[go: up one dir, main page]

WO2024263867A1 - Installation et procédé durables de dessalement d'eau - Google Patents

Installation et procédé durables de dessalement d'eau Download PDF

Info

Publication number
WO2024263867A1
WO2024263867A1 PCT/US2024/034947 US2024034947W WO2024263867A1 WO 2024263867 A1 WO2024263867 A1 WO 2024263867A1 US 2024034947 W US2024034947 W US 2024034947W WO 2024263867 A1 WO2024263867 A1 WO 2024263867A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
calcium
calcium carbonate
hydroxide
brine
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/US2024/034947
Other languages
English (en)
Inventor
Alex DRAK
Tomer EFRAT
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ide Americas Inc
Original Assignee
Ide Americas Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Ide Americas Inc filed Critical Ide Americas Inc
Priority to AU2024312006A priority Critical patent/AU2024312006A1/en
Publication of WO2024263867A1 publication Critical patent/WO2024263867A1/fr
Anticipated expiration legal-status Critical
Pending legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/04—Feed pretreatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/16—Feed pretreatment
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/18—Carbonates
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F5/00—Compounds of magnesium
    • C01F5/14—Magnesium hydroxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F5/00—Compounds of magnesium
    • C01F5/24—Magnesium carbonates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/06—Specific process operations in the permeate stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/263—Chemical reaction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/2642—Aggregation, sedimentation, flocculation, precipitation or coagulation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/2649—Filtration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • C02F1/004—Processes for the treatment of water whereby the filtration technique is of importance using large scale industrial sized filters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F2001/5218—Crystallization
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/108—Boron compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
    • C02F5/02—Softening water by precipitation of the hardness
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis

Definitions

  • the present invention relates generally to a more environmentally sustainable production of desalinated water and to a sustainable desalination plant.
  • 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.
  • 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.
  • 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.
  • SWRO sea water reverse osmosis pass
  • BWRO brackish water reverse osmosis
  • the main chemicals used for operation are sodium hydroxide (NaOH), sulphuric acid (H 2 SO 4 ), calcium carbonate (CaCO 3 ) and carbon dioxide (CO 2 ).
  • 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.
  • 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.
  • the fluids are selected from a group consisting of brine, effluents, waste and any combination thereof.
  • 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.
  • the process according to the first aspect includes 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 (CaCO 3 ).
  • 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 (CaCO 3 ), according to the following formula: Ca(OH)2 + Ca(HCO3)2 -> 2CaCO3 + 2H2O.
  • the process further comprises introducing calcium hydroxide (Ca(OH) 2 ) into the at least one reactor.
  • Ca(OH) 2 calcium hydroxide
  • 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.
  • Ca(OH) 2 calcium hydroxide
  • NaOH sodium hydroxide
  • 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.
  • 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.
  • the calcium-based chemical as defined above may be selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.
  • 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.
  • the step of regenerating the calcium carbonate comprises calcination comprising heating the calcium carbonate to a temperature of at least 500°C.
  • 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.
  • said step of hydrolysis of the calcium carbonate is performed at a temperature of less than 500°C.
  • 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.
  • 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.
  • 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.
  • Ca(OH) 2 calcium hydroxide
  • the process as defined above further comprises the step of regenerating at least some of the magnesium hydroxide precipitant to a magnesium-based chemical.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • at least a portion of the calcium carbonate, (CaCO 3 ) is used in the post treatments of the permeate water post the desalination step.
  • 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.
  • said fluids are selected from a group consisting of brine, effluents, waste and any combination thereof.
  • 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.
  • 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 (CaCO 3 ).
  • Ca(OH) 2 calcium hydroxide
  • 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.
  • 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.
  • 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.
  • 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.
  • said hydrolysis reactor operates at a temperature of less 500°C.
  • 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 ).
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • Ca(OH)2 calcium hydroxide
  • 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.
  • 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.
  • the at least one reactor is a fluidized bed reactor.
  • 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.
  • 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.
  • 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.
  • 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.
  • only a portion of the brine is fed through the reactor with the remaining brine bypassing the at least one reactor.
  • a process for the desalination of sea water 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.
  • 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 (CaCO 3 ).
  • Ca(OH)2 calcium hydroxide
  • NaOH sodium hydroxyanisole
  • CaCO 3 calcium carbonate
  • Ca(OH) 2 Ca(OH) 2 + Ca(HCO3)2 — > 2CaCO3 + 2H2O.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • the step of regenerating the calcium carbonate comprises calcination comprising heating the calcium carbonate to a temperature of at least 500°C.
  • 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.
  • said step of hydrolysis of the calcium carbonate is performed at a temperature of less than 500°C.
  • 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.
  • 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.
  • 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.
  • 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.
  • At least a portion of the magnesium-based chemical 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.
  • 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.
  • 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.
  • 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.
  • at least one of sodium hydroxide or calcium hydroxide is added to the permeate prior to its introduction to the second pass.
  • calcium hydroxide regenerated from the conversion of precipitated calcium carbonate is added to the permeate prior to its introduction into the second pass.
  • 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.
  • a desalination plant having enhanced sustainability 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.
  • 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 (CaCO 3 ).
  • Ca(OH) 2 calcium hydroxide
  • 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 (CaCO 3 ), according to the following formula: Ca(OH)2 + Ca(HCO3)2 --> 2CaCO3 + 2H2O.
  • 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.
  • At least a portion of the calcium hydroxide, Ca(OH) 2 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.
  • 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 ).
  • 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.
  • 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.
  • 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.
  • At least one, preferably both, of a filter unit and a clearwell is provided between the at least one reactor and the pass.
  • the at least one reactor is a fluidized bed reactor.
  • 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.
  • BWRO brackish water reverse osmosis pass
  • 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.
  • 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.
  • 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.
  • 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 (CO 2 ) 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 (CO 2 ) and any combination thereof regenerated from the calcium carbonate (CaCOs) precipitant to
  • 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.
  • Ca(OH) 2 calcium hydroxide
  • 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.
  • 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.
  • 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 (CaCO 3 ); at least one regeneration module to convert at least some of the calcium carbonate (CaCO 3 ) precipitant to at least one selected from a group consisting of calcium hydroxide (Ca(OH) 2 ), calcium oxide (CaO), carbon dioxide (CO 2 ) 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 (
  • 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 (CaCO 3 ).
  • a 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 (CaCO 3 ).
  • 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.
  • 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.
  • 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.
  • 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 (CaCO 3 ) and regenerating calcium hydroxide (Ca(OH) 2 ) and carbon dioxide (CO 2 ), 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.
  • Ca(OH) 2 calcium hydroxide
  • NaOH NaOH
  • CO 2 carbon dioxide
  • 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.
  • Mg(OH) 2 magnesium hydroxide
  • 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.
  • 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.
  • 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.
  • 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.
  • Any excess of the produced chemicals, such as calcium-based, magnesium-based and carbon dioxide may be sold as an additional income.
  • 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.
  • fluids are selected from a group consisting of brine, effluents, waste and any combination thereof.
  • 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.
  • brine fluids e.g., effluents, brackish water etc.
  • a process for the desalination of sea water 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.
  • 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).
  • 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.
  • Ca(OH) 2 Ca(OH) 2 + Ca(HCO3)2 -> 2CaCO3 + 2H2O.
  • 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.
  • Ca(OH) 2 calcium hydroxide
  • NaOH sodium hydroxide
  • 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.
  • the process further comprises the step of regenerating at least some of the calcium carbonate precipitant to a calcium- based chemical and carbon dioxide.
  • the calcium-based chemical is selected from a group consisting of calcium hydroxide or calcium oxide and any combination thereof.
  • 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.
  • 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.
  • Said step of hydrolysis of the calcium carbonate is preferably performed at a temperature of less than 500°C.
  • 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.
  • 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.
  • feeding at least a portion of brine through the at least one reactor containing calcium hydroxide (Ca(OH) 2 ) also precipitates magnesium hydroxide.
  • 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 process as defined above further comprises the step of regenerating at least some of the magnesium hydroxide precipitant to a magnesium- based chemical.
  • the process further comprises adding at least a portion of the regenerated magnesium-based chemical to the permeate to produce product water.
  • 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.
  • 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.
  • 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.
  • the process further comprises delivering at least a portion of the sea water to at least one of a filter unit and a clearwell.
  • 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.
  • 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.
  • the process excludes calcium carbonate contactor in the post -treatment of the permeate water.
  • 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.
  • 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 (CaCO 3 ).
  • 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 (CaCO 3 ), according to the following formula: Ca(OH)2 + Ca(HCO3)2 --> 2CaCO3 + 2H2O.
  • 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.
  • 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.
  • a self- sustainable desalination process for the desalination of sea water 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.
  • 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 (CaCO 3 ) from the at least a portion of the brine.
  • Ca(OH)2 calcium hydroxide
  • CaCO 3 calcium carbonate
  • 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 (CO 2 ), 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 (CO 2 ), magnesium hydroxide (Mg(OH) 2 ) and any combination thereof from said carbonates-based chemical.
  • 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 (CaCO 3 ); at least one regeneration module to convert at least some of the calcium carbonate (CaCO 3 ) 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 (CO 2 ) and any
  • 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.
  • Ca(OH) 2 calcium hydroxide
  • Mg(OH) 2 magnesium hydroxide
  • 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.
  • 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 (CaCO 3 ) and regenerating calcium hydroxide (Ca(OH) 2 ) and carbon dioxide (CO 2 ), 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.
  • 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.
  • Mg(OH) 2 magnesium hydroxide
  • 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.
  • At least a portion of the magnesium-based chemical 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.
  • Figure 1 is a schematic diagram illustrating a single pass SWRO system according to the prior art.
  • Figure 2 is a schematic diagram illustrating a double pass SWRO and BWRO system according to the prior art
  • Figure 3 is a schematic diagram of a more sustainable single pass SWRO system according to one embodiment of the present invention.
  • 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.
  • Figure 4 is a schematic diagram of a more sustainable double pass SWRO and BWRO system according to another embodiment of the present invention.
  • 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
  • Figure 7 is a schematic diagram of a more sustainable double pass SWRO and BWRO system according to another embodiment of the present invention.
  • 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.
  • 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.
  • 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.
  • Ca(OH) 2 calcium hydroxide
  • 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.
  • 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.
  • 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.
  • a calcium hydroxide (Ca(OH) 2 ) source to precipitate at least one carbonates-based chemical selected from a group consisting of calcium carbonate (CaCCh).
  • 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 (CO 2 ) and any combination thereof.
  • 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.
  • the at least one reactor having a calcium hydroxide (Ca(OH) 2 ) source also precipitates magnesium hydroxide
  • 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.
  • Ca(OH) 2 calcium hydroxide
  • CaCO 3 calcium carbonate
  • Ca(OH) 2 calcium hydroxide
  • CaO calcium oxide
  • CO 2 carbon dioxide
  • Mg(OH) 2 magnesium hydroxide
  • Ca(OH) 2 calcium hydroxide
  • CaO calcium oxide
  • CO 2 carbon dioxide
  • Mg(OH) 2 magnesium hydroxide
  • the calcium hydroxide Ca(OH) 2
  • CaO calcium oxide
  • CO 2 carbon dioxide
  • 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.
  • Ca(OH) 2 calcium hydroxide
  • Mg(OH)2 magnesium hydroxide
  • Ca(OH)2 calcium hydroxide
  • NaOH NaOH
  • CO 2 carbon dioxide
  • Mg(OH) 2 magnesium hydroxide
  • 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.
  • At least a portion of the magnesium-based chemical 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.
  • 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.
  • FIG. 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.
  • 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:
  • 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.
  • 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.
  • the regenerator 10 is a calcinator
  • the calcium carbonate is calcinated to result in the production of quicklime (calcium oxide) and carbon dioxide.
  • quicklime calcium oxide
  • 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.
  • the calcium hydroxide may be used in the post treatment process.
  • some of the calcium carbonate may be used in the post treatment process (as an alternative to regenerating the same in the reactor).
  • 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.
  • 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.
  • 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.
  • one ofthe advantages of the present invention is its operation at a higher pH that improves the boron rejection.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • the magnesium hydroxide may be delivered to the permeate water to provide drinking water.
  • 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.
  • FIG. 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.
  • 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.
  • 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).
  • 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.
  • 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.
  • 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.
  • 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.
  • calcium- based chemicals such as lime and quick lime
  • carbon dioxide for recycling and additional revenue streams.
  • 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.
  • 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.
  • regeneration of calcium carbonate back to calcium hydroxide may be provided by hydrolysis.
  • 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.
  • the hydrolysis products of calcium carbonate results in lime and carbon dioxide, according to the following equation:
  • the process and system parameters of the present invention can be further optimized to enhance cost and chemical savings.
  • 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.
  • the fact that the chemicals do not need to be delivered to the plant reduces the plant's carbon footprint.
  • the positive effect of alkalinity reduction from the brine is greater than the CO 2 emitted in the lime regeneration process.
  • magnesium hydroxide (Mg(OH) 2 )
  • Ca(OH) 2 calcium hydroxide
  • MgCO 3 magnesium carbonate
  • 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 (MgCO 3 ).
  • MgCO 3 magnesium carbonate
  • 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.
  • the reactor 2 mixes intake sea water with magnesium hydroxide to precipitate magnesium carbonate (MgCO 3 ) 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.
  • MgCO 3 magnesium carbonate
  • Magnesium hydroxide may be added to the permeate water, thereby enhancing the sustainability of the plant; and the CO 2 is used in the post treatment process.
  • magnesium oxide (similarly to calcium oxide) could be reacted with sea water to produce magnesium hydroxide.
  • 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.
  • the principles of the self-sustainability of the desalination process remains the same.
  • FIG. 8 of the accompanying drawings is a schematic diagram of a modified single pass SWRO system according to one embodiment of the present invention.
  • the carbonate removal (by precipitation of CaCO3) is performed after step of desalination (SWRO).
  • 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.
  • 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.
  • the fluids are selected from a group consisting of brine, effluents, waste and any combination thereof.
  • 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.
  • 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.
  • the fluids are selected from a group consisting of brine, effluents, waste and any combination thereof.
  • a precipitation reactor 2 such as a fluidized bed reactor
  • a precipitation reactor 2 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:
  • 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).
  • a treatment e.g., desalination process and plant
  • calcium carbonate contactors are not required.
  • 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).
  • 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.
  • the regenerator 10 is a calcinator
  • the calcium carbonate is calcinated to result in the production of quicklime (calcium oxide) and carbon dioxide.
  • quicklime calcium oxide
  • 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.
  • lime calcium hydroxide
  • the calcium hydroxide may be used in the post treatment process.
  • 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.
  • 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.
  • 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.
  • 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.
  • the magnesium hydroxide may be delivered to the permeate water to provide drinking water.
  • 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.
  • not all calcium carbonate, (CaCO 3 ) 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • calcium - based chemicals such as lime and quick lime
  • carbon dioxide for recycling and additional revenue streams.
  • 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.
  • 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.
  • regeneration of calcium carbonate (according to any of the embodiments disclosed in this application) back to calcium hydroxide may be provided by hydrolysis.
  • 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.
  • the hydrolysis products of calcium carbonate results in lime and carbon dioxide, according to the following equation:
  • the process and system parameters of the present invention can be further optimized to enhance cost and chemical savings.
  • 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.
  • the fact that the chemicals do not need to be delivered to the plant reduces the plant's carbon footprint.
  • the positive effect of alkalinity reduction from the brine is greater than the CO 2 emitted in the lime regeneration process.
  • 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 (MgCO 3 ).
  • MgCO 3 magnesium carbonate
  • FIG 9 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.
  • 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.
  • 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.
  • the principles of the self-sustainability of the desalination process remains the same.
  • 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.
  • the principles of the self-sustainability of the desalination process remains the same.
  • 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:
  • the NaOH will be provided by e.g., reaction of NaCI with water according to the following:
  • the HCI could be sold to any 3 rd party.
  • magnesium-based chemicals could be added in the post treatment (e.g., MgOH).
  • isotopic variants of compounds disclosed herein are intended to be encompassed by the disclosure.
  • 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.
  • ranges specifically include the values provided as endpoint values of the range.
  • 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.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Geology (AREA)
  • Inorganic Chemistry (AREA)
  • Nanotechnology (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Removal Of Specific Substances (AREA)

Abstract

L'invention concerne un procédé et une installation de dessalement d'eau de mer dans lesquels l'eau de mer est acheminée vers au moins une passe d'osmose inverse comprenant au moins une membrane d'osmose inverse pour produire un perméat d'eau et une saumure ; au moins une partie de la saumure est acheminée vers au moins un réacteur (2) pour l'élimination des produits chimiques à base de carbonates présents dans la saumure par précipitation du carbonate de calcium. Le carbonate de calcium est converti dans un régénérateur (10) pour produire de l'hydroxyde de calcium et du dioxyde de carbone. Il en résulte une série d'avantages sur le plan de la rentabilité globale et de la durabilité du processus ou de l'installation.
PCT/US2024/034947 2023-06-21 2024-06-21 Installation et procédé durables de dessalement d'eau Pending WO2024263867A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2024312006A AU2024312006A1 (en) 2023-06-21 2024-06-21 Sustainable desalination plant and sustainable method for the desalination of water

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IL303949 2023-06-21
IL303949A IL303949A (en) 2023-06-21 2023-06-21 Sustainable desalination plant and sustainable method for water desalination

Publications (1)

Publication Number Publication Date
WO2024263867A1 true WO2024263867A1 (fr) 2024-12-26

Family

ID=93936295

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2024/034947 Pending WO2024263867A1 (fr) 2023-06-21 2024-06-21 Installation et procédé durables de dessalement d'eau

Country Status (3)

Country Link
AU (1) AU2024312006A1 (fr)
IL (1) IL303949A (fr)
WO (1) WO2024263867A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4392959A (en) * 1981-05-15 1983-07-12 Coillet Dudley W Process for sterilization and removal of inorganic salts from a water stream
EP1460042A2 (fr) * 2003-03-18 2004-09-22 Uwe Meffert Procédé de production d'eau minérale potable
KR100854913B1 (ko) * 2007-10-01 2008-08-28 (주) 세화엠텍 초미립 경질 탄산칼슘 제조방법 및 장치
US20170341982A1 (en) * 2016-05-26 2017-11-30 X Development Llc Building materials from an aqueous solution
AU2021365682A1 (en) * 2020-10-20 2023-06-01 Yokogawa Electric Corporation Water treatment method and water treatment apparatus

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4392959A (en) * 1981-05-15 1983-07-12 Coillet Dudley W Process for sterilization and removal of inorganic salts from a water stream
EP1460042A2 (fr) * 2003-03-18 2004-09-22 Uwe Meffert Procédé de production d'eau minérale potable
KR100854913B1 (ko) * 2007-10-01 2008-08-28 (주) 세화엠텍 초미립 경질 탄산칼슘 제조방법 및 장치
US20170341982A1 (en) * 2016-05-26 2017-11-30 X Development Llc Building materials from an aqueous solution
AU2021365682A1 (en) * 2020-10-20 2023-06-01 Yokogawa Electric Corporation Water treatment method and water treatment apparatus

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
A. BOTHA ET AL.: "Preparation of a magnesium hydroxy carbonate from magnesium hydroxide", HYDROMETALLURGY, vol. 62, no. 3, December 2001 (2001-12-01), pages 175 - 18, XP004311741, [retrieved on 20011025], DOI: doi.org/10.1016/S0304-386X(01)00197-9 *

Also Published As

Publication number Publication date
IL303949A (en) 2025-01-01
AU2024312006A1 (en) 2025-12-04

Similar Documents

Publication Publication Date Title
US8999171B2 (en) Membrane and electrodialysis based seawater desalination with salt, boron and gypsum recovery
CA2812225C (fr) Procede de filtration par membrane a recuperation de retentat et injection de dioxyde de carbone
KR101943421B1 (ko) 삼투압 분리 시스템 및 방법
US6998053B2 (en) Water desalination process using ion selective membranes
CN101928088B (zh) 一种石化企业反渗透浓水的处理方法
WO2014089796A1 (fr) Procédé de traitement des eaux usées fortement concentrées telles que la saumure d'osmose inverse (ro)
EP1206414B1 (fr) Processus de dessalement d'eau salee a l'aide de membranes selectives ioniques
CA2659451A1 (fr) Procedes et systemes de dessalement qui comprennent une precipitation de composes de type carbonate
CN1507417A (zh) 水处理方法和水处理设备
KR20140105348A (ko) 삼투 에너지 회수가 가능한 담수화 시스템 및 방법
CN105198141B (zh) 一种高温高盐废水的零排放方法
CN113105025B (zh) 钠离子交换器再生高浓盐废水的联合处理方法
WO2024076619A1 (fr) Installation et procédé durable de dessalement d'eau
CN208008625U (zh) 一种反渗透浓水的分盐浓缩系统
WO2016160810A1 (fr) Procédés et systèmes de séparation osmotique
KR20210133631A (ko) 해수담수화 압력지연삼투 기술을 이용한 복합 담수화 시스템
CN110550802A (zh) 一种高盐水溶液零排放处理系统及方法
WO2024263867A1 (fr) Installation et procédé durables de dessalement d'eau
US20240123400A1 (en) Systems and methods for integrated direct air carbon dioxide capture and desalination mineral recovery
Ma et al. Efficient treatment of high-salinity aquaculture effluents through synergistic membrane distillation and VUV/UVC photolysis
KR101489853B1 (ko) 초고염도수의 삼투 에너지 회수가 가능한 담수화 시스템 및 방법
IL310951A (en) Sustainable Desalination Plant and Sustainable Method for the Desalination of Water
WO2020256759A1 (fr) Système et procédé de reminéralisation
AU2005100689A4 (en) Process for desalination of seawater with zero effluent and zero greenhouse gas emission
WO2025010402A1 (fr) Installation de dessalement durable et procédé durable pour le dessalement de l'eau

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 24826701

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: AU2024312006

Country of ref document: AU