Circular system to transform co2 emissions into durable mineralized carbonates with recycling of solvents, water and heat

Abstract

A circular system and method for mineralizing carbon dioxide and separating durable carbonate minerals from an aqueous solution and recycling purified brine resulting from the mineralizing of the carbon dioxide for further use in the mineralizing of the carbon dioxide, while recycling heat and water.

Description

[0001] CIRCULAR SYSTEM TO TRANSFORM CO2 EMISSIONS INTO DURABLE MINERALIZED CARBONATES WITH RECYCLING OF SOLVENTS, WATER AND HEAT

[0002] CROSS REFERENCE TO RELATED APPLICATION

[0003] The instant application is a PCT application of, and claims priority to, U.S. Provisional Application No. 63 / 548,588, filed on February 1, 2024, which is incorporated by reference herein in its entirety.

[0004] TECHNICAL FIELD

[0005] The system and process disclosed herein includes a circular and adaptable solution to utilize carbon dioxide by reacting with other chemicals, preferably sourced from, but not limited to, waste streams to produce durable mineralized carbonates that can be released to the environment or sold as products to other industries. Additionally, the process produces heat, water and purified solvents that can be reused in the system and process to reduce energy and material consumption. This holistic approach delivers significantly higher efficiency enhanced circularity, and greater value compared to incumbent technologies.

[0006] BACKGROUND

[0007] The advent of more affordable renewable energy sources and the continued advancements in the electrochemical activation (ECA) and membrane-free electrolysis technologies have improved the viability of smaller-scale chlor-alkali production. The COVID- 19 pandemic also sparked a demand for effective “Clean-in-Place” (CIP) production of disinfectant and detergent utilizing these same technologies.

[0008] According to the Synthesis Report (SYR) of the Intergovernmental Panel on Climate Change (IPCC) Sixth Assessment Report (AR6), humans have warmed the climate between 0.8- 1 3°C since pre-industrial levels through greenhouse gas (GHG) emissions, and climate warming above 1.5°C could cause long-lasting and irreversible damage such as loss of ecosystems, sea level rise, drought, extreme heat, extreme precipitation, increased forest fires, the spread of invasive species, and ocean acidification. To remain below 1.5°C of warming, global net anthropogenic GHG emissions must decrease from a current estimated rate of 59 ± 6.6 GtCO2- eq to net-zero GHG emissions in 2050. Doing so will require dramatic improvements in efficiency, conversion to renewable energy sources, and carbon dioxide removal (CDR) via nature-based and technological solutions.

[0009] Most proposed and early-stage solutions for CDR have focused on nature-based solutions such as large-scale forestation or agricultural enhancement, or technology-based solutions such as the large-scale deployment of Direct Air Capture (DAC) and geologic sequestration of captured carbon dioxide. These large-scale projects require massive amounts of time, funding, infrastructure construction of facilities and transportation pipelines, and unique challenges to safely inject, secure, and monitor sites for hundreds of years. The U.S. Congressional Research Service provided a review Injection and Geologic Sequestration of Carbon Dioxide: Federal Role and Issues for Congress (Updated September 22, 2022) that highlighted that only 2 Class VI wells had been permitted of a total 735,408 (less than 0.01%) as of the time of the report

[0010] The U.S. Department of Energy (DOE) National Energy Technology Laboratory (NETL) published Overview of Potential Failure Modes and Effects Associated with CO2 Injection and Storage Operations in Saline Formations DOE / NETL-2020 / 2634, December 18, 2020, that highlighted a variety of potential failure modes and effects of such failures, including three that could result in catastrophic impacts that represent reasonably foreseeable significant adverse impacts to the human environment: 1. Fast-conduit (high transmission) leakage of CO2 to the atmosphere along a surface-intersecting fault 2. Fast-conduit (high transmission) leakage of CO2 to the atmosphere along a wellbore 3. Triggered seismic event (“felt earthquake” above an approximate 6.0 magnitude).

[0011] In the difficult-to-decarbonize carbon dioxide-intensive manufacturing processes for chemicals, minerals, raw materials, equipment, and building products, the focus has been on incremental efficiency improvements or modest transitions to renewable power sources. Most industry initiatives neglect to recognize that vast amounts of industrial carbon dioxide generation do not come from the burning of fossil fuels, but rather the chemical reactions related to fermentation, calcination, and other exothermic processes. For instance, cement manufacturing is widely estimated to produce 8% of global anthropogenic GHG emissions, yet only 40% of carbon dioxide emissions are derived from fossil fuel combustion while the majority is due to calcination in the cement kiln. These calcination-related emissions alone represent nearly 5% of global carbon dioxide emissions, and there are vast amounts of CO2 emitted from chemical reactions and fermentation at breweries, distilleries, food production, silage, and other processes. A transition is urgently needed toward a system for sequestration of carbon dioxide that addresses the forgoing problems.

[0012] SUMMARY

[0013] There is disclosed herein a system for capturing carbon dioxide, converting the carbon dioxide to carbonate minerals and recycling solvents and heat for reuse. The system includes an alkali producing system that is configured for producing an aqueous alkali. The system for capturing carbon dioxide includes a carbon dioxide source. The system also includes a chemical absorption apparatus that is in communication with the alkali producing system and the carbon dioxide source. The chemical absorption apparatus is configured to react carbon dioxide with the aqueous alkali thereby chemically absorbing at least a portion of the carbon dioxide from inside the chemical absorption apparatus, into an aqueous solution. The system for capturing carbon dioxide includes a brine supply system that is configured to treat seawater therein and to discharge brine therefrom. The system for capturing carbon dioxide also includes a treatment system, that includes one or more dosing tanks, one or more aging mixing vessel system and a separator system. The treatment system is configured to selectively control chemical and physical properties and the residence time of substances flowing therethrough. The dosing tanks are located downstream of and in communication with the chemical absorption apparatus. The dosing tanks are configured to receive the aqueous solution from the chemical absorption apparatus and to treat the aqueous solution to create a treated aqueous solution. The aging mixing vessel systems are located downstream of the dosing tanks. The aging mixing vessel systems are configured to: (a) receive the brine from the brine supply system, (b) receive the treated aqueous solution from the at least one dosing tank, (c) create a slurry therein, and (d) discharge the slurry therefrom. The separator system is located downstream of the mixing vessel systems. The separator system is configured to receive the slurry from the aging mixing vessel systems. The separator system is configured to separate the brine from carbonate minerals and discharge the carbonate minerals and recovered brine in separate streams. The system for capturing carbon dioxide includes a recycle line that is configured to transport the recovered brine from the separator system back to the alkali producing system, for further production of an aqueous alkali.

[0014] In some embodiments, the alkali producing system is configured to produce sodium hydroxide. In some embodiments, the carbon dioxide source provided by one or more of fossil- fueled power plants, combined heat and power (CHP) plants, gas turbine CHP plants, gas engine CHP plants, biofuel engine CHP plants, combined cycle power plants adapted for CHP, fuel cell CHP plants, steam turbine CHP plants, biogas power plants, fixed dome / gasholder biogas plants, floating dome design biogas plants, natural gas engines and turbines, cement production facilities, steel and iron production facilities, aluminum production plants, glass manufacturing processes, ceramic production processes, refineries and petrochemical plants, ammonia production plants, lime and quicklime production facilities, paper and pulp mills, distilleries and breweries, landfills and composting facilities, wastewater treatment plants, food processing plants, carbonated beverage production facilities, residential and commercial heating systems, small-scale diesel or gasoline generators, maritime diesel engines, aviation engines, heavy-duty land vehicles, agricultural activities, livestock farming, mining operations, and construction sites.

[0015] In some embodiments, the chemical absorption apparatus is configured to react the carbon dioxide with the sodium hydroxide.

[0016] In some embodiments, the brine supply system includes one or more of an evaporator, a reverse osmosis system, an industrial waste brine source and geological brine source.

[0017] In some embodiments, the brine supply system includes one or more of an industrial waste brine source and geological brine source and the brines provided therefrom are concentrated via an evaporator and / or a reverse osmosis system.

[0018] In some embodiments, the evaporator and / or the reverse osmosis system is supplied with the seawater.

[0019] In some embodiments, the system for capturing carbon dioxide, further includes a pretreatment and conditioning system in a supply line to the evaporator, the reverse osmosis system, the industrial waste brine source, and / or the geological brine source.

[0020] In some embodiments, the pre-treatment and conditioning system includes one or more of an intake screen, a sand filter, a cartridge filter, a bag filter, a ultrafiltration unit, a chlorination system, a di chlorination system, a pH adjustment system, a hydrocyclone, a softening system, a micron filter, a de-gasifier system, an ozonation system, a UV sterilizer, a chemical dosing system, and additional concentrator units.

[0021] In some embodiments, the brine supply system includes a reverse osmosis system which is configured to produce the brine and water therefrom. In some embodiments, the alkali producing system includes a chlor-alkali process, an electro chemical activation system, a membrane-free electrolysis system, a causticization process using sodium carbonate and calcium hydroxide, a lime soda process, and a mineral extraction process comprising trona or alkali-containing minerals, and an alkali extraction unit.

[0022] In some embodiments, the system includes a power supply in electrical communication with the chlor-alkali process, the electro chemical activation system, and the membrane-free electrolysis system, wherein the power supply is preferably a renewable energy source. In some embodiments, the renewable energy source is at least one of a solar powered photo-voltaic system, a wind energy system, a fuel cell system powered by green hydrogen or renewable fuels, solar thermal systems, hydropower systems, geothermal energy systems, renewable hydrogen systems, a biomass or biogas fueled power plant, a waste-to-energy system, a waste-heat- recovery system and a hybrid renewable energy system.

[0023] In some embodiments, the alkali producing system is supplied with seawater.

[0024] In some embodiments, the system further includes a pre-treatment and conditioning system that includes one or more of an intake screen, a sand filter, a cartridge or bag filter, a ultrafiltration unit, a chlorination system, a dichlorination system, a pH adjustment system, a hydrocyclone, a softening system, a micron filter, a de-gasifier system, an ozonation system, a UV sterilizer, a chemical dosing system, and additional concentrator units, in a supply line for the seawater provided to the alkali producing system.

[0025] In some embodiments, the chemical and physical properties include purity, chemical composition, concentration, density, and states of matter.

[0026] In some embodiments, the chemical absorption apparatus includes one or more of packed columns, tray columns, spray columns, bubble columns, venturi scrubbers, mini or microreaction technology.

[0027] In some embodiments, the slurry discharged from the at least one aging mixing vessel system includes calcium carbonate and / or magnesium carbonate.

[0028] In some embodiments, the treated aqueous solution discharged from the chemical absorption system includes, for example, sodium carbonates (Na2COs) and sodium bicarbonates (NaHCCh), residual NaOH, other carbonates, hydroxides, and other byproducts. In some embodiments, the system includes one or more dryer located downstream of the separator system. The dryers are configured to receive and dry the carbonate minerals. In some embodiments, the separator system includes a mechanical separation unit, preferably a filter, a hydrocyclone, a decanter, a centrifuge and / or fluid-solid separation equipment that is combined with a washing step.

[0029] In some embodiments, the separator system includes two of the mechanical separation units arranged in a series configuration.

[0030] In some embodiments, the system includes a holding vessel located downstream of the dryers and in communication with the dryers via a conduit.

[0031] In some embodiments, the system includes (a) a first surface modification supply provided into the conduit. The first surface modification supply is configured to provide a first surface modification substance for application on the carbonate minerals; and / or (b) a second surface modification supply provided into the holding vessel. The second surface modification supply is configured to provide a second surface modification substance for application on the carbonate minerals.

[0032] In some embodiments, the first surface modification substance and / or the second surface modification substance is configured to increase reactivity of the carbonate minerals.

[0033] In some embodiments, the carbonate minerals include calcium carbonate and / or magnesium carbonate.

[0034] In some embodiments, the aging mixing vessel system includes an agitator therein.

[0035] In some embodiments, the recycle line includes a pre-treatment and conditioning system that includes an intake screen, a sand filter, a cartridge or bag filter, an ultrafiltration unit, a chlorination system, a dichlorination system, a pH adjustment system, a hydrocyclone, a softening system, a micron filter, a de-gasifier system, an ozonation system, a UV sterilizer, a chemical dosing system, and additional concentrator units therein.

[0036] In some embodiments, the recycle line discharges into a tank which has a recycle line that is in communication with the alkali producing system.

[0037] In some embodiments, the system includes a pre-treatment and conditioning system that includes an intake screen, a sand filter, a cartridge or bag filter, a ultrafiltration unit, a chlorination system, a dichlorination system, a pH adjustment system, a hydrocyclone, a softening system, a micron filter, a de-gasifier system, an ozonation system, a UV sterilizer, a chemical dosing system, and / or additional concentrator unit located in the recycle line. In some embodiments, the system includes a gas cooling device located downstream of the carbon dioxide source and upstream of the chemical absorption apparatus. The gas cooling device is configured for reducing temperature of the carbon dioxide provided by the carbon dioxide source.

[0038] In some embodiments, the gas cooling device is in heat transfer communication with an optional waste-heat-recovery system, the brine supply system, the dryers, and / or the holding vessels, for transferring heat thereto.

[0039] In some embodiments, the system includes a non-transitory computer readable storage medium comprising computer-executable instructions that is configured to instruct the selectively controlling of the chemical and physical properties of the substances flowing through the treatment system.

[0040] In some embodiments, a portion of the system is disposed in a container.

[0041] There is further disclosed herein a circular method of mineralizing carbon dioxide that includes capturing carbon dioxide from an emissions source; treating the carbon dioxide with sodium hydroxide and a brine; separating purified brine and carbonate minerals; discharging the carbonate minerals and purified brine in separate streams; and recycling the purified brine for use in the mineralizing carbon dioxide.

[0042] There is further disclosed herein a kit for capturing carbon dioxide, converting the carbon dioxide to carbonate minerals and recycling solvents and heat for reuse. The kit includes a container that has an exterior shell and an interior area, an electrical power connection that penetrates the exterior shell, brine supply connections that penetrate the exterior shell, and a carbon dioxide connection that penetrates the exterior shell. The interior area of the container has disposed therein an alkali producing system that is configured for producing an aqueous alkali. The alkali producing system is in electrical communication with the electrical power connection and the seawater connection. The interior area of the container has disposed therein a chemical absorption apparatus that is in communication with the alkali producing system and the carbon dioxide connection. The chemical absorption apparatus is configured to react carbon dioxide with the aqueous alkali thereby chemically absorbing at least a portion of the carbon dioxide from inside the chemical absorption apparatus into an aqueous solution that includes sodium carbonates (Na2COs), sodium bicarbonates (NaHCCh), and other byproducts. The interior area of the container has disposed therein a treatment system, which includes dosing tanks, an aging mixing vessel system and a separator system. The treatment system is configured to selectively control chemical and physical properties and residence time of substances flowing therethrough and being in fluid communication with the at least one brine connection. The dosing tanks are located downstream of and in communication with the chemical absorption apparatus. The dosing tanks are configured to receive the aqueous solution from the chemical absorption apparatus and to treat the aqueous solution to create a treated aqueous solution. The aging mixing vessel system is located downstream of the dosing tanks. The aging mixing vessel system is configured to: (1) receive the brine from the at least one brine connection, (2) receive the treated aqueous solution from the at least one dosing tanks, (3) create a slurry therein, and 4) discharge the slurry therefrom. The separator system is located downstream of the mixing vessel system. The separator system is configured to receive the slurry from the aging mixing vessel system. The separator system is configured to separate the brine from carbonate minerals and discharge the carbonate minerals and recovered brine in separate streams. The interior area of the container has disposed therein a recycle line that is configured to transport the recovered brine from the separator system back to the alkali producing system, for producing aqueous alkali.

[0043] BRIEF DESCRIPTION OF THE DRAWINGS

[0044] FIG. l is a block diagram of a novel system and process for capturing carbon dioxide, converting the carbon dioxide to carbonate minerals and recycling solvents and heat for reuse, disclosed herein; and

[0045] FIG. 2 is a schematic diagram of a portion of the system of FIG. 1, disposed in a container.

[0046] DETAILED DESCRIPTION

[0047] FIG. 1 depicts a flow diagram showing the system and process 100 for capturing carbon dioxide (CO2), converting the carbon dioxide to carbonate minerals and recycling solvents for reuse. The system 100 employs a mineralization of carbon dioxide, which refers to the process where carbon dioxide is converted into a solid carbonate mineral or solid carbonate minerals by reacting with certain other minerals, like those containing calcium or magnesium, effectively capturing and storing the carbon in a stable form and is used as a method for carbon sequestration. The solid carbonate mineral or solid carbonate minerals are in a granular, powder, rock, pellet or other suitable and / or durable form. The process is circular for the solvents which are recycled for use in the mineralization of the carbon dioxide. The system 100 recycles heat from the gas cooling device such as a chiller / heat exchanger 9 or chemical absorption apparatus 3 for use in heating the seawater 2W, for use in the evaporator 2A or the reverse osmosis system 2B, heating the industrial waste brine source 2C and / or the geological brine source 2C’. The recycled heat is also used in the dryers 7A, 7B. As used herein, the term brine refers to a concentrated aqueous solution of inorganic salt with a certain concentration of calcium chloride or magnesium chloride (individual or as mixture, as concentrated seawater, industrial waste brine or geological brine) supplied by the brine supply system 2. In some embodiments, the brine is a pre-mixed solution. In some embodiments, the brine is custom mixed, for example by combining anhydrous calcium chloride (CaCh) and / or magnesium chloride (MgCh) and water to specific desired concentrations.

[0048] Referring to FIG, 1, the use of an electrical energy source (e.g., preferably renewable energy sources 40) to power an alkali producing system 1, such as a chlor-alkali process 1A, an electrochemical activation system (EC A) IB, a membrane-free electrolysis system 1C, a causticization process ID using sodium carbonate and calcium hydroxide, a lime soda process IE, a mineral extraction process comprising trona or alkali-containing minerals IF, and / or an alkali extraction unit 1G (e.g., leaching of waste materials) to produce an alkali such as sodium hydroxide (NaOH) or other bases which feeds to a chemical absorption apparatus 3 which is located downstream of the alkali producing system 1 and in fluid communication therewith via a conduit 3A. Seawater 2W from a seawater source W is supplied to each of the chlor-alkali process 1A, the electrochemical activation system (ECA) IB, the membrane-free electrolysis system 1C, the causticization process ID, the lime soda process IE, the mineral extraction process IF, and the alkali extraction unit 1G, via a valve, actuator and conduit system that is selectively controlled by the control unit. Each of the chlor-alkali process 1 A, the electrochemical activation system (ECA) IB, the membrane-free electrolysis system 1C, the causticization process ID, the lime soda process IE, the mineral extraction process IF, and the alkali extraction unit 1G discharge the alkali 1H to the chemical absorption apparatus 3 via suitable valve, actuator and conduit system (e.g., individual discharge lines 1A’, IB’, 1C’, ID’, IE’, IF’ and 1G’) via the conduit 3A or each discharge directly to the chemical absorption apparatus 3. The chemical absorption apparatus 3 brings CO2 containing gas and a liquid into contact. In the chemical absorption apparatus 3 the CO2 absorbs in the liquid and bonds through a chemical reaction. The chemical absorption apparatus 3 is for example, packed columns, tray columns, spray columns, bubble columns, a venturi scrubber, reactor systems (e.g., mini and microreactors, impinging jet reactors, jet loop reactors) and other systems (rotating packed-beds, membrane contactors, spray jets). The system 100 includes an apparatus 9 to reduce the temperature of the CCh-rich gas stream (e.g., a gas cooling device such as a chiller / heat exchanger 9 which is configured to receive and cool a carbon dioxide rich gas stream and to transfer the heat to a liquid for a heat shift to other process units. The CCh-rich gases from the gas cooling device 9 (for example, as heat exchanger, chiller, refrigeration cycles) are combined with the sodium hydroxide (NaOH) in the chemical absorption apparatus 3. The resultant aqueous solution is then fed to a primary dosing tank 4A and / or an optional secondary dosing tank 4B which is fed to downstream aging tanks 5A, 5B where the aqueous solution is then mixed with a calcium and / or magnesium-rich brine from a seawater evaporator 2A, seawater reverse osmosis (RO) unit 2B, or concentrated brine 2C recycled from industrial waste or geologic sources 2C’. Process heat from the gas cooler 9 and the chemical absorption are used to support the concentration of the seawater 2A or the industrial waste brine or geologically sourced brine 2C. The reaction product from the absorption apparatus and the solution that contains magnesium and / or calcium are brought into contact and form a slurry due to precipitation. Due to the contact, a slurry that contains calcium carbonate and or magnesium carbonate as the main component forms and is stored in the aging tanks 5A, 5B downstream to next stages of dewatering and washing in a separator system such as a primary mechanical separation unit 6A and / or an optional secondary mechanical separation unit centrifuge 6B. The wastewater from the washing cycle is configured to be disposed or separately reprocessed while the purified brine (NaCl) will be recycled back to the alkali producing system 1 to restart the circular carbon dioxide mineralization cycle. In some embodiments, the discharge from the primary centrifuge 6A is transported to a first dryer 7A which discharges the solid carbonate minerals 8A such as calcium carbonate (CaCCh). In some embodiments, the discharge from the primary mechanical separation unit 6A is transported to a secondary mechanical separation unit 6B and then transported therefrom to a second dryer 7B which discharges the solid carbonate minerals 8B such as the inorganic salt with the chemical name magnesium carbonate (MgCCf). In some embodiments the primary mechanical separation unit 6A and the secondary mechanical separation unit 6B include a fdter, a hydrocyclone, a decanter, a centrifuge and fluid-solid separation equipment that is combined with a washing step. In some embodiments, primary mechanical separation unit 6A and the secondary mechanical separation unit 6B are arranged in a series configuration.

[0049] As shown in FIG. 1, a system for capturing carbon dioxide, converting the carbon dioxide to carbonate minerals and recycling solvents for reuse is generally designated by the numeral 100. The system 100 includes an alkali producing system 1 configured for producing an aqueous alkali 1H from seawater 2W supplied by a seawater source W. In some embodiments, a pretreatment and conditioning system F6 is provided in a supply line of the sea water 2W to the alkali producing system 1. In some embodiments, the alkali producing system 1 is configured to produce sodium hydroxide. The system 100 is in communication with a carbon dioxide source 50. The system 100 includes a chemical absorption apparatus 3 in communication with the alkali producing system 1 and the carbon dioxide source 50. The chemical absorption apparatus 3 is configured to react carbon dioxide with the aqueous alkali 1H (e.g., sodium hydroxide NaOH or calcium hydroxide (Ca(OH)2) thereby chemically absorbing at least a portion of the carbon dioxide from inside the chemical absorption apparatus 3 into an aqueous solution 3X that includes a carbonate (e.g., sodium carbonate (Na2COa), sodium bicarbonates (NaHCOa), or calcium carbonate (CaCOa) and water (H2O)). Examples of chemical reactions in the chemical absorption apparatus 3 are as follows:

[0050] Example with sodium hydroxide: CO2 + H2O + 2NaOH -> Na2COa + 2H2O

[0051] Example with calcium hydroxide: CO2 + Ca(OH)2 -> CaCOa + H2O

[0052] While the chemical absorption apparatus 3 is described as being configured to react carbon dioxide with the aqueous alkali 1H (e.g., sodium hydroxide NaOH or calcium hydroxide (Ca(OH)2) thereby chemically absorbing at least a portion of the carbon dioxide from inside the chemical absorption apparatus 3 into an aqueous solution 3X that includes a carbonate (e.g., sodium carbonate (Na2COs), sodium bicarbonates (NaHCOs), or calcium carbonate (CaCOa)) and water (H2O)), the present invention is not limited in this regard as other suitable aqueous alkalis 1H may be employed for chemically absorbing at least a portion of the carbon dioxide from inside the chemical absorption apparatus 3 into an aqueous solution 3X that includes a carbonate and waters, and in which the carbonates include but are not limited to (1) Alkali metal carbonates, for example, Lithium carbonate, Sodium carbonate, Potassium carbonate, Rubidium carbonate, Cesium carbonate, Francium carbonate; (2) Alkaline Earth metal carbonates, for example, Beryllium carbonate, Magnesium carbonate, Calcium carbonate, Strontium carbonate, Barium carbonate, Radium carbonate; (3) Lanthanide carbonates, for example, Lanthanum carbonate, Cerium carbonate, Praseodymium carbonate, Neodymium carbonate, Promethium carbonate, Samarium carbonate, Europium carbonate, Gadolinium carbonate, Terbium carbonate, Dysprosium carbonate, Holmium carbonate, Erbium carbonate, Thulium carbonate, Ytterbium carbonate, Lutetium carbonate; (4) Actinide carbonates, for example, Actinium carbonate, Thorium carbonate, Protactinium carbonate, Uranium carbonate, Neptunium carbonate, Plutonium carbonate, Americium carbonate, Curium carbonate, Berkelium carbonate, Californium carbonate, Einsteinium carbonate, Fermium carbonate, Mendelevium carbonate, Nobelium carbonate, Lawrencium carbonate; (5) Transition metal carbonates, for example, Scandium carbonate, Yttrium carbonate, Titanium carbonate, Zirconium carbonate, Hafnium carbonate, Rutherfordium carbonate, Vanadium carbonate, Niobium carbonate, Tantalum carbonate, Dubnium carbonate, Chromium carbonate, Molybdenum carbonate, Tungsten carbonate, Seaborgium carbonate, Manganese carbonate, Technetium carbonate, Rhenium carbonate, Bohrium carbonate, Iron carbonate, Ruthenium carbonate, Osmium carbonate, Hassium carbonate, Cobalt carbonate, Rhodium carbonate, Iridium carbonate, Nickel carbonate, Palladium carbonate, Platinum carbonate, Copper carbonate, Silver carbonate, Gold carbonate, Zinc carbonate, Cadmium carbonate, Mercury carbonate (6) Post-transition metal carbonates - Aluminum carbonate, Gallium carbonate, Indium carbonate, Thallium carbonate, Tin carbonate, Lead carbonate, Bismuth carbonate, Polonium carbonate, Astatine carbonate; and (7) combinations of multi-chemical carbonates, for example, dolomite, in which both Ca and Mg are present, (i.e., CaMg(CC>3)2)

[0053] In some embodiments, a gas cooling device 9 (e.g., a heat exchanger such as tube in shell heat exchanger or a chiller) is located downstream of the carbon dioxide source 50 and upstream of the chemical absorption apparatus 3. The gas cooling device 9 is configured for reducing the temperature of the carbon dioxide provided by the carbon dioxide source 50.

[0054] As shown in FIG. 1, the system 100 includes a brine supply system 2 that is configured to treat seawater 2W form a seawater source W and to discharge brine 2D from the brine supply system 2. The system 100 includes a treatment system 456 that is shown, for example, with two dosing tanks 4A, 4B, two aging mixing vessel systems 5A, 5B and a separator system 6A, 6B.

[0055] The treatment system 456 is configured to selectively control the process including, for example, chemical and physical properties (e.g., purity, chemical composition, concentration, density, and states of matter) and residence time of substances flowing therethrough. The process controls for the precipitation process and many of the desired carbonate characteristics have specific industry applications which are managed by the control unit. For example, process controls for the precipitation of specific CaCCh and MgCCh polymorphs, particle sizes, and related characteristics include, but are not limited to saturation level, temperature, pH, ionic strength, stirring, mixing, molar ratio, additive chemistry, additive concentration, time, surfactant ratio, equilibrium constant, sequencing, pressure, mass transfer coefficient, spatial concentration distribution, and agglomeration coefficient. In addition, process controls for CaCCh and MgCCf include but are not limited to purity (contaminants), fineness (screen / mesh residue), median particle size (d50%), specific surface area (BET), optical properties - brightness, color (Hunter Y), moisture, pH (powder), apparent density (tamped), apparent density (loose), oil absorption, specific gravity, mean refractive index, Hegman, particle size distribution, cumulative distribution, polymorphism (shape, crystal structure), aspect ratio, porosity, solubility, wettability, sheet gloss, opacity, smoothness, print show-through, and IGT surface strength. While two dosing tanks, two aging mixing vessels and two separator systems are shown and described, the present invention is not limited in this regard, as more or less than two dosing tanks, two aging mixing vessels and two separator systems may be employed.

[0056] In some embodiments, the system 100 includes a control unit that includes non-transitory computer readable storage medium 70 with computer-executable instructions 71 configured to instruct the selectively controlling of the chemical and physical properties and residence time of the substances flowing through the treatment system 456.

[0057] In some embodiments, the system 100 includes a non-transitory computer-readable storage medium 70 storing computer-executable instructions 71 that enable automatic or semiautomatic monitoring and control of various chemical and physical properties of substances flowing through the treatment system 456. For example, one or more pressure, temperature, pH, and conductivity sensors can provide real-time data to a controller or processor that executes the instructions 71. The controller then adjusts operating parameters — such as flow rates, mixing speeds, chemical dosing levels, and residence times — through feedback loops, actuators, and motors to maintain desired process conditions. This coordinated approach helps ensure consistent product quality, reaction efficiency, and system stability over a wide range of operating scenarios.

[0058] As shown in FIG. 1, the dosing tanks 4A, 4B are located downstream of and in fluid communication with the chemical absorption apparatus 3. The dosing tanks 4A, 4B are configured to receive the aqueous solution 3X from the chemical absorption apparatus 3 and to treat the aqueous solution 3X to create a treated aqueous solution 4X. The aging mixing vessel systems 5A, 5B are located downstream of and in fluid communication with the dosing tanks 4A, 4B. The aging mixing vessel systems 5A, 5B are configured to: (a) receive the brine 2D from the brine supply system 2; (b) receive the treated aqueous solution 4X from one or both of the dosing tanks 4A, 4B; (c) create a slurry 5X therein, and (d) discharge the slurry 5X therefrom. Each of the aging mixing vessel systems 5A, 5B includes an agitator 5K. In particular, each of the aging mixing vessel systems 5A, 5B are located downstream of and in selective fluid communication with the evaporator 2A, the reverse osmosis system 2B, the heating the industrial waste brine source 2C and / or the geological brine source 2C’, via suitable valve arrangements and controlled by valve actuators and the control unit to supply the brine 2D from one or more of the evaporator 2A, the reverse osmosis system 2B, the industrial waste brine source 2C and / or the geological brine source 2C’, to either or both of the aging mixing vessel systems 5 A, 5B where the brine 2D is mixed with the treated aqueous solution 4X from the dosing tanks 4A, 4B.

[0059] In some embodiments, the chemical absorption apparatus 3, includes, for example, packed columns, tray columns, spray columns, bubble columns and venturi scrubber.

[0060] In some embodiments, the treated aqueous solution 4X discharged from the chemical absorption apparatus 3 includes sodium carbonates (JSfeCCE), sodium bicarbonates (NaHCCh), and byproducts.

[0061] In some embodiments, the slurry 5X discharged from the aging mixing vessel systems 5 A, 5B contains calcium carbonate and / or magnesium carbonate, as the main component forms.

[0062] As shown in FIG. 1, the separator systems 6A, 6B (e.g., centrifuges) are located downstream of and in fluid communication with the mixing vessel systems 5A, 5B. The separator systems 6A, 6B are configured to receive the slurry 5X from the aging mixing vessel systems 5 A, 5B. The separator systems 6A, 6B are configured to separate the brine 2D from carbonate minerals 7X and discharge the carbonate minerals 7X and recovered brine (i.e., a concentrated aqueous solution of sodium chloride NaCl) in separate streams. In some embodiments, the separator systems 6A, 6B are arranged in a series configuration.

[0063] As shown in FIG. 1, the system 100 includes a recycle line 10R configured to transport the recovered brine 10A from the separator systems 6 A, 6B back to the alkali producing system 1, for producing sodium hydroxide. The recycle line 10R is shown with an optional a pretreatment and conditioning system F4 positioned therein. In some embodiments, the recycle line 10R discharges into a tank 10T which has a recycle line 10B that is in fluid communication with the alkali producing system 1 via return lines. In particular, the recycle line 10B selectively supplies recovered brine 10A to each of the chlor-alkali process 1A, the electrochemical activation system (EC A) IB, the membrane-free electrolysis system 1C, the causticization process ID, the lime soda process IE, the mineral extraction process IF, and the alkali extraction unit 1G via suitable valves, actuators and conduit arrangements which are controlled by the control unit. An optional pre-treatment and conditioning system F5 is shown, for example, located in the recycle line 10B.

[0064] In some embodiments, the carbon dioxide source 50 is a fossil-fueled power plant (coal, oil, and natural gas), combined heat and power (CHP) plants, gas turbine CHP plants, gas engine CHP plants, biofuel engine CHP plants, combined cycle power plants adapted for CHP, fuel cell CHP plants, steam turbine CHP plants, biogas power plants (including biogas CHP engines), fixed dome / gasholder biogas plants, floating dome design biogas plants, natural gas engines and turbines, cement production facilities, steel and iron production facilities, aluminum production plants, glass manufacturing processes, ceramic production processes, refineries and petrochemical plants, ammonia production plants, lime and quicklime production facilities, paper and pulp mills, distilleries and breweries, landfills and composting facilities, wastewater treatment plants, food processing plants, carbonated beverage production facilities, residential and commercial heating systems, small-scale diesel or gasoline generators, maritime diesel engines, aviation (jet engines), heavy-duty vehicles (trucks, buses), agricultural activities (fertilizer production and machinery), livestock farming (CO2 from methane decomposition), mining operations, construction sites.

[0065] In some embodiments, the chemical absorption apparatus 3 is configured to react the carbon dioxide with the sodium hydroxide.

[0066] In some embodiments, the carbonate is sodium carbonate (Na2CO3). In some embodiments, the brine supply system 2 includes an evaporator 2A, a reverse osmosis system 2B, an industrial waste brine source 2C and / or a geological brine source 2C’. The evaporator 2A and the reverse osmosis system 2B is supplied with the seawater 2W from a seawater source W. An optional pre-treatment and conditioning system Fl, F2, F3 is shown, for example, in a supply line to evaporator 2A, the reverse osmosis system 2B, the industrial waste brine source 2C and the geological brine source 2C’. The reverse osmosis system 2B is configured to produce the brine 2D and water (e.g., potable water) 2E therefrom. In some embodiments, industrial waste brine source 2C and the geological brine source 2C are in fluid communication with the evaporator 2A and the reverse osmosis system 2B, via respective supply lines 2XE and 2XR. In some embodiments, the industrial waste brine source 2C and the geological brine source 2C’ and the brines provided therefrom are concentrated via the evaporator 2A and / or the reverse osmosis system 2B.

[0067] In some embodiments, the alkali producing system 1 includes a chlor-alkali process 1A (e.g., electrolysis), an electro chemical activation system IB, a membrane-free electrolysis system 1C, a causticization process ID using sodium carbonate and calcium hydroxide, a lime soda process IE, a mineral extraction process comprising trona or alkali-containing minerals IF, and an alkali extraction unit 1G.

[0068] In some embodiments, the aqueous alkali 1H is provided by electrolysis of sodium chloride NaCl brines, electrolysis including but not limited to a mercury cell method, diaphragm method, membrane method and membrane-free method. In some embodiments, the alkali extraction unit 1G involves alkali leaching of waste materials including but not limited to biomass ash, biomass fly ash, refuse derived fuel fly ash, municipal solid waste incineration, mine tailings, mine gangue, non-ferrous slag, blast furnace slag, cement dust, coal ash, industrial waste clinker, stamp sand, and galvanic sewage sludge. In some embodiments, the aqueous alkali 1H is provided via trona mixed with an aqueous lime solution.

[0069] A power supply 40 is electrically connected to electricity consuming components of the alkali producing system 1 via an electrical bus 40B (shown in dashed lines). For example, power supply 40 is electrically connected the chlor-alkali process 1A, the electro chemical activation system IB, and the membrane-free electrolysis system 1C. The power supply 40 is a renewable energy source or other suitable electrical power supply. The renewable energy source is a solar powered photo-voltaic system, a wind energy system, a fuel cell system and / or a biomass fueled power plant. In some embodiments. The alkali producing system 1 is supplied with seawater 2W. Optionally a pre-treatment and conditioning system Fl, F2 is provided in a supply line for the seawater 2W. Optionally a pre-treatment and conditioning system F3 is provided in a supply line for the industrial waste brine source 2C and the geological brine source 2C’.

[0070] The pre-treatment and conditioning systems (Fl, F2, F3, F4, F5 and / or F6) include one or more of an intake screen, a sand filter, a cartridge filter, a bag filter, a ultrafiltration unit, a chlorination system, a dichlorination system, a pH adjustment system, a hydrocyclone, a softening system, a micron filter, a de-gasifier system, an ozonation system, a UV sterilizer, a chemical dosing system, and additional concentrator units. The respective applications of the pre-treatment and conditioning systems (Fl, F2, F3, F4, F5 and / or F6) can be the same or different ones of the intake screen, the sand filter, the cartridge filter, the bag filter, the ultrafiltration unit, the chlorination system, the dichlorination system, the pH adjustment system, the hydrocyclone, the softening system, the micron filter, the de-gasifier system, the ozonation system, the UV sterilizer, the chemical dosing system, and the additional concentrator units.

[0071] As shown in FIG. 1, the system 100 includes two dryers 7A, 7B located downstream of the separator system 6A, 6B. The dryers 7A, 7B are configured to receive and dry the carbonate minerals. A holding vessel 8(a), 8(b) is located downstream of each of the dryers 7A, 7B and in communication with the at least one dryer 7A, 7B via respective conduits 7Y.

[0072] While two dryers 7A, 7B are shown and described, the present invention is not limited in this regard as more or less than two dryers may be employed.

[0073] In some embodiments, a first surface modification supply is 7C provided into the conduit 7Y, the first surface modification supply 7C being configured to provide a first surface modification substance for application on the carbonate minerals; and a second surface modification supply 7C’ is provided into the holding vessel 8A, 8B the second surface modification supply 7C being configured to provide a second surface modification substance for application on the carbonate minerals. The first surface modification substance and the second surface modification substance are configured to increase reactivity, affect surface hardness, affect oil absorption resistance, affect hydrophilic properties, affect lipophilic properties, improve the affinity with organic substances such as resin, improve stability, improve the dispersion and affinity in polymer matrices such as polyolefins, of the carbonate minerals. The surface modification supply includes, but is not limited to, surfactants, coupling agents, polymer modifiers. In some embodiments the surface modification includes treatment with (1) fatty acids (e g., stearic acid, to create a hydrophobic layer and improve dispersion), (2) Silane coupling agents (for polymer compatibility), (3) polymer coating, (4) metal coating, and (5) treatment with phosphate, aluminate, silicate, or barium salts, for acid-resistance.

[0074] In some embodiments, the carbonate minerals include calcium carbonate and / or magnesium carbonate.

[0075] As shown in FIG. 1, the system 100 includes a control unit including a non-transitory computer readable storage medium (70) comprising computer-executable instructions (71) configured to instruct the selectively controlling of the chemical and physical properties and residence time of the substances flowing through the treatment system (456).

[0076] As shown in FIG. 2, the system 100 is disposed in an interior area 62 of a container 60.

[0077] As shown in FIG. 2, a kit 1000 for capturing carbon dioxide, converting the carbon dioxide to carbonate minerals and recycling solvents and heat for reuse, includes the kit a container 60 (e.g., a housing, a shipping container for easy transport and hooking. The entire system 100 is disposed in one or more shipping containers) that has an exterior shell 61 and an interior area 62, an electrical power connection 63 penetrates the exterior shell 61, brine supply connection 64, 67 penetrate the exterior shell 61 and supply a header 65. A carbon dioxide connection 66 penetrates the exterior shell 61. The interior area 62 of the container 60 includes (a) an alkali producing system 1 configured for producing an aqueous alkali 1H, the alkali producing system is in electrical communication with the electrical power connection 63 and the seawater connection 64; and (b) a chemical absorption apparatus 3 is in communication with the alkali producing system 1 and carbon dioxide connection 66, the chemical absorption apparatus 3 is configured to react carbon dioxide with the aqueous alkali 1H thereby chemically absorbing at least a portion of the carbon dioxide from inside the chemical absorption apparatus 3 into an aqueous solution 3X comprising a carbonate and water; (c) a treatment system 456, includes the two dosing tanks 4A, 4B, the aging mixing vessel system 5A, 5B and the separator system 6A, 6B. The treatment system 456 is configured to selectively control chemical and physical properties and residence time of substances flowing therethrough and is in fluid communication with the at brine connections 64, 67. The dosing tanks 4A, 4B are located downstream of and in communication with the chemical absorption apparatus 3. The dosing tanks 4A, 4B are configured to receive the aqueous solution 3X from the chemical absorption apparatus 3 and to treat the aqueous solution 3X to create a treated aqueous solution 4X. The aging mixing vessel system 5 A, 5B is located downstream of the dosing tanks 4A, 4B. The aging mixing vessel system 5A, 5B is configured to (1) receive the brine from the at least one brine connection 64, 67, (2) receive the treated aqueous solution 4X from the at least one dosing tank 4A, 4B, (3) create a slurry 5X therein, and (4) discharge the slurry 5X therefrom. The separator system 6A, 6B is located downstream of the mixing vessel system 5A, 5B and is configured to receive the slurry 5X from the aging mixing vessel system 5A, 5B. The separator system 6A, 6B is configured to separate the brine 2D from carbonate minerals 7X and discharge the carbonate minerals 7X and recovered brine 10A in separate streams 10R and 68, 68’ (also see 7X in FIG. 1). As shown in FIG. 2, the carbonate minerals 7X are collected in the interior area 62 via line 68’ or are transported out of the container at a penetration 68. The kit 1000 includes a recycle line 10R configured to transport the recovered brine 10A from the separator system 6A, 6B back to the alkali producing system 1, for producing the sodium hydroxide.

[0078] There is disclosed herein a circular method of mineralizing carbon dioxide (CO2). The circular method of mineralizing carbon dioxide includes capturing carbon dioxide from an emissions source; treating the carbon dioxide with sodium hydroxide and a brine; separating purified brine and carbonate minerals; discharging the carbonate minerals and purified brine in separate streams; and recycling the purified brine for use in the mineralizing carbon dioxide.

[0079] As shown in FIG. l,the recovered brine 10A is optionally transported via line 10RR and line 1 OK to a discharge point in a line between the brine supply system 2 and the aging mixing vessel system 5A, 5B. In some embodiments, the recovered brine 10A is optionally transported via line 10RR and line 10M to the evaporator 2A. In some embodiments, the recovered brine 10A is optionally transported via line 10B, line 10BB and line 10W to be returned to the seawater source W for conservation purposes. In some embodiments, the recovered brine 10A is optionally transported via line 1 OB, line 10BB and line 10Q to the evaporator 2A. In some embodiments, the recovered brine 10A is optionally transported via linelOB, line 10BB and line 10L to a discharge point in a line between the brine supply system 2 and the aging mixing vessel system 5 A, 5B. In some embodiments, the recovered brine 10A is optionally transported to the geological brine source 2C’.

[0080] In some embodiments, chlorine is recovered and recycled from the chlor-alkali process. In some embodiments, the amount of recovered brine 10B is sufficient to offset at least a portion of the amount of brine provided by the seawater 2W supplied by a seawater source W to the alkali producing system 1. In some embodiments, the amount of recovered brine 10B is sufficient to offset at least a portion of the amount of brine provided by the seawater 2W supplied by the seawater source W to the aging and mixing vessel system 5 A, 5B. In some embodiments, the recovered brine 10B is selectively transported to the evaporator 2A. The recovered brine 10B has largely been depleted of Ca or Mg and therefore the recovered brine 10B is, in some embodiments, recycled back to the aging and mixing vessel system 5 A, 5B for dilution and as a method to conserve water. In some embodiments, there are two separate runs, rather than a direct path from the aging and mixing vessel system 5A (once brine has been depleted of Ca) and transported to the aging and mixing vessel system 5B (to extract Mg). The recovered brine 10B which has been depleted of Ca is treated, and then fed to the aging and mixing vessel system 5B for the Mg cycle.

[0081] In some embodiments, system 100 for capturing carbon dioxide includes a water purifying and recycling system 90 that connects into the recycle line 10B or the recycle line 10R to supply the recovered brine 10A to the water purifying and recycling system 90, which discharges purified water therefrom via a water discharge line 2EE, for conservation (e.g., to avoid depletion of the water table) and recycling of the water discharged therefrom. In some embodiments, the water discharge line 2EE provides the purified water to the alkali producing system 1 and / or the brine supply system for dilution of the brine. In some embodiments, the water discharge line 2EE provides the purified water to the separator system 6A, 6B for use in a washing of the slurry 5X. In some embodiments, the water purifying and recycling system 90 is in fluid communication with the gas cooling device 9 for recovery of water from the condensation of humidity in the carbon dioxide rich gas stream provided by the carbon dioxide source 50. In some embodiments, water is recovered from wastewater in from the washing process.

[0082] The disclosure is not limited to the foregoing illustrative examples and the examples should be considered in all respects as illustrative and not restrictive, reference being made to the appended claims, rather than to the foregoing examples, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced. In the specification, the singular forms also include the plural forms, unless the context clearly dictates otherwise. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. In the case of conflict, the present specification will control.

Claims

What is claimed is:

1. A system (100) for capturing carbon dioxide, converting the carbon dioxide to carbonate minerals and recycling solvents, water and heat for reuse, the system (100) comprising: an alkali producing system (1) configured for producing an aqueous alkali (1H); a carbon dioxide source (50); a chemical absorption apparatus (3) in communication with the alkali producing system (1) and the carbon dioxide source (50), the chemical absorption apparatus (3) being configured to react carbon dioxide with the aqueous alkali (1H) thereby chemically absorbing at least a portion of the carbon dioxide from inside the chemical absorption apparatus (3) into an aqueous solution (3X); a brine supply system (2) configured to discharge brine (2D) therefrom; a treatment system (456), comprising at least one dosing tank (4A, 4B), at least one aging mixing vessel system (5 A, 5B) and a separator system (6A, 6B), the treatment system (456) being configured to selectively control chemical and physical properties and the residence time of substances flowing therethrough; the at least one dosing tank (4A, 4B) being located downstream of and in communication with the chemical absorption apparatus (3), the at least one dosing tank (4A, 4B) being configured to receive the aqueous solution (3X) from the chemical absorption apparatus (3) and to treat the aqueous solution (3X) to create a treated aqueous solution (4X); the at least one aging mixing vessel system (5 A, 5B) located downstream of the at least one dosing tank (4A, 4B), the at least one aging mixing vessel system (5 A, 5B) being configured to:(a) receive the brine (2D) from the brine supply system (2),(b) receive the treated aqueous solution (4X) from the at least one dosing tank (4A, 4B),(c) create a slurry (5X) therein, and(d) discharge the slurry (5X) therefrom; the separator system (6A, 6B) being located downstream of the at least one mixing vessel system (5 A, 5B), the separator system (6 A, 6B) being configured to receive the slurry (5X) from the at least one aging mixing vessel system (5 A, 5B), the separator system (6A, 6B) beingconfigured to separate the brine (2D) from carbonate minerals (7X) and discharge the carbonate minerals (7X) and recovered brine (10A) in separate streams; and a recycle line (10R, 10B) configured to transport the recovered brine (10A) from the separator system (6A, 6B) back to the alkali producing system (1), for producing the aqueous alkali.

2. The system (100) of claim 1, wherein the alkali producing system (1) is configured to produce sodium hydroxide.

3. The system (100) of claim 1, wherein the carbon dioxide source (50) is at least one of fossil-fueled power plants, combined heat and power (CHP) plants, gas turbine CHP plants, gas engine CHP plants, biofuel engine CHP plants, combined cycle power plants adapted for CHP, fuel cell CHP plants, steam turbine CHP plants, biogas power plants, fixed dome / gasholder biogas plants, floating dome design biogas plants, natural gas engines and turbines, cement production facilities, steel and iron production facilities, aluminum production plants, glass manufacturing processes, ceramic production processes, refineries and petrochemical plants, ammonia production plants, lime and quicklime production facilities, paper and pulp mills, distilleries and breweries, landfills and composting facilities, wastewater treatment plants, food processing plants, carbonated beverage production facilities, residential and commercial heating systems, small-scale diesel or gasoline generators, maritime diesel engines, aviation engines, heavy-duty land vehicles, agricultural activities, livestock farming, mining operations, and construction sites.

4. The system (100) of claim 2, wherein the chemical absorption apparatus (3) is configured to react the carbon dioxide with the sodium hydroxide.

5. The system (100) of claim 1, wherein the brine supply system (2) comprises at least one of an evaporator (2A), a reverse osmosis system (2B), an industrial waste brine source (2C) and geological brine source (2C’).

6. The system (100) of claim 1, wherein the brine supply system (2) comprises at least one of an industrial waste brine source (2C) and geological brine source (2C’) and the brines provided therefrom are concentrated via at least one of an evaporator (2A) and a reverse osmosis system (2B).

7. The system (100) of claim 5, wherein at least one of the at least one the evaporator (2A) and the reverse osmosis system (2B) is supplied with the seawater (2W).

8. The system (100) of claim 1, further comprising a pre-treatment and conditioning system (Fl, F2, F3) in a supply line to at least one of the evaporator (2A), the reverse osmosis system (2B), the industrial waste brine source (2C) and the geological brine source (2C’).

9. The system (100) of claim 8, wherein the pre-treatment and conditioning system (Fl, F2, F3) comprises at least one of an intake screen, a sand filter, a cartridge filter, a bag filter, a ultrafiltration unit, a chlorination system, a di chlorination system, a pH adjustment system, a hydrocyclone, a softening system, a micron filter, a de-gasifier system, an ozonation system, a UV sterilizer, a chemical dosing system, and additional concentrator units.

10. The system (100) of claim 1, wherein the brine supply system (2) comprises a reverse osmosis system (2B) which is configured to produce the brine (2D) and water (2E) therefrom.

11. The system (100) of claim 1, wherein the alkali producing system (1) comprises at least one of a chlor-alkali process (1 A), an electro chemical activation system (IB), and a membrane- free electrolysis system ( 1 C).

12. The system (100) of claim 11, further comprising a power supply (40) to at least one of the chlor-alkali process (1A), the electro chemical activation system (IB), and the membrane- free electrolysis system (1 C), wherein the power supply (40) is preferably a renewable energy source.

13. The system (100) of claim 1, wherein the alkali producing system (1) comprises at least one of a causticization process using sodium carbonate and calcium hydroxide (ID), a lime soda process (IE), and a mineral extraction process comprising trona or alkali-containing minerals (IF), and an alkali extraction unit (1G).

14. The system (100) of claim 12, wherein the renewable energy source is at least one of a solar powered photo-voltaic system, a wind energy system, a fuel cell system powered by green hydrogen or renewable fuels, solar thermal systems, hydropower systems, geothermal energy systems, renewable hydrogen systems, a biomass or biogas fueled power plant, a waste-to- energy system, a waste-heat-recovery system and a hybrid renewable energy system.

15. The system (100) of claim 1, wherein the alkali producing system (1) is supplied with seawater (2W).

16. The system (100) of claim 15, further comprising a pre-treatment and conditioning system (F6) comprising at least one of an intake screen, a sand filter, a cartridge or bag filter, a ultrafiltration unit, a chlorination system, a dichlorination system, a pH adjustment system, a hydrocyclone, a softening system, a micron filter, a de-gasifier system, an ozonation system, a UV sterilizer, a chemical dosing system, and additional concentrator units, in a supply line for the seawater (2W) provided to the alkali producing system (1).

17. The system (100) of claim 1, wherein the chemical and physical properties comprise at least one of purity, chemical composition, concentration, density, and states of matter.

18. The system (100) of claim 1, wherein the chemical absorption apparatus (3) comprises at least one of packed columns, tray columns, spray columns, bubble columns, venturi scrubbers, mini or microreaction technology.

19. The system (100) of claim 1, wherein the treated aqueous solution (4X) discharged from the chemical absorption apparatus (3) comprises sodium carbonates (Na2CO ), sodium bicarbonates (NaHCCh), and byproducts.

20. The system (100) of claim 1, wherein the slurry (5X) discharged from the at least one aging mixing vessel system (5 A, 5B) comprises at least one of calcium carbonate and magnesium carbonate.

21. The system (100) of claim 1, further comprising at least one dryer (7 A, 7B) located downstream of the separator system (6A, 6B), the at least one dryer (7 A, 7B) being configured to receive and dry the carbonate minerals.

22. The system (100) of claim 1, wherein the separator system (6A, 6B) comprises at least one of a mechanical separation unit, preferably a filter, a hydrocyclone, a decanter, a centrifuge and fluid-solid separation equipment that is combined with a washing step.

23. The system (100) of claim 1, wherein the separator system (6 A, 6B) comprises two of the mechanical separation units arranged in a series configuration.

24. The system (100) of claim 21, further comprising a holding vessel (8A, 8B) located downstream of the at least one dryer (7 A, 7B) and in communication with the at least one dryer (7 A, 7B) via a conduit (7Y).

25. The system (100) of claim 23, further comprising at least one of:(a) a first surface modification supply (7C) provided into the conduit (7Y), the first surface modification supply (7C) being configured to provide a first surface modification substance for application on the carbonate minerals; and(b) a second surface modification supply (7C’) provided into the holding vessel (8A, 8B) the second surface modification supply (7C) being configured to provide a second surface modification substance for application on the carbonate minerals.

26. The system (100) of claim 25, wherein at least one of the first surface modification substance and the second surface modification substance is configured to increase reactivity of the carbonate minerals.

27. The system (100) of claim 1, wherein the carbonate minerals comprise at least one of calcium carbonate and magnesium carbonate.

28. The system (100) of claim 1, wherein the at least one aging mixing vessel system (5A, 5B) comprises an agitator (5K).

29. The system (100) of claim 1, wherein the recycle line (10R) comprises a pre-treatment and conditioning system (F4) comprising at least one of an intake screen, a sand filter, a cartridge or bag filter, a ultrafiltration unit, a chlorination system, a dichlorination system, a pH adjustment system, a hydrocyclone, a softening system, a micron filter, a de-gasifier system, an ozonation system, a UV sterilizer, a chemical dosing system, and additional concentrator units (F4) therein.

30. The system (100) of claim 1, wherein the recycle line (10R) discharges into a tank (10T) which has another recycle line (10B) that is in communication with the alkali producing system (1).

31. The system (100) of claim 30, further comprising a pre-treatment and conditioning system (F5) comprising at least one of an intake screen, a sand filter, a cartridge or bag filter, a ultrafiltration unit, a chlorination system, a dichlorination system, a pH adjustment system, a hydrocyclone, a softening system, a micron filter, a de-gasifier system, an ozonation system, a UV sterilizer, a chemical dosing system, and additional concentrator unit located in the recycle line (10B).

32. The system (100) of claim 1, further comprising a gas cooling device (9) located downstream of the carbon dioxide source (50) and upstream of the chemical absorption apparatus (3), the gas cooling device (9) being configured for reducing temperature of the carbon dioxide provided by the carbon dioxide source (50).

33. The system (100) of claim 32, wherein the gas cooling device (9) is in heat transfer communication with at least one of a waste-heat-recovery system, the brine supply system (2), the dryers (2A, 2B), and the holding vessels (8A, 8B), for transferring heat thereto.

34. The system (100) of claim 1, further comprising a non-transitory computer readable storage medium (70) comprising computer-executable instructions (71) configured to instruct the selectively controlling of the chemical and physical properties of the substances flowing through the treatment system (456).

35. A container (1000) comprising the system (100) of any of claims 1 to 34.

36. A circular method of mineralizing carbon dioxide comprising: capturing carbon dioxide from a source; treating the carbon dioxide with sodium hydroxide and a brine; separating purified brine and carbonate minerals; discharging the carbonate minerals and purified brine in separate streams; and recycling the purified brine for use in the mineralizing carbon dioxide.

37. A kit (1000) for capturing carbon dioxide, converting the carbon dioxide to carbonate minerals and recycling solvents and heat for reuse, the kit (1000) comprising: a container (60) having an exterior shell (61) and an interior area (62), an electrical power connection (63) penetrating the exterior shell (61), at least one brine supply connection (64, 67) penetrating the exterior shell (61), a carbon dioxide connection (66) penetrating the exterior shell (61); the interior area (62) of the container (60) comprising:(a) an alkali producing system (1) configured for producing an aqueous alkali (1H), the alkali producing system being in electrical communication with the electrical power connection (63) and the seawater connection (64);(b) a chemical absorption apparatus (3) in communication with the alkali producing system (1) and carbon dioxide connection (66), the chemical absorption apparatus (3) being configured to react carbon dioxide with the aqueous alkali (1H) thereby chemically absorbing at least a portion of the carbon dioxide from inside the chemical absorption apparatus (3) into an aqueous solution (3x) comprising a carbonate and water;(c) a treatment system (456), comprising at least one dosing tank (4A, 4B), at least one aging mixing vessel system (5 A, 5B) and a separator system (6A, 6B), the treatment system (456) being configured to selectively control chemical and physical properties and residence time of substances flowing therethrough and being in fluid communication with the at least one brine connection (64, 67);(i) the at least one dosing tank (4A, 4B) being located downstream of and in communication with the chemical absorption apparatus (3), the at least one dosing tank (4A, 4B) being configured to receive the aqueous solution (3x) from the chemical absorption apparatus (3) and to treat the aqueous solution (3x) to create a treated aqueous solution (4x);(ii) the at least one aging mixing vessel system (5 A, 5B) located downstream of the at least one dosing tank (4A, 4B), the at least one aging mixing vessel system (5 A, 5B) being configured to:(1) receive the brine from the at least one brine connection (64,67),(2) receive the treated aqueous solution (4x) from the at least one dosing tank (4A, 4B),(3) create a slurry (5x) therein, and(4) discharge the slurry (5x) therefrom;(iii) the separator system (6A, 6B) being located downstream of the at least one mixing vessel system (5 A, 5B), the separator system (6A, 6B) being configured to receive the slurry (5x) from the at least one aging mixing vessel system (5 A, 5B), the separator system (6A, 6B) being configured to separate the brine (2(d)) from carbonate minerals (7x) and discharge the carbonate minerals (7x) and recovered brine (10a) in separate streams; and(d) a recycle line (10R) configured to transport the recovered brine (10a) from the separator system (6A, 6B) back to the alkali producing system (1), for producing aqueous alkali.

38. The system (100) of claim 1, further comprising a water purifying and recycling system (90) that connects into the recycle line (10B, 10R) to supply the recovered brine (10A) to the water purifying and recycling system (90), which discharges purified water therefrom via a water discharge line (2EE).

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