Ammonia organic acid salt mediated carbon sequestration material production methods and systems for practicing the same

Abstract

Ammonia organic acid salt mediated carbon dioxide (CO2) sequestering methods and systems are provided. Aspects of the methods include contacting a gaseous source of CO2 and an aqueous capture ammonia to produce a CO2 sequestering carbonate product and an aqueous ammonium organic acid salt, and then subjecting the aqueous ammonium organic acid salt to dialysis regeneration to produce a regenerated aqueous ammonia capture liquid. Also provided are systems configured for carrying out the methods.

Description

[0001]Atty Docket No.: BLUE-061WO AMMONIA ORGANIC ACID SALT MEDIATED CARBON SEQUESTRATION MATERIAL PRODUCTION METHODS AND SYSTEMS FORPRACTICING THESAMECROSS-REFERENCETORELATEDAPPLICATIONSPursuant to 35 U.S.C. §119(e), this application claims priority to the filing date of United States Provisional Patent Application Serial No. 63 / 694,368 filed September 13, 2024, and to United States Provisional Patent Application Serial No. 63 / 724,817 filed November 25, 2024, the disclosures of which applications are herein incorporated by reference. INTRODUCTIONCarbon dioxide (CO2) is a naturally occurring chemical compound that is present in Earth's atmosphere as a gas. Sources of atmospheric CO2 are varied, and include humans and other living organisms that produce CO2 in the process of respiration, as well as other naturally occurring sources, such as volcanoes, hot springs, and geysers. Additional major sources of atmospheric CO2 include industrial plants. Many types of industrial plants (including cement plants, refineries, steel mills and power plants) combust various carbon-based fuels, such as fossil fuels and syngases. Fossil fuels that are employed include coal, natural gas, oil, petroleum coke and biofuels. Fuels are also derived from tar sands, oil shale, coal liquids, and coal gasification and biofuels that are made via syngas. The environmental effects of CO2 are of significant interest. CO2 is commonly viewed as a greenhouse gas. The phrase "global warming" is used to refer to observed and continuing rise in the average temperature of Earth's atmosphere and oceans since the late 19th century. Because human activities since the industrial revolution have rapidly increased concentrations of atmospheric CO2, anthropogenic CO2has been implicated in global warming and climate change, as well as increasing oceanic bicarbonate concentration. Ocean uptake of fossil fuel CO2is now proceeding at about 1 million metric tons of CO2per hour. Since the early 20th century, the Earth's mean surface temperature has increased by about 0.8 °C (1.4 °F), with about two-thirds of the increase occurring since 1980. The effects of global warming on the environment and for human life are numerous and varied. Some effects of recent climate change may already be occurring. Atty Docket No.: BLUE-061WO Rising sea levels, glacier retreat, Arctic shrinkage, and altered patterns of agriculture are cited as direct consequences, but predictions for secondary and regional effects include extreme weather events, an expansion of tropical diseases, changes in the timing of seasonal patterns in ecosystems, and drastic economic impact. Projected climate changes due to global warming have the potential to lead to future large-scale and possibly irreversible effects at continental and global scales. The likelihood, magnitude, and timing is uncertain and controversial, but some examples of projected climate changes include significant slowing of the ocean circulation that transports warm water to the North Atlantic, large reductions in the Greenland and Western Antarctic Ice Sheets, accelerated global warming due to carbon cycle feedbacks in the terrestrial biosphere, and releases of terrestrial carbon from permafrost regions and methane from hydrates in coastal sediments. While a matter of scientific debate, it is believed that excess atmospheric CO2 is a significant contributing factor to global warming. Since the beginning of the Industrial Revolution, the concentration of CO2 has increased by about 100 parts-per-million (ppm) (i.e., from 280 ppm to 380 ppm), and was recently observed to reach an average daily value of over 400 ppm. As such, there is great interest in the sequestration of CO2, particularly in a manner sufficient to at least ameliorate the ever-increasing amounts of anthropogenic CO2 that is present in the atmosphere. Concerns over anthropogenic climate change and ocean acidification, have fueled an urgency to discover scalable, cost effective, methods of carbon capture and sequestration (CCS). Typically, methods of CCS separate pure CO2 from complex flue streams, compress the purified CO2, and finally inject it into underground saline reservoirs for geologic sequestration. These multiple steps are very energy and capital intensive. Carbonate mineralization is another method to sequester large amounts of CO2, in gigaton (Gt, i.e., 1,000,000,000 tons) volumes, sustainably. SUMMARY Ammonia organic acid salt mediated carbon dioxide (CO2) sequestering methods and systems are provided. Aspects of the methods include contacting a gaseous source of CO2and an aqueous capture ammonia to produce a CO2sequestering carbonate product and an aqueous ammonium organic acid salt, and then subjecting the aqueous ammonium organic acid salt to dialysis regeneration to produce a regenerated aqueous Atty Docket No.: BLUE-061WO ammonia capture liquid. Also provided are systems configured for carrying out the methods. BRIEF DESCRIPTION OF THE FIGURES FIG.1: Provides a schematic of a one-step membrane mediated ammonia regeneration protocol according to an embodiment of the invention. FIG.2: Provides a schematic of a two-step membrane mediated ammonia regeneration protocol according to an embodiment of the invention. FIG.3: A model that incorporates alkalinity regeneration into CaCO3 production. FIG.4: Mechanically pressing CaCO3 constituents into a material. DETAILEDDESCRIPTIONAmmonia organic acid salt mediated carbon dioxide (CO2) sequestering methods and systems are provided. Aspects of the methods include contacting a gaseous source of CO2 and an aqueous capture ammonia to produce a CO2 sequestering carbonate product and an aqueous ammonium organic acid salt, and then subjecting the aqueous ammonium organic acid salt to dialysis regeneration to produce a regenerated aqueous ammonia capture liquid. Also provided are systems configured for carrying out the methods. Before the present invention is described in greater detail, it is to be understood that this invention is not limited to particular embodiments described, as such may, of course, vary. It is also to be understood that the terminology used herein is for the purpose of describing particular embodiments only, and is not intended to be limiting, since the scope of the present invention will be limited only by the appended claims. Where a range of values is provided, it is understood that each intervening value, to the tenth of the unit of the lower limit unless the context clearly dictates otherwise, between the upper and lower limit of that range and any other stated or intervening value in that stated range, is encompassed within the invention. The upper and lower limits of these smaller ranges may independently be included in the smaller ranges and are also encompassed within the invention, subject to any specifically excluded limit in the stated range. Where the stated range includes one or both of the limits, ranges excluding either or both of those included limits are also included in the invention. Atty Docket No.: BLUE-061WO Certain ranges are presented herein with numerical values being preceded by the term "about." The term "about" is used herein to provide literal support for the exact number that it precedes, as well as a number that is near to or approximately the number that the term precedes. In determining whether a number is near to or approximately a specifically recited number, the near or approximating unrecited number may be a number which, in the context in which it is presented, provides the substantial equivalent of the specifically recited number. 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. Although any methods and materials similar or equivalent to those described herein can also be used in the practice or testing of the present invention, representative illustrative methods and materials are now described. All publications and patents cited in this specification are herein incorporated by reference as if each individual publication or patent were specifically and individually indicated to be incorporated by reference and are incorporated herein by reference to disclose and describe the methods and / or materials in connection with which the publications are cited. The citation of any publication is for its disclosure prior to the filing date and should not be construed as an admission that the present invention is not entitled to antedate such publication by virtue of prior invention. Further, the dates of publication provided may be different from the actual publication dates which may need to be independently confirmed. It is noted that, as used herein and in the appended claims, the singular forms “a”, “an”, and “the” include plural referents unless the context clearly dictates otherwise. It is further noted that the claims may be drafted to exclude any optional element. As such, this statement is intended to serve as antecedent basis for use of such exclusive terminology as “solely,” “only” and the like in connection with the recitation of claim elements, or use of a “negative” limitation. As will be apparent to those of skill in the art upon reading this disclosure, each of the individual embodiments described and illustrated herein has discrete components and features which may be readily separated from or combined with the features of any of the other several embodiments without departing from the scope or spirit of the present invention. Any recited method can be carried out in the order of events recited or in any other order which is logically possible. Atty Docket No.: BLUE-061WO While the apparatus and method has or will be described for the sake of grammatical fluidity with functional explanations, it is to be expressly understood that the claims, unless expressly formulated under 35 U.S.C. §112, are not to be construed as necessarily limited in any way by the construction of "means" or "steps" limitations, but are to be accorded the full scope of the meaning and equivalents of the definition provided by the claims under the judicial doctrine of equivalents, and in the case where the claims are expressly formulated under 35 U.S.C. §112 are to be accorded full statutory equivalents under 35 U.S.C. §112. METHODS As summarized above, aspects of the invention include methods of using an aqueous ammonia organic acid salt, e.g., ammonia acetate, to produce carbon dioxide (CO2) sequestering material. Accordingly, aspects of the invention include CO2 sequestration processes, i.e., processes (methods, protocols, etc.) that result in CO2 sequestration. By "CO2 sequestration" is meant the removal or segregation of an amount of CO2 from an environment, such as the Earth's atmosphere or a gaseous waste stream produced by an industrial plant, so that some or all of the CO2 is no longer present in the environment from which it has been removed. CO2 sequestering methods of the invention sequester CO2 by producing a solid storage stable CO2 sequestering product from an amount of CO2, such that the CO2 is sequestered. The solid storage stable CO2 sequestering product is a storage stable composition that incorporates an amount of CO2 into a storage stable form, such as an above-ground storage or underwater storage stable form, so that the CO2 is no longer present as, or available to be, a gas in the atmosphere. Sequestering of CO2 according to methods of the invention allows for long-term storage of CO2 in a manner such that CO2 does not become part of the atmosphere. As summarized above, aspects of the methods include: contacting an aqueous ammonia capture liquid with a gaseous source of CO2under conditions sufficient to produce a CO2sequestering carbonate and an aqueous ammonium organic acid salt, e.g., ammonium acetate; and subjecting the aqueous ammonium organic acid salt to dialysis regeneration to produce a regenerated aqueous ammonia capture liquid. Each of these aspects of the methods is now further described in greater detail. CO2Capture Atty Docket No.: BLUE-061WO Embodiments of the methods include contacting an aqueous capture liquid, such as an aqueous capture ammonia, with a gaseous source of CO2(i.e., a CO2containing gas) under conditions sufficient to produce an aqueous carbonate liquid, such as an aqueous ammonium carbonate. The gaseous source of CO2, i.e., the CO2containing gas, may be pure CO2or be combined with one or more other gasses and / or particulate components, depending upon the source, e.g., it may be a multi-component gas (i.e., a multi-component gaseous stream). In certain embodiments, the CO2containing gas is obtained from an industrial plant, e.g., where the CO2containing gas is a waste feed from an industrial plant. Industrial plants from which the CO2containing gas may be obtained, e.g., as a waste feed from the industrial plant, may vary. Industrial plants of interest include, but are not limited to, power plants and industrial product manufacturing plants, such as, but not limited to, chemical and mechanical processing plants, refineries, cement plants, steel plants, etc., as well as other industrial plants that produce CO2 as a byproduct of fuel combustion or other processing step (such as calcination by a cement plant). Waste feeds of interest include gaseous streams that are produced by an industrial plant, for example as a secondary or incidental product, of a process carried out by the industrial plant. Of interest in certain embodiments are waste streams produced by industrial plants that combust fossil fuels, e.g., coal, oil, natural gas, as well as man-made fuel products of naturally occurring organic fuel deposits, such as but not limited to tar sands, heavy oil, oil shale, etc. In certain embodiments, power plants are pulverized coal power plants, supercritical coal power plants, mass burn coal power plants, fluidized bed coal power plants, gas or oil-fired boiler and steam turbine power plants, gas or oil-fired boiler simple cycle gas turbine power plants, and gas or oil-fired boiler combined cycle gas turbine power plants. Of interest in certain embodiments are waste streams produced by power plants that combust syngas, i.e., gas that is produced by the gasification of organic matter, e.g., coal, biomass, etc., where in certain embodiments such plants are integrated gasification combined cycle (IGCC) plants. Of interest in certain embodiments are waste streams produced by Heat Recovery Steam Generator (HRSG) plants. Waste streams of interest also include waste streams produced by cement plants. Cement plants whose waste streams may be employed in methods of the invention include both wet process and dry process plants, which plants may employ shaft kilns or rotary kilns, and may include pre-calciners. Each of these types of industrial plants may burn a single Atty Docket No.: BLUE-061WO fuel, or may burn two or more fuels sequentially or simultaneously. A waste stream of interest is industrial plant exhaust gas, e.g., a flue gas. By "flue gas" is meant a gas that is obtained from the products of combustion from burning a fossil or biomass fuel that are then directed to the smokestack, also known as the flue of an industrial plant. Waste streams produced by cement plants are also suitable for systems and methods of the invention. Cement plant waste streams include waste streams from both wet process and dry process plants, which plants may employ shaft kilns or rotary kilns, and may include pre-calciners. These industrial plants may each burn a single fuel, or may burn two or more fuels sequentially or simultaneously. Other industrial plants such as smelters and refineries are also useful sources of waste streams that include carbon dioxide. Industrial waste gas streams may contain carbon dioxide as the primary non-air derived component, or may, especially in the case of coal-fired power plants, contain additional components (which may be collectively referred to as non-CO2 pollutants) such as nitrogen oxides (NOx), sulfur oxides (SOx), and one or more additional gases. Additional gases and other components may include CO, mercury and other heavy metals, and dust particles (e.g., from calcining and combustion processes). Additional non-CO2 pollutant components in the gas stream may also include halides such as hydrogen chloride and hydrogen fluoride; particulate matter such as fly ash, dusts, and metals including arsenic, beryllium, boron, cadmium, chromium, chromium VI, cobalt, lead, manganese, mercury, molybdenum, selenium, strontium, thallium, and vanadium; and organics such as hydrocarbons, dioxins, and PAH compounds. Suitable gaseous waste streams that may be treated have, in some embodiments, CO2 present in amounts of 200 ppm to 1,000,000 ppm; or 200 ppm to 500,000 ppm; or 200 ppm to 100,000 ppm; or 200 ppm to 10,000; or 200 ppm to 5,000 ppm; or 200 ppm to 2000 ppm; or 200 ppm to 1000 ppm; or 200 to 500 ppm; or 500 ppm to 1,000,000 ppm; or 500 ppm to 500,000 ppm; or 500 ppm to 100,000 ppm; or 500 ppm to 10,000; or 500 ppm to 5,000 ppm; or 500 ppm to 2000 ppm; or 500 ppm to 1000 ppm; or 1000 ppm to 1,000,000 ppm; or 1000 ppm to 500,000 ppm; or 1000 ppm to 100,000 ppm; or 1000 ppm to 10,000; or 1000 ppm to 5,000 ppm; or 1000 ppm to 2000 ppm; or 2000 ppm to 1,000,000 ppm; or 2000 ppm to 500,000 ppm; or 2000 ppm to 100,000 ppm; or 2000 ppm to 10,000; or 2000 ppm to 5,000 ppm; or 2000 ppm to 3000 ppm; or 5000 ppm to 1,000,000 ppm; or 5000 ppm to 500,000 ppm; or 5000 ppm to 100,000 ppm; or 5000 ppm to 10,000; or 10,000 ppm to 1,000,000 ppm; or 10,00 ppm to 500,000 ppm; or Atty Docket No.: BLUE-061WO 10,000 ppm to 100,000 ppm; or 50,000 ppm to 1,000,000 ppm; or 50,000 ppm to 500,000 ppm; or 50,000 ppm to 100,000 ppm; or 100,000 ppm to 1,000,000 ppm; or 100,000 ppm to 500,000 ppm; or 200,000 ppm to 1000 ppm, including 200,000 ppm to 2000 ppm, for example 180,000 ppm to 2000 ppm, or 180,000 ppm to 5000 ppm, also including 180,000 ppm to 10,000 ppm. The waste streams, particularly various waste streams of combustion gas, may include one or more additional non-CO2components, for example only, water, NOx (mononitrogen oxides: NO and NO2), SOx (monosulfur oxides: SO, SO2 and SO3), VOC (volatile organic compounds), heavy metals such as, but not limited to, mercury, and particulate matter (particles of solid or liquid suspended in a gas). Flue gas temperature may also vary. In some embodiments, the temperature of the flue gas comprising CO2 is from 0 ºC to 2000 ºC, or 0 ºC to 1000 ºC, or 0.degree ºC to 500 ºC, or 0 ºC to 100 ºC, or 0 ºC to 50 ºC, or 10 ºC to 2000 ºC, or 10 ºC to 1000 ºC, or 10 ºC to 500 ºC, or 10 ºC to 100 ºC, or 10 ºC to 50 ºC, or 50 ºC to 2000 ºC, or 50 ºC to 1000 ºC, or 50 ºC to 500 ºC, or 50 ºC to 100 ºC, or 100 ºC to 2000 ºC, or 100 ºC to 1000 ºC, or 100 ºC to 500 ºC, or 500 ºC to 2000 ºC, or 500 ºC to 1000 ºC, or 500 ºC to 800 ºC, or such as from 60 ºC to 700 ºC, and including 100 ºC to 400 ºC. In some instances, the gaseous source of CO2 is air and product gas produced by a direct air capture (DAC) system. DAC systems are a class of technologies capable of separating carbon dioxide CO2 directly from ambient air. A DAC system is any system that captures CO2 directly from air and generates a product gas that includes CO2 at a higher concentration than that of the air that is input into the DAC system. The concentration of CO2 in the air that is input to the DAC system may vary as CO2 concentrations in the Earth’s atmosphere are not homogeneous. In some instances, 100 ppm or greater, such as 500 ppm or greater, including 5,000 ppm or greater, such that the location of the DAC system is more efficient at CO2 capture in locations where CO2 concentrations are relatively high, e.g., near congested freeway interchanges, bad commute corridors, in industrial zones of metropolitan areas and the like. While the concentration of CO2in the DAC generated gaseous source of CO2may vary, in some instances the concentration 1,000 ppm or greater, such as 10,000 ppm or greater, including 100,000 ppm or greater, where the product gas may not be pure CO2, such that in some instances the product gas is 3% or more non-CO2constituents, such as 5% or more non-CO2constituents, including 10% or more non-CO2constituents. Non-CO2constituents that may be present in the product stream may be constituents that Atty Docket No.: BLUE-061WO originate in the input air and / or from the DAC system. In some instances, the concentration of CO2in the DAC product gas ranges from 1,000 to 999,000 ppm, such as 1,000 to 10,000 ppm, or 10,000 to 100,000 ppm or 100,000 to 999,000 ppm. DAC generated gaseous streams have, in some embodiments, CO2present in amounts of 200 ppm to 1,000,000 ppm; or 200 ppm to 500,000 ppm; or 200 ppm to 100,000 ppm; or 200 ppm to 10,000; or 200 ppm to 5,000 ppm; or 200 ppm to 2,000 ppm; or 200 ppm to 1,000 ppm; or 200 to 500 ppm; or 500 ppm to 1,000,000 ppm; or 500 ppm to 500,000 ppm; or 500 ppm to 100,000 ppm; or 500 ppm to 10,000; or 500 ppm to 5,000 ppm; or 500 ppm to 2,000 ppm; or 500 ppm to 1,000 ppm; or 1,000 ppm to 1,000,000 ppm; or 1,000 ppm to 500,000 ppm; or 1,000 ppm to 100,000 ppm; or 1,000 ppm to 10,000; or 1,000 ppm to 5,000 ppm; or 1,000 ppm to 2,000 ppm; or 2,000 ppm to 1,000,000 ppm; or 2,000 ppm to 500,000 ppm; or 2,000 ppm to 100,000 ppm; or 2,000 ppm to 10,000; or 2,000 ppm to 5,000 ppm; or 2,000 ppm to 3,000 ppm; or 5,000 ppm to 1,000,000 ppm; or 5,000 ppm to 500,000 ppm; or 5,000 ppm to 100,000 ppm; or 5,000 ppm to 10,000; or 10,000 ppm to 1,000,000 ppm; or 10,00 ppm to 500,000 ppm; or 10,000 ppm to 100,000 ppm; or 50,000 ppm to 1,000,000 ppm; or 50,000 ppm to 500,000 ppm; or 50,000 ppm to 100,000 ppm; or 100,000 ppm to 1,000,000 ppm; or 100,000 ppm to 500,000 ppm; or 200,000 ppm to 1000 ppm, including 200,000 ppm to 2,000 ppm, for example 180,000 ppm to 2,000 ppm, or 180,000 ppm to 5,000 ppm, also including 180,000 ppm to 10,000 ppm. The DAC product gas that is contacted with the aqueous capture liquid may be produced by any convenient DAC system. DAC systems are systems that extract CO2 from the air using media that binds to CO2 but not to other atmospheric chemicals (such as nitrogen and oxygen). As air passes over the CO2 binding medium, CO2 "sticks" to the binding medium. In response to a stimulus, e.g., heat, humidity, etc., the bound CO2 may then be released from the binding medium resulting the production of a gaseous CO2 containing product. DAC systems of interest include alkaline based systems, but are not limited to: amine based or hydroxide-based systems; CO2 sorbent / temperature swing based systems, and CO2sorbent / temperature swing based systems. In some instances, the DAC system is an amine based or a hydroxide based system, in which CO2is separated from air by contacting the air with an aqueous amine or an aqueous hydroxide liquid to produce an aqueous carbonate, such as an aqueous ammonium carbonate. Examples of hydroxide based DAC systems include, but are not limited to, those described in PCT published application Nos. WO / 2009 / 155539; WO / 2010 / 022339; WO / 2013 / 036859; and WO / 2013 / 120024; the disclosures of which are herein Atty Docket No.: BLUE-061WO incorporated by reference. In some instances, the DAC system is a CO2sorbent based system, in which CO2is separated from air by contacting the air with sorbent, such as an amine sorbent, followed by release of the sorbent captured CO2by subjecting the sorbent to one or more stimuli, e.g., change in temperature, change in humidity, etc. Examples of such DAC systems include, but are not limited to, those described in PCT published application Nos. WO / 2005 / 108297; WO / 2006 / 009600; WO / 2006 / 023743; WO / 2006 / 036396; WO / 2006 / 084008; WO / 2007 / 016271; WO / 2007 / 114991; WO / 2008 / 042919; WO / 2008 / 061210; WO / 2008 / 131132; WO / 2008 / 144708; WO / 2009 / 061836; WO / 2009 / 067625; WO / 2009 / 105566; WO / 2009 / 149292; WO / 2010 / 019600; WO / 2010 / 022399 ; WO / 2010 / 107942; WO / 2011 / 011740; WO / 2011 / 137398; WO / 2012 / 106703; WO / 2013 / 028688; WO / 2013 / 075981; WO / 2013 / 166432; WO / 2014 / 170184; WO / 2015 / 103401; WO / 2015 / 185434; WO / 2016 / 005226; WO / 2016 / 037668; WO / 2016 / 162022; WO / 2016 / 164563; WO / 2016 / 161998; WO / 2017 / 184652; and WO / 2017 / 009241; the disclosures of which are herein incorporated by reference. Another source of gaseous CO2 that may be employed in embodiments of the invention is ambient air. Such embodiments include directly contacting an aqueous capture liquid with the ambient air to produce a CO2 sequestering carbonate and CO2- depleted air to sequester the CO2 from the ambient air. Ambient air contacted with the aqueous capture liquid may, in some embodiments, have an amount of CO2 ranging from 300 ppm to 500 ppm. In addition, CO2-depleted air may have, in some embodiments, an amount of CO2 ranging from 100 ppm to 300 ppm. In some cases, directly contacting the aqueous capture liquid with the ambient air comprises drawing in the ambient air from a surrounding environment using a gas conveyor, and contacting the ambient air with the capture liquid. Gas conveyors may include, for example, an air pump or a turbine. In select embodiments, the gas conveyor is powered by a source of green energy, such as wind energy, hydroelectric energy, solar energy, geothermal energy or nuclear energy. The manner in which the aqueous capture liquid is contacted with the ambient air can include, for example, counter-current, co-current, or cross- current manners. Further details regarding such embodiments may be found in United States Provisional Patent Application Serial No.63 / 664,950; the disclosure of which is herein incorporated by reference. As summarized above, an aqueous capture liquid is contacted with the gaseous source of CO2under conditions sufficient to produce a CO2sequestering material. The Atty Docket No.: BLUE-061WO CO2sequestering material may be produced from the gaseous source of CO2and capture liquid by using a multistep or single step protocol, as desired. For example, in some embodiments, combination of the CO2capture liquid and gaseous source of CO2results in production of an aqueous carbonate, which aqueous carbonate is then subsequently contacted with a divalent cation source, e.g., a Ca2+and / or Mg2+source, to produce the CO2sequestering material. In yet other embodiments, a one-step CO2gas absorption carbonate precipitation protocol is employed. The concentration of ammonia in the aqueous capture ammonia may vary, where in some instances the aqueous capture ammonia includes ammonia (NH3) at a concentration ranging from 0.1 to 20.0 moles per liter (M), and in some instances 0.1 to 5.0 M, such as 0.1 to 4.0 M, e.g., 4.0 M, while in other instances from 2 to 20 M, such as 4 to 20 M. The aqueous capture ammonia may include any convenient water. Waters of interest from which the aqueous capture ammonia may be produced include, but are not limited to, freshwaters, seawaters, brine waters, produced waters and waste waters. In some instances the water of interest may be recycled water from a wastewater treatment plant, wherein the recycled water already includes NH3 at a concentration ranging from 10 to 500 ppm, and in some instances 10 to 100 ppm, such as 10 to 90 ppm, while in other instances from 100 to 500 ppm, such as from 150 to 500 ppm NH3. The pH of the aqueous capture ammonia may vary, ranging in some instances from 10.0 to 13.5, such as 10.0 to 13.0, including 10.5 to 12.5. Further details regarding aqueous capture ammonias of interest are provided in PCT published application No. WO / 2017 / 165849; the disclosure of which is herein incorporated by reference. The aqueous capture ammonia may further include an organic acid. In such instances, the organic acid may vary, where organic acids of interest include, but are not limited to: acetic acid, maleic acid, butyric acid, aspartic acid, malonic acid, citric acid, fumaric acid, lactic acid, succinic acid, pyruvic acid, phosphoric acid, carbonic acid, propionic acid, oxalic acid, glyoxylic acid, glycolic acid, acrylic acid, propiolic acid, tartronic acid, mesoxalic acid, dihydroxymalonic acid, hydracrylic acid, glycidic acid, butyric acid, isobutyric acid, acetoacetic acid, oxaloacetic acid, malic acid, tartaric acid, valeric acid, iso-valeric acid, glutaric acid, alpha-ketoglutaric acid, caproic acid, adipic acid, isocitric acid, enanthic acid, pimelic acid, caprylic acid, phthalic acid, pelargonic acid, cinnamic acid, capric acid, sebacic acid, lauric acid, mellitic acid, tridecylic acid, myristic acid, pentadecylic acid, palmitic acid, margaric acid, stearic acid, nonadecylic acid, arachidic acid, behenic acid, tricosylic acid, Atty Docket No.: BLUE-061WO lignoceric acid, pentacosylic acid, and cerotic acid, and combinations thereof. In some instances, the organic acid is acetic acid. When present the organic acid may be present in varying amounts, where in some instances, the amount of organic acid ranges from 0.001 M to 20 M, such as 0.06 g / l to 1201.0 g / l concentration of organic acid. The CO2 containing gas, e.g., as described above, may be contacted with the aqueous capture liquid, e.g., aqueous capture ammonia, using any convenient protocol. For example, contact protocols of interest include, but are not limited to: direct contacting protocols, e.g., bubbling the gas through a volume of the aqueous medium, concurrent contacting protocols, i.e., contact between unidirectionally flowing gaseous and liquid phase streams, countercurrent protocols, i.e., contact between oppositely flowing gaseous and liquid phase streams, and the like. Contact may be accomplished through use of infusers, bubblers, fluidic Venturi reactors, spargers, gas filters, sprays, trays, scrubbers, absorbers or packed column reactors, and the like, as may be convenient. In some instances, the contacting protocol may use a conventional absorber or an absorber froth column, such as those described in U.S. Patent Nos.7,854,791; 6,872,240; and 6,616,733; and in United States Patent Application Publication US-2012- 0237420-A1; the disclosures of which are herein incorporated by reference. The process may be a batch or continuous process. In some instances, a regenerative froth contactor (RFC) may be employed to contact the CO2 containing gas with the aqueous capture liquid, e.g., aqueous capture ammonia. In some such instances, the RFC may use a catalyst (such as described elsewhere), e.g., a catalyst that is immobilized on / to the internals of the RFC. Further details regarding a suitable RFC are found in U.S. Patent No.9,545,598, the disclosure of which is herein incorporated by reference. In some instances, the gaseous source of CO2 is contacted with the liquid using a microporous membrane contactor. Microporous membrane contactors of interest include a microporous membrane present in a suitable housing, where the housing includes a gas inlet and a liquid inlet, as well a gas outlet and a liquid outlet. The contactor is configured so that the gas and liquid contact opposite sides of the membrane in a manner such that molecule may dissolve into the liquid from the gas via the pores of the microporous membrane. The membrane may be configured in any convenient format, where in some instances the membrane is configured in a hollow fiber format. Hollow fiber membrane reactor formats which may be employed include, but are not limited to, those described in U.S. Patent Nos.7,264,725; 6,872,240 and 5,695,545; the disclosures of which are herein incorporated by reference. In some Atty Docket No.: BLUE-061WO instances, the microporous hollow fiber membrane contactor that is employed is a hollow fiber membrane contactor, which membrane contactors include polypropylene membrane contactors and polyolefin membrane contactors. Contact between the capture liquid and the CO2-containing gas occurs under conditions such that a substantial portion of the CO2 present in the CO2-containing gas goes into solution, e.g., to produce bicarbonate ions. By substantial portion is meant 10% or more, such as 50% or more, including 80% or more. The temperature of the capture liquid that is contacted with the CO2-containing gas may vary. In some instances, the temperature ranges from -1.4 to 100 °C, such as 20 to 80 °C and including 40 to 70 °C. In some instances, the temperature may range from -1.4 to 50 °C or higher, such as from -1.1 to 45 °C or higher. In some instances, cooler temperatures are employed, where such temperatures may range from -1.4 to 4 °C, such as -1.1 to 0 °C. In some instances, warmer temperatures are employed. For example, the temperature of the capture liquid in some instances may be 25 °C or higher, such as 30 °C or higher, and may in some embodiments range from 25 to 50 °C, such as 30 to 40 °C. The CO2-containing gas and the capture liquid are contacted at a pressure suitable for production of a desired CO2charged liquid. In some instances, the pressure of the contact conditions is selected to provide for optimal CO2absorption, where such pressures may range from 1 ATM to 100 ATM, such as 1 to 50 ATM, e.g., 20-30 ATM or 1 ATM to 10 ATM. Where contact occurs at a location that is naturally at 1 ATM, the pressure may be increased to the desired pressure using any convenient protocol. In some instances, contact occurs where the optimal pressure is present, e.g., at a location under the surface of a body of water, such as an ocean or sea. Contact is carried out in manner sufficient to produce an aqueous ammonium carbonate. The aqueous ammonium carbonate may vary, where in some instances the aqueous ammonium carbonate comprises at least one of ammonium carbonate and ammonium bicarbonate and in some instances comprises both ammonium carbonate and ammonium bicarbonate. The aqueous ammonium bicarbonate may be viewed as a DIC containing liquid. As such, in charging the aqueous capture ammonia with CO2, a CO2containing gas may be contacted with CO2capture liquid under conditions sufficient to produce dissolved inorganic carbon (DIC) in the CO2capture liquid, i.e., to produce a DIC containing liquid. The DIC is the sum of the concentrations of inorganic carbon species in a solution, represented by the equation: DIC = [CO2*] + [HCO3-] + [CO32-], Atty Docket No.: BLUE-061WO where [CO2*] is the sum of carbon dioxide ([CO2]) and carbonic acid ([H2CO3]) concentrations, [HCO3-] is the bicarbonate concentration (which includes ammonium bicarbonate) and [CO32-] is the carbonate concentration(which includes ammonium carbonate) in the solution. The DIC of the aqueous media may vary, and in some instances may be 3 ppm to 168,000 ppm carbon (C), such as 3 to 1,000 ppm, or 3 to 100 ppm, or 3 to 500 ppm, or 3 to 800 ppm, or 3 to 1,000 ppm, or 100 to 10,000 ppm, or 100 to 1,000 ppm, or 100 to 5,000 ppm, or 100 to 8,000 ppm, or 100 to 10,000 ppm, or 1,000 to 50,000 ppm, or 1,000 to 8,000 ppm, or 1,000 to 15,000 ppm, or 1,000 to 30,000 ppm, or 5,000 to 168,000 ppm, or 5,000 to 25,000 ppm, or such as from 6,000 to 65,000 ppm, and including 8,000 to 95,000 ppm carbon (C). The amount of CO2 dissolved in the liquid may vary, and in some instances ranges from 0.05 to 40 mM, such as 1 to 35 mM, including 25 to 30 mM. The pH of the resultant DIC containing liquid may vary, ranging in some instances from 4 to 12, such as 6 to 11 and including 7 to 11, e.g., 8 to 9.5. Where desired, the CO2 containing gas is contacted with the capture liquid in the presence of a catalyst (i.e., an absorption catalyst, either hetero- or homogeneous in nature) that mediates the conversion of CO2 to bicarbonate. Of interest as absorption catalysts are catalysts that, at pH levels ranging from 8 to 10, increase the rate of production of bicarbonate ions from dissolved CO2. The magnitude of the rate increase (e.g., as compared to control in which the catalyst is not present) may vary, and in some instances is 2-fold or greater, such as 5-fold or greater, e.g., 10-fold or greater, as compared to a suitable control. Further details regarding examples of suitable catalysts for such embodiments are found in U.S. Patent No.9,707,513, the disclosure of which is herein incorporated by reference. In some embodiments, the resultant aqueous ammonium carbonate is a two phase liquid which includes droplets of a liquid condensed phase (LCP) in a bulk liquid, e.g., bulk solution. By “liquid condensed phase” or “LCP” is meant a phase of a liquid solution which includes bicarbonate ions wherein the concentration of bicarbonate ions is higher in the LCP phase than in the surrounding, bulk liquid. LCP droplets are characterized by the presence of a meta-stable bicarbonate-rich liquid precursor phase in which bicarbonate ions associate into condensed concentrations exceeding that of the bulk solution and are present in a non-crystalline solution state. The LCP contains all of the components found in the bulk solution that is outside of the interface. However, the concentration of the bicarbonate ions is higher than in the bulk solution. In those situations where LCP droplets are present, the LCP and bulk solution may each contain Atty Docket No.: BLUE-061WO ion-pairs and pre-nucleation clusters (PNCs). When present, the ions remain in their respective phases for long periods of time, as compared to ion-pairs and PNCs in solution. Further details regarding LCP containing liquids are provided in U.S. Patent No.9,707,513, the disclosure of which is herein incorporated by reference. Production of Solid CO2Sequestering Carbonate As reviewed above, both multistep and single step protocols may be employed to produce the CO2 sequestering carbonate material from the CO2 containing gas the aqueous capture ammonia. For example, in some embodiments the product aqueous ammonium carbonate is forwarded to a CO2 sequestering carbonate production module, where divalent cations, e.g., Ca2+and / or Mg2+, are combined with the aqueous ammonium carbonate to produce the CO2 sequestering carbonate. In yet other instances, aqueous capture ammonia includes a source of divalent cations, e.g., Ca2+and / or Mg2+, such that aqueous ammonium carbonate combines with the divalent cations as it is produced to result in production of a CO2 sequestering carbonate. Accordingly, in some embodiments, following production of an aqueous carbonate, such as an aqueous ammonium carbonate, e.g., as described above, the aqueous carbonate is subsequently combined with a cation source under conditions sufficient to produce a solid CO2 sequestering carbonate. Cations of different valances can form solid carbonate compositions (e.g., in the form of carbonate minerals). In some instances, monovalent cations, such as sodium and potassium cations, may be employed. In other instances, divalent cations, such as alkaline earth metal cations, e.g., calcium (Ca2+) and magnesium (Mg2+) cations, may be employed. When cations are added to the aqueous carbonate, precipitation of carbonate solids, such as amorphous calcium carbonate (CaCO3) when the divalent cations include Ca2+, may be produced with a stoichiometric ratio of one carbonate-species ion per cation. Any convenient cation source may be employed in such instances. Cation sources of interest include, but are not limited to, the brine from water processing facilities such as sea water desalination plants, brackish water desalination plants, groundwater recovery facilities, wastewater facilities, blowdown water from facilities with cooling towers, and the like, which produce a concentrated stream of solution high in cation contents. Also of interest as cation sources are naturally occurring sources, such as but not limited to native seawater and geological brines, which may have varying Atty Docket No.: BLUE-061WO cation concentrations and may also provide a ready source of cations to trigger the production of carbonate solids from the aqueous ammonium carbonate. In yet other embodiments, the aqueous capture ammonia includes cations, e.g., as described above. The cations may be provided in the aqueous capture ammonia using any convenient protocol. In some instances, the cations present in the aqueous capture ammonia are derived from a second or draw liquid (such as a produced water), e.g., as described below, used in regeneration of the aqueous capture ammonia from an aqueous ammonium salt. In addition and / or alternatively, the cations may be provided by combining an aqueous capture ammonia with a cation source, e.g., as described above. The product CO2 sequestering carbonate compositions produced by embodiments of methods of the invention may vary greatly. The precipitated product may include one or more different carbonate compounds, such as two or more different carbonate compounds, e.g., three or more different carbonate compounds, five or more different carbonate compounds, etc., including non-distinct, amorphous carbonate compounds. Carbonate compounds of precipitated products of the invention may be compounds having a molecular formulation Xm(CO3)n where X is any element or combination of elements that can chemically bond with a carbonate group or its multiple, wherein X is in certain embodiments an alkaline earth metal and not an alkali metal; wherein m and n are stoichiometric positive integers. These carbonate compounds may have a molecular formula of Xm(CO3)n⋅H2O, where there are one or more structural waters in the molecular formula. The amount of carbonate in the product, as determined by coulometry using the protocol described as coulometric titration or by loss on ignition (LOI) using the standard test methods for LOI of solid combustion residues per ASTM D7348, may be 40% or higher, such as 70% or higher, including 80% or higher. The carbonate compounds of the precipitated products may include a number of different cations, such as but not limited to ionic species of: calcium, magnesium, sodium, potassium, sulfur, boron, silicon, strontium, and combinations thereof. Of interest are carbonate compounds of divalent metal cations, such as calcium and magnesium carbonate compounds. Specific carbonate compounds of interest include, but are not limited to: calcium carbonate minerals, magnesium carbonate minerals and calcium magnesium carbonate minerals. Calcium carbonate minerals of interest include, but are not limited to: calcite (CaCO3), aragonite (CaCO3), vaterite (CaCO3), ikaite (CaCO3⋅6H2O), and amorphous calcium carbonate (CaCO3). Magnesium carbonate minerals of interest include, but are not limited to magnesite (MgCO3), barringtonite Atty Docket No.: BLUE-061WO (MgCO3⋅2H2O), nesquehonite (MgCO3⋅3H2O), lanfordite (MgCO3⋅5H2O), hydromagnesite, and amorphous magnesium calcium carbonate (MgCO3). Calcium magnesium carbonate minerals of interest include, but are not limited to dolomite (CaMg)(CO3)2), huntite (Mg3Ca(CO3)4) and sergeevite (Ca2Mg11(CO3)13⋅H2O). Also of interest are carbonate compounds formed with Na, K, Al, Ba, Cd, Co, Cr, As, Cu, Fe, Pb, Mn, Hg, Ni, V, Zn, etc. The carbonate compounds of the product may include one or more waters of hydration, or may be anhydrous. In some instances, the amount by weight of magnesium carbonate compounds in the precipitate exceeds the amount by weight of calcium carbonate compounds in the precipitate. For example, the amount by weight of magnesium carbonate compounds in the precipitate may exceed the amount by weight calcium carbonate compounds in the precipitate by 5% or more, such as 10% or more, 15% or more, 20% or more, 25% or more, 30% or more. In some instances, the weight ratio of magnesium carbonate compounds to calcium carbonate compounds in the precipitate ranges from 1.5 - 5 to 1, such as 2-4 to 1 including 2-3 to 1. In some instances, the precipitated product may include hydroxides, such as divalent metal ion hydroxides, e.g., calcium and / or magnesium hydroxides. Further details regarding carbonate production and methods of using the carbonated produced thereby are provided in: U.S. Patent Nos.10,711,236; 10,203,434; 10,197,747; 9,993,799; 9,707,513 and 9,714,406; the disclosures of which are herein incorporated by reference. In some instances, carbonate production occurs in a continuous fashion, e.g., as described in U.S. Patent No.9,993,799, the disclosure of which is herein incorporated by reference. In some such instances, carbonate production may occur in the presence of a seed structure. By seed structure is meant a solid structure or material that is present flowing liquid, e.g., in the material production zone, prior to divalent cation introduction into the liquid. By "in association with" is meant that the material is produced on at least one of a surface of or in a depression, e.g., a pore, crevice, etc., of the seed structure. In such instances, a composite structure of the carbonate material and the seed structure is produced. In some instances, the product carbonate material coats a portion, if not all of, the surface of a seed structure, e.g., a carbonate coated seed structure. In some instances, the product carbonate materials fills in a depression of the seed structure, e.g., a pore, crevice, fissure, etc. Seed structures may vary widely as desired. The term "seed structure" is used to describe any object upon and / or in which the product carbonate material forms. Seed Atty Docket No.: BLUE-061WO structures may range from singular objects or particulate compositions, as desired. Where the seed structure is a singular object, it may have a variety of different shapes, which may be regular or irregular, and a variety of different dimensions. Shapes of interest include, but are not limited to, rods, meshes, blocks, etc. Also of interest are particulate compositions, e.g., granular compositions, made up of a plurality of particles. Where the seed structure is a particulate composition, the dimensions of particles may vary, ranging in some instances from 0.01 to 1,000,000 µm, such as 0.1 to 100,000 µm. The seed structure may be made up of any convenient material or materials. Materials of interest include both carbonate materials, such as described above, as well as non-carbonate materials. The seed structures may be naturally occurring, e.g., naturally occurring sands, shell fragments from oyster shells or other carbonate skeletal allochems, gravels, etc., or man-made, such as pulverized rocks, ground blast furnace slag, fly ash, cement kiln dust, red mud, returned concrete, recycled concrete, demolished concrete and the like. For example, the seed structure may be a granular composition, such as sand, which is coated with the carbonate material during the process, e.g., a white carbonate material or colored carbonate material, e.g., as described above. In some instances, seed structure may be coarse aggregates, such as friable Pleistocene coral rock, e.g., as may be obtained from tropical areas (e.g., Florida) that are too weak to serve as aggregate for concrete. In this case the friable coral rock can be used as a seed, and the solid CO2 sequestering carbonate mineral may be deposited in the internal pores, making the coarse aggregate suitable for use in concrete, allowing it to pass the Los Angeles abrasion test per AASHTO 96 and ASTMs C131 or C535. In some instances, where a lightweight aggregate is desired, the outer surface will only be penetrated by the solution of deposition, leaving the inner core relatively ‘hollow’ making a light weight aggregate for use in light weight concrete. The resultant solid CO2 sequestering carbonate may be used and / or further processed, e.g., as described in greater detail below. Ammonia Regeneration As summarized above, production of CO2sequestering carbonate from the aqueous ammonia capture liquid and the gaseous source of CO2yields an aqueous ammonium organic acid salt. The produced aqueous ammonium organic acid salt may vary with respect to the nature of the organic acid anion of the ammonium salt, where Atty Docket No.: BLUE-061WO specific ammonium organic acid salts that may be present in the aqueous ammonium organic acid salt include, but are not limited to, ammonium organic acids salts produced from organic acids selected from acetic acid, maleic acid, butyric acid, aspartic acid, malonic acid, citric acid, fumaric acid, lactic acid, succinic acid, pyruvic acid, phosphoric acid, carbonic acid, propionic acid, oxalic acid, glyoxylic acid, glycolic acid, acrylic acid, propiolic acid, tartronic acid, mesoxalic acid, dihydroxymalonic acid, hydracrylic acid, glycidic acid, butyric acid, isobutyric acid, acetoacetic acid, oxaloacetic acid, malic acid, tartaric acid, valeric acid, iso-valeric acid, glutaric acid, alpha-ketoglutaric acid, caproic acid, adipic acid, isocitric acid, enanthic acid, pimelic acid, caprylic acid, phthalic acid, pelargonic acid, cinnamic acid, capric acid, sebacic acid, lauric acid, mellitic acid, tridecylic acid, myristic acid, pentadecylic acid, palmitic acid, margaric acid, stearic acid, nonadecylic acid, arachidic acid, behenic acid, tricosylic acid, lignoceric acid, pentacosylic acid, and cerotic acid, and combinations thereof. In some embodiments, the organic acid is acetic acid, such that the aqueous ammonium organic acid salt is ammonium acetate. As reviewed above, aspects of the invention further include regenerating an aqueous capture ammonia, e.g., as described above, from the aqueous ammonium organic acid salt. By "regenerating an aqueous capture ammonium" is meant processing the aqueous ammonium organic acid salt in a manner sufficient to generate capture ammonia from the aqueous ammonium organic acid salt. The percentage of input ammonium salt that is converted to ammonia during this regeneration step may vary, ranging in some instances from 20 to 80%, such as 35 to 55%. Ammonia may be regenerated from an aqueous ammonium salt in this regeneration step using any convenient regeneration protocol. In some instances, the aqueous ammonium organic acid salt is subjected to dialysis regeneration to produce a regenerated aqueous ammonia capture liquid. By "subjected to dialysis regeneration" is meant that the aqueous ammonium organic acid salt is put through or processed by a regeneration protocol that generates an aqueous capture ammonia by using dialysis. The particular type of dialysis employed in regenerating the aqueous capture ammonia may vary. Examples of dialysis protocols that may be employed in embodiments of the invention include, but are not limited to: diffusion dialysis, electrodialysis, nanofiltration, and the like. As the aqueous capture ammonia is regenerated using dialysis regeneration, it is regenerated using a membrane mediated protocol. By "membrane mediated protocol" is Atty Docket No.: BLUE-061WO meant a process or method which employs a membrane at some time during the method. As such, membrane mediated alkali enrichment protocols are those processes in which a membrane is employed at some time during the process. While a given membrane mediated protocol may vary, in some instances the membrane mediated protocol includes contacting the aqueous ammonium organic acid salt liquid (which may be referred to as a first liquid) and a second liquid, e.g., a draw liquid, to opposite sides of a membrane. In embodiments, the first and second liquids are flowed past opposite sides of a membrane in a co- or counter-current fashion, as desired, resulting in regeneration of the aqueous capture ammonia. Where desired, a thermodynamic force is employed that facilitates the capture ammonia regeneration. Any convenient thermodynamic force or combination of forces may be employed, where thermodynamic driving forces that may be employed include, but are not limited to: osmotic force, ionic concentration, mechanical pressure, alkalinity, temperature, other chemical reactions, etc., and combinations thereof, e.g., combinations of osmotic force and mechanical pressure, e.g., as occurs in pressure assisted forward osmosis. In some instances, the membrane mediated protocol is one that employs an osmotic force to facilitate capture ammonia regeneration. Protocols of these embodiments may be referred to osmotic pressure mediated protocols. The phrase "osmotic pressure mediated protocol " is employed herein to refer to a process characterized by the presence of an osmotic pressure driving force, e.g., in the form of an osmotic pressure gradient, such that a first liquid (e.g., a draw liquid) of high solute concentration relative to that of a second liquid (e.g., a feed liquid) is used to induce a net flow of water through a membrane into the first (draw) liquid from the second (feed) liquid, thus effectively separating at least a portion of the water component of the feed from its solutes. In some embodiments, the draw and feed liquids differ from each other in terms of osmotic potential, where the osmotic potential of a given draw liquid will be higher than the feed liquid with which it is employed. The magnitude of the difference in osmotic potential between a pair of given draw and feed liquids may vary, and in some instances ranges from 0.1 bar to 150 bar, such as 20 bar to 60 bar, including 25 bar to 35 bar. In some instances, the membrane mediated protocol is one that employs an ionic concentration force to facilitate regeneration of the aqueous capture ammonia. Protocols of these embodiments may be referred to as ionic concentration mediated protocols. The Atty Docket No.: BLUE-061WO phrase "ionic concentration mediated protocol " is employed herein to refer to a process characterized by the presence of an ionic concentration driving force, e.g., in the form of an ionic concentration gradient, such that a first liquid of high ionic species concentration relative to that of a second liquid is used to induce a net flow of ions through a membrane from the first liquid into the second liquid. In some embodiments, a first liquid may include a high ionic strength medium. Such liquids of interest include aqueous media having a salinity of 2 ppt or more, such as 5 ppt or more, including 10 ppt or more. In some instances ,the high ionic strength liquid is an aqueous medium having a salinity that ranges from 3 to 200 ppt, such as 5 to 100 ppt. Membrane mediated protocols may vary, so long as they produce a regenerated capture ammonia, as described above. As such, a variety of different types of membranes, membrane configurations, contact protocols, first and second liquid pairings, etc., may be employed, where selection of a particular set of protocol parameters may depend on a number of different factors, such as the nature of the first and second liquids that are available. In some embodiments of the methods, a species selective membrane is employed. In some embodiments, a selective membrane may utilize dialysis diffusion through the membrane to selectively partition ions between the feed and the draw stream. Diffusion dialysis membranes are generally permeable to hydrogen ions and utilize differences in ion solubility and mobility within the membrane for selective ion separations between different liquids, e.g., feed and draw liquids. Examples of such membranes include, but are not limited to those described in: Liu et al., J. Membrane Science (2014) 451: 18-23; Hao et al., J. Membrane Science (2013) 425-426: 156-162; Gu et al., Desalination (2012) 304: 25-32; and Hao et al., J. Hazardous Materials (2013) 244-245: 348-356; as well as Nafion membranes, e.g., as described in Okada et al., Electrochimica Acta (1998) 43: 3741-3747. In some instances, the diffusion dialysis membrane employed is ion or charge selective membrane, i.e., a membrane that preferentially allows the passage of one type of charged species across the membrane relative to other species, e.g., other charged species and / or neutral species. For example, membranes of interest include cationic membranes, i.e., membranes that permit the passage of cations but not of anions. Also of interest are anionic membranes, i.e., membranes that permit the passage of cations but not of anions. Both cationic and anionic membranes find use in protocols where alkali enrichment is achieved by removing hydrogen ions from the initial liquid to produce the enhanced alkalinity liquid. In Atty Docket No.: BLUE-061WO these embodiments, as hydrogen ions are removed from the initial liquid, the pH of the initial liquid is increased to produce a product liquid of enhanced alkalinity relative to the initial liquid. The magnitude of the change in pH may vary, and in some instances ranges from 0.1 to 4 pH units, such as 0.5 to 2.0 pH units. In some instances, the membrane is an ionically selective membrane, e.g., a cationic or anionic membrane. The choice of whether to use an anionic or cationic membrane may depend on a number of factors, such as whether the membrane mediated alkali enrichment protocol is an osmotic pressure or ionic concentration mediated protocol, the nature of the first and second liquids, etc. Membranes employed in membrane mediated alkali enrichment protocols may vary with respect to porosity. In some embodiments, employed membranes may be size- based separators that allow molecules under a certain size to pass through, while preventing larger molecules from passing through. In this way, the membranes can be used to selectively retain molecules that are over a certain size while allowing other molecules that are below a certain size to pass through. In some embodiments, employed membranes include pores that range in size from 1 micron up to 2 microns, up to 3 microns, up to 4 microns, up to 5 microns, up to 6 microns, up to 7 microns, up to 8 microns, up to 9 microns, or up to 10 microns or more. In some embodiments, the membrane may include pores ranging in size from 1 Angstrom up to 10 Angstroms, up to 20 Angstroms, up to 30 Angstroms, up to 40 Angstroms, up to 50 Angstroms, up to 60 Angstroms, up to 70 Angstroms, up to 80 Angstroms, up to 90 Angstroms, up to 100 Angstroms, up to 200 Angstroms, up to 300 Angstroms, up to 400 Angstroms, up to 00 Angstroms, up to 600 Angstroms, up to 700 Angstroms, up to 800 Angstroms, up to 900 Angstroms or more. In some embodiments, the membrane includes a reverse osmosis membrane having pores ranging in size from 5 Angstroms up to 6 Angstroms, up to 7 Angstroms, up to 8 Angstroms. In some embodiments, the selective membrane may be a nano-filtration membrane, such as a membrane having pores ranging in size from 1 nanometer to 2 nanometers. In some embodiments, the selective membrane may include an ultra- filtration membrane, such as a membrane having pores ranging in size from 10 nanometers up to 20 nanometers, up to 30 nanometers, up to 40 nanometers, up to 50 nanometers, up to 60 nanometers, up to 70 nanometers, up to 80 nanometers, up to 90 nanometers, up to 100 nanometers, up to 125 nanometers, up to 150 nanometers, up to 175 nanometers, up to 200 nanometers, or more. Atty Docket No.: BLUE-061WO A given membrane employed in embodiments of the invention may have a variety of different physical dimensions. In some instances, membranes of interest having thicknesses ranging from 0.001 mm to 1 mm, such as 0.005 mm to 0.05 mm and including 0.03 mm to 0.3 mm. Membranes in accordance with embodiments of the invention can have a variety of configurations including thin films, hollow fiber membranes, spiral wound membranes, monofilaments and disk tubes. Membranes of interest can be made of organic or inorganic materials. In some embodiments, membranes made of materials such as cellulose acetate, cellulose nitrate, polysulfone, polyvinylidene fluoride, polyamide and acrylonitrile co-polymers may be used. Other membranes may be mineral membranes or ceramic membranes made of materials such as ZrO2 and TiO2. The material selected for use as the membrane may be selected to be able to withstand various process conditions to which the membrane may be subjected. For example, it may be desirable that the membrane be able to withstand elevated temperatures, such as those associated with sterilization or other high temperature processes. In some embodiments, a membrane module may be operated at a temperature in the range of 0 to 100°C, such as 40 to 50 °C. Likewise, the membrane may be selected to be able to maintain integrity under various pH conditions, such as a pH level ranging from 2 to 11, such as 7 to 10. The thickness of the membrane may vary, ranging in some instances from 0.01 mm to 0.1 mm, such as 0.02 mm to 0.06 mm and including 0.03 mm to 0.04 mm. Membranes employed in methods of the invention may be present in distinct regeneration units. A given unit may include one or more square meter (m2) of membrane, such as two or more m2membrane, e.g., 5 m2to 500,000 m2membrane, such as 40 m2to 400 m2membrane, including 50,000 m2to 250,000 m2membrane, which may be arranged so that the first and second fluids flow sequentially past each of the membranes, e.g., in a co- or counter-current fashion. In such units, the one or m2membrane may be positioned within a housing or casing, e.g., in a plate-and-frame structure or “stack”. The housing may be sized and shaped to accommodate the membrane(s) positioned therein. For example, the housing may be substantially cylindrical if housing spirally wound forward osmosis membranes. Alternatively, the housing may have a box configuration, e.g., where multiple membranes are arranged therein in a stacked or plate-and-frame structure. The housing of the membrane module may contain inlets to provide first and second liquids to the membrane module as well as outlets for withdrawal of product streams from the membrane module. In some Atty Docket No.: BLUE-061WO embodiments, the housing may provide at least one reservoir or chamber for holding or storing a fluid to be introduced to or withdrawn from the membrane module. In some embodiments, the housing may be insulated. A given dialysis regeneration protocol may employ a single-step membrane mediated dialysis regeneration protocol or a multi-step membrane mediated dialysis regeneration protocol, e.g., a two-step membrane mediated dialysis regeneration protocol, as desired. In a single-step protocol, a single type of membrane is employed in the regeneration of aqueous ammonia. Such protocols may find use where a given draw liquid includes both high concentrations (> 100 mM) of a desired divalent cation (i.e. Ca2+, Mg2+, Sr2+, etc…) and high alkalinity (> 100 mM). In a multi-step protocol, two or more different types membranes are sequentially employed to generate the aqueous capture ammonia. For example, in a two-step protocol, first and second membranes that differ from each other are employed, e.g., sequentially, to generate the aqueous capture ammonia. Such protocols may find use where a given draw liquid includes high concentrations (> 100 mM) of a desired divalent cation (i.e. Ca2+, Mg2+, Sr2+, etc…) or high alkalinity (> 100 mM), but not both. In accordance with one or more embodiments, the regeneration protocol may be performed using a forward osmosis separation system, which may be constructed and arranged so as to bring an aqueous ammonium organic acid salt and a second liquid into contact with first and second sides of a membrane (such as described above), respectively. Although the first and second liquids can remain stagnant, in some instances both the first and second liquids are introduced by cross flow, i.e., flows parallel to the surface of the membrane. This configuration may increase membrane surface area contact along one or more fluid flow paths, thereby increasing the efficiency of the forward osmosis. In some embodiments, the first and second solutions may flow in the same direction. In other embodiments, the first and second solutions may flow in opposite directions. In at least some embodiments, similar fluid dynamics may exist on both sides of a membrane surface. This may be achieved by strategic integration of the one or more forward osmosis membranes in the module or housing. The conditions of the ammonia regeneration step may vary as desired. The temperature of the liquids may vary, ranging in some instances from 0 to 100 °C, such as 4 to 80°C. The temperatures of the liquids may be the same or different. When different, the magnitude of any temperature variation may vary, ranging in some instances from 0.1 to 95 °C, such as 30 to 45 °C. The pressure of the liquids may also Atty Docket No.: BLUE-061WO vary, ranging in some instances from 1 to 30 bar, such as 1.5 to 2 bar. When different, the magnitude of any pressure variation may vary, ranging in some instances from 0.1 to 30 bar, such as 0.5 to 1 bar. The flow rates of the liquids may be the same or different, and in some instances range from 0.25 to 10 gallon / min, such as 0.5 to 1 gallon / min. When different, the magnitude of any flow rate variation between the draw and feed may vary, and in some instances ranges from 0.05 to 9.75 gallon / min, such as 1 to 3 gallon / min. Further details regarding membrane mediated protocols that may be employed in embodiments of the invention include those described in U.S. Patent Nos.9,707,513 and 10,898,854, the disclosures of which are herein incorporated by reference. The second liquid employed in methods of the invention may vary. In some instances, the second liquid differs from the aqueous ammonium organic acid salt in terms of osmotic potential, where the osmotic potential of a given second liquid may be higher or lower relative to the initial liquid with which it is employed, depending on the particular alkali recover protocol that is used (e.g., as described above). The magnitude of the difference in osmotic potential between any two given liquid pairs may vary, and in some instances ranges from 0.1 bar to 150 bar, such as 20 bar to 60 bar, including 25 bar to 35 bar. Any convenient liquid may be employed as the second liquid. In some embodiments, a second liquid may include a high ionic strength medium. In some embodiments, the second liquid contains non-hydrogen monovalent cations that are capable of crossing the membrane system to provide for charge balance and thereby facility in the alkalinity increase of the first liquid. In certain embodiments, the non- hydrogen monovalent cations include, but are not limited to: Na+, K+, and NH4+. Second liquids of interest include aqueous media having a salinity of 2 ppt or more, such as 5 ppt or more, including 10 ppt or more. In some instances the second liquid is an aqueous medium having a salinity that ranges from 3 to 50 ppt, such as 5 to 35 ppt. The pH of the second liquid may vary, and in some instances ranges from 4 to 12, such as 5 to 10 and including 6 to 9. In some instances, the second liquid may be referred to as a brine draw liquid. The term "brine" refers to water saturated or nearly saturated with salt and has a salinity that is 50 ppt (parts per thousand) or greater, such as 60 ppt or greater, and including 95 ppt or greater. Brine draw liquids of interest include, but are not limited to: man-made brines, such as geothermal plant wastewaters, oil field produced brines, fracking operation produced waters, desalination waste waters, etc., as well as Atty Docket No.: BLUE-061WO natural brines, such as surface brines found in bodies of water on the surface of the earth and deep brines, found underneath the earth, as well as other liquids having a salinity as described above. In some embodiments, a draw liquid includes a geological brine or a brine discharge from a desalination plant. As reviewed above, the second or draw liquid employed in the alkali enrichment protocol may vary. One type of draw liquid that may be employed is "produced water." As used herein, the term "produced water" means water that is produced along with oil or gas in an oil or gas recovery process. Typically, the oil or gas is separated from the water and the separated water is referred to as produced water which is one type of wastewater. Produced water typically contains organics, silica, boron, dissolved solids and suspended solids. Produced water typically includes natural contaminants that come from the subsurface environment. These contaminants include hydrocarbons from oil and inorganic salts. Produced water may also include manmade contaminants such as drilling mud, frac flow back water that includes spent fracturing fluids, including polymers and inorganic cross-leaking agents, polymer breaking agents, friction reduction chemicals, and artificial lubricants. These manmade contaminants are injected into wells as part of the drilling and production processes and recovered as contaminants in the produced water. In addition, the produced water may include contaminants that result from drilling mud. These contaminants may include acids and caustics such as soda ash, calcium carbonate, sodium hydroxide, and magnesium hydroxide. Furthermore, the contaminants in the produced water may include defoamers, emulsifiers, filtrate reducers, shale control inhibitors, deicers including methanol and other contaminants. Another type of draw liquid that may be employed is concrete production wash water, where the phrase "concrete production wash water" refers to wash water from concrete plants, trucks, etc. Concrete production wash water may be obtained from a variety of sources, including but not limited to: rinsing a ready-mix concrete truck after it has returned from a site project. Such wash waters may have pH in the range of 8-13, such as pH 9-10 or pH 11-12. Concrete production wash waters may contain commercial chemical admixtures for concrete, such as, but not limited to, chemical admixtures that comply with ASTM designation C494 or ASTM designation C260, that contain organic alkalinity such as, but not limited to, primary, secondary and tertiary amines, etc. Concrete production wash waters may also contain, in addition to chemical admixtures for concrete, dissolved metal cations, for example, dissolved monovalent alkali metal cations such as Lithium (Li+), sodium (Na+) or potassium (K+), dissolved Atty Docket No.: BLUE-061WO alkaline earth metal cations such as calcium (Ca2+), or other dissolved metal cations such as aluminum (Al3+) or iron (Fe2+, Fe3+). The positively charged cations may be charged-balanced with negatively charged anions such as, but not limited to, monovalent bicarbonate (HCO3-), chloride (Cl-), hydroxide (OH-) or nitrate (NO3-) ions, as well as divalent sulfate (SO42-) ions. Aqueous capture ammonia regeneration may include using an electrolysis mediated protocol, in which a direct electric current is introduced into the aqueous ammonium salt to regenerate ammonia. Any convenient electrolysis protocol may be employed. Examples of electrolysis protocols that may be adapted for regeneration of ammonia from an aqueous ammonium salt may employed one or more elements from the electrolysis systems described in U.S. Patent Nos.7,727,374 and 8,227,127, as well as published PCT Application Publication No. WO / 2008 / 018928; the disclosures of which are hereby incorporated by reference. The resultant regenerated aqueous capture ammonia may vary, e.g., depending on the particular regeneration protocol that is employed. In some instances, the regenerated aqueous capture ammonia includes ammonia (NH3) at a concentration ranging from 0.1 to 25 moles per liter (M), such as from 4 to 20 M, including from 12.0 to 16.0 M, as well as any of the ranges provided for the aqueous capture ammonia provided above. The pH of the aqueous capture ammonia may vary, ranging in some instances from 10.0 to 13.0, such as 10.0 to 12.5. In some instances, e.g., where the aqueous capture ammonia is regenerated in a geomass mediated protocol that does not include input of energy, e.g., as described above, the regenerated aqueous capture ammonia may further include cations, e.g., divalent cations, such as Ca2+. In addition, the regenerated aqueous capture ammonia may further include an amount of ammonium salt. In some instances, ammonia (NH3) is present at a concentration ranging from 0.05 to 4 moles per liter (M), such as from 0.05 to 1 M, including from 0.1 to 2 M. The pH of the aqueous capture ammonia may vary, ranging in some instances from 8.0 to 11.0, such as from 8.0 to 10.0. The aqueous capture ammonia may further include ions, e.g., monovalent cations, such as ammonium (NH4+) at a concentration ranging from 0.1 to 5 moles per liter (M), such as from 0.1 to 2 M, including from 0.5 to 3 M, divalent cations, such as calcium (Ca2+) at a concentration ranging from 0.05 to 2 moles per liter (M), such as from 0.1 to 1 M, including from 0.2 to 1 M, divalent cations, such as magnesium (Mg2+) at a concentration ranging from 0.005 to 1 moles per liter (M), such as from 0.005 to 0.1 M, including from 0.01 to 0.5 M, divalent anions, such as sulfate Atty Docket No.: BLUE-061WO (SO42-) at a concentration ranging from 0.005 to 1 moles per liter (M), such as from 0.005 to 0.1 M, including from 0.01 to 0.5 M. Aspects of the methods further include contacting the regenerated aqueous capture ammonia with a gaseous source of CO2, e.g., as described above, under conditions sufficient to produce a CO2 sequestering carbonate, e.g., as described above. In other words, the methods include recycling the regenerated ammonia into the process. In such instances, the regenerated aqueous capture ammonia may be used as the sole capture liquid, or combined with another liquid, e.g., make up water, to produce an aqueous capture ammonia suitable for use as a CO2 capture liquid. Where the regenerated aqueous ammonia is combined with additional water, any convenient water may be employed. Waters of interest from which the aqueous capture ammonia may be produced include, but are not limited to, freshwaters, seawaters, brine waters, produced waters and waste waters. FIG.1 provides an illustration of a one-step membrane mediated ammonia generation protocol. In the illustrated protocol, a produced water sample ("ancient salt water) contains both high concentrations (> 100 mM) of a desired divalent cation (i.e. Ca2+, Mg2+, Sr2+, etc…) and high alkalinity (> 100 mM). As illustrated, a flow purification design utilizes a single step dialysis membrane filtration process with custom dialysis membranes. The configuration can be utilized for recovery of both cations and alkalinity for regeneration of ammonia and calcium in the ammonium acetate reaction solution. FIG.2 provides an illustration of a two-step membrane mediated ammonia generation protocol. In the illustrated protocol, the produced water sample ("ancient salt water") only has the characteristic of high concentration (> 100 mM) of divalent cation (i.e. Ca2+, Mg2+, Sr2+, etc…) or a sample containing only high alkalinity (> 100 mM) but not both. As illustrated, a flow purification design utilizes a two-step membrane process. In the first step, the purification of cation with a custom dialysis membrane is performed. In the second step, the purification of alkalinity with another custom dialysis membrane is performed. The two-step method can be comprised of two different independent produced water samples / flows or a produce water sample subjected to a first step then directed to a second step or a combination thereof. Production of Materials from the CO2Sequestering Carbonate Product The product carbonate material may be further used, manipulated and / or combined with other compositions to produce a variety of end-use materials. In certain Atty Docket No.: BLUE-061WO embodiments, the product carbonate composition is refined (i.e., processed) in some manner. Refinement may include a variety of different protocols. In certain embodiments, the product is subjected to mechanical refinement, e.g., grinding, in order to obtain a product with desired physical properties, e.g., particle size, etc. In certain embodiments, the product is combined with a hydraulic cement, e.g., as a sand, a gravel, as an aggregate, etc., e.g., to produce final product, e.g., concrete or mortar. Also of interest are formed building materials. The formed building materials of the invention may vary greatly. By "formed" is meant shaped, e.g., molded, cast, cut or otherwise produced, into a man-made structure defined physical shape, i.e., configuration. Formed building materials are distinct from amorphous building materials, e.g., particulate (such as powder) compositions that do not have a defined and stable shape, but instead conform to the container in which they are held, e.g., a bag or other container. Illustrative formed building materials include, but are not limited to: bricks; boards; conduits; beams; basins; columns; drywalls etc. Further examples and details regarding formed building materials include those described in U.S. Patent No. 7,771,684; the disclosure of which is herein incorporated by reference. Also of interest are non-cementitious manufactured items that include the product of the invention as a component. Non-cementitious manufactured items of the invention may vary greatly. By non-cementitious is meant that the compositions are not hydraulic cements. As such, the compositions are not dried compositions that, when combined with a setting fluid, such as water, set to produce a stable product. Illustrative compositions include, but are not limited to: paper products; polymeric products; lubricants; asphalt products; paints; personal care products, such as cosmetics, toothpastes, deodorants, soaps and shampoos; human ingestible products, including both liquids and solids; agricultural products, such as soil amendment products and animal feeds; etc. Further examples and details non-cementitious manufactured items include those described in United States Patent No.7,829,053; the disclosure of which is herein incorporated by reference. Aggregates As summarized above, the methods and systems of the invention may be employed to produce carbonate coated seed structures, e.g., carbonate coated aggregates or, optionally without a seed structure, e.g., pure carbonate aggregates, Atty Docket No.: BLUE-061WO rocks, etc., for use in concretes and other applications. The carbonate coated aggregates may be conventional or lightweight aggregates. Aspects of the invention include CO2sequestering aggregate compositions. The CO2sequestering aggregate compositions include aggregate particles having a core and a CO2 sequestering carbonate coating on at least a portion of a surface of the core. The CO2sequestering carbonate coating is made up of a CO2sequestering carbonate material, e.g., as described above. The CO2sequestering carbonate material that is present in coatings of the coated particles of the subject aggregate compositions may vary. In some instances, the isotopic profile of the core of the aggregate differs from the carbonate coating of the aggregate, such that the aggregate has a carbonate coating with a first isotopic profile and a core with a second isotopic profile that is different from the first. In some instances, the carbonate material is a highly reflective microcrystalline / amorphous carbonate material. The microcrystalline / amorphous materials present in coatings of the invention may be highly reflective. As the materials may be highly reflective, the coatings that include the same may have a high total surface reflectance (TSR) value. TSR may be determined using any convenient protocol, such as ASTM E1918 Standard Test Method for Measuring Solar Reflectance of Horizontal and Low-Sloped Surfaces in the Field (see also R. Levinson, H. Akbari, P. Berdahl, Measuring solar reflectance – Part II: review of practical methods, LBNL 2010). In some instances, the backsheets exhibit a TSR value ranging from Rg;0 = 0.0 to Rg;0,= 1.0, such as Rg;0,= 0.25 to Rg;0,= 0.99, including Rg;0,= 0.40 to Rg;0,= 0.98, e.g., as measured using the protocol referenced above. In some instances, the coatings that include the carbonate materials are highly reflective of near infrared (NIR) light, ranging in some instances from 10 to 99%, such as 50 to 99%. By NIR light is meant light having a wavelength ranging from 700 nanometers (nm) to 2.5 millimeters (mm). NIR reflectance may be determined using any convenient protocol, such as ASTM C1371 Standard Test Method for Determination of Emittance of Materials Near Room Temperature Using Portable Emissometers or ASTM G173 Standard Tables for Reference Solar Spectral Irradiances: Direct Normal and Hemispherical on 37° Tilted Surface. In some instances, the coatings exhibit a NIR reflectance value ranging from Rg;0 = 0.0 to Rg;0 = 1.0, such as Rg;0 = 0.25 to Rg;0 = Atty Docket No.: BLUE-061WO 0.99, including Rg;0 = 0.40 to Rg;0 = 0.98, e.g., as measured using the protocol referenced above. In some instances, the carbonate coatings are highly reflective of ultraviolet (UV) light, ranging in some instances from 10 to 99%, such as 50 to 99%. By UV light is meant light having a wavelength ranging from 400 nm and 10 nm. UV reflectance may be determined using any convenient protocol, such as ASTM G173 referenced above. In some instances, the materials exhibit a UV value ranging from Rg;0 = 0.0 to Rg;0 = 1.0, such as Rg;0 = 0.25 to Rg;0 = 0.99, including Rg;0 = 0.4 to Rg;0 = 0.98, e.g., as measured using the protocol referenced above. In some instances, the coatings are reflective of visible light, e.g., where reflectivity of visible light may vary, ranging in some instances from 10 to 99%, such as 10 to 90%. By visible light is meant light having a wavelength ranging from 380 nm to 740 nm. Visible light reflectance properties may be determined using any convenient protocol, such as ASTM G173 referenced above. In some instances, the coatings exhibit a visible light reflectance value ranging from Rg;0 = 0.0 to Rg;0 = 1.0, such as Rg;0 = 0.25 to Rg;0 = 0.99, including Rg;0 = 0.4 to Rg;0 = 0.98, e.g., as measured using the protocol referenced above. The materials making up the carbonate components are, in some instances, amorphous or microcrystalline. Where the materials are microcrystalline, the crystal size, e.g., as determined using the Scherrer equation applied to the FWHM of X-ray diffraction pattern, is small, and in some instances is 1,000 microns (µm) or less in diameter, such as 100 microns or less in diameter, and including 10 microns or less in diameter. In some instances, the crystal size ranges in diameter from 1,000 µm to 0.001 µm, such as 10 to 0.001 µm, including 1 to 0.001 µm. In some instances, the crystal size is chosen in view of the wavelength(s) of light that are to be reflected. For example, where light in the visible spectrum is to be reflected, the crystal size range of the materials may be selected to be less than one-half the "to be reflected" range, so as to give rise to photonic band gap. For example, where the to be reflected wavelength range of light is 100 to 1,000 nm, the crystal size of the material may be selected to be 50 nm or less, such as ranging from 1 to 50 nm, e.g., 5 to 25 nm. In some embodiments, the materials produced by methods of the invention may include rod-shaped crystals and amorphous solids. The rod-shaped crystals may vary in structure, and in certain embodiments have length to diameter ratio ranging from 500 to 1, such as 10 to 1. In certain embodiments, Atty Docket No.: BLUE-061WO the length of the crystals ranges from 0.5 μm to 500 μm, such as from 5 μm to 100 μm. In yet other embodiments, substantially completely amorphous solids are produced. The density, porosity, and permeability of the coating materials may vary according to the application. With respect to density, while the density of the material may vary, in some instances the density ranges from 5 g / cm3to 0.01 g / cm3, such as 3 g / cm3to 0.3 g / cm3and including 2.7 g / cm3to 0.4 g / cm3. With respect to porosity, as determined by Gas Surface Adsorption as determined by the BET method (Brown Emmett Teller (e.g., as described in S. Brunauer, P. H. Emmett and E. Teller, J. Am. Chem. Soc., 1938, 60, 309. doi:10.1021 / ja01269a023) the porosity may range in some instances from 100 m2 / g to 0.1 m2 / g, such as 60 m2 / g to 1 m2 / g and including 40 m2 / g to 1.5 m2 / g. With respect to permeability, in some instances the permeability of the material may range from 0.1 to 100 darcies, such as 1 to 10 darcies, including 1 to 5 darcies (e.g., as determined using the protocol described in H. Darcy, Les Fontaines Publiques de la Ville de Dijon, Dalmont, Paris (1856)). Permeability may also be characterized by evaluating water absorption of the material. As determined by water absorption protocol, e.g., the water absorption of the material ranges, in some embodiments, from 0 to 25%, such as 1 to 15% and including from 2 to 9 %. The hardness of the materials may also vary. In some instances, the materials exhibit a Mohs hardness of 3 or greater, such as 5 or greater, including 6 or greater, where the hardness ranges in some instances from 3 to 8, such as 4 to 7 and including 5 to 6 Mohs (e.g., as determined using the protocol described in American Federation of Mineralogical Societies. "Mohs Scale of Mineral Hardness"). Hardness may also be represented in terms of tensile strength, e.g., as determined using the protocol described in ASTM C1167. In some such instances, the material may exhibit a compressive strength of 100 to 3,000 N, such as 400 to 2,000 N, including 500 to 1,800 N. In some embodiments, the carbonate material includes one or more contaminants predicted not to leach into the environment by one or more tests selected from the group consisting of Toxicity Characteristic Leaching Procedure (TCLP), Extraction Procedure Toxicity Test, Synthetic Precipitation Leaching Procedure, California Waste Extraction Test, Soluble Threshold Limit Concentration, American Society for Testing and Materials Extraction Test, and Multiple Extraction Procedure. Tests and combinations of tests may be chosen depending upon likely contaminants and storage conditions of the composition. For example, in some embodiments, the composition may include As, Cd, Cr, Hg, and Pb (or products thereof), each of which Atty Docket No.: BLUE-061WO might be found in a waste gas stream of a CO2emitter, such as in the flue gas of a coal- fired power plant. Since TCLP tests for As, Ba, Cd, Cr, Pb, Hg, Se, and Ag, TCLP may be an appropriate test for aggregates described herein. In some embodiments, a carbonate composition of the invention includes As, wherein the composition is predicted not to leach As into the environment. For example, a TCLP extract of the composition may provide less than 5.0 mg / L As indicating that the composition is not hazardous with respect to As. In some embodiments, a carbonate composition of the invention includes Cd, wherein the composition is predicted not to leach Cd into the environment. For example, a TCLP extract of the composition may provide less than 1.0 mg / L Cd indicating that the composition is not hazardous with respect to Cd. In some embodiments, a carbonate composition of the invention includes Cr, wherein the composition is predicted not to leach Cr into the environment. For example, a TCLP extract of the composition may provide less than 5.0 mg / L Cr indicating that the composition is not hazardous with respect to Cr. In some embodiments, a carbonate composition of the invention includes Hg, wherein the composition is predicted not to leach Hg into the environment. For example, a TCLP extract of the composition may provide less than 0.2 mg / L Hg indicating that the composition is not hazardous with respect to Hg. In some embodiments, a carbonate composition of the invention includes Pb, wherein the composition is predicted not to leach Pb into the environment. For example, a TCLP extract of the composition may provide less than 5.0 mg / L Pb indicating that the composition is not hazardous with respect to Pb. In some embodiments, a carbonate composition and aggregate that includes of the same of the invention may be non-hazardous with respect to a combination of different contaminants in a given test. For example, the carbonate composition may be non-hazardous with respect to all metal contaminants in a given test. A TCLP extract of a composition, for instance, may be less than 5.0 mg / L in As, 100.0 mg / L in Ba, 1.0 mg / L in Cd, 5.0 mg / mL in Cr, 5.0 mg / L in Pb, 0.2 mg / L in Hg, 1.0 mg / L in Se, and 5.0 mg / L in Ag. Indeed, a majority if not all of the metals tested in a TCLP analysis on a composition of the invention may be below detection limits. In some embodiments, a carbonate composition of the invention may be non-hazardous with respect to all (e.g., inorganic, organic, etc.) contaminants in a given test. In some embodiments, a carbonate composition of the invention may be non-hazardous with respect to all contaminants in any combination of tests selected from the group consisting of Toxicity Characteristic Leaching Procedure, Extraction Procedure Toxicity Test, Synthetic Precipitation Leaching Procedure, Atty Docket No.: BLUE-061WO California Waste Extraction Test, Soluble Threshold Limit Concentration, American Society for Testing and Materials Extraction Test, and Multiple Extraction Procedure. As such, carbonate compositions and aggregates including the same of the invention may effectively sequester CO2(e.g., as carbonates, bicarbonates, or a combinations thereof) along with various chemical species (or co-products thereof) from waste gas streams, industrial waste sources of divalent cations, industrial waste sources of proton-removing agents, or combinations thereof that might be considered contaminants if released into the environment. Compositions of the invention incorporate environmental contaminants (e.g., metals and co-products of metals such as Hg, Ag, As, Ba, Be, Cd, Co, Cr, Cu, Mn, Mo, Ni, Pb, Sb, Se, Tl, V, Zn, or combinations thereof) in a non-leachable form. The aggregate compositions of the invention include particles having a core region and a CO2 sequestering carbonate coating on at least a portion of a surface of the core. The coating may cover 10% or more, 20% or more, 30% or more, 40% or more, 50% or more, 60% or more, 70% or more, 80% or more, 90% or more, including 95% or more of the surface of the core. The thickness of the carbonate layer may vary, as desired. In some instances, the thickness may range from 0.1µm to 10 mm, such as 1 µm to 1,000 µm, including 10 µm to 500 µm. The core of the coated particles of the aggregate compositions described herein may vary widely. The core may be made up of any convenient aggregate material. Examples of suitable aggregate materials include, but are not limited to: natural mineral aggregate materials, e.g., carbonate rocks, sand (e.g., natural silica sand), sandstone, gravel, granite, diorite, gabbro, basalt, etc.; and synthetic aggregate materials, such as industrial byproduct aggregate materials, e.g., blast furnace slag, fly ash, municipal waste, and recycled concrete, etc. In some instances, the core comprises a material that is different from the carbonate coating such as a pellet made from any of the superfine materials referenced above. In some embodiments, the method of producing carbonate aggregates comprises the methods detailed in United States Application Serial No.17 / 297,278 filed on January 23, 2019; the disclosure of which applications is herein incorporated by reference and includes methods whereby the carbonate aggregates are produced optionally without a seed structure, e.g., pure carbonate aggregates. In some instances, the aggregates are lightweight aggregates. In such instances, the core of the coated particles of the aggregate compositions described herein may vary widely, so long as when it is coated it provides for the desired lightweight aggregate Atty Docket No.: BLUE-061WO composition. The core may be made up of any convenient material. Examples of suitable aggregate materials include, but are not limited to: conventional lightweight aggregate materials, e.g., naturally occurring lightweight aggregate materials, such as crushed volcanic rocks, e.g., pumice, scoria or tuff, and synthetic materials, such as thermally treated clays, shale, slate, diatomite, perlite, vermiculite, blast furnace slag, basic oxygen furnace slag, electric arc furnace slag and fly ash; as well as unconventional porous materials, e.g., crushed corals, synthetic materials like polymers and low density polymeric materials, recycled wastes such as wood, fibrous materials, cement kiln dust residual materials, demolished / recycled / returned concrete materials, recycled glass, various volcanic minerals, granite, silica bearing minerals, mine tailings and the like. The physical properties of the coated particles of the aggregate compositions may vary. Aggregates of the invention have a density that may vary so long as the aggregate provides the desired properties for the use for which it will be employed, e.g., for the building material in which it is employed. In certain instances, the density of the aggregate particles ranges from 1.1 to 5 g / cm3, such as 1.3 g / cm3to 3.15 g / cm3, and including 1.8 g / cm3to 2.7 g / cm3. Other particle densities in embodiments of the invention, e.g., for lightweight aggregates, may range from 1.1 to 2.2 g / cm3, e.g., 1.2 to 2.0 g / cm3or 1.4 to 1.8 g / cm3. In some embodiments the invention provides aggregates that range in bulk density (unit weight) from 35 lb / ft3to 200 lb / ft3, or 50 lb / ft3to 200 lb / ft3, or 75 lb / ft3to 175 lb / ft3, or 50 lb / ft3to 100 lb / ft3, or 75 lb / ft3to 125 lb / ft3, or 85 lb / ft3to 115 lb / ft3, or 100 lb / ft3to 200 lb / ft3, or 125 lb / ft3to 150 lb / ft3, or 140 lb / ft3to 160 lb / ft3, or 50 lb / ft3to 200 lb / ft3, or 35 lb / ft3to 200 lb / ft3. Some embodiments of the invention provide lightweight aggregate, e.g., aggregate that has a bulk density (unit weight) of 75 lb / ft3to 125 lb / ft3, such as 90 lb / ft3to 115 lb / ft3. In some instances, the lightweight aggregates have a weight ranging from 50 to 1,200 kg / m3, such as 80 to 11 kg / m3. The hardness of the aggregate particles making up the aggregate compositions of the invention may also vary, and in certain instances the hardness, expressed on the Mohs scale, ranges from 1.0 to 9, such as 1 to 7, including 1 to 6 or 1 to 5. In some embodiments, the Mohs hardness of aggregates of the invention ranges from 2-5, or 2- 4. In some embodiments, the Mohs hardness ranges from 2-6. Other hardness scales may also be used to characterize the aggregate, such as the Rockwell, Vickers, or Brinell scales, and equivalent values to those of the Mohs scale may be used to Atty Docket No.: BLUE-061WO characterize the aggregates of the invention; e.g., a Vickers hardness rating of 250 corresponds to a Mohs rating of 3; conversions between the scales are known in the art. The abrasion resistance of an aggregate may also be important, e.g., for use in a roadway surface, where aggregates of high abrasion resistance are useful to keep surfaces from polishing. Abrasion resistance is related to hardness but is not the same. Aggregates of the invention include aggregates that have an abrasion resistance similar to that of natural limestone, or aggregates that have an abrasion resistance superior to natural limestone, as well as aggregates having an abrasion resistance lower than natural limestone, as measured by art accepted methods, such as ASTM C131. In some embodiments aggregates of the invention have an abrasion resistance of less than 50%, or less than 40%, or less than 35%, or less than 30%, or less than 25%, or less than 20%, or less than 15%, or less than 10%, when measured by ASTM C131 referenced above. Aggregates of the invention may also have a porosity within particular ranges. As will be appreciated by those of skill in the art, in some cases a highly porous aggregate is desired, in others an aggregate of moderate porosity is desired, while in other cases aggregates of low porosity, or no porosity, are desired. Porosities of aggregates of some embodiments of the invention, as measured by water uptake after oven drying followed by full immersion for 60 minutes, expressed as % dry weight, can be in the range of 1 to 40%, such as 2 to 20%, or 2 to 15%, including 2 to 10% or even 3 to 9%. The dimensions of the aggregate particles may vary. Aggregate compositions of the invention are particulate compositions that may in some embodiments be classified as fine or coarse. Fine aggregates according to embodiments of the invention are particulate compositions that almost entirely pass through a No.4 sieve (ASTM C125 and ASTM C33). Fine aggregate compositions according to embodiments of the invention have an average particle size ranging from 10 µm to 4.75 mm, such as 50 µm to 3.0 mm and including 75 µm to 2.0 mm. Coarse aggregates of the invention are compositions that are predominantly retained on a No.4 sieve (ASTM C125 and ASTM C33). Coarse aggregate compositions according to embodiments of the invention are compositions that have an average particle size ranging from 4.75 mm to 200 mm, such as 4.75 to 150 mm in and including 5 to 100 mm. As used herein, "aggregate" may also in some embodiments encompass larger sizes, such as 3 inches (in.) to 12 in. or even 3 in. to 24 in., or larger, such as 12 in. to 48 in., or larger than 48 in. Atty Docket No.: BLUE-061WO In some instances, aggregates as described herein find use as aggregates of internal curing concretes, where the aggregates allow for the release of water over time to fully and evenly hydrate the cementitious components of the concrete. Internal curing aggregate products of such embodiments may be used to improve performance of concrete by increasing autogenous curing and reducing chemical shrinkage, leading to reduced cracking of the concrete body through the slow and uniform release of water throughout the placed concrete. Aspects of these embodiments include the use of internal curing aggregate products as described above to increase the performance of concrete, its various forms and types. As described above, the internal curing aggregate products are composed of, either partially or wholly, sequestered anthropogenic carbon from point source CO2 emitters, such as DAC systems and power plants, refineries and cement plants. The carbon, coming from carbon dioxide gas, is sequestered by methods of carbon capture and mineralization such as those in: U.S. Application Serial Nos. 14 / 204,994 published as US-2014-0322803-A1; 14 / 214,129 published as US 2014- 0271440 A1; and 14 / 861,996 published as US 2016-0082387 A1; as well as U.S. Patent Nos.9,707,513; 9,714,406 and 9,993,799; the disclosures of which are herein incorporated by reference. The captured CO2 results in synthetic limestone in the form of calcium or other divalent cationic carbonate solids composing part or all of the internal curing aggregate products for concrete. Aspects of the invention include use of a rock composed wholly or partially of aggregate for use in concrete, mortar, pavements or other building materials that contain CO2 stemming from DAC systems or the combustion of fossil fuels or other forms of fuels and other CO2 criteria pollutant sources. In some embodiments, aggregates, either fine or coarse, manufactured from methods of carbon capture and mineralization as described above are employed as internal curing aggregates for concrete and meat ASTM Standard Specification for Lightweight Aggregate for Internal Curing of Concrete C1761, which provides guidelines to estimate the amount of lightweight aggregate required for internal curing per unit volume of concrete. Further details regarding the use of aggregates in internal curing concrete applications are provided in U.S. Provisional Application Serial No.62 / 624,022 filed January 30, 2018, the disclosure of which is herein incorporated by reference. Concrete Dry Composites concrete dry composites that, upon combination with a suitable setting liquid (such as described below), produce a settable composition that sets and Atty Docket No.: BLUE-061WO hardens into a concrete or a mortar. Concrete dry composites as described herein include an amount of an aggregate, e.g., as described above, and a cement, such as a hydraulic cement. The term "hydraulic cement" is employed in its conventional sense to refer to a composition which sets and hardens after combining with water or a solution where the solvent is water, e.g., an admixture solution. Setting and hardening of the product produced by combination of the concrete dry composites of the invention with an aqueous liquid results from the production of hydrates that are formed from the cement upon reaction with water, where the hydrates are essentially insoluble in water. Aggregates of the invention find use in place of conventional natural rock aggregates used in conventional concrete when combined with pure Portland cement. Other hydraulic cements of interest in certain embodiments are Portland cement blends. The phrase "Portland cement blend" includes a hydraulic cement composition that includes a Portland cement component and significant amount of a non-Portland cement component. As the cements of the invention are Portland cement blends, the cements include a Portland cement component. The Portland cement component may be any convenient Portland cement. As is known in the art, Portland cements are powder compositions produced by grinding Portland cement clinker (more than 90%), a limited amount of calcium sulfate which controls the set time, and up to 5% minor constituents (as allowed by various standards). When the exhaust gases used to provide carbon dioxide for the reaction contain SOx, then sufficient sulphate may be present as calcium sulfate in the precipitated material, either as a cement or aggregate to offset the need for additional calcium sulfate. As defined by the European Standard EN197.1, "Portland cement clinker is a hydraulic material which shall consist of at least two-thirds by mass of calcium silicates (3CaO·SiO2 and 2CaO·SiO2), the remainder consisting of aluminium- and iron-containing clinker phases and other compounds. The ratio of CaO to SiO2 shall not be less than 2.0. The magnesium content (MgO) shall not exceed 5.0% by mass." The concern about MgO is that later in the setting reaction, magnesium hydroxide (Mg(OH)2), brucite, may form, leading to the deformation and weakening and cracking of the cement. In the case of magnesium carbonate containing cements, brucite will not form as it may with MgO. In certain embodiments, the Portland cement constituent of the present invention is any Portland cement that satisfies ASTM C150 Standard Specification of Portland Cement. ASTM C150 covers eight types of Portland cement, Types I-VIII, each possessing different properties, and used specifically for those properties. Atty Docket No.: BLUE-061WO Also of interest as hydraulic cements are carbonate containing hydraulic cements. Such carbonate containing hydraulic cements, methods for their manufacture and use are described in U.S. Patent No.7,735,274; the disclosure of which applications are herein incorporated by reference. In certain embodiments, the hydraulic cement may be a blend of two or more different kinds of hydraulic cements, such as Portland cement and a carbonate containing hydraulic cement. In certain embodiments, the amount of a first cement, e.g., Portland cement in the blend ranges from 10 to 90% (w / w), such as 30 to 70% (w / w) and including 40 to 60% (w / w), e.g., a blend of 80% OPC and 20% carbonate hydraulic cement. In some instances, the concrete dry composite compositions, as well as concretes produced therefrom, have a CARBONSTAR® Rating (CSR) that is less than the CSR of the control composition that does not include an aggregate of the invention. The CSR is a value that characterizes the embodied carbon (in the form of CaCO3 or other XmCO3) for any product, in comparison to how carbon intensive production of the product itself is (i.e., in terms of the production CO2). The CSR is a metric based on the embodied mass of or offset quantity of CO2 in a unit of concrete. Of the three components in concrete – water, cement and aggregate – cement is by far the most significant contributor to CO2 emissions, roughly 1:1 by mass (1 ton cement produces roughly 1 ton CO2). So, if a cubic yard of concrete uses 600 lb cement, then its CSR is 600. A cubic yard of concrete according to embodiments of the present invention which include 600 lb cement and in which at least a portion of the aggregate is carbonate coated aggregate, e.g., as described above, will have a CSR that is less than 600, e.g., where the CSR may be 550 or less, such as 500 or less, including 400 or less, e.g., 250 or less, such as 100 or less, where in some instances the CSR may be a negative value, e.g., -100 or less, such as -500 or less including -1,000 or less, where in some instances the CSR of a cubic yard of concrete having 600 lbs cement may range from 500 to - 5,000, such as -100 to -4,000, including -500 to -3,000. To determine the CSR of a given cubic yard of concrete that includes carbonate coated aggregate of the invention, an initial value of CO2generated for the production of the cement component of the concrete cubic yard is determined. For example, where the yard includes 600 lbs of cement, the initial value of 600 is assigned to the yard. Next, the amount of carbonate coating in the yard is determined. Since the molecular weight of carbonate is 100 a.u., and 44% of carbonate is CO2, the amount of carbonate coating is present in the yard is Atty Docket No.: BLUE-061WO then multiplied by 44% (0.44) and the resultant value subtracted from the initial value in order to obtain the CSR for the yard. For example, where a given yard of concrete mix is made up of 600 lb of cement, 300 lb of water, 1,429 lb of fine aggregate and 1,739 lb of coarse aggregate, the weight of a yard of concrete is 4,068 lb and the CSR is 600. If 10% of the total mass of aggregate in this mix is replaced by aggregate with a carbonate coating, e.g., as described above, the amount of carbonate present in the revised yard of concrete is 317 lbs. Multiplying this value by 44% yields 139. Subtracting this number from 600 provides a CSR of 461. Settable Compositions Settable compositions of the invention, such as concretes and mortars, are produced by combining a hydraulic cement with an amount of aggregate (fine for mortar, e.g., sand; coarse with or without fine for concrete) and an aqueous liquid, e.g., water, either at the same time or by pre-combining the cement with aggregate, and then combining the resultant dry components with water. The choice of coarse aggregate material for concrete mixes using cement compositions of the invention may have a minimum size of about 3 / 8 inch and can vary in size from that minimum up to one inch or larger, including in gradations between these limits. Finely divided aggregate is smaller than 3 / 8 inch in size and again may be graduated in much finer sizes down to 200-sieve size or so. Fine aggregates may be present in both mortars and concretes of the invention. The weight ratio of cement to aggregate in the dry components of the cement may vary, and in certain embodiments ranges from 1:10 to 4:10, such as 2:10 to 5:10 and including from 55:100 to 70:100. The liquid phase, e.g., aqueous fluid, with which the dry component is combined to produce the settable composition, e.g., concrete, may vary, from pure water to water that includes one or more solutes, additives, co-solvents, etc., as desired. The ratio of dry component to liquid phase that is combined in preparing the settable composition may vary, and in certain embodiments ranges from 2:10 to 7:10, such as 3:10 to 6:10 and including 4:10 to 6:10. In certain embodiments, the cements may be employed with one or more admixtures. Admixtures are compositions added to concrete to provide it with desirable characteristics that are not obtainable with basic concrete mixtures or to modify properties of the concrete to make it more readily useable or more suitable for a particular purpose or for cost reduction. As is known in the art, an admixture is any Atty Docket No.: BLUE-061WO material or composition, other than the hydraulic cement, aggregate and water, that is used as a component of the concrete or mortar to enhance some characteristic, or lower the cost, thereof. The amount of admixture that is employed may vary depending on the nature of the admixture. In certain embodiments the amounts of these components range from 0.1 to 50% w / w, such as 2 to 10% w / w. Admixtures of interest include finely divided mineral admixtures such as cementitious materials; pozzolans; pozzolanic and cementitious materials; and nominally inert materials. Pozzolans include diatomaceous earth, opaline cherts, clays, shales, fly ash, silica fume, volcanic tuffs and pumicites are some of the known pozzolans. Certain ground granulated iron and steel slags and high calcium fly ashes possess both pozzolanic and cementitious properties. Nominally inert materials can also include finely divided raw quartz, dolomites, limestone, marble, granite, and others. Fly ash is defined in ASTM C618. Other types of admixture of interest include plasticizers, accelerators, retarders, air-entrainers, foaming agents, water reducers, corrosion inhibitors, and pigments. As such, admixtures of interest include, but are not limited to: set accelerators, set retarders, air-entraining agents, defoamers, alkali-reactivity reducers, bonding admixtures, dispersants, coloring admixtures, corrosion inhibitors, dampproofing admixtures, gas formers, permeability reducers, pumping aids, shrinkage compensation admixtures, fungicidal admixtures, germicidal admixtures, insecticidal admixtures, rheology modifying agents, finely divided mineral admixtures, pozzolans, aggregates, wetting agents, strength enhancing agents, water repellents, and any other concrete or mortar admixture or additive. Admixtures are well-known in the art and any suitable admixture of the above type or any other desired type may be used; see, e.g., U.S. Patent No.7,735,274, incorporated herein by reference in its entirety. In some instances, the settable composition is produced using an amount of a bicarbonate-rich product (BRP) admixture, which may be liquid or solid form, e.g., as described in U.S. Patent No.9,714,406; the disclosure of which is herein incorporated by reference. In certain embodiments, settable compositions of the invention include a cement employed with fibers, e.g., where one desires fiber-reinforced concrete. Fibers can be made of zirconia containing materials, steel, carbon, fiberglass, or synthetic materials, e.g., polypropylene, nylon, polyethylene, polyester, rayon, high-strength aramid, (i.e. Kevlar®), or mixtures thereof. Atty Docket No.: BLUE-061WO The components of the settable composition can be combined using any convenient protocol. Each material may be mixed at the time of work, or part of or all of the materials may be mixed in advance. Alternatively, some of the materials are mixed with water with or without admixtures, such as high-range water-reducing admixtures, and then the remaining materials may be mixed therewith. As a mixing apparatus, any conventional apparatus can be used. For example, Hobart mixer, slant cylinder mixer, Omni Mixer, Henschel mixer, V-type mixer, and Nauta mixer can be employed. Following the combination of the components to produce a settable composition (e.g., concrete), the settable compositions are in some instances initially flowable compositions, and then set after a given period of time. The setting time may vary, and in certain embodiments ranges from 30 minutes to 48 hours, such as 30 minutes to 24 hours and including from 1 hour to 4 hours. The strength of the set product may also vary. In certain embodiments, the strength of the set cement may range from 5 Mpa to 70 MPa, such as 10 MPa to 50 MPa and including from 20 MPa to 40 MPa. In certain embodiments, set products produced from cements of the invention are extremely durable. e.g., as determined using the test method described in ASTM C1157. Structures Aspects of the invention further include structures produced from the aggregates and settable compositions of the invention. As such, further embodiments include manmade structures that contain the aggregates of the invention and methods of their manufacture. Thus, in some embodiments the invention provides a manmade structure that includes one or more aggregates as described herein. The manmade structure may be any structure in which an aggregate may be used, such as a building, dam, levee, roadway or any other manmade structure that incorporates an aggregate or rock. In some embodiments, the invention provides a manmade structure, e.g., a building, a dam, or a roadway, that includes an aggregate of the invention, where in some instances the aggregate may contain CO2from a fossil fuel source, e.g., as described above. In some embodiments the invention provides a method of manufacturing a structure, comprising providing an aggregate of the invention. Albedo Enhancing Applications Atty Docket No.: BLUE-061WO In some instances, the solid carbonate product may be employed in albedo enhancing applications. Albedo, i.e., reflection coefficient, refers to the diffuse reflectivity or reflecting power of a surface. It is defined as the ratio of reflected radiation from the surface to incident radiation upon it. Albedo is a dimensionless fraction, and may be expressed as a ratio or a percentage. Albedo is measured on a scale from zero for no reflecting power of a perfectly black surface, to 1 for perfect reflection of a white surface. While albedo depends on the frequency of the radiation, as used herein Albedo is given without reference to a particular wavelength and thus refers to an average across the spectrum of visible light, i.e., from about 380 to about 740 nm. As the methods of these embodiments are methods of enhancing albedo of a surface, the methods in some instances result in a magnitude of increase in albedo (as compared to a suitable control, e.g., the albedo of the same surface not subjected to methods of invention) that is .05 or greater, such as 0.1 or greater, e.g., 0.2 or greater, 0.3 or greater, 0.4 or greater, 0.5 or greater, 0.6 or greater, 0.7 or greater, 0.8 or greater, 0.9 or greater, including 0.95 or greater, including up to 1.0. As such, aspects of the subject methods include increasing albedo of a surface to 0.1 or greater, such as 0.2 or greater, e.g., 0.3 or greater, 0.4 or greater, 0.5 or greater, 0.6 or greater, 0.7 or greater, 0.8 or greater, 0.9 or greater, 0.95 or greater, including 0.975 or greater and up to approximately 1.0. Aspects of the methods include associating with a surface of interest an amount of a highly reflective microcrystalline or amorphous material composition, e.g., as described above, effective to enhance the albedo of the surface by a desired amount, such as the amounts listed above. The material composition may be associated with the target surface using any convenient protocol. As such, the material composition may be associated with the target surface by incorporating the material into the material of the object having the surface to be modified. For example, where the target surface is the surface of a building material, such as a roof tile or concrete mixture, the material composition may be included in the composition of the material so as to be present on the target surface of the object. Alternatively, the material composition may be positioned on at least a portion of the target surface, e.g., by coating the target surface with the composition. Where the surface is coated with the material composition, the thickness of the resultant coating on the surface may vary, and in some instances may range from 0.1 mm to 25 mm, such as 2 mm to 20 mm and including 5 mm to 10 mm. Atty Docket No.: BLUE-061WO Applications in use as highly reflective pigments in paints and other coatings like photovoltaic solar panels are also of interest. The albedo of a variety of surfaces may be enhanced. Surfaces of interest include at least partially facing skyward surfaces of both man-made and naturally occurring objects. Man-made surfaces of interest include, but are not limited to: roads, sidewalks, buildings and components thereof, e.g., roofs and components thereof (roof shingles, roofing granules, etc.) and sides, runways, and other man-made structures, e.g., walls, dams, monuments, decorative objects, etc. Naturally occurring surfaces of interest include, but are not limited to: plant surfaces, e.g., as found in both forested and non-forested areas, non-vegetated locations, water, e.g., lake, ocean and sea surfaces, etc. For example, the albedo of colored granules may be readily increased using methods as described herein to produce a carbonate layer on the surface of the colored roofing granules. While the thickness of the layer of carbonate material present on the surface of the colored roofing granules may vary, in some instances the thickness ranges from 0.1 to 200 µm, such as 1 to 150 µm, including 5 to 100 µm. A variety of different types of colored granules may be coated as described above, e.g., to enhance their reflectivity without substantially diminishing their color, if at all. Examples of types of granules that may be coated with a carbonate layer as described herein include roofing granules. Roofing granules that may be coated with a carbonate layer, e.g., to improve their reflectivity without substantially reducing their color, if at all, may include a core formed by crushed and screened mineral materials, which are subsequently coated with one or more color coating layers comprising a binder in which is dispersed one or more coloring pigments, such as suitable metal oxides. Inorganic binders may be employed. The binder can be a soluble alkaline silicate that is subsequently insolubilized by heat or by chemical reaction, such as by reaction between an acidic material and the alkaline silicate, resulting in an insoluble colored coating on the mineral particles. The base particles employed in the process of preparing the roofing granules of the present invention can take several forms. The base particles may be inert core particles. The core particles may be chemically inert materials, such as inert mineral particles, solid or hollow glass or ceramic spheres, or foamed glass or ceramic particles. Suitable mineral particles can be produced by a series of quarrying, crushing, and screening operations, are generally intermediate between sand and gravel in size (that is, between about No.8 Atty Docket No.: BLUE-061WO and about No.70 mesh). The core particles have an average particle size of from about 0.2 mm to about 3 mm, e.g., from about 0.4 mm to about 2.4 mm. In particular, suitably sized particles of naturally occurring materials such as talc, slag, granite, silica sand, greenstone, andesite, porphyry, marble, syenite, rhyolite, diabase, greystone, quartz, slate, trap rock, basalt, and marine shells can be used, as well as manufactured materials such as ceramic grog and proppants, and recycled manufactured materials such as crushed bricks, concrete, porcelain, fire clay, and the like. Solid and hollow glass spheres are available, for example, from Potters Industries Inc., P.O. Box 840, Valley Forge, Pa.19482-0840, such as SPHERIGLASS® solid “A” glass spheres product grade 1922 having a mean size of 0.203 mm, product code 602578 having a mean size of 0.59 mm, BALLOTTINI impact beads product grade A with a size range of 600 to 850 micrometers (Nos.20 to 30 mesh), and QCEL hollow spheres, product code 300 with a mean particle size of 0.090 mm. Glass spheres can be coated or treated with a suitable coupling agent if desired for better adhesion to the binder of the inner coating composition. In the granules, the particles can be coated with a coating composition that includes binder and a pigment. The coating binder can be an inorganic material, such as a metal-silicate binder, for example an alkali metal silicate, such as sodium silicate. The coatings pigments that may be used include, but are not limited to PC-9415 Yellow, PC-9416 Yellow, PC-9158 Autumn Gold, PC-9189 Bright Golden Yellow, V-9186 Iron-Free Chestnut Brown, V-780 Black, V0797 IR Black, V-9248 Blue, PC-9250 Bright Blue, PC-5686 Turquoise, V-13810 Red, V-12600 Camouflage Green, V12560 IR Green, V-778 IR Black, and V-799 Black. Methods as described herein may also be employed to produce frac sands. Frac sands are used in the oil and gas recovery industry to maintain porous void space in fractured geologic structure, so as to maintain geologic fracture integrity. Methods described herein may be employed to produce coated substrates and manufactured sands with tailorable surface coatings that can contribute to the buoyancy of the sand when in fluid flow. Methods as described herein may be employed to produce substrate with a closely regular patterning or irregular patterning of carbonate materials (crystalline or amorphous) as to effectively design the surface of the sands to maintain an above average buoyancy in the flow of fracking fluid, while the fluids are being pumped under very high pressure into the geologic fracture site. In some instances, the methods produce a product with a crystalline or amorphous however unreacted cementitious coating compound, such that upon contact with a second medium, the material could Atty Docket No.: BLUE-061WO react as an expansive cement, providing void space for gas and fluid flow from surrounding geologic structure. This expansive property could be activated by intimate fluid or gas contact, sustained fluid contact, or other magnetic or sound wave activation provided from the geologic surface. Methods of using the carbonate precipitate compounds described herein in varying applications as described above, including albedo enhancing applications, as well as compositions produced thereby, are further described in U.S. Patent No. 9,993,799 and in PCT published application No. WO / 2014 / 144 / 848; the disclosures of which applications are herein incorporated by reference. Recycling In some instances, the methods may include recirculating one or more of the reaction components from one stage of the process to another stage of the process. For example, as described above regenerated aqueous ammonia may be recycled to the CO2 capture stage. Cation salts and / or aggregates produced during ammonia regeneration may be recycled to the carbonate production stage. Waste heat produced at one stage, e.g., CO2 capture, may be employed at another stage, e.g., ammonia regeneration, e.g., as described above. The above are non-limiting examples of embodiments where recycling occurs. Production of Pure CO2 Gas One or more stages of the methods may result in the production of pure CO2 gas. For example, during the production of solid carbonate from the aqueous ammonium carbonate, up to one mol of CO2 may be produced for every 2 mols of ammonium bicarbonate. Alternatively or in addition, the ammonia regeneration step may result in the production of waste CO2. For example, during the ammonia regeneration step, waste CO2 may come from fugitive CO2 lost during heating or may come from alkalinity sources that contained embodied carbonate mineral. While such instances may result in the production of CO2, the overall process sequesters a net amount of CO2in a carbonate compound. Any produced CO2may be substantially pure CO2product gas, which may be sequestered by injection into a subsurface geological location, as described in greater detail below. Therefore, the process is an effective CO2sequestration process. The phrase "substantially pure" means that the product gas is pure CO2or is a CO2containing gas that has a limited amount of other, non-CO2 Atty Docket No.: BLUE-061WO components. Following production of the CO2product gas in such embodiments, aspects of the invention may include injecting the product CO2gas into a subsurface geological location to sequester CO2. By injecting is meant introducing or placing the CO2product gas into a subsurface geological location. Subsurface geological locations may vary, and include both subterranean locations and deep ocean locations. Subterranean locations of interest include a variety of different underground geological formations, such as fossil fuel reservoirs, e.g., oil fields, gas fields and un-mineable coal seams; saline reservoirs, such as saline formations and saline-filled basalt formations; deep aquifers; porous geological formations such as partially or fully depleted oil or gas formations, salt caverns, sulfur caverns and sulfur domes; etc. In some instances, the CO2 product gas may be pressurized prior to injection into the subsurface geological location. To accomplish such pressurization the gaseous CO2 can be compressed in one or more stages with, where desired, after cooling and condensation of additional water. The modestly pressurized CO2 can then be further dried, where desired, by conventional methods such as through the use of molecular sieves and passed to a CO2 condenser where the CO2 is cooled and liquefied. The CO2 can then be efficiently pumped with minimum power to a pressure necessary to deliver the CO2 to a depth within the geological formation or the ocean depth at which CO2 injection is desired. Alternatively, the CO2 can be compressed through a series of stages and discharged as a super critical fluid at a pressure matching that necessary for injection into the geological formation or deep ocean. Where desired, the CO2 may be transported, e.g., via pipeline, rail, truck or other suitable protocol, from the production site to the subsurface geological formation. In some instances, the CO2 product gas is employed in an enhanced oil recovery (EOR) protocol. Enhanced Oil Recovery (abbreviated EOR) is a generic term for techniques for increasing the amount of crude oil that can be extracted from an oil field. Enhanced oil recovery is also called improved oil recovery or tertiary recovery. In EOR protocols, the CO2product gas is injected into a subterranean oil deposit or reservoir. In some embodiments, the CO2product gas is recovered by contact with aqueous capture ammonia, e.g., as described above, to produce a solid CO2sequestering carbonate, e.g., as described above. For example, the CO2product gas from one stage of a method may be combined with fugitive aqueous capture ammonia vapor from another, separate stage of a method, to produce aqueous ammonium Atty Docket No.: BLUE-061WO carbonate that is used in a different stage of a method to produce a solid CO2sequestering carbonate, e.g., as described above. CO2gas production and sequestration thereof are further described in United States Application No.14 / 861,996 published as US 2016-0082387 A1 and now issued as U.S. Patent No.10,197,747, the disclosure of which is herein incorporated by reference. SYSTEMS Aspects of the invention further include systems for sequestering CO2 from a gaseous source of CO2 via a protocol such as described above. A system is an apparatus that includes functional modules or reactors, e.g., as described above, that are operatively coupled in a manner sufficient to perform methods of the invention, e.g., as described above. In some embodiments, aspects of such systems include: a CO2 gas / aqueous capture module and a carbonate production module. In some embodiments, aspects of such systems include a combine CO2 gas / aqueous capture module carbonate production module. In some instances, the systems include one or more of an aqueous capture ammonia module; a carbonate production module; and an aqueous capture ammonia regeneration module. In some instances, the CO2 gas / aqueous capture ammonia module comprises a hollow fiber membrane contactor. In some instances, the CO2 gas / aqueous capture ammonia module comprises a regenerative froth contactor. In some instances, the CO2 gas / aqueous capture ammonia module contains a combination of contactors, e.g., as described above, in different arrangements. In some instances, the system is operatively coupled to a gaseous source of CO2. As described above, the gaseous source of CO2 may be a multi-component gaseous stream, such as a flue gas. Operably coupled to the CO2 gas / aqueous capture ammonia module is a carbonate production module. Embodiments of modules include continuous reactors that are configured for producing CO2sequestering carbonate materials. As the systems include continuous reactors (i.e., flow reactors), they include reactors in which materials are carried in a flowing stream, where reactants (e.g., divalent cations, aqueous bicarbonate rich liquid, etc.) are continuously fed into the reactor and emerge as continuous stream of product. The continuous reactor components of the systems are therefore not batch reactors. A given system may include the continuous reactors, e.g., Atty Docket No.: BLUE-061WO as described herein, in combination with one or more additional elements, as described in greater detail below. In some embodiments, continuous reactors of the systems include: a flowing aqueous liquid, e.g., an aqueous ammonium carbonate; a divalent cation introducer configured to introduce divalent cations at an introduction location into the flowing aqueous liquid; and a non-slurry solid phase CO2sequestering carbonate material production location which is located at a distance from the divalent cation introducer. The flowing aqueous liquid is a stream of moving aqueous liquid, e.g., as described above, which may be present in the continuous reactor, where the continuous reactor may have any convenient configuration. Continuous reactors of interest include an inlet for a liquid and an outlet for the waste liquid, where the inlet and outlet are arranged relative to each other to provide for continuous movement or flow of the liquid into and out of the reactor. The reactor may have any convenient structure, where in some instances the reactor may have a length along which the liquid flows that is longer than any given cross sectional dimension of the reactor, where the inlet is at a first end of the reactor and the outlet is at a second end of the reactor. The volume of the reactor may vary, ranging in some instances from 10 L to 1,000,000 L, such as 1,000 L to 100,000 L. Continuous reactors of interest further include a divalent cation introducer configured to introduce divalent cations at an introduction location into the flowing aqueous liquid. Any convenient introducer may be employed, where the introducer may be a liquid phase or solid phase introducer, depending on the nature of the divalent cation source. The introducer may be located in some instances at substantially the same, if not the same, position as the inlet for the bicarbonate rich product containing liquid. Alternatively, the introducer may be located at a distance downstream from the inlet. In such instances, the distance between the inlet and the introducer may vary, ranging in some embodiments from 1 cm to 10 m, such as 10 cm to 1 m. The introducer may be operatively coupled to a source or reservoir of divalent cations. Continuous reactors of interest also include a non-slurry solid phase CO2sequestering carbonate material production location. This location is a region or area of the continuous reactor where a non-slurry solid phase CO2sequestering carbonate material is produced as a result of reaction of the divalent cations with bicarbonate ions of the bicarbonate rich product containing liquid. The reactor may be configured to produce any of the non-slurry solid phase CO2sequestering carbonate materials described above in the production location. In some instances, the production location is Atty Docket No.: BLUE-061WO located at a distance from the divalent cation introduction location. While this distance may vary, in some instances the distance between the divalent cation introducer and the material production location ranges from 1 cm to 10 m, such as 10 cm to 1 m. The production location may include seed structure(s), such as described above. In such instances, the reactor may be configured to contact the seed structures in a submerged or non-submerged format, such as described above. In non-submerged formats, the flowing liquid may be present on the surface of seed structures as a layer, e.g., of varying thickness, but a gas, e.g., air, separates at least two portions of the seed structure, e.g., two different particles, such that the particles are not submerged in the liquid. Further details regarding such reactors that may be employed as carbonate production modules in embodiments of the present systems are provide in U.S. Patent No.9,993,799; the disclosure of which is herein incorporated by reference. The aqueous capture ammonia regeneration module may vary so long it is configured to produce ammonia from the aqueous ammonium organic acid salt, e.g., via dialysis, such as described above. In some instances, the system is configured to recycle regenerated aqueous capture ammonia to the CO2 gas / aqueous capture ammonia module, e.g., as described above. In some instances, the systems and modules thereof are industrial scale systems, by which is meant that they are configured to process industrial scale amounts / volumes of input compositions (e.g., gases, liquids, solids, etc.). For example, the systems and modules thereof, e.g., CO2 contactor modules, carbonate production modules, ammonia regeneration modules, etc., are configured to process industrial scale volumes of liquids, e.g., 1,000 gal / day or more, such as 10,000 gal / day or more, including 25,000 gal / day or more, where in some instances, the systems and modules thereof are configured to process 1,000,000,000 gal / day or less, such as 500,000,000 gal / day or less. Similarly, the systems and modules thereof, e.g., CO2 contactor modules, etc., are configured to process industrial scale volumes of gases, e.g., 25,000 cubic feet / hour or more, such as 100,000 cubic feet / hour or more, including 250,000 cubic feet / hour or more, where in some instances, the systems and modules thereof are configured to process 500,000,000 cubic feet / hour or less, such as 100,000,000 cubic feet / hour or less. In some embodiments, a system is in fluidic communication with a source of aqueous media, such as a naturally occurring or man-made source of aqueous media, Atty Docket No.: BLUE-061WO and may be co-located with a location where a CO2sequestration protocol is conducted. The systems may be present on land or sea. For example, a system may be a land based system that is in a coastal region, e.g., close to a source of sea water, or even an interior location, where water is piped into the system from a salt water source, e.g., an ocean. Alternatively, a system may be a water based system, i.e., a system that is present on or in water. Such a system may be present on a boat, ocean-based platform etc., as desired. In certain embodiments, a system may be co-located with an industrial plant, e.g., a power plant, at any convenient location. In addition to the above components, systems of the invention further include a source of CO2containing gas, which component generates CO2containing gas that is introduced into the aqueous capture module, e.g., as described above. The following is offered by way of illustration and not by way of limitation. EXPERIMENTAL Example 1. Methods to Making CaCO3Minerals and Aggregates from Produced Waters The composition of produced waters will vary from wellsite to wellsite, but can be categorized into two types which would be feedstocks for a Blue Planet process. These being feedstocks containing mutually exclusive chemical properties and never both: a source of alkalinity and a source of metal ion binding. Through various iterations, these feedstocks can be further refined and concentrated to enhance the mineralization of CaCO3 for use as an aggregate. Method 1 (Equi-volume bulk mixing) By bulk mixing an equi-volume of an alkaline produced water feedstock and a Ca2+containing produced water feedstock, various fractions can be precipitated so CaCO3 is produced out of solution due to the concentration of the alkalinity and Ca2+already present in the produced waters. These precipitates will contain a mixtures of other ions present in the produced waters i.e. NaCl, KCl, SO4-, Mg2+, Br2+, and may require subsequent post-processing to remove these carry-over salts that are mineralized within the precipitated CaCO3. Atty Docket No.: BLUE-061WO Method 2 (Laminar, unidirectional flow) In flowing two streams of an alkaline feedstock and a Ca2+into one confined flow, a laminar flow behavior can be achieved such that one contact surface is exposed to enable diffusional chemical mixing between the two flows can occur without bulk mixing (see Method 1). In this case, depending on the amount of time for diffusion mixing to occur Ca2+and CO32-ions can diffuse to form mineralization precursors at the interface of the two flowing streams. Method 3 (Dialysis / Nanofiltration membrane filtration) Through use of dialysis / nanofiltration, specific moieties can be pre-filtered from the produce water feedstocks such that concentrated reagents for mineralization can be obtained. These include filtration for alkalinity, Ca2+, CO32-that all contribute to formation of CaCO3 minerals. An advantage of this method is the ability to mineralize without spectator ions and the possibility of contamination of non-Ca2+and non-CO32-ions. Example 2. A model that incorporates alkalinity regeneration into CaCO3 production The embodiment is a model that demonstrates the use of produced / brine water as a source of calcium for the production of CaCO3 aggregate material. It includes elements of an alkalinity regeneration unit integrated into a CaCO3 production facility using produced / brine water as a geomass source. The major components of this system include a calcium rich brine input, acetic acid to exchange chloride for acetate, CO2 absorption and CaCO3 mineralization, ammonium acetate is recycled then treated to provide aqueous ammonium hydroxide and acetic acid, and output of filtered, solid CaCO3. See FIG.3 for further details. Example 3. Mechanically pressing CaCO3 constituents into a material This embodiment demonstrates the ability to tune the physical characteristics, such as density, structure, and strength properties, of a CaCO3material (e.g., as produced using protocols described herein), as a function of an applied physical force during material formation. The abundance of CaCO3in the material can range from 0.1- 99.9% composition. Specifically, through use of applied forces during the formation of the material, a diverse set of physical properties in the formed CaCO3material is controlled. In the case of a centrifugal, rotation action, a force normal to the rotation is measured to be in the range of 100-200 PSI such that proximal CaCO3constituents Atty Docket No.: BLUE-061WO agglomerate to produce a continuous solid. Through an increase in applied force, such as a uniaxial mechanical pressing force in the range of 1000-15000 PSI, the ultrastructure of the CaCO3constituents can be modified in the form of pore size, pore size dispersity, grain boundaries, grain size, and aggregation. At higher forces, 25000- 35000 PSI range grain boundaries and sizes are further manipulated and the overall composition, microstructure of the CaCO3material can vary, such as decreasing moisture content with increasing forces, subsequently increasing the density and strength of the resulting CaCO3 material aggregate. See Figure 4. In at least some of the previously described embodiments, one or more elements used in an embodiment can interchangeably be used in another embodiment unless such a replacement is not technically feasible. It will be appreciated by those skilled in the art that various other omissions, additions and modifications may be made to the methods and structures described above without departing from the scope of the claimed subject matter. All such modifications and changes are intended to fall within the scope of the subject matter, as defined by the appended claims. It will be understood by those within the art that, in general, terms used herein, and especially in the appended claims (e.g., bodies of the appended claims) are generally intended as “open” terms (e.g., the term “including” should be interpreted as “including but not limited to,” the term “having” should be interpreted as “having at least,” the term “includes” should be interpreted as “includes but is not limited to,” etc.). It will be further understood by those within the art that if a specific number of an introduced claim recitation is intended, such an intent will be explicitly recited in the claim, and in the absence of such recitation no such intent is present. For example, as an aid to understanding, the following appended claims may contain usage of the introductory phrases “at least one” and “one or more” to introduce claim recitations. However, the use of such phrases should not be construed to imply that the introduction of a claim recitation by the indefinite articles “a” or “an” limits any particular claim containing such introduced claim recitation to embodiments containing only one such recitation, even when the same claim includes the introductory phrases “one or more” or “at least one” and indefinite articles such as “a” or “an” (e.g., “a” and / or “an” should be interpreted to mean “at least one” or “one or more”); the same holds true for the use of definite articles used to introduce claim recitations. In addition, even if a specific number of an introduced claim recitation is explicitly recited, those skilled in the art will recognize that Atty Docket No.: BLUE-061WO such recitation should be interpreted to mean at least the recited number (e.g., the bare recitation of “two recitations,” without other modifiers, means at least two recitations, or two or more recitations). Furthermore, in those instances where a convention analogous to “at least one of A, B, and C, etc.” is used, in general such a construction is intended in the sense one having skill in the art would understand the convention (e.g., “ a system having at least one of A, B, and C” would include but not be limited to systems that have A alone, B alone, C alone, A and B together, A and C together, B and C together, and / or A, B, and C together, etc.). In those instances where a convention analogous to “at least one of A, B, or C, etc.” is used, in general such a construction is intended in the sense one having skill in the art would understand the convention (e.g., “ a system having at least one of A, B, or C” would include but not be limited to systems that have A alone, B alone, C alone, A and B together, A and C together, B and C together, and / or A, B, and C together, etc.). It will be further understood by those within the art that virtually any disjunctive word and / or phrase presenting two or more alternative terms, whether in the description, claims, or drawings, should be understood to contemplate the possibilities of including one of the terms, either of the terms, or both terms. For example, the phrase “A or B” will be understood to include the possibilities of “A” or “B” or “A and B.” In addition, where features or aspects of the disclosure are described in terms of Markush groups, those skilled in the art will recognize that the disclosure is also thereby described in terms of any individual member or subgroup of members of the Markush group. As will be understood by one skilled in the art, for any and all purposes, such as in terms of providing a written description, all ranges disclosed herein also encompass any and all possible sub-ranges and combinations of sub-ranges thereof. Any listed range can be easily recognized as sufficiently describing and enabling the same range being broken down into at least equal halves, thirds, quarters, fifths, tenths, etc. As a non-limiting example, each range discussed herein can be readily broken down into a lower third, middle third and upper third, etc. As will also be understood by one skilled in the art all language such as “up to,” “at least,” “greater than,” “less than,” and the like include the number recited and refer to ranges which can be subsequently broken down into sub-ranges as discussed above. Finally, as will be understood by one skilled in the art, a range includes each individual member. Thus, for example, a group having 1-3 articles refers to groups having 1, 2, or 3 articles. Similarly, a group having 1-5 articles Atty Docket No.: BLUE-061WO refers to groups having 1, 2, 3, 4, or 5 articles, and so forth. Although the foregoing invention has been described in some detail by way of illustration and example for purposes of clarity of understanding, it is readily apparent to those of ordinary skill in the art in light of the teachings of this invention that certain changes and modifications may be made thereto without departing from the spirit or scope of the appended claims. Accordingly, the preceding merely illustrates the principles of the invention. It will be appreciated that those skilled in the art will be able to devise various arrangements which, although not explicitly described or shown herein, embody the principles of the invention and are included within its spirit and scope. Furthermore, all examples and conditional language recited herein are principally intended to aid the reader in understanding the principles of the invention and the concepts contributed by the inventors to furthering the art, and are to be construed as being without limitation to such specifically recited examples and conditions. Moreover, all statements herein reciting principles, aspects, and embodiments of the invention as well as specific examples thereof, are intended to encompass both structural and functional equivalents thereof. Additionally, it is intended that such equivalents include both currently known equivalents and equivalents developed in the future, i.e., any elements developed that perform the same function, regardless of structure. Moreover, nothing disclosed herein is intended to be dedicated to the public regardless of whether such disclosure is explicitly recited in the claims. The scope of the present invention, therefore, is not intended to be limited to the exemplary embodiments shown and described herein. Rather, the scope and spirit of present invention is embodied by the appended claims. In the claims, 35 U.S.C. §112(f) or 35 U.S.C. §112(6) is expressly defined as being invoked for a limitation in the claim only when the exact phrase "means for" or the exact phrase "step for" is recited at the beginning of such limitation in the claim; if such exact phrase is not used in a limitation in the claim, then 35 U.S.C. § 112 (f) or 35 U.S.C. §112(6) is not invoked.

Claims

Atty Docket No.: BLUE-061WO WHAT IS CLAIMED IS:

1. A method of sequestering CO2from a gaseous source of CO2, the method comprising: (a) contacting an aqueous ammonia capture liquid with a gaseous source of CO2 under conditions sufficient to produce a CO2 sequestering carbonate and an aqueous ammonium organic acid salt; and (b) subjecting the aqueous ammonium organic acid salt to dialysis filtration to produce a regenerated aqueous ammonia capture liquid; to sequester CO2 from the gaseous source of CO2.

2. The method according to Claim 1, wherein step (a) comprises contacting the aqueous ammonia capture liquid with the gaseous source of CO2 under conditions sufficient to produce an aqueous ammonium carbonate and then contacting the aqueous ammonium carbonate with a cation source to produce the CO2 sequestering carbonate.

3. The method according to Claim 1, wherein step (a) comprises contacting the aqueous ammonia capture liquid that includes a cation source with the gaseous source of CO2 under conditions sufficient to produce the CO2 sequestering carbonate and the aqueous ammonium organic acid salt.

4. The method according to any of the preceding claims, wherein the aqueous ammonium organic acid salt comprises an ammonium salt with an organic acid selected from the group consisting of acetic acid, maleic acid, butyric acid, aspartic acid, malonic acid, citric acid, fumaric acid, lactic acid, succinic acid, pyruvic acid, phosphoric acid, carbonic acid, propionic acid, oxalic acid, glyoxylic acid, glycolic acid, acrylic acid, propiolic acid, tartronic acid, mesoxalic acid, dihydroxymalonic acid, hydracrylic acid, glycidic acid, butyric acid, isobutyric acid, acetoacetic acid, oxaloacetic acid, malic acid, tartaric acid, valeric acid, iso-valeric acid, glutaric acid, alpha-ketoglutaric acid, caproic acid, adipic acid, isocitric acid, enanthic acid, pimelic acid, caprylic acid, phthalic acid, pelargonic acid, cinnamic acid, capric acid, sebacic acid, lauric acid, mellitic acid, tridecylic acid, myristic acid, pentadecylic acid, palmitic acid, margaric acid, stearic acid, nonadecylic acid, arachidic acid, behenic acid, tricosylic acid, lignoceric acid, pentacosylic acid, and cerotic acid, and combinations thereof.Atty Docket No.: BLUE-061WO 5. The method according to Claim 4, wherein the aqueous ammonium organic acid salt comprises ammonium acetate.

6. The method according to Claim 5, wherein the dialysis regeneration comprises a dialysis protocol selected from the group consisting of diffusion dialysis, electrodialysis and nanofiltration.

7. The method according to any of the preceding claims, wherein the dialysis regeneration employs a single-step membrane mediated dialysis regeneration protocol.

8. The method according to any of Claims 1 to 6, wherein the dialysis regeneration employs a two-step membrane mediated dialysis regeneration protocol.

9. The method according to any of the preceding claims, wherein the dialysis regeneration employs a brine.

10. The method according to Claim 9, wherein the brine comprises produced water.

11. The method according to any of Claims 2 to 10, wherein the cation source comprises an alkaline earth metal cation.

12. The method according to Claim 11, wherein the cation source is a source of divalent cations.

13. The method according to Claim 12, wherein the divalent cations comprise alkaline earth metal cations.

14. The method according to Claim 13, wherein the divalent alkaline earth metal cations are selected from the group consisting of Ca2+and Mg2+, and combinations thereof.

15. The method according to any of the preceding claims, wherein the production of the CO2sequestering carbonate produces CO2gas.Atty Docket No.: BLUE-061WO 16. The method according to Claim 15, wherein the produced CO2gas is recovered by contact with an aqueous capture ammonia liquid.

17. The method according to any of the preceding claims, wherein the method further comprises purification of the regenerated aqueous ammonia.

18. The method according to Claim 17, wherein the purification comprises stripping aqueous capture ammonia from the regenerated aqueous ammonia.

19. The method according to any of Claims 1 to 16, wherein the method does not comprise purification of the regenerated aqueous ammonia.

20. The method according to any of the preceding claims, wherein the gaseous source of CO2 comprises flue gas.

21. The method according to any of the preceding claims, wherein the method produces a CO2 sequestering aggregate.

22. A system for sequestering CO2 from a gaseous source of CO2, the system comprising: (a) a CO2 gas / aqueous capture liquid module; and (b) an aqueous capture liquid dialysis regeneration module coupled to a CO2 sequestering carbonate production module.

23. The system according to Claim 22, wherein the system further comprises a CO2 sequestering carbonate production module operatively coupled to a CO2 gas / aqueous capture liquid module.

24. The system according to Claim 22, wherein the system does not include a CO2sequestering carbonate production module separate from the CO2gas / aqueous capture liquid module.

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