Sustainable desalination plant and sustainable method for the desalination of water

Abstract

A sea water desalination process and plant wherein intake sea water is delivered to at least one reverse osmosis pass comprising at least one reverse osmosis membrane to produce permeate product water and brine; wherein at least a portion of the brine is delivered to at least one reactor 2 for the removal of carbonates-based chemical in the brine by precipitating calcium carbonate. The calcium carbonate is converted in a regenerator 10 to produce calcium hydroxide and carbon dioxide. This provides for a series of benefits in the overall cost efficiency and sustainability of the process / plant.

Description

[0001] Sustainable Desalination Plant and Sustainable Method for the Desalination of Water.

[0002] Field of the Invention.

[0003] The present invention relates generally to a more environmentally sustainable production of desalinated water and to a sustainable desalination plant.

[0004] Background

[0005] Desalination is a process that removes mineral components from sea water to provide water that is suitable for human consumption or irrigation. The by-product of the desalination process is brine, a super concentrated solution. A conventional seawater desalination plant delivers sea water, via an intake channel, through various pretreatment sites such as filters before being pumped under pressure through multiple reverse osmosis passes to form desalinated product water and concentrated sea water or brine. During this process, other minerals in addition to salt are removed from the water which must be re-introduced to provide an acceptable product water and therefore the water is also subjected to post-treatments, such as pH adjustment and the addition of minerals such as magnesium before being held in a holding tank for later consumption. The brine may be discharged back into the sea via a discharge channel or subjected to a further desalination process to create additional product water.

[0006] Conventional desalination processes and plants may include a single pass (as shown in Figure 1) or a double pass (see Figure 2), depending upon the required product water quality. One desalination process and system operated by the Applicant, IDE Technologies, is the two-pass concept as shown in Figure 2 where sea water is delivered through an intake channel through a filtration module to a clearwell from which it is passed through a first sea water reverse osmosis pass (SWRO) with the brine then passing through a brackish water reverse osmosis (BWRO) pass. The combined permeate from both passes is then treated to provide final product water quality. This process and system use chemicals which are both very costly and affect the sustainability level of the process / plant. In the current two-pass SWRO process as shown in Figure 1 the main chemicals used for operation are sodium hydroxide (NaOH), sulphuric acid (H2SO4), calcium carbonate (CaCO3) and carbon dioxide (CO2). The sodium hydroxide and sulphuric acid are used for boron rejection in the BWRO pass while calcium carbonate and carbon dioxide are used for final product remineralization in the post treatment stage. The cost of these chemicals is significant. It is desirable to improve this process to substantially reduce the total cost of the chemicals. Moreover, it would be advantageous to provide a self-sustainable desalination process / plant, or at least one that is partially self- sustainable, to self-produce the required chemicals for its own operation.

[0007] It is an object of the present invention to provide an improved fluid treatment process and plant that aims to address this issue.

[0008] Summary of the Invention

[0009] According to one aspect the present invention provides a process for treating fluids, the process comprising: feeding at least a portion of the fluids through at least one reactor for the removal of carbonates-based chemical.

[0010] In preferred embodiments of the process according to the first aspect of the invention, the fluids are selected from a group consisting of brine, effluents, waste and any combination thereof.

[0011] Preferably, said fluids are provided from a filtration process; said filtration being selected from a group consisting of desalination of seawater, reverse osmosis, forward osmosis, pressure-retarded osmosis, ultrafiltration, microfiltration and nanofiltration any combination thereof; optionally wherein said reactor is positioned in at least one location selected from a group consisting of prior to said filtration, post said filtration and any combination thereof.

[0012] It is preferable for the process according to the first aspect to include the step of containing or introducing into the reactor at least one selected from a group consisting of calcium hydroxide (Ca(OH)2), NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3). Alternatively or additionally, the process as defined above, may include the step of containing or introducing into the reactor at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3), according to the following formula: Ca(OH)2 + Ca(HCO3)2 -> 2CaCO3 + 2H2O.

[0013] Preferably, the process further comprises introducing calcium hydroxide (Ca(OH)2) into the at least one reactor.

[0014] More preferably still, the process comprises feeding at least a portion of brine through the at least one reactor containing or having introduced therein at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to increase the pH of the brine to at least pH 8.3.

[0015] The process as defined above may further comprise desalinating intake sea water comprising delivering the intake water to at least one pass comprising at least one reverse osmosis membrane to produce permeate water and brine.

[0016] Preferably, the process as defined above, further comprises the step of regenerating at least some of the calcium carbonate precipitant to a calcium- based chemical and carbon dioxide.

[0017] The calcium-based chemical as defined above may be selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.

[0018] More preferably, the step of regenerating the calcium carbonate to the calcium-based chemical comprises a method selected from at least one of calcinating the precipitated calcium carbonate, hydrolysing the precipitated calcium carbonate and any combination thereof.

[0019] In a preferred embodiment, the step of regenerating the calcium carbonate comprises calcination comprising heating the calcium carbonate to a temperature of at least 500°C.

[0020] Alternatively, or additionally, the step of regenerating the calcium carbonate comprises hydrolysing the calcium carbonate to produce at least one selected from the group consisting of calcium hydroxide, calcium oxide, carbon dioxide and any combination thereof. Preferably, said step of hydrolysis of the calcium carbonate is performed at a temperature of less than 500°C.

[0021] In preferred embodiments of the process of the invention, the calcium-based chemical is calcium oxide and the process further comprises mixing at least a portion of the calcium oxide with at least a portion of intake sea water and / or at least a portion of the brine and / or RO desalinated product water to form calcium hydroxide.

[0022] In further embodiments of the process as defined above, at least a portion of the calcium hydroxide formed by regeneration of the calcium carbonate is at least one selected from (a) recycled for use in the at least one reactor; (b) used in the post treatment process; (c) any combination thereof.

[0023] The process according to the first aspect of the invention as defined above may further comprise feeding at least a portion of brine through the at least one reactor containing calcium hydroxide (Ca(OH)2) to also precipitate magnesium hydroxide.

[0024] Preferably, the process as defined above, further comprises the step of regenerating at least some of the magnesium hydroxide precipitant to a magnesium-based chemical.

[0025] The process as defined above, may further comprise adding at least a portion of the regenerated magnesium-based chemical to the permeate to produce product water.

[0026] More preferably, the process as defined above, wherein feeding at least a portion of brine through the at least one reactor containing calcium hydroxide (Ca(OH)2) also precipitates magnesium hydroxide, further comprises the steps of (i) regenerating at least some ofthe calcium carbonate and magnesium hydroxide precipitants to produce a calcium- based chemical, a magnesium-based chemical and carbon dioxide; and, (ii) mixing at least some of the regenerated chemicals and carbon dioxide with the permeate product water to produce drinking water.

[0027] In embodiments of the process according to the present invention only a portion of the brine is fed through the reactor with the remaining brine bypassing the at least one reactor.

[0028] Optionally, the process as defined above, further comprises the step of mixing said portion of the brine fed through the at least one reactor with the remaining brine bypassing the at least one reactor. The process according to the first aspect of the invention as defined above, may optionally further comprise delivering at least a portion of the sea water to at least one of a filter unit and a clearwell.

[0029] The process according to the invention may further comprise passing at least a portion of the permeate from the reverse osmosis membranes of a first pass to a second pass of brackish water reverse osmosis. Optionally, the process may further comprise adding at least one of sodium hydroxide or calcium hydroxide to the permeate prior to its introduction to the second pass.

[0030] The process as defined above may further comprise regenerating the calcium hydroxide from the calcium carbonate precipitant and adding at least a portion of the regenerated calcium hydroxide to the permeate prior to its introduction to the second pass. Preferably, at least a portion of the calcium carbonate, (CaCO3), is used in the post treatments of the permeate water post the desalination step.

[0031] According to a second aspect of the present invention there is provided a plant for treating fluid comprising at least one conduit for delivering at least a portion of the fluid to the at least one reactor for the removal of carbonates-based chemical.

[0032] In preferred embodiments of the plant according to the second aspect of the invention, said fluids are selected from a group consisting of brine, effluents, waste and any combination thereof. Preferably, said fluids are provided from a filtration process; said filtration being selected from a group consisting of desalination of seawater, reverse osmosis, forward osmosis, pressure-retarded osmosis, ultrafiltration, microfiltration and nanofiltration any combination thereof; further wherein said reactor is positioned in at least one location selected from a group consisting of prior to said filtration, post said filtration and any combination thereof.

[0033] In further embodiments of the plant as defined above, said at least one reactor may have a calcium hydroxide (Ca(OH)2) source to precipitate at least one carbonates- based chemical selected from a group consisting of calcium carbonate (CaCO3).

[0034] Preferably, the reactor of the plant may contain or have introduced at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof introduced therein to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCCh), according to the following formula: Ca(OH)2 + Ca(HCO3)2 --> 2CaCO3 + 2H2O.

[0035] In preferred embodiments of the plant according to the second aspect of the invention there is provided at least one regeneration module to convert at least some of the calcium carbonate precipitant to a calcium-based chemical and carbon dioxide. Said at least one regeneration module may be selected from at least one of a calcinatory, a hydrolysis reactor and any combination thereof.

[0036] In embodiments of the plant according to the invention, said at least one regeneration module is a calcinatory provided for calcinating the precipitated calcium carbonate to produce at least one of calcium hydroxide, calcium oxide, carbon dioxide and any combination thereof. The calcinatory may comprise a rotary kiln for calcination of the calcium carbonate.

[0037] Alternatively or additionally, the at least one regeneration module comprises at least one hydrolysis reactor for hydrolysing the calcium carbonate to produce at least one selected from a group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO), carbon dioxide (CO2) and any combination thereof. Preferably, said hydrolysis reactor operates at a temperature of less 500°C.

[0038] The plant according to the second aspect of the invention as defined above, wherein a calcinatory is provided for calcinating the precipitated calcium carbonate, preferably produces calcium oxide and the plant further comprises at least one mixing reactor adapted to mix at least a portion of the calcium oxide with at least a portion of the intake sea and / or at least a portion of the brine to produce calcium hydroxide (Ca(OH)2).

[0039] In preferred embodiments, the plant includes at least one pipe provided to deliver at least one, preferably both, of a portion of the calcium -based chemical and carbon dioxide formed by the regeneration module to the permeate produced by the at least one reverse osmosis membrane to produce the product water.

[0040] Alternatively or additionally, the plant includes at least one pipe to recycle at least a portion of the calcium-based chemical formed by the regeneration module to the at least one reactor. In embodiments, the at least one reactor also precipitates magnesium hydroxide from the brine and at least one regeneration module is configured to regenerate at least some of the magnesium hydroxide precipitant to a magnesium-based chemical. Preferably, the plant includes at least one pipe to deliver at least a portion of the magnesium-based chemical formed by the regeneration module to the permeate produced by the at least one reverse osmosis membrane to produce drinking water.

[0041] In preferred embodiments of the plant according to the second aspect of the invention, the at least one reactor having a calcium hydroxide (Ca(OH)2) source also precipitates magnesium hydroxide; and, the plant further comprises at least one regeneration module regenerating at least some of the calcium carbonate and magnesium hydroxide precipitants to produce a calcium- based chemical, a magnesium-based chemical and carbon dioxide and piping to deliver at least some of the regenerated chemicals and carbon dioxide to the permeate product water to produce drinking water.

[0042] In embodiments, the plant according to the invention may include a bypass between the intake sea water and the reverse osmosis pass to enable the delivery of a portion of the sea water through the at least one reactor with the remaining intake sea water bypassing the at least one reactor.

[0043] Optionally, the plant as defined above, may include at least one of a filter unit and / or a clearwell provided between the at least one reactor and the pass.

[0044] In preferred embodiments, the at least one reactor is a fluidized bed reactor.

[0045] The plant according to the second aspect of the invention may further comprise a second brackish water reverse osmosis pass in fluid communication with the first pass, wherein at least a portion of the permeate from the first pass is delivered to the second pass. Preferably, at least one of a sodium hydroxide and calcium hydroxide source and any combination is provided between the first and second pass to introduce sodium hydroxide or calcium hydroxide to the permeate prior to its introduction to the second pass.

[0046] In preferred embodiments of the plant as defined above, delivery of at least a portion of the brine through the at least one reactor results in an increase in pH of the at least a portion of the brine to a pH of at least 8.3. In embodiments of the plant according to the second aspect of the invention only a portion of the brine is fed through the reactor with the remaining brine bypassing the at least one reactor.

[0047] According to a preferred embodiment of the first aspect of the present invention there is provided a process for the desalination of sea water, the process comprising: desalinating an intake of sea water to produce permeate product water and brine; and feeding at least a portion of the brine through at least one reactor for the removal of carbonates-based chemicals from the brine.

[0048] Preferably, the reactor contains or has introduced therein at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3).

[0049] Preferably, the reactor containing or is introduced with at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3), according to the following formula: Ca(OH)2 + Ca(HCO3)2 — > 2CaCO3 + 2H2O.

[0050] Preferably, the process includes the step of introducing calcium hydroxide (Ca(OH)2) into the at least one reactor. Desalinating said intake sea water preferably comprises delivering the intake water to at least one pass comprising at least one reverse osmosis membrane to produce the permeate water and brine. Preferably, the process may include feeding at least a portion of intake sea water through at least one reactor containing or having introduced therein at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof increases the pH of the intake water to at least pH 8.3. This enhances the boron rejection by the at least one reverse osmosis membrane to increase the overall efficiency of the process.

[0051] It is preferable for the process to include a step of regenerating chemicals from the calcium carbonate precipitant which may be re-used in the process, thereby enhancing the sustainability of the process. In a preferred embodiment, the process further comprises converting at least some of the calcium carbonate precipitant to a calcium- based chemical and carbon dioxide. The precipitated calcium carbonate may produce at least one selected from a group consisting of calcium hydroxide, calcium oxide, carbon dioxide and any combination thereof. Preferably, the calcium-based chemical is calcium hydroxide (Ca(OH)2). More preferably, the process comprises adding at least a portion of the converted calcium-based chemical and carbon dioxide to the permeate to produce product water.

[0052] The conversion of the calcium carbonate to the calcium-based chemical may comprise a method selected from at least one of calcinating the precipitated calcium carbonate, hydrolysing the precipitated calcium carbonate and any combination thereof. If the calcium-based chemical is calcium oxide, the process may further comprise mixing at least a portion of the calcium oxide with at least a portion of intake sea water to form calcium hydroxide.

[0053] In one embodiment, the step of regenerating the calcium carbonate comprises calcination comprising heating the calcium carbonate to a temperature of at least 500°C.

[0054] In an alternative embodiment, the step of regenerating calcium carbonate comprises hydrolysing the calcium carbonate to produce at least one selected from the group consisting of calcium hydroxide, calcium oxide, carbon dioxide and any combination thereof. Preferably, said step of hydrolysis of the calcium carbonate is performed at a temperature of less than 500°C.

[0055] The sustainability of the process may be further enhanced by at least a portion of the calcium hydroxide formed by conversion of the calcium carbonate being recycled for use in the at least one reactor. Preferably, at least a portion of the calcium hydroxide formed by regeneration of the calcium carbonate is at least one selected from (a) recycled for use in the at least one reactor; (b) used in the post treatment process; (c) any combination thereof.

[0056] Optionally, feeding at least a portion of intake sea waterthroughthe at least one reactor containing or is introduced with at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof also precipitates magnesium hydroxide (Mg(OH)2). The process may further comprise the step of regenerating at least some of the magnesium hydroxide precipitant to a magnesium- based chemical. At least a portion of the regenerated magnesium-based chemical may be added to the permeate to produce product water. Alternatively, the at least a portion of intake water is fed through at least one second reactor adapted to precipitate magnesium-based chemical selected from a group consisting of magnesium hydroxide, magnesium oxide and any combination thereof.

[0057] Alternatively, at least a portion of the magnesium-based chemical (MgOH or MgO) is at least one selected from (a) recycled for use in the at least one reactor; (b) used in the post treatment process; (c) any combination thereof.

[0058] All of the sea water may pass through the at least one reactor or only a portion of the sea water may be fed through the reactor with the remaining intake sea water bypassing the at least one reactor. The process may further comprise a step of mixing said portion of the sea water fed through the at least one reactor with the remaining intake sea water bypassing the at least one reactor.

[0059] The process may include passing at least a portion of the sea water through at least one filter unit. Additionally, or alternatively, the intake sea water may be delivered to a clearwell.

[0060] In one embodiment of the process of the invention at least a portion of the permeate from the at least one reverse osmosis membrane of a first pass is delivered to a second pass of brackish water reverse osmosis. Preferably, at least one of sodium hydroxide or calcium hydroxide is added to the permeate prior to its introduction to the second pass. More preferably, calcium hydroxide regenerated from the conversion of precipitated calcium carbonate is added to the permeate prior to its introduction into the second pass.

[0061] The process according to the invention preferably excludes a calcium carbonate contactor in the post-treatment of the permeate water. The ability to provide a process having a post treatment method with no carbonate contactor reactors also provides a significant benefit. Carbonate contactors are relatively huge reactors, but the current process requires only smaller (Ca(OH)2) reactors to deliver the final product. This is possible due to the reverse osmosis passes operating at higher pH to provide better biofouling resistance and better boron rejection, enabling the use of only (Ca(OH)2) reactors without the need for CaCCh reactors.

[0062] According to a preferred embodiment of the second aspect of the present invention there is provided a desalination plant having enhanced sustainability, the system comprising: at least one conduit for delivering at least a portion of an intake sea water to at least one reverse osmosis pass comprising at least one reverse osmosis membrane, to produce permeate product water and brine; and at least one conduit for delivering at least a portion of the brine to at least one reactor for the removal of carbonates-based chemical in the brine.

[0063] Preferably, said at least one reactor has a calcium hydroxide (Ca(OH)2) source to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3).

[0064] Preferably, the reactor contains or has introduced therein at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof introduced therein to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3), according to the following formula: Ca(OH)2 + Ca(HCO3)2 --> 2CaCO3 + 2H2O.

[0065] Preferably, at least one regeneration module is provided to convert at least some of the calcium carbonate precipitant to a calcium-based chemical and carbon dioxide. The at least one regeneration module may be selected from at least one of a calcinatory, a hydrolysis reactor and any combination thereof as hereinbefore defined.

[0066] It is preferable for at least a portion of the calcium hydroxide, Ca(OH)2, to be recycled for use in the at least one at least one reactor.

[0067] In one embodiment, the calcinatory provided for calcinating the precipitated calcium carbonate may produce calcium oxide and the system further comprises at least one mixing reactor adapted to mix at least a portion of the calcium oxide with at least a portion of the intake sea water to produce calcium hydroxide (Ca(OH)2).

[0068] Preferably, the system includes at least one pipe is provided to deliver at least one, preferably both, of a portion of the calcium -based chemical and carbon dioxide formed by the regeneration module to the permeate produced by the at least one reverse osmosis membrane to produce the product water. Alternatively or, more preferably, additionally, the system includes at least one pipe is provided to recycle at least a portion of the calcium-based chemical formed by the regeneration module to the at least one reactor. The at least one reactor may also precipitate magnesium hydroxide from the intake sea water and at least one regeneration module is configured to regenerate at least some of the magnesium hydroxide precipitant to a magnesium-based chemical. The system may further comprise at least one pipe to deliver at least a portion of the magnesium-based chemical formed by the regeneration module to the permeate produced by the at least one reverse osmosis membrane to produce drinking water.

[0069] In one embodiment, a bypass may be provided between the intake sea water and the reverse osmosis pass to enable the delivery of a proportion of the sea water through the at least one reactor with the remaining intake sea water bypassing the at least one reactor.

[0070] At least one, preferably both, of a filter unit and a clearwell is provided between the at least one reactor and the pass.

[0071] Preferably, the at least one reactor is a fluidized bed reactor.

[0072] The system may further comprise a second brackish water reverse osmosis pass (BWRO) is in fluid communication with the first pass, wherein at least a portion of the permeate from the first pass is delivered to the second pass. Preferably, at least one of a sodium hydroxide and / or calcium hydroxide source is provided between the first and second pass to introduce sodium hydroxide or calcium hydroxide to the permeate prior to its introduction to the second pass. Preferably, a double pass is employed to improve rejection of boron. Less sodium hydroxide or calcium hydroxide may be used than in a conventional two pass SWRO / BWRO process due to the higher pH of the SWRO permeate and better boron rejection at high pH in the SWRO. Post treatment reactors may again be replaced with the simple addition of calcium hydroxide and carbon dioxide to form the final product as with the single pass process and system, without the need for calcium carbonate contactors.

[0073] Preferably, at least a portion of the intake sea water delivered through the at least one reactor results in an increase in pH of the at least a portion of the intake water to a pH of at least 8.3, thereby enhancing boron rejection by said at least one reverse osmosis membrane to increase the overall efficiency of the desalination system.

[0074] A third aspect of the present invention provides a self-sustainable desalination process for the desalination of sea water, the process comprising: delivering sea water to an intake pipe; delivering under pressure all the intake water to at least one pass comprising at least one reverse osmosis membrane to produce permeate and brine; introducing calcium hydroxide (Ca(OH)2) into at least one reactor; passing at least a portion of the brine through the reactor to precipitate at least calcium carbonate (CaCOs) from the brine; regenerating at least some of the calcium carbonate (CaCOs) precipitant to at least one selected from the group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO) and carbon dioxide (CO2) and any combination thereof; and adding at least a portion of at least one of the calcium hydroxide (Ca(OH)2), calcium oxide (CaO) and carbon dioxide (CO2) and any combination thereof regenerated from the calcium carbonate (CaCOs) precipitant to at least one of (i) the permeate to produce product water and (ii) the at least one reactor, and any combination thereof.

[0075] The process may further comprise introducing calcium hydroxide (Ca(OH)2) into at least one reactor and passing at least a portion of the intake sea water through the reactor to precipitate at least calcium carbonate (CaCOs) from the sea water.

[0076] According to one embodiment of the present invention, the step of regenerating at least some of the calcium carbonate precipitant preferably comprises a method selected from at least one of calcinating the precipitated calcium carbonate, hydrolysing the precipitated calcium carbonate and any combination thereof. Preferably, said step of regenerating at least some of the calcium carbonate precipitant results in calcium- based chemical selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.

[0077] According to a fourth aspect of the present invention there is provided a self- sustainable desalination system for the desalination of sea water, the system comprising: a sea water intake; at least one reverse osmosis pass comprising at least one reverse osmosis membrane, wherein all the intake sea water is delivered through the pass to produce permeate and brine; at least one reactor having a calcium hydroxide (Ca(OH)2) source; at least one conduit for delivering at least a portion of the brine to the at least one reactor to precipitate calcium carbonate (CaCO3); at least one regeneration module to convert at least some of the calcium carbonate (CaCO3) precipitant to at least one selected from a group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO), carbon dioxide (CO2) and any combination thereof; and a recycling system to deliver at least a portion of at least one of the calcium hydroxide (Ca(OH)2), calcium oxide (CaO) and carbon dioxide (CO2) and any combination thereof regenerated from the calcium carbonate (CaCO3) precipitant to at least one of (i) the permeate to produce product water and (ii) the at least one reactor and any combination thereof.

[0078] The system may further comprise may at least one reactor having a calcium hydroxide (Ca(OH)2) source and at least one conduit for delivering at least a portion of the sea water from the intake to the at least one reactor to precipitate calcium carbonate (CaCO3).

[0079] Preferably, the at least one regeneration module is selected from at least one of calcinator, hydrolysing module and any combination thereof. The at least one regeneration module preferably results in calcium-based chemical selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.

[0080] A fifth aspect of the present invention provides a calcium carbonate reactor-free posttreatment desalination method for the treatment of permeate water comprising step of adding at least one of calcium hydroxide (Ca(OH)2) and magnesium hydroxide (Mg(OH)2) to intake sea water prior to desalinating the same, wherein said posttreatment desalination method is free of calcium carbonate reactor. Preferably, at least one of the calcium hydroxide (Ca(OH)2) and magnesium hydroxide (Mg(OH)2) is regenerated from the carbonate precipitated during said step of adding at least one of calcium hydroxide (Ca(OH)2) and magnesium hydroxide (Mg(OH)2) to intake sea water.

[0081] The post-treatment method may further comprise feeding at least a portion of intake sea water through at least one reactor, the reactor containing or is introduced therein with at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate calcium carbonate (CaCO3) and regenerating calcium hydroxide (Ca(OH)2) and carbon dioxide (CO2), wherein the regenerated calcium hydroxide is added to the reactor and for post-treatment of the permeate water and the carbon dioxide is used for post-treatment of the permeate water.

[0082] Feeding at least a portion of intake sea water through the at least one reactor may also precipitate magnesium hydroxide (Mg(OH)2) for post-treatment of the permeate water.

[0083] The post-treatment method may include desalinating said intake sea water comprising delivering the intake water to at least one pass comprising at least one reverse osmosis membrane to produce the permeate water and brine. Preferably, the post-treatment method further comprises the step of regenerating at least some of the calcium carbonate precipitant to a calcium- based chemical and carbon dioxide, wherein the calcium-based chemical is selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof. Preferably, regenerating the calcium carbonate to the calcium-based chemical comprises a method selected from at least one of calcinating the precipitated calcium carbonate, hydrolysing the precipitated calcium carbonate and any combination thereof. In a post-treatment method wherein the calcium-based chemical is calcium oxide, the process may further comprise mixing at least a portion of the calcium oxide with at least a portion of intake sea water to form calcium hydroxide. The product water produced by the various aspects of the invention preferably comprises drinking water.

[0084] Any excess of the produced chemicals, such as calcium-based, magnesium-based and carbon dioxide may be sold as an additional income.

[0085] It is to be appreciated that different types of regeneration methods and systems may be used for the production of calcium hydroxide, calcium oxide and carbon dioxide from the precipitated calcium carbonate and / or for regeneration of magnesium-based chemicals from magnesium hydroxide, as are known in the art.

[0086] It is another aspect of the present invention to provide a process for treating fluids, the process comprising: feeding at least a portion of the fluids through at least one reactor for the removal of carbonates-based chemical.

[0087] It is within the scope of the present invention where the fluids are selected from a group consisting of brine, effluents, waste and any combination thereof.

[0088] It is within the scope of the present invention where the fluids are provided from filtration process; said filtration are selected from a group consisting of desalination of seawater, reverse osmosis, forward osmosis, pressure-retarded osmosis, ultrafiltration, microfiltration and nanofiltration any combination thereof; further wherein said reactor is positioned in at least one location selected from a group consisting of prior to said filtration, post said filtration and any combination thereof.

[0089] The following disclosure is provided for brine fluids but is could be applied for any kind of fluids (e.g., effluents, brackish water etc.).

[0090] Thus, according to aspects of the present invention there is provided a process for the desalination of sea water, the process comprising: desalinating intake sea water to produce permeate product water and brine; feeding at least a portion of the brine through at least one reactor for the removal of carbonates-based chemical. In the process as defined above, the reactor may contain or have introduced thereto at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCOs).

[0091] In the process as defined above, the reactor may contain or have introduced thereto at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCCh), according to the following formula: Ca(OH)2 + Ca(HCO3)2 -> 2CaCO3 + 2H2O.

[0092] The process as defined above, preferably includes feeding at least a portion of brine through at least one reactor containing or having introduced therein at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to increase the pH of the brine to at least pH 8.3.

[0093] In embodiments, desalinating said intake sea water may comprise delivering the intake water to at least one pass comprising at least one reverse osmosis membrane to produce the permeate water and brine.

[0094] Preferably, the process further comprises the step of regenerating at least some of the calcium carbonate precipitant to a calcium- based chemical and carbon dioxide.

[0095] Preferably, the calcium-based chemical is selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.

[0096] The process as defined above may further comprise regenerating the calcium carbonate to the calcium-based chemical, the regeneration method being selected from at least one of calcinating the precipitated calcium carbonate, hydrolysing the precipitated calcium carbonate and any combination thereof.

[0097] In embodiments, regenerating the calcium carbonate comprises calcination comprising heating the calcium carbonate to a temperature of at least 500°C. In embodiments, regenerating the calcium carbonate comprises hydrolysing the calcium carbonate to produce at least one selected from the group consisting of calcium hydroxide, calcium oxide, carbon dioxide and any combination thereof.

[0098] Said step of hydrolysis of the calcium carbonate is preferably performed at a temperature of less than 500°C. In embodiments, the calcium-based chemical is calcium oxide and the process further comprises mixing at least a portion of the calcium oxide with at least a portion of intake sea water and / or at least a portion the brine and / or RO desalinated product water to form calcium hydroxide.

[0099] In embodiments, at least a portion of the calcium hydroxide formed by regeneration of the calcium carbonate is at least one selected from (a) recycled for use in the at least one reactor; (b) used in the post treatment process; (c) any combination thereof.

[0100] According to aspects of the process as defined above, feeding at least a portion of brine through the at least one reactor containing calcium hydroxide (Ca(OH)2) also precipitates magnesium hydroxide. Alternatively, the at least a portion of brine is fed through at least one second reactor adapted to precipitate magnesium-based chemical selected from a group consisting of magnesium hydroxide, magnesium oxide and any combination thereof.

[0101] In embodiments, the process as defined above, further comprises the step of regenerating at least some of the magnesium hydroxide precipitant to a magnesium- based chemical. Optionally, the process further comprises adding at least a portion of the regenerated magnesium-based chemical to the permeate to produce product water.

[0102] In embodiments of the present invention, the process as defined above comprises feeding at least a portion of brine through the at least one reactor containing calcium hydroxide (Ca(OH)2) also precipitates magnesium hydroxide; and the process further comprises the steps of (i) regenerating at least some of the calcium carbonate and magnesium hydroxide precipitants to produce a calcium- based chemical, a magnesium-based chemical and carbon dioxide; and, (ii) mixing at least some of the regenerated chemicals and carbon dioxide with the permeate product water to produce drinking water. Alternatively, the at least a portion of the brine is fed through at least one second reactor adapted to precipitate magnesium-based chemical selected from a group consisting of magnesium hydroxide, magnesium oxide and any combination thereof.

[0103] In embodiments, only a portion of the brine is fed through the reactorwith the remaining brine bypassing the at least one reactor. In embodiments, the process further comprises a step of mixing said portion of the brine fed through the at least one reactor with the remaining brine bypassing the at least one reactor.

[0104] In embodiments, the process further comprises delivering at least a portion of the sea water to at least one of a filter unit and a clearwell.

[0105] Optionally, the process may further comprise passing at least a portion of the permeate from the reverse osmosis membranes of a first pass to a second pass of brackish water reverse osmosis. The process may further comprise adding at least one of sodium hydroxide or calcium hydroxide to the permeate prior to its introduction to the second pass.

[0106] In embodiments, the process as defined above, further comprises regenerating the calcium hydroxide from the calcium carbonate precipitant and adding at least a portion of the regenerated calcium hydroxide to the permeate prior to its introduction to the second pass.

[0107] Optionally, the process excludes calcium carbonate contactor in the post -treatment of the permeate water.

[0108] It is another aspect of the present invention to provide a desalination system comprising: at least one reverse osmosis pass comprising at least one reverse osmosis membrane to produce permeate product water and brine; at least one conduit for delivering at least a portion of the brine to the at least one reactor for the removal of carbonates-based chemical.

[0109] According to this aspect of the present invention to provide the desalination system as defined above, said at least one reactor has a calcium hydroxide (Ca(OH)2) source to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3). The reactor preferably contains or has introduced thereto at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3), according to the following formula: Ca(OH)2 + Ca(HCO3)2 --> 2CaCO3 + 2H2O. In embodiments of the invention, the desalination system is as defined above, wherein the at least one reactor also precipitates magnesium hydroxide from the brine and at least one regeneration module is configured to regenerate at least some of the magnesium hydroxide precipitant to a magnesium-based chemical. Alternatively, the at least a portion of brine is fed through at least one second reactor adapted to precipitate magnesium-based chemical selected from a group consisting of magnesium hydroxide, magnesium oxide and any combination thereof. The system may further comprise at least one pipe to deliver at least a portion of the magnesium- based chemical formed by the regeneration module to the permeate produced by the at least one reverse osmosis membrane to produce drinking water.

[0110] According to yet a further aspect of the present invention there is provided a self- sustainable desalination process for the desalination of sea water, the process comprising: delivering sea water to an intake pipe; delivering under pressure all the intake water to at least one pass comprising at least one reverse osmosis membrane to produce permeate and brine; and, carbonates-based chemical removing from at least a portion of said brine.

[0111] Preferably, said carbonates-based chemical removing is performed by introducing calcium hydroxide (Ca(OH)2) into at least one reactor; and passing at least a portion of the brine through the reactor to precipitate at least calcium carbonate (CaCO3) from the at least a portion of the brine.

[0112] Additionally, said process may comprise a step of regenerating at least one selected from the group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO), carbon dioxide (CO2), magnesium hydroxide (Mg(OH)2) and any combination thereof. Said step of regenerating may be at least one selected from the group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO), carbon dioxide (CO2), magnesium hydroxide (Mg(OH)2) and any combination thereof from said carbonates-based chemical.

[0113] A further aspect of the present invention provides a self-sustainable desalination system for the desalination of sea water, the system comprising: a sea water intake; at least one reactor having a calcium hydroxide (Ca(OH)2) source; at least one reverse osmosis pass comprising at least one reverse osmosis membrane, wherein all the intake sea water is delivered through the pass to produce permeate and brine; at least one conduit for delivering at least a portion of the brine from to the at least one reactor to precipitate calcium carbonate (CaCO3); at least one regeneration module to convert at least some of the calcium carbonate (CaCO3) precipitant to at least one selected from a group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO), carbon dioxide (CO2) and any combination thereof; and a recycling system to deliver at least a portion of at least one of the calcium hydroxide (Ca(OH)2), calcium oxide (CaO) and carbon dioxide (CO2) and any combination thereof regenerated from the calcium carbonate (CaCO3) precipitant to at least one of (i) the permeate to produce product water and (ii) the at least one reactor and any combination thereof.

[0114] Preferably, the present invention provides a calcium carbonate reactor-free posttreatment desalination method for the treatment of water comprising step of desalinating intake sea water to produce permeate product water and brine; adding at least one of calcium hydroxide (Ca(OH)2), magnesium hydroxide (Mg(OH)2) to at least one a portion of the brine after said step of desalinating intake sea water, wherein said post-treatment desalination method is free of calcium carbonate reactor.

[0115] Preferably, the post-treatment method as defined above, includes at least one of the calcium hydroxide (Ca(OH)2), magnesium hydroxide (Mg(OH)2) is regenerated calcium carbonate precipitated during said step of adding at least one of calcium hydroxide (Ca(OH)2), magnesium hydroxide (Mg(OH)2) to intake sea water.

[0116] Preferably, the present invention includes the post-treatment method as defined above, further comprising feeding at least a portion of the brine through at least one reactor, the reactor containing or having introduced therein at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate calcium carbonate (CaCO3) and regenerating calcium hydroxide (Ca(OH)2) and carbon dioxide (CO2), wherein the regenerated calcium hydroxide is added to the reactor and for post-treatment of the permeate water and the carbon dioxide is used for post-treatment of the permeate water. Optionally, in the post-treatment method as defined above, feeding at least a portion of the brine through the at least one reactor also precipitates magnesium hydroxide (Mg(OH)2) for post-treatment of the permeate water.

[0117] Alternatively, the feeding of at least a portion of the brine is fed through at least one second reactor adapted to precipitate magnesium-based chemical selected from a group consisting of magnesium hydroxide, magnesium oxide and any combination thereof.

[0118] Alternatively, at least a portion of the magnesium-based chemical (MgOH or MgO) is at least one selected from (a) recycled for use in the at least one reactor; (b) used in the post treatment process; (c) any combination thereof.

[0119] Brief Description of the Drawings

[0120] For a better understanding of the present invention and to show more clearly how it may be carried into effect, reference will now be made by way of example only to the accompanying drawings in which:

[0121] Figure 1 is a schematic diagram illustrating a single pass SWRO system according to the prior art; and

[0122] Figure 2 is a schematic diagram illustrating a double pass SWRO and BWRO system according to the prior art;

[0123] Figure 3 is a schematic diagram of a more sustainable single pass SWRO system according to one embodiment of the present invention;

[0124] Figure 3a is a schematic diagram of a more sustainable SWRO system according to one embodiment of the present invention utilizing the brine flow from a desalination plant.

[0125] Figure 4 is a schematic diagram of a more sustainable double pass SWRO and BWRO system according to another embodiment of the present invention;

[0126] Figure 5 illustrates the hydrolysis of calcium carbonate; Figure 6 is a schematic diagram of a more sustainable single pass SWRO system according to another embodiment of the present invention;

[0127] Figure 7 is a schematic diagram of a more sustainable double pass SWRO and BWRO system according to another embodiment of the present invention; and.

[0128] Figure 8 is a schematic diagram of a more sustainable single pass SWRO system according to another embodiment of the present invention, in which the carbonate removal is performed post the desalination step.

[0129] Figure 9 is a schematic diagram of a more sustainable single pass SWRO system according to another embodiment of the present invention, in which the carbonate removal is performed both post the desalination step and prior to the desalination step.

[0130] Detailed Description of the invention.

[0131] The present invention is concerned with improving a sea water desalination process and plant by increasing their sustainability. This is achieved by the self-generation of most of the chemicals used in the desalination process / plant, thus reducing the need to deliver chemicals to the plant. In addition, the process also improves the boron rejection by the SWRO and reduces the overall footprint of the desalination plant. This provides an overall cost reduction in the production of desalinated water as well as providing a more sustainable process.

[0132] It is one object of the present invention to provide a process for the desalination of sea water, the process comprising: feeding at least a portion of intake sea water through at least one reactor for the removal of carbonates-based chemical; and desalinating said intake sea water to produce permeate product water and brine.

[0133] It is another object of the present invention to provide the process as defined above, wherein the reactor containing or is introduced with at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3).

[0134] It is another object of the present invention to provide the process as defined above, wherein the reactor containing or is introduced with at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3), according to the following formula: Ca(OH)2 + Ca(HCO3)2 --> 2CaCO3 + 2H2O.

[0135] It is another object of the present invention to provide the process as defined above, further comprising introducing calcium hydroxide (Ca(OH)2) into the at least one reactor.

[0136] It is another object of the present invention to provide the process as defined above, wherein feeding at least a portion of intake sea water through at least one reactor containing calcium hydroxide (Ca(OH)2) increases the pH of the intake water to at least pH 8.3.

[0137] It is another object of the present invention to provide the process as defined above, wherein desalinating said intake sea water comprises delivering the intake water to at least one pass comprising at least one reverse osmosis membrane to produce the permeate water and brine.

[0138] It is another object of the present invention to provide the process as defined above, further comprising the step of regenerating at least some of the calcium carbonate precipitant to a calcium- based chemical and carbon dioxide.

[0139] It is another object of the present invention to provide the process as defined above, wherein the calcium-based chemical is selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.

[0140] It is another object of the present invention to provide the process as defined above, wherein regenerating the calcium carbonate to the calcium-based chemical comprises a method selected from at least one of calcinating the precipitated calcium carbonate, hydrolysing the precipitated calcium carbonate and any combination thereof.

[0141] It is another object of the present invention to provide the process as defined above, wherein regenerating the calcium carbonate comprises calcination comprising heating the calcium carbonate to a temperature of at least 500°C. It is another object of the present invention to provide the process as defined above, wherein regenerating the calcium carbonate comprises hydrolysing the calcium carbonate to produce at least one selected from the group consisting of calcium hydroxide, calcium oxide, carbon dioxide and any combination thereof.

[0142] It is another object of the present invention to provide the process as defined above, wherein said step of hydrolysis of the calcium carbonate is performed at a temperature of less than 500°C.

[0143] It is another object of the present invention to provide the process as defined above, wherein the calcium-based chemical is calcium oxide and the process further comprises mixing at least a portion of the calcium oxide with at least a portion of intake sea water to form calcium hydroxide.

[0144] It is another object of the present invention to provide the process as defined above, wherein at least a portion of the calcium hydroxide formed by regeneration of the calcium carbonate is at least one selected from (a) recycled for use in the at least one reactor; (b) used in the post treatment process; (c) any combination thereof.

[0145] It is another object of the present invention to provide the process as defined above, wherein feeding at least a portion of intake sea water through the at least one reactor containing calcium hydroxide (Ca(0H)2) also precipitates magnesium hydroxide. Alternatively, the at least a portion of intake water is fed through at least one second reactor adapted to precipitate magnesium-based chemical selected from a group consisting of magnesium hydroxide, magnesium oxide and any combination thereof.

[0146] It is another object of the present invention to provide the process as defined above, further comprising the step of regenerating at least some of the magnesium hydroxide precipitant to a magnesium-based chemical.

[0147] It is another object of the present invention to provide the process as defined above, further comprising adding at least a portion of the regenerated magnesium-based chemical to the permeate to produce product water.

[0148] It is another object of the present invention to provide the process as defined above, wherein feeding at least a portion of intake sea water through the at least one reactor containing calcium hydroxide (Ca(0H)2) also precipitates magnesium hydroxide; and the process further comprises the steps of (i) regenerating at least some of the calcium carbonate and magnesium hydroxide precipitants to produce a calcium- based chemical, a magnesium-based chemical and carbon dioxide; and, (ii) mixing at least some of the regenerated chemicals and carbon dioxide with the permeate product water to produce drinking water. Alternatively, the at least a portion of intake water is fed through at least one second reactor adapted to precipitate magnesium-based chemical selected from a group consisting of magnesium hydroxide, magnesium oxide and any combination thereof.

[0149] It is another object of the present invention to provide the process as defined above, wherein only a portion of the sea water is fed through the reactor with the remaining intake sea water bypassing the at least one reactor.

[0150] It is another object of the present invention to provide the process as defined above, further comprising step of mixing said portion of the sea water fed through the at least one reactor with the remaining intake sea water bypassing the at least one reactor.

[0151] It is another object of the present invention to provide the process as defined above, further comprising delivering at least a portion of the sea water to at least one of a filter unit and a clearwell.

[0152] It is another object of the present invention to provide the process as defined above, further comprising passing at least a portion of the permeate from the reverse osmosis membranes of a first pass to a second pass of brackish water reverse osmosis.

[0153] It is another object of the present invention to provide the process as defined above, further comprising adding at least one of sodium hydroxide or calcium hydroxide to the permeate prior to its introduction to the second pass.

[0154] It is another object of the present invention to provide the process as defined above, further comprising regenerating the calcium hydroxide from the calcium carbonate precipitant and adding at least a portion of the regenerated calcium hydroxide to the permeate prior to its introduction to the second pass.

[0155] It is another object of the present invention to provide the process as defined above, wherein the process excludes calcium carbonate contactor in the post -treatment of the permeate water.

[0156] It is another object of the present invention to provide a desalination system comprising: at least one conduit for delivering at least a portion of an intake sea water to the at least one reactor for the removal of carbonates-based chemical; and at least one reverse osmosis pass comprising at least one reverse osmosis membrane, wherein at least a portion of the intake sea water is delivered through the at least one reactor prior to being delivered through the pass to produce permeate product water and brine.

[0157] It is another object of the present invention to provide the desalination system as defined above, wherein said at least one reactor having a calcium hydroxide (Ca(OH)2) source to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCCh).

[0158] It is another object of the present invention to provide the desalination system as defined above, wherein the reactor containing or is introduced with at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3), according to the following formula: Ca(OH)2 + Ca(HCO3)2 --> 2CaCO3 + 2H2O.

[0159] It is another object of the present invention to provide the desalination system as defined above, wherein at least one regeneration module is provided to convert at least some of the calcium carbonate precipitant to a calcium-based chemical and carbon dioxide.

[0160] It is another object of the present invention to provide the desalination system as defined above, wherein said at least one regeneration module is selected from at least one of a calcinatory, a hydrolysis reactor and any combination thereof.

[0161] It is another object of the present invention to provide the desalination system as defined above, wherein said at least one regeneration module is a calcinatory provided for calcinating the precipitated calcium carbonate to produce at least one of calcium hydroxide, calcium oxide, carbon dioxide and any combination thereof.

[0162] It is another object of the present invention to provide the desalination system as defined above, wherein the calcinatory comprises a rotary kiln for calcination of the calcium carbonate.

[0163] It is another object of the present invention to provide the desalination system as defined above, wherein the at least one regeneration module comprises at least one hydrolysis reactor for hydrolysing the calcium carbonate to produce at least one selected from a group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO), carbon dioxide (CO2) and any combination thereof.

[0164] It is another object of the present invention to provide the desalination system as defined above, wherein said hydrolysis reactor operates at a temperature of less 500°C.

[0165] It is another object of the present invention to provide the desalination system as defined above, wherein the calcinatory provided for calcinating the precipitated calcium carbonate produces calcium oxide and the system further comprises at least one mixing reactor adapted to mix at least a portion of the calcium oxide with at least a portion of the intake sea water to produce calcium hydroxide (Ca(OH)2).

[0166] It is another object of the present invention to provide the desalination system as defined above, wherein at least one pipe is provided to deliver at least one, preferably both, of a portion of the calcium -based chemical and carbon dioxide formed by the regeneration module to the permeate produced by the at least one reverse osmosis membrane to produce the product water.

[0167] It is another object of the present invention to provide the desalination system as defined above, wherein at least one pipe is provided to recycle at least a portion of the calcium-based chemical formed by the regeneration module to the at least one reactor.

[0168] It is another object of the present invention to provide the desalination system as defined above, wherein the at least one reactor also precipitates magnesium hydroxide from the intake sea water and at least one regeneration module is configured to regenerate at least some of the magnesium hydroxide precipitant to a magnesium- based chemical. Alternatively, the at least a portion of intake water is fed through at least one second reactor adapted to precipitate magnesium-based chemical selected from a group consisting of magnesium hydroxide, magnesium oxide and any combination thereof.

[0169] It is another object of the present invention to provide the desalination system as defined above, further comprising at least one pipe to deliver at least a portion of the magnesium-based chemical formed by the regeneration module to the permeate produced by the at least one reverse osmosis membrane to produce drinking water. It is another object of the present invention to provide the desalination system as defined above, wherein the at least one reactor having a calcium hydroxide (Ca(OH)2) source also precipitates magnesium hydroxide; and, the system includes at least one regeneration module regenerating at least some of the calcium carbonate and magnesium hydroxide precipitants to produce a calcium- based chemical, a magnesium-based chemical and carbon dioxide and piping to deliver at least some of the regenerated chemicals and carbon dioxide to the permeate product water to produce drinking water.

[0170] It is another object of the present invention to provide the desalination system as defined above, wherein a bypass is provided between the intake sea water and the reverse osmosis pass to enable the delivery of a portion of the sea water through the at least one reactor with the remaining intake sea water bypassing the at least one reactor.

[0171] It is another object of the present invention to provide the desalination system as defined above, wherein at least one of a filter unit and a clearwell is provided between the at least one reactor and the pass.

[0172] It is another object of the present invention to provide the desalination system as defined above, wherein the at least one reactor is a fluidized bed reactor.

[0173] It is another object of the present invention to provide the desalination system as defined above, wherein a second brackish water reverse osmosis pass is in fluid communication with the first pass, wherein at least a portion of the permeate from the first pass is delivered to the second pass.

[0174] It is another object of the present invention to provide the desalination system as defined above, wherein at least one of a sodium hydroxide and calcium hydroxide source and any combination is provided between the first and second pass to introduce sodium hydroxide or calcium hydroxide to the permeate prior to its introduction to the second pass.

[0175] It is another object of the present invention to provide the desalination system as defined above, wherein at least a portion of the intake sea water delivered through the at least one reactor results in an increase in pH of the at least a portion of the intake water to a pH of at least 8.3.

[0176] It is another object of the present invention to provide the desalination system as defined above, wherein said increase in pH to at least 8.3 of at least a portion of the intake sea water enhances boron rejection by said at least one reverse osmosis membrane to thereby increase the overall efficiency of the desalination system.

[0177] It is another object of the present invention to provide a self-sustainable desalination process for the desalination of sea water, the process comprising: delivering sea water to an intake pipe; carbonates-based chemical removing from said sea water; delivering under pressure all the intake water to at least one pass comprising at least one reverse osmosis membrane to produce permeate and brine.

[0178] It is another object of the present invention to provide the self-sustainable desalination process as defined above, wherein said carbonates-based chemical removing is performed by introducing calcium hydroxide (Ca(OH)2) into at least one reactor; and passing at least a portion of the intake sea water through the reactor to precipitate at least calcium carbonate (CaCO3) from the sea water.

[0179] It is another object of the present invention to provide the self-sustainable desalination process as defined above, additionally comprising step of regenerating at least one selected from the group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO), carbon dioxide (CO2), magnesium hydroxide (Mg(OH)2) and any combination thereof.

[0180] It is another object of the present invention to provide the self-sustainable desalination process as defined above, wherein said step of regenerating at least one selected from the group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO), carbon dioxide (CO2), magnesium hydroxide (Mg(OH)2) and any combination thereof from said carbonates-based chemical.

[0181] It is another object of the present invention to provide the self-sustainable desalination process as defined above, additionally comprising step of adding at least a portion of at least one of the calcium hydroxide (Ca(OH)2), calcium oxide (CaO) and carbon dioxide (CO2) and any combination thereof regenerated from the calcium carbonate (CaCO3) precipitant to at least one of (i) the permeate to produce product water and (ii) the at least one reactor, and any combination thereof.

[0182] It is another object of the present invention to provide a self-sustainable desalination system for the desalination of sea water, the system comprising: a sea water intake; at least one reactor having a calcium hydroxide (Ca(OH)2) source; at least one conduit for delivering at least a portion of the sea water from the intake to the at least one reactor to precipitate calcium carbonate (CaCO3); at least one reverse osmosis pass comprising at least one reverse osmosis membrane, wherein all the intake sea water is delivered through the pass to produce permeate and brine; at least one regeneration module to convert at least some of the calcium carbonate (CaCO3) precipitant to at least one selected from a group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO), carbon dioxide (CO2) and any combination thereof; and a recycling system to deliver at least a portion of at least one of the calcium hydroxide (Ca(OH)2), calcium oxide (CaO) and carbon dioxide (CO2) and any combination thereof regenerated from the calcium carbonate (CaCO3) precipitant to at least one of (i) the permeate to produce product water and (ii) the at least one reactor and any combination thereof.

[0183] It is another object of the present invention to provide a calcium carbonate reactor-free post-treatment desalination method for the treatment of permeate water comprising step of adding at least one of calcium hydroxide (Ca(OH)2), magnesium hydroxide (Mg(OH)2) to intake sea water prior to desalinating the same, wherein said posttreatment desalination method is free of calcium carbonate reactor.

[0184] It is another object of the present invention to provide the post-treatment method as defined above, wherein at least one of the calcium hydroxide (Ca(OH)2), magnesium hydroxide (Mg(OH)2) is regenerated calcium carbonate precipitated during said step of adding at least one of calcium hydroxide (Ca(OH)2), magnesium hydroxide (Mg(OH)2) to intake sea water.

[0185] It is another object of the present invention to provide the post-treatment method as defined above, further comprising feeding at least a portion of intake sea water through at least one reactor, the reactor containing or is introduced therein with at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate calcium carbonate (CaCO3) and regenerating calcium hydroxide (Ca(OH)2) and carbon dioxide (CO2), wherein the regenerated calcium hydroxide is added to the reactor and for post-treatment of the permeate water and the carbon dioxide is used for post -treatment of the permeate water. It is another object of the present invention to provide the post-treatment method as defined above, wherein feeding at least a portion of intake sea water through the at least one reactor also precipitates magnesium hydroxide (Mg(OH)2) for post-treatment of the permeate water.

[0186] Alternatively, the feeding of at least a portion of the intake water is fed through at least one second reactor adapted to precipitate magnesium-based chemical selected from a group consisting of magnesium hydroxide, magnesium oxide and any combination thereof.

[0187] Alternatively, at least a portion of the magnesium-based chemical (MgOH or MgO) is at least one selected from (a) recycled for use in the at least one reactor; (b) used in the post treatment process; (c) any combination thereof.

[0188] It is another object of the present invention to provide the post-treatment method as defined above, wherein desalinating said intake sea water comprises delivering the intake water to at least one pass comprising at least one reverse osmosis membrane to produce the permeate water and brine.

[0189] It is another object of the present invention to provide the post-treatment method as defined above, further comprising the step of regenerating at least some of the calcium carbonate precipitant to a calcium- based chemical and carbon dioxide.

[0190] It is another object of the present invention to provide the post-treatment method as defined above, wherein the calcium-based chemical is selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.

[0191] It is another object of the present invention to provide the post-treatment method as defined above, wherein regenerating the calcium carbonate to the calcium-based chemical comprises a method selected from at least one of calcinating the precipitated calcium carbonate, hydrolysing the precipitated calcium carbonate and any combination thereof.

[0192] It is another object of the present invention to provide the post-treatment method as defined above, wherein the calcium-based chemical is calcium oxide and the process further comprises mixing at least a portion of the calcium oxide with at least a portion of intake sea water to form calcium hydroxide.

[0193] It is another object of the present invention to provide the self-sustainable desalination process as defined above, wherein said step of regenerating at least some of the calcium carbonate precipitant comprises a method selected from at least one of calcinating the precipitated calcium carbonate, hydrolysing the precipitated calcium carbonate and any combination thereof.

[0194] It is another object of the present invention to provide the self-sustainable desalination process as defined above, wherein said step of regenerating at least some of the calcium carbonate precipitant results in calcium-based chemical selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.

[0195] It is another object of the present invention to provide the self-sustainable desalination process as defined above, wherein said at least one regeneration module is selected from at least one of calcinator, hydrolysing module and any combination thereof.

[0196] It is another object of the present invention to provide the self-sustainable desalination process as defined above, wherein said at least one regeneration module results in calcium-based chemical selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.

[0197] According to one embodiment of the present invention input sea water are reacted with lime (calcium hydroxide, Ca(OH)2) prior to its passage through the reverse osmosis passes to precipitate calcium carbonate. The calcium carbonate is then subsequently regenerated (by e.g., calcination / hydrolysis, as will be detailed hereinbelow, of the calcium carbonate) for reuse in the process / plant. This provides for a series of benefits in the overall cost efficiency and sustainability of the process / plant as detailed below.

[0198] Figure 3 of the accompanying drawings is a schematic diagram of a modified single pass SWRO system according to one embodiment of the present invention. The most significant change is the addition of a precipitation reactor 2 (such as a fluidized bed reactor) through which at least a portion of the initial sea water is passed prior to filtration 4 for carbonate removal. In the illustrated embodiment, the filtered water is then delivered to a clearwell 6 although it is to be appreciated that the use of a clearwell is optional. Calcium hydroxide is introduced into at least one pellet reactor 2 raising the pH of the water to at least 8.3 or higher for carbon removal by precipitating out calcium carbonate (and, optionally, magnesium hydroxide), according to the following equation:

[0199] Ca(OH)2+ Ca(HCO3)2— > 2CaCO3+ 2H2O This leads to the SWRO 8 operating at a higher pH which provides better biofouling resistance, better boron rejection and enables post treatment reactors to be free from calcium carbonate reactors. Instead, the post treatment reactors are replaced with the simple addition of lime (calcium hydroxide) and carbon dioxide to form the final product.

[0200] Thus, it is within the scope of the present invention to provide a desalination process and plant where calcium carbonate contactors are not required. Additionally, the calcium carbonate pellets produced as a by-product from the at least one precipitation reactor 2 are delivered to a regenerator 10 for the production of calcium-based chemicals, such as calcium hydroxide, calcium oxide, and carbon dioxide. The calcium-based chemicals will be reused in at least one pellet reactor 2 (or in the post treatment process) and the carbon dioxide would be used in the post treatment process (to produce drinking water). It should be noted that it could be a pellet reactor or a series of pellet reactors. Each of the pellet reactor could produce one or a combination of calcium-based chemicals, such as calcium hydroxide, calcium oxide, and carbon dioxide; and / or magnesium based chemicals selected from a group consisting of magnesium hydroxide, magnesium oxide and any combination thereof.

[0201] According to one embodiment the regeneration of calcium carbonate back to calcium hydroxide is provided by means of a calcinatory (kiln, burner), hydrolysis or any other methods known in the art.

[0202] In case the regenerator 10 is a calcinator, the calcium carbonate is calcinated to result in the production of quicklime (calcium oxide) and carbon dioxide. The exothermic mixing reaction of quicklime (calcium oxide) with water will result in lime (calcium hydroxide) - which could be, as detailed above, reused and introduced back to the pellet reactor 2. The energy released by this exothermic reaction can be used to compensate some of the thermal energy used for the calcination process. Alternatively, the calcium hydroxide may be used in the post treatment process. Additionally or alternatively, some of the calcium carbonate may be used in the post treatment process (as an alternative to regenerating the same in the reactor).

[0203] Additionally or alternatively, some of the magnesium-based is used in the post treatments of the permeate water post the desalination step. It should be noted that it is within the scope of the present invention to provide a calcination process in which the calcium carbonate is calcinated to form lime (calcium hydroxide) and carbon dioxide. Alternatively, at least a portion ofthe calcium carbonate can be used for post treatment of the permeate.

[0204] As noted above, at least a portion of the lime and carbon dioxide is recycled within the system for use within the pellet reactor (re-use of lime) or for post treatment of the permeate. Additionally, excess lime and carbon dioxide can be sold as an additional income.

[0205] It is to be appreciated that some or all of the intake water may pass through the precipitation reactor 2 to increase the pH of the water and form calcium carbonate. According to one embodiment, only a portion is passed through the reactor. According to that embodiment, a bypass channel should be provided, as indicated by the dashed lines in Figure 3. Furthermore, according to that embodiment, both portions of the intake water join together before the filtration unit 4.

[0206] As mentioned above, one ofthe advantages of the present invention is its operation at a higher pH that improves the boron rejection. In this respect, boron is naturally found in seawater and can adversely affect both humans and agriculture. Poor rejection of boron by RO membranes due to its small size and the boric molecule’s lack of charge at neutral and low pH represents a significant challenge. Elevating the pH of the feed water increases the rejection of boron by the RO membranes; and, increases the overall efficiency of the process.

[0207] Another significant advantage provided by the modified process of the invention is the self-sustainability provided by the on-situ production of calcium-based chemicals and carbon dioxide from the calcium carbonate precipitated which can be used for the posttreatment of the permeate to form product water, as well as being fed back to the pellet reactor. The process enables a much lower chemical consumption overall and allows for the use of smaller reactors.

[0208] Furthermore, the process is also environmentally friendly because it reduces the amount of carbonates in the seawater as compared with standard desalination processes. This enables an increase in carbon capture by the sea, reducing the carbon footprint of the plant. More specifically, the desalination process of the present invention, by enabling the precipitation as disclosed above, removes carbon dioxide from seawater (and hence reduces the amount thereof) thereby facilitating carbon dioxide capture from the atmosphere.

[0209] Thus, the present invention provides a number of overall benefits, including energy saving (especially in 2 pass desalination plants), cost savings, self-manufacture of the required chemicals resulting in a chemical cost saving, additional profit from selling excess chemicals and carbon capture credits with a significant reduction in total operating costs.

[0210] As illustrated in Figure 3, the precipitation reactor 10 may also precipitate magnesium hydroxide (Mg(OH)2) from the sea water intake. This also enhances the sustainability of the process / plant because this chemical may also be required to provide satisfactory drinking water from permeate water, in addition to calcium hydroxide. Thus, the magnesium hydroxide may be delivered to the permeate water to provide drinking water. Again, the magnesium hydroxide may be regenerated to form a magnesium- based chemical, such as magnesium oxide or magnesium hydroxide, which may be added to the permeate water, with any excess being sold for additional income.

[0211] Figure 4 of the accompanying drawings is a schematic diagram of a modified double pass SWRO system according to another embodiment of the present invention. The system incorporates the same significant modification as the single pass system shown in Figure 3, being a precipitation reactor 2 for the introduction of calcium hydroxide through which at least a proportion of the intake sea water is passed prior to delivery to a filtration unit 4 and, optionally, clearwell 6.

[0212] It is known that the front (upstream) membranes of the SWRO produce higher quality permeate (having lower salinity) than the permeate produced by the rear (downstream) membranes (having higher salinity). Several known desalination processes take advantage of the lower salinity front permeate by directing it straight to the product stream, while the higher salinity rear permeate is treated further, for example by diluting with seawater feed and recycling back through the membranes. In the present invention, the introduction of calcium hydroxide raises the pH of the water to at least 8.3 or higher and precipitates out calcium carbonate (and optionally, magnesium hydroxide). This leads to the SWRO 8 operating at a higher pH providing the ability to extract more permeate flow from the front of the SWRO pressure vessels, which do not then need to pass through a BWRO stage and provides elevated pH, better biofouling resistance (namely, higher amounts of high quality permeate having lower salinity) and improved boron rejection.

[0213] This is illustrated in Figure 4, with a portion bypassing the BWRO pass 18 while another portion of the permeate from the SWRO 8 is passed to the second pass BWRO 18 and sodium hydroxide and / or calcium hydroxide are introduced in order to elevate the pH level. The operating parameters of the first pass due to the introduction of calcium hydroxide enables the BWRO pass to be reduced in size and less chemicals have to be added to the water as the rejection of boron in the first pass is improved, as explained above. Thus, again overall operating costs are reduced.

[0214] The post treatment reactors can again be replaced with the simple addition of lime (calcium hydroxide) and carbon dioxide to form the final product without the need for calcium carbonate contactors. As with the system shown in Figure 3, the reactor 2 may also optionally precipitate magnesium hydroxide (Mg(OH)2) from the sea water intake which may also be delivered to the permeate water to provide drinking water. Again, the magnesium hydroxide may be regenerated to form a magnesium-based chemical, such as magnesium oxide or magnesium hydroxide, which may be added to the permeate water, thereby enhancing the sustainability of the plant.

[0215] Additionally, the calcium carbonate pellets produced as a by-product from the precipitation reactor 2 are again delivered to a regenerator 10 to produce calcium- based chemicals (such as lime and quick lime) and carbon dioxide for recycling and additional revenue streams. Thus, the incorporation of a precipitation reactor fed with calcium hydroxide also provides major advantages in a double pass system, significantly reducing the amount of chemicals used in the process and enabling a reduction in the BWRO stage size.

[0216] As mentioned above in relation to Figure 3, the regeneration of calcium carbonate back to calcium hydroxide is provided by means of a calcinatory (kiln, burner), hydrolysis or any other methods known in the art. In the embodiment illustrated in Figure 4, a calcinatory 10 is again used, with the calcium carbonate being delivered to a calcinatory 10 to produce quicklime (calcium oxide) and carbon dioxide. The calcination process takes place at temperatures below the melting point of calcium carbonate (limestone), being calcined at above 400°C; in some cases around 850°C, more preferably 1100°C to produce calcium oxide (quicklime) and carbon dioxide. The exothermic mixing reaction of quicklime (calcium oxide) with water will result in lime (calcium hydroxide) which can be re-used and the energy released by the exothermic mixing reaction can be used to compensate some of the thermal energy used for the calcination.

[0217] Alternatively, regeneration of calcium carbonate back to calcium hydroxide may be provided by hydrolysis. According to this embodiment, a calcium carbonate hydrolysis process may be incorporated into the process / system of the invention. This enables a lower calcination temperature of below 600°C to be used, as illustrated in Figure 5 of the accompanying drawings.

[0218] According to this embodiment, the hydrolysis products of calcium carbonate results in lime and carbon dioxide, according to the following equation:

[0219] CaCO3+H2O -> Ca(OH)2+ CO2

[0220] The process and system parameters of the present invention can be further optimized to enhance cost and chemical savings.

[0221] The modified desalination process and plant of the present application reduces the chemical cost of the plant, increases the plant sustainability due to self-production of chemicals, reducing the carbon footprint of the plant and provides the ability to generate carbon credits as well as providing the ability to generate additional source of income by selling chemicals. In addition, the fact that the chemicals do not need to be delivered to the plant reduces the plant's carbon footprint. Moreover, with two pass systems, there is safer BWRO operation due to it operating at lower supersaturation (lower pH). The positive effect of alkalinity reduction from the brine is greater than the CO2emitted in the lime regeneration process. Reference is now made to Figures 6-7 of the accompanying drawings illustrating another embodiment of the present invention. According to this embodiment, magnesium hydroxide (Mg(OH)2), rather than or in addition to, calcium hydroxide (Ca(OH)2) is added to reactor 2 to precipitate magnesium carbonate (MgCO3). Identical features already discussed in relation to Figures 3 and 4 are provided with the same reference numerals and only the differences will be discussed in detail.

[0222] According to this embodiment of the present invention input sea water is reacted with magnesium hydroxide, Mg(OH)2) in the reactor 2 prior to its passage through the reverse osmosis passes 8 to precipitate magnesium carbonate (MgCO3). Again the intake water may pass through a filter unit 4 and, optionally a clearwell 6, prior to its passage through the reverse osmosis passes 8. The magnesium carbonate is then subsequently regenerated in regenerator 10 (by e.g., calcination / hydrolysis, as described above with regard to the use of calcium hydroxide) for reuse in the process / plant. This provides for a series of benefits, as detailed above, in the overall cost efficiency and sustainability of the process / plant.

[0223] Thus, the reactor 2 mixes intake sea water with magnesium hydroxide to precipitate magnesium carbonate (MgCO3) from the sea water intake which is then regenerated to form a magnesium-based chemical, such as magnesium oxide or magnesium hydroxide and carbon dioxide. Magnesium hydroxide may be added to the permeate water, thereby enhancing the sustainability of the plant; and the CO2is used in the post treatment process.

[0224] As outlined above, magnesium oxide (similarly to calcium oxide) could be reacted with sea water to produce magnesium hydroxide.

[0225] As seen in the figures, it is optional for calcium carbonate to also precipitate in addition to magnesium carbonate (in reactor 2). In such a case, the calcium carbonate, as detailed above, will be regenerated as well for the internal use of the plant and the desalination process (e.g., in the post treatment).

[0226] It is noted that while Figure 6 illustrates a single pass desalination plant using a magnesium hydroxide reactor 2 equivalent to the calcium hydroxide reactor 2 of Figure 3, Figure 7 illustrates a double pass desalination process similar to that of Figure 4. However, the principles of the self-sustainability of the desalination process remains the same.

[0227] Reference is now made to Figure 8 of the accompanying drawings is a schematic diagram of a modified single pass SWRO system according to one embodiment of the present invention. In this embodiment, the carbonate removal (by precipitation of CaCO3) is performed after step of desalination (SWRO). According to this embodiment, the step of desalination (SWRO) produces permeate product water and brine. The carbonate removal (by precipitation of CaCO3) is performed to the resultant brine flow.

[0228] Reference is now made to Fig. 3a illustrating one aspect the present invention which provides a process for treating fluids, the process comprising: feeding at least a portion of the fluids through at least one reactor 2 for the removal of carbonates-based chemical.

[0229] In preferred embodiments of the process according to the first aspect of the invention, the fluids are selected from a group consisting of brine, effluents, waste and any combination thereof.

[0230] Preferably, said fluids are provided from a filtration process; said filtration being selected from a group consisting of desalination of seawater, reverse osmosis, forward osmosis, pressure-retarded osmosis, ultrafiltration, microfiltration and nanofiltration any combination thereof; optionally wherein said reactor is positioned in at least one location selected from a group consisting of prior to said filtration, post said filtration and any combination thereof.

[0231] Thus, the present invention provides a process fortreating fluids (e.g., brine) by feeding at least a portion of the fluids through at least one reactor 2 for the removal of carbonates-based chemical. According to one embodiment, the fluids are selected from a group consisting of brine, effluents, waste and any combination thereof.

[0232] As disclosed above, the most significant change is the addition of a precipitation reactor 2 (such as a fluidized bed reactor) through which at least a portion of the brine (or effluents, waste and any combination thereof) is passed to carbonate removal. Calcium hydroxide is introduced into the pellet reactor 2 raising the pH of the water to at least 8.3 or higher for carbon removal by precipitating out calcium carbonate (and , optionally, magnesium hydroxide), according to the following equation:

[0233] Ca(OH)2+ Ca(HCO3)2—> 2CaCO3+ 2H2O

[0234] As already stated, one of the significant advantages of the present invention is the post treatment reactors which, according to the present invention, are replaced with the simple addition of lime (calcium hydroxide) and carbon dioxide to form the final desalinated product (see Figure 3a).

[0235] Thus, it is within the scope of the present invention to provide a treatment (e.g., desalination process and plant) where calcium carbonate contactors are not required. Additionally, the calcium carbonate pellets produced as a by-product from the precipitation reactor 2 are delivered to a regenerator 10 forthe production of calcium- based chemicals, such as calcium hydroxide, calcium oxide, and carbon dioxide. The calcium-based chemicals will be reused in the pellet reactor 2 (or in the post treatment process) and the carbon dioxide would be used in the post treatment process (to produce drinking water).

[0236] According to one embodiment the regeneration of calcium carbonate back to calcium hydroxide is provided by means of a calcinatory (kiln, burner), hydrolysis or any other methods known in the art.

[0237] In case the regenerator 10 is a calcinator, the calcium carbonate is calcinated to result in the production of quicklime (calcium oxide) and carbon dioxide. The exothermic mixing reaction of quicklime (calcium oxide) with water will result in lime (calcium hydroxide) - which could be, as detailed above, reused and introduced back to the pellet reactor 2. The energy released by this exothermic reaction can be used to compensate some of the thermal energy used for the calcination process. Alternatively, the calcium hydroxide may be used in the post treatment process.

[0238] It should be noted that it is within the scope of the present invention to provide a calcination process in which the calcium carbonate is calcinated to form lime (calcium hydroxide) and carbon dioxide. As noted above, at least a portion of the lime and carbon dioxide is recycled within the system for use within the pellet reactor (re-use of lime) or for post treatment of the permeate. Additionally, excess lime and carbon dioxide can be sold as an additional income.

[0239] A significant advantage provided by the modified process of the invention is the selfsustainability provided by the on-situ production of calcium-based chemicals and carbon dioxide from the calcium carbonate precipitated which can be used for the posttreatment of the permeate to form product water, as well as being fed back to the pellet reactor. The process enables a much lower chemical consumption overall and allows for the use of smaller reactors.

[0240] Furthermore, the process is also environmentally friendly because it reduces the amount of carbonates in the seawater as compared with standard desalination processes. This enables an increase in carbon capture by the sea, reducing the carbon footprint of the plant. More specifically, the desalination process of the present invention, by enabling the precipitation as disclosed above, removes carbon dioxide from seawater (and hence reduces the amount thereof) thereby facilitating carbon dioxide capture from the atmosphere.

[0241] Thus, the present invention provides a number of overall benefits, including energy saving (especially in 2 pass desalination plants), cost savings, self-manufacture of the required chemicals resulting in a chemical cost saving, additional profit from selling excess chemicals and carbon capture credits with a significant reduction in total operating costs.

[0242] As illustrated in Figure 8, the precipitation reactor 2 may also precipitate magnesium hydroxide (Mg(OH)2) from the brine resultant from the desalination step. This also enhances the sustainability of the process / plant because this chemical may also be required to provide satisfactory drinking water from permeate water, in addition to calcium hydroxide. Thus, the magnesium hydroxide may be delivered to the permeate water to provide drinking water. Again, the magnesium hydroxide may be regenerated to form a magnesium-based chemical, such as magnesium oxide or magnesium hydroxide, which may be added to the permeate water, with any excess being sold for additional income. According to another embodiment of the present invention, not all calcium carbonate, (CaCO3), is regenerated (either by calcination or by hydrolysis) and at least a part thereof is used in the post treatment of the permeate water to produce the product water.

[0243] As disclosed in figure 4, the SWRO could have a double pass SWRO system. The system incorporates the same significant modification as the single pass system shown in Figure 8.

[0244] As above, also in a double pass SWRO system, the post treatment reactors can again be replaced with the simple addition of lime (calcium hydroxide) and carbon dioxide to form the final product without the need for calcium carbonate contactors. As with the system shown above, the reactor 2 may also optionally precipitate magnesium hydroxide (Mg(OH)2) from the sea water intake which may also be delivered to the permeate water to provide drinking water. Again, the magnesium hydroxide may be regenerated to form a magnesium-based chemical, such as magnesium oxide or magnesium hydroxide, which may be added to the permeate water, thereby enhancing the sustainability of the plant.

[0245] Additionally, the calcium carbonate pellets produced as a by-product from the precipitation reactor 2 are again delivered to a regenerator 10 to produce calcium - based chemicals (such as lime and quick lime) and carbon dioxide for recycling and additional revenue streams. Thus, the incorporation of a precipitation reactor fed with calcium hydroxide also provides major advantages in a double pass system, significantly reducing the amount of chemicals used in the process and enabling a reduction in the BWRO stage size.

[0246] As mentioned above, the regeneration of calcium carbonate back to calcium hydroxide is provided by means of a calcinatory (kiln, burner), hydrolysis or any other methods known in the art.

[0247] In the embodiment illustrated above, a calcinatory 10 is again used, with the calcium carbonate being delivered to a calcinatory 10 to produce quicklime (calcium oxide) and carbon dioxide. The calcination process takes place at temperatures below the melting point of calcium carbonate (limestone), being calcined at above 400°C; in some cases around 850°C, more preferably 1100°C to produce calcium oxide (quicklime) and carbon dioxide. The exothermic mixing reaction of quicklime (calcium oxide) with water will result in lime (calcium hydroxide) which can be re-used and the energy released by the exothermic mixing reaction can be used to compensate some of the thermal energy used for the calcination.

[0248] Alternatively, regeneration of calcium carbonate (according to any of the embodiments disclosed in this application) back to calcium hydroxide may be provided by hydrolysis. According to this embodiment, a calcium carbonate hydrolysis process may be incorporated into the process / system of the invention. This enables a lower calcination temperature of below 600°C to be used, as illustrated in Figure 5 of the accompanying drawings.

[0249] According to this embodiment, the hydrolysis products of calcium carbonate results in lime and carbon dioxide, according to the following equation:

[0250] CaCO3+H2O -> Ca(OH)2+ CO2

[0251] The process and system parameters of the present invention can be further optimized to enhance cost and chemical savings.

[0252] The modified desalination process and plant of the present application reduces the chemical cost of the plant, increases the plant sustainability due to self-production of chemicals, reducing the carbon footprint of the plant and provides the ability to generate carbon credits as well as providing the ability to generate additional source of income by selling chemicals. In addition, the fact that the chemicals do not need to be delivered to the plant reduces the plant's carbon footprint. Moreover, with two pass systems, there is safer BWRO operation due to it operating at lower supersaturation (lower pH). The positive effect of alkalinity reduction from the brine is greater than the CO2emitted in the lime regeneration process.

[0253] According to another embodiment of this invention, magnesium hydroxide (Mg(OH)2), rather than or in addition to, calcium hydroxide (Ca(OH)2) is added to reactor 2 to precipitate magnesium carbonate (MgCO3). Identical features as already discussed above are applicable substantially in the same manner. Reference is now made to figure 9 which illustrates and embodiment in which at least 2 carbonate removal reactors 2 are provided; at least one is as disclosed in figures 3- 4 and 6-7, where the calcium carbonate precipitation is performed to the intake water prior to the desalination step 8; and, at least one second carbonate removal reactor is as disclosed in figure 8, where the calcium carbonate precipitation is performed post the desalination step 8, to the brine.

[0254] All remaining features and / or principles of the self-sustainability of the desalination process remains the same.

[0255] Thus, according to one embodiment of the present invention, the at least one carbonate removal reactor is provided to the intake water prior to the filtration (e.g., desalination) step; and, at least one second carbonate removal reactor is performed post the filtration (e.g., desalination) step. Namely, to the brine.

[0256] It is noted that while Figure 6 illustrates a single pass desalination plant using a magnesium hydroxide reactor 2 equivalent to the calcium hydroxide reactor 2 of Figure 3, Figure 7 illustrates a double pass desalination process similar to that of Figure 4. However, the principles of the self-sustainability of the desalination process remains the same.

[0257] Also, while Figures 3-4 and 6-7 illustrates the carbonate removal by precipitation prior to the step of desalination, Figure 8 illustrates the carbonate removal by precipitation after the step of desalination. However, the principles of the self-sustainability of the desalination process remains the same.

[0258] As noted above, the precipitation reactor 2 can contain or is introduced with NaOH to precipitate Calcium-based chemicals, e.g., CaC03. The precipitation is according to the following:

[0259] NaOH +HCO3- -> H2O + CO32+ Na+

[0260] As the fluid (e.g., seawater brine) contains calcium the CO32will react therewith to precipitate Calcium carbonate according to the following:

[0261] CO32+ Ca+2-> CaCO3 According to one embodiment, the NaOH will be provided by e.g., reaction of NaCI with water according to the following:

[0262] NaCI-> NaOH + HCI.

[0263] (such reaction could be enabled by means of e.g., bipolar membranes).

[0264] While the NaOH could be used as disclosed above (for the precipitation of the CaCO3), the HCI could be sold to any 3rdparty.

[0265] It should be noted that in all the above embodiments, magnesium-based chemicals could be added in the post treatment (e.g., MgOH).

[0266] It is to be appreciated that modifications to the aforementioned process and systems may be made without departing from the principles embodied in the examples described and illustrated herein.

[0267] All references cited throughout this application, for example patent documents including issued or granted patents or equivalents; patent application publications; and non-patent literature documents or other source material; are hereby incorporated by reference herein in their entireties, as though individually incorporated by reference, to the extent each reference is at least partially not inconsistent with the disclosure in this application.

[0268] The terms and expressions which have been employed herein are used as terms of description and not of limitation, and there is no intention in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the invention claimed. Thus, it should be understood that although the present invention has been specifically disclosed by preferred embodiments, exemplary embodiments and optional features, modification and variation of the concepts herein disclosed may be resorted to by those skilled in the art, and that such modifications and variations are considered to be within the scope of this invention as defined by the appended claims. The specific embodiments provided herein are examples of useful embodiments of the present invention and it will be apparent to one skilled in the art that the present invention may be carried out using a large number of variations of the devices, device components, and method steps set forth in the present description. As will be obvious to one of skill in the art, methods and devices useful for the present methods can include a large number of optional composition and processing elements and steps.

[0269] When a group of substituents is disclosed herein, it is understood that all individual members of that group and all subgroups, including any isomers, enantiomers, and diastereomers of the group members, are disclosed separately. When a Markush group or other grouping is used herein, all individual members of the group and all combinations and sub-combinations possible of the group are intended to be individually included in the disclosure. When a compound is described herein such that a particular isomer, enantiomer or diastereomer of the compound is not specified, for example, in a formula or in a chemical name, that description is intended to include each isomer and enantiomer of the compound described individually or in any combination. Additionally, unless otherwise specified, all isotopic variants of compounds disclosed herein are intended to be encompassed by the disclosure. For example, it will be understood that any one or more hydrogens in a molecule disclosed can be replaced with deuterium or tritium. Isotopic variants of a molecule are generally useful as standards in assays for the molecule and in chemical and biological research related to the molecule or its use. Methods for making such isotopic variants are known in the art. Specific names of compounds are intended to be exemplary, as it is known that one of ordinary skill in the art can name the same compounds differently.

[0270] It must be noted that as used herein and in the appended claims, the singular forms “a”, “an”, and “the” include plural reference unless the context clearly dictates otherwise. Thus, for example, reference to “a cell” includes a plurality of such cells and equivalents thereof known to those skilled in the art, and so forth. As well, the terms “a” (or “an”), “one or more” and “at least one” can be used interchangeably herein. It is also to be noted that the terms “comprising”, “including", and “having” can be used interchangeably. The expression “of any of claims XX -YY” (wherein XX and YY refer to claim numbers) is intended to provide a multiple dependent claim in the alternative form, and in some embodiments is interchangeable with the expression “as in any one of claims XX- YY.”

[0271] Unless defined otherwise, all technical and scientific terms used herein have the same meanings as commonly understood by one of ordinary skill in the art to which this invention belongs. Although any methods and materials similar or equivalent to those described herein can be used in the practice or testing of the present invention, the preferred methods and materials are described. Nothing herein is to be construed as an admission that the invention is not entitled to antedate such disclosure by virtue of prior invention.

[0272] Whenever a range is given in the specification, for example, a range of integers, a temperature range, a time range, a composition range, or concentration range, all intermediate ranges and subranges, as well as all individual values included in the ranges given are intended to be included in the disclosure. As used herein, ranges specifically include the values provided as endpoint values of the range. As used herein, ranges specifically include all the integer values of the range. For example, a range of 1 to 100 specifically includes the end point values of 1 and 100. It will be understood that any subranges or individual values in a range or subrange that are included in the description herein can be excluded from the claims herein. The term “about” refers to any value being lower or greater than 20% of the defined measure. As used herein, “comprising” is synonymous and can be used interchangeably with “including,” “containing,” or “characterized by,” and is inclusive or open-ended and does not exclude additional, unrecited elements or method steps. As used herein, “consisting of’ excludes any element, step, or ingredient not specified in the claim element. As used herein, “consisting essentially of’ does not exclude materials or steps that do not materially affect the basic and novel characteristics of the claim. In each instance herein any of the terms “comprising”, “consisting essentially of’ and “consisting of’ can be replaced with either of the other two terms. The invention illustratively described herein suitably can be practiced in the absence of any element or elements, limitation or limitations which is not specifically disclosed herein.

[0273] One of ordinary skill in the art will appreciate that starting materials, biological materials, reagents, synthetic methods, purification methods, analytical methods, assay methods, and biological methods other than those specifically exemplified can be employed in the practice of the invention without resort to undue experimentation. All art-known functional equivalents, of any such materials and methods are intended to be included in this invention. The terms and expressions which have been employed are used as terms of description and not of limitation, and there is no intention in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the invention claimed. Thus, it should be understood that although the invention has been specifically disclosed by preferred embodiments and optional features, modification and variation of the concepts herein disclosed can be resorted to by those skilled in the art, and that such modifications and variations are considered to be within the scope of this invention as defined by the appended claims.

Claims

Claims:1 . A process for treating fluids, the process comprising: feeding at least a portion of the fluids through at least one reactor for the removal of carbonates-based chemical.

2. The process according to claim 1 , wherein at least a portion of the fluids are selected from a group consisting of brine, effluents, waste and any combination thereof.

3. The process according to claim 2, wherein said fluids are provided from filtration process; said filtration are selected from a group consisting of desalination of seawater, reverse osmosis, forward osmosis, pressure-retarded osmosis, ultrafiltration, microfiltration and nanofiltration any combination thereof; further wherein said reactor is positioned in at least one location selected from a group consisting of prior to said filtration, post said filtration and any combination thereof.

4. The process according to claim 1 , wherein the reactor contains or has introduced at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3).

5. The process according to claim 1 , wherein the reactor contains or has introduced at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3), according to the following formula: Ca(OH)2 + Ca(HCO3)2 --> 2CaCO3 + 2H2O.

6. The process according to any one of claims 1-5, further comprising introducing calcium hydroxide (Ca(OH)2) into the at least one reactor.

7. The process according to any one of claims 1 -6, wherein feeding at least a portion of brine through at least one reactor containing or having introduced at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof increases the pH of the brine to at least pH 8.3.

8. The process according to any one of claims 1 -7, further comprising desalinating intake sea water comprising delivering intake water to at least one pass comprising at least one reverse osmosis membrane to produce permeate water and brine, at least a portion of said brine being fed through the at least one reactor for the removal of carbonates-based chemical.

9. The process according to any one of claims 1 -8, further comprising the step of regenerating at least some of the calcium carbonate precipitant to a calcium- based chemical and carbon dioxide.

10. The process according to claim 9, wherein the calcium-based chemical is selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.11 . The process according to any one of claims 9 - 10, wherein regenerating the calcium carbonate to the calcium-based chemical comprises a method selected from at least one of calcinating the precipitated calcium carbonate, hydrolysing the precipitated calcium carbonate and any combination thereof.

12. The process according to claim 11 , wherein regenerating the calcium carbonate comprises calcination comprising heating the calcium carbonate to a temperature of at least 500°C.

13. The process according to claim 11 , wherein regenerating the calcium carbonate comprises hydrolysing the calcium carbonate to produce at least one selected from the group consisting of calcium hydroxide, calcium oxide, carbon dioxide and any combination thereof.

14. The process according to claim 13, wherein said step of hydrolysis of the calcium carbonate is performed at a temperature of less than 500°C.

15. The process according to any one of claims 13 - 14, wherein the calcium-based chemical is calcium oxide and the process further comprises mixing at least a portion of the calcium oxide with at least a portion of intake sea water and / or at least a portion the brine and / or RO desalinated product water to form calcium hydroxide.

16. The process according to any one of claims 11-15, wherein at least a portion of the calcium hydroxide formed by regeneration of the calcium carbonate is at least one selected from (a) recycled for use in the at least one reactor; (b) used in the post treatment process; (c) any combination thereof.

17. The process according to any one of claims 1 -16, wherein feeding at least a portion of the fluid through the at least one reactor containing calcium hydroxide (Ca(OH)2) also precipitates magnesium hydroxide.

18. The process according to claim 17, further comprising the step of regenerating at least some of the magnesium hydroxide precipitant to a magnesium-based chemical.

19. The process according to claim 18, further comprising adding at least a portion of the regenerated magnesium-based chemical to the permeate to produce product water.

20. The process according to any one of claims 2-19, wherein feeding at least a portion of brine through the at least one reactor containing calcium hydroxide (Ca(OH)2) also precipitates magnesium hydroxide; and the process further comprises the steps of (i) regenerating at least some of the calcium carbonate and magnesium hydroxide precipitants to produce a calcium- based chemical, a magnesium-based chemical and carbon dioxide; and, (ii) mixing at least some of the regenerated chemicals and carbon dioxide with the permeate product water to produce drinking water.21 . The process according to any one of claims 2-20, wherein only a portion of the brine is fed through the reactor with the remaining brine bypassing the at least one reactor.

22. The process according to claim 21 , further comprising step of mixing said portion of the brine fed through the at least one reactor with the remaining brine bypassing the at least one reactor.

23. The process according to any one of claims 8-22, further comprising delivering at least a portion of the sea water to at least one of a filter unit and a clearwell.

24. The process according to any one of claims 8-23, further comprising passing at least a portion of the permeate from the reverse osmosis membranes of a first pass to a second pass of brackish water reverse osmosis.

25. The process according to claim 24, further comprising adding at least one of sodium hydroxide or calcium hydroxide to the permeate prior to its introduction to the second pass.

26. The process according to claim 25, further comprising regenerating the calcium hydroxide from the calcium carbonate precipitant and adding at least a portion of the regenerated calcium hydroxide to the permeate prior to its introduction to the second pass.

27. The process according to any one of claims 8-26, wherein at least a portion of the calcium carbonate, (CaCOs), is used in the post treatments of the permeate water post the desalination step.

28. A plant for treating fluid comprising:at least one conduit for delivering at least a portion of the fluid to at least one reactor for the removal of carbonates-based chemical, wherein at least a portion of said fluids are selected from a group consisting of brine, effluents, waste and any combination thereof; further wherein said fluids are provided from a filtration process; said filtration being selected from a group consisting of desalination of seawater, reverse osmosis, forward osmosis, pressure-retarded osmosis, ultrafiltration, microfiltration and nanofiltration any combination thereof; further wherein said reactor is positioned in at least one location selected from a group consisting of prior to said filtration, post said filtration and any combination thereof.

29. The plant as claimed in claim 28, wherein said at least one reactor has a calcium hydroxide (Ca(OH)2) source to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3).

30. The plant according to claim 28 or 29, wherein the reactor contains or has introduced thereto at least one selected from a group consisting calcium hydroxide (Ca(OH)2) , NaOH and any combination thereof to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCO3), according to the following formula: Ca(OH)2 + Ca(HCO3)2 -> 2CaCO3 + 2H2O.31 . The plant as claimed in any one of claims 28 to 30 further comprising at least one conduit for delivering at least a portion of an intake sea water to at least one reverse osmosis pass comprising at least one reverse osmosis membrane, to produce permeate product water and brine; wherein the at least one conduit for delivering at least a portion of fluid to at least one reactor delivers the brine to the at least one reactor for the removal of carbonates-based chemical in the brine.

32. The plant as claimed in any of claims 28-31 , wherein at least one regeneration module is provided to convert at least some of the calcium carbonate precipitant to a calcium-based chemical and carbon dioxide.

33. The plant as claimed in claim 32, wherein said at least one regeneration module is selected from at least one of a calcinatory, a hydrolysis reactor and any combination thereof.

34. The plant according to claim 33, wherein said at least one regeneration module is a calcinatory provided for calcinating the precipitated calcium carbonate to produce at least one of calcium hydroxide, calcium oxide, carbon dioxide and any combination thereof.

35. The plant as claimed in claim 34, wherein the calcinatory comprises a rotary kiln for calcination of the calcium carbonate.

36. The plant as claimed in claim 33, wherein the at least one regeneration module comprises at least one hydrolysis reactor for hydrolysing the calcium carbonate to produce at least one selected from a group consisting of calcium hydroxide (Ca(OH)2), calcium oxide (CaO), carbon dioxide (CO2) and any combination thereof.

37. The plant according to claim 36, wherein said hydrolysis reactor operates at a temperature of less 500°C.

38. The plant as claimed in claim 34 or35 wherein the calcinatory provided for calcinating the precipitated calcium carbonate produces calcium oxide and the system further comprises at least one mixing reactor adapted to mix at least a portion of the calcium oxide with at least a portion of an intake sea water and / or at least a portion of brine to produce calcium hydroxide (Ca(OH)2).

39. The plant as claimed in any one of claims 32-38 wherein at least one pipe is provided to deliver at least one, preferably both, of a portion of the calcium -based chemical and carbon dioxide formed by the regeneration module to permeate produced by at least one reverse osmosis membrane to produce product water.

40. The plant as claimed in any one of claims 32-39, wherein at least one pipe is provided to recycle at least a portion of the calcium-based chemical formed by the regeneration module to the at least one reactor.41 . The plant as claimed in any one of claims 32-40, wherein the at least one reactor also precipitates magnesium hydroxide from the fluid and the at least one regeneration module is configured to regenerate at least some of the magnesium hydroxide precipitant to a magnesium-based chemical.

42. The plant as claimed in claim 41 , further comprising at least one pipe to deliver at least a portion of the magnesium-based chemical formed by the regeneration module to permeate produced by at least one reverse osmosis membrane to produce drinking water.

43. The plant as claimed in any of claims 28-42, wherein the at least one reactor having a calcium hydroxide (Ca(OH)2) source also precipitates magnesium hydroxide; and, the system includes at least one regeneration module regenerating at least some of the calcium carbonate and magnesium hydroxide precipitants to produce a calcium- based chemical, a magnesium-based chemical and carbon dioxide and piping to deliver at least some of the regenerated chemicals and carbon dioxide to permeate product water to produce drinking water.

44. The plant as claimed in any one of claims 31-43, wherein a bypass is provided between the intake sea water and the reverse osmosis pass to enable the delivery of a portion of the sea water through the at least one reactor with the remaining intake sea water bypassing the at least one reactor.

45. The plant as claimed in any one of claims 31-44, wherein at least one of a filter unit and a clearwell is provided between the at least one reactor and the pass.

46. The plant as claimed in any one of claims 28-45, wherein the at least one reactor is a fluidized bed reactor.

47. The plant as claimed in any one of claims 31-46, wherein a second brackish water reverse osmosis pass is in fluid communication with the first pass, wherein at least a portion of the permeate from the first pass is delivered to the second pass.

48. The plant as claimed in claim 47, wherein at least one of a sodium hydroxide and calcium hydroxide source and any combination is provided between the first and second pass to introduce sodium hydroxide or calcium hydroxide to the permeate prior to its introduction to the second pass.

49. The plant as claimed in any one of claims 31-48, wherein at least a portion of the brine delivered through the at least one reactor results in an increase in pH of the at least a portion of the brine to a pH of at least 8.3.

50. The plant as claimed in any one of claims 31-49, wherein only a portion of the brine is fed through the reactor with the remaining brine bypassing the at least one reactor.

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