode cell frame 210 features out-flow port 216 positioned near thetop edge 215 of thecathode cell frame 210. For the neighboringanode frame 200, however, the out-flow port (not shown) is positioned near thebottom edge 208 while the in-flow port 204 is positioned near thetop edge 207. This provides a cross flow condition for the fluid being processed. - The
ME unit 130 may be physically stabilized using two end frames as aclamping unit 300. As shown inFIG. 5 , clampingunit 300 comprises two clampingframes center opening openings translucent sidewalls - Each of the clamping frames 310 and 311 also features apertures. Each aperture of the
clamping frame 310 is aligned with an aperture of theclamping frame 311. The apertures of the clamping frames 310 and 311 may be predrilled or may be made at the time of assembly. - Fastening
rods fastening components 340 placed at each end or at least one end of thefastening rods fastening components 340 may are rotated in a clockwise direction so that clampingframes spacers membranes 220 until the ME cell is sealed and stabilized. It is contemplated, however, that the clamping frames 310 and 311 may be forced closer together by hydraulic equipment in lieu of fastening components. - Herein, according to one embodiment of the invention, each rod (e.g., rod 330) comprises a
body portion 331, afirst end 332 and asecond end 333. Afirst end 332 is sized with a diameter less than the diameter of one of the apertures formed within theclamping frame 310. Inserted through this aperture, thefirst end 332 ofrod 330 may be threaded to receive thefastening component 340. Illustrative examples of a “fastening component” include, but are not limited or restricted to different types of hardware such as a threaded nut, wing nut, lock nut or the like. Thefastening component 340 is used to tighten and pull together the clamping frames 310 and 320. - It is contemplated, however, that the
fastening component 340 may be a fastener that does not require threaded ends ofrods front surfaces fastening components 340 are slid on therods fastening components 340 or the like. - The
second end 333 ofrod 330 may be sized with a diameter greater than the diameter of its corresponding aperture placed in thesecond clamping frame 311. Thus, thefirst end 332 and thebody portion 331 ofrod 330 is inserted through the aperture until thesecond end 333 engages with the wall forming the aperture. Alternatively, however, thesecond end 333 may be sized with a diameter less than the diameter of its corresponding aperture. Hence, another fastening component would be placed thereon. - Referring now to
FIGS. 2 and 6 ,cathode 400 comprises a material formed as amesh screen 410. The material is referred to as “expanded metal,” such as, for example, platinum, stainless steel or a base material electroplated or cladded with a conductive material (e.g., platinum plated titanium, iridium plated titanium, iridium oxide coated titanium, etc.). Of course, thecathode 400 may be deployed in a variety of embodiments besides as an expanded metal screen cathode, such as a filling (e.g., negatively charged metal or carbon beads) for example. - Herein, for this embodiment,
cathode 400 comprises a plurality of electrical connectors (electrodes) 420 and 430, aportion electrodes mesh screen 410 for coupling with abus bar 250 on atop edge 215 of thecell frame 210 as shown inFIG. 3 . Thebus bar 250 includesconnectors connectors - For this embodiment of the invention, as shown in
FIG. 3 ,anode cell frame 200 comprises theanode 260, which is configured as a self-supporting screen and placed betweenscreen spacer 230 and housed within theanolyte compartment 202 ofanode cell frame 200. The screen is self-supporting by the inclusion of aframe 261 bordering a perimeter ofscreening material 262. Abus bar 270 is attached to theanode 260 via connectors as used for attachment of thecathode 400. However, in this embodiment, the connectors may need to be of greater length thanconnectors FIG. 6 . - Referring still to
FIG. 3 , the cell frames 200 and 210 of theME unit 130 are completely closed, but may be coupled to an external tank with ventilation. This coupling allows off-gassing when the electrodes are energized and electrochemical reactions occur in the inside of the cell frames 200 and 210 at the electrodes. - Each
spacer spacers membrane 220. - In another embodiment, as shown in
FIG. 7 , a second exemplary embodiment of theME unit 130 is shown. TheME unit 130 comprises theanode cell frame 200 and thecathode cell frame 210 separated by a third non-conductive frame (referred to as “PVC frame”) 500. Theanode cell frame 200 neighbors afirst screen spacer 510. Afirst membrane 520 is interposed between thefirst screen spacer 510 and asecond screen spacer 530, whichneighbors PVC frame 500.PVC frame 500 is similar in construction to cell frames 200 and 210 but does not include electrodes. This multiple membrane configuration with additional components (e.g.,spacer 540, second membrane, spacer 560) may be repeated to support an additional membrane betweenPVC frame 500 andcathode cell frame 210. It is noted that these additional components may be repeated for additional cell frames or cells. - For instance, as shown in
FIG. 8 , it is contemplated that multiple cells may be interconnected through PVC frames. As an illustration, afirst cell 600 comprises ananode cell frame 605, acathode cell frame 610, and afirst membrane 615.Spacers 620 and/or 625 may be optionally provided between thefirst membrane 615 and the respective cell frames 605 and 610. Asecond cell 630 comprises ananode cell frame 635, acathode cell frame 640, asecond membrane 645 andoptional spacers 650 and/or 655. APVC frame 660 is interposed between thecells FIG. 3 . - When an ED unit is utilized such as in desalination as described below, it has a similar construction to an ME unit as shown in
FIGS. 5 and 6 . The ED unit would feature multiple cell frames alternating between anode and cathode cell frames with an inert frame placed between each anode and cathode cell frame pair. The ED unit would further feature clamping frames at each end of the ED unit and secured together through hydraulics for example. - IV. Brine Recovery/Removal of Monovalent Ion
- Referring now to
FIG. 9 , an exemplary embodiment of a flowchart of the operations of an EMS subsystem to recover the brine solution and remove an impurity, such as a monovalent anion (perchlorate) for example, from theME unit 130 is shown. A brine solution, being a high volume in order of magnitude of a thousand gallons or more, is feed into an in-flow port of a cathode cell frame in order to flow through the catholyte compartment of the ME unit (block 700). A conductive maintenance solution, having a volume substantially less in magnitude than the brine solution, is applied to the anolyte compartment of the ME unit via an in-flow port of an anode cell frame (block 710). - Generally concurrent to the supply of the brine and maintenance solutions, the electrodes associated with these compartments are energized to generate a current that forces monovalent anions to migrate from the catholyte compartment through the membrane to the anolyte compartment (block 720). Since perchlorate is a monovalent ion, depending on the adjusted current density in the EMS subsystem, it migrates into the anolyte compartment of the EMS subsystem.
- Due to this migration, the perchlorate accumulates in the anolyte compartment of the ME unit (block 730). This migration causes a significant reduction in the perchlorate concentration in the contaminated brine solution. Moreover, an electro-chemical decomposition (off-gassing) of water during processing of the contaminated brine solution causes an increased concentration of the reusable brine solution (block 740).
- Hence, as shown in
block 750, the reusable brine solution, substantially free of the perchlorate, is output from an out-flow port of the cathode cell frame and can be used for further regeneration of the ion exchange resins (block 750). This avoids unnecessary disposal of the brine solution. The maintenance solution with an elevated level of perchlorate is output from an out-flow port of the anode cell frame for waste treatment or storage (block 760). - It is contemplated that another monovalent anion, such as nitrate, may be treated in a manner similar to perchlorate. This will be facilitated when nitrate is removed from an ion exchange resin bed with a brine solution.
- If nitrate is contaminant of an aqueous solution (surface water, groundwater, potable water, etc.), an alternative treatment process can be applied. Such treatment would be conducted within an ED unit, not an ME unit. For this embodiment of the invention, the process solution (e.g., surface, potable or ground water) is feed into an in-flow port of a cathode cell frame in order to flow through the catholyte compartment of the ED unit. The maintenance solution is feed into the anolyte compartment. Once the electrodes associated with these compartments are energized, the nitrate migrates into the anolyte compartment and outputs the same as reject.
- V. Brine Recovery/Removal of Heavy Metal
- Referring now to
FIG. 10 , an exemplary embodiment of a flowchart of the operations of theEMS subsystem 100 to recover the brine solution and remove an impurity, such as heavy metals for example, from theME unit 130 is shown. The operations are substantially equivalent to the operations for removing perchlorate as described inFIG. 9 ; however, the contaminated brine solution is fed into the in-flow port of the anode cell frame while a negatively conductive maintenance solution is fed into the in-flow port of the cathode cell frame (blocks 800 and 810). - Generally concurrent to the supply of the brine and conductive maintenance solutions, the electrodes associated with these compartments are energized (block 820). The amount of current is adjusted so that the current density forces any of the heavy metals to migrate from the anolyte compartment through the membrane to the catholyte compartment (block 830). As a result, the heavy metals accumulate in the catholyte compartment of the ME unit (block 840), while off-gassing of the water forming a portion of the contaminated brine solution causes an increased concentration of the reusable brine solution (block 850).
- Hence, the reusable brine solution, substantially free of heavy metals, is output from an out-flow port of the anode cell frame (block 860). The maintenance solution with an elevated level of heavy metals is output from an out-flow port of the cathode cell frame for waste treatment or storage (block 860).
- VI. Brine Recovery/Removal of Hardness
- Referring now to
FIG. 11 , an exemplary embodiment of an EMS subsystem for reducing hardness in drinking water and recycling the brine solution for reuse is shown. Hardness in drinking water is removed by an ionexchange softening system 900. Typically, these ion exchange resin beds are regenerated with a combination ofbrine solution 910 andsurface water 920 that removes the hardness (e.g., calcium, magnesium, barium, strontium, iron and manganese) from the ion exchange resin beds. Previously, the contaminatedbrine solution 930 now containing the hardness was discharged into a wastewater treatment plant or into percolation ponds, if available, as illustrated by dashedarrow 940. - According to one embodiment of the invention, the ion
exchange softening system 900 is in fluid communications with amembrane separation system 950, such as a nano-filter for example, to remove hardness from the contaminatedbrine solution 930 that has been further diluted by the softeningsystem 900. TheEMS subsystem 100 receives a filteredbrine solution 960, which has been diluted so as to have a lower concentration than thebrine solution 910. TheEMS subsystem 100 operates by increasing the concentration of the brine solution for reuse. - Referring now to
FIG. 12 , an exemplary embodiment of a flowchart of the operations of theEMS subsystem 100 to increase the concentration of the decontaminated brine solution for reuse is shown. After treatment by the nano-filter to remove hardness, the filtered brine solution is directed to flow into an anolyte compartment of a first cell frame of the ME unit via an in-flow port (block 1000). A negatively conductive solution having a volume substantially less than the volume of the filtered brine solution, perhaps less than ten times that of the filtered brine solution, is applied to a catholyte compartment of a second cell frame of the ME unit via an in-flow port (block 1010). Generally concurrent to the supply of solutions, the electrodes associated with these compartments are energized to generate a current that forces the metals associated with hardness to migrate from the anolyte compartment through the membrane to the catholyte compartment (blocks 1020 and 1030). - Due to this migration and electrochemical decomposition (off-gassing) of water forming the filtered brine solution, an increased concentration of the brine solution is produced (block 1040). Hence, the filtered brine solution, substantially free of the hardness, can be reused for further regeneration of the ion exchange resin beds without disposal or further treatment (block 1050).
- VII. Brine Recovery/Water Desalination
- Referring to
FIG. 13 , an exemplary embodiment of EMS subsystem for water desalination and recycling of the brine solution for reuse is shown. Herein, feedwater 1100 with low overall quality (e.g., ground water, potable water, etc.) is supplied to one or more pre-filtration systems (e.g., micro-filter, ultra-filter, etc.) 1110. According to this embodiment of the invention, thepre-filtration system 1110 is designed to remove suspended solids and other organic material from thefeed water 1100. Thefiltrate 1120, namely the filtered feed water, is supplied to a membrane separation system 1130 (e.g., nano-filter, Reverse Osmosis, etc.) in order to remove one or more selected impurities (e.g., total dissolved solids). The membrane separation system 1130 produces apermeate 1140, which undergoes disinfection 1150 (e.g., ultraviolet light radiation, chlorination, etc.). This results inpurified water 1160. - During these operation, a
first reject solution 1170 and asecond reject solution 1175 are provided to theEMS subsystem 100 fromsystems 1110 and 1130, respectively. TheEMS subsystem 100 removes the impurities associated with thereject solutions EMS subsystem 100 provides a filtered,concentrated reject solution 1190 for disposal or recycling. - VIII. Brine Recovery/Removal of Bivalent Ion (Arsenic)
- Referring now to
FIG. 14 , an exemplary embodiment of a flowchart of the operations of theEMS subsystem 100 to recover the brine solution and remove an impurity, such as a bivalent anion (arsenic) for example, is shown. The brine solution is based on a monovalent aqueous salt solution, so that arsenate can be separated from the brine solution using selective membranes. - More specifically, the
EMS subsystem 100 is configured with an ED unit (block 1200). A contaminated brine solution with an elevated level of arsenate is feed into an anolyte compartment of the anode cell frame via an in-flow port of an anode cell frame (block 1210). A negatively conductive maintenance solution, having a volume substantially less in magnitude than the contaminated brine solution, is applied to an catholyte compartment of the ME unit via an in-flow port of an cathode cell frame (block 1220). - Generally concurrent to the supply of the contaminated brine and maintenance solutions, the electrodes associated with these compartments are energized to generate a current that forces monovalent salt ions of the brine solution to accumulate within the catholyte compartment through membrane migration (
blocks 1230 and 1240). Since arsenate is a bivalent ion, it will remain in the anolyte compartment and be output with the maintenance solution for waste treatment and/or disposal (block 1250). This filters the contaminated brine solution, and in combination with out-gassing, produces a filtered, concentrated brine solution for regeneration of ion exchange resin beds (block 1260). - While the invention has been described in terms of several embodiments, the invention should not be limited to only those embodiments described, but can be practiced with modification and alteration within the spirit and scope of the appended claims. The description is thus to be regarded as illustrative instead of limiting.
Claims (21)
1. A process system comprising:
an impurity separation subsystem to remove a selected impurity from a feed water and to produce a reject solution with an elevated level of the selected impurity and an output solution having a substantially reduced level of the impurity; and
an electrolytic membrane separation (EMS) subsystem in fluid communications with the impurity separation subsystem, the EMS subsystem to receive the reject solution from the impurity separation subsystem and an electrically conductive solution, to transfer the selected impurity to the conductive solution.
2. The process system of claim 1 , wherein the EMS subsystem further increases concentration of the reject solution for reuse.
3. The process system of claim 2 , wherein the impurity separation system is an ion exchange unit that comprises ion exchange resin that filter the selected impurity from the feed water.
4. The process system of claim 3 , wherein the reject solution is a brine solution used to regenerate the ion exchange resin.
5. The process system of claim 2 , wherein the reject solution is a diluted brine regenerate solution that achieves an increased concentration through off-gasing.
6. The process system of claim 1 , wherein the EMS subsystem further produces a diluate after removal of the selected impurity from the reject solution and outputs the diluate to a flow including the output solution.
7. The process system of claim 1 , wherein the EMS subsystem comprises
a first cell frame comprises an anolyte compartment to house an anode, the anolyte compartment comprises a first in-flow port and a first out-flow port;
a second cell frame having a catholyte compartment to house a cathode, the catholyte compartment comprises a second in-flow port and a second out-flow port; and
a membrane positioned between the anolyte compartment and the catholyte compartment.
8. The process system of claim 7 , wherein the conductive solution is supplied to the anolyte compartment of the EMS subsystem through the first in-flow port and the reject solution is supplied to the catholyte compartment of the EMS subsystem through the second in-flow port.
9. The process system of claim 8 , wherein the reject solution is a brine solution used to regenerate an ion exchange resin.
10. The process system of claim 9 , wherein the EMS subsystem produces a reusable brine solution after transfer of the selected impurity to the conductive solution for output from the second out-flow port and outputs the conductive solution with the selected impurities via the first out-flow port as waste.
11. The process system of claim 7 , wherein the conductive solution, being negatively conductive, is supplied to the catholyte compartment of the EMS subsystem through the second in-flow port and the reject solution is supplied to the anolyte compartment of the EMS subsystem through the first in-flow port.
12. The process system of claim 1 further comprising:
a pre-filtration system in fluid communications with the impurity separation system where the feed water is a filtrate being a filtered feed water.
13. An electrolytic membrane separation (EMS) subsystem comprising:
a first cell frame comprises an anolyte compartment to house an anode, the anolyte compartment comprises a first in-flow port and a first out-flow port positioned above said first in-flow port;
a second cell frame having a catholyte compartment to house a cathode, the catholyte compartment comprises a second in-flow port and a second out-flow port positioned above said second in-flow port; and
at least one membrane positioned between the anolyte compartment and the catholyte compartment,
wherein the EMS subsystem is adapted to (i) receive a brine solution, used to regenerate an ion exchange resin and having an elevated level of at least one type of impurity, into one compartment of the anolyte and catholyte compartments, (ii) receive a conductive solution having a volume substantially less than a volume of the brine solution into a different compartment than the compartment supplied with the brine solution, (iii) remove the at least one type of impurity from the brine solution, and (iii) produce a resulant brine solution that may be reused for regeneration of an ion exchange resin.
14. The EMS subsystem of claim 13 further producing a waste solution including the conductive solution having at least one type of impurity.
15. The EMS subsystem of claim 13 , wherein the catholyte compartment to receive the brine solution and the anolyte compartment to receive the conductive solution.
16. The method of claim 13 , wherein the anolyte compartment to receive the brine solution and the catholyte compartment to receive the conductive solution being negatively charged.
17. A method comprising:
providing an electrolytic membrane separation (EMS) subsystem that comprises a plurality of compartments each including an electrode being one or an anode and a cathode;
supplying a brine solution having a first volume and an increased level of an impurity to a first compartment of the plurality of compartments;
supplying a conductive solution to a second compartment of the plurality of compartments, the conductive solution having a second volume substantially less than the first volume; and
energizing the electrodes to cause ions associated with the impurity to migrate from the reject solution to the second compartment; and
outputting the conductive solution having the impurity as waste.
18. The method of claim 17 further comprising:
outputting a resultant brine solution for reuse in regenerating ion exchange resins.
19. The method of claim 18 further comprising:
off-gasing the brine solution as the impurity has been removed to produce the resultant brine solution.
20. The method of claim 17 , wherein the impurity comprises one of a monovalent ion and a heavy metal.
21. The method of claim 17 , wherein the impurity comprises one of a monovalent ion and a heavy metal.
Priority Applications (3)
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US10/763,691 US20050161343A1 (en) | 2004-01-22 | 2004-01-22 | Apparatus and method for brine separation and reuse |
US13/652,401 US9017538B2 (en) | 2004-01-22 | 2012-10-15 | Apparatus and method for brine separation and reuse |
US14/694,956 US9809470B1 (en) | 2004-01-22 | 2015-04-23 | System for brine separation and reuse |
Applications Claiming Priority (1)
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US10/763,691 US20050161343A1 (en) | 2004-01-22 | 2004-01-22 | Apparatus and method for brine separation and reuse |
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US13/652,401 Continuation US9017538B2 (en) | 2004-01-22 | 2012-10-15 | Apparatus and method for brine separation and reuse |
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US20050161343A1 true US20050161343A1 (en) | 2005-07-28 |
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US13/652,401 Expired - Lifetime US9017538B2 (en) | 2004-01-22 | 2012-10-15 | Apparatus and method for brine separation and reuse |
US14/694,956 Expired - Lifetime US9809470B1 (en) | 2004-01-22 | 2015-04-23 | System for brine separation and reuse |
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US13/652,401 Expired - Lifetime US9017538B2 (en) | 2004-01-22 | 2012-10-15 | Apparatus and method for brine separation and reuse |
US14/694,956 Expired - Lifetime US9809470B1 (en) | 2004-01-22 | 2015-04-23 | System for brine separation and reuse |
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Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2011133835A1 (en) * | 2010-04-22 | 2011-10-27 | Spraying Systems Co. | Electrolyzing system |
Families Citing this family (1)
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US20050161343A1 (en) * | 2004-01-22 | 2005-07-28 | Reinhard Fred P. | Apparatus and method for brine separation and reuse |
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US4880513A (en) * | 1986-06-20 | 1989-11-14 | The Graver Company | Method and apparatus for generating acid and base regenerants and the use thereof to regenerate ion-exchange resins |
US5225054A (en) * | 1992-03-02 | 1993-07-06 | Cominco Ltd. | Method for the recovery of cyanide from solutions |
US5352345A (en) * | 1991-05-07 | 1994-10-04 | Alliedsignal Inc. | Ion exchange resin regenerant waste recovery and recycling via bipolar membranes |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
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US3607694A (en) * | 1968-04-08 | 1971-09-21 | Sybron Corp | Per(halo-oxygen) acid oxidation,purification and recovery process |
US20050161343A1 (en) * | 2004-01-22 | 2005-07-28 | Reinhard Fred P. | Apparatus and method for brine separation and reuse |
-
2004
- 2004-01-22 US US10/763,691 patent/US20050161343A1/en not_active Abandoned
-
2012
- 2012-10-15 US US13/652,401 patent/US9017538B2/en not_active Expired - Lifetime
-
2015
- 2015-04-23 US US14/694,956 patent/US9809470B1/en not_active Expired - Lifetime
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
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US4880513A (en) * | 1986-06-20 | 1989-11-14 | The Graver Company | Method and apparatus for generating acid and base regenerants and the use thereof to regenerate ion-exchange resins |
US5352345A (en) * | 1991-05-07 | 1994-10-04 | Alliedsignal Inc. | Ion exchange resin regenerant waste recovery and recycling via bipolar membranes |
US5225054A (en) * | 1992-03-02 | 1993-07-06 | Cominco Ltd. | Method for the recovery of cyanide from solutions |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011133835A1 (en) * | 2010-04-22 | 2011-10-27 | Spraying Systems Co. | Electrolyzing system |
CN102947490A (en) * | 2010-04-22 | 2013-02-27 | 喷雾系统公司 | Electrolyzing system |
US8753489B2 (en) | 2010-04-22 | 2014-06-17 | Spraying Systems Co. | Electrolyzing system |
US9103043B2 (en) | 2010-04-22 | 2015-08-11 | Spraying Systems Co. | Electrolyzing system |
Also Published As
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US9017538B2 (en) | 2015-04-28 |
US9809470B1 (en) | 2017-11-07 |
US20130098756A1 (en) | 2013-04-25 |
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