EXTRACTION OF CARBON DIOXIDE FROM WATER RELATED APPLICATIONS This application claims priority under 35 U.S.C. § 119(e) to U.S. Provisional Patent Application No.63/376,448, filed September 21, 2022, and entitled “Extractive Desorption of Molecular CO2 From Sub-Saturated Aqueous Solutions,” which is incorporated herein by reference in its entirety for all purposes. GOVERNMENT SPONSORSHIP This invention was made with Government support under DE-AR0001409 awarded by the U.S. Department of Energy. The Government has certain rights in the invention. TECHNICAL FIELD Systems and methods related to the extraction of carbon dioxide (CO ₂ ) from water are generally described. BACKGROUND Conventional processes for the extraction of CO2 from seawater generally rely on the protonation of the water feed stream to convert dissolved inorganic carbons (DICs) to molecularly soluble CO ₂ or carbonic acid. Since the fugacity (or partial pressure) of CO ₂ in the acidified seawater is low, conventional processes utilize a vacuum to desorb CO ₂ as a pure stream suitable for pressurization for either geologic storage or utilization. To avoid the simultaneous desorption of naturally dissolved dioxygen (O2) and dinitrogen (N2), the seawater can be degassed by a vacuum prior to protonation of the water feed water stream, incurring significant capital costs and energy penalties. Accordingly, improved systems and methods for the removal of CO2 from water are needed. SUMMARY The present disclosure is related to systems and methods for the extraction of CO ₂ from water. The subject matter of the present invention involves, in some cases, interrelated products, 8913774.1 alternative solutions to a particular problem, and/or a plurality of different uses of one or more systems and/or articles. According to certain embodiments, a system for removing CO2 from water is described. In some embodiments, the system comprises a water treatment unit configured to adjust pH of the water comprising one or more carbon-containing species from a first pH level to a second pH level that is lower than the first pH level to convert at least some of the one or more carbon- containing species to CO ₂ . In certain embodiments, the system comprises a CO ₂ -extraction unit comprising a CO2-permeable membrane, wherein the CO2-extraction unit is configured to comprise a CO2-extraction solution, and wherein the CO2-extraction unit is configured to remove the CO ₂ from the water across the CO ₂ -permeable membrane into the CO ₂ -extraction solution. In some embodiments, the system comprises a water regeneration unit configured to adjust the pH of the water from the second pH level to the first pH level. According to some embodiments, a system for removing CO2 from water comprises a CO ₂ -extraction unit comprising a CO ₂ -permeable membrane, wherein the CO ₂ -extraction unit is configured to comprise a CO2-extraction solution comprising a CO2-extractor, and wherein the CO2-extraction unit is configured to remove the CO2 from the water across the CO2-permeable membrane into the CO ₂ -extraction solution to produce a CO ₂ -complexed CO ₂ -extractor. In certain embodiments, the system comprises an electrochemical cell fluidically connected to the CO2-extraction unit, wherein the electrochemical cell comprises an anode chamber and a cathode chamber, wherein an outlet of the CO ₂ -extraction unit is fluidically connected to an inlet of the anode chamber such that the system is configured to: (i) flow the CO ₂ -extraction solution comprising the CO2-complexed CO2-extractor from the CO2-extraction unit to the anode chamber,; and (ii) oxidize at least a portion of the CO2-extraction solution in the anode chamber to release CO ₂ from the CO ₂ -complexed CO ₂ -extractor. In certain embodiments, a method for removing CO2 from water is described. In some embodiments, the method comprises adjusting pH of the water comprising one or more carbon- containing species from a first pH level to a second pH level that is lower than the first pH level to convert at least some of the one or more carbon-containing species to the CO2. In certain embodiments, the method comprises exposing the water comprising the CO2 to a CO2-extraction unit comprising a CO ₂ -permeable membrane. In some embodiments, the method comprises exposing a CO ₂ -extraction solution to the CO ₂ -extraction unit. In certain embodiments, the 8913774.1 method comprises removing the CO ₂ from the water across the CO ₂ -permeable membrane into the CO2-extraction solution. In some embodiments, the method comprises adjusting the pH of the water from the second pH level to the first pH level. According to some embodiments, a method for removing CO ₂ from water comprises exposing the water comprising the CO2 to a CO2-extraction unit comprising a CO2-permeable membrane. In certain embodiments, the method comprises exposing a CO2-extraction solution comprising a CO ₂ -extractor to the CO ₂ -extraction unit comprising the CO ₂ -permeable membrane. In some embodiments, the method comprises removing the CO2 from the water across the CO2-permeable membrane into the CO2-extraction solution to produce a CO2- complexed CO ₂ -extractor. In certain embodiments, the method comprises flowing the CO ₂ - extraction solution comprising the CO ₂ -complexed CO ₂ -extractor from an outlet of the CO ₂ - extraction unit to an inlet of an anode chamber of an electrochemical cell. In some embodiments, the method comprises oxidizing at least a portion of the CO2-extraction solution in the anode chamber to release CO ₂ from the CO ₂ -complexed CO ₂ -extractor. According to certain embodiments, a system for removing CO2 from water comprises a CO2-extraction unit comprising a CO2-permeable membrane configured to remove the CO2 from the water, wherein the water comprises the CO ₂ at a partial pressure of greater than or equal to 0.01 bar and at least one gas other than CO2 at a partial pressure of greater than or equal to 0.01 bar. Other advantages and novel features of the present invention will become apparent from the following detailed description of various non-limiting embodiments of the invention when considered in conjunction with the accompanying figures. In cases where the present specification and a document incorporated by reference include conflicting and/or inconsistent disclosure, the present specification shall control. If two or more documents incorporated by reference include conflicting and/or inconsistent disclosure with respect to each other, then the document having the later effective date shall control. BRIEF DESCRIPTION OF THE DRAWINGS Non-limiting embodiments of the present invention will be described by way of example with reference to the accompanying figures, which are schematic and are not intended to be drawn to scale. In the figures, each identical or nearly identical component illustrated is 8913774.1 typically represented by a single numeral. For purposes of clarity, not every component is labeled in every figure, nor is every component of each embodiment of the invention shown where illustration is not necessary to allow those of ordinary skill in the art to understand the invention. In the figures: FIG.1 shows a schematic diagram of a system for removing CO2 from water, in accordance with certain embodiments. FIG.2 shows a schematic diagram of an electrochemical system for removing CO ₂ from water, in accordance with certain embodiments. FIG.3A shows, according to certain embodiments, a schematic diagram of a conventional system for removing CO ₂ from seawater. FIG.3B shows, according to certain embodiments, a schematic diagram of a system for removing CO2 from seawater. FIG.4A shows, according to certain embodiments, organic redox systems for removing CO ₂ from water. FIG.4B shows, according to certain embodiments, an electrochemically mediated amine regeneration (EMAR) system for removing CO2 from water. FIG.4C shows, according to certain embodiments, a pH swing system for removing CO ₂ from water. FIG.4D shows, according to certain embodiments, a bipolar membrane electrodialysis system for removing CO ₂ from water. FIG.5A shows, according to certain embodiments, a schematic diagram of removing CO2 from acidified seawater across a membrane into an extractant. FIG.5B shows, according to certain embodiments, a schematic diagram of using a membrane contactor for CO ₂ extraction. FIG.5C shows, according to certain embodiments, distilled water (left) and an aqueous solution of a quinone (right) after passing through a membrane contactor. FIG.6 shows, according to certain embodiments, a cyclic voltammogram (CV) of anthraquinone-2,7-disulfonic acid. FIG.7A shows, according to certain embodiments, a schematic diagram of a CO2 extraction system using a quinone, wherein CO ₂ is extracted from a water phase by the electrochemical reduction of the quinone. 8913774.1 FIG.7B shows, according to certain embodiments, a schematic diagram of the CO ₂ extraction system using the quinone shown in FIG.7A, wherein CO2 is desorbed from the quinone by electrochemical oxidation. FIG.8 shows, according to certain embodiments, the CO ₂ concentration at an outlet of a quinone reservoir in the CO2 extraction system shown in FIGS.7A-7B as a function of time. FIG.9A shows, according to certain embodiments, a schematic diagram of an ocean capture system combined with a quinone-based CO ₂ extraction system, wherein CO ₂ is extracted from a water phase by the electrochemical reduction of the quinone. FIG.9B shows, according to certain embodiments, a schematic diagram of the ocean capture system combined with the quinone-based CO ₂ extraction system shown in FIG.9A, wherein CO ₂ is desorbed from the quinone by electrochemical oxidation. FIG.10 shows, according to certain embodiments, the volumetric gas flow rate from the ocean capture system combined with the quinone-based CO2 extraction system shown in FIGS. 9A-9B as a function of time. FIG.11 shows, according to certain embodiments, a schematic diagram of an extractant mediated direct ocean capture (DOC) system. FIG.12A shows, according to certain embodiments, a schematic diagram of a schematic diagram of a conventional system for removing CO2 from water that utilizes a single stage degassing system. FIG.12B shows, according to certain embodiments, the CO2-extraction effectiveness of the system shown in FIG.12A. FIG.13A shows, according to certain embodiments, a schematic diagram of a schematic diagram of a conventional system for removing CO2 from water that utilizes a double stage degassing system. FIG.13B shows, according to certain embodiments, the CO2-extraction effectiveness of the system shown in FIG.13A. DETAILED DESCRIPTION Systems and methods related to the extraction of CO2 from water are generally described. According to certain embodiments, the system comprises a CO ₂ -extraction unit comprising a CO ₂ -permeable membrane. The CO ₂ -permeable membrane may separate a water flow chamber 8913774.1 of the CO ₂ -extraction unit (e.g., configured to flow the water) from a CO ₂ -extraction solution flow chamber of the CO2-extracion unit (e.g., configured to flow a CO2-extraction solution comprising a CO2-extrcator) such that dissolved CO2 in the water permeates through the CO2- permeable membrane and complexes with the CO ₂ -extractor in the CO ₂ -extraction solution. The CO2-extractor advantageously has a comparatively high affinity for CO2 as compared to other gases that may be dissolved in the water (e.g., N2 and/or O2), resulting in a CO2-extraction system that complexes CO ₂ even under low partial pressures of CO ₂ . The CO ₂ -permeable membrane may be configured to prevent contamination of the CO2-extraction solution by the water and/or loss of the CO2-extraction solution to the water. In some embodiments, for example, the CO ₂ -permeable membrane may comprise a plurality of pores comprising air (e.g., air plastron) that prevent the water and the CO ₂ -extraction solution in the CO ₂ -extraction unit from mixing. After the CO2-extractor complexes the CO2 to form a CO2-complexed CO2-extractor, the CO ₂ -extraction solution may flow to a CO ₂ -extraction solution regeneration unit to: (i) release CO2 from the CO2-complexed CO2-extractor; and (ii) regenerate the CO2-extractor. In certain embodiments, for example, the CO2-extraction solution regeneration unit comprises an electrochemical cell, and the CO ₂ -extraction solution may be oxidized in an anode chamber of the electrochemical cell to release CO2 from the CO2-complexed CO2-extractor. The CO2- extraction solution comprising the CO2 released from the CO2-extractor may then flow to a flash tank to remove CO ₂ from the CO ₂ -extraction solution. After removing CO ₂ in the flash tank, the CO ₂ -extraction solution may flow to a cathode chamber of the electrochemical cell to reduce the CO2-extraction solution and regenerate the CO2-extractant. After regenerating the CO2- extractant, the CO2-extraction solution may flow to the CO2-extraction unit to extract more CO2 from water. In certain aspects, the systems described herein advantageously do not comprise a degasification unit and/or a vacuum configured to remove one or more gases from the water, which is in contrast with conventional systems for removing CO ₂ from water. In conventional systems, for example, CO2 is removed from the water via vacuum, and the water is degassed prior to removing the CO2 to avoid desorption of other naturally dissolved gases (O2 and N2) in the water. Furthermore, the CO ₂ removed in conventional systems via vacuum has a low partial pressure (e.g., 0.01-0.08 bar), and a multistage compression process is used to raise the pressure 8913774.1 of the CO ₂ for industry uses. Alternatively, the CO ₂ removed from the water in the systems described herein has a comparatively higher partial pressure, therefore significantly reducing energy demands and the overall process footprint as compared to conventional systems. According to certain embodiments, the system comprises a water treatment unit for acidification of water (e.g., a water acidification unit). FIG.1 shows a schematic diagram of system 100a for removing CO2 from water, in accordance with certain embodiments. As shown in FIG.1, system 100a comprises water treatment unit 102. In certain embodiments, an inlet of the water treatment unit is fluidically connected a water source such that water flowing from the water source flows into the water treatment unit. Referring to FIG.1, for example, inlet 104a of water treatment unit 102 may be fluidically connected to a water source (not shown in FIG.1). Any of a variety of suitable water sources may be envisioned, including, but not limited to, a sea, an ocean, a river, a stream, a lake, a pond, a reservoir, a spring, ground water, and the like. The water used in the system may be water from any of the water sources described herein. In some embodiments for example, the water used in the system is seawater, ocean water, river water, stream water, lake water, pond water, reservoir water, spring water, ground water, and the like. In certain embodiments, the water used in the system is wastewater (e.g., from a wastewater stream). In certain embodiments, the water from the water source, prior to flowing through the water treatment unit, may comprise CO ₂ (e.g., dissolved CO ₂ ). The water from the water source may comprise CO2 at any of a variety of suitable pressures (e.g., partial pressures) prior to flowing through the water treatment unit. In some embodiments, for example, the water from the water source comprises CO ₂ at a pressure (e.g., partial pressure) of greater than or equal to 0.01 bar, greater than or equal to 0.02 bar, greater than or equal to 0.03 bar, greater than or equal to 0.04 bar, greater than or equal to 0.05 bar, greater than or equal to 0.06 bar, greater than or equal to 0.07 bar, greater than or equal to 0.08 bar, greater than or equal to 0.09 bar, greater than or equal to 0.1 bar, or greater than or equal to 0.5 bar prior to flowing through the water treatment unit. In certain embodiments, the water from the water source comprises CO2 at a pressure (e.g., partial pressure) of less than or equal to 1 bar, less than or equal to 0.5 bar, less than or equal to 0.1 bar, less than or equal to 0.09 bar, less than or equal to 0.08 bar, less than or equal to 0.07 8913774.1 bar, less than or equal to 0.06 bar, less than or equal to 0.05 bar, less than or equal to 0.04 bar, less than or equal to 0.03 bar, or less than or equal to 0.02 bar prior to flowing through the water treatment unit. Combinations of the above recited ranges are possible (e.g., the water from the water source may comprise CO ₂ at a pressure (e.g., partial pressure) of greater than or equal to 0.01 bar and less than or equal to 1 bar prior to flowing through the water treatment unit, the water from the water source may comprise CO2 at a pressure (e.g., partial pressure) of greater than or equal to 0.04 bar and less than or equal to 0.06 bar prior to flowing through the water treatment unit). Other ranges are also possible. In certain embodiments, the water from the water source comprises no or substantially no CO ₂ (e.g., dissolved CO ₂ ) prior to flowing through the water treatment unit. The water from the water source, prior to flowing through the water treatment unit, may comprise one or more gases (e.g., one or more dissolved gases) other than CO2, in some embodiments. For example, in certain embodiments, the water in the water source comprises O2, N ₂ , and/or combinations thereof prior to flowing through the water treatment unit. In some embodiments, the water comprises one or more volatile organic gases, such as carbon monoxide (CO) and/or methane (CH4). Other gases are also possible. The water from the water source may comprise the one or more gases other than CO ₂ (e.g., O2 and/or N2) at any of a variety of suitable pressures (e.g., partial pressures) prior to flowing through the water treatment unit. In certain embodiments, for example, the water from the water source comprises the one or more gases other than CO ₂ at a pressure (e.g., partial pressure) of greater than or equal to 0.01 bar, greater than or equal to 0.1 bar, greater than or equal to 0.2 bar, greater than or equal to 0.3 bar, greater than or equal to 0.4 bar, greater than or equal to 0.5 bar, greater than or equal to 0.6 bar, greater than or equal to 0.7 bar, greater than or equal to 0.8 bar, greater than or equal to 0.9 bar, greater than or equal to 1 bar, or greater than or equal to 2 bar prior to flowing through the water treatment unit. In some embodiments, the water from the water source comprises the one or more gases other than CO2 at a pressure (e.g., partial pressure) of less than or equal to 5 bar, less than or equal to 2 bar, less than or equal to 1 bar, less than or equal to 0.9 bar, less than or equal to 0.8 bar, less than or equal to 0.7 bar, less than or equal to 0.6 bar, less than or equal to 0.5 bar, less than or equal to 0.4 bar, less than or equal to 0.3 bar, less than or equal to 0.2 bar, or less than or equal to 0.1 bar prior to flowing through the water treatment unit. Combinations of the above recited ranges are possible (e.g., the water from 8913774.1 the water source comprises the one or more gases other than CO ₂ at a pressure (e.g., partial pressure) of greater than or equal to 0.01 bar and less than or equal to 5 bar prior to flowing through the water treatment unit, the water from the water source comprises the one or more gases other than CO ₂ at a pressure (e.g., partial pressure) of greater than or equal to 0.2 bar and less than or equal to 0.8 bar prior to flowing through the water treatment unit). Other ranges are also possible. The water from the water source may comprise one or more carbon-containing species prior to flowing the water through the water treatment unit. The one or more carbon-containing species may be any of a variety of suitable DICs. In certain embodiments, for example, the one or more carbon-containing species comprise CO ₂ , bicarbonate (HCO ₃ -), and/or carbonate (CO ₃ ^2- ). Other carbon-containing species are also possible. The water from the water source may comprise the one or more carbon-containing species prior to flowing through the water treatment unit at any of a variety of suitable concentrations. In certain embodiments, for example, the concentration of the one or more carbon-containing species in the water from the water source prior to flowing through the water treatment unit may be greater than or equal to 0.1 mM, greater than or equal to 0.5 mM, greater than or equal to 1 mM, greater than or equal to 1.5 mM, greater than or equal to 2 mM, greater than or equal to 2.5 mM, greater than or equal to 5 mM, or greater than or equal to 10 mM. In some embodiments, the concentration of the one or more carbon-containing species in the water from the water source prior to flowing through the water treatment unit may be less than or equal to 20 mM, less than or equal to 10 mM, less than or equal to 5 mM, less than or equal to 3 mM, less than or equal to 2.5 mM, less than or equal to 2 mM, less than or equal to 1.5 mM, less than or equal to 1 mM, or less than or equal to 0.5 mM. Combinations of the above recited ranges are possible (e.g., the concentration of the one or more carbon-containing species in the water from the water source prior to flowing through the water treatment unit may be greater than or equal to 0.1 mM and less than or equal to 20 mM, the concentration of the one or more carbon-containing species in the water from the water source prior flowing through the water treatment unit may be greater than or equal to 1.5 mM and less than or equal to 2.5 mM). Other ranges are also possible. The water from the water source (e.g., prior to flowing through the water treatment unit) may have a first pH level. The first pH level of the water may be any of a variety of suitable pH 8913774.1 values. In certain embodiments, the first pH level is a neutral or basic pH. For example, in some embodiments, the first pH level is greater than or equal to 7, greater than or equal to 7.5, greater than or equal to 8, or greater than or equal to 8.5, or greater than or equal to 9. In certain embodiments, the first pH level is less than or equal to 9.5, less than or equal to 9, less than or equal to 8.5, less than or equal to 8, or less than or equal to 7.5. Combinations of the above recited ranges are possible (e.g., the first pH level is greater than or equal to 7 and less than or equal to 9.5, the first pH level is greater than or equal to 8 and less than or equal to 9). Other ranges are also possible. In some embodiments, the water treatment unit is configured to acidify water flowing through the water treatment unit. For example, in accordance with certain embodiments, the water treatment unit is configured to adjust the pH of the water flowing through the water treatment unit from the first pH level to a second pH level that is lower than the first pH level. In certain embodiments, the water flowing through the water treatment unit comprises the one or more carbon-containing species, and adjusting the pH of the water from the first pH level to the second pH level that is lower than the first pH converts at least some of the one or more carbon- containing species to CO2. The water treatment unit may acidify the water by any of a variety of suitable means that would be known to a person of ordinary skill in the art. In certain embodiments, for example, the water treatment unit utilizes one or more acids (e.g., hydrochloric acid, sulfuric acid, nitric acid, and the like) to acidify the water. In some embodiments, the water treatment unit utilizes an electrochemical-based acidification process via one or more reactive electrodes and/or water splitting (e.g., bipolar membrane water splitting). The second pH level of the water (e.g., after flowing through the water treatment unit) may be any of a variety of suitable pH values. In some embodiments, the first pH level is a neutral or acidic pH. For example, in certain embodiments, the second pH level is less than or equal to 7, less than or equal to 6.5, less than or equal to 6, less than or equal to 5.5, less than or equal to 5, or less than or equal to 4.5. In some embodiments, the second pH level is greater than or equal to 4, greater than or equal to 4.5, greater than or equal to 5, greater than or equal to 5.5, greater than or equal to 6, or greater than or equal to 6.5. Combinations of the above recited ranges are possible (e.g., the second pH level is less than or equal to 7 and greater than or equal 8913774.1 to 4, the second pH level is less than or equal to 6 and greater than or equal to 5). Other ranges are also possible. In certain embodiments, the water may comprise CO2 (e.g., dissolved CO2) after flowing through the water treatment unit. In some embodiments, after the flowing through the water treatment unit, the water comprises a higher partial pressure of CO2 as compared to the partial pressure of CO2 in the water prior to flowing through the water treatment unit. For example, in some embodiments, at least some of the carbon-containing species in the water from the water source are converted to CO2 after flowing through the water treatment unit. The water may comprise CO2 at any of a variety of suitable pressures (e.g., partial pressures) after flowing through the water treatment unit. In some embodiments, for example, the water from the water source comprises CO ₂ at a pressure (e.g., partial pressure) of greater than or equal to 0.01 bar, greater than or equal to 0.05 bar, greater than or equal to 0.06 bar, greater than or equal to 0.07 bar, greater than or equal to 0.08 bar, greater than or equal to 0.09, greater than or equal to 0.1 bar, greater than or equal to 0.2 bar, greater than or equal to 0.3 bar, greater than or equal to 0.4 bar, greater than or equal to 0.5 bar, greater than or equal to 1 bar, or greater than or equal to 2 bar after to flowing through the water treatment unit. In certain embodiments, the water comprises CO ₂ at a pressure (e.g., partial pressure) of less than or equal to 5 bar, less than or equal to 2 bar, less than or equal to 1 bar, less than or equal to 0.5 bar, less than or equal to 0.4 bar, less than or equal to 0.3 bar, less than or equal to 0.2 bar, less than or equal to 0.1 bar, less than or equal to 0.09 bar, less than or equal to 0.08 bar, less than or equal to 0.07 bar, less than or equal to 0.06 bar, or less than or equal to 0.05 bar after flowing through the water treatment unit. Combinations of the above recited ranges are possible (e.g., the water may comprise CO2 at a pressure (e.g., partial pressure) of greater than or equal to 0.01 bar and less than or equal to 5 bar after flowing through the water treatment unit, the water may comprise CO2 at a pressure (e.g., partial pressure) of greater than or equal to 0.06 bar and less than or equal to 0.08 bar after flowing through the water treatment unit). Other ranges are also possible. The water may comprise one or more gases (e.g., one or more dissolved gases) other than CO2 after flowing through the water treatment unit, in some embodiments. For example, in certain embodiments, the water comprises O2, N2, and/or combinations thereof after flowing through the water treatment unit. Other gases are also possible. 8913774.1 The water may comprise the one or more gases other than CO ₂ (e.g., O ₂ and/or N ₂ ) at any of a variety of suitable pressures (e.g., partial pressures) after flowing through the water treatment unit. In certain embodiments, for example, the water comprises the one or more gases other than CO ₂ at a pressure (e.g., partial pressure) of greater than or equal to 0.01 bar, greater than or equal to 0.1 bar, greater than or equal to 0.2 bar, greater than or equal to 0.3 bar, greater than or equal to 0.4 bar, greater than or equal to 0.5 bar, greater than or equal to 0.6 bar, greater than or equal to 0.7 bar, greater than or equal to 0.8 bar, greater than or equal to 0.9 bar, greater than or equal to 1 bar, or greater than or equal to 2 bar after flowing through the water treatment unit. In some embodiments, the water comprises the one or more gases other than CO2 a pressure (e.g., partial pressure) of less than or equal to 5 bar, less than or equal to 2 bar, less than or equal to 1 bar, less than or equal to 0.9 bar, less than or equal to 0.8 bar, less than or equal to 0.7 bar, less than or equal to 0.6 bar, less than or equal to 0.5 bar, less than or equal to 0.4 bar, less than or equal to 0.3 bar, less than or equal to 0.2 bar, or less than or equal to 0.1 bar after flowing through the water treatment unit. Combinations of the above recited ranges are possible (e.g., the water comprises the one or more gases other than CO2 at a pressure (e.g., partial pressure) of greater than or equal to 0.01 bar and less than or equal to 5 bar after flowing through the water treatment unit, the water comprises the one or more gases other than CO ₂ at a pressure (e.g., partial pressure) of greater than or equal to 0.2 bar and less than or equal to 0.8 bar after flowing through the water treatment unit). Other ranges are also possible. According to some embodiments, the partial pressure of the one or more gases other than CO ₂ (e.g., O ₂ and/or N ₂ ) after flowing through the water treatment unit may be the same or substantially the same as the partial pressure of the one or more gases other than CO2 prior to flowing through the water treatment unit. In some embodiments, the water comprises no or substantially no carbon-containing species (e.g., DICs such as CO2, HCO3-, and/or CO3 ^2- ) after flowing through water treatment unit. In certain embodiments, for example, the carbon-containing species in the water prior to flowing through the water treatment unit are converted to CO ₂ (e.g., by the water treatment unit). According to certain embodiments, the system does not comprise a degasification unit and/or a vacuum configured to remove one or more gases (e.g., dissolved gases) from the water. In some embodiments, for example, the water used in the system may comprise one or more gases (e.g., one or more dissolved gases), as explained herein in greater detail. Advantageously, 8913774.1 a system that does not include a degasification unit and/or a vacuum significantly reduces energy demands and overall process footprint. Any of a variety of amounts of dissolved gases may be removed from the water from the water source prior to flowing the water through the system (e.g., through the water treatment unit, through the CO2-extraction unit, and/or through the water regeneration unit). In some embodiments, for example, less than or equal to 90%, less than or equal to 80%, less than or equal to 70%, less than or equal to 60%, less than or equal to 50%, less than or equal to 40%, less than or equal to 30%, less than or equal to 20%, less than or equal to 10%, less than or equal to 5%, or less than or equal to 1% of dissolved gases may be removed form the water from the water source prior to flowing the water through the system. In certain embodiments, greater than or equal to 0%, greater than or equal to 1%, greater than or equal to 5%, greater than or equal to 10%, greater than or equal to 20%, greater than or equal to 30%, greater than or equal to 40%, greater than or equal to 50%, greater than or equal to 60%, greater than or equal to 70%, or greater than or equal to 80% of dissolved gases are removed from the water from the water source prior to flowing the water through the system. Combinations of the above recited ranges are possible (e.g., less than or equal to 90% and greater than or equal to 0% of dissolved gases are removed from the water from the water source prior to flowing the water through the system, less than or equal to 10% and greater than or equal to 1% of dissolved gases are removed from the water from the water source prior to flowing the water through the system). Other ranges are also possible. According to certain embodiments, the system comprises a CO ₂ -extraction unit. Referring to FIG.1, for example, system 100a comprises CO2-extraction unit 106. In some embodiments, the CO2-extraction unit is configured to remove CO2 from water, which is explained herein in greater detail. According to some embodiments, the CO2-extraction unit comprises a water flow chamber. Referring to FIG.1, for example, CO2-extraction unit 106 comprises water flow chamber 108. The water flow chamber may be configured to comprise water, in some embodiments. In other embodiments, the water flow chamber comprises water. According to certain embodiments, for example, an outlet of the water treatment unit is fluidically connected to an inlet of the water flow chamber such that water flowing from the water treatment unit flows 8913774.1 into the water flow chamber. Referring, for example, to FIG.1, outlet 110a of water treatment unit 102 may be fluidically connected to inlet 104b of water flow chamber 108. In certain embodiments, the CO2-extraction unit comprises a CO2-extraction solution flow chamber. Referring to FIG.1, for example, CO ₂ -extraction unit 106 comprises CO ₂ - extaction solution flow chamber 112. The CO2-extaction solution flow chamber may, in some embodiments, be configured to comprise a CO2-extraction solution comprising a CO2-extractor. In other embodiments, the CO ₂ -extraction solution flow chamber comprises a CO ₂ -extraction solution comprising a CO2-extractor. Suitable CO2-extraction solutions and CO2-extractors are explained herein in greater detail. In some embodiments, the CO ₂ -extraction unit comprises a CO ₂ -permeable membrane. As shown in FIG.1, for example, CO ₂ -extraction unit 106 comprises CO ₂ -permebale membrane 114. The CO2-permeable membrane is permeable to CO2, in some embodiments. In certain embodiments, the CO2-permeable membrane is at least partially permeable to one or more additional gases. For example, in some embodiments, the CO ₂ -permeable membrane is at least partially permeable to O2 and/or N2. The water flow chamber and the CO2-extaction solution flow chamber may, in some embodiments, be separated by the CO ₂ -permeable membrane. Referring to FIG.1, for example, water flow chamber 108 and CO2-extaction solution flow chamber 112 are separated by CO2- permeable membrane 114. According to some embodiments, the CO2-permeable membrane may advantageously be configured to: (i) prevent water flowing in the water flow chamber from mixing with the CO ₂ -extraction solution flowing in the CO ₂ -extraction solution flow chamber; and (ii) prevent the CO2-extraction solution flowing in the CO2-extraction solution flow chamber from mixing with the water flowing in the water flow chamber. For example, in some embodiments, the CO ₂ -permeable comprises a plurality of pores. Without wishing to be bound by theory, the plurality of pores may provide resistance to mass transfer across the semi- permeable membrane. In certain embodiments, the plurality of pores comprise a gas. For example, the plurality of pores may comprise air (e.g., air plastron), in some embodiments. According to some embodiments, the CO2-permeable membrane comprises a first surface and a second surface. For example, as shown in FIG.1, CO2-permeable membrane 114 comprises first surface 116 and second surface 118. In certain embodiments, the first surface of the CO ₂ -permeable membrane is substantially opposite the second surface of the CO ₂ -permeable 8913774.1 membrane. Referring, for example, to FIG.1, first surface 116 of CO ₂ -permeable membrane 114 is substantially opposite second surface 118 of CO2-permeable membrane 114. According to some embodiments, the water flow chamber is configured to flow water comprising CO ₂ in contact with the first surface of the CO ₂ -permeable membrane. For example, as shown in FIG.1, water flow chamber 108 is configured to flow water comprising CO2 in contact with first surface 116 of CO2-permeable membrane 114. In certain embodiments, the CO ₂ -extraction solution flow chamber is configured to flow the CO2-extraction solution in contact with the second surface of the CO2-permeable membrane. Referring to FIG.1, for example, CO2-extraction solution flow chamber 112 is configured to flow the CO ₂ -extraction solution in contact with second surface 118 of CO ₂ -permeable membrane 114. As described above, the CO2-extraction unit is configured to remove CO2 from water across the CO2-permeable membrane into the CO2-extraction solution. In accordance with certain embodiments, for example, the CO ₂ -permeable membrane is configured such that CO ₂ passes through the CO2-permeable membrane from the water (e.g., flowing in the water flow chamber) into the CO2-extraction solution (e.g., flowing in the CO2-extraction solution chamber). In some embodiments, after the CO ₂ passes through the CO ₂ -permeable membrane from the water into the CO2-extraction solution, the CO2 complexes with the CO2-extractor to produce a CO2-complexed CO2-extractor. In some embodiments, the CO ₂ -permeable membrane is a symmetric or substantially symmetric membrane. For example, in certain embodiments, the CO ₂ -permeable membrane comprises a plurality of pores having symmetric or essentially symmetric pore structures. In other embodiments, the CO2-permeable membrane is an asymmetric membrane. In certain embodiments, for example, the CO ₂ -permeable membrane comprises a plurality of pores having asymmetric pore structures such that the pores gradually become larger across the membrane from the water flow chamber to the CO2-extraction solution flow chamber. According to certain embodiments, the asymmetric membrane may comprise two layers. For example, in some embodiments, the asymmetric membrane comprises a first layer having a plurality of pores with a first size distribution (e.g., in contact with the water flowing in the water flow chamber) and a second layer having a plurality of pores with a second size distribution, wherein the second size 8913774.1 distribution is larger than the first size distribution (e.g., in contact with the CO ₂ -extraction solution flowing in the CO2-extraction solution flow chamber) The CO2-permeable membrane may comprise any of a variety of suitable materials. In certain embodiments, for example, the CO ₂ -permeable membrane comprises a hollow-fiber membrane (HFM). The CO2-permeable membrane may comprise a hydrophobic material, in some embodiments. In some embodiments, for example, the CO2-permeable membrane comprises a polymer. Suitable polymers include, but are not limited to, polypropylene and/or polytetrafluoroethylene. Other materials are also possible and would be known to a person of ordinary skill in the art. As described above, the CO ₂ -extraction unit comprises a CO ₂ -extraction solution comprising a CO ₂ -extractor. In certain embodiments, for example, the CO ₂ -extraction solution comprises a CO2-extractor dissolved, suspended, and/or dispersed in the CO2-extraction solution. The CO2-extraction solution may comprise any of a variety of suitable solvents. The solvent of the CO ₂ -extraction solution may depend, in some embodiments, on the CO ₂ -extractor. According to some embodiments, the solvent is a non-volatile solvent (e.g., under ambient conditions). In certain embodiments, the CO2-extraction solution comprises an organic, aprotic solvent. In other embodiments, the CO ₂ -extraction solution comprises an aqueous, protic solvent. According to some embodiments, the CO2-extractor has an affinity for complexing CO2. In certain embodiments, for example, the CO ₂ -extractor has a comparatively higher affinity for complexing CO ₂ as compared to O ₂ and/or N ₂ . The CO2-extractor may comprise any of a variety of suitable materials. According to certain embodiments, the CO2-extractor is non-volatile (e.g., under ambient conditions). In some embodiments, the CO ₂ -extractor comprises a redox active moiety (e.g., an organic redox active moiety). In certain embodiments, the CO2-extractor comprises a quinone (e.g., 1,4- naphthoquinone, antraquinone-2,7-disulfonic acid, and the like), a disulfide (e.g., diphenyl sulfide and the like), and/or a bipyridine (e.g., 4,4′-bipyridine and the like). The CO2-extractor comprises an organic dye (e.g., neutral red, chloranil, and the like), in accordance with certain embodiments. In some embodiments, the CO2-extractor comprises an amine (e.g., ethylenediamine and the like). In certain embodiments, the CO ₂ -extractor comprises CO ₃ ^2- . 8913774.1 Other quinones, disulfides, bipyridines, and/or amines are also possible and would be known to a person of ordinary skill in the art. According to some embodiments, the CO2-extraction solution comprises an organic, aprotic solvent and the CO ₂ -extractor comprises a redox active moiety (e.g., an organic redox active moiety) such as a quinone, a disulfide, and/or a bipyridine. In certain embodiments, the CO2-extraction solution comprises an aqueous, protic solvent and the CO2-extractor comprises CO ₃ ^2- . According to certain embodiments, the system comprises a CO2-extraction solution regeneration unit. Referring to FIG.1, for example, system 100a comprises CO2-extraction solution regeneration unit 120. In some embodiments, the CO ₂ -extraction solution regeneration unit is configured to release CO ₂ from the CO ₂ -complexed CO ₂ -extractor and to regenerate the CO2-extractor. According to some embodiments, an outlet of the CO2-extraction solution flow chamber is fluidically connected to an inlet of the CO ₂ -extraction solution regeneration unit such that the CO2-extraction solution (e.g., comprising the CO2-complexed CO2-extractor) flowing from the CO2-extraction solution flow chamber flows into the CO2-extraction solution regeneration unit. Referring to FIG.1, for example, outlet 110b of CO ₂ -extraction solution flow chamber 112 is fluidically connected to inlet 104c of CO2-extraction solution regeneration unit 120. The CO2-extraction solution regeneration unit may be configured to release CO2 from the CO ₂ -complexed CO ₂ -extractor and to regenerate the CO ₂ -extractor by any of a variety of suitable means. In some embodiments, for example, the CO ₂ -extraction solution regeneration unit comprises an electrochemical cell. In certain embodiments, the CO2-extractor may comprise a redox active moiety (e.g., a quinone, a disulfide, a bipyridine) that complexes CO2 in the CO2- extraction unit, as described herein, in an activated (e.g., reduced) form, thereby producing the CO2-complexed CO2-extractor. The electrochemical cell may be configured, in some embodiments, to oxidize the CO2-complexed activated (e.g., reduced) CO2-extractor in an anode chamber to produce a deactivated (e.g., neutral) CO ₂ -extractor that releases CO ₂ (e.g., from the quinone, a disulfide, and/or bipyridine). In certain embodiments, the electrochemical cell may be configured to reduce the deactivated (e.g., neutral) CO2-extractor in a cathode chamber to regenerate the activated (e.g., reduced) CO ₂ -extractor. 8913774.1 In some embodiments, the CO ₂ -extractor comprises an amine (e.g., ethylenediamine) that complexes CO2 in the CO2-extraction unit, as described herein, thereby producing the CO2- complexed CO2-extractor (e.g., carbamate). The electrochemical cell may be configured, in some embodiments, to oxidize a metal (e.g., a metal electrode), such as copper (Cu), in an anode chamber to produce a metal-amine (e.g., Cu(II)-ethylenediamine) that releases CO2 (e.g., from the carbamate). In certain embodiments, the electrochemical cell may be configured to reduce the metal-amine in a cathode chamber to regenerate the CO ₂ -extractor (e.g., the amine) and the metal (e.g., Cu). This process is known as the EMAR process and is described in further detail in U.S. Patent Application No.16/150,186, filed October 2, 2018, published as U.S. Patent Publication No 2019/0099711 on April 4, 2019, issued as U.S. Patent No.11,446,604 on September 20, 2022, and entitled “Methods and Systems for Removing CO ₂ From a Feed Gas,” which is incorporated herein by reference in its entirety. In some embodiments, the CO2-extracor comprises CO3 ^2- that complexes CO2 in the CO ₂ -extraction unit, as described herein, via a pH swing process, thereby producing the CO ₂ - complexed CO2-extractor (e.g., two equivalents of HCO3-). In certain embodiments, the electrochemical cell may be configured to generate a proton (H ⁺ ) via one or more intercalation electrodes to produce one equivalent of HCO ₃ - that releases CO ₂ (e.g., from the two equivalents of HCO3-). In some embodiments, the electrochemical cell may be configured to remove a proton via the one or more intercalation electrodes to regenerate the CO2-extractor (e.g., CO3 ^2- ). According to some embodiments, the CO ₂ -extraction solution regeneration unit comprises a thermal regeneration unit. In certain embodiments, for example, the CO ₂ -extractor may comprise an amine (e.g., ethylenediamine) that complexes CO2 in the CO2-extraction unit, as described herein, thereby producing the CO2-complexed CO2-extractor (e.g., carbamate). The thermal regeneration unit may be configured, in some embodiments, to release CO ₂ from the CO2-complexed CO2-extractor via an amine scrubbing process. According to certain embodiments, the CO2-extraction solution regeneration unit comprises bipolar membrane electrodialysis unit. According to certain embodiments, the system comprises a flash tank. Referring to FIG. 1, for example, system 100a comprises flash tank 122. The flash tank may be configured, in some embodiments, to remove CO ₂ (e.g., released from the CO ₂ -extractor) from the CO ₂ - extraction solution. 8913774.1 In some embodiments, an outlet of the CO ₂ -extraction solution regeneration unit is fluidically connected to an inlet of the flash tank such that the CO2-extraction solution (e.g., comprising CO2 released from the CO2-extractor and the CO2-extractor) flowing from the CO2- extraction solution regeneration unit flows into the flash tank. As shown in FIG.1, for example, outlet 110c of CO2-extraction solution regeneration unit 120 is fluidically connected to inlet 104d of flash tank 122. According to some embodiments, an outlet of the flash tank is fluidically connected to an inlet of the CO2-extraction solution flow chamber such that the CO2-extraction solution (e.g., comprising the CO2-extractor) flowing from the flash tank flows into the CO2-extraction solution flow chamber. For example, referring to FIG.1, outlet 110d of flash tank 122 is fluidically connected to inlet 104e of CO ₂ -extraction solution flow chamber 112. In some embodiments, after flowing from the flash tank to the CO2-extraction solution flow chamber, the CO2- extraction solution comprising the CO2-extractor may be configured to remove CO2 from water. The system may therefore be configured as a continuous process, in some embodiments, so that CO2 is continuously removed from the water flowing in the water chamber of the CO2-extraction unit by the CO2-extraction solution comprising the CO2-extractor flowing in the CO2-extraction solution flow chamber. In accordance with certain embodiments, the system comprises a compressor. For example, referring to FIG.1, system 100a comprises compressor 124. The compressor may be configured, in some embodiments, to compress the CO ₂ removed by the flash tank. In some embodiments, a gaseous outlet of the flash tank is fluidically connected to a gaseous inlet of the compressor such the CO2 flowing from the flash tank flows into the compressor. As shown in FIG.1, for example, gaseous outlet 126a of flash tank 122 is fluidically connected to gaseous inlet 128 of compressor 124. The pressure of the CO2 flowing from the flash tank into the compressor may be any of a variety of suitable pressures. In some embodiments, for example, the pressure of the CO2 flowing from the flash tank into the compressor may be greater than or equal to 0.1 bar, greater than or equal to 0.5 bar, greater than or equal to 0.6 bar, greater than or equal to 0.7 bar, greater than or equal to 0.8 bar, greater than or equal to 0.9 bar, greater than or equal to 1 bar, greater than or equal to 1.5 bar, greater than or equal to 2 bar, greater than or equal to 2.5 bar, greater than or equal to 3 bar, greater than or equal to 3.5 bar, greater than or equal to 4 bar, or greater 8913774.1 than or equal to 4.5 bar. In certain embodiments, the pressure of the CO ₂ flowing from the flash tank into the compressor may be less than or equal to 5 bar, less than or equal to 4.5 bar, less than or equal to 4 bar, less than or equal to 3.5 bar, less than or equal to 3 bar, less than or equal to 2.5 bar, less than or equal to 2 bar, less than or equal to 1.5 bar, less than or equal to 1 bar, less than or equal to 0.9 bar, less than or equal to 0.8 bar, less than or equal to 0.7 bar, less than or equal to 0.6 bar, or less than or equal to 0.5 bar. Combinations of the above recited ranges are possible (e.g., the pressure of the CO ₂ flowing from the flash tank into the compressor may be greater than or equal to 0.1 bar and less than or equal to 5 bar, the pressure of the CO2 flowing from the flash tank into the compressor may be greater than or equal to 0.9 bar and less than or equal to 1.5 bar). Other ranges are also possible. According to some embodiments, a gaseous outlet of the compressor may be fluidically connected to a CO2-collection unit such that the compressed CO2 flowing from the compressor may be collected in the CO2-collection unit. Referring to FIG.1, for example, gaseous outlet 126b of compressor 124 may be fluidically connected to a CO ₂ -collection unit (not shown in FIG.1). In certain embodiments, the collected CO2 in the CO2-collection unit may be used for geologic storage and/or industry utilization. The pressure of the CO ₂ flowing from the compressor into the CO ₂ -collection unit may be any of a variety of suitable pressures. In some embodiments, for example, the pressure of the CO2 flowing from the compressor into the CO2-collection unit may be greater than or equal to 5 bar, greater than or equal to 10 bar, greater than or equal to 20 bar, greater than or equal to 50 bar, greater than or equal to 100 bar, greater than or equal to 150 bar, or greater than or equal to 200 bar. In certain embodiments, the pressure of the CO2 flowing from the compressor into the CO2-collection unit may be less than or equal to 250 bar, less than or equal to 200 bar, less than or equal to 150 bar, less than or equal to 100 bar, less than or equal to 50 bar, less than or equal to 20 bar, or less than or equal to 10 bar. Combinations of the above recited ranges are possible (e.g., the pressure of the CO2 flowing from the compressor into the CO2-collection unit may be greater than or equal to 5 bar and less than or equal to 250 bar, the pressure of the CO ₂ flowing from the compressor into the into the CO2-collection unit may be greater than or equal to 100 bar and less than or equal to 150 bar). Other ranges are also possible. 8913774.1 According to certain embodiments, the system comprises a water regeneration unit for de-acidification water (e.g., a water de-acidification unit). Referring, for example, to FIG.1, system 100a comprises water regeneration unit 130. In certain embodiments, an outlet of the water flow chamber is fluidically connected to an inlet of the water regeneration unit such that water flowing from the water flow chamber flows into the water regeneration unit. As shown in FIG.1, for example, outlet 110e of water flow chamber 108 is fluidically connected to inlet 104f of water regeneration unit 130. In some embodiments, the water regeneration unit is configured to de-acidify water flowing through the water regeneration unit. For example, in accordance with certain embodiments, the water regeneration unit is configured to adjust the pH of water flowing through the water regeneration unit from the second pH level to the first pH level. The water regeneration unit may de-acidify the water by any of a variety of suitable means that would be known to a person of ordinary skill in the art. In some embodiments, for example, the water regeneration unit utilizes one or more bases (e.g., potassium hydroxide, sodium hydroxide, and the like) to de-acidify the water. The second pH level of the water (e.g., prior to flowing through the water regeneration unit) may be any of the previously described pH values with respect to the water treatment unit (e.g., the second pH level is less than or equal to 7 and greater than or equal to 4). The first pH level of the water (e.g., after flowing through the water regeneration unit) may be any of the previously described pH values with respect to the water treatment unit (e.g., the first pH level is greater than or equal to 7 and less than or equal to 9.5). According to certain embodiments, the water comprises no or substantially no CO2 (e.g., dissolved CO2) after flowing through the water regeneration unit. The water may comprise one or more gases (e.g., one or more dissolved gases) other than CO2 after flowing through the water regeneration unit, in some embodiments. For example, in certain embodiments, the water comprises O2, N2, and/or combinations thereof after flowing through the water regeneration unit. Other gases are also possible. The water may comprise the one or more gases other than CO2 (e.g., O2 and/or N2) at any of a variety of suitable pressures (e.g., partial pressures) after flowing through the water regeneration unit. In certain embodiments, for example, the water comprises the one or more gases other than CO ₂ at a pressure (e.g., partial pressure) of greater than or equal to 0.01 bar, 8913774.1 greater than or equal to 0.1 bar, greater than or equal to 0.2 bar, greater than or equal to 0.3 bar, greater than or equal to 0.4 bar, greater than or equal to 0.5 bar, greater than or equal to 0.6 bar, greater than or equal to 0.7 bar, greater than or equal to 0.8 bar, greater than or equal to 0.9 bar, greater than or equal to 1 bar, or greater than or equal to 2 bar after flowing through the water regeneration unit. In some embodiments, the water comprises the one or more gases other than CO2 a pressure (e.g., partial pressure) of less than or equal to 5 bar, less than or equal to 2 bar, less than or equal to 1 bar, less than or equal to 0.9 bar, less than or equal to 0.8 bar, less than or equal to 0.7 bar, less than or equal to 0.6 bar, less than or equal to 0.5 bar, less than or equal to 0.4 bar, less than or equal to 0.3 bar, less than or equal to 0.2 bar, or less than or equal to 0.01 bar after flowing through the water regeneration unit. Combinations of the above recited ranges are possible (e.g., the water comprises the one or more gases other than CO ₂ at a pressure (e.g., partial pressure) of greater than or equal to 0.01 bar and less than or equal to 5 bar after flowing through the water regeneration unit, the water comprises the one or more gases other than CO2 at a pressure (e.g., partial pressure) of greater than or equal to 0.4 bar and less than or equal to 0.6 bar after flowing through the water regeneration unit). Other ranges are also possible. In some embodiments, the water comprises no or substantially no carbon-containing species (e.g., DICs such as CO ₂ , HCO ₃ -, and/or CO ₃ ^2- ) after flowing through water regeneration unit. According to some embodiments, an outlet of the water regeneration unit is fluidically connected to a water source such that water flowing from the water regeneration unit (e.g., at the first pH level) flows into a water source. Referring to FIG.1, for example, outlet 110f of water regeneration unit 130 may be fluidically connected to a water source (not shown in FIG.1). The water source may be any of the previously described water sources with respect to the water treatment unit (e.g., a sea, an ocean, a river, a stream, a lake, a pond, a reservoir, a spring, ground water, and the like). The water source fluidically connected to the inlet of the water treatment unit may be the same or different than the water source fluidically connected to the outlet of the water regeneration unit. Referring to FIG.1, for example, the water source fluidically connected to inlet 104a of water treatment unit 102 may be the same or different than the water source fluidically connected to outlet 110f of water regeneration unit 130. 8913774.1 According to certain embodiments, the system may comprise one or more fluid pumps configured to facilitate the flow of a fluid (e.g., the water, the CO2-extraction solution) through the system. For example, in certain embodiments, one or more fluid pumps may be associated with the water treatment unit, the CO ₂ -extraction unit, the CO ₂ -solution regeneration unit (e.g., electrochemical cell), the flash tank, and/or the water regeneration unit to facilitate the flow of a fluid through each component of the system. As described above, the CO ₂ -extraction solution regeneration unit may comprise an electrochemical cell, in accordance with certain embodiments. FIG.2 shows a schematic diagram of an electrochemical system for removing CO2 from water, in accordance with certain embodiments. As shown, for example, in FIG.2, system 100b comprises electrochemical cell 132, in some embodiments. In some embodiments, the electrochemical cell is fluidically connected to the CO2-extraction unit. For example, referring to FIG.2, electrochemical cell 132 is fluidically connected to CO2-extraction unit 106. According to certain embodiments, the electrochemical cell comprises an anode chamber and a cathode chamber. As shown, for example, in FIG.2, electrochemical cell 132 comprises anode chamber 134 and cathode chamber 136. According to some embodiments, the anode chamber comprises a first electrode (e.g., an anode). The anode chamber may comprise any of a variety of suitable first electrode materials. In certain embodiments, for example, the first electrode comprises a carbon-based material (e.g., a graphite-based material), such as a carbon cloth, a carbon paper, a carbon textile, a carbon felt, and the like. In some embodiments, the first electrode comprises a material capable of intercalating protons (e.g., MnO2, TiO2, and the like), a reactive material (e.g., bismuth (Bi)), and/or a metal (e.g., Cu). Other materials are also possible. According to some embodiments, an outlet of the CO ₂ -extraction unit (e.g., an outlet of the CO2-extraction solution flow chamber) is fluidically connected to an inlet of the anode chamber such that the CO2-extraction solution comprising the CO2-complexed CO2-extractor flowing from the CO ₂ -extraction solution flow chamber flows into the anode chamber. Referring to FIG.2, for example, outlet 110b of CO2-extraction solution flow chamber 112 is fluidically connected to inlet 104g of anode chamber 134. In certain embodiments, the system is configured to flow the CO ₂ -extraction solution comprising the CO ₂ -complexed CO ₂ -extractor from the CO ₂ -extraction unit (e.g., from an outlet 8913774.1 of the CO ₂ -extraction solution flow chamber) to the anode chamber (e.g., to an inlet of the anode chamber). Referring to FIG.2, for example, system 100b is configured to flow the CO2- extraction solution comprising the CO2-complexed CO2-extractor from outlet 110b of CO2- extraction solution flow chamber 112 to inlet 104g of anode chamber 134. In some embodiments, the CO2-extraction solution is an electrolyte solution for the electrochemical cell. In certain embodiments, the CO2-extraction solution may comprise an electrolyte salt. Any of a variety of suitable electrolyte salts may be employed. In some embodiments, the electrolyte salt may comprise an alkali metal salt and/or an alkaline earth metal salt. For example, the electrolyte salt may comprise an alkali metal and/or an alkaline earth metal salt of nitrate, borate, a halide, phosphate, a phosphonate, carbonate, sulfate, and/or perchlorate. Other electrolyte salts are also possible. According to some embodiments, upon application of a potential across the electrochemical cell, the anode chamber may be configured to oxidize at least a portion of the CO2-extraction solution in the anode chamber to release CO2 from the CO2-complexed CO2- extractor. Referring, for example, to FIG.2, upon application of potential 138 across electrochemical cell 132, anode chamber 134 may be configured to oxidize at least a portion of the CO2-extraction solution in anode chamber 134 to release CO2 from the CO2-complexed CO2- extractor. In some non-limiting embodiments, the CO ₂ -extractor may comprise a redox active moiety (e.g., a quinone, a disulfide, and/or a bipyridine). The redox active CO ₂ -extractor may, in some embodiments, complex CO2 in the CO2-extraction unit, as described herein, in an activated (e.g., reduced) form, thereby producing the CO2-complexed CO2-extractor. In certain embodiments, upon application of the potential across the electrochemical cell, the anode chamber may be configured to oxidize at least a portion of the CO2-extraction solution to release CO2 from the CO2-complexed CO2-extractor, thereby producing a deactivated (e.g., neutral) CO ₂ -extractor. In certain embodiments, an outlet of the anode chamber is fluidically connected to an inlet of the flash tank such that the CO2-extraction solution (e.g., comprising CO2 released from the CO ₂ -extractor and the deactivated CO ₂ -extractor) flowing from the anode chamber flows into 8913774.1 the flash tank (e.g., to remove CO ₂ released from the CO ₂ -extractor). Referring, for example, to FIG.2, outlet 110h of anode chamber 134 is fluidically to inlet 104d of flash tank 122. In certain embodiments, the cathode chamber comprises a second electrode (e.g., a cathode). The cathode chamber may comprise any of a variety of suitable second electrode materials. In certain embodiments, for example, the second electrode comprises a carbon-based material (e.g., a graphite-based material), such as a carbon cloth, a carbon paper, a carbon textile, a carbon felt, and the like. In some embodiments, the second electrode comprises a material capable of intercalating protons (e.g., MnO2, TiO2, and the like), a reactive material (e.g., bismuth (Bi)), and/or a metal (e.g., Cu). Other materials are also possible. According to certain embodiments, an outlet of the flash tank is fluidically connected to an inlet of the cathode chamber such that the CO ₂ -extraction solution (e.g., comprising the deactivated CO2-extractor) flowing from the flash tank flows into the cathode chamber. Referring, for example, to FIG.2, outlet 110d of flash tank 122 is fluidically connected to inlet 104h of cathode chamber 136. In certain embodiments, upon application of a potential across the electrochemical cell, the cathode chamber may be configured to reduce at least a portion of the CO2-extraction solution in the cathode chamber to regenerate the CO ₂ -extractor. For example, referring to FIG. 2, upon application of potential 138 across electrochemical cell 132, cathode chamber 136 may be configured to reduce at least a portion of the CO2-extraction solution in cathode chamber 136 to regenerate the CO ₂ -extractor. In certain non-limiting embodiments, the CO ₂ -extractor may comprise a redox active moiety (e.g., a quinone, a disulfide, and/or a bipyridine). The redox active CO2-extractor may, in some embodiments, release CO2 in the anode chamber, as described herein, thereby producing the deactivated (e.g., neutral) CO ₂ -extractor. In some embodiments, upon application of the potential across the electrochemical cell, the cathode chamber may be configured to reduce at least a portion of the CO2-extraction solution to regenerate the CO2-extractor, thereby producing the activated (e.g., reduced) CO ₂ -extractor. According to some embodiments, an outlet of the cathode chamber is fluidically connected to an inlet of the CO2-extraction solution flow chamber such that the CO2-extraction solution (e.g., comprising the activated CO ₂ -extractor) flowing from the cathode chamber flows into the CO ₂ -extraction solution flow chamber. Referring, for example, to FIG.2, outlet 110g of 8913774.1 cathode chamber 136 is fluidically connected to inlet 104e of CO ₂ -extraction solution flow chamber 112. According to certain embodiments, the system is configured to flow the CO2-extraction solution comprising the CO ₂ -extractor (e.g., activated CO ₂ -extractor) from the cathode chamber (e.g., from an outlet of the cathode chamber) to the CO2-extraction solution flow chamber (e.g., to an inlet of the CO2-extraction solution flow chamber). Referring to FIG.2, for example, system 100b may be configured to flow the CO ₂ -extraction solution comprising the CO ₂ - extractor from outlet 110g of cathode chamber 136 to inlet 104e of CO2-extraction solution flow chamber 112. According to certain embodiments, the electrochemical cell may comprise a separator. Referring to FIG.2, for example, electrochemical cell 132 comprises separator 140. The separator may be configured to separate the anode chamber from the cathode chamber. For example, as shown in FIG.2, separator 140 is configured to separate anode chamber 134 from cathode chamber 136. Any of a variety of suitable separator materials may be utilized. In certain embodiments, for example, the separator comprises a cation exchange membrane or an anion exchange membrane. In some embodiments, the separator comprises Nafion. Other materials are also possible and would be known to a person of ordinary skill in the art. According to certain embodiments, a method for removing CO2 from water is described. In some embodiments, the method comprises adjusting the pH of water comprising one or more carbon-containing species (e.g., IDCs such as CO ₂ , HCO ₃ -, and/or CO ₃ ^2- ) from a first pH level (e.g., greater than or equal to 7 and less than or equal to 9.5) to a second pH level (e.g., less than or equal to 7 and greater than or equal to 4) that is lower than the first pH level to convert at least some of the one or more carbon-containing species to the CO ₂ . In certain embodiments, adjusting the pH of the water from the first pH level to the second pH level comprises flowing the water (e.g., from a water source) through a water treatment unit configured to acidify the water. Referring to FIG.1, for example, adjusting the pH of the water from the first pH level to the second pH level comprises flowing the water (e.g., from a water source, not shown in FIG.1) through water treatment unit 102 configured to acidify the water (e.g., via inlet 104a). According to certain embodiments, the method comprises exposing the water comprising the CO ₂ to a CO ₂ -extraction unit comprising a CO ₂ -permeable membrane. In some 8913774.1 embodiments, exposing the water comprising the CO ₂ to the CO ₂ -extraction unit comprises flowing the water from an outlet of the water treatment unit to an inlet of the water flow chamber. Referring to FIG.1, for example, exposing the water comprising the CO2 to CO2- extraction unit 106 comprises flowing the water comprising the CO ₂ from outlet 110a of water treatment unit to inlet 104b of water flow chamber 108. In some embodiments, exposing the water comprising the CO2 to the CO2-extraction unit comprises contacting a first surface of the CO ₂ -permeable membrane with the water comprising the CO2. For example, referring to FIG.1, exposing the water comprising the CO2 to CO2- extraction unit 106 comprises contacting first surface 116 of CO2-permeable membrane 114 with the water comprising the CO ₂ . According to certain embodiments, the method comprises exposing a CO ₂ -extraction solution comprising a CO2-extractor to the CO2-extraction unit. In certain embodiments, exposing the CO2-extraction solution comprising the CO2-extractor to the CO2-extraction unit comprises contacting a second surface of the CO ₂ -permeable membrane with the CO ₂ -extraction solution. As shown in FIG.1, for example, exposing the CO2-extraction solution comprising the CO2-extractor to CO2-extraction unit 106 comprises contacting second surface 118 of CO2- permeable membrane 114 with the CO ₂ -extraction solution comprising the CO ₂ -extractor. In some embodiments, the method comprises removing the CO2 from the water across the CO2-permeable membrane into the CO2-extraction solution comprising the CO2-extractor to produce a CO ₂ -complexed CO ₂ -extractor. In accordance with certain embodiments, removing the CO ₂ from the water comprises passing the CO ₂ through the CO ₂ -permeable membrane from the water to the CO2-extraction solution comprising the CO2-extractor to produce a CO2- complexed CO2-extractor. Referring to FIG.1, for example, removing the CO2 from the water comprises passing the CO ₂ through CO ₂ -permeable membrane 114 from the water (e.g., in water flow chamber 108) to the CO2-extraction solution comprising the CO2-extractor (e.g., in CO2- extraction solution flow chamber 112) to produce the CO2-complexed CO2-extractor. According to certain embodiments, the method comprises flowing the CO ₂ -extraction solution comprising the CO2-complexed CO2-extractor from an outlet of the CO2-extraction solution flow chamber to an inlet of a CO2-extraction solution regeneration unit configured to release CO ₂ from the CO ₂ -complexed CO ₂ -extractor and to regenerate the CO ₂ -extractor. As shown, for example, in FIG.1, the method comprises flowing the CO ₂ -extraction solution 8913774.1 comprising the CO ₂ -complexed CO ₂ -extractor from outlet 110b of CO ₂ -extraction solution flow chamber 112 to inlet 104c CO2-extraction solution regeneration unit 120. In certain embodiments, the method comprises releasing CO2 from the CO2-complexed CO ₂ -extractor and regenerating the CO ₂ -extractor in the CO ₂ -extraction solution regeneration unit. For example, referring to FIG.1, the method comprises releasing CO2 from the CO2- complexed CO2-extractor and regenerating the CO2-extractor in CO2-extraction solution regeneration unit 120. In some embodiments, the method comprises flowing the CO2-extraction solution comprising the CO2-extractor and the CO2 released from the CO2-extractor from an outlet of the CO ₂ -extraction solution regeneration unit to an inlet of a flash tank configured to remove CO ₂ from the CO ₂ -extraction solution. As shown in FIG.1, for example, the method comprises flowing the CO2-extraction solution comprising the CO2-extractor and the CO2 released from the CO2-extractor from outlet 110c of CO2-extraction solution regeneration unit 120 to inlet 104d of flash tank 122. In certain embodiments, the method comprises removing CO2 from the CO2-extraction solution in the flash tank. For example, referring to FIG.1, the method comprises removing CO2 from the CO ₂ -extraction solution in flash tank 122. According to certain embodiments, the method comprises flowing the CO2-extraction solution comprising the CO2-extractor from an outlet of the flash tank to an inlet of the CO2- extraction solution flow chamber. As shown in FIG.1, for example, the method comprises flowing the CO ₂ -extraction solution from outlet 110d of flash tank 122 to inlet 104e of CO ₂ - extraction solution flow chamber 112. In some embodiments, the method comprises flowing the CO2 removed by the flash tank from a gaseous outlet of the flash tank to a gaseous inlet of a compressor configured to compress the CO2. For example, as shown in FIG.1, the method comprises flowing the CO2 removed by flash tank 122 from gaseous outlet 126a of flash tank 122 to gaseous inlet 128 of compressor 124 configured to compress the CO ₂ . According to some embodiments, the method comprises compressing the CO2 in the compressor. Referring to FIG.1, for example, the method comprises compressing the CO2 in compressor 124. 8913774.1 In accordance with certain embodiments, the method comprises flowing the compressed CO2 from a gaseous outlet of the compressor to a CO2-collection unit. As shown in FIG.1, for example, the method comprises flowing the compressed CO2 from gaseous outlet 126b of compressor 124 to a CO ₂ -collection unit (not shown in FIG.1). In some embodiments, the method comprises adjusting the pH of the water from the second pH level (e.g., less than or equal to 7 and greater than or equal to 4) to the first pH level (e.g., greater than or equal to 7 and less than or equal to 9.5). In certain embodiments, adjusting the pH of the water from the second pH level to the first pH level comprises flowing the water from an outlet of the water flow chamber to an inlet of a water regeneration unit configured to de-acidify the water. For example, as shown in FIG.1, adjusting the pH of the water from the second pH level to the first pH level comprises flowing the water from outlet 110e of water flow chamber 108 to inlet 104f of water regeneration unit 130 configured to de-acidify the water. In some embodiments, the method comprises flowing the water (e.g., at the first pH level) from an outlet of the water regeneration unit to a water source. For example, referring to FIG.1, the method comprises flowing the water from outlet 110f of water regeneration unit 130 to a water source (not shown in FIG.1). As described herein, the CO ₂ -extraction solution regeneration unit may comprise an electrochemical cell. According to certain embodiments, the method comprises flowing the CO2-extraction solution comprising the CO2-complexed CO2-extractor from an outlet of the CO ₂ -extraction unit (e.g., an outlet of the CO ₂ -extraction solution flow chamber) to an inlet of an anode chamber of an electrochemical cell. For example, as shown in FIG.2, the method comprises flowing the CO2-extraction solution comprising the CO2-complexed CO2-extractor from outlet 110b of CO2-extraction solution flow chamber 112 to inlet 104g of anode chamber 134 of electrochemical cell 132. In some embodiments, the method comprises oxidizing at least a portion of the CO2- extraction solution in the anode chamber to release CO2 from the CO2-complexed CO2-extractor. Referring to FIG.2, for example, the method comprises oxidizing at least a portion of the CO ₂ - extraction solution in anode chamber 134 to release CO2 from the CO2-complexed CO2- extractor. In some embodiments, oxidizing at least the portion of the CO2-extraction solution in the anode chamber to release CO ₂ from the CO ₂ -complexed CO ₂ -extractor comprises applying a potential across the electrochemical cell. Referring, for example to FIG.2, oxidizing at least the 8913774.1 portion of the CO ₂ -extraction solution in anode chamber 134 to release CO ₂ from the CO ₂ - complexed CO2-extractor comprises applying potential 138 across electrochemical cell 132. In some non-limiting embodiments, the CO2-extractor may comprise a redox active moiety (e.g., a quinone, a disulfide, and/or a bipyridine). The redox active CO ₂ -extractor may, in some embodiments, complex CO2 in the CO2-extraction unit, as described herein, in an activated (e.g., reduced) form, thereby producing the CO2-complexed CO2-extractor. In certain embodiments, oxidizing at least the portion of the CO ₂ -extraction solution in the anode chamber comprises applying the potential across the electrochemical cell to release CO2 from the CO2- complexed CO2-extractor, thereby producing a deactivated (e.g., neutral) CO2-extractor. In accordance with certain embodiments, the method comprises flowing the CO ₂ - extraction solution comprising the CO ₂ released from the CO ₂ -extractor and the deactivated CO ₂ - extractor from an outlet of the anode chamber to an inlet of a flash tank. For example, as shown in FIG.2, the method comprises flowing the CO2-extraction solution comprising the CO2 released from the CO ₂ -extractor and the deactivated CO ₂ -extractor from outlet 110h of anode chamber 134 to inlet 104d of flash tank 122. In some embodiments, the method comprises removing CO2 from the CO2-extraction solution in the flash tank. Referring to FIG.2, for example, the method comprises removing CO ₂ from the CO2-extraction solution in flash tank 122. In certain embodiments, the method comprises flowing the CO2-extraction solution comprising the deactivated CO ₂ -extractor from an outlet of the flash tank to an inlet of the cathode chamber. As shown, for example, in FIG.2, the method comprises flowing the CO ₂ - extraction solution from outlet 110d of flash tank 122 to inlet 104h of cathode chamber 136. According to certain embodiments, the method comprises reducing at least a portion of the CO ₂ -extraction solution in a cathode chamber to regenerate the CO ₂ -extractor. For example, referring to FIG.2, the method comprises reducing at least a portion of the CO2-extraction solution in cathode chamber 136 to regenerate the CO2-extractor. In some embodiments, reducing at least a portion of the CO ₂ -extraction solution in a cathode chamber to regenerate the CO2-extractor comprises applying a potential across the electrochemical cell. Referring, for example, to FIG.2, reducing at least a portion of the CO2-extraction solution in cathode chamber 136 to regenerate the CO ₂ -extractor comprises applying potential 138 across electrochemical cell 132. 8913774.1 In certain non-limiting embodiments, the CO ₂ -extractor may comprise a redox active moiety (e.g., a quinone, a disulfide, and/or a bipyridine). The redox active CO2-extractor may, in some embodiments, release CO2 in the anode chamber, as described herein, thereby producing the deactivated (e.g., neutral) CO ₂ -extractor. In some embodiments, reducing at least a portion of the CO2-extraction solution in the cathode chamber comprises applying the potential across the electrochemical cell to regenerate the CO2-extractor, thereby producing the activated (e.g., reduced) CO ₂ -extractor. In some embodiments, the method comprises flowing the CO2-extraction solution comprising the CO2-extractor (e.g., activated CO2-extractor) from an outlet of the cathode chamber to an inlet of the CO ₂ -extraction solution flow chamber. As shown in FIG.2, for example, the method comprises flowing the CO ₂ -extraction solution comprising the CO ₂ - extractor from outlet 104h of cathode chamber 136 to inlet 104e of CO2-extraction solution flow chamber 112. EXAMPLE 1 The following example describes a system for the removal of CO2 from seawater. FIG.3A shows a schematic diagram of a conventional process for removing CO ₂ from seawater. As shown in FIG.3A, seawater is degassed to remove O2 and N2 prior to feeding the seawater to an electrochemical cell. In addition, CO2 is desorbed under vacuum, requiring multistage compression to raise the pressure of the pure stream from nominally 0.01 bar to 150 bar. An exemplary system for the removal of CO2 from seawater is shown in FIG.3B. As shown in FIG.3B, the acidified seawater is introduced to a membrane contactor where it is exposed to an electrochemically activated solvent that has a high affinity for the CO ₂ , and with which it complexes even under very low partial pressures. The sorbent has little to no affinity for O2 or N2, and thus these gases are not co-extracted with the CO2, obviating the need for pre- degasification. The membrane separating the feed water and the extractant is selected to prevent loss of extractant to the ocean water, or contamination of the extractant by the ocean water. Once the extractant is loaded with complexed CO2, it is introduced to the anode chamber of an electrochemical cell, where it is deactivated by oxidation and the CO ₂ is removed in a flash tank. The extractant is then fed to the cathode chamber to be activated by electrochemical reduction 8913774.1 before being sent back to the membrane contactor unit. The electrochemical cell is smaller than both the membrane contactor and the acidification/alkalization cells and considerably reduces the need for low pressure vacuum pumps and compressors, therefore significantly reducing energy demands and overall process footprint. See also FIG.11, which shows a schematic diagram of an extractant mediated direct ocean capture (DOC) system. In this system, the solution can be pumped to high pressures before it is fed to the regeneration cell and therefore the CO ₂ can be released at high pressure. However, the physically dissolved CO2 concentration following disengagement is larger than at lower release pressures, therefore diminishing the working capacity of the activated sorbent. This can be addressed by reducing the pressure in the flash tank, and then re-pressurizing the solution before it is sent to the cathode chamber. The additional pumping energy for re-pressurization is minimal relative to other energetic demands. An advantage of this high-pressure cell operation with reduced-pressure disengagement is that bubble formation within the electrochemical cell is suppressed, along with their many negative effects on required overpotentials, etc., to sustain high current operations. The extractant can be either an organic (aprotic) or an aqueous (protic) solution of redox active components, e.g., quinones, disulfides, bipyridines, and/or organic dyes (FIG.4A). In aprotic media the CO2 sorption is via direct complexation with the reduced redox molecules, while in aqueous media protonation of the reduced redox moieties leads to large increases in pH which allows extraction of the CO ₂ as a carbonate and/or bicarbonate (FIG.4C). In some approaches, this pH modulation can be through the intercalation and de-intercalation of protons from suitable electrodes and not from direct electrochemical activity of agents in solution. In this case, a swing process is utilized since one electrode will be depleted of, and the other replenished with, protons, and the flows and polarities are reversed periodically. In other approaches, amines can be used for the capture of the CO2, which can then be regenerated by introduction of, e.g., cupric ions, which displace and liberate the CO2, as in the EMAR process (FIG.4B). In yet other approaches, bipolar membrane electrodialysis may be utilized for the capture of the CO2 (FIG.4D). Since the fugacity of the free CO2 in the acidified ocean water is on a par with its fugacity in conventional industrial flue gases, traditional sorbents such as amines, which have low 8913774.1 capacity for CO ₂ under ambient air conditions, can be used effectively for extraction of the CO ₂ and can then be regenerated thermally. The membrane prevents mixing of the phases and dissolution of the solvent in the feed water, while permitting the cross-over of the CO ₂ . The membrane has selectivity for CO ₂ over other dissolved gases, and the solvent has a higher capacity for CO2 than for other gases. An exemplary configuration is when the pores of the membrane are filled with air (see FIG.3B), so that they offer minimal diffusional resistance to transfer across the membrane and the majority of the mass transfer resistance is on the feed water side, as it would be in any membrane desorption unit. As previously described, in conventional CO ₂ recovery operations, a vacuum is used to facilitate the release of CO ₂ from acidified water, resulting in low CO ₂ partial pressures in the final product stream that require significant compression to bring them up to desired pressures. To avoid producing CO2 gas at these low concentrations, an exemplary system was designed for extraction of CO ₂ from acidified seawater. A CO ₂ absorbent was used in the system, promoting the CO2 transfer from seawater to the absorbent. Since both the acidified water and the CO2 absorbent are in liquid phases, the two phases were separated by a membrane that selectively passes CO ₂ while blocking the transport of water or CO ₂ absorbent (FIG.5A). For this purpose, a membrane contactor with hollow fiber membranes was selected, and a test was carried out to see if the membrane could successfully separate the two phases. As shown in FIG.5B, deionized (DI) water and an aqueous solution of a quinone (50 mM of antraquinone-2,7-disulfonic acid) were fed to each inlet of the membrane contactor at a 1 mL/min flow rate. The photographs of the two phases after passing through the membrane contactor are shown in FIG.5C. The DI water (left) remained transparent, while the quinone solution (right) had a dark red color. Through this experiment, it was confirmed that the membrane contactor could prevent the mixing of the two phases, and specifically, no transfer of the absorbent molecules to the water was observed. In this system, after the CO ₂ absorbent extracts CO ₂ from the acidified water, the CO ₂ should be desorbed, and the absorbent should be regenerated, obtaining a highly concentrated CO2 stream. Anthraquinone-2,7-disulfonic acid was selected as the CO2 absorbent. The reduced quinone absorbs CO ₂ and can desorb CO ₂ by oxidizing the quinone electrochemically after the absorption is completed. Therefore, the redox reaction of quinone was investigated using cyclic 8913774.1 voltammetry (CV). FIG.6 shows apparent redox peaks, indicating that the quinone is successfully reduced and oxidized. An aqueous solution containing 50 mM of anthraquinone- 2,7-disulfonic acid and 0.3 M of NaCl was used as the electrolyte, and graphite felt was used as a working electrode. FIGS.7A-7B show the process diagrams of the system used for the transport of CO2 from water to the quinone solution in the membrane contactor. The system was operated in two steps. In the first sep (FIG.7A), the quinone was reduced in the electrochemical cell, and fed to the fibers within the membrane contactor, while the aqueous solution containing CO2 was introduced to the shell side of the contactor unit. This solution was prepared by adding hydrochloric acid to a 10 mM aqueous NaHCO ₃ solution. In the electrochemical cell, the ferricyanide redox couple reacted at the counter electrode. After 30 minutes, the system switched to the second step (FIG. 7B), in which the quinone was oxidized and the CO2 released. To verify that CO2 did transfer from the water phase to the quinone solution, the quinone reservoir was purged with nitrogen, and the CO ₂ concentration in the outlet was measured using a CO ₂ sensor. As shown in FIG.8, the CO2 concentration increased when the oxidative current was applied (left of the dotted line). From this result, it was confirmed that the CO2 contained in the water stream was transferred to the quinone solution through the membrane contactor, and the transferred CO ₂ could be desorbed through the electrochemical oxidation of the quinone. The electrochemical CO2 removal from simulated oceanwater combined with the quinone-based CO ₂ extraction was also demonstrated. FIGS.9A-9B show the process diagrams of this system. In the first step (FIG.9A), the acidified oceanwater from a Bi/BiOCl system was pumped to the membrane contactor, and CO2 was transferred to the quinone solution that was reduced in the other electrochemical cell. Then, the CO2-depleted oceanwater entered the other compartment of the Bi/BiOCl cell to be re-alkalized. After completing this step, the system switched to the second step (FIG.9B), in which the quinone solution was oxidized in the electrochemical cell, and the CO2 released. A nitrogen sweep stream was not used with measurement of the CO ₂ concentration, but the amount of gas released from the system was followed with a mass flow meter. As shown in FIG.10, the gas flow rate increased when the oxidative current was applied, indicating that CO2 was released at high concentration without the use of a sweep gas or a vacuum pump. 8913774.1 EXAMPLE 2 The following example describes the percentage of CO2 recovered from water using conventional degassing systems. In the limit of infinite membrane contactor area with a fixed driving force, the phase speciation resulting from degassing seawater or removing CO2 with vacuum can be determined with a standard flash calculation, subject to the following assumptions: (i) gas and liquid streams leaving the flash tank are in equilibrium with each other; (ii) the flash tank operates at isothermal conditions – all streams enter and leave at the specified temperature; (iii) complete separation of vapor and liquid phases is achieved – no liquid is entrained in the effluent vapor phase; and (iv) vapor solubilities are assumed to be governed by Henry’s law, and binary interactions are neglected. All modeled components “i” are considered volatile (i ∈ {H ₂ O, CO ₂ , O ₂ , N ₂ }). For ease of notation, the subset of gas-only species are denoted with a subscript j (j ∈ {CO ₂ , O ₂ , N ₂ }). Denoting molar flow rates of feed, vapor effluent, and liquid effluent as F _m , V _m , and L _m , respectively, and respective liquid and vapor fractions of species as xi and yi, respectively, the following mass balances and Dalton’s law relations can be determined: ^ _^ ^ _^,^ = ^ _^ ^ _^,^ + ^ _^ ^ _^,^ (1) (2) ^ _^^^ = ^ _^^^,^^^ (^ _^^^^^ ) (3) Solubility of gas phase species (CO2, O2, and N2) in water is determined using Henry’s constant. Data provided by the Engineering Equation Solver (EES) thermodynamic package define Henry’s constant relation with the following convention: ^ _^ (4) ^ _^ = ^ _^ (^ _^^^^^ ) Using the above equations, the effectiveness values (i.e., percentage of CO ₂ recovered from the seawater stream) for single (see FIGS.12A-12B) and double stage degassing systems (see FIGS.3A-13B) can be determined. The data indicates that, in conventional systems, the strength of the vacuum used to remove CO ₂ from water is proportional to the CO ₂ removal efficiency but requires more compression work downstream to raise the CO2 pressure such that the CO2 is suitable for industry applications. The conventional systems therefore result in an overall greater energy 8913774.1 penalty as compared to the systems described herein, which: (i) do not use a vacuum to remove CO2 from water; and (ii) utilize less compression downstream, as the removed CO2 has a greater pressure than the CO2 removed in conventional systems. While several embodiments of the present invention have been described and illustrated herein, those of ordinary skill in the art will readily envision a variety of other means and/or structures for performing the functions and/or obtaining the results and/or one or more of the advantages described herein, and each of such variations and/or modifications is deemed to be within the scope of the present invention. More generally, those skilled in the art will readily appreciate that all parameters, dimensions, materials, and configurations described herein are meant to be exemplary and that the actual parameters, dimensions, materials, and/or configurations will depend upon the specific application or applications for which the teachings of the present invention is/are used. Those skilled in the art will recognize, or be able to ascertain using no more than routine experimentation, many equivalents to the specific embodiments of the invention described herein. It is, therefore, to be understood that the foregoing embodiments are presented by way of example only and that, within the scope of the appended claims and equivalents thereto, the invention may be practiced otherwise than as specifically described and claimed. The present invention is directed to each individual feature, system, article, material, kit, and/or method described herein. In addition, any combination of two or more such features, systems, articles, materials, kits, and/or methods, if such features, systems, articles, materials, kits, and/or methods are not mutually inconsistent, is included within the scope of the present invention. All definitions, as defined and used herein, should be understood to control over dictionary definitions, definitions in documents incorporated by reference, and/or ordinary meanings of the defined terms. The indefinite articles “a” and “an,” as used herein in the specification and in the claims, unless clearly indicated to the contrary, should be understood to mean “at least one.” The phrase “and/or,” as used herein in the specification and in the claims, should be understood to mean “either or both” of the elements so conjoined, i.e., elements that are conjunctively present in some cases and disjunctively present in other cases. Multiple elements listed with “and/or” should be construed in the same fashion, i.e., “one or more” of the elements 8913774.1 so conjoined. Other elements may optionally be present other than the elements specifically identified by the “and/or” clause, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, a reference to “A and/or B”, when used in conjunction with open-ended language such as “comprising” can refer, in one embodiment, to A only (optionally including elements other than B); in another embodiment, to B only (optionally including elements other than A); in yet another embodiment, to both A and B (optionally including other elements); etc. As used herein in the specification and in the claims, “or” should be understood to have the same meaning as “and/or” as defined above. For example, when separating items in a list, “or” or “and/or” shall be interpreted as being inclusive, i.e., the inclusion of at least one, but also including more than one, of a number or list of elements, and, optionally, additional unlisted items. Only terms clearly indicated to the contrary, such as “only one of” or “exactly one of,” or, when used in the claims, “consisting of,” will refer to the inclusion of exactly one element of a number or list of elements. In general, the term “or” as used herein shall only be interpreted as indicating exclusive alternatives (i.e. “one or the other but not both”) when preceded by terms of exclusivity, such as “either,” “one of,” “only one of,” or “exactly one of.” “Consisting essentially of,” when used in the claims, shall have its ordinary meaning as used in the field of patent law. As used herein in the specification and in the claims, the phrase “at least one,” in reference to a list of one or more elements, should be understood to mean at least one element selected from any one or more of the elements in the list of elements, but not necessarily including at least one of each and every element specifically listed within the list of elements and not excluding any combinations of elements in the list of elements. This definition also allows that elements may optionally be present other than the elements specifically identified within the list of elements to which the phrase “at least one” refers, whether related or unrelated to those elements specifically identified. Thus, as a non-limiting example, “at least one of A and B” (or, equivalently, “at least one of A or B,” or, equivalently “at least one of A and/or B”) can refer, in one embodiment, to at least one, optionally including more than one, A, with no B present (and optionally including elements other than B); in another embodiment, to at least one, optionally including more than one, B, with no A present (and optionally including elements other than A); 8913774.1 in yet another embodiment, to at least one, optionally including more than one, A, and at least one, optionally including more than one, B (and optionally including other elements); etc. It should also be understood that, unless clearly indicated to the contrary, in any methods claimed herein that include more than one step or act, the order of the steps or acts of the method is not necessarily limited to the order in which the steps or acts of the method are recited. In the claims, as well as in the specification above, all transitional phrases such as “comprising,” “including,” “carrying,” “having,” “containing,” “involving,” “holding,” “composed of,” and the like are to be understood to be open-ended, i.e., to mean including but not limited to. Only the transitional phrases “consisting of” and “consisting essentially of” shall be closed or semi-closed transitional phrases, respectively, as set forth in the United States Patent Office Manual of Patent Examining Procedures, Section 2111.03. 8913774.1