US20220356101A1

US20220356101A1 - High salinity water purification processes and systems

Info

Publication number: US20220356101A1
Application number: US17/871,710
Authority: US
Inventors: Stephen M. Mosher
Original assignee: Aphinity Inc
Current assignee: Aphinity Inc
Priority date: 2018-12-10
Filing date: 2022-07-22
Publication date: 2022-11-10
Also published as: US20200180989A1; US11396468B2

Abstract

A high salinity water purification system and process, including a forward osmosis system and a reverse osmosis or nanofiltration system. A concentrated brine of a zinc or iron complex combined with a salt or acid draws pure water across the FO membrane from the influent water. The diluted brine is pumped through a vessel holding an anionic adsorption media to remove the zinc or iron complex and the resultant brine is passed through the RO or nanofiltration system to obtain purified water and a concentrated brine stream. The adsorption media is regenerated by a rinse cycle using fresh water or water from the RO system, removing the zinc or iron complex adhered to the media. The resultant brine is stored and mixed with the output of the RO system.

Description

CROSS-REFERENCE TO RELATED APPLICATION

This application claims priority of U.S Non-Provisional Application Ser. No. 16/706,601, filed Dec. 6, 2019, which in turn claimed the benefit of U.S. Provisional Application No. 62/777,602 filed Dec. 10, 2018, the entire contents of which applications are incorporated herein by this reference.

BACKGROUND

One of the greatest challenges in water treatment is addressing high levels of total dissolved solids (TDS) in water—basically: how to desalinate high TDS solutions. An emerging treatment technology is a process called “forward osmosis” (FO). This process differs from traditional reverse osmosis (RO). A traditional RO system pushes water at high pressure through a membrane that essentially filters out dissolved minerals and produces a clean water stream and a concentrated salt water stream. An FO system draws water across the membrane to purify it at a low pressure which reduces membrane fouling potential. With an RO, the higher the total dissolved solids of the water, the higher the pumping pressure required and subsequently higher capital and operating cost. The higher the overall total dissolved solids, the more complex and expensive the technical solution is.
One example of high TDS water is produced water, which is the water that comes from deep within the ground during the production of oil. As oil is brought out of the ground, water comes with it, which is thus called “produced water”. This water is very difficult to treat as it not only has high levels of suspended solids and organics which can blind filter media and membranes, the water is also extremely high in dissolved mineral salt content. Typically, the produced water is either hauled off site to a disposal well or directly injected back into the ground for disposal. Hauling the water is very costly and recent research indicates that injecting produced water back into injection wells can cause formation damage underground. For that reason, injection wells are being reduced as a possible solution for waste disposal. The best solution is to minimize the amount of water put back into the ground and utilize any good water for other industrial uses. Yet treating this water is extremely difficult.

BRIEF DESCRIPTION OF THE DRAWINGS

Features and advantages of the disclosure will readily be appreciated by persons skilled in the art from the following detailed description when read in conjunction with the drawing wherein:

FIG. 1 is a schematic diagram illustrating an exemplary embodiment of a high salinity water purification system and process.

FIG. 2 is a schematic diagram illustrating a second exemplary embodiment of a high salinity water purification system and process.

FIG. 3 is a schematic diagram illustrating a third exemplary embodiment of a high salinity water purification system and process.

FIG. 4 is a schematic diagram illustrating a fourth exemplary embodiment of a high salinity water purification system and process.

DETAILED DESCRIPTION

In the following detailed description and in the several figures of the drawing, like elements are identified with like reference numerals. The figures are not to scale, and relative feature sizes may be exaggerated for illustrative purposes.
Water naturally wants to be in a state of equilibrium with respect to mineral content. An FO system utilizes a high TDS brine stream with stronger osmotic attraction than a waste stream to pull or draw pure water from the waste stream across a semipermeable membrane into the high TDS brine which thus dilutes it. The osmosis process will naturally continue until the osmotic attraction of the two streams are approximately equivalent. The water that is pulled across the membrane and essentially dilutes the brine solution is then extracted from the brine in various traditional treatment technologies, most commonly reverse osmosis (RO) or nanofiltration. The pure water is produced in one stream from the RO and the other stream re-concentrates the brine solution which then becomes the feed water back to the FO membrane. The process is then repeated in a continual process.
The benefit of the FO system is the natural osmotic driving pressure is much lower than the pressure on a traditional RO membrane which minimizes the fouling potential and subsequently reduces operating and maintenance cost of the FO membrane system. A significant challenge with implementing a forward osmosis system is how to efficiently process and re-concentrate extremely high TDS brines. This application describes low cost, high efficiency methods of accomplishing high TDS brine draw re-concentration.
As noted above, the forward osmosis solution is highly advantageous because instead of pushing water across a membrane at high pressure which damages separation membranes (often beyond repair), FO “pulls or draws” pure water across the membrane at low pressure through natural osmosis and a brine solution which allows for easier and more effective membrane cleaning. This minimizes membrane fouling, whereas at high pressure RO membranes become fouled beyond repair. In the FO continual process, the pure water is produced and the concentrate stream from the RO system re-concentrates up the brine to continue pulling pure water across the FO membrane. However, in this FO brine recycling process, there are limitations as to how high a reverse osmosis system can re-concentrate the reject brine stream which limits how much water and what TDS of water an FO system can process. This new process technology advancement works in combination with the reverse osmosis system, or alternatively a nanofiltration system, to concentrate up the brine levels to even higher levels than ever possible (excluding use of high energy, high cost evaporators) which will help achieve greater water savings at a lower operating and capital cost. As is well known in the art, nanofiltration uses a different membrane than RO, with a different pore size to filter differently.
First Embodiment:
A two-step water purification system and process is illustrated in FIG. 1. This embodiment employs a strong anionic base adsorption media such as a resin or membrane to recycle a zinc or iron-based brine draw combined with a sodium or magnesium-based brine draw (or acid) before a high salinity reverse osmosis or nanofiltration system for improved brine draw recycling performance and overall higher efficiency. Zinc or iron-based brines are unique in that they naturally have an extremely high osmotic attraction which makes it beneficial as an FO brine draw. Zinc combined with a salt such as chloride can become “complexed” thus giving it a natural selective attraction/affinity to the adsorption media used in the purification process. This happens when the zinc or iron is in combination with a brine (sodium chloride as an example) or in combination with an acid such as hydrochloric acid. Either of these two conditions makes the zinc into the form that the adsorption media will adsorb it, as described more fully below. The brine is in sufficient concentration levels to complex the zinc or iron-based compound.
Zinc or iron-based brines are also unique in that there are anionic adsorption media with specific chemical affinity for zinc or iron-based brines. What makes this process even more unique is that the adsorption media rinse “elutant” for these specific adsorption media, e.g. a resin or membrane, is plain water as opposed to another brine, acid, or base chemical. This makes rinse/flush cost of the adsorption media solution extremely inexpensive and low energy.
In the following description of the first embodiment, zinc-based brines are specifically described. it will be understood that iron-based brines also provide similar properties, and may alternatively be used in the process.
The first step in processing the brine from the FO system is to separate the zinc-based brine from a sodium or magnesium-based brine, or acid (combined with pure water) using the adsorption media. The second step is to process the sodium or magnesium-based brine (or acid) by purifying it with a standard high salinity RO or nanofiltration system, thus producing clean water and a re-concentrated brine. This re-concentrated brine is then blended with the eluted zinc-based brine from the adsorption media rinse process. The combined brine solution is then fed back to the FO membrane and is used in a continual process.
The first step is done in a manner that uses a low-energy strong base anion exchange media (resin or membrane) and fresh water for the flush. Utilizing fresh water for rinse is a key factor because it is extremely low cost. There are many resins and membranes that can separate zinc from resin (and membranes), but the more zinc to be removed, the more flushing chemical needed which drives up operating cost significantly. The process of this embodiment by which the unique anionic media removes zinc involves the zinc-based brine being combined with another brine (or acid, such as HCl). This combined brine is in a multivalent form as opposed to a normal cationic phase, thus allowing the anionic adsorption media to have a strong natural attraction to it. This strong attraction binds or adheres the zinc to the anionic media. When the brine is removed from the media and the media goes into the rinse or backwash cycle with fresh water, the accompanying brine is flushed from the adsorption media which reverses the multivalency of the zinc-based brine, and thus the zinc-based brine is easily removed from the resin with just low total dissolved solids water. For this reason, the FO brine draw includes a blend of multiple brine solutions or the zinc-based brine is in combination with an acid (such as HCl).
This process utilizes a combined blend of brines or acid, to include zinc chloride, zinc bromide, ferric chloride, sodium chloride, sodium bromide, and or magnesium chloride as primary examples (also to include: LiCl, CaCl 2, LiCl and HCl, HCl, KCl, CsCl, NH 4Cl, and HONH 3Cl). The acid can be in solution with the zinc brine, but that is not necessary. Zinc chloride will attach to the adsorption media in the presence of an acid (such as HCl) or in the presence of another brine (such as NaCl). The acid would be in the brine or in place of the salt-based brine and consistent throughout the FO system. To recover the costly brine draw material and minimize waste, strong base anion adsorption media is used to first separate the zinc bromide or zinc chloride brine salts thus leaving the effluent solution as only pure water combined with the magnesium chloride, sodium bromide, or sodium chloride brine draw to be processed by the high salinity RO or nanofiltration system. The strong base anion adsorption media is flushed with clean, permeate water in a final step of the process.
Referring now to the schematic of FIG. 1, a storage tank 1 holds the influent water for the process, which is a moderate TDS fluid, in the range of 30,000 to 150,000 ppm. The process water 3 is pumped by pump 2 to provide a brine stream on the input side of FO membrane system 4. The output side of the FO membrane has a concentrated brine draw containing Zinc complex (or iron) and other salt brine. The concentrated brine draw is a high TDS fluid, in the range of 250,000 to 500,00 ppm. The high brine draw fluid draws pure water across the FO membrane, leaving a diluted brine draw, which did not pass through the FO membrane, containing the Zinc complex (or iron) and other salt brine. With pure water having been drawn out by the FO system, the process water leaving the FO system is a concentrated fluid, with a TDS in the range of 300,000 to 500,000 ppm. The concentrated process fluid 5 is waste from the process, to be hauled off-site or otherwise disposed of.
The diluted brine draw 6 from the FO process is pumped by pump 7 through vessel controls 23, including a valve system, to media vessels 8A, 8B holding a Zinc or iron complex adsorption media, e.g. a strong anionic base resin or membrane which has an extremely high osmotic attraction to the zinc or iron-based complexes in the diluted brine draw. The zinc or iron complex adheres to the adsorption media, separating the zinc bromide or zinc chloride so that the output 10 pumped from the vessels 8A, 8B by pump 9 is essentially free of the zinc or iron complex. This diluted brine draw 10 has NaCl, NaBr or MgCl2 (or acid) and is a moderate TDS fluid, on the order of 30,00 to 150,000 ppm.
One example of the adsorption media suitable for the purpose is Strong Base Anion, Gel Type 1, Quaternary Amine Functional Group, Styrene Crosslinked with Divinylbenzene, Chloride Form.
Zinc chloride when combined in solution with sodium (or magnesium) chloride brine will form a divalent anionic complex of [ZnCl4]2—which has a direct chemical “selective” affinity for strong base anion resin and membrane media. In this form, the Zinc complex will be adsorbed onto the media (resin or membrane) but allow other cations to pass and not be adsorbed on the media. The media is maintained in the chloride form, but with such high levels of chloride present in the subsequent brine (sodium or magnesium chloride brine), the chloride is not affected or exchanged. Just the zinc chloride complex is adsorbed to the resin or membrane media. The adsorption media, such as the resin, has selective attraction to various ions such as chloride, hydroxide, and hydrogen. When the resin goes through an ion exchange process, one ion is exchanged (ion to be removed) for the “ion form” (ion naturally on the resin). In this case, if there was “ion exchange”, chloride would be released into the water as the zinc was adsorbed. But since the brine has such a high concentration of chloride in the brine, e.g., at least 30,000 ppm, there is no release of the chloride. In this case, there is not technically “ion exchange;” there is no actual exchange of ions, just adsorption.
During the rinse or “flush” step of the resin to remove the zinc chloride complex from the resin or membrane, the sodium or magnesium chloride brine is flushed from the media tank, then RO permeate water fills the tank. This removal of the brine and replacement with low TDS water neutralizes the valency of the complex which reverses the adsorption process, thus zinc chloride complex sloughs off the resin and dissolves into the RO water. In the flush process, a minimal amount of RO water is utilized to maximize zinc chloride concentration in the solution to re-form a brine. This flushed product is then blended back with rejection brine from the high salinity RO system (sodium or magnesium chloride brine) which forms a blended high brine solution (zinc chloride and sodium or magnesium chloride). This then reestablishes the zinc chloride complex and thus the purification process can be repeated. The zinc chloride has a natural strong osmotic “draw” which makes it beneficial as a brine draw in the forward osmosis process. An important feature is the use of fresh water to neutralize the zinc chloride complex in a continual process with no required special rinse chemicals, significantly reducing the material costs in the process.
The diluted brine draw 10 is pumped from vessels 8A, 8B into a high salinity RO membrane system 11, with the fluid passed through the membrane constituting RO permeate water, essentially or relatively pure water. The relative percentage of RO permeate water recovered from the process water 3 is typically on the order of 50% to 80%.
The brine draw 12 from the RO system which did not pass through the RO membrane is a concentrated brine draw, a high TDS fluid with TDS 250,000 ppm. The brine draw 12 does not have zinc or iron), which had been removed by the adsorption media 8 in vessels 8A, 8B. The concentrated brine draw 12 is stored in brine storage tank 13, for mixing with zinc (or iron) flushed from the adsorption media during a rinse cycle. The storage tank may include a mixer and optional heat exchanger 14.
In this embodiment, a part 19 of the RO permeate water is used for rinse adsorption in a rinse cycle for the adsorption media 8 in vessels 8A, 8B. The RO permeate water used for this purpose is stored in tank 11 for use during the rinse cycle.
During the rinse cycle, the vessel 8A or 8B is isolated from the pumps 7 and 9 by valves of the vessel controls 23. The sodium or magnesium-based brine (or acid) is drained from the isolated vessel, either to the brine storage tank or pumped to the RO. Permeate product water 19 stored in tank 20 (or fresh water from another source) is released into and fills the isolated vessel through control valve 22, reversing the multivalent condition of the zinc (or iron) complex previously adsorbed onto the media in the isolated vessel. The media releases the zinc (or iron) brine which is dissolved back into the permeate water (or fresh or tap water). During the rinse cycle, the water released into the vessel 8A may be allowed to rest in contact with the media. An optional step is to recirculate the permeate water over the media to minimize water used in the process and increase zinc (or iron) concentration in solution. After the cycle is complete, with the zinc in solution in the water, the resulting brine is released from the isolated vessel by operation of vessel controls 26 (essentially a three-way valve) into tank 13 for mixing with the concentrated brine draw 12. Now, to revert to the purification mode for the system, valve 22 is closed, and vessel controls reconnect the pump 7 to the input of the isolated vessel and to pump 9, and pumps 2, 7, 9 and 15 are activated. The resulting brine 16 from tank 13 is a concentrated brine draw containing a Zinc or iron complex and other salts.
The zinc-based (or iron) removal media vessels 8A and 8B are designed to be in a “dual”, “twin”, or “multiple train” mode where one vessel is online and operational while the other vessel (s) is/are regenerated then put back into a “standby” ready-for-use condition. There is a continuous flow of zinc-based (or iron) concentrate waste from the rinse process thus the brine draw is optimally recycled.
The tank 13 may include a heat exchanger 14 for heating the brine if necessary, and a cooling heat exchanger 16 may be located downstream of the heat exchanger. The purpose of the cooling heat exchanger is to cool down the brine draw prior to entering the forward osmosis membrane to minimize mineral fouling on the forward osmosis membrane. This brine draw loop is a continuous processing loop with multiple pumps. The pumps build up heat over time, so a cooling step controls fluid temperature which in turn minimizes the potential for mineral scale fouling on the FO membrane.
To recover clean water from high brine or highly saline water streams such as sea water, manufacturing waste streams, produced water or fracturing flow back water, the high brine recovery or rinse system is implemented as noted above. The treatment technology described above splits out the pure water thus making it available for reuse and at the same time re-concentrates up the brine draw so the system works in a continuous low cost, high efficiency process. This is done in a manner that uses a low energy strong base anion adsorption media, such as a resin, and fresh water for resin rinse. Utilizing fresh water for rinsing is an important factor because it is extremely low cost.
There are many resins that can separate zinc from resin, but the more zinc to be removed, the more regeneration chemical needed which drives up operating cost significantly. Traditional cationic resins used for zinc removal would utilize so much rinse chemical that the process would be cost prohibitive. In the process described above regarding FIG. 1, the unique anionic resin removes zinc from the zinc-based brine which is combined with another brine (or acid, like HCl); in this form the brine is multivalent thus allowing the anionic resin to have an attraction to it. When the resin goes into the rinse cycle with fresh water, this flushes the accompanying brine from the resin which reverses the multivalency of the brine and thus the zinc-based brine is easily removed from the resin with just tap water. For this reason, it is important that the FO brine draw include or consist of a blend of multiple brine solutions blended together or be in combination with an acid (such as HCl). These are to include zinc chloride, zinc bromide, sodium chloride, and or magnesium chloride as examples (but not limited to). To recover the costly brine draw material and minimize waste, a strong base anion exchange resin is used to first separate the zinc bromide or zinc chloride brine salts thus leaving the effluent solution as only pure water combined with the magnesium chloride, sodium bromide, or sodium chloride brine draw to be processed by the high salinity reverse osmosis system. The strong base anion resin is regenerated with clean, permeate water from the final step of the process. The high salinity reverse osmosis (or nanofiltration) system is then used as the final processing step to produce permeate water for reuse at the same time producing a high total dissolved solids brine to be blended with the regenerant from the resin stage in the process.
Overall system recovery rate can be as high as 50-80% depending on the influent water quality and salt content, while net operating pressures are minimal due to low fouling factors and thus optimal energy efficiency (no evaporation process required).
This process has the potential to treat incoming water streams that are over 300,000 ppm TDS and extract pure water from the stream without using evaporative processes. This has yet to be achieved using any other technology outside of high energy cost, high operating cost, and high capital cost evaporator technologies.
Exemplary applications for the system and process include sea water desalination, mining waste water treatment, produced water and frac flow back treatment, industrial waste water recycling, food processing waste water recycling, brine concentration “weight up” processes, juice concentration food processing, and power plant effluent treatment.
Following is an equipment list for the system illustrated in FIG. 1:
Equipment Item List,: 1) Influent Storage water tank for primary feed water to the system; 2) Feed water pump; 3) Process water fed into FO membrane system; 4) Forward Osmosis membrane system; 5) Effluent Waste Rejection from the FO system; 6) Diluted Brine Draw containing Zinc Complex (or iron) and other brine salts (example sodium chloride, magnesium chloride); 7) Media pump to Anionic media 8) Adsorption media (resin or membrane) for Zinc complex; 8A, 8B) Vessels for holding the adsorption media; 9) RO Feed pump 10) Diluted Brine Draw with No Zinc or Iron Complex 11) High Salinity Reverse Osmosis system 12) Concentrated Brine Draw with sodium or magnesium chloride only (no zinc complex 13) Brine Storage and Mix tank 14) Zinc (or Iron) Chloride Brine from Brine Flush 15) Forward Osmosis pump; 16) Cooling Heat Exchanger; 17) Concentrated Brine draw containing both Zinc (or iron) chloride and sodium (or magnesium) chloride; 18) RO Permeate Water 19) RO Permeate Product Water for Adsorption Rinse; 20) Water Storage tank for RO permeate and Resin Flush; 21) Pump for Resin Rinse process to neutralize zinc chloride complex; 22) Control Valve; 23) Media Vessel Controls.
Second Embodiment.
FIG. 2 is a schematic diagram illustrating a second embodiment of a high salinity water purification system. This system employs a three-step brine draw recycling process. The process uses the combination of a strong anionic base adsorption ion resin or strong base anion adsorption membrane, sometimes referred to as “media,” in addition to a capacitive deionization system to recycle a zinc-based (or iron) brine draw combined with a sodium or magnesium-based brine draw (or acid) (which may include LiCl, CaCl 2, LiCl and HCl, HCl, KCl, CsCl, NH 4Cl, and HONH 3Cl). The brine draw is processed by a high salinity reverse osmosis system for improved brine draw recycling performance, overall higher efficiency, and lower operational cost.
The system and process of FIG. 2 differs from that of FIG. 1 in the rinse process. The purification cycle for the process of FIG. 2 is identical to that of the process of FIG. 1. The process of FIG. 2 utilizes an alternative adsorption media rinse.
The purpose of the capacitive deionization system is to further remove pure water and thus concentrate up the flushed zinc salts removed from the flushing/rinsing process. This process is used in lieu of an evaporator or heat exchanger to evaporate pure water off. Capacitive deionization is a more energy efficient method of removing pure water when compared to evaporator technologies.
The capacitive deionization system 30 (FIG. 2) works as follows. An aqueous stream containing dissolved solids (salt) is passed between two oppositely charged super capacitors (electric double layer capacitors, or EDLC). As the liquid passes through the dielectric spacer separating the capacitors, ions are attracted to the oppositely charged capacitor layers. The ions leave the water within the dielectric layer, pass through a charge specific membrane coating, and are adsorbed onto the surface area of the carbon super capacitor. When the capacitors have filled with ions, the polarity is reversed, and the ions are discharged back into the dielectric spacer and removed from the system. A 3-way valve is situated at the outlet of the device which directs the brine 32 away from the cleaned water 31.
Equipment Item List (items added to equipment of the embodiment of FIG. 1): 30) Capacitive Deionization System; 31) Capacitive Deionization Permeate; 32) Capacitive Deionization Concentrate Waste Containing Zinc chloride concentrate.
The first step in processing the brine in a rinse cycle is to separate the zinc-based brine from a sodium, magnesium-based brine, or acid (combined with pure water). After flushing with fresh, low TDS water (first step), the eluted brine is concentrated (second step) with the capacitive deionization system 30. The sodium or magnesium-based brine (or acid) is purified with a standard high salinity RO system, thus producing clean water and a re-concentrated brine. This re-concentrated brine is then blended with the eluted zinc-based brine from the media rinse and capacitive deionization processes. The combined brine solution is then fed back to the FO membrane and is used in a continual process.
The first step is done in a manner that uses a low-energy strong base anion exchange media (resin or membrane) and fresh water for the flush. This flushed brine from the offline media vessel 8A or 8B is then concentrated with the capacitive deionization (CD) system 30 to get maximum concentration from the zinc-based (or iron) brine. The CD permeate 31 is fed back to the vessel controls 23 for recycling. The CD concentrate is passed into the brine storage tank 13.
The high salinity reverse osmosis (or nanofiltration) system is then used as the final processing step to produce permeate water for reuse at the same time producing a high total dissolved solids brine to be blended with the capacitive deionization concentrate from the first media stage in the process. Overall system recovery rate can be as high as 50-80% depending on the influent water quality and salt content, while net operating pressures are minimal due to low fouling factors and thus optimal energy efficiency (no evaporation process required).
Third Embodiment.
FIG. 3 illustrates a further embodiment of a high salinity water purification system. This system is similar to that of FIG. 1 but incorporates two changes to enhance performance. A first change is that a caustic feed tank 24, feed line 25 and caustic chemical pump 32A are added, with a pH sensor 31 in water storage tank 20. A pH controller 30 is responsive to the pH sensor signal, to control the pump 32A to pump a caustic chemical stored in the feed tank to make the RO resin flush water “alkaline” and have a pH in the range of 9-12. Examples of the caustic include sodium hydroxide, potassium hydroxide, calcium hydroxide, calcium oxide, magnesium hydroxide, calcium carbonate, sodium carbonate, and ammonium carbonate. By slightly altering the pH of the rinse water, i.e. the RO water used to rinse the resin, this helps the zinc to release from the resin in higher concentration than just straight RO water alone, which makes the rinse water higher concentration. By raising the pH, the changing point in which the zinc chloride complex changes from anionic to cationic is altered. This allows the more rapid release of ions off of the resin which in turn increases the concentration in the rinse water.
A second change incorporated in the embodiment of FIG. 3 is the addition of acid feed tank 26, acid feed line 27, acid chemical pump 32B and pH sensor 29 in the brine storage tank 13. A pH controller is responsive to signals from the pH sensor 29 to control the acid chemical pump 32B to pump acid chemical from the tank 26 to the brine storage tank 13 as needed to control the pH of the brine in tank 13 to approximately the range 2.5 to 5.0. As the alkaline water from tank 20 flushes the adsorption media in tanks 8A, 8B, the water slowly turns acidic again. The pH of the brine in tank 13 may need to be slightly altered, by slightly lowering the pH so that the brine mixture becomes an anionic complex once again to that the process can be repeated. Examples of the acid chemical in the tank 26 include hydrochloric acid, sulfuric acid, phosphoric acid, muriatic acid, citric acid, sulfamic acid, carbonic acid and nitric acid.
By adding slight amounts of caustic to boost the pH of the rinse water to make it more alkaline releases the zinc in the rinse step more efficiently so the concentration is higher. The higher concentration of zinc chloride is addressed by adding a slight amount of acid to the brine in tank 13 to turn the brine mixture back to an anionic complex.
Fourth Embodiment.
FIG. 4 a further embodiment of a high salinity water purification system. This system is similar to that of FIG. 2 but incorporates the two changes to enhance performance described above with respect to FIG. 3. Thus, a caustic feed system is added to the system of FIG. 2 to add caustic as needed to the water in tank 20 to maintain the pH in the range of 9-12. The feed system includes the feed tank 24, pH controller 30, pump 32A, feed line 25 and pH sensor 31.
Similarly, an acid feed system has been added to control the pH of the brine in tank 13 to approximately 2.5 to 5.0. The acid feed system includes tank 26, pH controller 28, pH sensor 29, and acid feed line 27.
Although the foregoing has been a description and illustration of specific embodiments of the subject matter, various modifications and changes thereto can be made by persons skilled in the art without departing from the scope and spirit of the invention.

Claims

What is claimed is:

1. A system for purifying high salinity influent fluids, comprising:

a forward osmosis (FO) system comprising an FO membrane, an influent side input port and an influent side output port arranged on an influent side of the FO membrane, and an FO output side input port and an FO output side output port arranged on an output side of the FO membrane;

one or more vessels holding an anionic base adsorption media for removing zinc or iron complex from a brine;

a reverse osmosis (RO) or nanofiltration system;

the FO system configured to receive the influent fluid at the influent side input port and to pass concentrated fluid out the influent side output port;

the RO or nanofiltration system configured to receive input fluid at an input port and to pass concentrated fluid which did not pass through a membrane of the RO or through the nanofiltration system at an output port, and purified fluid which has passed through the RO membrane or nanofiltration system;

a recirculating brine flow path;

a concentrated brine draw containing zinc or iron complex and another salt brine or acid pumped into the FO output side input port, the concentrated brine draw having a level of total dissolved solids (TDS) higher than the TDS level in the influent fluid;

a pump for pumping the concentrated brine draw through the FO system from the FO output side input port to the FO output side output port, wherein pure water is drawn through the FO membrane to dilute the concentrated brine draw; the recirculating brine flow path passing from the FO output side output port to the one or more vessels to remove the zinc or iron complex from the diluted concentrated brine and to the RO or nanofiltration system and then to the FO output side input port, the diluted concentrated brine is in a multivalent form, allowing the anionic adsorption media to have a strong natural attraction to it; and

a rinse system for rinsing the adsorption media with an elutant containing water in a rinse cycle to remove the zinc or iron complex to form a resultant brine with zinc or iron complex, and then combining the resultant brine with the RO stream of concentrated brine draw to reconstitute a concentrated brine draw passed into the recirculating brine flow path to the FO output side input port.

2. The system of claim 1, wherein the rinse system comprises:

a brine storage tank in fluid communication with the one or more vessels;

an elutant source;

a valve system for passing elutant into one of the one or more vessels from the elutant source to rinse the adsorption media to remove the zinc or iron complex from the anionic adsorption media;

a brine storage tank for storing brine from the rinsing including the zinc or iron complex;

a mixer for mixing the stored brine with the concentrated fluid from the RO or nanofiltration system to pass into the brine recirculation path.

3. The system of claim 2, further comprising a cooling heat exchanger in the recirculating brine flow path downstream of the brink tank for cooling the brine draw prior to entering the FO membrane to reduce mineral fouling on the FO membrane.

4. The system of claim 2, further comprising:

a sensor for measuring the pH of the reconstituted brine draw;

an acid feed tank for storing an acid;

a pump for introducing acid from the tank into the reconstituted brine draw to control the pH of the reconstituted brine draw to approximately 2.5 to 5.0.

5. The system of claim 1, wherein the elutant is fresh water.

6. The system of claim 1, wherein the elutant is purified water from the RO or nanofiltration system.

7. The system of claim 1, wherein said one or more vessels comprises a plurality of vessels, and wherein one vessel is operational for passing the diluted brine draw over the anionic adsorption media while at least another of the plurality of vessels is in a rinse cycle or in a standby, ready-for-use condition.

8. The system of claim 1, further comprising:

a capacitive deionization system for processing the resultant brine to form a capacitive deionization permeate and a capacitive deionization concentrate;

the capacitive deionization permeate combined with the diluted brine draw prior to passing the diluted brine draw over the anionic adsorption media;

the capacitive deionization concentrate passed into a brine storage tank for combination with the concentrated brine draw.

9. The system of claim 1, further comprising:

an elutant tank holding the elutant; a caustic tank for holding a caustic;

a sensor for measuring the pH of the elutant stored in the elutant tank;

and a pump for introducing sufficient caustic from the caustic tank into the elutant tank to maintain the pH of the elutant in a range of 9 to 12.

10. The system of claim 1, wherein:

the influent fluid has levels of TDS in the range of 30,000 to 150,000 ppm; and

the concentrated brine draw has levels of TDS in the range of 250,000 to 500,000 ppm.

11. The system of claim 1, wherein the concentrated brine draw includes one or more of zinc chloride, zinc bromide, sodium chloride and magnesium chloride.

12. The system of claim 1, wherein the acid comprises one of hydrochloric acid, sulfuric acid, phosphoric acid, muriatic acid, citric acid, sulfamic acid, carbonic acid and nitric acid.