Process for water treatment

Abstract

The present disclosure generally relates to processes of water treatment, including saline water desalination and brine electrodialysis.

Description

PROCESS FOR WATER TREATMENTTECHNICAL FIELD

[0001] The present disclosure generally relates to processes of water treatment, including saline water desalination and brine electrodialysis.BACKGROUND

[0002] Climate change, severe droughts and population growth have led to water shortages in many regions. In an effort to develop alternative water resources, a variety of technologies have been explored including greywater recycling, water reclamation and reuse, and seawater desalination.

[0003] Desalination can be achieved through various techniques including distillation, reverse osmosis, nanofiltration, and electrodialysis. Distillation is one of oldest and most widely used processes in desalination. It involves heating saline water to generate steam and then condensing the steam back into liquid form. A variety of techniques can be used for heating saline water including solar distillation, natural evaporation, vacuum distillation, multi-stage flash distillation, multiple-effect distillation, and vapor-compression distillation. However, these processes typically utilize enormous amounts of energy and are therefore economically unfavorable.

[0004] Osmosis-based desalination is the leading process in desalination. This process exists primarily as Sea Water Reverse Osmosis (SWRO) desalination. The Reverse Osmosis (RO) process utilizes semi-permeable membranes and it involves the application of pressure to induce water permeation through the membranes while retaining the undesired salts in the retentate. High-pressure pumping of the seawater is required in order to pressurize the seawater through the membranes thereby overcoming the osmotic pressure and facilitating the flow of water through the RO membranes. Common types of RO membranes include Cellulose Acetate (CA) membranes, Thin Film Composite (TFC) membranes, Polyamide (PA) membranes, and Hollow Fiber membranes. Water subjected to RO processes can also undergo pre-treatment prior to RO and / or post- treatment following RO. Pre-treatment may include steps such as removal of colloids from the feedwater, addition of chemicals such as anti-scalants to prevent scaling and fouling on the membranes, and filtration of seawater to remove smaller suspended particles. Post- treatmentmay include pH adjustment, disinfection and remineralization of the treated water to ensure that it meets quality standards and requirements.

[0005] US 2005 / 0098499 describes a process for treating water containing dissolved salts selected from the group consisting of calcium sulfate, calcium chloride, magnesium sulfate, magnesium chloride, sodium carbonate, sodium chloride, sodium sulfate, calcium carbonate, and mixtures thereof comprising: (a) adding to said water about 0.1 to about 60 g / L of a compound selected from the group consisting of sodium hydroxide, sodium carbonate, potassium hydroxide, potassium carbonate, calcium hydroxide, calcium carbonate, aluminum hydroxide, aluminum sulfate, aluminum potassium sulfate, and mixtures thereof, whereby a precipitate forms in said water; (b) separating said precipitate from said water; and (c) desalinating said water.

[0006] A key limitation of SWRO desalination is the high boron concentration found in desalinated water which may confer toxicity risks and harmful effects on plants and humans. For example, boron levels as low as 0.3 mg / L have been found to cause toxicity symptoms in commercial crops such as reduced root growth, inhibited photosynthesis, and low chlorophyll levels in plant leaves (Yermiyahu, Science 2007, 318, 920-921).

[0007] There exists a wide disparity in boron levels of freshwater sources (0.02 to 0.2 mg / L) and seawater (4 to 6 mg / L). In the Mediterranean Sea, boron concentration has been measured to be as high as 9.6 mg / L (Argust, Biological Trace Element Research 66 (1998) 131-143). In seawater, boron exists primarily as boric acid, which easily permeates through the RO membranes during the RO process. For efficient boron removal, a multiple-pass configuration involving increasing the pH of the RO permeate obtained from the first pass is typically required in order to convert boric acid to borate ions that are characterized by increased diameter thereby enabling their rejection by the RO membranes. However, utilization of the “second pass” or “boron pass” involves significantly high energy and capital costs and it also reduces the overall product water of the desalination plant.

[0008] Alternative processes for reducing boron levels include various modifications of the RO membranes to better capture boron species. For example, the incorporation of UiO-66 into the RO membrane was shown to create a highly porous structure which resulted in a 11% increase in boron removal (Liu et al., J. Memb. Sci. 2019, 580, 101-109). Shultz et al. (Desalination 2018, 431, 66-72) described in-situ modification of the RO membranes with decylamine and dodecylamine thereby achieving 2-4 fold reduction in the level of permeated boron. Tu et al. (Desalination 2013, 310, 115-121) disclosed the addition of polyols includingglycerol, mannitol, or sorbitol to the RO feed solution and Dydo et al. (Desalination 2014, 334 (1), 39-45) disclosed the use of D-mannitol to form boron-D-mannitol complexes under specified conditions.

[0009] The principle of electrodialysis (ED) desalination was first presented in 1890 by Maigrot and Sabates, and its development into industrial scale started for more than 50 years ago. The operation of ED is driven by the development of ion exchange membranes produces high water recovery and does not require phase change, reaction, or chemicals. These advantages provide environmental benefits without the use of fossil fuels and chemical detergents. Whilst there are a number of reviews that have attempted to optimise ED performance for various applications, ED technology still has limitations involving scaling, membrane fouling, and permselectivity. Al-Amshawee et al. (Electrodialysis desalination for water and wastewater: A review, Chemical Engineering Journal, Volume 380, 2020, 122231, ISSN 1385-8947) review the principles of ED desalination.

[0010] Electrodialysis reversal desalination, commonly abbreviated EDR, is a water desalination process in which electricity is applied to electrodes to pull naturally occurring dissolved salts through an ion exchange membrane to separate the water from the salts. US 2011 / 0210069 discloses a water treatment process comprising: providing a membrane desalination unit: providing a first conduit connected with the membrane desalination unit and configured to transport a first stream of feed water to the membrane desalination unit; providing a second conduit connected with the membrane desalination unit and configured to transport a first stream of product water of lower salinity than the first stream of feed water out of the membrane desalination unit; providing an electrical separation unit; providing a third conduit connected with the membrane desalination unit and the electrical separation unit and configured to transport a first stream of reject water of higher salinity than the first stream of feed water from the membrane desalination unit to the electrical separation unit; providing a fourth conduit connected with the electrical separation unit and configured to transport a second stream of product water of lower salinity than the first stream of reject water out from the electrical separation unit; providing a precipitation unit; providing a fifth conduit connected with the precipitation unit and the electrical separation unit and configured to transport a second stream of reject water of higher salinity than the first stream of reject water from the electri cal separation unit to the precipitation unit; providing a sixth conduit connected with the precipitation unit and the electrical separation unit and configured to transport a second stream of feed water of lower salinity than the second stream of reject water from the precipitation unit to the electricalseparation unit; providing a seventh conduit connected with the precipitation unit and configured to release a discharge stream of water; and providing a chemical injection unit in communication with at least one of the electrical separation unit and the precipitation unit, wherein the membrane desalination unit comprises a nanofiltration membrane device or a reverse osmosis membrane device and wherein the electrical separation unit comprises an electrodialysis reversal desalination device or a super-capacitive desalination device.

[0011] As through known water desalination processes the inlet water (e.g., seawater) is separated into drinkable water and salt-concentrated brine, one of the drawbacks of the existing processes relates to the disposal of brine. Specifically, as it is typically not further used, its disposal involves both pollution and high cost.

[0012] There remains an unmet need for processes of obtaining desalinated water from seawater sources, which minimize the pollution associated therewith.

[0013] There also remains an unmet need for processes of obtaining desalinated water from seawater sources with reduced levels of boron species that is suitable for plant irrigation and / or human consumption.SUMMARY OF THE INVENTION

[0014] The present invention is directed to systems and processes for water desalination. The present invention is further directed to systems and processes for desalination of water, for example seawater, which provide efficient removal of undesired boron species, efficient exploitation of resources and minimization of waste.

[0015] Disclosed herein for the first time is a process for obtaining desalinated water with reduced amounts of boron species by (a) pre-treatment of the water entering desalination and (b) recycling of side products of both the desalination process and the pre-treatment process. Advantageously, the pre-treatment of prior to desalination enables enhanced boron rejection in the first pass of Reverse Osmosis (RO) desalination while retaining process resilience to carbonate scale and process stability. The process of the present invention affords considerable chemical and energy savings, while producing minimal by products and residues which are recovered and recycled back into the process. The process of the present invention is therefore economically advantageous saving both capital expenditure (CAPEX) and operational expenditure (OPEX) and environmentally beneficial.

[0016] According to some embodiments, there is provided a process for desalinating saline water, the process comprising the steps of:(I) providing saline water comprising carbonated species selected from the group consisting of: CO2, H2CO3, HCO3- , CO32and a combination thereof, and NaCl;(II) admixing a carbonated species chelator with the saline water of step (I) to form a CaCO3precipitate and decarbonated water;(III) separating the CaCO3precipitate of step (II) from the decarbonated water;(IV) desalinating the decarbonated water of step (III) to form desalinated water and brine, wherein the brine comprises NaCl;(V) performing an electrodialysis of the brine of step (IV) to form an acidic solution of HC1 and a basic solution of NaOH; and(VI) performing step (Via), step (VIb), or both, wherein step (Via) comprises contacting the HC1 formed in step (V) with at least a portion of the separated CaCO3precipitate of step (III) to form CaCl2and CO2; and wherein step (VIb) comprises repeating steps (I) to (IV) in a consecutive cycle, by using the NaOH formed in step (V) as the carbonated species chelator of a consecutive step (II).

[0017] According to some embodiments, the saline water is seawater or brackish water.

[0018] According to some embodiments, the saline water is seawater.

[0019] According to some embodiments, the saline water of step (I) has a saline water NaCl concentration, the desalinated water has a desalinated water NaCl concentration and the brine has brine NaCl concentration, wherein the saline water NaCl concentration is higher than the desalinated water NaCl concentration and lower than the brine NaCl concentration.

[0020] According to some embodiments, the saline water of step (I) further comprises Ca+2cations; the saline water of step (I) is supplemented with Ca+2ions by addition of soluble Calcium salt; and / or the carbonated species chelator of step (II) comprises Ca+2cations..

[0021] According to some embodiments, the admixing of step (II) entails forming CO3'2anions, and wherein the CaCO3precipitate is formed upon ion pairing of the Ca+2cations and said CO32anions.

[0022] According to some embodiments, the saline water of step (I) comprises Ca+2cations.

[0023] According to some embodiments, the carbonated species chelator of step (II) comprises NaOH.

[0024] According to some embodiments, the saline water of step (I) comprises at least one of: CO2, H2CO3, and HCO3‘.

[0025] According to some embodiments, the saline water of step (I) comprises Ca+2cations, wherein the carbonated species chelator of step (II) comprises NaOH, and wherein the admixing of saline water with the NaOH in step (II) entails carrying out one or more of the following chemical reactions:Ca+2+ CO2+ 2NaOH CaCO3+ 2Na++ H2O;Ca+2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2Na+;Ca+2+ HCO3- + NaOH CaCO3+ H2O + Na+, thereby producing CaCO3as a solid water-insoluble precipitate and decarbonated water suitable for subsequent desalination.

[0026] According to some embodiments, the process comprises step (Via).

[0027] According to some embodiments, the process further comprises a step of isolating the CaCl2formed in step (Via).

[0028] According to some embodiments, the process further comprises a step of isolating and storing the CaCl2formed in step (Via).

[0029] According to some embodiments, the process further comprises a step of storing at least a portion of the CaCl2formed in step (Via); and / or supplementing the saline water of step (I) with a portion of the CaCl2formed in step (Via) to increase a concentration of Ca+2ions therein. According to some embodiments, the process further comprises a step of storing at least a portion of the CaCl2formed in step (Via). According to some embodiments, the process further comprises supplementing the saline water of step (I) with a portion of the CaCl2formed in step (Via) to increase a concentration of Ca+2ions therein.

[0030] According to some embodiments, the process further comprises a step of isolating and storing the CO2formed in step (Via) thereby achieving Carbon Capture and Storage (CCS) or carbon removal.

[0031] According to some embodiments, the process comprises step (VIb).

[0032] According to some embodiments, the saline water of step (I) further comprises Ca+2cations or step (I) further comprises supplementing the saline water with Ca+2cations. According to some embodiments, the saline water of step (I) further comprises Ca+2cations. According to some embodiments, step (I) further comprises supplementing the saline water with Ca+2cations.

[0033] According to some embodiments, the saline water of step (I) comprises at least one of: CO2, H2CO3, and HCO3‘.

[0034] According to some embodiments, the admixing of saline water with the NaOH in consecutive step (II) entails carrying out one or more of the following chemical reactions:Ca+2+ CO2+ 2NaOH CaCO3+ 2Na++ H2O;Ca+2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2Na+;Ca+2+ HCO3- + NaOH CaCO3+ H2O + Na+, thereby producing CaCO3as a solid water-insoluble precipitate and decarbonated water suitable for subsequent desalination.

[0035] According to some embodiments, the saline water comprises HCO3‘, and wherein the admixing of saline water with the NaOH in step (II) entails carrying out the following chemical reaction:Ca+2+ HCO3- + NaOH CaCO3+ H2O + Na+. thereby producing CaCO3as a solid water-insoluble precipitate and decarbonated water suitable for subsequent desalination upon the separation of step (III).

[0036] According to some embodiments, the process comprises both step (Via) and step (VIb).

[0037] According to some embodiments, the brine electrodialysis of step (V) further entails forming deionized brine, and wherein the process further comprises repeating steps (I) to (IV) in a consecutive cycle, wherein consecutive step (IV) comprises desalinating a combination of the deionized brine and the decarbonated water of consecutive step (III) to form desalinated water and brine, wherein the brine comprises NaCl.

[0038] According to some embodiments, the process further comprises dissolving at least a portion of the separated CaCO3precipitate of step (III) and admixing the solution with the desalinated water of step (IV) thereby supplementing the desalinated water with essential Ca+2ions.

[0039] According to some embodiments, dissolving the portion of the separated CaCO3precipitate entails performing the following chemical reaction:CaCO3+ CO2+ H2O Ca(HCO3)2.

[0040] According to some embodiments, the process comprises step (Via), wherein a portion of the CO2formed upon the reaction between the HC1 and the separated CaCO3precipitate is employed in the dissolution of the portion of the separated CaCO3precipitate.

[0041] According to some embodiments, the saline water comprises HCO3‘ and CO3'2.

[0042] According to some embodiments, the saline water comprises at least 2 HCO3‘ ions per one CO3'2ion.

[0043] According to some embodiments, the saline water comprises 3 to 3000 HCO3‘ ions per one CO3'2ion.

[0044] According to some embodiments, the concentration of carbonated species in the saline water is at least 0.1 mM.

[0045] According to some embodiments, the saline water of step (I) has pH in the range of6 to 10.

[0046] According to some embodiments, the saline water of step (I) has pH in the range of7 to 9.

[0047] According to some embodiments, the salinity of the saline water of step (I) is in the range of 0.5 to 100 g / L.

[0048] According to some embodiments, admixing a carbonated species chelator with the saline water to form a CaCO3precipitate in step (II) further comprises adding nucleation seeds to the saline water.

[0049] According to some embodiments, the nucleation seeds comprise CaCO3particles.

[0050] According to some embodiments, the process further comprises a step of using a portion of the separated CaCO3precipitate as the nucleation seeds.

[0051] According to some embodiments, desalinating the decarbonated water in step (IV) comprises reverse osmosis. According to some embodiments, desalinating the decarbonated water comprises a single reverse osmosis cycle. According to some embodiments, desalinating the decarbonated water comprises at least two reverse osmosis cycles. According to some embodiments, desalinating the decarbonated water comprises two reverse osmosis cycles.According to some embodiments, desalinating the decarbonated water comprises two reverse osmosis cycles wherein the second reverse osmosis cycle is performed on a portion of the permeate of the first reverse osmosis cycle. According to some embodiments, desalinating the decarbonated water comprises at least two reverse osmosis cycles wherein each reverse osmosis cycle after the first cycle is performed on a portion of the permeate of the previous reverse osmosis cycle. According to some embodiments, each reverse osmosis cycle is performed on a portion constituting 70% or less of the permeate of the previous reverse osmosis cycle. According to some embodiments, each reverse osmosis cycle after the first cycle is performed on a portion constituting 50% or less of the permeate of the previous reverse osmosis cycle. According to some embodiments, each reverse osmosis cycle after the first cycle is performed on a portion constituting 30% or less of the permeate of the previous reverse osmosis cycle.

[0052] According to some embodiments, the saline water of step (I) comprises at least one boron species at a first total boron species concentration.

[0053] According to some embodiments, the desalinated water formed in step (IV) has a second total boron species concentration, which is at least 10% lower than the first total boron species concentration.

[0054] According to some embodiments, the saline water of step (I) comprises boric acid.

[0055] According to some embodiments, admixing the carbonated species chelator with the saline water in step (II), entails increasing hydroxide ion concentration within the water; and wherein the hydroxide ions within the water react with the boric acid to form a borate.

[0056] According to some embodiments, the process comprises enhancing the removal of boron species from saline water undergoing desalination, which entails at least 10% more reduction in boron species content after a single reverse osmosis cycle as compared to the reduction in the absence of steps (II) and (III).

[0057] According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination comprises at least 30% more reduction in boron species content after a single reverse osmosis cycle as compared to the reduction in the absence of steps (II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination comprises at least 50% more reduction in boron species content after a single reverse osmosis cycle as compared to the reduction in the absence of steps (II) and (III). According to some embodiments, the second total boron species concentration is less than 1.5 mg / L.

[0058] According to some embodiments, the desalination of step (IV) entails passing the decarbonated water of step (III) through a selective membrane, which selectively prevents passage of borate over boric acid, thereby reducing the boron species concentration within the water.

[0059] According to some embodiments, passing the decarbonated water of step (III) through the selective membrane further reduces the total salt concentration within the decarbonated water of step (III), thereby desalinating the decarbonated water and reducing its boron species concentration in one step.

[0060] According to some embodiments, the process further comprises providing a carbon removal system, wherein at least one of steps (II) and (III) is carried out within the carbon removal system, wherein the carbon removal system comprises a fluidized bed pellet reactor, wherein step (II) comprises admixing in the fluidized bed pellet reactor the carbonated species chelator with the saline water to form the CaCO3precipitate and the decarbonated water.

[0061] According to some embodiments, the fluidized bed pellet reactor comprises a first fluid inlet pipe, a fluid outlet pipe and an enclosed reaction chamber, each of the fluid inlet pipe and the fluid outlet pipe is in fluid communication with the reaction chamber, wherein step (II) comprises inserting the saline water into the reaction chamber through the fluid inlet pipe, and wherein the admixing of the saline water with the carbonated species chelator in step (II) is carried out within the reaction chamber.

[0062] According to some embodiments, the fluidized bed pellet reactor further comprises a second fluid inlet pipe, and step (II) comprises forming a composition of the carbonated species chelator in water and inserting the formed composition into the reaction chamber through the second fluid inlet pipe.

[0063] According to some embodiments, the composition of the carbonated species chelator comprises the basic solution of NaOH formed is step (V), and wherein forming the basic solution of NaOH is performed according to step (V).

[0064] According to some embodiments, step (III) further comprises evacuating the decarbonated water through the fluid outlet pipe.

[0065] According to some embodiments, the fluidized bed pellet reactor further comprises a semi-permeable filter, which is permeable to water and impermeable to solids above a predetermined diameter, and is positioned to separate between the reaction chamber and the fluid outlet pipe; wherein the evacuation of the decarbonated water of step (III) comprises filteringthe decarbonated water from the CaCO3precipitate by flowing the decarbonated water through the semi-permeable filter, and flowing the filtered decarbonated water through the fluid outlet pipe.

[0066] According to some embodiments, the semi-permeable filter has a cutoff is in the range of 0.07 to 0.16 millimeters.

[0067] According to some embodiments, step (II) further entail forming CaCO3fine particles.

[0068] According to some embodiments, step (III) further comprises filtering the decarbonated water from the CaCO3fine particles by flowing the decarbonated water through a second semi-permeable filter. According to some embodiments, step (III) comprises: filtering the decarbonated water from the CaCO3precipitate by flowing the decarbonated water through the semi-permeable filter; filtering the filtered decarbonated water from the CaCO3fine particles by flowing the filtered decarbonated water through a second semi-permeable filter; and flowing the decarbonated water filtered exiting the second semi-permeable filter through the fluid outlet pipe.

[0069] According to some embodiments, the second semi-permeable filter has a cutoff of no more than 1 micrometer. According to some embodiments, the second semi-permeable filter has a cutoff of no more than 5 micrometer. According to some embodiments, the second semi- permeable filter has a cutoff of no more than 10 micrometer. According to some embodiments, the second semi-permeable filter has a cutoff of at least 15 micrometer. According to some embodiments, the second semi-permeable filter has a cutoff of no more than 25 micrometer.

[0070] According to some embodiments, the enclosed reaction chamber comprises a top end and a bottom end, wherein fluid outlet pipe is connected to the reaction chamber in the vicinity of its top end, and the first fluid inlet pipe is connected to the reaction chamber in the vicinity of its bottom end.

[0071] According to some embodiments, the fluidized bed pellet reactor further comprises a solid outlet pipe, wherein step (III) further comprises evacuating the CaCO3precipitate through the solid outlet pipe, thereby isolating the CaCO3precipitate from the decarbonated water.

[0072] According to some embodiments, the enclosed reaction chamber comprises a top end and a bottom end, wherein the solid outlet pipe is connected to the reaction chamber in the vicinity of its bottom end.

[0073] According to some embodiments, the fluidized bed pellet reactor further comprises a solid inlet pipe, wherein step (II) further comprises inserting seeds of CaCOs or sand into the reaction chamber through the solid inlet pipe.

[0074] According to some embodiments, step (II) further comprises fluidizing the seeds in the reaction chamber.

[0075] According to some embodiments, the solid inlet pipe is connected to the reaction chamber.

[0076] According to some embodiments, the fluidized bed pellet reactor comprises: a first fluid inlet pipe, a second fluid inlet pipe, a solid inlet pipe, a fluid outlet pipe, a solid outlet pipe and an enclosed reaction chamber, which comprises a top end and a bottom end, wherein the fluid outlet pipe is connected to the reaction chamber in the vicinity of its top end, the solid inlet pipe is connected to the reaction chamber, and each of the solid outlet pipe and the fluid inlet pipe is connected to the reaction chamber in the vicinity of its bottom end; wherein the saline water comprises HCO3-, and the carbonated species chelator comprises NaOH; step (II) comprises: inserting the saline water into the reaction chamber through the first fluid inlet pipe; preparing a composition of NaOH in water and inserting the formed composition into the reaction chamber through the second fluid inlet pipe; and inserting CaCOs or sand seeds into the reaction chamber through the solid inlet pipe and fluidizing said seeds, thereby inducing precipitation of CaCOs formed from a chemical reaction between the Ca+2, HCO3- and the NaOH, so that the formed CaCOs is sinking to the bottom end of the reaction chamber and the decarbonated water flows in the direction of the top end of the reaction chamber; and step (III) comprises evacuating the decarbonated water from the top end of the reaction chamber through the fluid outlet pipe; and / or evacuating the CaCOs from the bottom end of the reaction chamber through the solid outlet pipe.

[0077] According to some embodiments, the carbonated species chelator is NaOH, wherein the fluidized bed pellet reactor further comprises a solid inlet pipe, wherein step (III) further comprises inserting seeds of the CaCOs into the reaction chamber through the solid inlet pipe and fluidizing the seeds in the reaction chamber to a fluidized grains height, thereby inducing precipitation and maturation of CaCOs pellets.

[0078] According to some embodiments, the fluidized grains height is in the range of 0.6 meter to 12.4 meter.

[0079] According to some embodiments, there is provided a process for electrodialysis of brine, the process comprising the steps of:(I) providing brine comprising carbonated species selected from the group consisting of: CO2, H2CO3, HCO3- , CO32and a combination thereof, and NaCl;(II) admixing a carbonated species chelator with the brine of step (I) to form a CaCO3precipitate and decarbonated brine;(III) separating the CaCO3precipitate of step (II) from the decarbonated brine;(V) performing an electrodialysis of the decarbonated brine of step (III) to form an acidic solution of HC1 and a basic solution of NaOH;(Via) optionally contacting the HC1 formed in step (V) with at least a portion of the separated CaCO3precipitate of step (III) to form CaCl2and CO2; and(VIb) optionally repeating steps (I) to (III) in a consecutive cycle, by using the NaOH formed in step (V), and, optionally, the CaCl2formed in step (Via) as the carbonated species chelator of the consecutive step (II).

[0080] According to some embodiments, the brine of step (I) further comprises Ca+2cations; the brine of step (I) is supplemented with Ca+2ions by addition of soluble calcium salt; and / or the carbonated species chelator of step (II) comprises Ca+2cations. Each possibility represents a separate embodiment of the invention.

[0081] According to some embodiments, the carbonated species chelator of step (II) comprises NaOH.

[0082] According to some embodiments, the brine of step (I) comprises at least one of: CO2, H2CO3, and HCO3- ; wherein the carbonated species chelator of step (II) comprises NaOH, and wherein the admixing of brine with the NaOH in step (II) entails carrying out one or more of the following chemical reactions:Ca+2+ CO2+ 2NaOH CaCO3+ 2Na++ H2O;Ca+2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2Na+;Ca+2+ HCO3’ + NaOH CaCO3+ H2O + Na+, thereby producing CaCO3as a solid water-insoluble precipitate and decarbonated brine suitable for subsequent desalination.

[0083] According to some embodiments, the process comprises step (Via) and further comprises a step of isolating the CaCl2formed in step (Via).

[0084] According to some embodiments, the process comprises a step of storing at least a portion of the CaCl2formed in step (Via); and / or supplementing the brine of consecutive step (I) with a portion of the CaCl2formed in step (Via) to increase a concentration of Ca+2ions therein. Each possibility represents a separate embodiment of the invention.

[0085] According to some embodiments, admixing a carbonated species chelator with the saline water to form a CaCO3precipitate in step (II) further comprises adding nucleation seeds to the brine, wherein the nucleation seeds comprise CaCO3or sand particles.

[0086] Certain embodiments of the present disclosure may include some, all, or none of the above advantages. One or more technical advantages may be readily apparent to those skilled in the art from the figures, descriptions and claims included herein. Moreover, while specific advantages have been enumerated above, various embodiments may include all, some or none of the enumerated advantages.

[0087] In addition to the exemplary aspects and embodiments described above, further aspects and embodiments will become apparent by reference to the figures and by study of the following detailed descriptions.BRIEF DESCRIPTION OF THE DRAWINGS

[0088] Examples illustrative of embodiments are described below with reference to figures attached hereto. In the figures, identical structures, elements or parts that appear in more than one figure are generally labeled with a same numeral in all the figures in which they appear. Alternatively, elements or parts that appear in more than one figure may be labeled with different numerals in the different figures in which they appear. Dimensions of components and features shown in the figures are generally chosen for convenience and clarity of presentation and are not necessarily shown in scale. The figures are listed below.

[0089] Figure 1A is a block diagram representing a desalination process, according to some embodiments.

[0090] Figure IB is a block diagram representing a desalination process, according to some embodiments.

[0091] Figure 1C is a block diagram representing a process for treatment of a CaCO3precipitate, according to some embodiments.

[0092] Figure 2 is a schematic cross-section illustration of a pellet reactor, according to some embodiments.

[0093] Figure 3 is a schematic illustration of an electrodialysis device, according to some embodiments.DETAILED DESCRIPTION OF THE INVENTION

[0094] In the following description, various aspects of the disclosure will be described. For the purpose of explanation, specific configurations and details are set forth in order to provide a thorough understanding of the different aspects of the disclosure. However, it will also be apparent to one skilled in the art that the disclosure may be practiced without specific details being presented herein. Furthermore, well-known features may be omitted or simplified in order not to obscure the disclosure.

[0095] The processes of the present invention are suitable for desalination of seawater, brackish water, or other types of water.

[0096] According to some embodiments, the present invention provides a process for desalinating saline water. According to some embodiments, the present invention provides a process for enhancing the removal of boron species from saline water undergoing desalination.

[0097] According to some embodiments, the processes of the present invention comprise the steps of:(I) providing saline water comprising carbonated species selected from the group consisting of: CO2, H2CO3, HCO3- , CO32and a combination thereof, and NaCl;(II) admixing a carbonated species chelator with the saline water of step (I) to form a CaCCF precipitate and decarbonated water;(III) separating the CaCCF precipitate of step (II) from the decarbonated water;(IV) desalinating the decarbonated water of step (III) to form desalinated water and brine, wherein the brine comprises NaCl; and(V) performing an electrodialysis of the brine of step (IV) to form an acidic solution of HC1 and a basic solution of NaOH.

[0098] According to some embodiments, the process further comprises step (Via) of contacting the HC1 formed in step (V) with at least a portion of the separated CaCO3precipitate of step (III) to form CaCl2and CO2.

[0099] The phrase “at least a portion” of a specified material, element or article is intended to mean all or a fraction of the material, element, or article. It is to be understood that subsequent references to “the portion” may relate to the fraction and / or to the entire material, element or article, based in the context and specific embodiment.

[0100] According to some embodiments, the process further comprises step (VIb) of repeating steps (I) to (IV) in a consecutive cycle, by using the NaOH formed in step (V) as the carbonated species chelator of a consecutive step (II).

[0101] According to some embodiments, the process comprises step (VI) of performing step (Via), step (VIb), or both. According to some embodiments, the process comprises performing both step (Via) and step (VIb).

[0102] According to some embodiments, the process comprises repeating steps (I) to (V) a plurality of cycles. According to some embodiments, the process comprises repeating steps (I) to (VI) a plurality of cycles.

[0103] The term “plurality of cycles” refers to two or more cycles.

[0104] Although some embodiments of the present process relate to a batch reaction, it is to be understood that the present process may be carried out continuously.

[0105] According to some embodiments, the process comprises performing steps (I)-(VI) continuously. According to some embodiments, the process comprises performing steps (I)-(VI) repeatedly.

[0106] Exemplary processes according to the present invention are presented in Figures 1A, IB and 1C. Although Figures 1A, IB and 1C represent specific embodiments of the present process, broken lines and brackets therein represent an optional step of the specific embodiment.

[0107] Specific reference is now made to step (I) of the present process. According to some embodiments, the present process comprises step (I) of providing saline water. According to some embodiments, step (I) is also represented as step 1000 in Figure 1A and Figure IB.

[0108] Salts present in seawater and saline water are inorganic and typically include mostly sodium chloride, NaCl. Additional chloride salts present at lower concentrations in seawater is potassium chloride, KC1, magnesium chloride MgCl2and calcium chloride CaCl2. Other lower concentration salts in seawater include sulfates, bicarbonates and bromides of sodium, potassium, magnesium, and calcium.

[0109] According to some embodiments, the saline water provided in step (I) comprises NaCl.

[0110] Carbonated species present in seawater are inorganic and typically include CO2, H2CO3, HCO3- and CO32. They are also commonly termed dissolved inorganic carbon (DIC) species, and their relative ratio is pH depended.

[0111] According to some embodiments, the saline water provided in step (I) comprises carbonated species selected from the group consisting of: CO2, H2CO3, HCCO3- CO32and a combination thereof.

[0112] Within the present disclosure, the term “DIC concentration” should be interpreted as the sum of the molar concentrations of CO2, H2CO3, HCCO3-and CO32within a mixture, e.g., an aqueous mixture. For example, an aqueous mixture comprising 0.1M HCO,' and 0.15M CO ,'2and devoid of other DIC species is said to have a DIC concentration of 0.25M.

[0113] According to some embodiments, the saline water comprises HCO3-. According to some embodiments, the saline water further comprises CO3-2. According to some embodiments, the saline water comprises HCO3- and CO3-2.

[0114] According to some embodiments, the saline water comprises at least 0.1 HCO3- ions per one CO3-2ion. According to some embodiments, the saline water comprises at least 0.5 HCO3- ions per one CO ,'2ion. According to some embodiments, the saline water comprises at least 1 HCO3- ion per one CO3-2ion. According to some embodiments, the saline water comprises at least 1.5 HCO3- ions per one CO32ion. According to some embodiments, the saline water comprises at least 2 HCO3- ions per one CO32ion. According to some embodiments, the saline water comprises at least 2.3 HCO3- ions per one CO32ion. According to some embodiments, the saline water comprises at least 3 HCO3- ions per one CO32ion. According to some embodiments, the saline water comprises at least 5 HCO3- ions per one CO32ion.According to some embodiments, the saline water comprises at least 6 HCO3- ions per one CO3-2ion. According to some embodiments, the saline water comprises at least 10 HCO3- ions per one CO32ion. According to some embodiments, the saline water comprises at least 20 HCO3- ions per one CO3-2ion. According to some embodiments, the saline water comprises at least 50 HCO3- ions per one CO3-2ion. According to some embodiments, the saline water comprises at least 100 HCO3- ions per one CO32ion. According to some embodiments, the saline water comprises at least 1000 HCO3- ions per one CO32ion.

[0115] According to some embodiments, the saline water comprises 0.1 to 100, 1 to 100, 2 to 3000, 3 to 3000, 3-1000, 3-500, 3-250 or 3-100 HCO3- ions per one CO3-2ion. Each possibility represents a separate embodiment of the invention.

[0116] Typically, in natural water sources, the concentration of carbonated species is at least 0.1 millimolar (mM), 0.25 millimolar (mM), 0.5 millimolar (mM), at least 1 mM, at least 1.5 mM, at least 2 mM, at least 3 mM, at least 4 mM or at least 5 mM according to some embodiments. Each possibility represents a separate embodiment of the invention. It is to be understood that said concentrations are present without intentional human intervention intended to increase to CO2concentration.

[0117] According to some embodiments, the concentration of the carbonated species is at least 0.1 millimolar (mM). According to some embodiments, the concentration of the carbonated species is at least 0.25 millimolar (mM). According to some embodiments, the concentration of the carbonated species is at least 0.5 millimolar (mM). According to some embodiments, the concentration of the carbonated species is at least 0.75 millimolar (mM). According to some embodiments, the concentration of the carbonated species is at least 1 millimolar (mM). According to some embodiments, the concentration of the carbonated species is at least 1.25 mM. According to some embodiments, the concentration of the carbonated species is at least 1.5 mM. According to some embodiments, the concentration of the carbonated species is at least 1.75 mM. According to some embodiments, the concentration of the carbonated species is at least 2 mM. According to some embodiments, the concentration of the carbonated species is at least 2.25 mM. According to some embodiments, the concentration of the carbonated species is in the range of 1.0 to 50.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 1.0 to 25.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 1.0 to 10.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 1.0 to 5.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of0.1 to 50.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 0.1 to 25.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 0.1 to 10.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 0.1 to 5.0 mM.

[0118] According to some embodiments, the saline water of the present invention typically includes one or more alkaline earth metals, e.g., magnesium, calcium, etc., such that they may be viewed as alkaline-earth-metal-containing waters. Examples of such waters are those that include calcium in amounts ranging from 50 ppm to 20,000 ppm, such as 200 ppm to 5000 ppm and including 400 ppm to 1000 ppm. According to some embodiments, the carbonated water source is a sea or an ocean. According to some embodiments, the carbonated water source is a sea. According to some embodiments, the carbonated water source is an ocean.

[0119] According to some embodiments, the saline water provided in step (I) has low concentration of the alkaline earth metals, and step (I) includes supplementing the saline water with soluble alkaline earth metal salts. According to some embodiments, step (I) includes supplementing the saline water with a Ca+2salt. According to some embodiments, the Ca+2salt is a water-soluble Ca+2salt. According to some embodiments, the Ca+2salt comprises CaCl2. According to some embodiments, step (I) includes supplementing the saline water with the CaCl2produced in step (Via).

[0120] Typically, seawater (i.e., water derived from oceans or other seas) has a salinity of between 31 g / kg and 38 g / kg. Thus, according to some embodiments, the saline water has a total salt concentration of at least 1% w / w. According to some embodiments, the saline water has a total salt concentration of at least 1.5% w / w. According to some embodiments, the saline water has a total salt concentration of at least 2% w / w. According to some embodiments, the saline water has a total salt concentration of at least 2.5% w / w. According to some embodiments, the saline water has a total salt concentration of at least 3% w / w. According to some embodiments, the saline water has a total salt concentration in the ranges of 1-6% w / w, 2-5% w / w or 3-4% w / w. Each possibility represents a separate embodiment of the invention.

[0121] Alternatively, according to some embodiments, the saline water is derived from an unnatural water source, for example the retentate of a desalination plant. Specifically, brine from desalination plants is contemplated as the source of saline water, according to some embodiments. Thus, according to some embodiments, the saline water is brine from a desalination plant.

[0122] According to some embodiments, the saline water comprises wastewater. According to some embodiments, the saline water is a mixture of natural water with wastewater. According to some embodiments, the saline water is a mixture of seawater with wastewater. According to some embodiments, the saline water comprises brackish water.

[0123] The term “brackish water” refers to water having an amount of dissolved salts greater than 0.5 grams per liter.

[0124] According to some embodiments, the salinity of the saline water of step (I) is in the range of 0.5 to 100 g / L, 30-40 g / L, 0.5-3 g / L, 3-20 g / L, 20-50 g / L, 50-65 g / L or 0.1 to 0.5 g / L. Each possibility represents a separate embodiment of the invention.

[0125] The ratio between the concentration of the carbonates and bicarbonate ions is determined by the pH and salinity of the saline water. For example, for seawater having typical pH of 8.2, there are 6 bicarbonate ions for each carbonate ion.

[0126] Thus, according to some embodiments, saline water comprises HCO3- at a concentration of at least 0.1 millimolar (mM). According to some embodiments, saline water comprises HCO3- at a concentration of at least 0.25 millimolar (mM). According to some embodiments, saline water comprises HCO3- at a concentration of at least 0.5 millimolar (mM). According to some embodiments, saline water comprises HCO3- at a concentration of at least 0.75 millimolar (mM). According to some embodiments, the HCO3- concentration in the saline water is at least 1 mM. According to some embodiments, the HCO3- concentration in the saline water is at least 1.25 mM. According to some embodiments, the HCO3- concentration in the saline water is at least 1.5 mM. According to some embodiments, the HCO3- concentration in the saline water is at least 1.75 mM. According to some embodiments, the HCO3- concentration in the saline water is at least 2 mM. According to some embodiments, the HCO3- concentration in the saline water is at least 2.25 mM. According to some embodiments, the HCO3- concentration in the saline water is in the range of 0.5 to 10 mM, 0.5 to 5 mM, 0.5 to 4 mM or 0.5 to 3 mM. Each possibility represents a separate embodiment of the invention.

[0127] According to some embodiments, at least 25% mol / mol of the total carbon dioxide species in the saline water of step (I) is HCO3- . According to some embodiments, at least 50% mol / mol of the total carbon dioxide species in the saline water of step (I) is HCO3- . According to some embodiments, at least 60% mol / mol of the total carbon dioxide species in the saline water of step (I) is HCO3- .

[0128] The mol / mol unit, as used herein refers to a relation between the number of molecules of a first species and number of molecules of a second species within a specified volume, wherein the first species may include or be included in the second species. For example, in a solution of 0.2 mol CO32and 0.8 mol HCO3- , 20% mol / mol of the total carbonated species is CO32and 80% mol / mol is HCO3- .

[0129] According to some embodiments, the saline water of step (I) comprises CO3-2at a concentration of no more than 20 millimolar (mM). According to some embodiments, the CO3-2concentration in the saline water is no more than 10 millimolar. According to some embodiments, the CO3-2concentration in the saline water is no more than 5 millimolar. According to some embodiments, the CO3-2concentration in the saline water is no more than 3 millimolar. According to some embodiments, the CO3-2concentration in the saline water is no more than 1 millimolar. According to some embodiments, the CO3-2concentration in the saline water is no more than 0.5 millimolar.

[0130] Similarly, according to some embodiments, the saline water comprises CO3-2at a concentration of no more than 20 millimolar (mM). According to some embodiments, the CO3-2concentration in the saline water is no more than 10 millimolar. According to some embodiments, the CO3-2concentration in the saline water is no more than 5 millimolar. According to some embodiments, the CO3-2concentration in the saline water is no more than 3 millimolar. According to some embodiments, the CO3-2concentration in the saline water is no more than 1 millimolar. According to some embodiments, the CO3-2concentration in the saline water is no more than 0.5 millimolar. According to some embodiments, the CO3-2concentration in the saline water is in the range of 0 to 2 millimolar.

[0131] According to some embodiments, the saline water of step (I) has pH of no more than 11.5. According to some embodiments, the saline water of step (I) has pH of no more than 11. According to some embodiments, the saline water of step (I) has pH of no more than 10.5. According to some embodiments, the saline water of step (I) has pH of no more than 10.According to some embodiments, the saline water of step (I) has pH of no more than 9.5.According to some embodiments, the saline water of step (I) has pH of no more than 9. According to some embodiments, the saline water of step (I) has pH of no more than 8.5.According to some embodiments, the saline water of step (I) has pH of at least 5. According to some embodiments, the saline water of step (I) has pH of at least 5.5. According to some embodiments, the saline water of step (I) has pH of at least 6. According to some embodiments, the saline water of step (I) has pH of at least 6.5. According to some embodiments, the salinewater of step (I) has pH of at least 7. According to some embodiments, the carbonated water of step (I) has pH of at least 7.5. According to some embodiments, the saline water of step (I) has pH of at least 8. According to some embodiments, the saline water of step (I) has pH in the range of 6-11, 7-11, 7-10, 7-8.5, 7.5-8.4, 6-7, 7-8, 8-9, 9-10 or 10-11. Each possibility represents a separate embodiment of the invention.

[0132] According to some embodiments, the saline water of step (I) comprises at least one of: CO2, H2CO3, and HCO3‘.

[0133] According to some embodiments, the saline water is seawater.

[0134] According to some embodiments, the saline water of step (I) further comprises Ca+2cations or wherein the carbonated species chelator of step (II) comprises Ca+2cations. According to some embodiments, step (I) comprises supplementing the saline water with a Ca+2salt. According to some embodiments, the Ca+2salt is a soluble Ca+2salt. According to some embodiments, step (I) comprises supplementing the saline water with a soluble Ca+2salt to reach sufficient amount of Ca+2ions for the precipitation of step (II). According to some embodiments, the Ca+2salt comprises the CaCl2produced in step (Via). According to some embodiments, step (I) comprises supplementing the saline water with a soluble Ca+2, comprising the CaCl2produced in step (Via) to reach a sufficient amount of Ca+2ions enabling the precipitation of step (II).

[0135] According to some embodiments, the sufficient amount is at least 1 mol Ca+2per 1 mol of carbonated species in the saline water. It is to be understood that “1 mol of carbonated species” is intended to refer to the total carbonated species, for example, a saline sample that comprises w moles of CO2, x moles of H2CO3, y moles of HCCE' and z moles of CO32can be considered to include (w+x+y+z) mol carbonated species. According to some embodiments, the sufficient amount is at least 2 mol Ca+2per 1 mol of carbonated species in the saline water. According to some embodiments, the sufficient amount is at least 5 mol Ca+2per 1 mol of carbonated species in the saline water. According to some embodiments, the sufficient amount is at least 10 mol Ca+2per 1 mol of carbonated species in the saline water. According to some embodiments, the sufficient amount is at least 25 mol Ca+2per 1 mol of carbonated species in the saline water. According to some embodiments, the sufficient amount is at least 1 mol Ca+2per 50 mol of carbonated species in the saline water. According to some embodiments, the sufficient amount is at least 100 mol Ca+2per 1 mol of carbonated species in the saline water.

[0136] According to some embodiments, the sufficient amount is 1 to 100 mol Ca+2per 1 mol of carbonated species in the saline water, including each value and sub-range within thespecified range. According to some embodiments, the sufficient amount is 2 to 50 mol Ca+2per 1 mol of carbonated species in the saline water.

[0137] According to some embodiments, the saline water of step (I) comprises Ca+2cations.

[0138] Specifically, seawater typically contains around 400 ppm calcium. This amount enables the CaCO3precipitation in step (II), as detailed below, without additional calcium source(s), according to some embodiments.

[0139] According to some embodiments, the saline water comprises HCO3-. According to some embodiments, the saline water further comprises CO3-2. According to some embodiments, the saline water comprises HCO3- and CO32.

[0140] According to some embodiments, the saline water comprises HCO3- and CO3-2. According to some embodiments, the saline water comprises at least one HCO3- ion per one CO32ion. According to some embodiments, the saline water comprises at least 2 HCO3- ions per one CO3-2ion. According to some embodiments, the saline water comprises 3 to 3000 HCO3- ions per one CO3-2ion, including each value within the specified range. According to some embodiments, the saline water comprises at least 1000 HCO3- ions per one CO32ion.

[0141] According to some embodiments, the saline water comprises carbonated species at a concentration of at least 1 mM. According to some embodiments, the saline water comprises CO3-2at a concentration of no more than 10 mM. According to some embodiments, the concentration of carbonated species in the saline water is at least 0.1 mM.

[0142] According to some embodiments, the salinity of the saline water is in the range of 0.01 to 100 g / L, including each value within the specified range.

[0143] According to some embodiments, the salinity of the saline water is in the range of 0.5 to 100 g / L, including each value within the specified range.

[0144] According to some embodiments, the salinity of the saline water is in the range of 0.5 to 8 g / L, including each value within the specified range.

[0145] According to some embodiments, the salinity of the saline water is in the range of 2 to 6 g / L, including each value within the specified range.

[0146] According to some embodiments, the salinity of the saline water is in the range of 3 to 5 g / L, including each value within the specified range.

[0147] The term “salinity” as used herein refers to the total concentration of dissolved salts in a given sample of water, as measured by conductivity, and expressed as a mass of salts in a given volume of solution, expressed in grams per liter (gr / L) or grams per kilogram (gr / kg).

[0148] According to some embodiments, the saline water of step (I) comprises at least one boron species at a first total boron species concentration.

[0149] According to some embodiments, the saline water of step (I) comprises at least one boron species. According to some embodiments, at least one boron species comprises boric acid. According to some embodiments, the saline water of step (I) comprises at least one boron species at a first total boron species concentration.

[0150] The term “total boron species concentration” refers to the total concentration of boric acid, its salts (e.g., borate) and derivatives.

[0151] Specific reference is now made to step (II) of the present process. According to some embodiments, the present process comprises step (II) of admixing a carbonated species chelator with the saline water of step (I). According to some embodiments, step (II) is also represented as step 1010 in Figure 1A and Figure IB.

[0152] According to some embodiments, admixing a carbonated species chelator with the saline water entails forming a CaCO3precipitate and decarbonated water.

[0153] According to some embodiments, the carbonated species chelator is a base. According to some embodiments, the carbonated species chelator is a Lewis base.

[0154] According to some embodiments, the carbonated species chelator is an inorganic compound. According to some embodiments, the carbonated species chelator is an inorganic base.

[0155] According to some embodiments, the carbonated species chelator comprises a hydroxide salt. According to some embodiments, the hydroxide salt is selected from the group consisting of sodium hydroxide (NaOH), potassium hydroxide (KOH) and a combination thereof. According to some embodiments, the carbonated species chelator comprises NaOH. According to some embodiments, the carbonated species chelator is NaOH.

[0156] As specified above, due to the relatively high Ca+2concentration in seawater, simple inorganic bases such as NaOH were found to be sufficient in precipitating CaCO3under the present conditions of step (II), according to some embodiments. However, according to some embodiments, it is contemplated that calcium-containing bases, such as Ca(OH)2, may be usedas the carbonated species chelator. Alternatively, according to some embodiments, it is contemplated to supplement the saline water of step (I) with soluble calcium salts such as CaCl2.

[0157] According to some embodiments, the carbonated species chelator is a Ca+2salt. According to some embodiments, the carbonated species chelator is a Ca+2base. According to some embodiments, the carbonated species chelator is an inorganic Ca+2basic salt. According to some embodiments, the carbonated species chelator is Ca(OH)2 or CaO. Each possibility represents a separate embodiment of the invention. According to some embodiments, the carbonated species chelator is Ca(OH)2.

[0158] According to some embodiments, the carbonated species chelator of step (II) comprises NaOH.

[0159] According to some embodiments, the admixing of step (II) entails forming CO3'2anions, and wherein the CaCO3precipitate is formed upon ion pairing of the Ca+2cations and said CO3'2anions.

[0160] According to some embodiments, the saline water of step (I) comprises Ca+2cations, wherein the carbonated species chelator of step (II) comprises NaOH, and wherein the admixing of saline water with the NaOH in step (II) entails carrying out one or more of the following chemical reactions:Ca+2+ CO2+ 2NaOH CaCO3+ 2Na++ H2O;Ca+2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2Na+; andCa+2+ HCO3‘ + NaOH CaCO3+ H2O + Na+. Each possible reaction represents a separate embodiment of the invention.

[0161] According to some embodiments, the contacting of saline water with the NaOH in step (II) entails carrying two or more of the above chemical reactions. According to some embodiments, the contacting of saline water with the NaOH in step (II) entails carrying each of the above chemical reactions.

[0162] According to some embodiments, the admixing of saline water with the NaOH in step (II) entails carrying out at least the following chemical reaction:Ca+2+ CO2+ 2NaOH CaCO3+ 2Na++ H2O.

[0163] According to some embodiments, the admixing of saline water with the NaOH in step (II) entails carrying out at least the following chemical reaction:Ca+2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2Na+.

[0164] According to some embodiments, the admixing of saline water with the NaOH in step (II) entails carrying out at least the following chemical reaction:Ca+2+ HCO3’ + NaOH CaCO3+ H2O + Na+.

[0165] According to some embodiments, the admixing of saline water with the NaOH in step (II) and the above chemical reaction(s) result in producing CaCO3as a solid water-insoluble precipitate.

[0166] According to some embodiments, the admixing of saline water with the NaOH in step (II) and the above chemical reaction(s) result in producing decarbonated water. According to some embodiments, the produced decarbonated water is suitable for subsequent desalination. According to some embodiments, the produced decarbonated water is suitable for subsequent desalination following separation from the CaCO3precipitate and filtration.

[0167] According to some embodiments, the carbonated species chelator is provided to step (II) as an aqueous mixture. According to some embodiments, the carbonated species chelator is provided to step (II) as an aqueous solution.

[0168] According to some embodiments, the carbonated species chelator is NaOH, which is provided to step (II) as an aqueous mixture. According to some embodiments, the carbonated species chelator is NaOH, which is provided to step (II) as an aqueous solution of NaOH.

[0169] According to some embodiments, the aqueous solution of NaOH is provided to step (II) from an electrodialysis of NaCl. According to some embodiments, the aqueous solution of NaOH is provided to step (II) from an electrodialysis of the brine of step (IV). According to some embodiments, the aqueous solution of NaOH is the basic solution of NaOH formed in step (V).

[0170] According to some embodiments, the concentration of the carbonated species chelator is at least 0.01 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 0.05 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 0.1 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 0.25 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 0.5 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 1 g / L. According to some embodiments, the concentration of the carbonated species chelator isat least 1.5 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 2 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 5 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 10 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 25 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 50 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 100 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 200 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 500 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 0.01 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 0.05 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 0.1 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 0.25 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 0.5 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 1 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 1.5 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 2 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 5 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 10 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 25 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 50 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 100 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 200 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 500 g / L.

[0171] According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 1000 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 500 g / L.According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 200 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 100 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 50 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 25 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 10 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 5 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 2.5 g / L.

[0172] According to some embodiments, the chemical reaction of step (II) is a mono-phasic reaction.

[0173] Specifically, the term “mono-phasic reaction” refers to a reaction, where the reactants are in the same phase. Such reactions are much more rapid and easy to carry out, compared to biphasic reactions (e.g., liquid-gas reaction, liquid-(insoluble) solid reaction, and solid-gas reaction). The reaction of step (II) takes place in the liquid phase as the reactants are dissolved in water, according to some embodiments.

[0174] According to some embodiments, the CaCCL precipitate formed by the reaction of step (II) is water-insoluble. The term “water-insoluble” as used herein refers to a compound, which has aqueous solubility of 0.5 g / L or less at 25 °C and neutral pH. In particular, as detailed below, CaCCL is only sparingly soluble, which leads to its precipitation and separation from the water.

[0175] Specifically, the aqueous solubility of CaCCL is 13 mg / L at 25°C.

[0176] According to some embodiments, the solid water-insoluble precipitate is CaCCL in any crystalline or amorphous form including, but not limited to, calcite, aragonite, calcium carbonate monohydrate, amorphous calcium carbonate and the like. Each possibility represents a separate embodiment of the present invention.

[0177] It is to be understood that the amount of the carbonated species chelator (e.g., NaOH) is determined by the pH of the saline water, DIC concentration, and the specific reaction stoichiometry.

[0178] According to some embodiments, the admixing thereof in step (II) entails contacting 0.25 to 4 moles of carbonated species per 1 mol of carbonated species chelator. According tosome embodiments, the admixing thereof in step (II) entails contacting 0. 5 to 2, 0.5 to 1.5 or 0.5 to 1.25 moles of carbonated species per 1 mol of carbonated species chelator. Each possibility represents a separate embodiment of the invention.

[0179] Alongside the dissolved inorganic carbon (DIC) species, sea water also contains relatively high concentration of divalent ions, most prominently magnesium (~50 mM). Interestingly, while the concentrations product of the calcium and carbonate ions exceeds the solubility product of calcium carbonate 3.3xl0'9M2[William M Haynes. CRC handbook of chemistry and physics. CRC press, 2014], precipitation is inhibited. This is explained by inhibition of nucleation by the presence of trace molecules in seawater [Elizabeth A Burton and Lynn M Walter. The role of pH in phosphate inhibition of calcite and aragonite precipitation rates in seawater. Geochimica et Cosmochimica Acta, 54(3):797-808, 1990], the effects of seawater ionic strength on the activities of calcium and carbonate [Pierpaolo Zuddas and Alfonso Mucci. Kinetics of calcite precipitation from seawater: li. the influence of the ionic strength. Geochimica et Cosmochimica Acta, 62(5):757-766, 1998] or both.

[0180] Thus, it is common that despite the insolubility of CaCO3its precipitation from aqueous compositions is often sluggish. One way of encountering this hurdle is to induce its precipitation, e.g., through seeding small crystals, over which dissolved CaCO3tend to precipitate more rapidly to form larger CaCO3crystals or pellets, according to some embodiments.

[0181] According to some embodiments, forming a solid water-insoluble precipitate in step (II) comprises inducing precipitation from the water. According to some embodiments, forming a solid water-insoluble precipitate in step (II) comprises inducing precipitation from the water, through seeding nucleation seeds as described herein (e.g., seeds of the water-insoluble precipitate in the mixture of step (II)).

[0182] According to some embodiments, admixing a carbonated species chelator with the saline water to form a solid water-insoluble precipitate in step (II) further comprises adding nucleation seeds of the water-insoluble precipitate to the mixture of step (II).

[0183] the terms “nucleation seed” and “nucleation seeding material” as used herein are interchangeable and mean any solid capable of promoting the local formation of a grain, in particular a crystal.

[0184] According to some embodiments, admixing a carbonated species chelator with the saline water to form a solid water-insoluble precipitate in step (II) further comprises addingnucleation seeds to the saline water. According to some embodiments, the nucleation seeds may be of the same material of the water-insoluble precipitate or of a different material. Suitable nucleation seeds of different materials, may include, but not limited to sand particles. According to some embodiments, the nucleation seeds include particles comprising the same material of the water-insoluble precipitate. According to some embodiments, the nucleation seeds consist essentially of particles of the same material of the water-insoluble precipitate. The phrase “the nucleation seeds consist essentially of particles of the same material of the water-insoluble precipitate” is intended to mean that admixing a carbonated species chelator with the saline water to form a solid water-insoluble precipitate in step (II) further comprises adding nucleation seeds composition to the saline water, wherein the composition comprises particles of the same material of the water-insoluble precipitate, and wherein the subsequent precipitation entails growing of crystals over the particles of the same material of the water-insoluble precipitate. According to some embodiments, the nucleation seeds include CaCO3. According to some embodiments, at least a portion of the CaCO3is provided from the water-insoluble precipitate. According to some embodiments, the CaCO3is provided from the water-insoluble precipitate. According to some embodiments, at least a portion of the CaCO3is not provided from the waterinsoluble precipitate. According to some embodiments, the CaCO3is not provided from the water-insoluble precipitate. According to some embodiments, the nucleation seeds consist of particles of the same material of the water-insoluble precipitate of step (II).

[0185] According to some embodiments, the nucleation seeds comprise CaCO3particles or sand particles. Each possibility represents a separate embodiment of the invention. According to some embodiments, the nucleation seeds comprise CaCO3particles.

[0186] According to some embodiments, the process further comprises a step of using a portion of the separated CaCO3precipitate as the nucleation seeds. According to some embodiments, the process further comprises a step of crushing a portion of the separated CaCO3precipitate and using is as the nucleation seeds.

[0187] According to some embodiments, admixing the carbonated species chelator with the saline water in step (II), entails increasing hydroxide ion concentration within the water; and wherein the hydroxide ions within the water react with the boric acid to form a borate.

[0188] According to some embodiments, upon the admixing the following reaction is taking place:B(OH)3+ O H-→ B(OH)4-

[0189] In particular, with NaOH as the chelator, the reaction, according to some embodiments, is:B(OH)3+ NaOH NaB(OH)4.

[0190] As detailed herein, the process of the present invention may be carried out using a system, which is provided and elaborated herein. According to some embodiments, the system of the present invention comprises a pellet reactor 100 as described herein.

[0191] Reference is now made to Figure 2, which shows the pellet reactor 100, according to some embodiments.

[0192] According to some embodiments, step (II) comprises admixing in the pellet reactor 100 the saline water with the carbonated species chelator to form CaCO3as a solid waterinsoluble precipitate, and decarbonated water.

[0193] Generally, pellet reactors are typically cylindrical or conic vessels filled with nucleation seeds. Water is pumped through the reactor in an upward direction at relatively high speeds to maintain the grains fluidized. At the bottom of the reactor, a reactant is dosed. As a result, a solid product becomes super-saturated and precipitates on the grains, which gradually turn into marble-like pellets, periodically removed from the reactor and replaced by new grains. Some of these pellets may then be reused as nucleation seeding material, according to some embodiments.

[0194] According to some embodiments, the pellet reactor 100 is a fluidized bed reactor.

[0195] The term "fluidized bed reactor" may be used to refer to reactors comprising a vessel that contains a granular solid material (e.g., nucleation seeding material, such as CaCO3grains), in which a fluid (e.g., a gas or a liquid, such as a carbonated aqueous solution) is passed through the granular solid material at velocities sufficiently high as to suspend the solid material and cause it to behave as though it were a fluid. The term "circulating fluidized bed reactor" may be used to refer to fluidized bed reactors in which the granular solid material is passed out of the reactor, circulated through a line in fluid communication with the reactor, and recycled back, at least partially, into the reactor.

[0196] According to some embodiments, the pellet reactor 100 comprises a fluid inlet pipe 110. According to some embodiments, the pellet reactor 100 comprises a fluid outlet pipe 120. According to some embodiments, the pellet reactor 100 comprises an enclosed reaction chamber

[0197] According to some embodiments, the enclosed reaction chamber 130 comprises a top end 132 and a bottom end 134. The top end 132 and a bottom end 134 of the enclosed reaction chamber 130 are aligned with the corresponding top- and bottom ends of the pellet reactor 100, and are understood to the skilled in the art, upon witnessing any pellet reactor positioned on the ground. Specifically, the bottom end is positioned on the ground, on which the reactor is operating.

[0198] According to some embodiments, the fluid inlet pipe 110 is in fluid communication with the enclosed reaction chamber 130. According to some embodiments, the fluid inlet pipe 110 is connected to the enclosed reaction chamber 130.

[0199] According to some embodiments, step (I) comprises inserting the saline water into the enclosed reaction chamber 130 through the fluid inlet pipe 110. According to some embodiments, the fluid inlet pipe 110 comprises a valve (not shown) configured to monitor the liquid flow into the enclosed reaction chamber 130. According to some embodiments, the valve is configured to allow unidirectional flow of liquids into the enclosed reaction chamber 130.

[0200] According to some embodiments, the pellet reactor 100 comprises a second fluid inlet pipe 112.

[0201] According to some embodiments, the second fluid inlet pipe 112 is in fluid communication with the enclosed reaction chamber 130. According to some embodiments, the second fluid inlet pipe 112 is connected to the enclosed reaction chamber 130.

[0202] According to some embodiments, step (II) comprises providing the carbonated species chelator as a fluid composition into the enclosed reaction chamber 130 through the second fluid inlet pipe 112. According to some embodiments, the fluid composition is an aqueous NaOH composition.

[0203] According to some embodiments, the second fluid inlet pipe 112 comprises a valve (not shown) configured to monitor the liquid flow into the enclosed reaction chamber 130. According to some embodiments, the valve is configured to allow unidirectional flow of liquids into the enclosed reaction chamber 130.

[0204] According to some embodiments, a semi-permeable filter is positioned to separate between the reaction chamber 130 and the second fluid inlet pipe 112. According to some embodiments, the provision of the carbonated species chelator into the enclosed reaction chamber 130 through the second fluid inlet pipe 112 further comprises filtering the fluidcomposition from solids present therein, by flowing the fluid composition through the semi- permeable filter.

[0205] According to some embodiments, the second fluid inlet pipe 112 is located in the vicinity of the enclosed reaction chamber bottom end 134.

[0206] According to some embodiments, the pellet reactor 100 further comprises a semi- permeable filter (not shown), which is permeable to water but impermeable to solids above a predetermined diameter. According to some embodiments, the predetermined diameter is in the range of 1 micron to 3 mm, 10 micron to 3 mm or 50 micron to 3 mm. Each possibility represents a separate embodiment of the invention.

[0207] According to some embodiments, the semi-permeable filter is positioned to separate between the reaction chamber 130 and the fluid inlet pipe 110. According to some embodiments, the provision of the saline water into the enclosed reaction chamber 130 through the fluid inlet pipe 110 further comprises filtering the saline water from solids present therein, by flowing the carbonated water through the semi-permeable filter, and flowing the filtered water through the fluid inlet pipe 110.

[0208] Typically, pressurized gas or liquid enters the fluidized bed vessel through numerous holes via a plate known as a distributor plate, located at the bottom of the fluidized bed. The fluid flows upward through the bed, causing the solid particles to be suspended. If the inlet fluid is disabled, the bed may settle, pack onto the plate or trickle down through the plate. Many industrial beds use a sparger distributor instead of a distributor plate. The fluid is then distributed through a series of perforated tubes.

[0209] According to some embodiments, the pellet reactor 100 further comprises a distributor plate 190. According to some embodiments, the distributor plate 190 is configured to increase the flow of the saline water into the enclosed reaction chamber 130. According to some embodiments, the distributor plate 190 is configured to increase the flow of the saline water into the enclosed reaction chamber 130, so as to create a fluidized environment there within.

[0210] According to some embodiments, the distributor plate 190 is located in the vicinity of the enclosed reaction chamber bottom end 134. According to some embodiments, the fluid inlet pipe 110 is located in the vicinity of the enclosed reaction chamber bottom end 134. According to some embodiments, the distributor plate 190 is located between the connection of the fluid inlet pipe 110 to the pellet reactor 100 and the enclosed reaction chamber top end 132.

[0211] According to some embodiments, the carbonated species chelator is provided in step (II) as an aqueous composition. According to some embodiments, step (II) comprises providing an aqueous mixture of the carbonated species chelator.

[0212] According to some embodiments, step (II) comprises providing an aqueous mixture of the carbonated species chelator through the fluid inlet pipe 112.

[0213] According to some embodiments, the process comprises forming an aqueous solution of the chelator through electrodialysis.

[0214] According to some embodiments, the process comprises forming an aqueous solution of the chelator and flowing the mixture through the fluid inlet pipe 112 into the enclosed reaction chamber 130.

[0215] According to some embodiments, the fluid outlet pipe 120 is in fluid communication with the reaction chamber 130. According to some embodiments, the fluid outlet pipe 120 is connected to the reaction chamber 130. According to some embodiments, each of the fluid inlet pipe 110 and the fluid outlet pipe 120 is in fluid communication with the reaction chamber 130.

[0216] According to some embodiments, the fluid outlet pipe 120 comprises a valve (not shown) configured to monitor the liquid flow out of the enclosed reaction chamber 130. According to some embodiments, the valve is configured to allow unidirectional flow of liquids away from the enclosed reaction chamber 130.

[0217] According to some embodiments, the fluid outlet pipe 120 comprises a standard filter (not shown) which is permeable to water but impermeable to solids above a predetermined diameter, and prevents small seeds of the precipitate to leave the reaction chamber 130 through the fluid outlet pipe 120.

[0218] According to some embodiments, step (III) further comprises evacuating the water through the fluid outlet pipe 120. According to some embodiments, step (III) further comprises evacuating the water from the enclosed reaction chamber 130 through the fluid outlet pipe 120.

[0219] As further detailed above, step (III) comprises separating the precipitate from the water.

[0220] As can be understood by a person having ordinary skill in the art during step (III), the contents of the enclosed reaction chamber 130 include liquids (e.g., the decarbonated water) and solids (e.g., the CaCO3precipitate). In order to separate the precipitate from the water thesolid may simply be filtered from the liquid using a standard filter which is permeable to water but impermeable to solids above a predetermined diameter.

[0221] According to some embodiments, the pellet reactor 100 further comprises a semi- permeable filter (not shown), which is permeable to water but impermeable to solids above a predetermined diameter. According to some embodiments, the semi-permeable filter is positioned to separate between the reaction chamber 130 and the fluid outlet pipe 120. According to some embodiments, the evacuation of the water of step (III) further comprises filtering the water from the precipitate by flowing the water through the semi-permeable filter, and flowing the filtered water through the fluid outlet pipe 120.

[0222] According to some embodiments, step (III) further comprises filtering the decarbonated water from small CaCO3fines by flowing the decarbonated water through an additional semi-permeable filter (not shown), and flowing the filtered decarbonated water through the fluid outlet pipe 120. According to some embodiments, the additional semi- permeable filter has a cutoff of at least 1 micrometer. According to some embodiments, the additional semi-permeable filter has a cutoff of at least 5 micrometer. According to some embodiments, the additional semi-permeable filter has a cutoff of at least 10 micrometer. According to some embodiments, the additional semi-permeable filter has a cutoff of at least 15 micrometer. According to some embodiments, the additional semi-permeable filter has a cutoff of at least 25 micrometer.

[0223] According to some embodiments, the fluid outlet pipe 120 is located in the vicinity of the enclosed reaction chamber top end 132.

[0224] Specifically, it is preferable according to some embodiments, that the enclosed reaction chamber 130 is an elongated structure, wherein the fluid inlet pipe 110 is located in the vicinity of its bottom end 134 and the fluid outlet pipe 120 is located in the vicinity of its top end 132. Without wishing to be bound by any theory of mechanism of action, this structure allows to induce flow of the pressurized reactants provided in steps (I) and (II) from the bottom end 132 to the top end 134 of the enclosed reaction chamber 130. This results in high concentration of the decarbonated water in the vicinity of the enclosed reaction chamber top end 132, where it is evacuated, according to some embodiments. The bottom to top configurational considerations are further elaborated below, when discussing the nucleation seeding and solid system (e.g., the solid inlet pipe 140 and the solid outlet pipe 150).

[0225] Thus, according to some embodiments, the fluid outlet pipe 120 is connected to the reaction chamber 130 in the vicinity of its top end 132, and the fluid inlet pipe 110 is connected to the reaction chamber 130 in the vicinity of its bottom end 134.

[0226] According to some embodiments, the pellet reactor further comprises a solid outlet pipe 150. According to some embodiments, the precipitate is evacuated through the solid outlet pipe 150 thereby separating the precipitate from the water.

[0227] According to some embodiments, the solid outlet pipe 150 comprises a valve (not shown) configured to monitor the solid flow out of the enclosed reaction chamber 130. According to some embodiments, the valve is configured to allow unidirectional flow of solid away from the enclosed reaction chamber 130.

[0228] As detailed above, a mixture of solids and liquid may be present inside the enclosed reaction chamber 130, according to some embodiments. However, the solids and liquid may be easily separated. For example, the reaction chamber 130 can be drained from liquid through the filter and fluid outlet pipe 120 to keep mostly water-insoluble precipitate (e.g., CaCO3) in the chamber 130, and then evacuating the chamber 130 from the solids through the solid outlet 150. Thus, according to some embodiments, the present process comprises first evacuating the water from the enclosed reaction chamber 130 and then evacuating the solid water-insoluble precipitate therefrom.

[0229] It is to be understood by the person having ordinary skill in the art that typically solids precipitate into the bottom of a reaction vessel after a reaction, and thus they may be preferably evacuated from the bottom of the vessel. Thus, according to some embodiments, in order to achieve efficient separation of the solid water-insoluble precipitate from the water, the solid outlet pipe 150 is preferably located in the vicinity of the enclosed reaction chamber bottom end 134, above the distributor plate 190, according to some embodiments.

[0230] According to some embodiments, the solid outlet pipe 150 is connected to the reaction chamber 130 in the vicinity of its bottom end 134.

[0231] According to some embodiments, the pellet reactor 100 further comprises a solid inlet pipe 140. According to some embodiments, step (II) further comprises inserting nucleation seeds as described herein (e.g., seeds of the CaCCF, precipitate) into the reaction chamber 130 through the solid inlet pipe 140.

[0232] Some advantages of the nucleation seeding step are detailed above.

[0233] According to some embodiments, the solid inlet pipe 140 comprises a valve (not shown) configured to monitor the solid flow into the enclosed reaction chamber 130. According to some embodiments, the valve is configured to allow unidirectional flow of solids into the enclosed reaction chamber 130.

[0234] According to some embodiments, step (II) further comprises fluidizing the nucleation seeds in the reaction chamber 130.

[0235] According to some embodiments, step (II) further comprises fluidizing the nucleation seeds in the reaction chamber 130, thereby inducing precipitation formed from a chemical reaction between the carbonated species and the chelator.

[0236] The pellet reactor 100 may be a cylindrical fluidized bed reactor having elongated structure, according to some embodiments. According to some embodiments, the pellet reactor 100 may be with or without a conical shaped base. As detailed above, a solution of saline water (e.g., from seawater) and chelator (e.g. NaOH) may be fed into the lower part of the reaction chamber 130. Also, nucleation seeds of the precipitate (e.g., CaCO3seeds) may be added to the enclosed reaction chamber 130 from the solid inlet pipe 140 at the vicinity of the top of the reactor 132, according to some embodiments. The bottom-to-top pressurize stream of the reactant mixture results in fluidizing the nucleation seeds in the enclosed reaction chamber 130, according to some embodiments. This fluidization results in rapid precipitation over the nucleation seed, to form pellets of the precipitate in the pellet reactor 100. According to some embodiments, the chelator is NaOH which dissolves in the saline water, and subsequently elevating the pH, which in turn promotes deprotonation of bicarbonate ions to carbonate ions. Then, the increase of the pH increases the concentration of carbonate ions and promotes precipitation of CaCO3. This is further promoted by the nucleation seeds, which provide surface area for the precipitation reaction to occur, and grow in their diameter as it proceeds. Following precipitation of CaCO3, the concentration of inorganic carbon in the mixture within the reaction chamber 130 decreases as it flows toward the upper end 132 thereof, according to some embodiments. At the top of the enclosed reaction chamber 130 water is discharged through the fluid outlet pipe 120 and are further subjected to desalination, according to some embodiments. At the same time, due to the increase in the size of the nucleation seed crystals due to their maturation and growth, they become heavier and gradually sink to lower parts of the enclosed reaction chamber 130. Eventually, the largest seeds reach the bottom of the reactor where they are discharged through the solid outlet pipe 150. As further detailed below, these crystals or pellets, may then be further processed (e.g., in step (Via)) for supplementing the desalinatedwater with calcium mineral, according to some embodiments. To maintain the number of CaCO3seeds within the enclosed reaction chamber 130 constant, new nucleation seeds may be periodically or continuously added to the enclosed reaction chamber 130, through the solid inlet pipe 140, to compensate for the ones that are discharged as pellets, according to some embodiments. The new seeds may be obtained from crushing large pellets and / or CaCO3from any one of the steps of the present process, according to some embodiments.

[0237] According to some embodiments, the nucleation seeds include crystals having a first average diameter. According to some embodiments, the precipitate CaCO3species formed in step (II) includes pellets having a second average diameter. According to some embodiments, the CaCO3seeds include crystals having a first average diameter. According to some embodiments, the CaCO3formed in step (II) includes pellets having a second average diameter.

[0238] The differences in diameter are indicated in Figure 2, which shows the precipitate formed in the reaction of step (II) as large stars, which sink towards the bottom end 134 of the reaction chamber 130, and the nucleation seeds inserted to the reaction chamber 130 through the solid inlet pipe 140, as smaller stars, which are fluidized.

[0239] According to some embodiments, the second diameter is at least 50%, at least 100%, at least 200%, at least 500%, or at least 1000% larger than the first diameter.

[0240] According to some embodiments, the solid inlet pipe 140 is connected to the reaction chamber 130.

[0241] According to some embodiments, the fluidized bed pellet reactor 100 comprises: a fluid inlet pipe 110, a solid inlet pipe 140, a fluid outlet pipe 120, a solid outlet pipe 150 and an enclosed reaction chamber 130, which comprises a top end 132 and a bottom end 134, wherein the solid inlet pipe 140 is connected to the reaction chamber 130, the fluid outlet pipe 120 is connected to the reaction chamber 130 in the vicinity of its top end 132, and each of the solid outlet pipe 150 and the fluid inlet pipe 110 is connected to the reaction chamber 130 in the vicinity of its bottom end 134; wherein the saline water comprises Ca+2cations and at least HCO3- , and the chelator comprises NaOH; step (II) comprises: inserting the basic NaOH solution formed in step (V) into the reaction chamber 130 through the fluid inlet pipe 110; inserting CaCO3seeds into the reaction chamber 130 through the solid inlet pipe 140 and fluidizing said seeds, thereby inducing precipitation of CaCO3formed from a chemical reaction between the HCO3- and the NaOH in the presence of the Ca+2cations, so that the formed CaCO3is sinking to the bottom end 134 of the reaction chamber 130 and the water flows to the vicinity of the topend 132 of the reaction chamber 130; and evacuating the water for desalination from the top end 132 of the reaction chamber 130 through the fluid outlet pipe 120; and step (III) comprises evacuating the CaCO3from the bottom end 134 of the reaction chamber 130 through the solid outlet pipe 150.

[0242] According to some embodiments, step (II) further comprises inserting seeds of the CaCO3precipitate into the reaction chamber 130 through the solid inlet pipe 140 and fluidizing the seeds in the reaction chamber 130 to a fluidized grains height 136, thereby inducing precipitation and maturation of solid CaCO3pellets. According to some embodiments, the carbon dioxide scavenger is NaOH, wherein the fluidized bed pellet reactor 100 further comprises a solid inlet pipe 140, wherein step (III) further comprises inserting seeds of the CaCO3into the reaction chamber 130 through the solid inlet pipe 140 and fluidizing the seeds in the reaction chamber to a fluidized grains height, thereby inducing precipitation and maturation of CaCO3pellets.

[0243] The term “fluidized grains height”, which is commonly referred as “fluidized bed height”, as used herein refers to the distance between the bottom pellets (positioned on the distributor plate 190) and the most elevated fluidized seeds, as portrayed in Figure 2, element 136.

[0244] According to some embodiments, the fluidized grains height 136 is in the range of 0.5 meter to 12 meters, including each value and sub-range within the specified range. According to some embodiments, the fluidized grains height 136 is in the range of 0.5 meter to 1 meter. According to some embodiments, the fluidized grains height 136 is in the range of 0.5 meter to 2 meter. According to some embodiments, the fluidized grains height 136 is in the range of 0.75 meter to 2.5 meter. According to some embodiments, the fluidized grains height 136 is in the range of 0.75 meter to 3.5 meter. According to some embodiments, the fluidized grains height 136 is in the range of 1 meter to 2 meter. According to some embodiments, the fluidized grains height 136 is in the range of 1 meter to 3 meter. According to some embodiments, the fluidized grains height 136 is in the range of 1.5 meter to 3 meter. According to some embodiments, the fluidized grains height 136 is in the range of 1.5 meter to 4 meter. According to some embodiments, the fluidized grains height 136 is in the range of 2 meter to 4 meter. According to some embodiments, the fluidized grains height 136 is in the range of 2 meter to 5 meter. According to some embodiments, the fluidized grains height 136 is in the range of 2.5 meter to 5 meter. According to some embodiments, the fluidized grains height 136 is in the range of 2.5 meter to 6 meter. According to some embodiments, the fluidized grains height 136 is inthe range of 3 meter to 5 meter. According to some embodiments, the fluidized grains height 136 is in the range of 3 meter to 6 meter. According to some embodiments, the fluidized grains height 136 is in the range of 4 meter to 7 meter. According to some embodiments, the fluidized grains height 136 is in the range of 4 meter to 8 meter. According to some embodiments, the fluidized grains height 136 is in the range of 5 meter to 9 meter. According to some embodiments, the fluidized grains height 136 is in the range of 5 meter to 10 meter. According to some embodiments, the fluidized grains height 136 is in the range of 6 meter to 10 meter. According to some embodiments, the fluidized grains height 136 is in the range of 6 meter to 12 meter. According to some embodiments, the fluidized grains height 136 is in the range of 9 meter to 12 meter.

[0245] According to some embodiments, the fluidized grains height 136 is at least 0.5 meter.According to some embodiments, the fluidized grains height 136 is at least 1 meter. According to some embodiments, the fluidized grains height 136 is at least 1.5 meter. According to some embodiments, the fluidized grains height 136 is at least 2 meter. According to some embodiments, the fluidized grains height 136 is at least 2.5 meter. According to some embodiments, the fluidized grains height 136 is at least 3 meter. According to some embodiments, the fluidized grains height 136 is at least 3.5 meter. According to some embodiments, the fluidized grains height 136 is at least 4 meter. According to some embodiments, the fluidized grains height 136 is at least 4.5 meter. According to some embodiments, the fluidized grains height 136 is at least 5 meter. According to some embodiments, the fluidized grains height 136 is at least 5.5 meter. According to some embodiments, the fluidized grains height 136 is at least 6 meter.

[0246] According to some embodiments, the fluidized grains height 136 is no more than 12 meter. According to some embodiments, the fluidized grains height 136 is no more than 11 meter. According to some embodiments, the fluidized grains height 136 is no more than 10 meter. According to some embodiments, the fluidized grains height 136 is no more than 9 meter.According to some embodiments, the fluidized grains height 136 is no more than 8 meter.According to some embodiments, the fluidized grains height 136 is no more than 7 meter.According to some embodiments, the fluidized grains height 136 is no more than 6 meter.According to some embodiments, the fluidized grains height 136 is no more than 5 meter.According to some embodiments, the fluidized grains height 136 is no more than 4 meter.According to some embodiments, the fluidized grains height 136 is no more than 3 meter.

[00247] It is to be understood that the steps of the present process may occur alternately or simultaneously in a flow-type process.

[0248] According to some embodiments, fluidizing said seeds in step (II) entails providing a pressurized stream of the saline water through the distributor plate 190 in the direction from the enclosed reaction chamber bottom end 134 to the enclosed reaction chamber top end 132.

[0249] According to some embodiments, the process comprises step (Via) of contacting the HC1 formed in step (V) with at least a portion of the separated CaCO3precipitate of step (III) to form CaCl2and CO2. According to some embodiments, the CO2formed in step (Via) is in the gas form. According to some embodiments, the CO2gas is isolated from the mixture and stored. According to some embodiments, the CO2gas is stored in a dedicated container (not shown) or designated storage site (such as underground geological formations, not shown). Suitable containers for CO2storage, include, but not limited to gas cylinders. Other storage processes include, but are not limited to, condensing the CO2, (e.g., liquidating it) and storing it as a condensed state within depleted oil or gas fields or saline aquifers, or injecting it to geological formations made of silicate rocks, thereby leading to chemical mineralization of the CO2. Each possibility represents a separate embodiment of the invention.

[0250] According to some embodiments, the process comprises dissolving a portion of the CaCO3in an aqueous acidic composition comprising the carbon dioxide formed in step (Via); and admixing the solution with the desalinated water, thereby supplementing the desalinated water with calcium ions and carbonated species.

[0251] According to some embodiments, the dissolution of the portion of the CaCO3in the aqueous acidic carbon dioxide composition, entails performing an acid-base chemical reaction.

[0252] According to some embodiments, the acid-base chemical reaction it represented by Scheme I.

[0253] Scheme I:

[0254] CaCO3+ CO2+ H2O Ca(HCO3)2.

[0255] According to some embodiments, the CaCO3in Scheme I is in a solid state. According to some embodiments, the carbon dioxide in Scheme I is at least partially dissolved in water. According to some embodiments, the carbon dioxide in Scheme I is dissolved in water. According to some embodiments, the water in Scheme I in a liquid state. According to someembodiments, the Ca(HCO3)2 in Scheme I is at least partially dissolved in water. According to some embodiments, the Ca(HCO3)2 in Scheme I is dissolved in water.

[0256] It is to be understood that upon dissolution in water carbon dioxide is at least partially in the form of carbonic acid H2CO3. Thus, Scheme I may be also portrayed as shown in Scheme la.

[0257] Scheme la:

[0258] CaCO3+ H2CO3Ca(HCO3)2.

[0259] According to some embodiments, there is provided a system as disclosed herein.

[0260] Specific reference is now made to step (III) of the present process. According to some embodiments, the present process comprises step (III) of separating the CaCO3precipitate of step (II) from the decarbonated water. According to some embodiments, step (III) is also represented as step 1020 and step 1030 in Figure 1A and Figure IB.

[0261] According to some embodiments, step (III) comprises isolating the CaCO3precipitate. According to some embodiments, step (III) comprises isolating the decarbonated water.

[0262] According to some embodiments, in step (III) any solid-liquid separation process can be utilized, for example filtration, decantation, and the like.

[0263] According to the principles of the present invention, the separated precipitate is recovered. According to the principles of the present invention, at least a portion of the separated precipitate is recovered. According to some embodiments, at least a portion of the separated precipitate is reused.

[0264] Within the scope of the present invention is the recovery and reuse of the precipitate to re-mineralize the water that underwent desalination. The World Health Organization recommends the inclusion of calcium ions in desalinated and naturally soft due to their acknowledged public health beneficial effects. Calcium ions are typically added to desalinated waters in a "post treatment" step, typically through the addition of dissolved CaCO3which releases to the water both Ca2+ions and carbonate alkalinity. Thus, according to some embodiments, the separated precipitate of step (III) is dissolved and the solution admixed with the desalinated water thereby supplementing the desalinated water with calcium and carbonate ions. Reference to this remineralization process is made in Figure 1C, step 1240.

[0265] According to some embodiments, the reuse comprises dissolving at least a portion of the precipitate and admixing the solution with the desalinated water thereby supplementing the desalinated water with essential ions.

[0266] According to some embodiments, the process comprises dissolving a portion of the CaCO3in an aqueous acidic composition thereby supplementing the desalinated water with calcium ions and carbonated species.

[0267] According to some embodiments, the process further comprises dissolving at least a portion of the separated CaCO3precipitate of step (III) and admixing the solution with the desalinated water of step (IV) thereby supplementing the desalinated water with essential Ca+2ions.

[0268] According to some embodiments, the process further comprises dissolving at least a portion of the separated CaCO3precipitate of step (III) and admixing the solution with the desalinated water of step (IV) and an acidic composition, thereby supplementing the desalinated water with essential Ca+2ions.

[0269] According to some embodiments, the acidic composition is an acidic CO2composition. It is to be understood that “acidic CO2composition” may include, but not limited to, a solution of CO2dissolved (e.g., as H2CO3) in water, or CO2(e.g., as gas), which is added into the desalinated water of step (IV) or to the mixture thereof with CaCO3. Each possibility represents a separate embodiment of the invention.

[0270] According to some embodiments, the acidic CO2composition comprises the carbon dioxide formed in step (Via). According to some embodiments, the acidic CO2composition is the carbon dioxide formed in step (Via).

[0271] According to some embodiments, the process further comprises dissolving at least a portion of the separated CaCO3precipitate of step (III) and admixing the solution with the desalinated water of step (IV) and CO2, thereby supplementing the desalinated water with essential Ca+2ions.

[0272] According to some embodiments, the process further comprises dissolving at least a portion of the separated CaCO3precipitate of step (III) and admixing the solution with the desalinated water of step (IV) and a portion of the CO2formed in step (Via) thereby supplementing the desalinated water with essential Ca+2ions.

[0273] According to some embodiments, the dissolution of the portion of the CaCO3in the aqueous acidic carbon dioxide composition, entails performing an acid-base chemical reaction.

[0274] According to some embodiments, the acid-base chemical reaction it represented by Scheme I.

[0275] Scheme I:

[0276] CaCO3+ CO2+ H2O Ca(HCO3)2.

[0277] According to some embodiments, the CaCO3in Scheme I is in a solid state. According to some embodiments, the carbon dioxide in Scheme I is at least partially dissolved in water. According to some embodiments, the carbon dioxide in Scheme I is dissolved in water. According to some embodiments, the water in Scheme I in a liquid state. According to some embodiments, the Ca(HCO3)2in Scheme I is at least partially dissolved in water. According to some embodiments, the Ca(HCO3)2in Scheme I is dissolved in water.

[0278] It is to be understood that upon dissolution in water carbon dioxide is at least partially in the form of carbonic acid H2CO3. Thus, Scheme I may be also portrayed as shown in Scheme la.

[0279] Scheme la:CaCO3+ H2CO3Ca(HCO3)2.

[0280] According to some embodiments, the process comprises step (Via), wherein a portion of the CO2formed upon the reaction between the HC1 and the separated CaCO3precipitate is employed in the dissolution of the portion of the separated CaCO3precipitate.

[0281] Specific reference is now made to step (IV) of the present process. According to some embodiments, the present process comprises step (IV) of desalinating the decarbonated water of step (III). According to some embodiments, step (IV) is also represented as step 1040 in Figure 1A and Figure IB.

[0282] According to some embodiments, the present process comprises step (IV) of desalinating the decarbonated water entails forming desalinated water (step 1050 in Figures 1A, IB and 1C) and brine (step 1060 in Figures 1A and IB). According to some embodiments, the brine comprises NaCl.

[0283] Typically, according to some embodiments, desalination processes include flowing of the pre-desalinated water stream through a desalination membrane. The aqueous streampassing the membrane is called the permeate stream, and is salt (typically mostly NaCl) depleted compared to the water entering the membrane. This stream formed the basis for the desalinated water, as further processes (e.g., further filtering and / or remineralization) may be performed thereon. The aqueous stream retained at the membrane is called the retentate stream, and is salt enriched compared to the water entering the membrane. This stream is also called brine, due to its high salt concentration.

[0284] According to some embodiments, the desalinating of step (IV) entails reducing the total salt concentration within the water by at least 30%, at least 40%, at least 50%, at least 60%, at least 70% or at least 80%. Each possibility represents a separate embodiment of the invention.

[0285] According to some embodiments, the saline water of step (I) has a saline water NaCl concentration. According to some embodiments, the desalinated water has a desalinated water NaCl concentration. According to some embodiments, the brine has brine NaCl concentration. According to some embodiments, the saline water NaCl concentration is higher than the desalinated water NaCl concentration. According to some embodiments, the saline water NaCl concentration and lower than the brine NaCl concentration.

[0286] According to some embodiments, the saline water NaCl concentration is at least 10% higher than the desalinated water NaCl concentration. According to some embodiments, the saline water NaCl concentration is at least 25% higher than the desalinated water NaCl concentration. According to some embodiments, the saline water NaCl concentration is at least 50% higher than the desalinated water NaCl concentration. According to some embodiments, the saline water NaCl concentration is at least 100% higher than the desalinated water NaCl concentration. According to some embodiments, the saline water NaCl concentration is at least 150% higher than the desalinated water NaCl concentration. According to some embodiments, the saline water NaCl concentration is at least 200% higher than the desalinated water NaCl concentration. According to some embodiments, the saline water NaCl concentration is at least 300% higher than the desalinated water NaCl concentration. According to some embodiments, the saline water NaCl concentration is at least 400% higher than the desalinated water NaCl concentration. According to some embodiments, the saline water NaCl concentration is at least 500% higher than the desalinated water NaCl concentration.

[0287] According to some embodiments, the brine NaCl concentration is at least 10% higher than the desalinated water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 25% higher than the desalinated water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 50% higher than the desalinatedwater NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 100% higher than the desalinated water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 150% higher than the desalinated water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 200% higher than the desalinated water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 300% higher than the desalinated water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 400% higher than the desalinated water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 500% higher than the desalinated water NaCl concentration.

[0288] According to some embodiments, the brine NaCl concentration is at least 10% higher than the saline water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 25% higher than the saline water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 50% higher than the saline water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 100% higher than the saline water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 150% higher than the saline water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 200% higher than the saline water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 300% higher than the saline water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 400% higher than the saline water NaCl concentration. According to some embodiments, the brine NaCl concentration is at least 500% higher than the saline water NaCl concentration.

[0289] According to some embodiments, desalinating the water comprises reverse osmosis. According to some embodiments, desalinating the water comprises a single reverse osmosis cycle. According to some embodiments, desalinating the water comprises two reverse osmosis cycles. According to some embodiments, desalinating the water comprises at least two reverse osmosis cycles. According to some embodiments, desalinating the water comprises two reverse osmosis cycles wherein the second reverse osmosis cycle is performed on a portion of the permeate of the first reverse osmosis cycle. According to some embodiments, desalinating the water comprises two reverse osmosis cycles wherein the second reverse osmosis cycle is performed on a portion constituting 70% or less of the permeate of the first reverse osmosis cycle. According to some embodiments, desalinating the water comprises two reverse osmosis cycles wherein the second reverse osmosis cycle is performed on a portion constituting 50% orless of the permeate of the first reverse osmosis cycle. According to some embodiments, desalinating the water comprises two reverse osmosis cycles wherein the second reverse osmosis cycle is performed on a portion constituting 30% or less of the permeate of the first reverse osmosis cycle.

[0290] According to some embodiments, boron species concentrations following the process of the present invention and a single reverse osmosis cycle are less than 1.5 mg / L. According to some embodiments, boron species concentrations following the process of the present invention and a single reverse osmosis cycle are in the range of about 0.1 to about 1.5 mg / L, including each value within the specified range.

[0291] Advantageously, the process of the present invention affords desalinated water with reduced undesired boron levels such that it either obviates the second pass in the SWRO desalination process or reduces the water flow in the second pass such that only a portion of the water is required to undergo the second pass. Furthermore, the process of the present invention also affords a smaller dosage of caustic addition in order to retain product boron specification. Finally, the need for chemical reagents is minimized by recycling and reusing the by-products obtained in the process.

[0292] According to some embodiments, any one of the processes of the present invention entails enhancing the removal of boron species from saline water undergoing desalination. According to some embodiments, the saline comprises a boron species at a first boron species concentration and step (IV) comprises desalinating the decarbonated water of step (III) to form desalinated water having a second boron species concentration which is lower than the first boron species concentration.

[0293] According to some embodiments, the boron species comprises boric acid.

[0294] According to some embodiments, admixing the carbonated species chelator with the saline water in step (II), entails increasing hydroxide ion concentration within the water. According to some embodiments, upon the admixing in step (II) hydroxide ions within the water react with the boric acid to form a borate. According to some embodiments, upon admixing the NaOH chelator with the saline water, the hydroxide ions within the mixture of step (II) react with the boric acid to form a borate.

[0295] According to some embodiments, upon the admixing the following reaction is taking place:

[0296] B(OH)3+ OH-→nnwB(OH )4- .

[0297] According to some embodiments, the desalination of step (IV) entails passing the water of step (III) through a selective membrane. According to some embodiments, the selective membrane selectively prevents passage of borate over boric acid, thereby reducing the boron species concentration withing the water. According to some embodiments, passing the water of step (III) through the selective membrane further reduces the total salt concentration within the water of step (III), thereby desalinating the water and reducing its boron species concentration in one step.

[0298] According to some embodiments, the selective separation of the selective membrane is based on ion size.

[0299] Specifically, as can be appreciated by the person having ordinary skill in the art, typical desalination processes are based on passing saline water through selective membrane that selectively prevent passage of large ions, thereby forming a salt enriched fractions, which does not pass the membrane, and a salt depleted at the selective membrane outlet. In addition, one of the drawbacks of the known procedures is that boric acid has a small enough diameter to penetrate through the membrane. Advantageously, upon carrying out the process of the present invention, the boric acid is transformed into borate, which has an ionic diameter larger than that of boric acid and is selectively filtered out of the desalinated water upon passage through the desalination membrane.

[0300] According to some embodiments, the decarbonated water of step (III) comprises at least one boron species at a first total boron species concentration. According to some embodiments, the saline water of step (I) comprises at least one boron species at a first total boron species concentration.

[0301] The term “first total boron species concentration” is used herein in some embodiments to describe the concentration of the total boron species in the saline water of step(I) and is some embodiment to describe the concentration of the total boron species in the decarbonated water of step (III). Specifically, between steps (I) and (III) boron may change its form (e.g., from boric acid to borate), but not its total quantity, according to some embodiments. As the total volume of the water is not significantly altered by the addition of the chelator in step(II), it is hypothesized that the concentration of the total boron species in the saline water of step (I) and the concentration of the total boron species in the decarbonated water of step (III) are comparable.

[0302] The term “comparable” is intended to refer to two values differing one from the other by up to 25%.

[0303] According to some embodiments, the decarbonated water of step (III) comprises borate.

[0304] According to some embodiments, the desalinated water formed in step (IV) has a second total boron species concentration, which is at least 10% lower than the first total boron species concentration. According to some embodiments, the desalinated water formed in step (IV) has a second total boron species concentration, which is at least 20% lower than the first total boron species concentration. According to some embodiments, the desalinated water formed in step (IV) has a second total boron species concentration, which is at least 30% lower than the first total boron species concentration. According to some embodiments, the desalinated water formed in step (IV) has a second total boron species concentration, which is at least 40% lower than the first total boron species concentration. According to some embodiments, the desalinated water formed in step (IV) has a second total boron species concentration, which is at least 50% lower than the first total boron species concentration. According to some embodiments, the desalinated water formed in step (IV) has a second total boron species concentration, which is at least 60% lower than the first total boron species concentration. According to some embodiments, the desalinated water formed in step (IV) has a second total boron species concentration, which is at least 70% lower than the first total boron species concentration. According to some embodiments, the desalinated water formed in step (IV) has a second total boron species concentration, which is at least 80% lower than the first total boron species concentration. According to some embodiments, the desalinated water formed in step (IV) has a second total boron species concentration, which is at least 90% lower than the first total boron species concentration. It is to be understood that, according to some embodiments, the first total boron species concentration refers to the saline water of step (I) and according to some embodiments, the first total boron species concentration refers to the decarbonated water of step (III).

[0305] According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination comprises at least 10% more reduction in boron species content after a single reverse osmosis cycle as compared to the reduction in the absence of steps (II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination comprises at least 20% more reduction in boron species content after a single reverse osmosis cycle as compared to the reduction in the absence of steps(II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination comprises at least 30% more reduction in boron species content after a single reverse osmosis cycle as compared to the reduction in the absence of steps (II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination comprises at least 40% more reduction in boron species content after a single reverse osmosis cycle as compared to the reduction in the absence of steps (II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination comprises at least 50% more reduction in boron species content after a single reverse osmosis cycle as compared to the reduction in the absence of steps (II) and (III).

[0306] According to the principles of the present invention, improved boron removal is achieved by utilizing the process of the present invention. For example, according to some embodiments, the boron concentrations after a single RO cycle no more than 1.5 mg / L. According to some embodiments, the boron concentrations after a single RO cycle no more than 1.2 mg / L. According to some embodiments, the boron concentrations after a single RO cycle no more than 1 mg / L. According to some embodiments, the boron concentrations after a single RO cycle no more than 0.8 mg / L. According to some embodiments, the boron concentrations after a single RO cycle no more than 0.5 mg / L. According to some embodiments, the boron concentrations after a single RO cycle in the range of 0.1 to 1.5 mg / L. According to some embodiments, the boron concentrations after a single RO cycle are in the range of 0.5 to 1.5 mg / L.

[0307] According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination comprises at least 10%, 20%, 30%, 40%, 50% or more reduction in boron species content after a single reverse osmosis cycle as compared to the reduction in the absence of steps (II) and (III). Thus, while the second reverse osmosis cycle can be eliminated due to the pre-treatment of the water, in some embodiments, the second reverse osmosis cycle is performed on a portion of the water that has been subjected to the first reverse osmosis cycle. According to some embodiments, the portion of water undergoing the second reverse osmosis cycle is 70% or less of the permeate of the first reverse osmosis cycle. According to some embodiments, the portion of water undergoing the second reverse osmosis cycle is 50% or less of the permeate of the first reverse osmosis cycle. According to some embodiments, the portion of water undergoing the second reverse osmosis cycle is 30% or less of the permeate of the first reverse osmosis cycle.

[0308] According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination allows reduction of at least 10% of the portion of water undergoing the second reverse osmosis cycle as compared to the portion in the absence of steps (II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination allows reduction of at least 20% of the portion of water undergoing the second reverse osmosis cycle as compared to the portion in the absence of steps (II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination allows reduction of at least 30% of the portion of water undergoing the second reverse osmosis cycle as compared to the portion in the absence of steps (II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination allows reduction of at least 40% of the portion of water undergoing the second reverse osmosis cycle as compared to the portion in the absence of steps (II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination allows reduction of at least 50% of the portion of water undergoing the second reverse osmosis cycle as compared to the portion in the absence of steps (II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination allows reduction of at least 70% of the portion of water undergoing the second reverse osmosis cycle as compared to the portion in the absence of steps (II) and (III). According to some embodiments, enhancing the removal of boron species from saline water undergoing desalination allows reduction of at least 90% of the portion of water undergoing the second reverse osmosis cycle as compared to the portion in the absence of steps (II) and (III).

[0309] Specific reference is now made to step (V) of the present process. According to some embodiments, the present process comprises step (V) of performing an electrodialysis of the brine of step (IV). According to some embodiments, step (V) is also represented as step 1070 in Figure 1A and IB.

[0310] According to some embodiments, step (V) includes a pre-treatment of the brine to remove divalent ions that may be harmful to ion exchange and bipolar membranes. According to some embodiments, removal of divalent ions is performed by softening, nanofiltration, ion exchange or other method.

[0311] According to some embodiments, the electrodialysis of the brine results in the formation of an acidic solution of HC1 (step 1090 in Figures 1A and IB). According to someembodiments, the electrodialysis of the brine results in the formation of a basic solution of NaOH (step 1080 in Figures 1A and IB).

[0312] According to some embodiments, the brine electrodialysis of step (V) further entails forming deionized brine (step 1100 in Figure IB).

[0313] According to some embodiments, the process further comprises repeating steps (I) to (IV) in a consecutive cycle, wherein consecutive step (IV) comprises desalinating a combination of the deionized brine of consecutive step (V) and the decarbonated water of consecutive step (III) to form desalinated water and brine (broken arrow between step 1100 and step 1040 in Figure IB).

[0314] Reference is now made to Figure 3, which shows the electrodialysis system, according to some embodiments.

[0315] The electrodialysis system of Figure 3 is a standard electrodialysis system, which is configured to form an acidic solution of HC1 and a basic solution of NaOH from the brine of step (IV). Electrodialysis apparatuses are typically composed of two electrodes, an anode and a cathode, separated from one another by one or more ion-selective membranes. Ion-selective membranes suitable for use in the present invention include, but are not limited to, anionselective, cation-selective and bipolar membranes. Each possibility represents a separate embodiment.

[0316] Thus, the system comprises an anode, a cathode, an anion exchange membrane, a cation exchange membrane, a brine chamber and acid chamber and a base chamber, according to some embodiments. According to some embodiments, the anion exchange membrane is positioned to separate between the brine chamber and the anode, wherein the acid chamber is defined there between. According to some embodiments, upon application of electric potential, the negative chloride ions of the brine flow toward the anode and are separated from the brine chamber in the acid chamber as HC1. According to some embodiments, the cation exchange membrane is positioned to separate between the brine chamber and the cathode, wherein the base chamber is defined there between. According to some embodiments, upon application of electric potential, the positive sodium ions of the brine flow toward the cathode and are separated from the brine chamber in the base chamber as NaOH.

[0317] According to certain embodiments, electrodialysis in step (V) is bipolar membrane electrodialysis (BPED). In some embodiments, electrodialysis in step (V) is electroelectrodialysis (EED).

[0318] In some embodiments, the brine, comprising the monovalent NaCl salt separated from the desalinated water is introduced into the brine chamber and the monovalent Na+cations are transported from the brine chamber to the base chamber through the cation exchange membrane to produce a base NaOH solution comprising the monovalent Na+cations. Simultaneously, Cl’ anions are transported through the anion exchange membrane to the acid chamber to produce the acid solution comprising the hydrochloric acid, HC1. The respective base and acid solutions can then be utilized for further processes, as described herein.

[0319] In other embodiments, the brine comprising the monovalent NaCl salt is introduced into the brine chamber where the acid is formed and the monovalent Na+cations are transported from the brine chamber to the base chamber through the cation exchange membrane to produce a base solution comprising the monovalent Na+cations. In other embodiments, the brine comprising the monovalent NaCl salt is introduced into the brine chamber where the acid is formed and the monovalent Cl’ anions are transported from the brine chamber to the acid chamber through the anion exchange membrane to produce an acid solution comprising the monovalent Cl’ anions.

[0320] Within the scope of the present invention are electrodialysis modes of operation such as water-splitting electrodialysis (WSED), electro-electrodialysis (EED), and bipolar membrane electrodialysis (BPED). Each possibility represents a separate embodiment. Currently preferred is the use of BPED whereby a bipolar membrane is utilized to convert a saline solution comprising the monovalent salt into the corresponding acid and base under the influence of an electrical field.

[0321] Typically, the flow rate at which the brine is introduced into the brine chamber is for example at least 1 dm3 / h, at least 10 dm3 / h, at least 100 dm3 / h, or at least 1000 dm3 / h, according to some embodiments. Each possibility represents a separate embodiment of the invention. The flow rates may be, according to some embodiments, between about 1 to about 10000 dm3 / h, for example about 10 to about 5000 dm3 / h, including each value within the specified ranges. Exemplary flow rates include, but are not limited to, about 1, about 5, about 10, about 20, about 30, about 40, about 50, about 60, about 70, about 80, about 90, about 100, about 200, about 300, about 400, about 500, about 600, about 700, about 800, about 900, about 1000 dm3 / h, about 2000 dm3 / h, about 3000 dm3 / h, about 4000 dm3 / h, about 5000 dm3 / h , about 6000 dm3 / h, about 7000 dm3 / h, about 8000 dm3 / h, about 9000 dm3 / h, about 10000 dm3 / h. Each possibility represents a separate embodiment.

[0322] While electrodialysis can be performed at room temperatures, it can also be performed at elevated temperatures. Suitable temperatures at which electrodialysis can be performed include from about 20°C to about 80°C, for example from about 40°C to about 70°C, including each value within the specified ranges. Exemplary temperatures for performing the electrodialysis include, but are not limited to, about 20°C, about 25°C, about 30°C, about 35°C, about 40°C, about 45°C, about 50°C, about 55°C, about 60°C, about 65°C, about 70°C, about 75°C, and about 80°C. Each possibility represents a separate embodiment.

[0323] As contemplated herein, in some embodiments, step (V) comprises performing an electrolysis of the brine of step (IV). According to some embodiments, the electrolysis it a chloralkali process. In accordance with these embodiments, the chloride ions of the brine undergo oxidation on the anode to form chlorine (Ch). At the cathode, water is reduced to hydroxide and hydrogen gas. The net process is the electrolysis of an aqueous solution of NaCl into sodium hydroxide (NaOH), hydrogen gas, and chlorine gas. Thus, according to some embodiments, step (V) comprises performing an electrolysis of the brine of step (IV) to form a basic solution of NaOH, hydrogen gas, and chlorine gas. According to some embodiments, step (VIb) comprises repeating steps (I) to (IV) in a consecutive cycle, by using the NaOH formed by the electrolysis of step (V) as the carbonated species chelator of the consecutive step (II).

[0324] Specific reference is now made to step (Via) of the present process. According to some embodiments, the present process comprises step (Via) of contacting the HC1 formed in step (V) with at least a portion of the separated CaCO3precipitate of step (III). According to some embodiments, step (Via) is also represented by the arrow between 1090 and 1020 in Figure IB.

[0325] According to some embodiments, the contacting of the HC1 and the CaCO3precipitate entails forming CaCl2(1200 in Figure 1C). According to some embodiments, the contacting of the HC1 and the CaCO3precipitate entails forming CO2(1210 in Figure 1C).

[0326] The net reaction is described in Scheme II:

[0327] Scheme II

[0329] According to some embodiments, the process further comprises sequestering the CO2(1290 in Figure 1C).

[0330] According to some embodiments, the process comprises step (Via).

[0331] According to some embodiments, the process further comprises a step of isolating the CaCl2formed in step (Via).

[0332] According to some embodiment, a portion of the isolated CaCl2formed in step (Via) is used to supplement the saline water of consecutive step (I) with Ca+2ions.

[0333] According to some embodiments, isolating the CaCl2comprises dehydrating an aqueous CaCl2composition (e.g., slurry) formed in step (Via).

[0334] According to some embodiments, the process further comprises a step of dehydrating the CaCl2formed in step (Via).

[0335] According to some embodiments, the process further comprises a step of dehydrating and storing the CaCl2formed in step (Via). Specifically, CaCl2has commercial value, inter alia, as a concrete additive, desiccant and road surfacing agent).

[0336] According to some embodiments, the process further comprises a step of isolating the CO2formed in step (Via).

[0337] According to some embodiments, the process further comprises a step of isolating and storing the CO2formed in step (Via) thereby achieving Carbon Capture and Storage (CCS) or carbon removal. This step is represented as step 1230 in Figure 1C.

[0338] In addition, a portion of the CO2formed in step (Via) may be used as detailed herein for the remineralization of the desalinated water. This is elaborated above. In short, according to some embodiments, a portion of the CO2formed in step (Via) may be mixed with a portion of the CaCO3precipitated in step (II) and the desalinated water of step (VI).

[0339] According to some embodiments, this may lead to an acid-base type chemical reaction represented by Scheme I and Scheme IA:

[0340] Scheme I:

[0341] CaCO3+ CO2+ H2O Ca(HCO3)2.

[0342] It is to be understood that upon dissolution in water carbon dioxide is at least partially in the form of carbonic acid H2CO3. Thus, Scheme I may be also portrayed as shown in Scheme la.

[0343] Scheme la:

[0344] CaCO3+ H2CO3Ca(HCO3)2.

[0345] The formation of the more soluble calcium bicarbonate salt enables reconstitution of some of the calcium ions to the desalinated water, which may advantageously form mineral water, according to some embodiments.

[0346] Specific reference is now made to step (VIb) of the present process. According to some embodiments, the present process comprises step (VIb) of repeating steps (I) to (IV) in a consecutive cycle, by using the NaOH formed in step (V) as the carbonated species chelator of a consecutive step (II). According to some embodiments, step (Via) is also represented as the line from 1080 to 1010 in Figure 1A.

[0347] According to some embodiments, the process comprises step (VIb).

[0348] In general, the consecutive cycle of steps according to the present process may have a similar characterization as characterized herein for the base steps, according to some embodiments.

[0349] The main salt in saline water is NaCl. As a result, the electrodialysis of step (V) is performed over a concentrated aqeous NaCl, which, in return results in the formation of an NaOH solution. The NaOH solution is an appropriate carbonated species chelator for the consecutive step(s) (II), according to some embodiments. However, according to some embodiments, NaOH does not include the calcium (Ca+2) cations required for the precipitation of CaCO3. As a result, according to some embodiments, consecutive step (II), when performed with NaOH solution as chelator, requires that the saline water provided in consecutive step (I) comprises Ca+2. According to some embodiments, the saline water provided in consecutive step (I) comprises Ca+2at a sufficient amount for the precipitation of consecutive step (II). According to some embodiments, consecutive step (I) comprises supplementing the saline water provided therein with a soluble Ca+2salt to reach sufficient amount of Ca+2ions for the precipitation of consecutive step (II). According to some embodiments, consecutive step (I) comprises supplementing the saline water provided therein with a soluble CaCl2salt produced in step (Via) to reach sufficient amount of Ca+2ions for the precipitation of consecutive step (II).

[0350] Thus, according to some embodiments, the saline water of step (I) further comprises Ca+2cations. Thus, according to some embodiments, the saline water of step (I) further comprises Ca+2cations at a concentration of at least 50 ppm. According to some embodiments, the saline water of step (I) further comprises Ca+2cations at a concentration of at least 100 ppm. According to some embodiments, the saline water of step (I) further comprises Ca+2cations at a concentration of at least 150 ppm. According to some embodiments, the saline water of step (I)further comprises Ca+2cations at a concentration of at least 200 ppm. According to some embodiments, the saline water of step (I) further comprises Ca+2cations at a concentration of at least 300 ppm. According to some embodiments, the saline water of step (I) further comprises Ca+2cations at a concentration of at least 350 ppm. According to some embodiments, the saline water of step (I) further comprises Ca+2cations at a concentration of at least 400 ppm.

[0351] According to some embodiments, the saline water of consecutive step(s) (I) further comprises Ca+2cations at a concentration of at least 50 ppm. According to some embodiments, the saline water of consecutive step(s) (I) further comprises Ca+2cations at a concentration of at least 100 ppm. According to some embodiments, the saline water of consecutive step(s) (I) further comprises Ca+2cations at a concentration of at least 150 ppm. According to some embodiments, the saline water of consecutive step(s) (I) further comprises Ca+2cations at a concentration of at least 200 ppm. According to some embodiments, the saline water of consecutive step(s) (I) further comprises Ca+2cations at a concentration of at least 300 ppm. According to some embodiments, the saline water of consecutive step(s) (I) further comprises Ca+2cations at a concentration of at least 350 ppm. According to some embodiments, the saline water of consecutive step(s) (I) further comprises Ca+2cations at a concentration of at least 400 ppm.

[0352] According to some embodiments, the saline water of consecutive step (I) comprises at least one of: CO2, H2CO3, and HCO3- .

[0353] According to some embodiments, the admixing of saline water with the NaOH in consecutive step (II) entails carrying out one or more of the following chemical reactions:Ca+2+ CO2+ 2NaOH CaCO3+ 2Na++ H2O;Ca+2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2Na+;Ca+2+ HCO3’ + NaOH CaCO3+ H2O + Na+, thereby producing CaCO3as a solid water-insoluble precipitate and decarbonated water suitable for subsequent desalination.

[0354] According to some embodiments, the contacting of saline water with the NaOH in consecutive step(s) (II) entails carrying two or more of the chemical reactions. According to some embodiments, the contacting of saline water with the NaOH in consecutive step(s) (II) entails carrying each of the above chemical reactions.

[0355] According to some embodiments, the admixing of saline water with the NaOH in consecutive step(s) (II) entails carrying out at least the following chemical reaction:Ca+2+ CO2+ 2NaOH CaCO3+ 2Na++ H2O.

[0356] According to some embodiments, the admixing of saline water with the NaOH in consecutive step(s) (II) entails carrying out at least the following chemical reaction:Ca+2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2Na+.

[0357] According to some embodiments, the admixing of saline water with the NaOH in consecutive step(s) (II) entails carrying out at least the following chemical reaction:Ca+2+ HCO3- + NaOH CaCO3+ H2O + Na+.

[0358] According to some embodiments, the admixing of saline water with the NaOH in consecutive step(s) (II) and the above chemical reaction(s) result in producing CaCO3as a solid water-insoluble precipitate.

[0359] According to some embodiments, the saline water of consecutive step(s) (I) comprises HCO3‘, and wherein the admixing of saline water with the NaOH in consecutive step(s) (II) entails carrying out the following chemical reaction:Ca+2+ HCO3- + NaOH CaCO3+ H2O + Na+, thereby producing CaCO3as a solid water-insoluble precipitate and decarbonated water suitable for subsequent desalination upon the separation of step (III).

[0360] According to some embodiments, the admixing of saline water with the NaOH in consecutive step(s) (II) and the above chemical reaction(s) result in producing decarbonated water. According to some embodiments, the produced decarbonated water is suitable for subsequent desalination. According to some embodiments, the produced decarbonated water require an additional step of filtration prior to subsequent desalination.

[0361] Specific reference is now made to the present process of brine electrodialysis. In particular, the present invention further provides a process for the electrolysis of brine. Brine electrolysis may be a convenient route for the production of hydrochloric acid, metal chlorides, sodium hydroxide, other hydroxide compounds and other sodium salts. One of the challenges for successful transformation of brine into the desired products (e.g., HC1 and NaOH) relates to the carbon dioxide species dissolved in the starting brine (e.g., in the form of CO2, H2CO3, HCO3‘, and / or CO32), which interfere with the electrodialysis. The present invention provide a process, which includes several steps, which are mutual with the water-desalination process described above, but, which is directed to removal of the carbon dioxide species from brine, followed by an electrodialysis of the carbon dioxide species-depleted brine.

[0362] Specific reference is now made to step (I) of the present process of brine desalination. According to some embodiments, the present process comprises step (I) of providing brine.

[0363] The term “brine”, as used herein, refers to an aqueous composition (e.g., solution) comprising a high-concentration solution of salt (typically sodium chloride or calcium chloride). According to some embodiments, brine may refer to the salt solutions ranging from about 3.5% (a typical concentration of seawater, on the lower end of that of solutions used for brining foods) up to about 26% (a typical saturated solution, depending on temperature). Brine may form naturally due to evaporation of ground saline water but it is also generated in the mining of sodium chloride.

[0364] According to some embodiments, the brine comprises NaCl. According to some embodiments, the NaCl is the major salt component in the brine. According to some embodiments, brine comprises at least 4% NaCl w / w. According to some embodiments, brine comprises at least 7% NaCl w / w. According to some embodiments, brine comprises at least 10% NaCl w / w. According to some embodiments, brine comprises at least 15% NaCl w / w. According to some embodiments, brine comprises at least 20% NaCl w / w. According to some embodiments, brine comprises at least 25% NaCl w / w. According to some embodiments, brine comprises 20% to 30% NaCl w / w, including each value and sub-range within the specified range.

[0365] According to some embodiments, the brine provided in step (I) comprises carbonated species selected from the group consisting of: CO2, H2CO3, HCO3-, CO32and a combination thereof. According to some embodiments, the brine comprises HCO3'. According to some embodiments, the brine further comprises CO 3-2. According to some embodiments, the brine comprises HCO3- and CO32.

[0366] According to some embodiments, the brine comprises at least 0.1 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 0.5 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 1 HCO3- ion per one CO32ion. According to some embodiments, the brine comprises at least 1.5 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 2 HCO3- ions per oneCO3- 2ion. According to some embodiments, the brine comprises at least 2.3 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 3 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 5 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 6 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 10 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 20 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 50 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 100 HCO3- ions per one CO32ion. According to some embodiments, the brine comprises at least 1000 HCO3- ions per one CO32ion.

[0367] According to some embodiments, the brine comprises 0.1 to 100, 1 to 100, 2 to 3000, 3 to 3000, 3-1000, 3-500, 3-250 or 3-100 HCCE' ions per one CO32ion. Each possibility represents a separate embodiment of the invention.

[0368] According to some embodiments, the concentration of the carbonated species in the brine is at least 0.1 millimolar (mM). According to some embodiments, the concentration of the carbonated species is at least 0.25 millimolar (mM). According to some embodiments, the concentration of the carbonated species is at least 0.5 millimolar (mM). According to some embodiments, the concentration of the carbonated species is at least 0.75 millimolar (mM). According to some embodiments, the concentration of the carbonated species is at least 1 millimolar (mM). According to some embodiments, the concentration of the carbonated species is at least 1.25 mM. According to some embodiments, the concentration of the carbonated species is at least 1.5 mM. According to some embodiments, the concentration of the carbonated species is at least 1.75 mM. According to some embodiments, the concentration of the carbonated species is at least 2 mM. According to some embodiments, the concentration of the carbonated species is at least 2.25 mM. According to some embodiments, the concentration of the carbonated species is at least 2.5 mM. According to some embodiments, the concentration of the carbonated species is at least 3 mM. According to some embodiments, the concentration of the carbonated species is at least 3.5 mM. According to some embodiments, the concentration of the carbonated species is at least 4 mM. According to some embodiments, the concentration of the carbonated species is at least 4. 5 mM. According to some embodiments, the concentration of the carbonated species is at least 5 mM. According to some embodiments, the concentration of the carbonated species is in the range of 1.0 to 50.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 1.0 to 25.0 mM. According to someembodiments, the concentration of the carbonated species is in the range of 1.0 to 10.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 1.0 to 5.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 0.1 to 50.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 0.1 to 25.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 0.1 to 10.0 mM. According to some embodiments, the concentration of the carbonated species is in the range of 0.1 to 5.0 mM.

[0369] Thus, according to some embodiments, brine comprises HCO3- at a concentration of at least 0.1 millimolar (mM). According to some embodiments, brine comprises HCO3- at a concentration of at least 0.25 millimolar (mM). According to some embodiments, brine comprises HCO3- at a concentration of at least 0.5 millimolar (mM). According to some embodiments, brine comprises HCO3- at a concentration of at least 0.75 millimolar (mM). According to some embodiments, the HCO3- concentration in the brine is at least 1 mM. According to some embodiments, the HCO3- concentration in the brine is at least 1.25 mM. According to some embodiments, the HCO3- concentration in the brine is at least 1.5 mM. According to some embodiments, the HCO3- concentration in the brine is at least 1.75 mM. According to some embodiments, the HCO3- concentration in the brine is at least 2 mM. According to some embodiments, the HCO3- concentration in the brine is at least 2.25 mM. According to some embodiments, the HCO3- concentration in the brine is at least 2.5 mM. According to some embodiments, the HCO3- concentration in the brine is at least 3 mM. According to some embodiments, the HCO3- concentration in the brine is at least 3.5 mM. According to some embodiments, the HCO ,' concentration in the brine is at least 4 mM. According to some embodiments, the HCO3- concentration in the brine is at least 4.5 mM. According to some embodiments, the HCO3- concentration in the brine is at least 5 mM. According to some embodiments, the HCO3- concentration in the brine is in the range of 0.5 to 10 mM, 0.5 to 5 mM, 0.5 to 4 mM or 0.5 to 3 mM. Each possibility represents a separate embodiment of the invention.

[0370] According to some embodiments, at least 25% mol / mol of the total carbon dioxide species in the brine of step (I) is HCO3-. According to some embodiments, at least 50% mol / mol of the total carbon dioxide species in the brine of step (I) is HCO3-. According to some embodiments, at least 60% mol / mol of the total carbon dioxide species in the brine of step (I) is HCO3-.

[0371] According to some embodiments, the brine of step (I) comprises CO32at a concentration of no more than 20 millimolar (mM). According to some embodiments, the CO3-2concentration in the brine is no more than 10 millimolar. According to some embodiments, the CO3-2concentration in the brine is no more than 5 millimolar. According to some embodiments, the CO3-2concentration in the brine is no more than 3 millimolar. According to some embodiments, the CO3-2concentration in the brine is no more than 1 millimolar. According to some embodiments, the CO3-2concentration in the brine is no more than 0.5 millimolar.

[0372] Similarly, according to some embodiments, the brine comprises CO3-2at a concentration of no more than 20 millimolar (mM). According to some embodiments, the CO3-2concentration in the brine is no more than 10 millimolar. According to some embodiments, the CO3-2concentration in the brine is no more than 5 millimolar. According to some embodiments, the CO3-2concentration in the brine is no more than 3 millimolar. According to some embodiments, the CO3-2concentration in the brine is no more than 1 millimolar. According to some embodiments, the CO3-2concentration in the brine is no more than 0.5 millimolar. According to some embodiments, the CO3-2concentration in the brine is in the range of 0 to 2 millimolar.

[0373] According to some embodiments, the brine of step (I) has pH of no more than 11.5. According to some embodiments, the brine of step (I) has pH of no more than 11. According to some embodiments, the brine of step (I) has pH of no more than 10.5. According to some embodiments, the brine of step (I) has pH of no more than 10. According to some embodiments, the brine of step (I) has pH of no more than 9.5. According to some embodiments, the brine of step (I) has pH of no more than 9. According to some embodiments, the brine of step (I) has pH of no more than 8.5. According to some embodiments, the brine of step (I) has pH of at least 5. According to some embodiments, the brine of step (I) has pH of at least 5.5. According to some embodiments, the brine of step (I) has pH of at least 6. According to some embodiments, the brine of step (I) has pH of at least 6.5. According to some embodiments, the brine of step (I) has pH of at least 7. According to some embodiments, the carbonated brine of step (I) has pH of at least 7.5. According to some embodiments, the brine of step (I) has pH of at least 8. According to some embodiments, the brine of step (I) has pH in the range of 6-11, 7-11, 7-10, 7-8.5, 7.5- 8.4, 6-7, 7-8, 8-9, 9-10 or 10-11. Each possibility represents a separate embodiment of the invention.

[0374] According to some embodiments, the brine of step (I) comprises at least one of: CO2, H2CO3, and HCO3‘.

[0375] According to some embodiments, the brine comprises carbonated species at a concentration of at least 1 mM. According to some embodiments, the brine comprises CO3'2at a concentration of no more than 10 mM. According to some embodiments, the concentration of carbonated species in the brine is at least 0.1 mM.

[0376] Specific reference is now made to step (II) of the present process of brine desalination. According to some embodiments, the present process comprises step (II) of admixing a carbonated species chelator with the brine of step (I).

[0377] According to some embodiments, admixing a carbonated species chelator with the brine entails forming a CaCO3precipitate and decarbonated brine.

[0378] According to some embodiments, the carbonated species chelator is a base. According to some embodiments, the carbonated species chelator is a Lewis base.

[0379] According to some embodiments, the carbonated species chelator is an inorganic compound. According to some embodiments, the carbonated species chelator is an inorganic base.

[0380] According to some embodiments, the carbonated species chelator comprises a hydroxide salt. According to some embodiments, the hydroxide salt is selected from the group consisting of sodium hydroxide (NaOH), potassium hydroxide (KOH), calcium hydroxide (Ca(OH)2), calcium oxide (CaO) and a combination thereof. According to some embodiments, the carbonated species chelator comprises NaOH. According to some embodiments, the carbonated species chelator is NaOH. According to some embodiments, the carbonated species chelator comprises Ca(OH)2. According to some embodiments, the carbonated species chelator is Ca(OH)2.

[0381] According to some embodiments, the carbonated species chelator is a Ca+2salt. According to some embodiments, the carbonated species chelator is a Ca+2base. According to some embodiments, the carbonated species chelator is an inorganic Ca+2basic salt. According to some embodiments, the carbonated species chelator is Ca(OH)2 or CaO. Each possibility represents a separate embodiment of the invention. According to some embodiments, the carbonated species chelator is Ca(OH)2.

[0382] According to some embodiments, the admixing of step (II) entails forming CO3'2anions, and wherein the CaCO3precipitate is formed upon ion pairing of the Ca+2cations and said CO32anions.

[0383] According to some embodiments, the brine of step (I) comprises Ca+2cations, wherein the carbonated species chelator of step (II) comprises NaOH. According to some embodiments, step (I) comprises supplementing the brine with Ca+2cations, wherein the carbonated species chelator of step (II) comprises NaOH. It is to be understood that the option wherein the brine of step (I) comprises Ca+2cations include the options (a) that the brine is provided with Ca+2cations; and (b) that Ca+2cations are added to the brine (e.g., before, after or during the addition of the chelator, such as NaOH). According to some embodiments, the admixing of brine with the NaOH in step (II) entails carrying out one or more of the following chemical reactions:Ca+2+ CO2+ 2NaOH CaCO3+ 2Na++ H2O;Ca+2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2Na+; andCa+2+ HCO3‘ + NaOH CaCO3+ H2O + Na+. Each possible reaction represents a separate embodiment of the invention.

[0384] According to some embodiments, the contacting of brine with the NaOH in step (II) entails carrying two or more of the above chemical reactions. According to some embodiments, the contacting of brine with the NaOH in step (II) entails carrying each of the above chemical reactions.

[0385] According to some embodiments, the admixing of brine with the NaOH in step (II) entails carrying out at least the following chemical reaction:Ca+2+ CO2+ 2NaOH CaCO3+ 2Na++ H2O.

[0386] According to some embodiments, the admixing of brine with the NaOH in step (II) entails carrying out at least the following chemical reaction:Ca+2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2Na+.

[0387] According to some embodiments, the admixing of brine with the NaOH in step (II) entails carrying out at least the following chemical reaction:Ca+2+ HCO3- + NaOH CaCO3+ H2O + Na+.

[0388] According to some embodiments, the admixing of brine with the NaOH in step (II) and the above chemical reaction(s) result in producing CaCO3as a solid water-insoluble precipitate.

[0389] According to some embodiments, the carbonated species chelator of step (II) comprises Ca(OH)2, CaO, or both, and wherein the admixing of brine with the carbonated species chelator in step (II) entails carrying out one or more of the following chemical reactions:Ca(OH)2+ CO2CaCO3+ H2O;Ca(OH)2+ H2CO3CaCO3+ 2H2O;Ca(OH)2+ HCO3- CaCO3+ H2O + OH';CaO + CO2CaCO3;CaO + H2CO3CaCO3+ H2O; andCaO + HCO3- CaCO3+ OH'. Each possible reaction represents a separate embodiment of the invention.

[0390] According to some embodiments, the admixing of brine with the calcium hydroxide or calcium oxide in step (II) and the above chemical reaction(s) result in producing CaCO3as a solid water-insoluble precipitate.

[0391] According to some embodiments, the admixing of the brine with the carbonated species chelator in step (II) and the above chemical reaction(s) result in producing decarbonated brine. According to some embodiments, the produced decarbonated brine is suitable for subsequent electrodialysis. According to some embodiments, the produced decarbonated brine is suitable for subsequent electrodialysis following separation from the CaCO3precipitate and filtration.

[0392] According to some embodiments, the carbonated species chelator is provided to step (II) as an aqueous mixture. According to some embodiments, the carbonated species chelator is provided to step (II) as an aqueous solution.

[0393] According to some embodiments, the carbonated species chelator is NaOH, which is provided to step (II) as an aqueous mixture. According to some embodiments, the carbonated species chelator is NaOH, which is provided to step (II) as an aqueous solution of NaOH.

[0394] According to some embodiments, the aqueous solution of NaOH is provided to step (II) from an electrodialysis of NaCl. According to some embodiments, the aqueous solution of NaOH is provided to step (II) from an electrodialysis of the brine of step (IV). According to some embodiments, the aqueous solution of NaOH is the basic solution of NaOH formed in step (V).

[0395] According to some embodiments, the concentration of the carbonated species chelator is at least 0.01 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 0.05 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 0.1 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 0.25 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 0.5 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least1 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 1.5 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 2 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 5 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 10 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 25 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 50 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 100 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 200 g / L. According to some embodiments, the concentration of the carbonated species chelator is at least 500 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 0.01 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 0.05 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 0.1 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 0.25 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 0.5 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 1 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 1.5 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least2 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 5 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 10 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 25 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 50 g / L. According to some embodiments, the concentration of thecarbonated species chelator provided in step (II) is at least 100 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 200 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is at least 500 g / L.

[0396] According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 1000 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 500 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 200 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 100 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 50 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 25 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 10 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 5 g / L. According to some embodiments, the concentration of the carbonated species chelator provided in step (II) is no more than 2.5 g / L.

[0397] According to some embodiments, the chemical reaction of step (II) is a mono-phasic reaction. According to some embodiments, the CaCCL precipitate formed by the reaction of step (II) is water-insoluble.

[0398] According to some embodiments, the admixing thereof in step (II) entails contacting 0.25 to 4 moles of carbonated species per 1 mol of carbonated species chelator. According to some embodiments, the admixing thereof in step (II) entails contacting 0.5 to 2, 0.5 to 1.5 or 0.5 to 1.25 moles of carbonated species per 1 mol of carbonated species chelator. Each possibility represents a separate embodiment of the invention.

[0399] According to some embodiments, forming a solid water-insoluble precipitate in step (II) comprises inducing precipitation from the brine. According to some embodiments, forming a solid water-insoluble precipitate in step (II) comprises inducing precipitation from the brine, through seeding nucleation seeds as described herein (e.g., seeds of the water-insoluble precipitate in the mixture of step (II)).

[0400] According to some embodiments, admixing a carbonated species chelator with the brine to form a solid water-insoluble precipitate in step (II) further comprises adding nucleation seeds of the water-insoluble precipitate to the mixture of step (II).

[0401] Further elaboration on nucleation techniques and reagents is described above when relating to step (II) of the desalination process, the embodiments thereof similarly apply to the present process of brine electrodialysis.

[0402] Furthermore, the systems described with respect to the desalination process (e.g., the pellet reactor 100) may be applied for the present brine electrodialysis process, as can be understood by the person having ordinary skill in the art.

[0403] Specific reference is now made to step (III) of the present process. According to some embodiments, the present process comprises step (III) of separating the CaCCF precipitate of step (II) from the decarbonated brine.

[0404] According to some embodiments, step (III) comprises isolating the CaCCF precipitate. According to some embodiments, step (III) comprises isolating the decarbonated brine.

[0405] According to some embodiments, in step (III) any solid-liquid separation process can be utilized, for example filtration, decantation, and the like.

[0406] According to the principles of the present invention, the separated precipitate is recovered. According to the principles of the present invention, at least a portion of the separated precipitate is recovered. According to some embodiments, at least a portion of the separated precipitate is reused.

[0407] Within the scope of the present invention is the recovery and reuse of the precipitate. According to some embodiments, the brine is formed in a desalination process and the reuse comprises dissolving at least a portion of the precipitate and admixing the solution with the desalinated water thereby supplementing the desalinated water with Ca+2. According to some embodiments, the process comprises dissolving a portion of the CaCCF in an aqueous acidic composition thereby supplementing the desalinated water with calcium ions. According to some embodiments, the process comprises dissolving a portion of the CaCCF in an aqueous acidic composition thereby supplementing the brine with calcium ions. According to some embodiments, the process further comprises dissolving at least a portion of the separated CaCCF precipitate of step (III) and admixing the solution with the brine of a step (I) of a subsequent sequence of the process, thereby supplementing the provided brine with Ca+2ions.

[0408] According to some embodiments, the process comprises step (Via), wherein a portion of the CO2formed upon the reaction between the HC1 and the separated CaCO3precipitate is employed in the dissolution of the portion of the separated CaCO3precipitate.

[0409] For the sake of convenience, the present process of brine electrodialysis is described with the step numbered (V) following the step numbered (III). This is so that parallel steps of the brine electrodialysis and water desalination processes will be numbered similarly. In view of any requirement to present process steps in a consecutive manner, the step numbers may be change to conform with the requirements, e.g., step (V) of the brine electrodialysis process may be renumbered (IV).

[0410] Specific reference is now made to step (V) of the present process of brine electrodialysis. According to some embodiments, the present process comprises step (V) of performing an electrodialysis of the decarbonated brine.

[0411] According to some embodiments, step (V) includes a pre-treatment of the decarbonated brine to remove divalent ions that may be harmful to ion exchange and bipolar membranes. According to some embodiments, removal of divalent ions is performed by softening, nanofiltration, ion exchange or other method.

[0412] According to some embodiments, the electrodialysis of the decarbonated brine results in the formation of an acidic solution of HC1 (step 1090 in Figures 1A and IB). According to some embodiments, the electrodialysis of the decarbonated brine results in the formation of a basic solution of NaOH (step 1080 in Figures 1A and IB).

[0413] Furthermore, the systems described with respect to the desalination process (e.g., the electrodialysis system of Figure 3) may be applied for the present brine electrodialysis process, as can be understood by the person having ordinary skill in the art.

[0414] As the composition of the decarbonated brine of the brine electrodialysis process is similar to the brine composition provided to step (V) of the desalination process, steps (V) that the two processes can be similar and any embodiment described with respect to step (V) of the desalination process, may similarly apply to step (V) of the brine electrodialysis process.

[0415] Specific reference is now made to step (Via) of the present brine electrodialysis process. According to some embodiments, the present process comprises step (Via) of contacting the HC1 formed in step (V) with at least a portion of the separated CaCCF precipitate of step (III). Again with respect to step (Via), steps (Via) of the brine electrodialysis process and the water desalination process can be similar and any embodiment described with respect to step(Via) of the desalination process, may similarly apply to step (Via) of the brine electrodialysis process.

[0416] According to some embodiment, a portion of the isolated CaCl2formed in step (Via) is used to supplement the brine of consecutive step (I) with Ca+2ions.

[0417] Specific reference is now made to step (VIb) of the present brine electrodialysis process. According to some embodiments, the present process comprises step (VIb) of repeating steps (I) to (III) in a consecutive cycle, by using the NaOH formed in step (V) and, optionally, the CaCl2formed in step (Via) as the carbonated species chelator of a consecutive step (II).

[0418] According to some embodiments, the process comprises step (VIb).

[0419] According to some embodiments, step (VIb) comprises of repeating steps (I) to (III) in a consecutive cycle, by using a combination of the NaOH formed in step (V) and, optionally, the CaCl2formed in step (Via) as the carbonated species chelator of a consecutive step (II).

[0420] According to some embodiments, the admixing of brine with the NaOH in step (II) entails carrying out one or more of the following chemical reactions: CaCl2+ CO2+ 2NaOH CaCO3+ 2NaCl + H2O; CaCl2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2NaCl; and CaCl2+ HCO3‘ + NaOH CaCO3+ H2O + NaCl + Cl". Each possible reaction represents a separate embodiment of the invention.

[0421] In general, the consecutive cycle of steps according to the present process may have a similar characterization as characterized herein for the base steps, according to some embodiments.

[0422] The main salt in brine may be NaCl. As a result, the electrodialysis of step (V) is performed over a concentrated aqeous NaCl, which, in return results in the formation of an NaOH solution. The NaOH solution is an appropriate carbonated species chelator for the consecutive step(s) (II), according to some embodiments. However, according to some embodiments, NaOH does not include the calcium (Ca+2) cations required for the precipitation of CaCO3. As a result, according to some embodiments, consecutive step (II), when performed with NaOH solution as chelator, requires that the brine provided in consecutive step (I) comprises Ca+2. According to some embodiments, consecutive step (I) comprises supplementing the brine provided therein with a soluble Ca+2salt to reach sufficient amount of Ca+2ions for theprecipitation of consecutive step (II). According to some embodiments, consecutive step (I) comprises supplementing the brine provided therein with a soluble CaCl2salt produced in step (Via) to reach sufficient amount of Ca+2ions for the precipitation of consecutive step (II).

[0423] The foregoing description of the specific embodiments will so fully reveal the general nature of the invention that others can, by applying current knowledge, readily modify and / or adapt for various applications such specific embodiments without undue experimentation and without departing from the generic concept, and, therefore, such adaptations and modifications should and are intended to be comprehended within the meaning and range of equivalents of the disclosed embodiments. It is to be understood that the phraseology or terminology employed herein is for the purpose of description and not of limitation. The means, materials, and steps for carrying out various disclosed functions may take a variety of alternative forms without departing from the invention.

Claims

CLAIMS1. A process for desalinating saline water, the process comprising the steps of:(I) providing saline water comprising carbonated species selected from the group consisting of: CO2, H2CO3, HCO3- , CO32and a combination thereof, and NaCl;(II) admixing a carbonated species chelator with the saline water of step (I) to form a CaCO3precipitate and decarbonated water;(III) separating the CaCO3precipitate of step (II) from the decarbonated water;(IV) desalinating the decarbonated water of step (III) to form desalinated water and brine, wherein the brine comprises NaCl;(V) performing an electrodialysis of the brine of step (IV) to form an acidic solution of HC1 and a basic solution of NaOH; and(VI) performing step (Via), step (VIb), or both, wherein step (Via) comprises contacting the HC1 formed in step (V) with at least a portion of the separated CaCO3precipitate of step (III) to form CaCl2and CO2; and wherein step (VIb) comprises repeating steps (I) to (IV) in a consecutive cycle, by using the NaOH formed in step (V) as the carbonated species chelator of a consecutive step (II).

2. The process according to claim 1, wherein the saline water is seawater or brackish water.

3. The process according to any one of claims 1 to 2, wherein the saline water of step (I) has a saline water NaCl concentration, the desalinated water has a desalinated water NaCl concentration and the brine has brine NaCl concentration, wherein the saline water NaCl concentration is higher than the desalinated water NaCl concentration and lower than the brine NaCl concentration.

4. The process according to any one of claims 1 to 3, wherein the saline water of step (I) further comprises Ca+2cations; the saline water of step (I) is supplemented with Ca+2ions by addition of soluble Calcium salt; and / or the carbonated species chelator of step (II) comprises Ca+2cations.

5. The process according to claim 4, wherein the admixing of step (II) entails forming CO3'2anions, and wherein the CaCO3precipitate is formed upon ion pairing of the Ca+2cations and said CO32anions.

6. The process according to any one of claims 4 to 5, wherein the saline water of step (I) comprises Ca+2cations.

7. The process according to any one of claims 1 to 6, wherein the carbonated species chelator of step (II) comprises NaOH.

8. The process according to any one of claims 1 to 7, wherein the saline water of step (I) comprises at least one of: CO2, H2CO3, and HCCO3-9. The process according to claim 8, wherein the saline water of step (I) comprises Ca+2cations, wherein the carbonated species chelator of step (II) comprises NaOH, and wherein the admixing of saline water with the NaOH in step (II) entails carrying out one or more of the following chemical reactions:thereby producing CaCO3as a solid water-insoluble precipitate and decarbonated water suitable for subsequent desalination.

10. The process according to any one of claims 1 to 9, comprising step (Via).

11. The process according to claim 10, further comprising a step of isolating the CaCl2formed in step (Via).

12. The process according to any one of claims 10 to 11, further comprising a step of storing at least a portion of the CaCl2formed in step (Via); and / or supplementing the saline water of consecutive step (I) with a portion of the CaCl2formed in step (Via) to increase the concentration of Ca+2ions therein.

13. The process according to claim 10, further comprising a step of isolating the CO2formed in step (Via).

14. The process according to any one of claims 10 to 13, further comprising a step of isolating and storing the CO2formed in step (Via) thereby achieving Carbon Capture and Storage (CCS) or carbon removal.

15. The process according to any one of claims 1 to 14, comprising step (VIb).

16. The process according to claim 15, wherein the saline water of step (I) further comprises Ca+2cations or wherein step (I) further comprises supplementing the saline water with Ca+2cations.

17. The process according to claim 16, wherein the saline water of step (I) comprises at least one of: CO2, H2CO3, and HCO3- .

18. The process according to any one of claims 16 to 17, wherein the admixing of saline water with the NaOH in consecutive step (II) entails carrying out one or more of the following chemical reactions:Ca+2+ CO2+ 2NaOH CaCO3+ 2Na++ H2O;Ca+2+ H2CO3+ 2NaOH CaCO3+ 2H2O+ 2Na+;Ca+2+ HCO3’ + NaOH CaCO3+ H2O + Na+, thereby producing CaCO3as a solid water-insoluble precipitate and decarbonated water suitable for subsequent desalination.

19. The process according to claim 18, wherein the saline water comprises HCO3', and wherein the admixing of saline water with the NaOH in step (II) entails carrying out the following chemical reaction:Ca+2+ HCO3’ + NaOH CaCO3+ H2O + Na+. thereby producing CaCO3as a solid water-insoluble precipitate and decarbonated water suitable for subsequent desalination upon the separation of step (III).

20. The process according to any one of claims 1 to 19, which comprises both step (Via) and step (VIb).

21. The process according to any one of claims 1 to 20, wherein the brine electrodialysis of step (V) further entails forming deionized brine, and wherein the process further comprises repeating steps (I) to (IV) in a consecutive cycle, wherein consecutive step(IV) comprises desalinating a combination of the deionized brine and the decarbonated water of consecutive step (III) to form desalinated water and brine, wherein the brine comprises NaCl.

22. The process according to any one of claims 1 to 21, further comprising dissolving at least a portion of the separated CaCO3precipitate of step (III) and admixing the solution with the desalinated water of step (IV) thereby supplementing the desalinated water with essential Ca+2ions.

23. The process according to claim 22, wherein dissolving the portion of the separated CaCO3precipitate entails performing the following chemical reaction:CaCO3+ CO2+ H2O Ca(HCO3)2.

24. The process according to any one of claims 22 to 23, which comprises step (Via), wherein a portion of the CO2formed upon the reaction between the HC1 and the separated CaCO3precipitate is employed in the dissolution of the portion of the separated CaCO3precipitate.

25. The process according to any one of claims 1 to 24, wherein the saline water comprises HCO3‘ and CO3'2, wherein the saline water comprises at least 2 HCO3‘ ions per one CO3'2ion.

26. The process according to any one of claims 1 to 25, wherein the concentration of carbonated species in the saline water is at least 0.1 mM.

27. The process according to any one of claims 1 to 26, wherein the saline water of step (I) has pH in the range of 6 to 10.

28. The process according to any one of claims 1 to 27, wherein the salinity of the saline water of step (I) is in the range of 0.5 to 100 g / L.

29. The process according to any one of claims 1 to 28, wherein admixing a carbonated species chelator with the saline water to form a CaCO3precipitate in step (II) further comprises adding nucleation seeds to the saline water, wherein the nucleation seeds comprise CaCO3or sand particles.

30. The process according to claim 29, further comprising a step of using a portion of the separated CaCO3precipitate as the nucleation seeds.

31. The process according to any one of claims 1 to 30, wherein desalinating the decarbonated water in step (IV) comprises reverse osmosis.

32. The process according to claim 31, wherein desalinating the decarbonated water comprises a single reverse osmosis cycle.

33. The process according to claim 31, wherein desalinating the decarbonated water comprises at least two reverse osmosis cycles.

34. The process according to claim 33, wherein desalinating the decarbonated water comprises at least two reverse osmosis cycles wherein each reverse osmosis cycle after the first cycle is performed on a portion of the permeate of the previous reverse osmosis cycle, wherein each reverse osmosis cycle after the first is performed on a portion constituting 70% or less of the permeate of the previous reverse osmosis cycle; or wherein each reverse osmosis cycle after the first is performed on a portion constituting 50% or less of the permeate of the previous reverse osmosis cycle.

35. The process according to claim 34, wherein each reverse osmosis cycle after the first is performed on a portion constituting 30% or less of the permeate of the previous reverse osmosis cycle.

36. The process according to any one of claims 1 to 35, wherein the process further comprises providing a carbon removal system, wherein at least one of steps (II) and (III) is carried out within the carbon removal system, wherein the carbon removal system comprises a fluidized bed pellet reactor, wherein step (III) comprises admixing in the fluidized bed pellet reactor the carbonated species chelator with the saline water to form the CaCO3precipitate and the decarbonated water.

37. The process according to claim 36, wherein the fluidized bed pellet reactor comprises a first fluid inlet pipe, a fluid outlet pipe and an enclosed reaction chamber, each ofthe fluid inlet pipe and the fluid outlet pipe is in fluid communication with the reaction chamber, wherein step (II) comprises inserting the saline water into the reaction chamber through the fluid inlet pipe, and wherein the admixing of the saline water with the carbonated species chelator in step (II) is carried out within the reaction chamber.

38. The process according to any one of claims 35 to 37, wherein step (III) further comprises evacuating the decarbonated water through the fluid outlet pipe.

39. The process according to claim 38, wherein the fluidized bed pellet reactor further comprises a semi-permeable filter, which is permeable to water and impermeable to solids above a predetermined diameter, and is positioned to separate between the reaction chamber and the fluid outlet pipe; wherein the evacuation of the decarbonated water of step (III) comprises filtering the decarbonated water from the CaCO3precipitate by flowing the decarbonated water through the semi-permeable filter, and flowing the filtered decarbonated water through the fluid outlet pipe.

40. The process according to claim 39, wherein the semi-permeable filter has a cutoff is in the range of 0.07 to 0.16 millimeters.

41. The process according to any one of claims 36 to 40, wherein the fluidized bed pellet reactor further comprises a solid inlet pipe connected to the reaction chamber, wherein step (II) further comprises inserting seeds of CaCO3or sand into the reaction chamber through the solid inlet pipe.

42. The process according to claim 41, wherein step (II) further comprises fluidizing the seeds in the reaction chamber.

43. The process according to any one of claims 36 to 42, wherein the carbonated species chelator is NaOH, wherein the fluidized bed pellet reactor further comprises a solid inlet pipe, wherein step (II) further comprises inserting seeds of the CaCO3into the reaction chamber through the solid inlet pipe and fluidizing the seeds in the reaction chamber to a fluidized grains height, thereby inducing precipitation and maturation of CaCO3pellets, wherein the fluidized grains height is in the range of 0.6 meter to 12.4 meter.

44. A process for electrodialysis of brine, the process comprising the steps of:(I) providing brine comprising carbonated species selected from the group consisting of: CO2, H2CO3, HCO3-,CO3-2and a combination thereof, and NaCl;(II) admixing a carbonated species chelator with the brine of step (I) to form a CaCO3precipitate and decarbonated brine;(III) separating the CaCO3precipitate of step (II) from the decarbonated brine;(V) performing an electrodialysis of the decarbonated brine of step (III) to form an acidic solution of HC1 and a basic solution of NaOH;(Via) optionally contacting the HC1 formed in step (V) with at least a portion of the separated CaCO3precipitate of step (III) to form CaCl2and CO2; and(VIb) optionally repeating steps (I) to (III) in a consecutive cycle, by using the NaOH formed in step (V), and, optionally, the CaCl2formed in step (Via) as the carbonated species chelator of the consecutive step (II).

45. The process according to claim 44, wherein the brine of step (I) further comprises Ca+2cations; the brine of step (I) is supplemented with Ca+2ions by addition of soluble calcium salt; and / or the carbonated species chelator of step (II) comprises Ca+2cations.

46. The process according to any one of claims 44 to 45, wherein the carbonated species chelator of step (II) comprises NaOH.

47. The process according to claim 45, wherein the brine of step (I) comprises at least one of: CO2, H2CO3, and HCO3-; wherein the carbonated species chelator of step (II) comprises NaOH, and wherein the admixing of brine with the NaOH in step (II) entails carrying out one or more of the following chemical reactions:Ca+2+ HCO3- + NaOH CaCO3+ H2O + Na+, thereby producing CaCO3as a solid water-insoluble precipitate and decarbonated brine suitable for subsequent desalination.

48. The process according to any one of claims 44 to 47, comprising step (Via) and further comprising a step of isolating the CaCl2formed in step (Via)49. The process according to claim 48, further comprising a step of storing at least a portion of the CaCl2formed in step (Via); and / or supplementing the brine of consecutive step (I) with a portion of the CaCl2formed in step (Via) to increase the concentration of Ca+2ions therein.

50. The process according to any one of claims 44 to 49, wherein admixing a carbonated species chelator with the saline water to form a CaCO3precipitate in step (II) further comprises adding nucleation seeds to the brine, wherein the nucleation seeds comprise CaCO3or sand particles.

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