DESALINATION BRINE CONCENTRATION SYSTEM AND METHOD

Abstract

A system and method for producing very high concentration brine streams from which commercially efficiently obtained minerals may be obtained is produced by a dual membrane brine concentrator system (DTRI Concentrator). The system includes a nano-filtration system which removes divalent ions from the seawater, a brine concentrator such as a hollow fine fiber forward osmosis system which receives and further concentrates the brine rejected from the nano-filtration system, a SWRO system which receives the NF system permeate and removes monovalent ions, and another brine concentrator which further concentrates the brine rejected from SWRO system. Various permeate and reject brine flow may be forwarded through the Dual Membrane Brine Concentrator system, and multiple stages of the system components may be used, to enhance brine concentration and improve system efficiency.

Claims

1. A brine concentration system, comprising: a divalent ion concentration unit configured to receive a saline source fluid; a monovalent ion concentration unit; wherein the divalent ion concentration unit is configured to produce a concentrated divalent ion product stream and a reduced-concentration divalent ion stream, the monovalent ion concentration unit is configured to produce from the reduced-concentration divalent ion stream a concentrated monovalent ion product stream and a reduced-concentration monovalent product stream.

2. The brine concentration system of claim 1, wherein the monovalent ion concentration unit includes one or more reverse osmosis membrane units, and one or more monovalent ion concentration unit hollow fine fiber units downstream of the one or more reverse osmosis units, and at least one of the one or more monovalent ion concentration unit hollow fine fiber units receives from an upstream one of the one or more reverse osmosis units or an upstream one of the one or more monovalent ion concentration unit hollow fine fiber units a first portion of a monovalent ion concentration unit retentate stream at a shell side of the at least one of the one or more monovalent ion concentration unit hollow fine fiber units, and a second portion of the monovalent ion concentration unit retentate stream at a bore side of the at least one of the one or more monovalent ion concentration unit hollow fine fiber units, the first and second portions of the monovalent ion concentration unit retentate stream are proportioned to prevent a differential pressure between the shell side and the bore side of the at least one of the one or more monovalent ion concentration unit hollow fine fiber units from exceeding a predetermined monovalent ion concentration unit differential pressure limit.

3. The brine concentration system of claim 2, wherein the divalent ion concentration unit includes one or more nano-filtration units, and one or more divalent ion concentration unit hollow fine fiber units downstream of the one or more nano-filtration units, and at least one of the one or more divalent ion concentration unit hollow fine fiber units receives from an upstream one of the one or more nano-filtration units or an upstream one of the one or more divalent ion concentration unit hollow fine fiber units a first portion of a divalent ion concentration unit retentate stream at a shell side of the at least one of the one or more divalent ion concentration unit hollow fine fiber units, and a second portion of the divalent ion concentration unit retentate stream at a bore side of the at least one of the one or more divalent ion concentration unit hollow fine fiber units, the first and second portions of the divalent ion concentration unit retentate stream being proportioned to prevent a differential pressure between the shell side and the bore side of the at least one of the one or more divalent ion concentration unit hollow fine fiber units from exceeding a predetermined divalent ion concentration unit differential pressure limit.

4. The brine concentration system of claim 1, wherein a total dissolved solids concentration of the first concentrated product stream is greater than 80,000 ppm, and

5. The brine concentration system of claim 1, wherein a total dissolved solids concentration of the second concentrated product stream is greater than 120,000 ppm.

6. The brine concentration system of claim 1, wherein a recovery of the brine concentration system is at least 60%.

7. The brine concentration system of claim 1, wherein a specific power consumption of the brine concentration system is less than 5 kWh/m.sup.3.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0033] FIG. 1 is a schematic illustration of a typical seawater reverse osmosis system.

[0034] FIG. 2 is a schematic illustration of a typical nano-filtration—seawater reverse osmosis system.

[0035] FIG. 3 is a schematic illustration of an embodiment of a dual nano-filtration—reverse osmosis brine concentration system in accordance with the present invention.

[0036] FIG. 4 is a schematic illustration of another embodiment of a dual nano-filtration—reverse osmosis brine concentration system in accordance with the present invention.

DETAILED DESCRIPTION

[0037] FIG. 3 schematically shows the features of an embodiment of a dual nano-filtration—reverse osmosis brine concentration system in accordance with the present invention. The dual NF-SWRO brine concentration system 300 includes a nano-filtration system 310 and a two-stage reverse osmosis system with a first membrane unit 320 and a second membrane unit 321.

[0038] In the NF portion in this embodiment of brine concentration system 300, there is further an NF-side hollow fine fiber-forward osmosis unit 311, a NF inlet pump 312 that increases the pressure of the source seawater stream 313 being fed to inlet 314 of the NF system 310, and a NF-side energy recovery device 315 (e.g., a pump) that recovers pressure energy from the concentrated NF brine reject product stream 316 emitted from the HFF unit shell-side outlet 317.

[0039] In the SWRO portion of brine concentration system 300, there is an SWRO inlet pump 322, a first stage hollow fine filter-forward osmosis unit 323, a second stage hollow fine filter-forward osmosis unit 324, an SWRO-side energy recovery pump 325, and two intermediate pumps 326, 327.

[0040] The following provides a description of the operation of the FIG. 3 embodiment, using approximate numerical values that are provided solely for illustrative purposes, recognizing that the details of a specific installation of a facility incorporating this novel dual nano-filtration—reverse osmosis brine concentration system, as well as the desired qualities of both the product water and the highly concentrated reject brine streams, will drive the actual system operating parameters. Variables that may affect the system operating parameters include the salinity level of the source seawater, the ambient temperature of the source seawater, the temperature of the ambient environment to which process heat is rejected, etc. Note that due to rounding, numbers such as mass flows may not sum to 100% from the beginning to the end of the operations.

[0041] The source seawater 313 in this embodiment is assumed to have a TDS concentration of 42,000 ppm and a temperature of 25 ° C. Pump 312 raises the pressure of the seawater to approximately 15 Bars at a flow rate of approximately 11.5 tons/hour, and passes the pressurized seawater via inlet 314 to NF system 310's brine side 318. The NF system 310 in this example provides approximately 75% recovery, with the lower-concentration stream 331 from the permeate side 319 of the NF system 310 being produced at a rate of approximately 8.6 tons/hour at a TDS concentration of approximately 33,600 ppm, and the divalent-ion-rich rejected brine stream 332 leaving the brine side of the NF system 310 at a rate of approximately 2.9 tons/hour at a TDS concentration of approximately 67,000 ppm.

[0042] The majority of the NF reject brine stream 332 has its post-NF system pressure of approximately 13 Bar increased by an intermediate pump 333 to approximately 60 Bar before the stream is feed to the inlet 334 of the shell side of the HFF-FO unit 311. As small portion 335 of the NF reject brine stream 332 (in this example, approximately 7%) is also fed to the bore side of the HFF-FO unit 311, in this example at a rate of approximately 0.2 tons/hour, to limit the differential pressure between the shell and bore sides to minimize the potential for membrane failure.

[0043] The output of the NF-side HFF-FO unit 311 includes a lower concentration flow 336 at approximately 19,000 ppm at a rate of approximately 0.7 tons/hour, and the highly concentrated, divalent ion-rich NF-side HFF-FO reject product stream 316 at approximately 83,000 ppm at a rate of approximately 2.2 tons/hour. The lower concentration flow 336 in this embodiment is blended with and further lowers the concentration of the NF system's lower-concentration stream 331 (i.e., 19,000 ppm fluid diluting the 33,600 ppm fluid in stream 331) prior to entry into the SWRO side of the NF-SWRO brine concentration system 300. The NF-side HFF-FO brine reject product stream 316, still having a pressure of approximately 59 Bars, releases a portion of its energy in the NF energy recovery device 315. With an energy recovery efficiency on the order of 80%, the energy recovery device 315 may return several kW for further use. The final product 337 of this portion of the NF-SWRO brine concentration system 300, is released with its pressure lowered to approximately 2 Bars for further processing, such as divalent mineral extraction.

[0044] On the SWRO side of the NF-SWRO brine concentration system 300, the SWRO inlet pump 322 receives the diluted stream 331 at a rate of approximately 9.3 tons/hour and at approximately 32,500 ppm, and raised the pressure of the stream to approximately 69 Bars. This SWRO inlet stream 340 then enters the inlet of the brine side of the first stage 320 of the SWRO system. Because the saline water being fed to the SWRO system has a significantly lower TDS, it is possible to increase the recovery of SWRO system to 55% or more.

[0045] At a net driving pressure (NDP) of approximately 30 Bars, the SWRO first stage 320 operates at approximately 58% recovery, producing relatively low pressure (approximately 2 Bar) permeate 341 with a TDS concentration of less than 300 ppm at a rate of approximately 5.4 tons/hour, and an SWRO brine reject stream 342 of approximately 78,000 ppm at a rate of approximately 3.9 tons per hour at approximately 68 Bars.

[0046] The reject brine stream 342 from the SWRO first stage 320 is then fed to the SWRO second stage unit 321, via an intermediate pump 327 which increases the stream pressure to approximately 80 Bar. The second reverse osmosis stage, operating at 20% recovery, generates permeate water product 343 at the rate of approximately 0.8 tons/hour. With a TDS concentration below 300 ppm, this product water 343 may be combined with the similar-concentration product water 341 from the SWRO first stage 320.

[0047] The now monovalent ion-rich SWRO reject brine stream 344 emerges from the SWRO second stage 321 with a TDS concentration of approximately 97,000 ppm at a rate of approximately 3.1 tons/hour at approximately 79 Bars. The majority of the reject brine stream 344 enters the shell side of first stage countercurrent HFF-FO unit 323, while a small portion 345 (approximately 0.2 tons/hour) is injected into the bore side to offset the shell-side pressure to avoid membrane rupture. Operating at approximately 17% recovery, the SWRO first stage HFF-FO unit 323 generates a bore-side stream 346 with a TDS concentration of approximately 32,500 ppm at approximately 0.7 tons/hour. In this example the operating parameters of the SWRO HFF-FO unit 323 (e.g., NDP) have been adjusted so that the concentration of the bore-side stream 346 is approximately the same as the concentration of the stream entering SWRO inlet pump 322.

[0048] The HFF-FO first stage unit 323 also generates a higher-concentration brine stream 347 at approximately 117,000 ppm at a rate of 2.4 tons/hour. As with the first stage, the majority of the brine stream 347 is fed into the shell side of the HFF-FO second stage unit 324, with a small portion 348 (approximately 0.7 tons/hour) being fed into the bore side to provide the desired counter-pressure. The second stage 324, operating with approximately 21% recovery, generates a bore-side outlet stream 349 with a TDS concentration of approximately 78,000 ppm at a rate of approximately 1.0 ton/hour. In this embodiment, the HFF-FO second stage bore-side outlet stream 349 is returned via intermediate pump 326 to the brine stream 342 flowing from the SWRO first stage 320 to SWRO second stage 321. As with the HFF-FO first stage 323, the operating parameters of the HFF-FO second stage unit 324 are adjusted such that the concentration of the outlet stream 349 is approximately the same as the brine stream passing between the SWRO stages.

[0049] The HFF-FO second stage unit 324 also outputs the highly-concentrated, monovalent ion-rich reject brine stream 350 at approximately 1.3 tons/hour at approximately 147,500 ppm TDS concentration and approximately 78 Bars. The reject brine stream 350 then passes through SWRO energy recovery device 325 to recover approximately 2.8 kW before rejecting the monovalent-rich stream 338 at approximately 2 Bars for further processing, such as monovalent mineral extraction. Moreover, even if not used for any other purpose, the highly concentrated brine has over two times smaller volume than the SWRO brine in a typical conventional SWRO process, such as that in FIG. 1, and this stream may be processed through a crystallizer system to convert the highly concentrated brine into a disposable solid residue, thereby providing a system with zero liquid discharge to the environment.

[0050] The number of SWRO stages and the number of HFF FO brine concentration stages may be varied depending on the TDS concentration and mineral content of the saline source water and the desired final TDS level of the concentrated brine. Also, the foregoing numerical examples will vary depending on the actual facility design, and use of features such as recycling flow, which provides steady-state operating numbers that are slightly different than in a first cycle.

[0051] Another embodiment of the present invention is illustrated in FIG. 4. In this embodiment, the primary components and flows of the NF-SWRO brine concentration system 400 are generally as in the FIG. 3 embodiment. However, in FIG. 4 rather than using a NF-side HFF-FO unit 311, a reverse osmosis unit 411 further concentrates the reject brine stream 432 from the NF system 410. Because the resulting permeate stream 436 from the RO unit 411 has a substantially lower TDS concentration (less than 1000 ppm) as compared to the NF-side HFF-FO unit 311's permeate stream 336 (approximately 19,000 ppm), the stream 436 is not combined with the NF system's lower concentration stream 431 as in the FIG. 3 embodiment, but instead is routed outside of the NF-SWRO brine concentration system 400 for use in other applications and/or further processing, for example, to further lower its sub-1000 ppm TDS concentration.

[0052] As demonstrated in the foregoing example embodiments, the DTRI concentrator of present invention allows the reverse osmosis system recovery level to be significantly increased, as well as increasing energy savings and at the same time yielding a useful byproduct production, while not exceeding the commercially-available membranes' typical burst pressures. Comparison of examples of SWRO, NR-SWRO and the present invention's system shows improvements in recovery, with an example DTRI Concentrator achieving recovery of 61.5% as compared to 50% for SWRO and 45% for NF-SWRO systems, and specific power consumption of 4.5 kWh/m.sup.3 of product water, as compared to conventional brine concentrators which typically use 15-25 kWh/m.sup.3.

[0053] Although 83 Bars is assumed as a bursting pressure in this example embodiment, membrane products having higher bursting pressure (in some cases, up to 120 Bars) may be used in the present invention, with appropriate adjustment of the system operating parameters, as long as the osmotic pressure difference on the two sides of the membranes is maintained below the bursting pressure.

[0054] The present invention is not limited to solely to systems having a nano-filtration unit to receive the saline source water, as long as the alternative to the nano-filtration unit provides for selective removal of at least some of the divalent ions from the source seawater before separation in a SWRO membrane unit. For example, the present invention includes a system that does not have NF membrane treatment of the saline source water, but instead has an HFF FO concentrator, optionally with chemical treatment if needed. Similarly, a brackish water reverse osmosis (BWRO) system may be used instead of a NF unit to provide selective ion removal prior to SWRO processing.

[0055] The processing of the nano-filtration retentate discharge may also be provided by alternative concentration processes, such as use of HFF-FO in concurrent and/or counter-current flow patterns, use of HFF-RO units that also generate a low concentration (e.g., less than 1000 ppm) permeate fresh water product, and/or use of other types of membranes to further concentrate the nano-filtration retentate discharge stream.

[0056] On the SWRO side of the system, the SWRO retentate concentration portion may include multiple concentration stages (e.g., 1-5 stages of HFF and/or other types of concentrators that are effective at concentrating a monovalent ion discharge stream). depending on, for example, a particular installation's saline source water TDS, the TDS to be fed to the SWRO unit(s), or the target concentrated brine product TDS.

[0057] It is also possible to provide alternative routings of permeate from the hollow fine fiber units, with the separation performance of the individual hollow fine fiber units being adjusted as needed to ensure their respective permeate streams have a TDS concentration that is relatively close to that of the feed stream to which they are being routed. For example, in the FIG. 3 embodiment, the first stage HFF-FO unit 323 may be operated so that its permeate has a concentration altered from 32,500 ppm to around 78,000 ppm to make this permeate suitable for feeding to the reverse osmosis second stage membrane unit 321 instead of the reverse osmosis first stage membrane unit 320.

[0058] In addition to recovery of minerals and other byproducts from the concentrated products, the products may themselves be further processed for other purposes and/or used subsequently in other processes. For example, the highly concentrated product(s) may be processed through a crystallizer in order to achieve a zero liquid discharge system. Alternatively, the minerals contained in the divalent ion-rich product from the nano-filtration side of the present dual brine concentration system may be used in further post-generation treatment of the desalinated water produced by the present invention.

[0059] The foregoing disclosure has been set forth merely to illustrate the invention and is not intended to be limiting. Because such modifications of the disclosed embodiments incorporating the spirit and substance of the invention may occur to persons skilled in the art, the invention should be construed to include everything within the scope of the appended claims and equivalents thereof.

[0060] Listing of Reference Labels:

[0061] 1 SWRO system

[0062] 2 seawater

[0063] 3 pump

[0064] 4 RO inlet

[0065] 5 RO system

[0066] 6 RO product outlet

[0067] 7 product water

[0068] 8 RO reject brine outlet

[0069] 9 concentrated brine

[0070] 10 energy recovery device

[0071] 11 nano-filtration system

[0072] 12 seawater

[0073] 13 pump

[0074] 14 nano-filtration unit

[0075] 15 reduced-concentration outlet fluid

[0076] 16 nano-filter byproduct brine

[0077] 17 pump

[0078] 18 container

[0079] 19 inlet

[0080] 20 outlet

[0081] 21 product water

[0082] 22 concentration side output

[0083] 23 reject brine stream

[0084] 24 energy recovery device

[0085] 300 NF-SWRO brine concentration system

[0086] 310 nano-filtration system

[0087] 311 NF-side hollow fine fiber-forward osmosis unit

[0088] 312 NF inlet pump 312

[0089] 313 seawater stream

[0090] 314 NF inlet

[0091] 315 NF-side energy recovery device

[0092] 316 NF-side HFF-FO brine reject product stream

[0093] 317 HFF unit shell-side outlet

[0094] 318 NF system brine side

[0095] 319 NF system permeate side

[0096] 320 reverse osmosis first stage membrane unit

[0097] 321 reverse osmosis second stage membrane unit

[0098] 322 SWRO inlet pump

[0099] 323 first stage hollow fine filter-forward osmosis unit

[0100] 324 second stage hollow fine filter-forward osmosis unit

[0101] 325 SWRO-side energy recovery pump 325

[0102] 326 intermediate pump

[0103] 327 intermediate pump

[0104] 331 lower-concentration stream

[0105] 332 reject brine stream

[0106] 333 intermediate pump

[0107] 334 HFF-FO unit shell side inlet

[0108] 335 portion of reject brine stream

[0109] 336 NF-side HFF-FO unit lower concentration flow

[0110] 337 NF-side brine concentration system product

[0111] 338 SWRO-side brine concentration system product

[0112] 340 SWRO inlet stream

[0113] 341 permeate product water

[0114] 342 SWRO brine reject stream

[0115] 343 permeate water product

[0116] 344 SWRO reject brine stream

[0117] 345 portion of reject brine stream

[0118] 346 bore-side stream

[0119] 347 higher-concentration brine stream

[0120] 348 portion of higher-concentration brine stream

[0121] 349 HFF-FO second stage bore-side outlet stream

[0122] 350 monovalent ion-rich reject brine stream

[0123] 400 NF-SWRO brine concentration system 400

[0124] 411 reverse osmosis unit

[0125] 431 NF system lower concentration stream

[0126] 432 reject brine stream

[0127] 436 permeate stream