IL326366A

IL326366A - Method for reducing boron in desalinated water

Info

Publication number: IL326366A
Application number: IL326366A
Authority: IL
Inventors: Dan Peled; Dan Deviri; Iddo Mehnashe Tsur
Original assignee: Carbon Blue Ltd; Dan Peled; Dan Deviri; Iddo Mehnashe Tsur
Priority date: 2023-08-15
Filing date: 2024-08-11
Publication date: 2026-04-01
Also published as: WO2025037307A1

Description

PCT / IL2024 / 0508 METHOD FOR REDUCING BORON SPECIES IN DESALINATED WATER TECHNICAL FIELD [ 0001 ] The present disclosure generally relates to methods of water desalination .

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 methods 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 methods typically utilize enormous amounts of energy and are therefore economically unfavorable . [ 0004 ] Osmosis - based desalination is the leading method in desalination . This method 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 antiscalants to prevalent scaling and fouling on the membranes , and filtration of seawater to remove smaller suspended particles . Post- treatment may include pH adjustment , disinfection and remineralization of the treated water to ensure that it meets quality standards and requirements .

PCT / IL2024 / 0508 [ 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 , 129–029 ) . [ 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 ) 341–131 ) . 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 methods 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 , 27–66 ) 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 , 121–511 ) disclosed the addition of polyols including glycerol , mannitol , or sorbitol to the RO feed solution and Dydo et al . ( Desalination 2014 , 334 PCT / IL2024 / 0508 ( 1 ) , 39-45 ) disclosed the use of D - mannitol to form boron - D - mannitol complexes under specified conditions . [ 0009 ] There remains an unmet need for methods 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 [ 0010 ] The present invention is directed to systems and methods for pre - treatment of water prior to desalination . The present invention is further directed to systems and methods for desalination of water , for example seawater , which provide efficient removal of undesired boron species . [ 0011 ] Disclosed herein for the first time is a process for obtaining desalinated water with reduced amounts of boron species by pre - treatment of the water entering desalination thereby enabling enhanced boron rejection in the first pass of 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 . [ 0012 ] According to a first aspect , the present invention provides a process for pre - treatment of saline water prior to desalination , the process comprising the steps of : ( I ) providing saline water comprising carbonated species selected from the group consisting of : CO2 , H2CO3 , HCO3 , CO32 and a combination thereof ; ( II ) admixing a carbonated species chelator with the saline water of step ( I ) to form a solid water - insoluble precipitate ; and ( III ) separating the water - insoluble precipitate of step ( II ) from the water thereby obtaining water suitable for subsequent desalination , wherein the process further comprises recovering the separated precipitate of step ( III ) and reusing at least a portion thereof by regenerating a carbonated species chelator from the portion of the precipitate for subsequent use in step ( II ) , and PCT / IL2024 / 0508 [ 0013 ] optionally dissolving a portion of the recovered precipitate and admixing the solution with the desalinated water thereby supplementing the desalinated water with essential ions .

According to a second aspect , the present invention provides a process for desalinating saline water , the process comprising the steps of : ( I ) ( II ) ( III ) providing saline water comprising carbonated species selected from the group consisting of : CO2 , H2CO3 , ¯3OCH , ²3OC and a combination thereof ; admixing a carbonated species chelator with the saline water of step ( I ) to form a solid water - insoluble precipitate ; separating the water - insoluble precipitate of step ( II ) from the water ; and ( IV ) desalinating the water of step ( III ) , [ 0014 ] wherein the process further comprises recovering the separated precipitate of step ( III ) and reusing at least a portion thereof by regenerating a carbonated species chelator from the portion of the precipitate for subsequent use in step ( II ) , and optionally dissolving a portion of the recovered precipitate and admixing the solution with the desalinated water thereby supplementing the desalinated water with essential ions .

According to a third aspect , the present invention provides a process for enhancing the removal of boron species from saline water undergoing desalination , the process comprising the steps of : ( I ) ( II ) providing saline water comprising carbonated species selected from the group consisting of : CO2 , H2CO3 , HCO3 , ²3OC and a combination thereof ; admixing a carbonated species chelator with the saline water of step ( I ) to form a solid water - insoluble precipitate ; ( III ) separating the water - insoluble precipitate of step ( II ) from the water ; and ( IV ) desalinating the water of step ( III ) . [ 0015 ] According to some embodiments , the saline water comprises a boron species at a first boron species concentration . According to some embodiments , step ( IV ) comprises desalinating PCT / IL2024 / 0508 the water of step ( III ) to form desalinated water having a second boron species concentration . According to some embodiments , the second boron species concentration is at least 10 % lower than the first boron species concentration . According to some embodiments , the second boron species concentration is at least 20 % lower than the first boron species concentration . According to some embodiments , the second boron species concentration is at least 30 % lower than the first boron species concentration . According to some embodiments , the second boron species concentration is at least 40 % lower than the first boron species concentration . According to some embodiments , the second boron species concentration is at least 50 % lower than the first boron species concentration . According to some embodiments , the second boron species concentration is at least 60 % lower than the first boron species concentration . According to some embodiments , the second boron species concentration is at least 70 % lower than the first boron species concentration . [ 0016 ] 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 . For example , the phrase : " recovering the separated precipitate of step ( III ) and reusing at least a portion thereof by regenerating a carbonated species chelator from the portion of the precipitate for subsequent use in step ( II ) " is intended to cover both the option of : ( a ) recovering the separated precipitate of step ( III ) and reusing it by regenerating a carbonated species chelator from the precipitate for subsequent use in step ( II ) ; and ( b ) recovering the separated precipitate of step ( III ) and reusing a fraction thereof , which is less than the entire separated precipitate , by regenerating a carbonated species chelator from the fraction of the precipitate for subsequent use in step ( II ) . [ 0017 ] According to some embodiments , the process of the third aspect further comprises recovering the separated precipitate of step ( III ) and reusing at least a portion thereof by regenerating a carbonated species chelator from the portion of the precipitate for subsequent use in step ( II ) , and optionally dissolving a portion of the recovered precipitate and admixing the solution with the desalinated water thereby supplementing the desalinated water with essential ions . [ 0018 ] [ 0019 ] According to some embodiments , the saline water is seawater .

According to some embodiments , the saline water comprises HCO3 . According to some embodiments , the saline water further comprises CO32 . According to some embodiments , the saline water comprises HCO3 and ²²3OC .

PCT / IL2024 / 0508 [ 0020 ] According to some embodiments , the saline water comprises at least one ¯3OCH ion per one ²OC ion . According to some embodiments , the saline water comprises at least HCO3 ions per one ²3OC ion . According to some embodiments , the saline water comprises 3 to 3000 ¯3OCH ions per one ²3OC ion , including each value within the specified range . According to some embodiments , the saline water comprises at least 1000 HCO3 ions per one ²3OC ion . [ 0021 ] 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 ²OC at a concentration of no more than 10 mM . [ 0022 ] According to some embodiments , the saline water has pH in the range of 6 to 10 , including each value within the specified range . According to some embodiments , the saline water has pH in the range of 7 to 9 , including each value within the specified range . [ 0023 ] 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 . [ 0024 ] 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 . [ 0025 ] 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 . [ 0026 ] According to some embodiments , the salinity of the saline water is in the range of to 6 g / L , including each value within the specified range . [ 0027 ] According to some embodiments , the salinity of the saline water is in the range of to 5 g / L , including each value within the specified range . [ 0028 ] 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 ) . [ 0029 ] According to some embodiments , the carbonated species chelator is an inorganic base . According to some embodiments , the carbonated species chelator is a Ca + 2 salt . According to some embodiments , the mole ratio between the carbonated species and the Ca + 2 salt is in the range of about 0.5-25 : 1 , including all iterations of ratios within the specified range . [ 0030 ] [ 0031 ] According to some embodiments , the carbonated species chelator is Ca ( OH ) 2 .

According to some embodiments , the saline water comprises HCO3 , and step ( II ) entails carrying out the following chemical reaction : PCT / IL2024 / 0508 HCO3 + Ca ( OH ) 2 → CaCO3 + H2O + OH ; thereby producing CaCO3 as the solid water- insoluble precipitate . [ 0032 ] According to some embodiments , step ( II ) entails carrying out one or more of the following chemical reactions : CO2 + Ca ( OH ) 2 → CaCO3 + O₂H ; H2CO3 + Ca ( OH ) 2 → CaCO3 + 2H2O ; ¯3OCH + Ca ( OH ) 2 → CaCO3 + H2O + ‍HO ; thereby producing CaCO3 as the solid water- insoluble precipitate . [ 0033 ] According to some embodiments , step ( II ) further entails carrying out the following reaction : ²3OC + Ca ( OH ) 2 → CaCO3 + 2OH " , thereby producing CaCO3 as the solid water - insoluble precipitate . [ 0034 ] 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 ) . [ 0035 ] 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 . [ 0036 ] 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 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 00 PCT / IL2024 / 0508 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 CaCO3 is provided from the water - insoluble precipitate . According to some embodiments , the CaCO3 is provided from the water - insoluble precipitate . According to some embodiments , at least a portion of the CaCO3 is not provided from the water- insoluble precipitate . According to some embodiments , the CaCO3 is 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 to the mixture of step ( II ) . [ 0037 ] According to some embodiments , the solid water - insoluble precipitate has aqueous solubility of no more than 100 mg / L at 25 ° C . [ 0038 ] [ 0039 ] According to some embodiments , the solid water - insoluble precipitate is CaCO3 .

According to some embodiments , regenerating a carbonated species chelator from the precipitate comprises heating the precipitate to induce thermal decomposition . [ 0040 ] According to some embodiments , the solid water - insoluble precipitate is CaCO3 and regenerating a carbonated species chelator from the portion of the precipitate comprises heating the portion of the CaCO3 to induce thermal decomposition into carbon dioxide and a decarbonated solid material . According to some embodiments , regenerating a carbonated species chelator comprises mixing the decarbonated solid material with water . [ 0041 ] According to some embodiments , the process comprises dissolving a portion of the CaCO3 in an aqueous acidic composition comprising the carbon dioxide formed upon said thermal decomposition ; and admixing the solution with the desalinated water , thereby supplementing the desalinated water with calcium ions and carbonated species . According to some embodiments , the solid water - insoluble precipitate is CaCO3 and regenerating a carbonated species chelator from the portion of the precipitate comprises heating the portion of the CaCO3 to induce thermal decomposition into carbon dioxide and a decarbonated solid material ; and the process further comprises dissolving a portion of the CaCO3 in an aqueous acidic composition , the acidic composition comprising the carbon dioxide formed upon said thermal decomposition ; that the process further comprises admixing the solution with the desalinated water , thereby supplementing the desalinated water with calcium ions and carbonated species .

PCT / IL2024 / 0508 [ 0042 ] According to some embodiments , the dissolution of the portion of the CaCO3 in the aqueous acidic carbon dioxide composition , entails performing an acid - base chemical reaction .

According to some embodiments , the acid - base chemical reaction it represented by [ 0043 ] Scheme I. [ 0044 ] Scheme I : [ 0045 ] CaCO3 + CO2 + H2O → Ca ( HCO3 ) 2 .

According to some embodiments , the CaCO3 in 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 ) 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 . [ 0046 ] 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 Ia . [ 0047 ] Scheme Ia : [ 0048 ] CaCO3 + H2CO3 → Ca ( HCO3 ) 2 .

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 water comprises a boron species at a first boron species concentration and step ( IV ) comprises desalinating the water of step ( III ) to form desalinated water having a second boron species concentration which is lower than the first boron species concentration . [ 0049 ] According to some embodiments , the boron species comprises boric acid . [ 0050 ] 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 Ca ( OH ) 2 chelator with the saline water , the hydroxide ions within the mixture of step ( II ) react with the boric acid to form a borate . 30 PCT / IL2024 / 0508 [ 0051 ] According to some embodiments , upon the admixing the following reaction is taking place : [ 0052 ] [ 0053 ] B ( OH ) 3 + OH → B ( OH ) ¯˜4 .

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 . [ 0054 ] According to some embodiments , the selective separation of the selective membrane is based on ion size . [ 0055 ] 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 . [ 0056 ] 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 . [ 0057 ] According to some embodiments , the solid water - insoluble precipitate is CaCO3 and the process comprises dissolving a portion of the CaCO3 in acidic conditions and admixing the solution with the desalinated water thereby supplementing the desalinated water with calcium ions and carbonated species . [ 0058 ] 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 two reverse osmosis PCT / IL2024 / 0508 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 % 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 30 % or less of the permeate of the first reverse osmosis cycle . [ 0059 ] 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 ) . [ 0060 ] 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 . [ 0061 ] According to some embodiments , the present invention further provides a system , wherein at least steps ( II ) to ( III ) are carried out within .

PCT / IL2024 / 0508 [ 0062 ] According to some embodiments , the system comprises a pellet reactor , wherein step ( II ) comprises admixing in the pellet reactor the saline water with the carbonated species chelator to form a solid water - insoluble precipitate . [ 0063 ] According to some embodiments , the pellet reactor is a fluidized bed reactor . [ 0064 ] According to some embodiments , the pellet reactor comprises a 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 . [ 0065 ] According to some embodiments , step ( II ) comprises dissolving the carbonated species chelator in the saline water and inserting the formed solution into the reaction chamber through the fluid inlet pipe . [ 0066 ] According to some embodiments , step ( III ) further comprises evacuating the water through the fluid outlet pipe . [ 0067 ] According to some embodiments , the 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 water of step ( III ) 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 . [ 0068 ] 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 fluid inlet pipe is connected to the reaction chamber in the vicinity of its bottom end . [ 0069 ] According to some embodiments , the pellet reactor further comprises a solid outlet pipe , wherein step ( III ) comprises evacuating the precipitate through the solid outlet pipe , thereby separating the precipitate from the water . [ 0070 ] 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 .

PCT / IL2024 / 0508 [ 0071 ] According to some embodiments , the pellet reactor further comprises a solid inlet pipe , wherein step ( II ) further comprises inserting nucleation seeds as described herein into the reaction chamber through the solid inlet pipe . According to some embodiments , the pellet reactor further comprises a solid inlet pipe , wherein step ( II ) further comprises inserting nucleation seeds of the water - insoluble precipitate into the reaction chamber through the solid inlet pipe . [ 0072 ] According to some embodiments , step ( II ) further comprises fluidizing the seeds in the reaction chamber . [ 0073 ] According to some embodiments , the enclosed reaction chamber comprises a top end and a bottom end , wherein the solid inlet pipe is connected to the reaction chamber in the vicinity of its top end . [ 0074 ] According to some embodiments , the fluidized bed pellet reactor comprises : a 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 each of the solid inlet pipe and the fluid outlet pipe is connected to the reaction chamber in the vicinity of its top end , 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 Ca ( OH ) 2 ; step ( II ) comprises dissolving the Ca ( OH ) 2 in the saline water and inserting the formed solution into the reaction chamber through the fluid inlet pipe ; inserting CaCO3 seeds into the reaction chamber through the solid inlet pipe in the vicinity of the reaction chamber top end and fluidizing said seeds , thereby inducing precipitation of CaCO3 formed from a chemical reaction between the HCO3 and the Ca ( OH ) 2 , so that the formed CaCO3 is sinking to the bottom end of the reaction chamber and the water flows in the direction of the top end of the reaction chamber ; evacuating the water for subsequent desalination from the top end of the reaction chamber through the fluid outlet pipe ; and evacuating the CaCO3 from the bottom end of the reaction chamber through the solid outlet pipe . [ 0075 ] According to some embodiments , the pellet reactor further comprises a second fluid inlet pipe . According to some embodiments , the second fluid inlet pipe is in fluid communication with the reaction chamber . According to some embodiments , step ( II ) comprises inserting the carbonated species chelator into the reaction chamber through the second fluid inlet pipe . According to some embodiments , step ( II ) comprises inserting a composition of the carbonated species chelator into the reaction chamber through the second fluid inlet pipe . According to some embodiments , the composition is a solution , a slurry , a dispersion or an emulsion . Each possibility represents a separate embodiment of the invention . According to some embodiments , PCT / IL2024 / 0508 the composition is an aqueous composition . According to some embodiments , the composition is an aqueous Ca ( OH ) 2 composition . According to some embodiments , the second fluid inlet pipe is connected to the reaction chamber in the vicinity of its bottom end . [ 0076 ] According to some embodiments , step ( II ) comprises : inserting the saline water into the reaction chamber through the first fluid inlet pipe ; hydrating the Ca ( OH ) 2 in water to form an aqueous Ca ( OH ) 2 composition ; and inserting the formed composition into the reaction chamber through the second fluid inlet pipe . [ 0077 ] According to some embodiments , the system comprises a calciner configured to regenerate the precipitate . [ 0078 ] According to some embodiments , the calciner is a circulating fluidized bed calciner . [ 0079 ] According to some embodiments , the calciner comprises a solid inlet pipe , a gas outlet pipe and a heating chamber , wherein each of the pipes is in fluid communication with the heating chamber , wherein recovery and reuse of the separated precipitate of step ( III ) comprises : inserting the separated precipitate through the solid inlet pipe into the heating chamber ; elevating the temperature within the heating chamber , to form carbon dioxide gas and the decarbonated solid material ; and evacuating the carbon dioxide gas through the gas outlet pipe . [ 0080 ] According to some embodiments , the heating chamber is a combustion chamber ; wherein the calciner further comprises a first gas inlet pipe , and a second gas inlet pipe , each is in fluid communication with the combustion chamber , wherein elevating the temperature within the heating chamber comprises inserting a combustible gas through the first gas inlet pipe into the combustion chamber , inserting oxygen gas through the second gas inlet pipe combustion chamber , and combusting the gas mixture in the combustion chamber to elevate the temperature . [ 0081 ] According to some embodiments , the calciner further comprises a solid outlet in fluid communication with the heating chamber , wherein the decarbonated solid material is evacuated through the solid outlet . [ 0082 ] According to some embodiments , the system comprises a slaker which is configured to convert the decarbonated solid material formed into a carbonated species chelator in the slaker . [ 0083 ] According to some embodiments , the slaker comprises a solid inlet pipe , a steam or water inlet pipe , an outlet pipe and a slaking chamber , wherein each of the pipes is in fluid communication with the slaking chamber , wherein converting the decarbonated solid material formed into a carbonated species chelator comprises : inserting the decarbonated solid into the PCT / IL2024 / 0508 slaking chamber through the solid inlet pipe ; inserting steam or water into the slaking chamber through the steam or water inlet pipe ; reacting the steam or water with the decarbonated solid material to form a carbonated species chelator ; and evacuating the carbonated species chelator through the outlet pipe .

According to some embodiments , the slaker is a circulating fluidized bed steam [ 0084 ] slaker . [ 0085 ] According to some embodiments , the slaker comprises a solid inlet pipe , a steam inlet pipe , an outlet pipe and a slaking chamber , wherein each of the pipes is in fluid communication with the slaking chamber , wherein converting the decarbonated solid material formed into a carbonated species chelator comprises : inserting the decarbonated solid into the slaking chamber through the solid inlet pipe ; inserting steam into the slaking chamber through the steam inlet pipe ; reacting the steam with the decarbonated solid material to form a carbonated species chelator ; and evacuating the carbonated species chelator through the outlet pipe . [ 0086 ] [ 0087 ] According to some embodiments , the slaker is a water slaker .

According to some embodiments , the slaker comprises a solid inlet pipe , a water inlet pipe , an outlet pipe and a slaking chamber , wherein each of the pipes is in fluid communication with the slaking chamber , wherein converting the decarbonated solid material formed into a carbonated species chelator comprises : inserting the decarbonated solid into the slaking chamber through the solid inlet pipe ; inserting water into the slaking chamber through the water inlet pipe ; reacting the water with the decarbonated solid material to form a carbonated species chelator ; and evacuating the carbonated species chelator through the outlet pipe . [ 0088 ] According to some embodiments , there is provided a system comprising : [ 0089 ] a fluidized bed pellet reactor comprising : [ 0090 ] a fluid inlet pipe , [ 0091 ] a solid inlet pipe , [ 0092 ] a fluid outlet pipe , [ 0093 ] a solid outlet pipe , and [ 0094 ] an enclosed reaction chamber , which comprises a top end and a bottom end , PCT / IL2024 / 0508 [ 0095 ] wherein each of the solid inlet pipe and the fluid outlet pipe is connected to the reaction chamber in the vicinity of its top end , 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 ; [ 0096 ] a circulating fluidized bed calciner comprising : [ 0097 ] a solid inlet pipe , [ 0098 ] a gas outlet pipe , [ 0099 ] a first gas inlet pipe , [ 00100 ] a second gas inlet pipe , [ 00101 ] a solid outlet pipe , and [ 00102 ] a combustion chamber , [ 00103 ] wherein each of the pipes is in fluid communication with the combustion chamber ; and [ 00104 ] a circulating fluidized bed steam slaker comprising : [ 00105 ] a solid inlet pipe , [ 00106 ] a steam inlet pipe , [ 00107 ] an outlet pipe and [ 00108 ] a slaking chamber , [ 00109 ] wherein each of the pipes is in fluid communication with the slaking chamber ; [ 00110 ] wherein the solid outlet pipe of the pellet reactor is in fluid communication with the solid inlet pipe of the calciner , wherein the solid outlet pipe of the calciner is in fluid communication with the solid inlet pipe of the slaker , and wherein the outlet pipe of the slaker is in fluid communication with the liquid inlet pipe of the pellet reactor or with the second fluid inlet pipe of the pellet reactor . According to some embodiments , the outlet pipe of the slaker is in fluid communication with the second fluid inlet pipe of the pellet reactor [ 00111 ] 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 .

PCT / IL2024 / 0508 [ 00112 ] 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 [ 00113 ] 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 . [ 00114 ] Figure 1A is a schematic illustration of a hitherto known SWRO process . Numbers 1-14 represent different sampling points . [ 00115 ] Figure 1B is a schematic illustration of a SWRO process according to some embodiments . Numbers 1-16 represent different sampling points . [ 00116 ] Figure 2 is a schematic cross - section illustration of a pellet reactor , according to some embodiments . [ 00117 ] Figure 3 is a schematic illustration of a circulating fluidized bed calciner , according to some embodiments . [ 00118 ] Figure 4 is a schematic illustration of a circulating fluidized bed steam slaker , according to some embodiments .

DETAILED DESCRIPTION OF THE INVENTION [ 00119 ] 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 . [ 00120 ] The methods of the present invention are suitable for desalination of seawater , brackish water , or other types of water .

PCT / IL2024 / 0508 [ 00121 ] According to some embodiments , the present invention provides a method for pre- treatment of saline water prior to desalination . According to some embodiments , the present invention provides a method for desalinating saline water . According to some embodiments , the present invention provides a method for enhancing the removal of boron species from saline water undergoing desalination . [ 00122 ] steps of : ( I ) According to some embodiments , the methods of the present invention comprise the providing saline water comprising carbonated species selected from the group consisting of : CO2 , H2CO3 , HCO3 , ²3OC and a combination thereof ; ( II ) admixing a carbonated species chelator with the saline water of step ( I ) to form a solid water - insoluble precipitate ; and ( III ) separating the water - insoluble precipitate of step ( II ) from the water . [ 00123 ] 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 . According to some embodiments , the reuse comprises regenerating a carbonated species chelator from at least a portion of the precipitate for subsequent use . 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 . [ 00124 ] Figure 1A schematically represents a process flow diagram of a conventional double pass sea water desalination treatment , without energy recovery or recirculation streams . In this conventional treatment , filtered sea water ( stream 1 ) , enter a high - pressure pump , then enter at high pressure to the first pass Sea Water Reverse Osmosis ( SWRO ) desalination ( stream 2 ) . Stream 3 is a first pass , where reject / brine is discharged to the sea . All of first pass desalinated low pressure permeate ( stream 4 ) is dosed with caustic ( e.g. , NaOH ) to increase pH level for improved boron rejection . It is then pressurized , and enters another complementary desalination process termed second pass , required for improvement of final permeate chemical qualities , mainly boron and chlorides content . The second pass may vary in configuration , yet typically requires several sub stages to increase the recovery of the pass ( permeate flow derived out of the feed flow ) . In Figure 1A , a typical 3 - stage configuration is displayed , with streams 7-9 & 11-13 PCT / IL2024 / 0508 being the internal streams related to the 2nd pass ( each stage has a feed , brine and product stream ) . A second pass permeate ( stream 14 ) is directed to disinfecting and chemical conditioning for drinking . The reject ( stream 10 ) is typically recycled to 1st pass feed . [ 00125 ] Figure 1B is a schematic illustration of the methods of desalination and boron removal of the present invention , according to some embodiments . In this particular embodiment , saline water pre - treated according to the process of the present invention ( stream ) , enter a high - pressure pump , then enter at high pressure to the 1st pass SWRO desalination ( stream 2 ) . First pass reject / brine is then discharged to the sea ( stream 3 ) . The first pass desalinated low pressure permeate ( stream 4 ) is characterized by a high pH level and lower boron content ( due to 1st pass modified feed conditions ) . It is split into two streams : stream 5 , which is directed to final product treatment ; and stream 6 is directed to further treatment . It is pressurized , and enters another complementary desalination process termed second pass , required for improvement of final permeate chemical qualities , mainly boron and chlorides content . The second pass may vary in configuration , yet typically requires several sub stages to increase the recovery of the pass ( permeate flow derived out of the feed flow ) . In the particular embodiment represented in Figure 1B , a typical 3 - stage configuration is displayed , with streams 8-10 & 12-14 are the internal streams related to the 2nd pass ( each stage has a feed , brine and product stream ) . The second pass permeate ( stream 15 ) is mixed with the bypassed 1st pass product ( stream 5 ) and is directed to disinfecting and chemical conditioning for drinking . The reject ( stream 11 ) is typically recycled to 1st pass feed . [ 00126 ] Thus , the depicted embodiment of the present process is characterized by a smaller pass 2 and a higher overall recovery rate vs. the conventional 2 pass design . [ 00127 ] According to some embodiments , in the present process , which includes three main modules , a chelator , e.g. , lime ( Ca ( OH ) 2 ) , is added to saline water , e.g. , seawater . When in contact with the carbonated species that are found in the saline water , the chelator induces precipitation of a precipitate , e.g. , CaCO3 . The precipitate is then calcinated to release CO2 as a high - concentration gas stream , while coincidently producing quicklime ( CaO ) . In the next steps , according to some embodiments , the CaO is slaked to regenerate the lime which may then be used for additional cycle ( s ) . The precipitate may also be used to remineralize the desalinated water as required from the public health perspective and the suitability of the water for irrigation of agricultural crops and municipal gardening plants . [ 00128 ] 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 PCT / IL2024 / 0508 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 . [ 00129 ] As detailed herein , step ( I ) of the present invention includes providing saline water comprising carbonated species selected from the group consisting of : CO2 , H2CO3 , ˜3OCH , ¯3OC and a combination thereof . [ 00130 ] Carbonated species present in seawater are inorganic and typically include CO2 , H2CO3 , HCO3 and ²3OC . They are also commonly termed dissolved inorganic carbon ( DIC ) species , and their relative ratio is pH depended . [ 00131 ] Within the present disclosure , the term " DIC concentration " should be interpreted as the sum of the molar concentrations of CO2 , H2CO3 , HCO3 and ²3OC within a mixture , e.g. , an aqueous mixture . For example , an aqueous mixture comprising 0.1M HCO3 and 0.15M CO3-and devoid of other DIC species is said to have a DIC concentration of 0.25M . [ 00132 ] According to some embodiments , the saline water comprises HCO3 . According to some embodiments , the saline water further comprises CO32 . According to some embodiments , the saline water comprises HCO3 and ²OC . [ 00133 ] According to some embodiments , the saline water comprises at least 0.1 ¯3OCH ions per one CO32 ion . According to some embodiments , the saline water comprises at least 0.HCO3 ions per one ²3OC ion . According to some embodiments , the saline water comprises at least 1 HCO3 ion per one CO32 ion . According to some embodiments , the saline water comprises at least 1.5 HCO3 ions per one ²²3OC ion . According to some embodiments , the saline water comprises at least 2 HCO3 ions per one ²²3OC ion . According to some embodiments , the saline water comprises at least 2.3 HCO3 ions per one CO32 ion . According to some embodiments , the saline water comprises at least 3 HCO3 ions per one ²²3OC ion . According to some embodiments , the saline water comprises at least 5 HCO3 ions per one ²3OC ion . According to some embodiments , the saline water comprises at least 6 HCO3 ions per one ²²3OC ion . According to some embodiments , the saline water comprises at least 10 HCO3 ions per one ²3OC ion . According to some embodiments , the saline water comprises at least 20 ¯3OCH ions . - per one CO2 ion . According to some embodiments , the saline water comprises at least HCO3 ions per one ²3OC ion . According to some embodiments , the saline water comprises at PCT / IL2024 / 0508 least 100 HCO3 ions per one CO32 ion . According to some embodiments , the saline water comprises at least 1000 HCO3 ions per one CO32 ion . [ 00134 ] According to some embodiments , the saline water comprises 0.1 to 100 , 1 to 100 , to 3000 , 3 to 3000 , 3-1000 , 3-500 , 3-250 or 3-100 HCO3 ions per one ²3OC ion . Each possibility represents a separate embodiment of the invention . [ 00135 ] 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.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 CO2 concentration . [ 00136 ] 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.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 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 .

PCT / IL2024 / 0508 [ 00137 ] Saline water according to the principles of the present invention typically include 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 . [ 00138 ] 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 . [ 00139 ] 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 . [ 00140 ] 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 . [ 00141 ] 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 , 3–5.0 g / L , 02–3 g / L , 05–02 g / L , 56–05 g / L or 0.1 to 0.5 g / L . Each possibility represents a separate embodiment of the invention . [ 00142 ] 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 . [ 00143 ] 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 PCT / IL2024 / 0508 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 ¯3OCH 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 mM or 0.5 to 3 mM . Each possibility represents a separate embodiment of the invention . [ 00144 ] 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 " . [ 00145 ] 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 CO2 and 0.8 mol HCO3 , 20 % mol / mol of the total carbonated species is CO3 and 80 % mol / mol is ¯3OCH . [ 00146 ] According to some embodiments , the saline water of step ( I ) comprises CO32 at a concentration of no more than 20 millimolar ( mM ) . According to some embodiments , the CO3 * ² concentration in the saline water is no more than 10 millimolar . According to some embodiments , the CO32 concentration in the saline water is no more than 5 millimolar . According to some embodiments , the ²3OC concentration in the saline water is no more than millimolar . According to some embodiments , the CO32 concentration in the saline water is no more than 1 millimolar . According to some embodiments , the CO32 concentration in the saline water is no more than 0.5 millimolar . [ 00147 ] Similarly , according to some embodiments , the saline water comprises ²3OC at a concentration of no more than 20 millimolar ( mM ) . According to some embodiments , the ²²3OC concentration in the saline water is no more than 10 millimolar . According to some PCT / IL2024 / 0508 " -embodiments , the CO3-2 concentration in the saline water is no more than 5 millimolar . According to some embodiments , the ²3OC concentration in the saline water is no more than millimolar . According to some embodiments , the ²3OC concentration in the saline water is no more than 1 millimolar . According to some embodiments , the CO32 concentration in the saline water is no more than 0.5 millimolar . According to some embodiments , the CO32 concentration in the saline water is in the range of 0 to 2 millimolar . [ 00148 ] 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 saline water 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 11–6 , 11–7 , 01–7 , 5.8–7 , 4.8–5.7 , 7–6 , 8–7 , 9–8 , 01–9 or 11–01 . Each possibility represents a separate embodiment of the invention . [ 00149 ] As detailed herein , according to some embodiments , step ( II ) of the present method comprises admixing the saline water with a carbonated species chelator . [ 00150 ] According to some embodiments , the carbonated species chelator is a base . According to some embodiments , the carbonated species chelator is a Lewis base . [ 00151 ] According to some embodiments , the carbonated species chelator is an inorganic compound . According to some embodiments , the carbonated species chelator is an inorganic base . [ 00152 ] According to some embodiments , the carbonated species chelator is a Ca + 2 salt . According to some embodiments , the carbonated species chelator is a Ca + 2 base . According to some embodiments , the carbonated species chelator is an inorganic Ca + 2 basic salt .

PCT / IL2024 / 0508 [ 00153 ] In particular , as detailed herein , according to some embodiments , carbonated species chelator provided in step ( II ) is to react with the carbonated species ( e.g. , with ¯3OCH ) to form a water - insoluble precipitate . Thus , in order for the precipitate to be a water - insoluble solid , the counter - cation should be carefully selected , according to some embodiments . Calcium salts are often water - insoluble ( CaCO3 has aqueous solubility of 0.013 g / L at 25 ° C ) , so calcium salts are advantageous for use as the carbonated species chelator of the present method , according to some embodiments . [ 00154 ] According to some embodiments , the carbonated species chelator is Ca ( OH ) 2 or CaO . Each possibility represents a separate embodiment of the invention . [ 00155 ] According to some embodiments , the carbonated species chelator is Ca ( OH ) 2 . [ 00156 ] Advantageously , despite the very low aqueous solubility of CaCO3 , calcium hydroxide , Ca ( OH ) 2 , is about 140 times more soluble ( 1.7-1.9 g / L at 0-20 ° C ) , which is beneficial for the promotion of the reaction between the carbonated species and the carbonated species chelator . Therefore , Ca ( OH ) 2 may be used as the present carbonated species chelator . [ 00157 ] 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 . [ 00158 ] 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 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 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 PCT / IL2024 / 0508 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 . [ 00159 ] 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 . [ 00160 ] According to some embodiments , the chemical reaction of step ( II ) is a mono - phasic reaction . [ 00161 ] 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 . [ 00162 ] According to some embodiments , the 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 . [ 00163 ] According to some embodiments , the precipitate has aqueous solubility of no more than 100 mg / L at 25 ° C . According to some embodiments , the precipitate has aqueous solubility of no more than 500 mg / L at 25 ° C , no more than 300 mg / L at 25 ° C , no more than 200 mg / L at ° C , no more than 100 mg / L at 25 ° C , no more than 75 mg / L at 25 ° C , no more than 50 mg / L at ° C , no more than 33 mg / L at 25 ° C , no more than 25 mg / L at 25 ° C , no more than 20 mg / L at ° C or no more than 15 mg / L at 25 ° C . Each possibility represents a separate embodiment of the invention . [ 00164 ] Specifically , the aqueous solubility of CaCO3 is 13 mg / L at 25 ° C . [ 00165 ] According to some embodiments , the solid water - insoluble precipitate is CaCO3 .

PCT / IL2024 / 0508 [ 00166 ] According to some embodiments , the solid water - insoluble precipitate is CaCO3 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 embodiments of the present invention . [ 00167 ] According to some embodiments , the saline water comprises HCO3 , and the carbonated species chelator comprises Ca ( OH ) 2 . According to some embodiments , the contacting of saline water with the Ca ( OH ) 2 in step ( II ) entails carrying out the chemical reaction : [ 00168 ] HCO3 + Ca ( OH ) 2 → CaCO3 + H2O + OH ; [ 00169 ] thereby producing CaCO3 as the solid water - insoluble precipitate and water . Specifically , as detailed above , CaCO3 is only sparingly soluble , which leads to its precipitation and separation from the water . [ 00170 ] According to some embodiments , the carbonated species chelator comprises Ca ( OH ) 2 . According to some embodiments , the contacting of saline water with the Ca ( OH ) 2 in step ( II ) entails carrying one or more of the chemical reactions : [ 00171 ] CO2 + Ca ( OH ) 2 → CaCO3 + H2O ; [ 00172 ] H2CO3 + Ca ( OH ) 2 → CaCO3 + O₂H2 ; [ 00173 ] HCO3 + Ca ( OH ) 2 → CaCO3 + H2O + ‍HO ; [ 00174 ] ²OC + Ca ( OH ) 2 → CaCO3 + ¯H02 ; [ 00175 ] thereby producing CaCO3 as the solid water - insoluble precipitate and water . Each possible reaction represents a separate embodiment of the invention . According to some embodiments , the contacting of saline water with the Ca ( OH ) 2 in step ( II ) entails carrying two or more of the chemical reactions . According to some embodiments , the contacting of saline water with the Ca ( OH ) 2 in step ( II ) entails carrying three or more of the chemical reactions . According to some embodiments , the contacting of saline water with the Ca ( OH ) 2 in step ( II ) entails carrying each of the above chemical reactions . [ 00176 ] It is to be understood that the amount of the carbonated species chelator ( e.g. , Ca ( OH ) 2 ) is determined by the pH of the saline water , DIC concentration , and the specific reaction stoichiometry . [ 00177 ] 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 PCT / IL2024 / 0508 some embodiments , the admixing thereof in step ( II ) entails contacting 0.25 to 1.5 , 0.33 to 1.or 0.5 to 1 moles of carbonated species per 1 mol of carbonated species chelator . Each possibility represents a separate embodiment of the invention . According to some embodiments , the admixing thereof in step ( II ) entails contacting 0.75 to 4 , 0.8 to 3 or 1 to 2 moles of carbonated species per 1 mol of carbonated species chelator . Each possibility represents a separate embodiment of the invention . [ 00178 ] According to some embodiments , the carbonated species chelator is Ca + 2 salt , the saline water comprises carbonated species , and the admixing thereof in step ( II ) entails contacting 0.75 to 2.5 moles of carbonated species per 1 mol of Ca + ² . According to some embodiments , admixing thereof in step ( II ) entails contacting 1 to 2 moles of carbonated species per 1 mol of Ca + ² . [ 00179 ] According to some embodiments , the carbonated species chelator is Ca + 2 salt , the saline water comprises carbonated species , and the admixing thereof in step ( II ) entails contacting 0.5 to 2.5 moles of carbonated species per 1 mol of Ca + 2 . [ 00180 ] Although some embodiments of the present method relate to a batch reaction , it is to be understood that the present method may be carried out continuously . [ 00181 ] According to some embodiments , the method comprises performing steps ( I ) – ( III ) continuously . According to some embodiments , the method comprises performing steps ( I ) - ( III ) repeatedly . [ 00182 ] According to some embodiments , the admixing of the carbonated species chelator with the carbonated species in step ( II ) entails contacting the carbonated species chelator and the saline water continuously or in batches at a predetermined rate , so as to maintain a ratio of 0.to 2.5 moles of carbonated species per 1 mol of Ca + 2 in the mixture of step ( II ) . According to some embodiments , the predetermined rate is determined so as to maintain a ratio of 1 to 2 moles of carbonated species per 1 mol of Ca + 2 in the mixture of step ( II ) . [ 00183 ] According to some embodiments , the admixing of the carbonated species chelator with the carbonated species in step ( II ) entails contacting the carbonated species chelator and the saline water continuously or in batches at a predetermined rate , so as to maintain a ratio of 0.to 2.5 moles of carbonated species per 1 mol of Ca + 2 in the mixture of step ( II ) . [ 00184 ] According to some embodiments , steps ( I ) and ( II ) entail continuously providing the carbonated species and the Ca + 2 salt at a relative rate of 0.75 to 2.5 moles of carbonated species per 1 mol of Cat . According to some embodiments , steps ( I ) and ( II ) entail continuously PCT / IL2024 / 0508 providing the carbonated species and the Ca + ² salt at a relative rate of 1 to 2 moles of carbonated species per 1 mol of Ca * . [ 00185 ] According to some embodiments , steps ( I ) and ( II ) entail continuously providing the carbonated species and the Ca + 2 salt at a relative rate of 0.5 to 2.5 moles of carbonated species per 1 mol of Ca + . [ 00186 ] Alongside the dissolved inorganic carbon ( DIC ) species , sea water also contains relatively high concentration of divalent ions , most prominently calcium ( ~ 10 mM ) and magnesium ( ~ 50 mM ) . Interestingly , while the concentrations product of the calcium and carbonate ions exceeds the solubility product of calcium carbonate 3.3 × 109 ²M [ 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 ) : 808–797 , 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 : Ii . the influence of the ionic strength . Geochimica et Cosmochimica Acta , 62 ( 5 ) : 667–757 , 1998 ] or both . [ 00187 ] Thus , it is common that despite the insolubility of CaCO3 its 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 CaCO3 tend to precipitate more rapidly to form larger CaCO3 crystals or pellets , according to some embodiments . [ 00188 ] 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 ) ) . [ 00189 ] According to some embodiments , the precipitate is then separated from the water in step ( III ) . Any solid - liquid separation method can be utilized , for example filtration , decantation , and the like . [ 00190 ] According to some embodiments , regenerating a carbonated species chelator from the precipitate comprises heating the precipitate to induce thermal decomposition .

PCT / IL2024 / 0508 [ 00191 ] According to some embodiments , the solid water - insoluble precipitate is CaCO3 and regenerating a carbonated species chelator from the precipitate comprises heating the precipitate to induce thermal decomposition into carbon dioxide and a decarbonated solid material . According to some embodiments , the decarbonated solid material comprises CaO . According to some embodiments , regenerating a carbonated species chelator comprises mixing the decarbonated solid material with water . [ 00192 ] 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 . [ 00193 ] 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.mg / L . are [ 00194 ] 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 .

PCT / IL2024 / 0508 [ 00195 ] 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 CaCO3 which releases to the water both ²aC + ions and carbonate alkalinity . Thus , according to some embodiments , the separated precipitate of step ( III ) is dissolved and admixed the solution with the desalinated water thereby supplementing the desalinated water with calcium and carbonate ions . 2+ [ 00196 ] As detailed herein , the method 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 , a calciner 200 and a slaker 300 as described herein . [ 00197 ] According to some embodiments , the system comprises a pellet reactor 100 . Reference is now made to Figure 2 , which shows the pellet reactor 100 . [ 00198 ] According to some embodiments , step ( II ) comprises admixing in the pellet reactor 100 the saline water with the carbonated species chelator to form a solid water - insoluble precipitate and water . [ 00199 ] 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 . [ 00200 ] According to some embodiments , the pellet reactor 100 is a fluidized bed reactor . [ 00201 ] 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 CaCO3 grains ) , 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 PCT / IL2024 / 0508 reactor , circulated through a line in fluid communication with the reactor , and recycled back , at least partially , into the reactor . [ 00202 ] 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 130 . [ 00203 ] 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 . [ 00204 ] 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 . [ 00205 ] 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 . [ 00206 ] According to some embodiments , the pellet reactor 100 comprises a second fluid inlet pipe 112 . [ 00207 ] 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 . [ 00208 ] 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 Ca ( OH ) 2 composition . [ 00209 ] 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 .

PCT / IL2024 / 0508 According to some embodiments , the valve is configured to allow unidirectional flow of liquids into the enclosed reaction chamber 130 . [ 00210 ] 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 fluid composition from solids present therein , by flowing the fluid composition through the semi- permeable filter . [ 00211 ] According to some embodiments , the second fluid inlet pipe 112 is located in the vicinity of the enclosed reaction chamber bottom end 134 . [ 00212 ] 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 . [ 00213 ] 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 . [ 00214 ] 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 . [ 00215 ] 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 .

PCT / IL2024 / 0508 [ 00216 ] 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 . [ 00217 ] 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 . [ 00218 ] According to some embodiments , step ( II ) comprises providing an aqueous mixture of the carbonated species chelator through the fluid inlet pipe 110 . [ 00219 ] According to some embodiments , the method comprises pre - mixing the saline water and the carbonated species chelator to form an aqueous mixture , which is reacted in step ( II ) . [ 00220 ] According to some embodiments , step ( II ) comprises mixing the saline water provided in step ( I ) and the carbonated species chelator provided in step ( II ) , and flowing the mixture through the fluid inlet pipe 110 into the enclosed reaction chamber 130. According to some embodiments , step ( II ) comprises dissolving the carbonated species chelator in the saline water and inserting the formed solution into the reaction chamber 130 through the fluid inlet pipe 110 . [ 00221 ] 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 . [ 00222 ] 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 . [ 00223 ] 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 .

PCT / IL2024 / 0508 [ 00224 ] 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 . [ 00225 ] water . As further detailed above , step ( III ) comprises separating the precipitate from the [ 00226 ] 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 water ) and solids ( e.g. , the precipitate ) . In order to separate the precipitate from the water the solid may simply be filtered from the liquid using a standard filter which is permeable to water but impermeable to solids above a predetermined diameter . [ 00227 ] 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 . [ 00228 ] According to some embodiments , the fluid outlet pipe 120 is located in the vicinity of the enclosed reaction chamber top end 132 . [ 00229 ] 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 ) . [ 00230 ] 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 .

PCT / IL2024 / 0508 [ 00231 ] 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 . [ 00232 ] 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 . [ 00233 ] 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 method comprises first evacuating the water from the enclosed reaction chamber 130 and then evacuating the solid water - insoluble precipitate therefrom . [ 00234 ] 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 . [ 00235 ] According to some embodiments , the solid outlet pipe 150 is connected to the reaction chamber 130 in the vicinity of its bottom end 134 . [ 00236 ] 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 precipitate ) into the reaction chamber 130 through the solid inlet pipe 140 . [ 00237 ] Some advantages of the nucleation seeding step are detailed above . [ 00238 ] 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 .

PCT / IL2024 / 0508 [ 00239 ] According to some embodiments , step ( II ) further comprises fluidizing the nucleation seeds in the reaction chamber 130 . [ 00240 ] 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 . [ 00241 ] 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. , Ca ( OH ) 2 ) may be fed into the lower part of the reaction chamber 130. Also , nucleation seeds of the precipitate ( e.g. , CaCO3 seeds ) 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 Ca ( OH ) 2 which dissolves in the saline water , and subsequently increasing the concentration of calcium ions and the pH , which in turn promotes deprotonation of bicarbonate ions to carbonate ions . Then , the increase of the pH and concentration of calcium ions increases the concentration product of the calcium and 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 fed into the calciner 200 for further processing , according to some embodiments . To maintain the number of CaCO3 seeds within the enclosed reaction chamber 130 constant , new nucleation seeds may be periodically added to its top end 132 , through the solid inlet pipe 140 , to compensate for the ones that are discharged as pellets , according to some PCT / IL2024 / 0508 embodiments . The new seeds may be obtained from crushing large pellets and / or CaCO3 from any one of the steps of the present method . [ 00242 ] According to some embodiments , the nucleation seeds include crystals having a first average diameter . According to some embodiments , the precipitate species formed in step ( II ) includes pellets having a second average diameter . According to some embodiments , the CaCOseeds include crystals having a first average diameter . According to some embodiments , the CaCO3 formed in step ( II ) includes pellets having a second average diameter . [ 00243 ] 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 at the top end 132 of the reaction chamber 130 through the solid inlet pipe 140 , as smaller stars , which are fluidized . [ 00244 ] 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 . [ 00245 ] According to some embodiments , the solid inlet pipe 140 is connected to the reaction chamber 130 in the vicinity of its top end 132 . [ 00246 ] 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 each of the solid inlet pipe 140 and 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 at least HCO3 , and the chelator comprises Ca ( OH ) 2 ; step ( II ) comprises : dissolving the Ca ( OH ) 2 in the carbonated water and inserting the formed solution into the reaction chamber 130 through the fluid inlet pipe 110 ; inserting CaCO3 seeds into the reaction chamber 130 through the solid inlet pipe 140 in the vicinity of the reaction chamber top end 132 and fluidizing said seeds , thereby inducing precipitation of CaCO3 formed from a chemical reaction between the HCO3 and the Ca ( OH ) 2 , so that the formed CaCO3 is sinking to the bottom end 134 of the reaction chamber 130 and the water flows to the vicinity of the top end 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 CaCO3 from the bottom end 134 of the reaction chamber 130 through the solid outlet pipe 150 .

PCT / IL2024 / 0508 [ 00247 ] According to some embodiments , step ( III ) further comprises inserting seeds of the solid water - insoluble precipitate into the reaction chamber 130 through the solid inlet pipe 1and fluidizing the seeds in the reaction chamber 130 to a fluidized grains height 136 , thereby inducing precipitation and maturation of solid water - insoluble precipitate pellets . According to some embodiments , the carbonated species chelator is Ca ( OH ) 2 , wherein the fluidized bed pellet reactor 100 further comprises a solid inlet pipe 140 , wherein step ( III ) further comprises inserting seeds of the CaCO3 into 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 CaCO3 pellets . [ 00248 ] 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 . [ 00249 ] 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 meter . According to some embodiments , the fluidized grains height 136 is in the range of 0.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 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 6 meter . According to some embodiments , the fluidized grains height 136 is in the 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 PCT / IL2024 / 0508 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 meter . According to some embodiments , the fluidized grains height 136 is in the range of 9 meter to 12 meter . [ 00250 ] 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 . [ 00251 ] According to some embodiments , the fluidized grains height 136 is no more than 20 meter . According to some embodiments , the fluidized grains height 136 is no more than meter . According to some embodiments , the fluidized grains height 136 is no more than 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 . [ 00252 ] It is to be understood that the steps of the present method may occur alternately or simultaneously in a flow - type process . [ 00253 ] According to some embodiments , fluidizing said seeds in step ( II ) entails providing a pressurized stream of the saline water and chelator through the distributor plate 190 in the PCT / IL2024 / 0508 direction from the enclosed reaction chamber bottom end 134 to the enclosed reaction chamber top end 132 . [ 00254 ] According to some embodiments , further detailed herein , is the regeneration of the precipitate by dissociating the precipitate to form carbon dioxide and a decarbonated solid material . [ 00255 ] According to some embodiments , dissociation of the precipitate includes thermally , electrically or chemically dissociating the precipitate , or a combination thereof . Each possibility represents a separate embodiment of the invention . According to some embodiments , dissociation of the precipitate includes thermally dissociating the precipitate . According to some embodiments , dissociation of the precipitate includes calcining the precipitate . [ 00256 ] According to some embodiments , dissociating the precipitate comprises heating the precipitate to induce thermal decomposition into carbon dioxide and a decarbonated solid material . [ 00257 ] As detailed above , one particular precipitate is CaCO3 , according to some embodiments . When inducing thermal dissociation to CaCO3 it is dissociated into CO2 and CaO according the reaction scheme below : CaCO3 ) CaO + CO2 . [ 00258 ] According to some embodiments , the decarbonated solid material comprises CaO . According to some embodiments , the decarbonated solid material is CaO . [ 00259 ] According to some embodiments , the CO2 formed in the dissociation is in the gas form . According to some embodiments , the CO2 gas is isolated from the mixture and stored . According to some embodiments , the CO2 gas is stored in a dedicated container ( not shown ) or designated storage site ( such as underground geological formations , not shown ) . Suitable containers for CO2 storage , include , but not limited to gas cylinders . Other storage methods 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 . [ 00260 ] According to some embodiments , the process comprises dissolving a portion of the CaCO3 in an aqueous acidic composition comprising the carbon dioxide formed upon said thermal decomposition ; and admixing the solution with the desalinated water , thereby PCT / IL2024 / 0508 supplementing the desalinated water with calcium ions and carbonated species . According to some embodiments , the solid water - insoluble precipitate is CaCO3 and regenerating a carbonated species chelator from the portion of the precipitate comprises heating the portion of the CaCO3 to induce thermal decomposition into carbon dioxide and a decarbonated solid material ; and the process further comprises dissolving a portion of the CaCO3 in an aqueous acidic composition , the acidic composition comprising the carbon dioxide formed upon said thermal decomposition ; that the process further comprises admixing the solution with the desalinated water , thereby supplementing the desalinated water with calcium ions and carbonated species . [ 00261 ] According to some embodiments , the dissolution of the portion of the CaCO3 in the aqueous acidic carbon dioxide composition , entails performing an acid - base chemical reaction . [ 00262 ] According to some embodiments , the acid - base chemical reaction it represented by Scheme I. [ 00263 ] Scheme I : [ 00264 ] CaCO3 + CO2 + H2O → Ca ( HCO3 ) 2 .

According to some embodiments , the CaCO3 in 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 ) 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 . [ 00265 ] 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 Ia . [ 00266 ] Scheme Ia : CaCO3 + H2CO3 → Ca ( HCO3 ) 2 . [ 00267 ] Reference is now made to Figure 3 . [ 00268 ] According to some embodiments , the system described herein comprises a calciner 200. According to some embodiments , the precipitate is dissociated in the calciner 200 .

PCT / IL2024 / 0508 [ 00269 ] The term " calciner " generally refers to a steel cylinder that rotates inside a heated furnace and performs indirect high - temperature processing ( 550-1150 ° C ) within a controlled atmosphere . [ 00270 ] According to some embodiments , the calciner 200 is a circulating fluidized bed calciner . [ 00271 ] According to some embodiments , the calciner 200 comprises a solid inlet pipe 210 . According to some embodiments , the calciner 200 comprises a gas outlet pipe 220. According to some embodiments , the calciner 200 comprises a heating chamber 230 . [ 00272 ] According to some embodiments , the solid inlet pipe 210 is in fluid communication with the solid outlet pipe 150 of the pellet reactor 100 . [ 00273 ] According to some embodiments , the solid inlet pipe 210 is in fluid communication with the heating chamber 230 . [ 00274 ] According to some embodiments , the precipitate is inserted through the solid inlet pipe 210 into the heating chamber 230 . [ 00275 ] According to some embodiments , the solid inlet pipe 210 comprises a valve ( not shown ) configured to monitor the solid flow into the heating chamber 230. According to some embodiments , the valve is configured to allow unidirectional flow of solids into the heating chamber 230 . [ 00276 ] According to some embodiments , the gas outlet pipe 220 is in fluid communication with the heating chamber 230. According to some embodiments , the gas outlet pipe 220 is in fluid communication with the dedicated CO2 storage container ( not shown ) . [ 00277 ] According to some embodiments , elevating the temperature within the heating chamber 230 induces dissociating of the precipitate to form carbon dioxide gas and the decarbonated solid material . [ 00278 ] According to some embodiments , the carbon dioxide gas is evacuated through the gas outlet pipe 220 . [ 00279 ] According to some embodiments , the gas outlet pipe 220 comprises a valve ( not shown ) configured to monitor the gas flow out of the heating chamber 230. According to some embodiments , the valve is configured to allow unidirectional flow of gas away from the heating chamber 230 .

PCT / IL2024 / 0508 [ 00280 ] As detailed below , one option of dissociating the water - insoluble precipitate in the heating chamber 230 into carbon dioxide and a decarbonated solid material , involves combustion , according to some embodiments . As either oxygen gas or air may be used to promote the combustion , other gasses ( e.g. , water vapor and nitrogen gas ) may be present in the heating chamber 230 , and these may also be evacuated together with the CO2 gas . [ 00281 ] According to some embodiments , the heating chamber 230 is a combustion chamber . According to some embodiments , the heating chamber 230 comprises a furnace . [ 00282 ] According to some embodiments , the calciner further comprises an oxidizing gas inlet pipe 240. The oxidizing gas inlet pipe 240 is also referred as " first gas inlet pipe " in various sections of the present disclosure . According to some embodiments , the calciner further comprises reducing fluid pipe 250. The reducing fluid pipe 250 is also referred as " second gas inlet pipe " in various sections of the present disclosure . [ 00283 ] According to some embodiments , the oxidizing gas inlet pipe 240 is in fluid communication with the heating chamber 230. According to some embodiments , the reducing fluid pipe 250 is in fluid communication with the heating chamber 230 . [ 00284 ] According to some embodiments , the oxidizing gas inlet pipe 240 comprises a valve ( not shown ) configured to monitor the gas flow into the heating chamber 230. According to some embodiments , the valve is configured to allow unidirectional flow of oxidizing gas into the heating chamber 230 . [ 00285 ] According to some embodiments , the reducing fluid pipe 250 comprises a valve ( not shown ) configured to monitor the fluid flow into the heating chamber 230. According to some embodiments , the valve is configured to allow unidirectional flow of fluid into the heating chamber 230 . [ 00286 ] As detailed above , according to some embodiments , one product of the reaction of step ( II ) is water - insoluble precipitate ( e.g. , CaCO3 ) , which may be evacuated through the solid outlet pipe 150 of the pellet reactor 100. As , according to some embodiments , the solid outlet pipe 150 of the pellet reactor 100 is in fluid communication with the solid inlet pipe 210 of the calciner 200 , the formed precipitate , if not crushed and reused as nucleation seeds or for re- mineralizing the desalinated water with essential ions , may be fed to the calciner 200 through the solid inlet pipe 210. The calciner 200 , according to some embodiments , is a circulating fluidized bed reactor . It includes a heating chamber 230 , in which the precipitate is fluidized by a mix of reducing fluid ( s ) and air or oxygen , according to some embodiments . Reducing fluids PCT / IL2024 / 0508 include , but are not limited to , natural gas , oil and / or hydrogen gas . The gas mixture is combusted and the produced heat is used to thermally decompose the calcium carbonate pellets according to the following chemical reaction : [ 00287 ] [ 00288 ] CaCO3 ( s ) → CaO ( s ) + CO2 ( g ) According to some embodiments , following the thermal decomposition of the calcium carbonate pellets , the quicklime ( CaO ) solids are conveniently separated from the gas phase which contains CO2 from the decomposition of the CaCO3 as well as CO2 that originates from the combustion of the reducing fluid , optionally with water vapors and nitrogen ( if the reducing fluid was mixed with air rather than pure oxygen ) . Heat from the quicklime and the outgoing exhaust gas may be recovered using heat exchangers ( not shown ) , according to some embodiments . The gas phase is then evacuated through the gas outlet pipe 220 , according to some embodiments . Optionally , the gas it dried and sequestered in geologic formation in land or sea thereafter , according to some embodiments . The solid CaO formed in the dissociation reaction may then be evacuated and further processed as detailed below ( when discussing evacuation through the solid outlet 260 ) . [ 00289 ] According to some embodiments , elevating the temperature within the heating chamber comprises inserting a combustible gas through the reducing fluid pipe 250 ; inserting oxygen gas through the oxidizing gas inlet pipe 240 , and combusting the gas mixture in the combustion chamber 230 to elevate the temperature therein . [ 00290 ] According to some embodiments , the oxygen gas inserted into the combustion chamber 230 through the oxidizing gas inlet pipe 240 is provided therein as air . [ 00291 ] According to some embodiments , the method further comprises absorbing the heat produced in the combustion . Specifically , in order to maintain an environmentally friendly process the CO2 formed by the combustion is also stored and the resulting heat is used for power generation , according to some embodiments . According to some embodiments , absorbing the heat produced in the combustion is performed using a heat exchanger . Therefore , according to some embodiments , the system further comprises a heat exchanger configured to draw energy produced in the reaction within the heating chamber 230 . [ 00292 ] Also , as detailed with respect to the distributor plate 190 of the pellet reactor 100 , according to some embodiments , the calciner 200 may also include a distributor plate 290 . According to some embodiments , the calciner 200 comprises a distributor plate 290 configured PCT / IL2024 / 0508 to transfer a pressurized stream of the oxygen gas from the oxidizing gas inlet pipe 240 to the heating chamber 230 . [ 00293 ] Furthermore , as elaborated above , the decarbonated solid material , e.g. , CaO is used to regenerate the chelator molecules to be used in steps ( II ) . For this , the decarbonated solid material should be evacuated from the calciner 200 , according to some embodiments . [ 00294 ] According to some embodiments , the calciner 200 further comprises a solid outlet pipe 260 through which the decarbonated solid material is evacuated . According to some embodiments , the solid outlet pipe 260 is in fluid communication with the heating chamber 230 .

According to some embodiments , the solid outlet pipe 260 comprises a valve ( not shown ) configured to monitor the solid flow out of the heating chamber 230. According to some embodiments , the valve is configured to allow unidirectional flow of solids out of the heating chamber 230 . [ 00295 ] [ 00296 ] According to some embodiments , the method further comprises processing the decarbonated solid material into the carbonated species chelator . According to some embodiments , the method further comprises processing the decarbonated solid material into a carbonated species chelator to be reused in step ( II ) . [ 00297 ] Reference is now made to Figure 4 . [ 00298 ] According to some embodiments , the system comprises a slaker 300. According to some embodiments , the process further comprises processing the decarbonated solid material into a carbonated species chelator in the slaker 300 . [ 00299 ] According to some embodiments , the slaker 300 is a circulating fluidized bed steam slaker . [ 00300 ] According to some embodiments , the slaker 300 comprises a solid inlet pipe 310 . [ 00301 ] According to some embodiments , the slaker 300 comprises a steam inlet pipe 320 .

According to some embodiments , the slaker 300 is a water slaker , which comprises a water inlet pipe 320 . [ 00302 ] [ 00303 ] [ 00304 ] According to some embodiments , the slaker 300 comprises a slaking chamber 330 .

According to some embodiments , the slaker 300 comprises a solid outlet pipe 340 . [ 00305 ] According to some embodiments , the solid inlet pipe 310 of the slaker 300 is in fluid communication with the solid outlet 260 of the calciner 200. Specifically , as specified above , PCT / IL2024 / 0508 the decarbonated solid material produced in the calciner 200 is transferred for further processing in the slaker 300 . [ 00306 ] According to some embodiments , the solid inlet pipe 310 is in fluid communication with the slaking chamber 330 . [ 00307 ] According to some embodiments , each of the pipes 310 , 320 and 340 is in fluid communication with the slaking chamber 330 . [ 00308 ] According to some embodiments , processing the decarbonated solid material comprises inserting the decarbonated solid material into the slaking chamber 330 through the solid inlet pipe 310 . [ 00309 ] According to some embodiments , the solid inlet pipe 310 comprises a valve ( not shown ) configured to monitor the solid flow into the slaking chamber 330. According to some embodiments , the valve is configured to allow unidirectional flow of solids into the slaking chamber 330 . [ 00310 ] According to some embodiments , processing the decarbonated solid material further comprises inserting steam into the slaking chamber through the steam inlet pipe 320. According to some embodiments , processing the decarbonated solid material further comprises inserting water into the slaking chamber through the water inlet pipe 320 . [ 00311 ] According to some embodiments , processing the decarbonated solid material further comprises reacting the steam with the decarbonated solid material in the slaking chamber 330 to form a carbonated species chelator . According to some embodiments , processing the decarbonated solid material further comprises reacting the water with the decarbonated solid material in the slaking chamber 330 to form a carbonated species chelator . [ 00312 ] According to some embodiments , the steam inlet pipe 320 comprises a valve ( not shown ) configured to monitor steam flow into the slaking chamber 330. According to some embodiments , the valve is configured to allow unidirectional flow of steam into the slaking chamber 330. According to some embodiments , the steam inlet pipe 320 comprises a valve ( not shown ) configured to monitor water flow into the slaking chamber 330. According to some embodiments , the valve is configured to allow unidirectional flow of water into the slaking chamber 330 . [ 00313 ] According to some embodiments , processing the decarbonated solid material further comprises reacting the steam or water with the CaO in the slaking chamber 330 to form Ca ( OH ) 2 . The reaction scheme is shown below : PCT / IL2024 / 0508 [ 00314 ] CaO + H2O Ca ( OH ) [ 00315 ] According to some embodiments , processing the decarbonated solid material further comprises evacuating the carbonated species chelator through the outlet pipe 340 . [ 00316 ] According to some embodiments , the outlet pipe 340 comprises a valve ( not shown ) configured to monitor flow out of the slaking chamber 330. According to some embodiments , the valve is configured to allow unidirectional flow out of the slaking chamber 330 . [ 00317 ] According to some embodiments , the slaker 300 further comprises a steam outlet pipe 350. According to some embodiments , processing the decarbonated solid material further comprises evacuating excess steam from the slaking chamber 330 through the steam outlet pipe 350 . [ 00318 ] According to some embodiments , the steam outlet pipe 350 comprises a valve ( not shown ) configured to monitor flow of steam out of the slaking chamber 330. According to some embodiments , the valve is configured to allow unidirectional steam flow out of the slaking chamber 330 . [ 00320 ] [ 00319 ] According to some embodiments , there is provided a system as disclosed herein .

According to some embodiments , there is provided a system comprising : a fluidized bed pellet reactor comprising : a 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 each of the solid inlet pipe and the fluid outlet pipe is connected to the reaction chamber in the vicinity of its top end , 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 ; a circulating fluidized bed calciner comprising : a solid inlet pipe , a gas outlet pipe , a first gas inlet pipe , a second gas inlet pipe , a solid outlet pipe , and a combustion chamber , wherein each of the pipes is in fluid communication with the combustion chamber ; and a circulating fluidized bed steam slaker comprising : a solid inlet pipe , a steam inlet pipe , a solid outlet pipe , a steam outlet pipe and a slaking chamber , wherein each of the pipes is in fluid communication with the slaking chamber ; wherein the solid outlet pipe of the pellet reactor is in fluid communication with the solid inlet pipe of the calciner , wherein the solid outlet pipe of the calciner is in fluid communication with the solid inlet pipe of the slaker , and wherein the solid outlet pipe of the slaker is in fluid communication with the liquid inlet pipe of the pellet reactor .

EXAMPLES PCT / IL2024 / 0508 [ 00321 ] Seawater reverse osmosis ( SWRO ) desalination was performed on feed water with or without pre - treatment by the process according to certain embodiments of the present invention . [ 00322 ] Table 1 outlines typical feed water parameters . [ 00323 ] Table 1 .

Ion ( mg / l ) Water treatment without pre- Water with pre - treatment Hardness , as CaCO3 6438.27 6398.Ca 421.70 405.Mg 1313.70 1313.Na 11033.00 11033.K 408.41 408.NH4 0.00 0.Ba 0.000 0.0Sr 8.135 8.1H 0.00 0.CO3 14.23 25.HCO3 104.70 7.SO4 2775.60 2775.Cl 19804.20 19804.F 1.33 1.NO3 0.00 0.PO4 0.00 0.OH 0.13 3.SiO1.00 1.B 4.59 4.CO0.42 0.NH3 0.00 0.TDS 35890.59 35788.pH 8.10 9.

Saturations Water treatment without / CaSO4 ksp * 100 , % SrSO4 / ksp * 100 , % pre- Water with pre - treatment 26 BaSO4 / ksp * 100 , % SiO2 saturation , % CaF2 / ksp * 100 , % Ca3 ( PO4 ) 2 saturation index 0.21. 0.3.

PCT / IL2024 / 0508 CCPP , mg / l [ 00324 ] The feed waters with or without pre - treatment were then subjected to a SWRO 2- pass system operating on ³m002 / hr SW , Figures 1B and 1A , respectively . Numbers 1-14 in Figure 1A and Numbers 61–1 in Figure 1B represent different sampling points . The first Pass operated at 45 % recovery without energy recovery . The second pass feed in the water without pre - treatment case was injected with NaOH to elevate the pH and operate on the entire water stream derived from the first pass at 93 % recovery . No product conditioning has been added to the system in the example ( remineralization or disinfection ) . [ 00325 ] Tables 2A and 2B outline the parameters used for the RO with and without pre- treatment , respectively . [ 00326 ] Table 2A .

Perm . Flow / Vessel Stagewise Flux Flux Beta Pressure Pass - m3 / m3 / m3 / h h h Perm . Perm . TDS Imh Imh beta bar bar bar bar mg / 1-1 | 90.1 90.1 | 8.3 8.3 | 4.6 36.3 | 15.3 | 1.07 | 1 0 | 49.4 | 312.

Element type SWCMAX Element quantity PV # × Elem # 144 24 × 6M CPA7 - LD 24 4 × 6M 2-1 | 27.6 | 12.1 | 5.2 | 32.9 | 30.9 | 1.18 | 1 | 0 11.8 1. 0 10.7 4.1 CPA7 - LD 12 2 × 6M | 9.9 12.7 CPA7 - LD 6 1 × 6M 2-2 11.3 | 10.4 4.8 | 27.5 | 25.3 | 1.16 | 0.8 | 2-3 6.2 9.5 | 3.4 | 31.6 | 27.7 | 1.23 | 0.7 | [ 00327 ] The process operating according to embodiments of the present invention used half the stream of the first pass as feed of the second pass and the second pass system size was reduced in half . In addition , no additional NaOH was added to pass 2 .

Pass - Stage [ 00328 ] Table 2B .

Perm Flow Flux Flux Vessel Stagewise Pressure PCT / IL2024 / 0508 Element type Element quantity PV # × Elem # m3 / m3 / m3 / h h h Imh Imh beta bar bar bar bar mg / l 1-1 | | | 36.3 / 15.3 / 1.90.1 8.3 4.6 36.3 15.3 1.07 100 49.5 314.SWC144 24 x 6M MAX CPA7 - LD 48 8 × 6M CPA7 - LD 24 4 × 6M 09.4 19.2 CPA7 - LD 12 2 × 6M 2-1 | 51.3 | 11.2 | 4.8 | 30.7 [ 28.7 [ 1.18 [ 0.9 | 3 | 0 | 11.2 2.30 11.2 2.2-2 | 20.9 | 9.7 | 4.5 | 25.5 | 23.4 | 1.16 0.8 30 10.2 6.2-3 | 11.6 | 8.9 | 3.1 | 29.9 [ 26.11.23 | 0.6 | [ 00329 ] Tables 3A and 3B outline the water parameters following RO with and without pre- treatment , respectively . Numbers 1-16 in Table 3A refer to the different sampling points in Figure 1B and numbers 1-14 in Table 3B refer to the different sampling points in Figure 1A . [ 00330 ] Table 3A .

Flow Pressure TDS Econd Stream No. B ( m3 / h ) ( bar ) ( mg / l ) pH ( sμ / cm ) 200 0 35789 4.59 9.50 5642 ( Pass 1 feed ) 200 50.4 35789 4.59 9.50 5643 110 49.4 64842 7.88 9.31 9844 ( Pass 1 product ) 90.0 312 0.575 8.19 65 41.6 0 312 0.58.19 66 48.4 0 312 0.575 8.19 67 ( Pass 2 feed ) 48.4 12.8 312 0.575 8.19 68 20.8 11.8 725 1.07 8.53 159 9.54 10.7 1575 1.8.83 3010 3.39 9.86 4450 3.82 9.20 7811 3.39 0 4450 3.82 9.20 7812 27.6 3.00 1.41 0.201 6.15 2.13 11.3 3.00 4.09 0.440 6.63 8.14 6.18 0 12.7 0.722 7.14 26.15 45.0 0 3.64 0.332 6.58 7.16 ( Final product ) | 86.0 152 0.449 7.89 328 [ 00331 ] Table 3B .

PCT / IL2024 / 0508 Flow Pressure TDS Econd Stream No. B pH ( m3 / h ) ( bar ) ( mg / l ) ( sμ / cm ) 200 0 35891 4.59 8.10 5582 ( Pass 1 feed ) 200 50.5 35891 4.59 8.10 5583 110 49.5 65031 6.99 8.18 9804 ( Pass 1 product ) 90.0 0 315 1.66 6.79 65 90.0 0 317 1.66 9.60 86 ( Pass 2 feed ) 90.0 12.1 317 1.66 9.60 87 38.7 11.2 734 3.52 9.86 178 17.9 10.2 1583 6.96 10.1 346.30 9.43 4500 18.1 10.3 8410 6.30 0 4500 18.1 10.3 8411 51.3 3.00 2.14 0.253 7.75 5.12 20.9 3.00 6.17 0.576 8.22 17.13 11.6 0 19.2 0.982 8.72 56.14 ( Final product ) 83.7 0 5.51 0.435 8.17 15.NaOH dosing [ 00332 ] 2.3 mg / 1 ( as 100 % chemical ) Thus , the process which includes pre - treatment according to certain embodiments of the present invention showed significant reduction in boron levels already after the first pass . It can therefore obviate the need for a second pass or reduce the portion of water undergoing the second pass thus reducing the second pass size . Due to the increase in pH following the process of the present invention , it also allows a reduced dosage of caustic ( NaOH ) addition after the first pass . [ 00333 ] Table 4 outlines the parameters obtained by the conventional SWRO process ( left column ) vs. SWRO process according to embodiments of the present invention which altogether eliminates the second pass ( middle column ) or reduces the portion of water that undergoes the second pass ( right column ) .

PCT / IL2024 / 0508 [ 00334 ] Table 4 .

Pass 1 Inlet flow [ ³m / hr ] 200.00 200.00 200.Pass 1 Permeate Boron [ mg / 1 B ] 1.66 0.58 0.Pass 1 Permeate pH 6.79 8.8.

Pass 2 total Membranes Pass 2 Bypass flow [ ³m / hr ] 90.1 41.

Total Permeate Boron [ mg / l B ] 0.44 0.58 0.Total end product [ ³m / hr ] 83.7 90 86.Increased product compared to typical 7.5 % 3.5 % Overall system recovery 41.9 % 45.0 % 43.3 % Lower Pass 2 flow causes energy 0.75 0.reduction KW / ³m of : No Caustic to Pass 2 causes dosage 2.3 2.saving of caustic ( as 100 % mg / l ) of : Yearly dosage of NaOH ( 48 % ) [ Ton / yr ] 3. [ 00335 ] The process of the present invention therefore affords significant reduction of boron in the permeate , less occurrence of organic fouling ( due to the elevated pH of the effluent ) and reduced load of CCPP ( calcium carbonate precipitation potential ) thereby improving anti - scale effect . The CCPP is reduced from ~ 21 to -4 mg / l as CaCO3 , thus saving both capital and operational expenses . [ 00336 ] 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

1. A process for pre-treatment of saline water prior to desalination, the process comprising the steps of: (I) providing saline water comprising carbonated species selected from the group consisting of: CO2, H2CO3, HCO3-, CO3-2 and a combination thereof; (II) admixing a carbonated species chelator with the saline water of step (I) to form a solid water-insoluble precipitate; and (III) separating the water-insoluble precipitate of step (II) from the water thereby obtaining water suitable for subsequent desalination, wherein the process further comprises recovering the separated precipitate of step (III) and reusing at least a portion thereof by regenerating a carbonated species chelator from the portion of the precipitate for subsequent use in step (II), and optionally dissolving a portion of the recovered precipitate and admixing the solution with the desalinated water thereby supplementing the desalinated water with essential ions.

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

3. The process according to claim 1 or 2, wherein the saline water comprises HCO3- and CO3-2.

4. The process according to claim 3, wherein the saline water comprises 3 to 30HCO3- ions per one CO3-2 ion.

5. The process according to any one of claims 1 to 4, wherein the concentration of carbonated species in the saline water is at least 0.1 mM.

6. The process according to any one of claims 1 to 5, wherein the saline water of step (I) has pH in the range of 6 to 10.

7. The process according to any one of claims 1 to 6, wherein the salinity of the saline water of step (I) is in the range of 0.5 to 100 g/L.

8. The process according to any one of claims 1 to 7, wherein the carbonated species chelator is an inorganic base.

9. The process according to any one of claims 1 to 8, wherein the carbonated species chelator is a Ca+2 salt.

10. The process according to any one of claims 1 to 9, wherein the carbonated species chelator is Ca(OH)2.

11. The process according to claim 10, wherein the saline water comprises CO3-2, and wherein the admixing of saline water with the Ca(OH)2 in step (II) entails carrying out either of the following chemical reactions: CO2 + Ca(OH)2 → CaCO3 + H2O; H2CO3 + Ca(OH)2 → CaCO3 + 2H2O; HCO3- + Ca(OH)2 → CaCO3 + H2O + OH-; CO3-2 + Ca(OH)2 → CaCO3 + 2OH-; thereby producing CaCO3 as the solid water-insoluble precipitate and water suitable for subsequent desalination.

12. The process according to claim 11, wherein the saline water comprises HCO3-, and wherein the admixing of saline water with the Ca(OH)2 in step (II) entails carrying out the following chemical reaction: HCO3- + Ca(OH)2 → CaCO3 + H2O + OH-; thereby producing CaCO3 as the solid water-insoluble precipitate and water suitable for subsequent desalination.

13. The process according to any one of claims 1 to 12, wherein admixing a carbonated species chelator with the saline water to form a solid water-insoluble precipitate in step (II) further comprises adding nucleation seeds to the saline water.

14. The process according to claim 13, wherein the nucleation seeds comprise particles of the water-insoluble precipitate to the mixture of step (II).

15. The process according to any one of claims 1 to 14, wherein the solid water-insoluble precipitate is CaCO3.

16. The process according to any one of claims 1 to 15, wherein the solid water-insoluble precipitate is CaCO3 and regenerating a carbonated species chelator from the portion of the precipitate comprises heating the portion of the CaCO3 to induce thermal decomposition into carbon dioxide and a decarbonated solid material.

17. The process according to claim 16, wherein the process comprises dissolving a portion of the CaCO3 in an aqueous acidic composition comprising the carbon dioxide formed upon said thermal decomposition; and admixing the solution with the desalinated water, thereby supplementing the desalinated water with calcium ions.

18. The process according to claim 17, wherein the dissolution entails performing the following chemical reaction: CaCO3 + CO2 + H2O → Ca(HCO3)2.

19. The process according to any one of claims 16 to 18, wherein regenerating a carbonated species chelator comprises mixing the decarbonated solid material with water.

20. The process according to any one of claims 1 to 19, wherein the solid water-insoluble precipitate is CaCO3 and the process comprises dissolving a portion of the CaCO3 in acidic conditions and admixing the solution with the desalinated water thereby supplementing the desalinated water with calcium ions.

21. The process according to any one of claims 1 to 20, wherein the saline water comprises a boron species.

22. The process according to claim 21, wherein admixing the carbonated species chelator with the saline water in step (II), entails increasing hydroxide ion concentration within the water; and wherein upon the admixing in step (II) hydroxide ions within the water react with the boric acid to form a borate.

23. 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-, CO3-2 and a combination thereof; (II) admixing a carbonated species chelator with the saline water of step (I) to form a solid water-insoluble precipitate; (III) separating the water-insoluble precipitate of step (II) from the water; and (IV) desalinating the water of step (III), wherein the process further comprises recovering the separated precipitate of step (III) and reusing at least a portion thereof by regenerating a carbonated species chelator from the portion of the precipitate for subsequent use in step (II), and optionally dissolving a portion of the recovered precipitate and admixing the solution with the desalinated water of step (IV) thereby supplementing the desalinated water with essential ions.

24. The process according to claim 23, wherein the saline water comprises HCO3- and CO3-2.

25. The process according to claim 24, wherein the saline water comprises at least 2 HCO3- ions per one CO3-2 ion.

26. The process according to any one of claims 23 to 25, wherein the concentration of carbonated species in the saline water is at least 0.1 mM.

27. The process according any one of claims 23 to 26, wherein the saline water of step (I) has pH in the range of 7 to 9.

28. The process according to any one of claims 23 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 23 to 28, wherein the carbonated species chelator is a Ca+2 salt.

30. The process according to any one of claims 23 to 29, wherein the carbonated species chelator is Ca(OH)2.

31. The process according to claim 30, wherein the saline water comprises CO3-2, and wherein the admixing of saline water with the Ca(OH)2 in step (II) entails carrying out either of the following chemical reactions: CO2 + Ca(OH)2 → CaCO3 + H2O; H2CO3 + Ca(OH)2 → CaCO3 + 2H2O; HCO3- + Ca(OH)2 → CaCO3 + H2O + OH-; CO3-2 + Ca(OH)2 → CaCO3 + 2OH-; thereby producing CaCO3 as the solid water-insoluble precipitate and water suitable for subsequent desalination.

32. The process according to claim 31, wherein the saline water comprises HCO3-, and wherein the admixing of saline water with the Ca(OH)2 in step (II) entails carrying out the following chemical reaction: HCO3- + Ca(OH)2 → CaCO3 + H2O + OH-; thereby producing CaCO3 as the solid water-insoluble precipitate and water for subsequent desalination.

33. The process according to any one of claims 23 to 32, wherein admixing a carbonated species chelator with the saline water to form a solid water-insoluble precipitate in step (II) further comprises adding nucleation seeds to the saline water.

34. The process according to claim 33, wherein the nucleation seeds comprise particles of the water-insoluble precipitate to the mixture of step (II).

35. The process according to any one of claims 23 to 34, wherein the solid water-insoluble precipitate has aqueous solubility of no more than 100 mg/L at 25℃.

36. The process according to any one of claims 23 to 35, wherein the solid water-insoluble precipitate is CaCO3.

37. The process according to any one of claims 23 to 36, wherein the solid water- insoluble precipitate is CaCO3 and regenerating a carbonated species chelator from the portion of the precipitate comprises heating the portion of the CaCO3 to induce thermal decomposition into carbon dioxide and a decarbonated solid material.

38. The process according to claim 37, wherein regenerating a carbonated species chelator comprises mixing the decarbonated solid material with water.

39. The process according to any one of claims 23 to 38, wherein the solid water- insoluble precipitate is CaCO3 and the process comprises dissolving a portion of the CaCO3 in acidic conditions and admixing the solution with the desalinated water thereby supplementing the desalinated water with calcium ions.

40. The process according to any one of claims 23 to 39, wherein desalinating the water comprises reverse osmosis.

41. The process according to claim 40, wherein 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.

42. The process according to any one of claims 23 to 41, wherein the saline water comprises a boron species.

43. The process according to claim 42, wherein admixing the carbonated species chelator with the saline water in step (II), entails increasing hydroxide ion concentration within the water; and wherein upon the admixing in step (II) hydroxide ions within the water react with the boric acid to form a borate.

44. A process for enhancing the removal of boron species from saline water undergoing desalination, the process comprising the steps of: (I) providing saline water comprising carbonated species selected from the group consisting of: CO2, H2CO3, HCO3-, CO3-2 and a combination thereof, wherein the saline water comprises a boron species at a first boron species concentration; (II) admixing a carbonated species chelator with the saline water of step (I) to form a solid water-insoluble precipitate; (III) separating the water-insoluble precipitate of step (II) from the water; and (IV) desalinating the water of step (III) to form desalinated water having a second boron species concentration, which is at least 10% lower than the first boron species concentration.

45. The process according to claim 44, wherein the boron species concentrations after a single reverse osmosis cycle are less than 1.5 mg/L.

46. The process according to any one of claims 44 to 45, wherein the carbonated species chelator is Ca(OH)2.

47. The process according to claim 46, wherein the boron species comprises boric acid.

48. The process according to claim 47, wherein upon admixing the Ca(OH)2 chelator with the saline water, the hydroxide ions within the mixture of step (II) react with the boric acid to form a borate.

49. The process according to claim 48, wherein the desalination of step (IV) entails passing the water of step (III) through a selective membrane, which selectively prevents passage of borate over boric acid, thereby reducing the boron species concentration withing the water.

50. The process according to claim 49, wherein 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. For the Applicant, WeBB+Co. Patent Attorneys