Multistage absorption and desorption for co 2 separations

Abstract

The present disclosure describes systems and methods for capturing carbon dioxide from carbon dioxide-containing streams, such as carbon dioxide-containing gas streams. The systems described herein may comprise one or more absorption stages, one or more electrochemical cells, and / or one or more desorption stages. For example, in some embodiments, the system comprises an absorption stage, a multiplicity of electrochemical cells, and a multiplicity of desorption stages. In some embodiments, the system comprises a multiplicity of absorption stages, a multiplicity of electrochemical cells, and a desorption stage. In some embodiments, the system comprises a multiplicity of absorption stages, a multiplicity of electrochemical cells, and a multiplicity of desorption stages. Certain of the methods described herein may be performed in and / or using such a system.

Description

[0001]MULTISTAGE ABSORPTION AND DESORPTION FOR CO2 SEPARATIONS RELATED APPLICATIONS This application claims priority under 35 U.S.C. § 119(e) to U.S. Provisional Patent Application No. 63 / 707,718, filed October 15, 2024, and entitled “Multistage Absorption and Desorption for Electrochemically Mediated CO2Separations,” 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 Methods and systems for multistage absorption and desorption for CO2 separations are generally described. SUMMARY This Summary introduces a selection of concepts in simplified form that are described further below in the Detailed Description. This Summary neither identifies key or essential features, nor limits the scope, of the claimed subject matter. In one aspect, a system is provided. In some embodiments, the system comprises: an absorption stage comprising a sorbent; a multiplicity of desorption stages; and a multiplicity of electrochemical cells, wherein: each desorption stage in the multiplicity of desorption stages is fluidically connected to at least one of the electrochemical cells in the multiplicity of electrochemical cells; and at least one electrochemical cell in the multiplicity of electrochemical cells is fluidically connected to the absorption stage. In another aspect, a system is provided. In some embodiments, the system comprises: a multiplicity of absorption stages comprising a sorbent; a desorption stage; and a multiplicity of electrochemical cells, wherein: each absorption stage in the multiplicity of absorption stages is fluidically connected to at least one of the electrochemical cells in the multiplicity of electrochemical cells; and at least one electrochemical cell in the multiplicity of electrochemical cells is fluidically connected to the desorption stage. In another aspect, a method is provided. In some embodiments, the method comprises: in a first absorption stage, reacting carbon dioxide with a sorbent within a sorbent stream having #14498906v1 a first total CO2 loading to form a sorbent stream having a second total CO2 loading that is greater than the first total CO2loading; in a cathodic chamber of a first electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the second total CO2 loading; in a second absorption stage, reacting carbon dioxide with the sorbent within the sorbent stream having the second total CO2loading to form a sorbent stream having a third total CO2loading that is greater than the second total CO2loading; in an anodic chamber of the first electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the third total CO2 loading; in a desorption stage, releasing carbon dioxide from the sorbent stream having the third total CO2loading to form a sorbent stream having a fourth total CO2 loading that is less than the third total CO2 loading and that may optionally be equal to the first total CO2 loading; and in a cathodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the fourth total CO2 loading. In another aspect, a method is provided. In some embodiments, the method comprises: in a first absorption stage, reacting carbon dioxide with a sorbent within a sorbent stream having a first total CO2loading to form a sorbent stream having a second total CO2loading that is greater than the first total CO2 loading; in a cathodic chamber of a first electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the second total CO2loading; in a second absorption stage, reacting carbon dioxide with the sorbent within the sorbent stream having the second total CO2 loading to form a sorbent stream having a third total CO2 loading that is greater than the second total CO2 loading; in an anodic chamber of the first electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the third total CO2 loading; in an anodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the third total CO2loading; in a desorption stage, releasing carbon dioxide from the sorbent stream having the third total CO2loading to form a sorbent stream having a fourth total CO2 loading that is less than the third total CO2 loading and that may optionally be equal to the first total CO2 loading; and in a cathodic chamber of the second electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the fourth total CO2 loading. In another aspect, a method is provided. In some embodiments, the method comprises: in a first absorption stage, reacting carbon dioxide with a sorbent within a sorbent stream having a first total CO2 loading to form a sorbent stream having a second total CO2 loading that is greater than the first total CO2 loading; in a cathodic chamber of a first electrochemical cell, #14498906v1 performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the second total CO2loading; in a second absorption stage, reacting carbon dioxide with sorbent within the sorbent stream having the second total CO2 loading to form a sorbent stream having a third total CO2 loading that is greater than the second total CO2 loading; in an anodic chamber of the first electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the third total CO2loading; in a first desorption stage, releasing carbon dioxide from the sorbent stream having the third total CO2 loading to form a sorbent stream having a fourth total CO2 loading that is less than the third total CO2loading; in an anodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the fourth total CO2 loading; in a second desorption stage, releasing carbon dioxide from the sorbent stream having the fourth total CO2loading to form a sorbent stream having a fifth total CO2loading that is less than the fourth total CO2 loading and that may optionally be equal to the first total CO2 loading; and in a cathodic chamber of the second electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the fifth total CO2loading. In another aspect, a method is provided. In some embodiments, the method comprises: in an absorption stage, reacting carbon dioxide with a sorbent within a sorbent stream having a first total CO2loading to form a sorbent stream having a second total CO2loading that is greater than the first total CO2 loading; in an anodic chamber of a first electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the second total CO2loading; in a first desorption stage, releasing CO2from the sorbent stream having the second total CO2 loading to form a sorbent stream having a third total CO2 loading that is less than the second total CO2 loading; in an anodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the third total CO2loading; in a second desorption stage, releasing CO2from the sorbent stream having the third total CO2 loading to form a sorbent stream having a fourth total CO2 loading that is less than the third total CO2 loading and may optionally be equal to the first total CO2loading; and in a cathodic chamber of the second electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the fourth total CO2 loading. In another aspect, a system and / or method for separating (capturing) CO2is provided. In some embodiments, the system and / or method comprises: a. one or more pumps for moving CO2; b. a power supply for the one or more pumps; c. tubing and a valve; d. a feed gas #14498906v1 comprising CO2; e. an absorber that captures CO2; f. a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2 absorption in stages, followed by sequential deactivation and desorption; wherein activation and absorption are concurrent or sequential; g. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and h. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell. In another aspect, a system and / or method for separating (capturing) CO2 is provided. In some embodiments, the system and / or method comprises: a. one or more pumps for moving CO2; b. a power supply for the one or more pumps; c. tubing and a valve; d. a feed gas comprising CO2; e. an absorber that captures CO2; f. a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in stages; wherein activation and absorption are concurrent or sequential; g. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and h. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell. In another aspect, a system and / or method for separating (capturing) CO2 is provided. In some embodiments, the system and / or method comprises: a. one or more pumps for moving CO2; b. a power supply for the one or more pumps; c. tubing and a valve; d. a feed gas comprising CO2; e. an absorber that captures CO2; f. a multiplicity of electrochemical cells, wherein: i. one or more electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2absorption in stages, followed by sequential deactivation and desorption in stages; and ii. one or more electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2desorption in stages, g. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and h. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell. In another aspect, a system for separating CO2 is provided. In some embodiments, the system comprises: a. an absorber that captures CO2; b. a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2 absorption in stages, followed by sequential deactivation and desorption; wherein activation and absorption are concurrent or sequential; c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power #14498906v1 supply for creating an electrical current between an anode and a cathode of the electrochemical cell. In another aspect, a system for separating CO2 is provided. In some embodiments, the system comprises: a. an absorber that captures CO2; b. a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2desorption in stages; wherein activation and absorption are concurrent or sequential; c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell. In another aspect, a system is provided. In some embodiments, the method comprises: a. an absorber that captures CO2; b. a multiplicity of electrochemical cells, wherein i. one or more electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2 absorption in stages, followed by sequential deactivation and desorption in stages; and ii. one or more electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2desorption in stages, c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell. In another aspect, a method is provided. In some embodiments, the method comprises: a. providing a feed gas comprising CO2 to an absorber that captures CO2; b. providing the absorbed CO2 to a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2absorption in stages, followed by sequential deactivation and desorption; wherein activation and absorption are concurrent or sequential; c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell. In another aspect, a method is provided. In some embodiments, the method comprises: a. providing a feed gas comprising CO2 to an absorber that captures CO2; b. providing the absorbed CO2to a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in stages; wherein activation and absorption are concurrent or sequential; c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell. #14498906v1 In another aspect, a method is provided. In some embodiments, the method comprises: a. providing a feed gas comprising CO2to an absorber that captures CO2; b. providing the absorbed CO2 to a multiplicity of electrochemical cells, wherein i. one or more electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2 absorption in stages, followed by sequential deactivation and desorption in stages; and ii. one or more electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in stages, c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell. The following Detailed Description references the accompanying drawings which form a part this application, and which show, by way of illustration, specific example implementations. Other implementations may be made without departing from the scope of the disclosure. BRIEF DESCRIPTION OF THE DRAWINGS Non-limiting embodiments of the present disclosure 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 unless otherwise indicated. In the figures, each identical or nearly identical component illustrated is 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 disclosure shown where illustration is not necessary to allow those of ordinary skill in the art to understand the disclosure. In the figures: FIG. 1A is a schematic of a system comprising a multiplicity of absorption stages, a multiplicity of electrochemical cells, and a desorption stage, according to certain embodiments. FIG. 1B is a schematic of a system comprising a multiplicity of absorption stages, a multiplicity of electrochemical cells, and a desorption stage, according to certain embodiments. FIG. 1C is a schematic of a system comprising a multiplicity of absorption stages, a multiplicity of electrochemical cells, and a desorption stage, according to certain embodiments. FIG. 1D is a schematic of a system comprising an absorption stage, a multiplicity of electrochemical cells, and a multiplicity of desorption stages, according to certain embodiments. FIG. 1E a schematic of a system comprising an absorption stage, a multiplicity of electrochemical cells, and a multiplicity of desorption stages, according to certain embodiments. #14498906v1 FIG. 1F a schematic of a system comprising multiplicity of absorption stages, a multiplicity of electrochemical cells, and a multiplicity of desorption stages, according to certain embodiments. FIGS. 2A-2D show the following, in accordance with certain embodiments. FIG. 2A shows a direct cycle for a generic redox-active absorbent operating in aprotic media. A and A- represent the dormant and activated states, respectively. FIG. 2B shows a semi-direct cycle operating in protic media. AH represents the activated protonated state. FIG. 2C shows an indirect cycle: an electrochemically inert absorbent with a redox-active blocker species. Band B+ represent the dormant and activated states of the blocker, respectively. Inset graphs in FIGS. 2A-2C show the fraction of redox species active as a function of applied potential E, with the standard potential, E0, marked by a dashed gray line. FIG. 2D shows an example sorbent used in direct and semi-direct processes. FIGS. 3A-3D show depictions of previously proposed systems; a) depiction of a 4-stage configuration with sequential activation, absorption, deactivation, and desorption b) depiction of 3 stage system with sequential activation and absorption followed by concurrent deactivation and desorption c) depiction of 3 stage system with concurrent activation and absorption followed by sequential deactivation and desorption d) depiction of a two-stage configuration with coupled activation and absorption, and with coupled deactivation and desorption. FIGS. 3E-3H show thermodynamic cycles for CO2separations with an arbitrary electrochemical sorbent, with the minimum work of separation for a given process represented by the area enclosed, in accordance with certain embodiments. Cycles correspond to the processes depicted in FIGS. 3A-3D. FIG. 3E shows a thermodynamic cycle for a 4-stage configuration with sequential activation, absorption, deactivation, and desorption; numbers correspond to states shown in FIG. 3A. FIG 3F shows a thermodynamic cycle for a 3-stage configuration with concerted activation and absorption followed by sequential deactivation and desorption (see FIG. 3B). FIG. 3G shows a thermodynamic cycle for a 3-stage configuration with sequential activation and absorption followed by concerted deactivation and desorption (see FIG. 3C). FIG. 3H shows a thermodynamic cycle for a two-stage configuration with coupled activation and absorption, and with coupled deactivation and desorption (see FIG. 3D). FIGS. 4A-4B show depictions of multistage systems, in accordance with certain embodiments. FIG. 4A is a depiction of a system with electrochemical activation and CO2 absorption in stages, followed by sequential deactivation and desorption. FIG. 4B is a depiction of a system with sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in stages. #14498906v1 FIGS. 5A-5B show thermodynamic cycles for newly proposed CO2 separations with an arbitrary electrochemical sorbent, with the minimum work of separation with such a process represented by the area enclosed, in accordance with certain embodiments. FIG. 5A shows a thermodynamic cycle for a system with electrochemical activation and CO2 absorption in stages, followed by sequential deactivation and desorption; numbers correspond to states in FIG. 4A. FIG. 5B shows a thermodynamic cycle for a system with sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in stages; numbers correspond to states in FIG. 4B. FIGS. 6A-6B show the following, in accordance with certain embodiments. FIG. 6A shows a nominal thermodynamic cycle for a system with sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in four stages. FIG. 6B shows a percentage of deactivation / desorption decoupling penalty reduced as a function of stages. FIG. 7 shows the maximum predicted CO2 partial pressure experienced in the cell as a function of the number of desorption stages, in accordance with certain embodiments. FIGS. 8A-8H show depictions of previously proposed systems and their corresponding thermodynamic cycles. On all plots, the curved dotted lines denote potentials for constant CO2loadings over all speciations (CO2 ,g, CO2 ,sol, and Q-mCO2) and the horizontal lines denote CO2 isobars. FIG. 8A is a depiction of a 4-stage EMCC system configuration with discrete, sequential activation, absorption, deactivation, and desorption. FIG. 8B shows corresponding thermodynamic cycle for a 4-state system in FIG. 8A with 50% state of charge swing. FIG.8C is a depiction of 3-stage system with concurrent activation and absorption followed by sequential deactivation and desorption. FIG. 8D shows corresponding thermodynamic cycle for a 3-stage system in FIG. 8C with cathodic absorption. FIG 8E is a depiction of 3-stage system with sequential activation and absorption followed by concurrent deactivation and desorption. FIG. 8F shows corresponding thermodynamic cycle for a 3-stage system with anodic desorption shown in FIG. 8E. FIG. 8G is a depiction of 2-stage system featuring both concurrent activation and absorption and concurrent deactivation and desorption. FIG. 8H shows a corresponding thermodynamic cycle for a system with cathodic absorption and anodic desorption shown in FIG. 8G. FIGS. 9A-9D depict process diagrams and thermodynamic cycles for newly proposed multistage CO2 separation systems with the minimum process work represented by the area enclosed, in accordance with certain embodiments. Sorbent properties are identical to those assumed in FIGS. 8A-8H. FIG. 9A is a depiction of an EMCC system configuration with activation and absorption split over two stages, followed by discrete deactivation and desorption, #14498906v1 . FIG. 9B shows corresponding thermodynamic cycle diagram for sequential system with staged absorption shown in FIG. 9A, with the original 4-stage process overlaid as a dotted line. FIG. 9C is a depiction of an EMCC system configuration with sequential activation and absorption followed by deactivation and desorption split over two discrete stages. FIG. 9D shows a corresponding thermodynamic cycle diagram for sequential system with staged desorption shown in FIG. 9C, with the original 4-stage process overlaid as a dotted line. FIGS. 10A-10F depict multistage EMCC systems in the limit of many stages, in accordance with certain embodiments. FIG. 10A is a depiction of an EMCC system configuration with activation and absorption split over many counterflowing stages in series, followed by sequential deactivation and desorption. FIG. 10B shows a thermodynamic cycle diagram for sequential system with 10 absorption stages shown in FIG. 10A, with the original 4- stage process overlaid as a dotted line. FIG. 10C is a depiction of an EMCC system configuration with activation and absorption split over many stages with feed gas piped into each in parallel, followed by sequential deactivation and desorption. FIG. 10D shows a thermodynamic cycle diagram for sequential system with 10 absorption stages from parallelized feed gas shown in FIG. 10C, with the original 4-stage process overlaid as a dotted line. FIG. 10E is a depiction of an EMCC system configuration with sequential activation and absorption followed by deactivation and desorption split over many stages. FIG. 10F shows a corresponding thermodynamic cycle diagram for sequential system with desorption split over 10 stages shown in FIG. 10E, with the original 4-stage process overlaid as a dotted line. Parameters in b / d / f are identical to those used in FIGS. 8A-8H. FIGS. 11A-11D show performance metrics as a function of the number of sequential gas exchange stages, calculated by iteratively generating and evaluating process cycle diagrams in the manner depicted in FIG. 10B, FIG. 10D, and FIG. 10F, in accordance with certain embodiments. FIG. 11A shows the process work of staged absorption in series or in parallel with anodic desorption, benchmarked against 3-stage work, ideal work for 50% capture, and work of capture from an infinite reservoir. FIG. 11B shows the maximum achievable CO2 capture as a function of the number of parallel absorption stages. FIG. 11C shows the reduction in work penalty associated with discrete operations relative to concerted operations. Here, absorption is assumed to occur with feed gas piped in series, as it approaches the 2-stage limit. FIG. 11D shows the maximum anodic CO2 partial pressure as a function of the number of desorption stages. DETAILED DESCRIPTION #14498906v1 The present disclosure describes systems and methods for capturing carbon dioxide from carbon dioxide-containing streams, such as carbon dioxide-containing gas streams. The systems described herein may comprise one or more absorption stages, one or more electrochemical cells, and / or one or more desorption stages. For example, in some embodiments, the system comprises an absorption stage, a multiplicity of electrochemical cells, and a multiplicity of desorption stages. In some embodiments, the system comprises a multiplicity of absorption stages, a multiplicity of electrochemical cells, and a desorption stage. In some embodiments, the system comprises a multiplicity of absorption stages, a multiplicity of electrochemical cells, and a multiplicity of desorption stages. Certain of the methods described herein may be performed in and / or using such a system. As atmospheric carbon dioxide (CO2) concentrations continue to increase beyond pre- industrial levels, it is desirable to develop economical, energy-efficient, and scalable CO2separation technologies, such as carbon capture systems. Carbon capture systems may be useful both for decarbonizing industrial activities and remediating legacy emissions. In particular, electrochemical carbon capture systems such as electrochemically mediated sorbent-based carbon capture systems are attractive as an electrically driven alternative to traditional thermally based separations, which are energy-intensive and often rely on the use of fossil fuels. In electrochemically mediated sorbent-based carbon capture systems, a sorbent (such as redox-active sorbent) is used to capture CO2as the CO2bonds with and / or associates with the sorbent. The sorbent may be configured to undergo a change in its state of charge when subjected to an electrochemical reaction (e.g., reduction and / or oxidation). In some embodiments, reduction of the sorbent may activate the sorbent. Oxidation of the sorbent may deactivate the sorbent. As described in greater detail below, the activated (e.g., reduced) sorbent may be reactive with CO2, and the deactivated (e.g., oxidized) sorbent may not be reactive with CO2and / or may release CO2associated with the sorbent. As described in greater detail below, it may be advantageous to control and / or modify the reactivity of the sorbent with CO2in order to capture and / or release CO2 at a particular time and / or in a particular stage of the system. Electrochemical reactions involving the sorbent may be performed to modulate and / or control the absorption and release of CO2by the sorbent, for example activating the sorbent via a reduction reaction prior to and / or while reacting the sorbent with CO2 and / or deactivating the sorbent via an oxidation reaction prior to and / or while releasing CO2 from the sorbent. Many currently available or proposed electrochemically mediated sorbent-based carbon capture systems are configured as two-stage systems or four-stage systems. Four-stage systems, in which the activation of the sorbent is performed separately from the capture of CO2 using the #14498906v1 activated sorbent (e.g., by reacting and / or associating the CO2 with the sorbent) and the deactivation of the sorbent is performed separately from the release of the CO2, are typically preferred due to their straightforward design. Four-stage systems often use standard absorption columns and flash tanks separate from the electrochemical cell for easier gas handling (as shown in the diagram of FIG. 3A and associated thermodynamic cycle of FIG. 3E); however, this comes at the expense of a buildup of products in the activation / deactivation cell (e.g., the electrochemical cell), resulting in a thermodynamic penalty and reducing energy efficiency. These penalties can be offset by moving to three-stage system architectures, binding activated sorbent with CO2upon formation (as shown in the diagram of FIG. 3B and associated thermodynamic cycle in FIG. 3F) or removing CO2 from the system immediately upon release (as shown in the diagram of FIG. 3C and thermodynamic cycle in FIG. 3G). Accounting only for variations in open circuit potential, the minimum energy of CO2separation using a particular sorbent is achieved using a two-stage system, with combined activation / absorption and deactivation / desorption occurring in the cell (as shown in the diagram in FIG. 3D and associated thermodynamic cycle in FIG. 3H). This configuration can be challenging to achieve in practice, as it necessitates the use of gas diffusion electrodes or hollow fiber membranes. Increases in activation and mass transfer overpotentials with such architectures often outweigh improvements in the minimum thermodynamic work required. The systems and methods provided in this disclosure may comprise a multiplicity of absorption stages and / or a multiplicity of desorption stages. The absorption stage(s) and desorption stage(s) are present in the system in combination with a multiplicity of electrochemical cells. For example, in some embodiments, an electrochemically mediated carbon capture system with multiple stages of sequential activation / absorption (as shown in FIG. 4A, in accordance with certain embodiments) or deactivation / desorption (as shown in FIG. 4B, in accordance with certain embodiments) is described. These systems and methods may be used to perform multiple sequential activation and absorption steps and / or multiple sequential deactivation and desorption steps. The systems and methods described herein may have, in accordance with certain embodiments, several advantages over existing carbon capture systems. For example, these systems and methods may leverage the practical designs of systems in which the sorbent activation and absorption and / or sorbent deactivation and desorption are separated (e.g., 4-stage systems, as described above) while achieving significantly higher efficiency. For example, these systems and methods may facilitate practical integration with the designs of existing 4-stage systems, while also reducing the thermodynamic penalties associated with deviating from the ideal 2-stage case. The energy savings of some of the proposed systems #14498906v1 relative to typical 4-stage systems are shown in FIGS. 5A-5B, according to certain embodiments. The systems and methods described herein may involve the use of a sorbent. The sorbent can be a material that reacts with (e.g., absorbs) carbon dioxide. The sorbent may be an electrochemically modulated sorbent. For example, as noted above, the sorbent may be activated (e.g., such that it is reactive with CO2) and / or deactivated (such that it is not reactive with CO2 and / or releases CO2) by an electrochemical reaction. In some embodiments, the sorbent is activated when reduced and deactivated when oxidized. A sorbent reacting with CO2 may comprise the sorbent physically associating with the CO2or chemically reacting with the CO2 to form a different compound. In some embodiments, the sorbent is contained within a sorbent stream. For example, as described in greater detail below, the sorbent may be contained within a medium, such that the sorbent and the medium together comprise the sorbent stream. The medium may comprise a liquid, such as a solvent. The sorbent may be dissolved within the medium and / or suspended within the medium, such that when the medium is conveyed (e.g., pumped), the sorbent is conveyed along with it. For example, the medium may be conveyed from a first location within the system (e.g., an absorption stage) to a second location within the system (e.g., an electrochemical cell), and the sorbent may be conveyed from the first location to the second location along with the medium. The sorbent and / or sorbent stream may be present in any of the components of the system. For example, the sorbent stream may be present in the absorption stage and / or the multiplicity of absorption stages, the desorption stage and / or the multiplicity of desorption stages, and / or the electrochemical cell and / or the multiplicity of electrochemical cells. The sorbent stream may be present in the cathodic chamber of an electrochemical cell and / or the anodic chamber of an electrochemical cell. In certain embodiments, the sorbent stream can be cycled through the various components of the systems described herein, as shown in the accompanying figures and explained in further detail elsewhere herein. The sorbent stream may have a total CO2 loading. The “total CO2 loading” of a given sorbent stream generally refers to the total amount of CO2that has reacted with and / or associated with the sorbent and the amount (if any) of CO2 contained within (e.g., absorbed within) any component of the sorbent stream that is not the sorbent (e.g., the medium, as described elsewhere herein). For example, sorbent within a sorbent stream having a first total CO2loading may react with and / or associate with CO2 to form a sorbent stream having a second total CO2 loading, where the second total CO2 loading is greater than the first total CO2 loading. #14498906v1 Similarly, a sorbent stream having a third total CO2 loading may release CO2 to form a sorbent stream having a fourth total CO2loading, where the third total CO2loading is greater than the fourth total CO2 loading. As discussed in greater detail below, a sorbent stream may be transformed from a first total CO2 loading to a second total CO2 loading by contacting the sorbent stream with CO2such that the sorbent contained therein reacts with CO2(e.g., in the absorption stage, in which case, the second total CO2loading would be higher than the first total CO2 loading), or by releasing CO2 from the sorbent stream (e.g., in a desorption stage, as described below, in which case, the second total CO2 loading would be lower than the first total CO2loading). In some embodiments, a sorbent may be activated and / or deactivated within a sorbent stream without changing the total CO2 loading of the sorbent stream. For example, in some embodiments, the sorbent within a sorbent stream may have reacted with and / or associated with CO2 (e.g., may have absorbed CO2). In some embodiments, when the sorbent is deactivated, the CO2 may be released from the sorbent but still contained within the sorbent stream (e.g., may be contained and / or dissolved within a medium of the sorbent stream). In some embodiments, a sorbent may be activated within a sorbent stream, the total CO2loading the sorbent stream may not change until said sorbent stream is contacted with CO2 such that the CO2 reacts with and / or associates with the activated sorbent. In some embodiments, for a given sorbent, such as an electrochemically modulated sorbent (denoted "Q"), electrochemical carbon capture systems operate through four primary reactions: a. Electrochemical: Sorbent activation (Q + e ^ Q-) b. Gas Exchange: CO2 absorption (CO2,g ^ CO2,sol ; Q- + CO2,aq ^ Q-CO2) c. Electrochemical: Sorbent deactivation (Q- CO2 Q + CO2,aq + e-) d. Gas Exchange: CO2release (CO2,sol ^ CO2,g) These reactions can be performed individually as sequential unit operations or with concerted electrochemical and gas exchange steps (e.g., coupled activation / absorption or deactivation / desorption, as described above). Any of a variety of suitable sorbent chemistries may be used in the systems and methods described herein, as described in greater detail below. Sorbent chemistries may vary but, in general, follow one of three schemes: direct binding of CO2 to a redox active sorbent, semi- direct CO2absorption via a pH-swing in protic media, or indirect modulation of an electrochemically inactive CO2 sorbent through the use of faradaic blockers. These schemes are summarized in FIGS. 2A-2C, in which FIG. 2A shows a direct cycle for a generic redox-active #14498906v1 absorbent operating in aprotic media, where A and A- represent the dormant and activated states, respectively. FIG. 2B shows a semi-direct cycle operating in protic media, where AH represents the activated protonated state. FIG. 2C shows an indirect cycle, comprising an electrochemically inert absorbent with a redox-active blocker species, where B and B+ represent the dormant and activated states of the blocker, respectively. The sorbent may comprise any of a variety of suitable materials. For example, the sorbent may comprise a quinone, a bipyridine, a disulfide, and / or a transition metal complex. FIG. 2D shows several non-limiting examples types of sorbents that may be used in direct and semi-direct absorption processes, as described above. The systems and methods described herein may use any number of other types of sorbents (e.g., any suitable electrochemically modulated sorbent). As noted above, the sorbent may be contained within a medium (e.g., as part of a sorbent stream comprising the sorbent and the medium). In some embodiments, the medium is a protic medium. The protic medium may be a protic solvent, such as water. In some embodiments, the medium is an aprotic medium, such as an aprotic solvent. The aprotic solvent may comprise diglyme, dimethyl sulfoxide, dimethylformamide, and / or an ionic liquid. In some embodiments, the medium is chosen such that the sorbent is stably and / or safely contained within the medium. In some embodiments, the medium may have a synergistic effect on the reaction of the sorbent with carbon dioxide during absorption of the carbon dioxide by the sorbent. For example, a protic medium may facilitate a pH swing in a semi-direct absorption process, as described above. An aprotic medium may facilitate the reaction of carbon dioxide with an electrochemically active sorbent in a direct absorption process, as described above. The medium may also have synergistic effects on the release of CO2 from the sorbent or one or more chemical reactions involving the sorbent. In some embodiments, a system for capturing carbon dioxide is provided. In some embodiments, the system comprises an absorption stage, such as first absorption stage 102a of system 100a shown in FIG. 1A. The absorption stage may be configured to facilitate contact between a sorbent (e.g., within a sorbent stream) and CO2. For example, the absorption stage may be configured to facilitate contact between a carbon dioxide-containing gas stream and a sorbent contained within the absorption stage. In FIG. 1A, the carbon dioxide-containing second absorption stage output gas stream 180b is provided to first absorption stage 102a, which may facilitate contact between the CO2and a sorbent (e.g., within a sorbent stream) contained within first absorption stage 102a. Contacting the CO2 and the sorbent may cause the CO2 to react with #14498906v1 the sorbent, thereby transferring the CO2 from the carbon dioxide-containing second absorption stage output gas stream 180b to the sorbent stream. As described in greater detail below, the sorbent stream may have a particular CO2 loading prior to being contacted with the CO2. In some embodiments, the sorbent stream may transition from a first total CO2loading to a second total CO2loading that is higher than the first total CO2loading within the absorption stage. For example, in FIG. 1A, first absorption stage input stream 110a may have a first total CO2 loading, and may be transformed into first absorption stage output stream 110b having a second, higher total CO2 loading within first absorption stage 102a. First absorption stage 102a of system 100a facilitates the contact of the sorbent within first absorption stage input stream 110a (which has a first total CO2 loading) with CO2 within second absorption stage output gas stream 180b, allowing the CO2 to react with the sorbent contained within first absorption stage input stream 110a and form first absorption stage output stream 110b (which has a second total CO2 loading that is higher than the first total CO2 loading). The absorption stages described herein may have any of a variety of suitable configurations. For example, the absorption stage may comprise an absorption column or a hollow fiber contactor. The absorption column may be any suitable type of absorption column, such as a packed column or a plate column. The hollow fiber contactor may have a shell-and- tube configuration or a crossflow configuration. In some embodiments, a hollow fiber contactor comprises microporous and / or composite fibers, which may comprise ceramic, metal, and / or polymeric materials. As noted above, some embodiments, the sorbent is or is contained in a liquid phase (e.g., the sorbent may be contained in a protic medium or an aprotic medium). In some such embodiments, the absorption stage is a gas-liquid contact vessel. The absorption stage may be configured as a counterflow absorber or a co-flow absorber. In some embodiments, one, more, or all of the absorption stages in the system can produce a stream comprising sorbent and having a CO2loading, as measured in moles per liter, that is at least 0.001% higher, at least 0.005% higher, at least 0.01% higher, at least 0.05% higher, at least 0.1% higher, at least 0.5% higher, at least 1% higher, at least 2% higher, at least 5% higher, at least 25% higher, at least 50% higher, at least 100% higher, at least 250% higher, at least 500% higher, or more than the CO2 loading of the stream comprising sorbent that is input to the absorption stage. (To illustrate, a stream having a CO2 loading that is 100% higher than another stream would have a loading of CO2that is two times the loading of CO2in the other stream.) For example, in FIGS. 1A-1F, one, more, or all of absorption stages 102a, 102b, 102, 202a, and / or 202b can produce a stream comprising sorbent and having a CO2 loading (e.g., #14498906v1 streams 110b, 110d, 130b, 210b, and / or 210d, respectively), as measured in moles per liter, that is at least 0.001% higher, at least 0.005% higher, at least 0.01% higher, at least 0.05% higher, at least 0.1% higher, at least 0.5% higher, at least 1% higher, at least 2% higher, at least 5% higher, at least 25% higher, at least 50% higher, at least 100% higher, at least 250% higher, at least 500% higher, or more than the CO2loading of the stream comprising sorbent that is input to the absorption stage (e.g., streams 110a, 110c, 130a, 210a, and 210c, respectively). In some embodiments, the system comprises a multiplicity of absorption stages. The multiplicity of absorption stages may comprise two or more absorption stages. For example, system 100a shown in FIG. 1A comprises a multiplicity of absorption stages comprising first absorption stage 102a and second absorption stage 102b. The multiplicity of absorption stages may comprise any suitable number of absorption stages. For example, the multiplicity of absorption stages may comprise two more absorption stages, three or more absorption stages, five our more absorption stages, ten or more absorption stages, twenty or more absorption stages, or more. As described in greater detail below, a system comprising a multiplicity of absorption stages may advantageously increase the efficiency of the system. In certain embodiments, each additional absorption stage in the multiplicity of absorption stages may be associated with improved efficiency of the system. In some embodiments, two or more absorption stages in the plurality of absorption stages are fluidically connected and / or in fluidic communication. For example, in FIG. 1A, first absorption stage 102a and second absorption stage 102b of system 100a are directly fluidically connected by second absorption stage output gas stream 180b, which provides CO2-containing gas to first absorption stage 102a from second absorption stage 102b. As used herein, two elements are in fluidic communication with each other when fluid may be transported from one of the elements to the other of the elements without otherwise altering the configurations of the elements or a configuration of an element between them (such as a valve). For example, a first absorption stage and a second absorption stage connected by a conduit lacking any valves or comprising an open valve (thus allowing for the flow of fluid between the absorption stage and the electrochemical cell) are considered to be in fluidic communication with each other. In contrast, two conduits separated by a closed valve (thus preventing the flow of fluid between the conduits) are not considered to be in fluidic communication with each other. As used herein, two elements are fluidically connected to each other when they are connected such that, under at least one configuration of the elements and any intervening elements, the two elements are in fluidic communication with each other. For example, a first #14498906v1 absorption stage and a second absorption stage connected by a valve and conduits that permit flow between the first absorption stage and the second absorption stage in at least one configuration of the valve would be said to be fluidically connected to each other, even when the position of the valve does not place the first absorption stage and the second absorption stage in fluidic communication. Elements that are in fluidic communication with each other are always fluidically connected to each other, but not all elements that are fluidically connected to each other are necessarily in fluidic communication with each other. Various components are described herein as being fluidically connected. Fluidic connections may be either direct fluidic connections or indirect fluidic connections. Generally, a direct fluidic connection exists between a first region and a second region (and the two regions are said to be directly fluidically connected to each other) when they are fluidically connected to each other and when the composition of the fluid at the second region of the fluidic connection has not substantially changed relative to the composition of the fluid at the first region of the fluidic connection (i.e., no fluid component that was present in the first region of the fluidic connection is present in a weight percentage in the second region of the fluidic connection that is more than 5% different from the weight percentage of that component in the first region of the fluidic connection). As an illustrative example, a stream that connects first and second units, and in which the pressure and temperature of the fluid is adjusted but the composition of the fluid is not altered, would be said to directly fluidically connect the first and second units. If, on the other hand, a separation step is performed and / or a chemical reaction is performed that substantially alters the composition of the stream contents during passage from the first unit to the second unit, the stream would not be said to directly fluidically connect the first and second units. In some embodiments, a direct fluidic connection between a first region and a second region can be configured such that the fluid does not undergo a phase change from the first region to the second region. In some embodiments, the direct fluidic connection can be configured such that at least 50 wt% (or at least 75 wt%, at least 90 wt%, at least 95 wt%, or at least 98 wt%) of the fluid (e.g., liquid) in the first region is transported to the second region via the direct fluidic connection. Any of the fluidic connections described herein may be, in some embodiments, direct fluidic connections. For example, in the figures, in certain instances in which two units (e.g., an electrochemical cell, an absorption stage, a desorption stage, etc.) are shown as being connected by only streams or conduits, those two units can be directly fluidically connected, in some embodiments. In other cases, the fluidic connections may be indirect fluidic connections. #14498906v1 In some embodiments, at least two absorption stages in the multiplicity of absorption stages are in gaseous communication. For example, as noted above, in FIG. 1A, first absorption stage 102a and second absorption stage 102b of system 100a are in gaseous communication, such that the carbon dioxide-containing second absorption stage output gas stream 180b that is output from second absorption stage 102b is provided to first absorption stage 102a. In some embodiments, two absorption stages may not be in gaseous communication. For example, as shown in FIG. 1C, first absorption stage 102a and second absorption stage 102b of system 100c are not in gaseous communication. In some embodiments in which the system comprises two or more absorption stages, two or more such absorption stages may be physically contained within the same unit. For example, the two or more absorption stages may be contained within the same plate absorption column. In some embodiments, the two or more absorption stages are physically contained in separate units. For example, a first absorption stage may comprise a first packed absorption column, and a second absorption stage may comprise a second packed absorption column. The absorption stage may comprise any other suitable unit operation configured to facilitate the absorption of carbon dioxide by a sorbent and / or sorbent stream. In some embodiments, the system comprises a desorption stage. For example, system 100a shown in FIG. 1A comprises desorption stage 106. The desorption stage may be configured to facilitate the release of carbon dioxide from a sorbent stream, as described elsewhere herein. In some embodiments, the desorption stage is configured to accept an input comprising a sorbent (e.g., a sorbent stream having a first total CO2 loading). The desorption stage may be configured to facilitate the desorption of carbon dioxide from the sorbent stream and produce as an output a carbon dioxide-containing gas stream and a sorbent stream having a second total CO2 loading that is lower than the first total CO2 loading. For example, in FIG. 1B, desorption stage 106 of system 100b accepts desorption stage input stream 110g, which comprises a sorbent, as an input. Desorption stage 106 facilitates the release of CO2from desorption stage input stream 110g, and produces carbon-dioxide containing desorption stage output gas stream 112 and desorption stage output stream 110f as outputs, in which desorption stage output stream 110f has a lower total CO2loading than desorption stage input stream 110g. The desorption stage may have any of a variety of suitable configurations. For example, the desorption stage may comprise a flash tank, a packed and / or trayed vessel, and / or a membrane contactor and / or degassing unit. In some embodiments, the system comprises a multiplicity of desorption stages. The multiplicity of desorption stages may comprise two or more desorption stages. For example, #14498906v1 system 100d shown in FIG. 1D comprises a multiplicity of desorption stages comprising first desorption stage 106a and second desorption stage 106b. In some embodiments, two or more desorption stages in the plurality of absorption stages are fluidically connected and / or in fluidic communication. For example, in FIG. 1D first desorption stage 106a and second desorption stage 106b of system 100e are fluidically connected by first desorption stage output gas stream 112a and gas output redirect stream 112c, which provide CO2-containing gas from first desorption stage 106a to second desorption stage 106b. In some such embodiments, first desorption stage 106a and second desorption stage 106b of system 100d are said to be in gaseous communication. The multiplicity of desorption stages may comprise any suitable number of desorption stages. For example, the multiplicity of desorption stages may comprise two more desorption stages, three or more desorption stages, five our more desorption stages, ten or more desorption stages, twenty or more desorption stages, or more. As described in greater detail below, a system comprising a multiplicity of desorption stages may advantageously increase the efficiency of the system. In certain embodiments, each additional desorption stage in the multiplicity of desorption stages may be associated with improved efficiency of the system. In some embodiments in which the system comprises a multiplicity of (e.g., two or more) desorption stages, each of the desorption stages may be of the same type or of a different type. For example, the system may comprise a first desorption stage comprising a flash tank and a second desorption stage comprising a gas stripper. The desorption stage may comprise any other suitable unit operation configured to facilitate the desorption of carbon dioxide from a sorbent stream. In some embodiments, one, more, or all of the desorption stages in the system can be configured such that at least 0.001%, at least 0.005%, at least 0.01%, at least 0.05%, at least 0.1%, at least 0.5%, at least 1%, at least 2%, at least 5%, at least 10%, at least 25%, or more of the CO2that enters the desorption stage via the stream comprising sorbent exits the desorption stage as CO2 gas (e.g., separate from another stream exiting the desorption stage that comprises sorbent). For example, in FIGS. 1A-1F, one, more, or all of desorption stages 106, 106a, 106b, 206a, and 206b can be configured such that at least 0.001%, at least 0.005%, at least 0.01%, at least 0.05%, at least 0.1%, at least 0.5%, at least 1%, at least 2%, at least 5%, at least 10%, at least 25%, or more of the CO2 that enters the desorption stage via the stream comprising sorbent (e.g., via streams 110e, 110g, 130c, 112c, 210e, and / or 212c) exits the desorption stage as CO2gas (e.g., via streams 112, 112a, 112b, 212a, and / or 212b). In some embodiments, the system is configured such that at least 0.1%, at least 0.5%, at least 1%, at least 2%, at least 5%, at least #14498906v1 10%, at least 25%, at least 50%, at least 75%, at least 90%, at least 95%, at least 99%, at least 99.9%, at least 99.99%, or more of the CO2that is adsorbed in the adsorber(s) of the system is desorbed in the desorber(s) of the system and exits the system as CO2 gas (e.g., via streams 112, 112a, 112b, 212a, and / or 212b). The system may comprise an electrochemical cell. In some embodiments, the electrochemical cell is configured to facilitate one or more chemical reactions involving a sorbent. The electrochemical cell may be configured to facilitate one or more chemical reactions involving a sorbent that is contained within a sorbent stream. For example, the electrochemical cell may be configured to facilitate one or more electrochemical reactions involving the sorbent (e.g., activating and / or deactivating by reducing and / or oxidizing the sorbent), as described elsewhere herein. In some embodiments, the electrochemical cell is configured to facilitate one or more electrochemical reactions (e.g., involving a sorbent) when an electrical potential is applied to the electrochemical cell (e.g., using a power supply). An electrochemical reaction involving the sorbent may change a property of the sorbent. For example, as noted above, the electrochemical reaction may reduce (e.g., activate) and / or oxidize (e.g., deactivate) the sorbent. The electrochemical cell may be configured to facilitate any of a variety of electrochemical reactions involving the sorbent. For example, the electrochemical cell may be configured to facilitate a liquid-solid electrochemical reaction, such as the corrosion and electrodeposition of copper or zinc in an electrochemically mediated amine regeneration system, ion-intercalating material, and / or ion-adsorbing material. In some embodiments, the electrochemical cell is configured to facilitate a liquid-liquid electrochemical reaction, such as homogeneous oxidation and reduction of a dissolved or liquid quinone, disulfide, and / or phenazine. The electrochemical cell may be configured to facilitate a liquid-gas electrochemical reaction, such as a hydrogen oxidation / evolution reaction and / or a an oxidation reduction / evolution reaction. In some embodiments, the electrochemical cell comprises a cathodic chamber and an anodic chamber. For example, first electrochemical cell 104a of system 100a shown in FIG. 1A comprises cathodic chamber 120a and anodic chamber 120b. The cathodic chamber and the anodic chamber may be separated by an ion-permeable material, such as ion-permeable material 124 separating cathodic chamber 120a and anodic chamber 120b of first electrochemical cell 104a of system 100a. In some embodiments, the ion-permeable material is an ion-permeable membrane. The ion-permeable material may be selective or non-selective. In some embodiments, the cathodic chamber comprises a cathode. The cathode may comprise a porous electrode and / or planar electrode comprising graphite, conductive carbon, titanium, copper steel, and / or zinc. In some embodiments, the cathode comprises a deposited #14498906v1 electrocatalyst. In some embodiments, the cathode does not comprise a deposited electrocatalyst. In some embodiments, the cathodic chamber contains and / or is configured to contain a sorbent and / or a sorbent stream. The cathode may be configured to facilitate and / or participate in one or more electrochemical reactions involving the sorbent. For example, the cathode may be configured to facilitate and / or participate in a reduction reaction involving the sorbent. In some embodiments, the reduction reaction activates the sorbent. Activating the sorbent may change a property of the sorbent, such as its state of charge, such that it becomes more energetically favorable for the sorbent to participate in one or more subsequent reactions, such as a reaction with CO2. Activating the sorbent may cause the sorbent to react with CO2(e.g., within the cathodic chamber and / or within an absorption stage to which the activated sorbent is conveyed). The anodic chamber may comprise an anode. The anode may comprise a porous electrode and / or planar electrode comprising graphite, conductive carbon, titanium, copper steel, and / or zinc. In some embodiments, the cathode comprises a deposited electrocatalyst. In some embodiments, the cathode does not comprise a deposited electrocatalyst. In some embodiments, the anodic chamber contains and / or is configured to contain a sorbent and / or a sorbent stream, as described elsewhere herein. The anode may be configured to facilitate and / or participate in one or more electrochemical reactions involving the sorbent. For example, the anode may be configured to facilitate and / or participate in an oxidation reaction involving the sorbent. In some embodiments, oxidation reaction deactivates the sorbent. Deactivating the sorbent may comprise changing a property of the sorbent, such as its state of charge, such that it becomes more energetically favorable for the sorbent to participate in one or more subsequent reactions, such as releasing CO2. Deactivating the sorbent may cause the sorbent to release CO2 (e.g., within the anodic chamber and / or within a desorption stage to which the deactivated sorbent is conveyed). The system may comprise one or more electrochemical cells. In some embodiments, the system comprises a multiplicity (e.g., two or more) electrochemical cells. For example, system 100a shown in FIG. 1A comprises a multiplicity of electrochemical cells comprising first electrochemical cell 104a and second electrochemical cell 104b. In some embodiments, two or more electrochemical cells in the plurality of electrochemical cells are directly fluidically connected and / or in direct fluidic communication. For example, in FIG. 1B, first electrochemical cell 104a and second electrochemical cell 104b of system 100b are directly fluidically connected via first anodic chamber output stream 110e, which provides sorbent from #14498906v1 anodic chamber 120b of first electrochemical cell 104a to anodic chamber 122b of second electrochemical cell 104b. The multiplicity of electrochemical cells may comprise any suitable number of electrochemical cells. For example, the multiplicity of electrochemical cells may comprise two more electrochemical cells, three or more electrochemical cells, five our more electrochemical cells, ten or more electrochemical cells, twenty or more electrochemical cells, or more. In some embodiments in which the system comprises a multiplicity of desorption stages, the system also comprises a multiplicity of electrochemical cells, and the multiplicity of electrochemical cells may comprise the same number of electrochemical cells as the number of desorption stages in the plurality of desorption stages. In some embodiments in which the system comprises a multiplicity of absorption stages, the system also comprises a multiplicity of electrochemical cells, and the multiplicity of electrochemical cells may comprise the same number of electrochemical cells as the number of absorption stages in the plurality of absorption stages. In some embodiments in which the system comprises a multiplicity of absorption stages and a multiplicity of desorption stages, the system also comprises a plurality of electrochemical cells, and the multiplicity of electrochemical cells may comprise the same number of electrochemical cells as whichever is higher of the number of desorption stages in the multiplicity of desorption stages and the number of absorption stages in the multiplicity of absorption stages. A system may comprise a greater number of electrochemical cells than the number of absorption stages and / or desorption stages in the system. In some embodiments, one or more of an absorption stage, a desorption stage, and / or an electrochemical cell (e.g., a cathodic chamber thereof, an anodic chamber thereof) of a system described herein may be fluidically connected and / or in fluidic communication. The absorption stage, desorption stage, and / or electrochemical cell may be fluidically connected in any of a variety of suitable configurations. For example, in some embodiments, an absorption stage and / or a desorption stage is fluidically connected to an electrochemical cell. In some embodiments in which the system comprises a multiplicity of absorption stages and a multiplicity of electrochemical cells, each absorption stage in the multiplicity of absorption stages may be fluidically connected to an electrochemical cell in the multiplicity of electrochemical cells. In some embodiments in which the system comprises a multiplicity of desorption stages and a multiplicity of electrochemical cells, each desorption stage in the multiplicity of desorption stages is fluidically connected to an electrochemical cell in the multiplicity of electrochemical cells. In certain embodiments, an absorption stage may be #14498906v1 fluidically connected to a cathodic chamber of an electrochemical cell. In some embodiments, a desorption stage may be fluidically connected to an anodic chamber of an electrochemical cell. In some embodiments, the absorption stage, desorption stage, and / or electrochemical cell being fluidically connected facilitates the transfer of material such as a sorbent stream between and / or within the absorption stage, the desorption stage, and / or the electrochemical cell. In some embodiments, the transfer of materials between and / or within the absorption stage, the desorption stage, and / or the electrochemical cell may be facilitated by one or more additional components of the system. For example, the system may comprise one or more pumps. The one or more pumps may be pumps for moving CO2. In some embodiments, the system comprises a power supply valve for the one or more pumps. Such pumps may be used to move an input gas (e.g., a feed gas) comprising CO2 into and / or within an absorption stage. The absorption stage, desorption stage, and / or electrochemical cell may be placed in fluidic communication via one or more conduits. The conduits may comprise tubing. In some embodiments, the system comprises one or more valves configured to control the flow of material between and / or within the absorption stage, the desorption stage, and / or the electrochemical cell. The system may comprise one or more conveying devices (e.g., pumps) for conveying material (e.g., a sorbent stream, a gas stream) between and / or within the absorption stage, the desorption stage, and / or the electrochemical cell. In some embodiments, the fluidic connection between the absorption stage, desorption stage, and / or electrochemical cell may have a variety of advantages in addition to facilitating transfer of material. For example, in some embodiments, the absorption of CO2 by the sorbent in the absorption stage may be an exothermic process, thereby raising the temperature of the sorbent and / or the sorbent stream and / or requiring cooling of the sorbent stream. In some embodiments, the desorption of CO2 from the sorbent in the desorption stage may be an endothermic process, thereby lowering the temperature of the sorbent and / or the sorbent stream and / or requiring heating of the sorbent stream. It may be beneficial to be able to physically separate the thermal management of absorption stages and desorption stages due to their competing thermodynamics. In some embodiments, the differing energetic properties of absorption and desorption can be synergistic. For example, in some embodiments, the absorption stage and the desorption stage may each be in fluidic communication with an electrochemical cell, such as in system 100b of FIG. 1B, in which first absorption stage 102a is in fluidic communication with cathodic chamber 122a of second electrochemical cell 104b via first absorption stage input stream 110a and desorption stage 106 is in fluidic communication with cathodic chamber 122a of second electrochemical cell 104b via desorption stage output #14498906v1 stream 110f. In certain embodiments, the electrochemical cell may experience internal heat transfer between the cathodic chamber and the anodic chamber. This may advantageously facilitate heat management of the exothermic (e.g., absorption) and endothermic (e.g., desorption) processes performed in the system. Several non-limiting examples of configurations of systems comprising an absorption stage, a desorption stage, and / or an electrochemical cell are described below. System 100a in FIG. 1A comprises a multiplicity of absorption stages comprising first absorption stage 102a and second absorption stage 102b, a multiplicity of electrochemical cells comprising first electrochemical cell 104a and second electrochemical cell 104b, and desorption stage 106. In system 100a, first absorption stage 102a is configured to accept as inputs first absorption stage input stream 110a comprising a sorbent and second absorption stage output gas stream 180b comprising a CO2-containing gas. The sorbent of first absorption stage input stream 110a and the CO2 of second absorption stage output gas stream 180b may be contacted within first absorption stage 102a, thereby transferring CO2 from second absorption stage output gas stream 180b to first absorption stage input stream 110a (e.g., via the CO2reacting with a sorbent, such as an activated sorbent, contained within first absorption stage input stream 110a). First absorption stage 102a is configured to produce as outputs first absorption stage output stream 110b comprising a sorbent and output gas stream 180c comprising a gas. First absorption stage output stream 110b may have a higher total CO2loading than first absorption stage input stream 110a (e.g., due to the reaction of the sorbent within first absorption stage input stream 110a with CO2 within first absorption stage 102a). The output gas stream 180c may comprise carbon dioxide in an amount less than second absorption stage output gas stream 180b, or output gas stream 180c may contain no carbon dioxide (e.g., due to the reaction of the CO2 within second absorption stage output gas stream 180b with the sorbent contained within first absorption stage input stream 110a). First absorption stage 102a is fluidically connected to cathodic chamber 120a of first electrochemical cell 104a such that first absorption stage output stream 110b can be delivered to cathodic chamber 120a of first electrochemical cell 104a. In FIG. 1A, first electrochemical cell 104a of system 100a comprises cathodic chamber 120a and anodic chamber 120b separated by ion-permeable material 124. First electrochemical cell 104a may be configured to facilitate one or more chemical reactions involving a sorbent in each of cathodic chamber 120a and anodic chamber 120b. Cathodic chamber 120a of first electrochemical cell 104a is configured to accept, as an input, first absorption stage output stream 110b and to produce as an output second absorption stage input stream 110c comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within #14498906v1 cathodic chamber 120a of first electrochemical cell 104a involving the sorbent within first absorption stage output stream 110b. For example, the sorbent provided to cathodic chamber 120a via first absorption stage output stream 110b may be activated (e.g., reduced) in the cathodic chamber. In some such embodiments, second absorption stage input stream 110c comprises activated sorbent. Second absorption stage input stream 110c may have the same total CO2loading first absorption stage output stream 110b (e.g., CO2may not be absorbed by and / or released from first absorption stage output stream 110b within the cathodic chamber). Cathodic chamber 120a of first electrochemical cell 104a is fluidically connected to second absorption stage 102b via second absorption stage input stream 110c such that second absorption stage input stream 110c can be delivered to second absorption stage 102b. Second absorption stage 102b of system 100a is configured to accept as inputs second absorption stage input stream 110c and input gas stream 180a comprising a CO2-containing gas. The sorbent of second absorption stage input stream 110c and the CO2 of input gas stream 180a may be contacted within second absorption stage 102b, thereby transferring CO2 from input gas stream 180a to second absorption stage input stream 110c (e.g., via the CO2reacting with a sorbent, such as an activated sorbent, contained within second absorption stage input stream 110c). Second absorption stage 102b is configured to produce as outputs second absorption stage output stream 110d comprising a sorbent and second absorption stage output gas stream 180b comprising CO2. Second absorption stage output stream 110d may have a higher total CO2loading than second absorption stage input stream 110c (e.g., due to the reaction of the sorbent within second absorption stage input stream 110c with CO2 within second absorption stage 102b. Second absorption stage output gas stream 180b may comprise CO2in an amount less than input gas stream 180a. Second absorption stage 102b is fluidically connected to anodic chamber 120b of first electrochemical cell 104a via second absorption stage output stream 110d such that second absorption stage output stream 110d can be delivered to anodic chamber 120b of first electrochemical cell 104a. Second absorption stage 102b is fluidically connected to first absorption stage 102a such that second absorption stage output gas stream 180b may be provided to first absorption stage 102a as an input. In FIG. 1A, anodic chamber 120b of first electrochemical cell 104a is configured to accept as an input second absorption stage output stream 110d and to produce as an output first anodic chamber output stream 110e comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within anodic chamber 120b of first electrochemical cell 104a involving the sorbent within second absorption stage output stream 110d. For example, the sorbent provided to anodic chamber 120b via second absorption stage output stream 110d may #14498906v1 be deactivated (e.g., oxidized) in the anodic chamber. In some such embodiments, first anodic chamber output stream 110e comprises deactivated sorbent. In certain embodiments, some CO2may be released from the sorbent within anodic chamber 120b. In some such embodiments, said CO2 may be contained within (e.g., dissolved in) another component of the sorbent stream, such as a medium (e.g., a liquid such as a solvent), and the total CO2loading of the sorbent stream does not change. For example, first anodic chamber output stream 110e may have the same total CO2 loading as second absorption stage output stream 110d. Anodic chamber 120b of first electrochemical cell 104a is fluidically connected to desorption stage 106 via first anodic chamber output stream 110e such that first anodic chamber output stream 110e can be delivered to desorption stage 106. In FIG. 1A, desorption stage 106 of system 100a is configured to accept as an input first anodic chamber output stream 110e comprising a sorbent. In desorption stage 106, CO2may be released from first anodic chamber output stream 110e. Desorption stage 106 is configured to produce as outputs desorption stage output stream 110f comprising a sorbent and desorption stage output gas stream 112 comprising CO2(e.g., CO2gas). Desorption stage output stream 110f may have a lower total CO2loading than the sorbent of first anodic chamber output stream 110e. Desorption stage 106 is fluidically connected to cathodic chamber 122a of second electrochemical cell 104b via desorption stage output stream 110f such that desorption stage output stream 110f can be delivered to cathodic chamber 122a of second electrochemical cell 104b. Second electrochemical cell 104b of system 100a shown in FIG. 1A comprises cathodic chamber 122a and anodic chamber 122b separated by ion-permeable material 124. Second electrochemical cell 104b may be configured to facilitate one or more chemical reactions involving a sorbent in each of cathodic chamber 122a and anodic chamber 122b. Cathodic chamber 122a of second electrochemical cell 104b is configured to receive as an input desorption stage output stream 110f and produce as an output first absorption stage input stream 110a. In some embodiments, one or more chemical reactions may be performed within cathodic chamber 122a of second electrochemical cell 104b involving the sorbent within desorption stage output stream 110f. For example, the sorbent provided to cathodic chamber 122a via desorption stage output stream 110f may be activated (e.g., reduced) in the cathodic chamber. In some such embodiments, first absorption stage input stream 110a comprises activated sorbent. First absorption stage input stream 110a may have the same total CO2loading as desorption stage output stream 110f (e.g., CO2 may not be absorbed and / or released from desorption stage output stream 110f within cathodic chamber 122a). Cathodic chamber 122a of second electrochemical #14498906v1 cell 104b is fluidically connected to first absorption stage 102a via first absorption stage input stream 110a such that first absorption stage input stream 110a can be delivered to first absorption stage 102a. In FIG. 1A, anodic chamber 122b of system 100a is configured to accept as an input second anodic chamber input stream 170a comprising a sorbent and to produce as an output second anodic chamber output stream 170b comprising a sorbent. In some embodiments, the second anodic chamber input stream 170a is drawn from a different part of the system. For example, the second anodic chamber input stream may be drawn from a reservoir (e.g., a reservoir of a material comprising the sorbent and medium). In some embodiments, second anodic chamber input stream may comprise a desorption stage output stream produced as an output from a desorption stage located elsewhere within the system. In accordance with certain embodiments, the system is configured such that the overall charge balance within system 100a is preserved. One or more chemical reactions may be performed within anodic chamber 122b of second electrochemical cell 104b involving the sorbent within second anodic chamber input stream 170a. For example, the sorbent provided to anodic chamber 122b via second anodic chamber input stream 170a may be deactivated (e.g., oxidized) in the anodic chamber. In some such embodiments, second anodic chamber output stream 170b comprises deactivated sorbent. System 100b in FIG. 1B comprises a multiplicity of absorption stages comprising first absorption stage 102a and second absorption stage 102b, a multiplicity of electrochemical cells comprising first electrochemical cell 104a and second electrochemical cell 104b, and desorption stage 106. The configuration of system 100b shown in FIG. 1B is the same as the configuration of system 100a shown in FIG. 1A, with the exception of the routing of first anodic chamber output stream 110e and the inputs to anodic chamber 122b of second electrochemical cell 104b and desorption stage 106, as described in detail below. In system 100b shown in FIG. 1B, anodic chamber 122b of second electrochemical cell 104b is configured to accept as an input first anodic chamber output stream 110e and to produce as an output desorption stage input stream 110g comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within anodic chamber 122b of second electrochemical cell 104b involving the sorbent within first anodic chamber output stream 110e. For example, the sorbent provided to anodic chamber 122b via first anodic chamber output stream 110e may be deactivated (e.g., oxidized) in the anodic chamber. In some such embodiments, desorption stage input stream110g comprises deactivated sorbent. In certain embodiments, some CO2 may be released from the sorbent within anodic chamber 122b. In #14498906v1 some such embodiments, said CO2 may be contained within (e.g., dissolved in) another component of the sorbent stream, such as a medium (e.g., a liquid such as a solvent), and the total CO2 loading of the sorbent stream does not change. For example, first anodic chamber output stream 110e may have the same total CO2 loading as stage input stream 110g. Anodic chamber 122b of second electrochemical cell 104b is fluidically connected to desorption stage 106 via desorption stage input stream 110g such that desorption stage input stream 110g can be delivered to desorption stage 106. In FIG. 1B, desorption stage 106 of system 100b is configured to accept as an input desorption stage input stream 110g. In desorption stage 106, CO2may be released from desorption stage input stream 110g. Desorption stage 106 is configured to produce as outputs desorption stage output stream 110f comprising a sorbent and desorption stage output gas stream 112 comprising CO2(e.g., CO2gas). The sorbent of desorption stage output stream 110f may have a lower total CO2 loading than desorption stage input stream 110g. Desorption stage 106 is fluidically connected to cathodic chamber 122a of second electrochemical cell 104b via desorption stage output stream 110f such that desorption stage output stream 110f can be delivered to cathodic chamber 122a of second electrochemical cell 104b. System 100c in FIG. 1C comprises a multiplicity of absorption stages comprising first absorption stage 102a and second absorption stage 102b, a multiplicity of electrochemical cells comprising first electrochemical cell 104a and second electrochemical cell 104b, and desorption stage 106. The configuration of system 100c is the same as the configuration of system 100b shown in FIG. 1B, with the exception of the gas input and output streams of the absorption stages, as described in detail below. In FIG. 1C, first absorption stage 102a of system 100c is configured to accept as inputs first absorption stage input stream 110a comprising a sorbent and first absorption stage input gas stream 180d comprising a CO2-containing gas. The sorbent of first absorption stage input stream 110a and the CO2of first absorption stage input gas stream 180d may be contacted within first absorption stage 102a, thereby transferring CO2 from first absorption stage input gas stream 180d to first absorption stage input stream 110a (e.g., via the CO2 reacting with a sorbent, such as an activated sorbent, contained within first absorption stage input stream 110a). First absorption stage 102a is configured to produce as outputs first absorption stage output stream 110b comprising a sorbent and output gas stream 180c comprising a gas. The gas of output gas stream 180c may comprise carbon dioxide in an amount less than first absorption stage input gas stream 180d or may contain no carbon dioxide. First absorption stage output stream 110b may have a higher total CO2 loading than first absorption stage input stream 110a (e.g., due to the #14498906v1 reaction of the sorbent within first absorption stage input stream 110a with CO2 within first absorption stage 102a). First absorption stage 102a is fluidically connected to cathodic chamber 120a of first electrochemical cell 104a via first absorption stage output stream 110b such that first absorption stage output stream 110b can be delivered to cathodic chamber 120a of first electrochemical cell 104a. In FIG. 1C, second absorption stage 102b of system 100c is configured to accept as inputs second absorption stage input stream 110c comprising a sorbent and input gas stream 180a comprising a CO2-containing gas. The sorbent of second absorption stage input stream 110c and the CO2of input gas stream 180a may be contacted within second absorption stage 102b, thereby transferring CO2 from input gas stream 180a to second absorption stage input stream 110c (e.g., via the CO2 reacting with a sorbent, such as an activated sorbent, contained within second absorption stage input stream 110c). Second absorption stage 102b is configured to produce as outputs second absorption stage output stream 110d comprising a sorbent and second absorption stage output gas stream 180b comprising a gas. The sorbent of second absorption stage output stream 110d may have a higher total CO2loading than second absorption stage input stream 110c (e.g., due to the reaction of the sorbent within second absorption stage input stream 110c with CO2 within second absorption stage 102b). The gas of second absorption stage output gas stream 180b may comprise carbon dioxide in an amount less than input gas stream 180a or may contain no carbon dioxide. Second absorption stage 102b is fluidically connected to anodic chamber 120b of first electrochemical cell 104a via second absorption stage output stream 110d such that second absorption stage output stream 110d can be delivered to anodic chamber 120b of first electrochemical cell 104a. System 100d in FIG. 1D comprises absorption stage 102, a multiplicity of electrochemical cells comprising first electrochemical cell 104a and second electrochemical cell 104b, and a multiplicity of desorption stages comprising first desorption stage 106a and second desorption stage 106b. In system 100d, shown in FIG. 1D absorption stage 102 is configured to accept as inputs absorption stage input stream 130a comprising a sorbent and input gas stream 180a comprising a CO2-containing gas. The sorbent of absorption stage input stream 130a and the CO2of input gas stream 180a may be contacted within absorption stage 102. The sorbent of first absorption stage input stream 130a and the CO2 of input gas stream 180a may be contacted within absorption stage 102, thereby transferring CO2from input gas stream 180a to absorption stage input stream 130a (e.g., via the CO2 reacting with a sorbent, such as an activated sorbent, contained within absorption stage input stream 130a). Absorption stage 102 is configured to produce, as outputs, #14498906v1 absorption stage output stream 130b comprising a sorbent and output gas stream 180c comprising a gas. Absorption stage output stream 130b may have a higher total CO2loading than absorption stage input stream 130a (e.g., due to the reaction of the sorbent within absorption stage input stream 130a with CO2 within absorption stage 102), The gas of output gas stream 180c may comprise carbon dioxide (e.g., CO2gas) in an amount less than input gas stream 180a or may contain no carbon dioxide. Absorption stage 102 is fluidically connected to anodic chamber 120b of first electrochemical cell 104a via absorption stage output stream 130b such that absorption stage output stream 130b can be delivered to anodic chamber 120b of first electrochemical cell 104a. In FIG. 1D, first electrochemical cell 104a of system 100a comprises cathodic chamber 120a and anodic chamber 120b separated by ion-permeable material 124. First electrochemical cell 104a may be configured to facilitate one or more chemical reactions involving a sorbent in each of cathodic chamber 120a and anodic chamber 120b. Anodic chamber 120b of first electrochemical cell 104a is configured to accept, as an input, absorption stage output stream 130b and to produce as an output first desorption stage input stream 130c comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within anodic chamber 120b of first electrochemical cell 104a involving the sorbent within absorption stage output stream 130b. For example, the sorbent provided to anodic chamber 120b via absorption stage output stream 130b may be deactivated (e.g., oxidized) in the anodic chamber. In some such embodiments, first desorption stage input stream 130c comprises deactivated sorbent. In certain embodiments, some CO2 may be released from the sorbent within anodic chamber 120b. In some such embodiments, said CO2may be contained within (e.g., dissolved in) another component of the sorbent stream, such as a medium (e.g., a liquid such as a solvent), and the total CO2 loading of the sorbent stream does not change. For example, first desorption stage input stream 130c may have the same total CO2loading as the sorbent in absorption stage output stream 130b. Anodic chamber 120b of first electrochemical cell 104a is fluidically connected to first desorption stage 106a via first desorption stage input stream 130c such that first desorption stage input stream 130c can be delivered to first desorption stage 106a. In FIG. 1D, first desorption stage 106a of system 100d is configured to accept as an input first desorption stage input stream 130c. In first desorption stage 106a, CO2 may be released from first desorption stage input stream 130c. First desorption stage 106a is configured to produce as outputs first desorption stage output stream 130d comprising a sorbent and first desorption stage output gas stream 112a comprising CO2 (e.g., CO2 gas). First desorption stage output stream 130d may have a lower total CO2 loading than the sorbent of first desorption stage #14498906v1 input stream 130c. First desorption stage 106a is fluidically connected to anodic chamber 122b of second electrochemical cell 104b via first desorption stage output stream 130d such that first desorption stage output stream 130d can be delivered to anodic chamber 122b of second electrochemical cell 104b. In some instances, first desorption stage 106a may be fluidically connected to second desorption stage 106b such that first desorption stage output gas stream 112a is provided (e.g., as shown by gas output redirect stream 112c) to second desorption stage 106b as an input. In FIG. 1D, second electrochemical cell 104b of system 100d comprises cathodic chamber 122a and anodic chamber 122b separated by ion-permeable material 124. Second electrochemical cell 104b may be configured to facilitate one or more chemical reactions involving a sorbent in each of cathodic chamber 122a and anodic chamber 122b. Anodic chamber 122b of second electrochemical cell 104b is configured to accept as an input first desorption stage output stream 130d and to produce as an output second desorption stage input stream 130e comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within anodic chamber 122b of second electrochemical cell 104b involving the sorbent within first desorption stage output stream 130d. For example, the sorbent provided to anodic chamber 122b via first desorption stage output stream 130d may be deactivated (e.g., oxidized) in the anodic chamber. In some such embodiments, second desorption stage input stream 130e comprises deactivated sorbent. In certain embodiments, some CO2may be released from the sorbent within anodic chamber 120b. In some such embodiments, said CO2 may be contained within (e.g., dissolved in) another component of the sorbent stream, such as a medium (e.g., a liquid such as a solvent), and the total CO2loading of the sorbent stream does not change. For example, second desorption stage input stream 130e may have the same total CO2 loading as the sorbent in first desorption stage output stream 130d. Anodic chamber 122b of second electrochemical cell 104b is fluidically connected to second desorption stage 106b via second desorption stage input stream 130e such that second desorption stage input stream 130e can be delivered to second desorption stage 106b. In FIG. 1D, second desorption stage 106b of system 100d is configured to accept as an input second desorption stage input stream 130e. In second desorption stage 106b, CO2may be released from second desorption stage input stream 130e. Second desorption stage 106b is configured to produce as outputs second desorption stage output stream 130f comprising a sorbent and second desorption stage output gas stream 112b comprising CO2(e.g., CO2gas). Second desorption stage output stream 130f may have a lower total CO2 loading than second desorption stage input stream 130e. Second desorption stage 106b is fluidically connected to #14498906v1 cathodic chamber 122a of second electrochemical cell 104b via second desorption stage output stream 130f such that second desorption stage output stream 130f can be delivered to cathodic chamber 122a of second electrochemical cell 104b. In some instances, second desorption stage 106b may be configured to receive of first desorption stage output gas stream 112a (e.g. as shown by gas output redirect stream 112c) as an input. In FIG. 1D, cathodic chamber 122a of second electrochemical cell 104b is configured to accept as an input second desorption stage output stream 130f and to produce as an output second cathodic chamber output stream 130g comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within cathodic chamber 122a of second electrochemical cell 104b involving the sorbent within second desorption stage output stream 130f. For example, the sorbent provided to cathodic chamber 122a via second desorption stage output stream 130f may be activated (e.g., reduced) in the cathodic chamber. In some such embodiments, second cathodic chamber output stream 130g comprises activated sorbent. Second cathodic chamber output stream 130g may have the same total CO2 loading as second desorption stage output stream 130f (e.g., CO2may not be absorbed by and / or released from second desorption stage output stream 130f within the cathodic chamber). Cathodic chamber 122a of second electrochemical cell 104b is fluidically connected to cathodic chamber 120a of first electrochemical cell 104a via second cathodic chamber output stream 130g such that second cathodic chamber output stream 130g can be delivered to cathodic chamber 120a as an input. In system 100d shown in FIG. 1D, cathodic chamber 120a of first electrochemical cell 104a is configured to accept as an input second cathodic chamber output stream 130g comprising a sorbent and to produce as an output absorption stage input stream 130a comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within cathodic chamber 122a of second electrochemical cell 104b involving the sorbent within second cathodic chamber output stream 130g. For example, the sorbent provided to cathodic chamber 120a via second cathodic chamber output stream 130g may be activated (e.g., reduced) in the cathodic chamber. In some such embodiments, absorption stage input stream 130a comprises activated sorbent. Absorption stage input stream 130a may have the same total CO2 loading as second cathodic chamber output stream 130g (e.g., CO2may not be absorbed by and / or released from second cathodic chamber output stream 130g within the cathodic chamber). Cathodic chamber 120a of first electrochemical cell 104a is fluidically connected to absorption stage 102 via absorption stage input stream 130a such that absorption stage input stream 130a can be delivered to absorption stage 102. #14498906v1 System 100e in FIG. 1E comprises absorption stage 102, a multiplicity of electrochemical cells comprising first electrochemical cell 104a and second electrochemical cell 104b, and a multiplicity of desorption stages comprising first desorption stage 106a and second desorption stage 106b. The configuration of system 100e shown in FIG. 1E is the same as the configuration of system 100d shown in FIG. 1D, with the exception of the routing of second cathodic chamber output stream 130g and the inputs to cathodic chamber 120a of first electrochemical cell 104a, as described in detail below. In FIG. 1E, cathodic chamber 122a of second electrochemical cell 104b is configured to accept as an input second desorption stage output stream 130f and to produce as an output absorption stage input stream 130a comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within cathodic chamber 122a of second electrochemical cell 104b involving the sorbent within second desorption stage output stream 130f. For example, the sorbent provided to cathodic chamber 122a via second desorption stage output stream 130f may be activated (e.g., reduced) in the cathodic chamber. In some such embodiments, absorption stage input stream 130a comprises activated sorbent. Absorption stage input stream 130a may have the same total CO2loading as second desorption stage output stream 130f (e.g., CO2 may not be absorbed by and / or released from second desorption stage output stream 130f within the cathodic chamber). Cathodic chamber 122a of second electrochemical cell 104b is fluidically connected to absorption stage 102 via absorption stage input stream 130a such that absorption stage input stream 130a can be delivered to absorption stage 102 as an input. In FIG. 1E, cathodic chamber 120a of first electrochemical cell 104a of system 100e is configured to accept, as an input, first cathodic chamber input stream 160a comprising a sorbent and to produce as an output first cathodic chamber output stream 160b comprising a sorbent. In some embodiments, the first cathodic chamber input stream 160a may be drawn from a different part of the system. For example, the first cathodic chamber input stream may be drawn from a reservoir (e.g., a reservoir of a material comprising the sorbent and medium). In some embodiments, first cathodic chamber input stream may comprise an absorption stage output stream produced as an output from an absorption stage located elsewhere within the system. In accordance with certain embodiments, the system is configured such that the overall charge balance within system 100e is preserved. In some embodiments, one or more chemical reactions may be performed within cathodic chamber 120a of first electrochemical cell 104a involving the sorbent within first cathodic chamber input stream 160a. For example, the sorbent provided to cathodic chamber #14498906v1 120a via first cathodic chamber input stream 160a may be activated (e.g., reduced) in the cathodic chamber. In some such embodiments, first cathodic chamber output stream 160b comprises activated sorbent. As noted above, a system described herein may comprise any number of absorption stages, desorption stages, and / or electrochemical cells. System 100f in FIG. 1F comprises a multiplicity of absorption stages comprising first absorption stage 202a and second absorption stage 202b, a multiplicity of electrochemical cells comprising first electrochemical cell 204a and second electrochemical cell 204b, and a multiplicity of desorption stages comprising first desorption stage 206a and second desorption stage 206b. In system 100f shown in FIG. 1F, first absorption stage 202a is configured to accept as inputs first absorption stage input stream 210a comprising a sorbent and second absorption stage output gas stream 280b comprising a CO2-containing gas. The sorbent of first absorption stage input stream 210a and the CO2 of second absorption stage output gas stream 280b may be contacted within first absorption stage 202a, thereby transferring CO2 from second absorption stage output gas stream 280b to first absorption stage input stream 210a (e.g., via the CO2reacting with a sorbent, such as an activated sorbent, contained within first absorption stage input stream 210a). First absorption stage 202a is configured to produce as outputs first absorption stage output stream 210b comprising a sorbent and output gas stream 280c comprising a gas. First absorption stage output stream 210b may have a higher total CO2loading than first absorption stage input stream 210a (e.g., due to the reaction of the sorbent within first absorption stage input stream 210a with CO2 within first absorption stage 202a). Output gas stream 280c may comprise carbon dioxide in an amount less than second absorption stage output gas stream 280b or may contain no carbon dioxide. First absorption stage 202a is fluidically connected to cathodic chamber 220a of first electrochemical cell 204a via first absorption stage output stream 210b such that first absorption stage output stream 210b can be delivered to cathodic chamber 220a of first electrochemical cell 204a. In FIG. 1F, First electrochemical cell 204a of system 100f comprises cathodic chamber 220a and anodic chamber 220b separated by ion-permeable material 224. First electrochemical cell 204a may be configured to facilitate one or more chemical reactions involving a sorbent in each of cathodic chamber 220a and anodic chamber 220b. Cathodic chamber 220a of first electrochemical cell 204a is configured to accept as an input first absorption stage output stream 210b and to produce as an output second absorption stage input stream 210c comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within cathodic chamber 220a of first electrochemical cell 204a involving the sorbent within first #14498906v1 absorption stage output stream 210b. For example, the sorbent provided to cathodic chamber 120a via first absorption stage output stream 210b may be activated (e.g., reduced) in the cathodic chamber. In some such embodiments, second absorption stage input stream 210c comprises activated sorbent. Second absorption stage input stream 210c may have the same total CO2loading as first absorption stage output stream 210b (e.g., CO2may not be absorbed by and / or released from first absorption stage output stream 210b within the cathodic chamber). Cathodic chamber 220a of first electrochemical cell 204a is fluidically connected to second absorption stage 202b via second absorption stage input stream 210c such that second absorption stage input stream 210c can be delivered to second absorption stage 202b. Second absorption stage 202b of system 100f shown in FIG. 1F is configured to accept as inputs second absorption stage input stream 210c comprising a sorbent and input gas stream 280a comprising a CO2-containing gas. The sorbent of second absorption stage input stream 210c and the CO2 of input gas stream 280a may be contacted within second absorption stage 202b, thereby transferring CO2 from input gas stream 280a to second absorption stage input stream 210c (e.g., via the CO2 reacting with a sorbent, such as an activated sorbent, contained within second absorption stage input stream 210c). Second absorption stage 202b is configured to produce as outputs second absorption stage output stream 210d comprising a sorbent and second absorption stage output gas stream 280b comprising a gas. Second absorption stage output stream 210d may have a higher total CO2 loading than second absorption stage input stream 210c (e.g., due to the reaction of the sorbent within second absorption stage input stream 210c with CO2 within second absorption stage 202b). The gas of second absorption stage output gas stream 280b may comprise CO2 (e.g., CO2 gas) in an amount less than input gas stream 280a. Second absorption stage 202b is fluidically connected to anodic chamber 220b of first electrochemical cell 204a via second absorption stage output stream 210d such that second absorption stage output stream 210d can be delivered to anodic chamber 220b of first electrochemical cell 204a. Second absorption stage 202b is fluidically connected to first absorption stage 202a such that second absorption stage output gas stream 280b may be provided to first absorption stage 202a as an input. In FIG. 1F, anodic chamber 220b of first electrochemical cell 204a is configured to accept as an input second absorption stage output stream 210d and to produce as an output first desorption stage input stream 210e comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within anodic chamber 220b of first electrochemical cell 204a involving the sorbent within second absorption stage output stream 210d. For example, the sorbent provided to anodic chamber 220b via second absorption stage output stream 210d may #14498906v1 be deactivated (e.g., oxidized) in the anodic chamber. In some such embodiments, first desorption stage input stream 210e comprises deactivated sorbent. In certain embodiments, some CO2 may be released from the sorbent within anodic chamber 220b. In some such embodiments, said CO2 may be contained within (e.g., dissolved in) another component of the sorbent stream, such as a medium (e.g., a liquid such as a solvent), and the total CO2loading of the sorbent stream does not change. For example, first desorption stage input stream 210e may have the same total CO2 loading as second absorption stage output stream 210d. Anodic chamber 220b of first electrochemical cell 204a is fluidically connected to first desorption stage 206a via first desorption stage input stream 210e such that first desorption stage input stream 210e can be delivered to first desorption stage 206a as an input. In FIG. 1F, first desorption stage 206a of system 100f is configured to accept as an input first desorption stage input stream 210e. In first desorption stage 206a, CO2may be released from first desorption stage input stream 210e. First desorption stage 206a is configured to produce as outputs first desorption stage output stream 210i comprising a sorbent and first desorption stage output gas stream 212a comprising a gas comprising CO2(e.g., CO2gas). First desorption stage output stream 210i may have a lower total CO2loading than first desorption stage input stream 210e. First desorption stage 206a is fluidically connected to anodic chamber 222b of second electrochemical cell 204b via first desorption stage output stream 210i such that first desorption stage output stream 210i can be delivered to anodic chamber 222b of second electrochemical cell 204b. In some instances, first desorption stage 206a may be fluidically connected to second desorption stage 206b such that of first desorption stage output gas stream 212a (e.g. as shown by gas output redirect stream 212c) is provided to second desorption stage 206b as an input. Second electrochemical cell 204b of system 100f shown in FIG. 1F comprises cathodic chamber 222a and anodic chamber 222b separated by ion-permeable material 224. Second electrochemical cell 204b may be configured to facilitate one or more chemical reactions involving a sorbent in each of cathodic chamber 222a and anodic chamber 222b. Anodic chamber 222b of second electrochemical cell 204b is configured to accept as an input first desorption stage output stream 210i and to produce as an output second desorption stage input stream 210h comprising a sorbent. In some embodiments, one or more chemical reactions may be performed within anodic chamber 222b of second electrochemical cell 204b involving the sorbent within first desorption stage output stream 210i. For example, the sorbent provided to anodic chamber 222b via first desorption stage output stream 210i may be deactivated (e.g., oxidized) in the anodic chamber. In some such embodiments, second desorption stage input #14498906v1 stream 210h comprises deactivated sorbent. In certain embodiments, some CO2 may be released from the sorbent within anodic chamber 222b. In some such embodiments, said CO2may be contained within (e.g., dissolved in) another component of the sorbent stream, such as a medium (e.g., a liquid such as a solvent), and the total CO2 loading of the sorbent stream does not change. For example, second desorption stage input stream 210h may have the same total CO2loading as first desorption stage output stream 210i. Anodic chamber 222b of second electrochemical cell 204b is fluidically connected to second desorption stage 206b via second desorption stage input stream 210h such that second desorption stage input stream 210h can be delivered to second desorption stage 206b. In FIG. 1F, second desorption stage 206b of system 100f is configured to accept as an input second desorption stage input stream 210h. In second desorption stage 206b, CO2 may be released from second desorption stage input stream 210h. Second desorption stage 206b is configured to produce as outputs second desorption stage output stream 210f comprising a sorbent and second desorption stage output gas stream 212b comprising CO2 (e.g., CO2 gas). Second desorption stage output stream 210f may have a lower total CO2loading than second desorption stage input stream 210h. Second desorption stage 206b is fluidically connected to cathodic chamber 222a of second electrochemical cell 204b via second desorption stage output stream 210f such that second desorption stage output stream 210f can be delivered to cathodic chamber 222a of second electrochemical cell 204b. In some instances, second desorption stage 206b may be configured to receive first desorption stage output gas stream 212a (e.g. as shown by gas output redirect stream 212c) as an input. In FIG. 1F, cathodic chamber 222a of second electrochemical cell 204b is configured to accept as an input second desorption stage output stream 210f and to produce as an output first absorption stage input stream 210a. In some embodiments, one or more chemical reactions may be performed within cathodic chamber 222a of second electrochemical cell 204b involving the sorbent within second desorption stage output stream 210f. For example, the sorbent provided to cathodic chamber 222a via second desorption stage output stream 210f may be activated (e.g., reduced) in the cathodic chamber. In some such embodiments, first absorption stage input stream 210a comprises activated sorbent. First absorption stage input stream 210a may have the same total CO2 loading as second desorption stage output stream 210f (e.g., CO2 may not be absorbed and / or released from second desorption stage output stream 210f within cathodic chamber 222a). Cathodic chamber 222a of second electrochemical cell 204b is fluidically connected to first absorption stage 202a via first absorption stage input stream 210a such that #14498906v1 first absorption stage input stream 210a can be delivered to first absorption stage 202a as an input. In some embodiments, methods are provided. In some embodiments, the method comprises reacting a sorbent with carbon dioxide (CO2). The sorbent may be contained within a sorbent stream. In some embodiments, when the sorbent is reacted with carbon dioxide, the CO2loading of the sorbent stream may change. For example, the method may comprise reacting a sorbent within a sorbent stream having a first total CO2 loading with CO2 to form a sorbent stream having a second total CO2 loading that is greater than the first CO2 loading. In some embodiments, reacting the sorbent within the sorbent stream with carbon dioxide may be performed in an absorption stage, such as an absorption stage of a system described herein. In some embodiments, the method comprises releasing CO2 from a sorbent stream. In some embodiments, when CO2is released from the sorbent stream, the CO2loading of the sorbent stream may change. For example, the method may comprise releasing CO2 from a sorbent stream having a second total CO2 loading to form a sorbent stream having a third total CO2loading. In some embodiments, releasing CO2from the sorbent stream may be performed in a desorption stage, such as a desorption stage of a system described herein. The method may comprise performing one or more chemical reactions involving the sorbent (e.g., the sorbent contained within the sorbent stream). In some embodiments, the one or more chemical reactions comprise one or more electrochemical reactions. The electrochemical reaction may comprise reducing and / or oxidizing the sorbent, as described above. For example, the one or more chemical reactions may activate (e.g., by reducing) and / or deactivate (e.g., by oxidizing) the sorbent. Activating and / or deactivating the sorbent may not alter the CO2loading of the sorbent stream. For example, even in embodiments in which deactivating the sorbent causes CO2 to be released from the sorbent, the CO2 may be contained within (e.g., dissolved in) a component of the sorbent stream that is not the sorbent, such as a medium (e.g., a liquid such as a solvent). In some embodiments, one or more chemical reactions may be performed to activate the sorbent within a sorbent stream having first total CO2 loading without altering the CO2 loading of the sorbent stream. In some embodiments, one or more steps of the method comprise altering the total CO2loading of a sorbent stream, activating a sorbent within a sorbent stream, and / or deactivating a sorbent within a sorbent stream. For example, in some embodiments, a method described herein comprises, in an absorption stage, reacting carbon dioxide with a sorbent within a sorbent stream having a particular total CO2 loading to form a sorbent having a different total CO2 loading. The method may comprise, in a cathodic chamber of an electrochemical cell, performing one or more #14498906v1 chemical reactions involving to activate a sorbent within a sorbent stream having a particular CO2loading. In some embodiments, the method comprises, in an anodic chamber of an electrochemical cell, performing one or more chemical reactions to deactivate a sorbent having a particular total CO2 loading. The method may comprise, in a desorption stage, releasing CO2 from a sorbent stream having a particular state of charge and a particular CO2loading to form a sorbent stream having a different CO2loading. Several non-limiting examples of methods are described below. Any of the methods described herein may be performed in a system as described herein. For illustrative purposes, reference is made to such systems when describing the methods below. However, it should be understood that the methods described herein do not necessarily have to be performed using a system, and that these methods may be performed using systems other than those referred to below. In some embodiments, a method described herein comprises, in a first absorption stage, reacting CO2 with a sorbent within a sorbent stream a first total CO2 loading to form a sorbent having a second total CO2loading that is greater than the first CO2loading. For example, as shown in FIG. 1A, first absorption stage input stream 110a provided as an input to first absorption stage 102a may have a first total CO2 loading. In first absorption stage 102a, sorbent within first absorption stage input stream 110a may react with CO2 in second absorption stage output gas stream 180b provided to first absorption stage 102a as an input. This reaction may form a sorbent stream having the first state of charge and a second total CO2 loading, such as first absorption stage output stream 110b, provided by first absorption stage 102a as an output. In some embodiments, the method comprises, in a cathodic chamber of a first electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the second total CO2 loading. For example, as shown in FIG. 1A, first absorption stage output stream 110b having the second total CO2loading may be provided as an input to cathodic chamber 120a of first electrochemical cell 104a. One or more chemical reactions may be performed within first electrochemical cell 104a involving the sorbent within first absorption stage output stream 110b. Second absorption stage input stream 110c, provided by cathodic chamber 120a of first electrochemical cell 104a as an output, may comprise the activated sorbent and have the second total CO2 loading. The method may comprise, in a second absorption stage, reacting carbon dioxide with the sorbent within the sorbent stream having the second total CO2loading to form a sorbent stream having a third total CO2 loading that is higher than the second total CO2 loading. For example, as shown in FIG. 1A, second absorption stage input stream 110c, comprising the #14498906v1 activated sorbent and having the second total CO2 loading, is provided to second absorption stage 102b as an input. In second absorption stage 102b, sorbent within second absorption stage input stream 110c may react with CO2 present in input gas stream 180a, which is provided to second absorption stage 102b as an input. This reaction may form second absorption stage output stream 110d, provided by second absorption stage 102b as an output, having the third total CO2loading. In some embodiments, the method comprises, in an anodic chamber of the first electrochemical cell, performing one or more electrochemical reactions to deactivate the within the sorbent stream having the third total CO2. For example, in FIG. 1A, second absorption stage output stream 110d having the third total CO2 loading may be provided to anodic chamber 120b of first electrochemical cell 104a as an input. One or more chemical reactions may be performed within first electrochemical cell 104a to deactivate the sorbent contained within second absorption stage output stream 110d. First anodic chamber output stream 110e, provided by anodic chamber 120b of first electrochemical cell 104a as an output, may comprise the deactivated sorbent and have the third total CO2loading. In some embodiments, the method comprises, in a desorption stage, releasing carbon dioxide from the sorbent stream having the third total CO2 loading to form a sorbent stream having a fourth total CO2 loading, which is less than the third total CO2 loading and may optionally be equal to the first total CO2loading. For example, as shown in FIG. 1A, first anodic chamber output stream 110e comprising having the third total CO2 loading may be provided to desorption stage 106 as an input. In desorption stage 106, carbon dioxide may be released from first anodic chamber output stream 110e to form desorption stage output stream 110f having the fourth total CO2 loading. Desorption stage output stream 110f may be provided by desorption stage 106 as an output and provided to cathodic chamber 122a of second electrochemical cell 104b. In some embodiments, the method comprises, in a cathodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to activate the sorbent contained within sorbent stream having the fourth total CO2 loading. For example, in FIG. 1A, desorption stage output stream 110f comprising having the fourth total CO2loading may be provided to cathodic chamber 122a of second electrochemical cell 104b as an input. One or more chemical reactions may be performed within second electrochemical cell 104b to activate said sorbent. First absorption stage input stream 110a provided by cathodic chamber 122a of second electrochemical cell 104b as an output may comprise the activated sorbent and have the fourth total CO2 loading, and may be provided to first absorption stage 102a as an input. #14498906v1 In some embodiments, the method comprises, in an anodic chamber of the second electrochemical cell, performing one or more electrochemical reactions to deactivate the sorbent within the sorbent stream having the third total CO2. For example, in FIG. 1B, first anodic chamber output stream 110e comprising having the third total CO2 loading may be provided to anodic chamber 122b of second electrochemical cell 104b as an input. One or more chemical reactions may be performed within second electrochemical cell 104b to deactivate said sorbent, forming desorption stage input stream 110g comprising the deactivated sorbent and having the third total CO2 loading. Desorption stage input stream 110g may be produced by anodic chamber 122b of second electrochemical cell 104b as an output and provided to desorption stage 106. In some embodiments, the method comprises, in an anodic chamber of the second electrochemical cell, performing one or more electrochemical reactions deactivating the sorbent having the fourth total CO2 loading. For example, in FIG. 1F, first desorption stage output stream 210i comprising having the fourth total CO2 loading may be provided to anodic chamber 222b of second electrochemical cell 204b as an input. One or more chemical reactions may be performed within second electrochemical cell 204b to deactivate said sorbent, forming second desorption stage input stream 210h comprising the deactivated sorbent and having the fourth total CO2 loading. The second desorption stage input stream 210h may be provided by anodic chamber 222b of second electrochemical cell 204b as an output and provided to second desorption stage 206b as an input. In some embodiments, the method comprises, in a second desorption stage, releasing carbon dioxide from the sorbent stream having fourth total CO2loading to form a sorbent stream having a fifth total CO2 loading that is less than the fourth total CO2 loading and may optionally be equal to the first total CO2 loading. For example, as shown in FIG. 1F, second desorption stage input stream 210h having the fourth total CO2loading may be provided to second desorption stage 206b as an input. In second desorption stage 206b, carbon dioxide may be released from second desorption stage input stream 210h to form second desorption stage output stream 210f having the fifth total CO2 loading. Second desorption stage output stream 210f may be provided by second desorption stage 206b as an output and provided to cathodic chamber 222a of second electrochemical cell 204b as an input. In some embodiments, the method comprises, in a cathodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to activate the sorbent having fifth total CO2. For example, in FIG. 1F, second desorption stage output stream 210f comprising the sorbent having the fifth total CO2 loading may be provided to cathodic chamber #14498906v1 222a of second electrochemical cell 204b as an input. One or more chemical reactions may be performed within second electrochemical cell 204b to activate said sorbent, forming first absorption stage input stream 210a comprising the activated sorbent and having the fifth total CO2 loading. First absorption stage input stream 210a may be provided by cathodic chamber 222a of second electrochemical cell 204b as an output, may comprise the sorbent having the first state of charge and the first total CO2loading. In some embodiments, a method described herein comprises, in an absorption stage, reacting CO2 with the sorbent within a sorbent stream having a first total CO2 loading to form a sorbent stream having a second total CO2loading. For example, as shown in FIG. 1D, absorption stage input stream 130a provided as an input to absorption stage 102 may comprise the sorbent stream having the first total CO2 loading. In absorption stage 102, the sorbent contained within absorption stage input stream 130a may react with CO2in input gas stream 180a provided to absorption stage 102 as an input. This reaction may form absorption stage output stream 130b having the second total CO2 loading. Absorption stage output stream 130b may be provided by absorption stage 102 as an output and provided to anodic chamber 120b of first electrochemical cell 104a as an input. In some embodiments, the method comprises, in the anodic chamber of a first electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the second total CO2. For example, as shown in FIG. 1D, absorption stage output stream 130b having the second total CO2 loading may be provided as an input to anodic chamber 120b of first electrochemical cell 104a. One or more chemical reactions may be performed within first electrochemical cell 104a to deactivate sorbent within absorption stage output stream 130b, forming first desorption stage input stream 130c comprising the deactivated sorbent and having the second total CO2 loading. First desorption stage input stream 130c may provided by anodic chamber 120b of first electrochemical cell 104a as an output and to first desorption stage 106a as an input. In some embodiments, the method comprises, in a first desorption stage, releasing carbon dioxide from the sorbent stream having the second total CO2 loading to form a sorbent having a third total CO2loading. For example, as shown in FIG. 1D, first desorption stage input stream 130c having the second total CO2 loading may be provided to first desorption stage 106a as an input. In first desorption stage 106a, carbon dioxide may be released from first desorption stage input stream 130c to form first desorption stage output stream 130d comprising the deactivated sorbent and having the third total CO2 loading. First desorption stage output stream 130d may #14498906v1 be provided by first desorption stage 106a as an output and provided to anodic chamber 122b of second electrochemical cell 104b as an input. In some embodiments, the method comprises, in an anodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to deactivate the sorbent contained within a sorbent stream having the third total CO2loading. For example, in FIG. 1D, first desorption stage output stream 130d comprising having third total CO2loading may be provided to anodic chamber 122b of second electrochemical cell 104b as an input. One or more chemical reactions may be performed within second electrochemical cell 104b to activate the sorbent within first desorption stage output stream 130d, forming the second desorption stage input stream 130e comprising the deactivated sorbent and having the third total CO2 loading. Second desorption stage input stream 130e may be provided by anodic chamber 120b as an output and may be provided to second desorption stage 106b as an input. In some embodiments, the method comprises, in a second desorption stage, releasing carbon dioxide from the sorbent stream having the third total CO2 loading to form a sorbent having a fourth total CO2loading, which may optionally be equal to the first total CO2loading. For example, as shown in FIG. 1D, second desorption stage input stream 130e having the third total CO2 loading may be provided to second desorption stage 106b as an input. In second desorption stage 106b, carbon dioxide may be released from second desorption stage input stream 130e to form second desorption stage output stream 130f having the fourth total CO2loading. Second desorption stage output stream 130f may be provided by second desorption stage 106b as an output and provided to cathodic chamber 122a of second electrochemical cell 104b as an input. In some embodiments, the method comprises, in a cathodic chamber of the second electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the fourth total CO2loading. For example, in FIG. 1E, second desorption stage output stream 130f having the fourth total CO2loading may be provided to cathodic chamber 122a of second electrochemical cell 104b as an input. One or more chemical reactions may be performed within second electrochemical cell 104b to activate sorbent within second desorption stage output stream 130f, forming absorption stage input stream 130a comprising the activated sorbent and having the fourth total CO2 loading. Absorption stage input stream 130a may be provided by cathodic chamber 122a as an output and provided to absorption stage 102 as an input. As noted above, the systems and methods described herein may have higher efficiency than existing four-stage systems. This can be demonstrated by the reduced thermodynamic work #14498906v1 associated with these systems and methods relative to existing systems. For example, FIGS. 5A- 5B show the thermodynamic work associated with a multistage system with multiple intermediate absorption steps during sorbent activation or multiple intermediate desorption steps during sorbent deactivation, according to certain embodiments. The area enclosed by these cycles (and therefore the minimum work required) is appreciably smaller than that enclosed by the four-stage system in FIG. 3D; this is quantified for staged desorption as a function of the number of stages in FIG. 6A-6B, according to certain embodiments. As shown in FIG. 6B, the penalty associated with shifting from anodic desorption to sequential deactivation and desorption is increasingly offset as the number of desorption stages increases, in certain embodiments. In the limit of a system with infinitely many stages of both absorption and desorption, the work would be identical to that of an ideal two-stage system. In practice, diminishing returns indicate that beyond a certain finite number of stages, capital costs associated with hardware (such as flash tanks, absorber columns, pumps, and piping) would outweigh energetic enhancements. Calculations are less straightforward for multistage activation and absorption as the feed gas conditions can vary in co-flow or counterflow, but similar trends hold. Beyond thermodynamic enhancements, desorption in stages is particularly relevant as it facilitates practical enhancements in gas handling. In real cells, accumulation of CO2 during deactivation eventually leads to nucleation and growth of bubbles, which passivate the electrode surface and increase overpotentials. FIG. 7 indicates the maximum partial pressure in the anodic chamber as a function of the number of desorption stages, according to certain embodiments, which is directly related to the accumulation of bubbles and associated overpotentials. The following Example Embodiment Description describes systems and methods for carbon capture, in accordance with certain embodiments. This Example Embodiment Description is intended to illustrate certain embodiments of the present invention, but does not exemplify the full scope of the invention. Electrochemically mediated sorbent-based carbon capture systems have recently gained attention as an alternative to traditional thermally based separations. Realizations of such systems typically require a choice between thermodynamically favorable but practically challenging two-stage systems, which combine activation with capture and deactivation with release, or pragmatic but less energy-efficient stepwise four-stage processes decoupling these steps. In this Example Embodiment Description, a thermodynamic assessment of multistage systems is presented, and such systems are shown to combine the practicality of sequential unit operations with the thermodynamic favorability of concerted operations. A generalized #14498906v1 thermodynamic assessment shows these systems approach the thermodynamic minimum energy of separation in the limit of many stages for an arbitrary sorbent chemistry. Staged desorption is further shown to decrease dramatically the amount of gas in the cell during deactivation, potentially reducing bubble-driven inefficiencies. As atmospheric carbon dioxide (CO2) concentrations continue to increase beyond pre-industrial levels, there is a pressing urgency to develop economical, energy-efficient, and scalable carbon dioxide separation technologies, both to decarbonize industrial activities and to remediate legacy emissions. Traditional sorbent-based carbon dioxide capture systems are driven by using variations in temperature or pressure to swing CO2sorption capacity, enabling uptake from a mixed gas feed and release into a pure CO2outlet stream. Electrochemically mediated carbon capture (EMCC) systems have recently gained attention as electrically driven alternatives to these traditional thermally based separations. EMCC systems employ applied electrical potentials to swing sorbent capacity, potentially enabling more favorable energetics, integration with renewable energy sources, and more modular, flexible scaling. A broad array of different chemistries and system designs have been proposed. Aqueous EMCC systems often leverage water dissociation to uptake CO2in alkaline conditions and to release it under neutral or acidic conditions. These pH variations can be driven by electrolytic cation exchange, bipolar membrane electrodialysis, or by electrochemical looping of gaseous H2 or O2. Another family of EMCC technologies leverages dissolved redox-active species to drive CO2uptake and release, either directly through CO2binding at an activated site or semi-directly through alkalinity modulation in protic media. The most widely studied examples are those of quinone compounds, which upon electrochemical reduction can either form a CO2-adduct or act as a proton acceptor depending on molecular properties and the solvent employed. Closely related are ‘indirect’ chemistries where CO2- binding sorbents are modulated by redox-active blocking species. The most developed implementation of such a system is electrochemically mediated amine regeneration by copper ion modulation, where carbamates will decompose to release CO2upon Cu2+complexation. This work concerns system designs for the latter cases of redox-active sorbents and blockers in solution. Systems employing redox-active sorbents and blockers operate through a series of electrochemical (activation / deactivation) and gas exchange (absorption / desorption) processes. The most straightforward embodiment is a four-stage system with each process carried out sequentially, employing a two-compartment electrochemical cell for electrochemical modulation and conventional absorption columns and flash tanks to facilitate gas exchange. Energetic savings are possible by combining activation with absorption or deactivation with desorption to #14498906v1 consume products as they form, binding CO2 to activated free sorbent in the cathodic chamber or removing free CO2from the anodic chamber. Such concerted systems have been demonstrated at the laboratory scale through the use of gas diffusion electrodes and in-cell hollow fibers. Initial results suggest that in many cases the projected thermodynamic enhancements achievable through concerted operations can be overshadowed by losses due to transport overpotentials and back diffusion of CO2, and the scalability of such systems is uncertain due to kinetic limitations. This motivates the development of multistage EMCC systems, which are shown in this Example Embodiment Description to achieve some of the energetic savings of concerted systems without sacrificing the flexibility and scalability of sequential systems. In this Example Embodiment Description, thermodynamic assessments of four-stage systems are described, and then these frameworks are extended to analyze multistage systems employing multiple discrete gas exchange and electrochemical steps. A high-level discussion of practical benefits and drawbacks of multistage systems is also provided. For a given electrochemically modulated sorbent (denoted “Q”) with m active sites each requiring one electron to be modulated, a corresponding EMCC system will operate through four primary reactions: i. Electrochemical: Sorbent activation (Q + me- → Qm-) ii. Gas Exchange: CO2 absorption (CO2,g →CO2,sol ; Q- + mCO2,sol → Q- mCO2) iii. Electrochemical: Sorbent deactivation (Q-mCO2→ Q + mCO2,aq+ me-) iv. Gas Exchange: CO2 release (CO2,sol → CO2,g) Unbound CO2in the system can either be gaseous (CO2,g) or dissolved in solvent (CO2,sol), and up to m CO2molecules can be bound to the activated sorbent (Q-mCO2). These reactions can be performed individually as sequential unit operations, or with concerted electrochemical and gas exchange steps (i.e., concurrent activation / absorption or deactivation / desorption). Combining these unit operations into a cyclic separation system yields a process with 4, 3, and 2 stages, respectively, as depicted in FIGS. 8A-8H. FIGS. 8A-8H show depictions of previously proposed systems and their corresponding thermodynamic cycles. On all plots, the curved dotted lines denote potentials for constant CO2loadings over all speciations (CO2,g, CO2,sol, and Q-mCO2) and the horizontal lines denote CO2 isobars. FIG. 8A is a depiction of a 4-stage EMCC system configuration with discrete, sequential #14498906v1 activation, absorption, deactivation, and desorption. FIG. 8B shows corresponding thermodynamic cycle for a 4-state system in FIG. 8A with 50% state of charge swing. FIG.8C) is a depiction of 3-stage system with concurrent activation and absorption followed by sequential deactivation and desorption. FIG. 8D shows corresponding thermodynamic cycle for a 3-stage system in FIG. 8C with cathodic absorption. FIG 8E is a depiction of 3-stage system with sequential activation and absorption followed by concurrent deactivation and desorption. FIG.8F shows corresponding thermodynamic cycle for a 3-stage system with anodic desorption shown in FIG. 8E. FIG. 8G is a depiction of 2-stage system featuring both concurrent activation and absorption and concurrent deactivation and desorption FIG. 8H shows a corresponding thermodynamic cycle for a system with cathodic absorption and anodic desorption shown inFIG. 8G. Cycles are evaluated using nominal values from the literature: T=323K, ^^^^ = 500,^^^,^^^=0.05, m=1, and ^^^^^,^^^^= 0.15 for all; ^^^^^,^^^ = 0.075 for the cases with cathodicabsorption. States 1 / 2 / 3a correspond to the positions during reduction / absorption and oxidation / desorption where the sorbent is sufficiently activated / deactivated to initiate gas exchange, and would be physically located within the electrochemical cell. The minimum process work for a given chemistry and system configuration can be modelled using previously developed frameworks. An arbitrary dormant sorbent, Q, is considered at atmospheric pressure P0,with m active sites, total concentration Q0, bindingconstant ^ and Henry’s constant ^ ^ ,^^^^^^^^ ^^,^^^ = ^!^ which is exposed to a CO2 partial pressure ^^ = ^^^^^^^ . Deviation from the reference potential can be expressed as:The normalized CO2 (2 = )34!^^ = )670!^^) by the following expression: The thermodynamic state of the system can be captured on an "#^$ − 2 diagram such as thatshown in FIG. 8B, which shows curved lines of constant CO2concentration accounting for all speciations, and horizontal lines capturing the actual partial pressure of the CO2within the solution. Three simple thermodynamic pathways exist for the different operations: 1. Follow constant 0^^^(alter the state of charge in a closed system) 2. Exchange gas (vertical line between CO2isobars) #14498906v1 3. Follow constant ^^^^(alter the state of charge while exchanging gas with a reservoir, along a horizontal CO2isobar) In the case of cathodic absorption, both 0^^^and ^^^^vary with the state of charge, so an additional mass balance equation is required to track the partial pressure at a state (xi, Pi) as CO2 is absorbed from ^^^^^,^^^^down to ^^^^^,^^^in counterflow: The equivalent mass balance equation for co-flow can be found in the literature; thermodynamically, the requisite minimum process work is identical for co-flow and counterflow cathodic absorption configurations, but the sorbent working capacity is higher in the counterflow case presented here. To evaluate minimum process energetics neglecting finite electrode overpotentials, cycle diagrams can be constructed from these pathways relating state of charge variation to excess thermodynamic potentials as a closed cycle analogous to a heat engine. Numerically, the work can be calculated as: Here, E denotes Faraday’s constant. Cycles of two, three, and four stage configurations are shown in FIG. 8B, FIG. 8D, FIG. 8F, and FIG. 8H. It can be observed visually that the work of separation can be reduced through combined electrochemical and gas exchange unit operations, as the shaded region shrinks as the number of stages decreases. For the example, parameters roughly corresponding to capture from 15% CO2flue gas with an amine solution, the minimum process works are 18, 10.1, 13.8, and 5.9 kJ / mol CO2for 4-stage, 3-stage with cathodic absorption, 3-stage with anodic desorption, and 2 stage systems respectively. The thermodynamic minimum work of concentrating CO2to 1 bar for a given ^^^^^,^^^^and ^^^^^,^^^can be calculated as: For the chosen parameters, Wmin=5.9 kJ / mol, corresponding precisely to the 2-stage work shaded in Fig. 8F as the processes 1a→2 and 2a→1 are both thermodynamically reversible. In the 2- stage case, state paths 1a→2 and 2a→1 are thermodynamically reversible, whereas 1→1a and 2→2a are thermodynamically irreversible; the irreversibility of processes 1→1a and 2→2a are the source of this minimum process work requirement. #14498906v1 Thermodynamics of Multistage EMCC Systems To reduce the thermodynamic penalty associated with decoupling electrochemical and gas exchange reactions, these processes can be divided into multiple stages, as shown in FIGS. 9A-9D. FIGS. 9A-9D depict process diagrams and thermodynamic cycles for proposed multistage CO2 separation systems with the minimum process work represented by the area enclosed. Sorbent properties are identical to those assumed in FIGS. 8A-8H. FIG. 9A is a depiction of an EMCC system configuration with activation and absorption split over two stages, followed by discrete deactivation and desorption. FIG. 9B shows corresponding thermodynamic cycle diagram for sequential system with staged absorption shown in FIG. 9A, with the original 4-stage process overlaid as a dotted line. FIG. 9C is a depiction of an EMCC system configuration with sequential activation and absorption followed by deactivation and desorption split over two discrete stages. FIG. 9D shows a corresponding thermodynamic cycle diagram for sequential system with staged desorption shown in FIG. 9C, with the original 4-stage process overlaid as a dotted line. Parameters in b and d are identical to those used in FIGS. 8A-8H. Staged absorption can be achieved in multiple ways: a counterflowing gas feed stream and liquid stream can be intermittently contacted, as shown in FIGS. 9A-9B and FIGS. 10A- 10B, or a feed gas stream can be divided over multiple absorption columns with varying sorbent states of charge, as in FIGS. 10C-10D. In the case of split feed gas streams, process energetics are agnostic to the effluent pressure; as in 4-stage systems, counterflowing sorbent will equilibrate to the inlet feed gas partial pressure, and the capture fraction is primarily a consideration for absorber column sizing and associated capital expenses. The latter case of a single gas stream with intermittent activation and absorption requires mass balances across the stages, as in the case of cathodic absorption. By contrast, implementing staged desorption is straightforward, as accumulated gaseous CO2in the anode is simply flashed down to a fixed outlet pressure periodically during deactivation, as shown in FIGS 2C-2D. Both staged absorption and desorption are shown to reduce the process work, with savings graphically indicated by the unshaded areas between the work curves and the dotted line denoting a 4-stage process. In this Example Embodiment Description, the four-stage work (18 kJ / mol) is reduced to 16.3 kJ / mol by an additional absorption stage, or to 16.7 kJ / mol by an additional desorption stage. Further insights can be drawn by extrapolating to the limiting case of many stages, depicted in FIGS. 10A-10F. #14498906v1 FIGS. 10A-10F depict multistage EMCC systems in the limit of many stages. FIG. 10A is a depiction of an EMCC system configuration with activation and absorption split over many counterflowing stages in series, followed by sequential deactivation and desorption. FIG. 10B shows a thermodynamic cycle diagram for sequential system with 10 absorption stages shown in FIG. 10A, with the original 4-stage process overlaid as a dotted line. FIG. 10C is a depiction of an EMCC system configuration with activation and absorption split over many stages with feed gas piped into each in parallel, followed by sequential deactivation and desorption. FIG. 10D shows a thermodynamic cycle diagram for sequential system with 10 absorption stages from parallelized feed gas shown in FIG. 10C, with the original 4-stage process overlaid as a dotted line. FIG. 10E is a depiction of an EMCC system configuration with sequential activation and absorption followed by deactivation and desorption split over many stages. FIG. 10F shows a corresponding thermodynamic cycle diagram for sequential system with desorption split over 10 stages shown in FIG. 10E, with the original 4-stage process overlaid as a dotted line. Parameters in b / d / f are identical to those used in FIGS. 8A-8H. In the limit of many feed gas contacting stages in series, the activation / absorption process begins to resemble that of cathodic absorption, depicted in FIGS. 10A-10B. In this limit, the alternative staged absorption system configuration where feed gas is parallelized into each absorber column begins to diverge, instead approaching absorption at constant CO2 partial pressure (FIGS. 10C-10D). As progressively more desorption stages are introduced, the curves for discretized deactivation / desorption begin to approach the anodic desorption limit, shown in FIGS. 10E-10F. It is important to note that while staged systems can lower the thermodynamic penalty of decoupling electrochemical and gas exchange reactions, these processes are fundamentally different from concerted pathways as they are thermodynamically irreversible. This is observed in FIG. 11A below, as the asymptotic energy consumption of staged absorption (FIGS. 10A-10B) or staged desorption (FIGS. 10E-10F) approaches but does not fully reach that of a concerted process. FIGS. 11A-11D show performance metrics as a function of the number of sequential gas exchange stages, calculated by iteratively generating and evaluating process cycle diagrams in the manner depicted in FIG. 10B, FIG. 10D, and FIG. 10F. FIG. 11A shows the process work of staged absorption in series or in parallel with anodic desorption, benchmarked against 3-stage work, ideal work for 50% capture, and work of capture from an infinite reservoir. FIG. 11B shows the maximum achievable CO2capture as a function of the number of parallel absorption stages. FIG. 11C shows the reduction in work penalty associated with discrete operations relative to concerted operations. Here, absorption is assumed to occur with feed gas piped in #14498906v1 series, as it approaches the 2-stage limit. FIG. 11D shows the maximum anodic CO2 partial pressure as a function of the number of desorption stages. Parameters are identical to those in the previous figures. FIG. 11A shows the work of processes with anodic desorption and varying absorption schemes - a standard 3-stage configuration, 50% capture via many stages with gas piped in series, many stages with gas piped in parallel, and 2-stage cathodic absorption. In the limit of many stages, process work for series fed multistage absorption asymptotically approaches the thermodynamic minimum work of separation, equal to that of a 2-stage system. In contrast, the process work of staged absorbers fed in parallel approaches that of capture from an inexhaustible reservoir of CO2: In the parallel fed case, the achievable capture fraction decreases with increasing stage count, as seen in FIG. 11B. While this effect is relatively insignificant in most applications for low numbers of stages, there is a meaningful drop-off at higher stage numbers. Thermodynamically, the process work of staged absorption from feed gas distributed in parallel is favorable compared to that of series absorption so long as the desired capture fraction is achievable. FIG. 11C compares the discrete operation penalty offsets achievable with staged absorption (in series) and staged desorption, denoted as P: For a given number of gas exchange steps, multistage desorption provides a greater relative thermodynamic enhancement, but their performances converge for more dilute ^^^^^,^^^^. Regardless of parameters, both processes asymptotically approach the work of a concerted process in the limit of many stages. Sensitivity studies of these metrics for variations in process and sorbent parameters are beyond the scope of this work, but the broad trends illustrated in FIGS. 11A-11D hold for most combinations of parameters yielding a physically achievable separation (T, ^^^^, ^^^,^^^, ^^^^^,^^^^, ^^^^^,^^^). Practical Considerations Beyond thermodynamics, significant practical benefits can be offered by staged processes, with staged desorption in particular alleviating challenges in gas handling. Gas- induced inefficiencies can be significant in electrochemical cells, as bubbles substantially limit achievable current densities by blocking active area and increasing ohmic losses. Specific to EMCC systems, the stoichiometric ratios inherent to sorbents dictate that gas volumes generated #14498906v1 per unit of circulating electrolyte volume are often significantly higher than those in more conventional chlor-alkali or water electrolysis cells. FIG. 11D implies that splitting desorption over multiple stages can significantly reduce the volume of gas buildup in the electrochemical cell. Benefits of implementation at scale are ultimately determined by a tradeoff between increased capital costs of gas exchange equipment and enhancements in cell performance enabling smaller stacks and / or improved energetics. Technoeconomic assessments suggest that staged desorption in particular could be beneficial in this regard. These assessments have projected that flash tanks would make up less than 1% of the total capital expenses of equipping a power plant with an EMAR carbon capture system, so costs of additional stages would mainly be embodied in additional pumps (totaling 9% of the retrofit CAPEX). Technoeconomic tradeoffs associated with varying absorption schemes are more challenging to evaluate at a high level, as absorber towers are highly sensitive to kinetics and transport, and the total system cost is much more sensitive to changes due to the higher associated CAPEX values. The absorption column CAPEX is likely to increase with a staged configuration, as the driving force for absorption is reduced. A rate-based model analogous to that used for intercooled thermal amine absorption towers would be needed to quantify the tradeoff. Technoeconomic analyses have projected that absorbers and blowers make up 9% and 5% of the retrofit CAPEX, respectively, and additional pumps would also be required. In either case, it is likely that only a few additional stages would be desirable before enhancements in cell performance are outweighed by increases in gas handling capital expenses. In this Example Embodiment Description, multistage absorption / desorption schemes are presented as a means to reduce the thermodynamic penalties associated with decoupling electrochemical reactions from gas exchange processes in electrochemically mediated carbon capture systems. Extending existing frameworks, the thermodynamic energy savings achievable through multistage gas exchange schemes are quantified, indicating that the decoupling penalties can be meaningfully offset. Beyond thermodynamic considerations, staged desorption is suggested as a promising means of reducing bubble-driven inefficiencies in systems at scale. It should be understood that the subject matter defined in the appended claims is not necessarily limited to the specific implementations described above. The specific implementations described above are disclosed as examples only. 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 #14498906v1 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, and / or method described herein. In addition, any combination of two or more such features, systems, articles, materials, and / or methods, if such features, systems, articles, materials, and / or methods are not mutually inconsistent, is included within the scope of the present invention. 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. 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 unless clearly indicated to the contrary. 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 without B (optionally including elements other than B); in another embodiment, to B without A (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 #14498906v1 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); 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. As used herein, “wt%” is an abbreviation of weight percentage. As used herein, “at%” is an abbreviation of atomic percentage. Some embodiments may be embodied as a method, of which various examples have been described. The acts performed as part of the methods may be ordered in any suitable way. Accordingly, embodiments may be constructed in which acts are performed in an order different than illustrated, which may include different (e.g., more or less) acts than those that are described, and / or that may involve performing some acts simultaneously, even though the acts are shown as being performed sequentially in the embodiments specifically described above. Use of ordinal terms such as “first,” “second,” “third,” etc., in the claims to modify a claim element does not by itself connote any priority, precedence, or order of one claim element over another or the temporal order in which acts of a method are performed, but are used merely as labels to distinguish one claim element having a certain name from another element having a same name (but for use of the ordinal term) to distinguish the claim elements. When a portion (e.g., a layer, a structure, a region) is “on”, “adjacent”, “above”, “over”, “overlying”, or “supported by” another portion, it can be directly on the portion, or an intervening portion (e.g., layer, structure, region) may also be present. Similarly, when a portion is “below” or “underneath” another portion, it can be directly below the portion, or an #14498906v1 intervening portion (e.g., layer, structure, region) may also be present. A portion that is “directly adjacent”, “directly on”, “immediately adjacent”, “in contact with”, or “directly supported by” another portion means that no intervening portion is present. It should also be understood that when a portion is referred to as being “on”, “above”, “adjacent”, “over”, “overlying”, “in contact with”, “below”, or “supported by” another portion, it may cover the entire portion or a part of the portion. In the claims, as well as in the specification above, all transitional phrases such as “comprising,” “including,” “carrying,” “having,” “containing,” “involving,” “holding,” 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. #14498906v1

Claims

CLAIMS What is claimed is:

1. A system for capturing carbon dioxide, comprising: an absorption stage comprising a sorbent; a multiplicity of desorption stages; and a multiplicity of electrochemical cells, wherein: each desorption stage in the multiplicity of desorption stages is fluidically connected to at least one of the electrochemical cells in the multiplicity of electrochemical cells; and at least one electrochemical cell in the multiplicity of electrochemical cells is fluidically connected to the absorption stage.

2. A system for capturing carbon dioxide, comprising: a multiplicity of absorption stages comprising a sorbent; a desorption stage; and a multiplicity of electrochemical cells, wherein: each absorption stage in the multiplicity of absorption stages is fluidically connected to at least one of the electrochemical cells in the multiplicity of electrochemical cells; and at least one electrochemical cell in the multiplicity of electrochemical cells is fluidically connected to the desorption stage.

3. The system of claim 2, wherein the desorption stage is part of a multiplicity of desorption stages, and wherein each desorption stage in the multiplicity of desorption stages is fluidically connected to at least one of the electrochemical cells in the multiplicity of electrochemical cells.

4. The system of any one of claims 1-3, wherein each of the electrochemical cells in the multiplicity of electrochemical cells comprises an anode, a cathode, and an ion- permeable material. #14498906v15. The system of claim 4, wherein the ion-permeable material comprises a selective ion-permeable membrane and / or a non-selective ion-permeable membrane.

6. The system of any one of claims 1-5, wherein each absorption stage is fluidically connected to a cathode of at least one of the electrochemical cells in the multiplicity of electrochemical cells.

7. The system of any one of claims 1-6, wherein each desorption stage is fluidically connected to an anode of at least one of the electrochemical cells in the multiplicity of the electrochemical cells.

8. The system of any one of claims 1-7, wherein the desorption stage or one or more desorption stages in the multiplicity of desorption stages comprises a flash tank.

9. The system of any one of claims 2-8, wherein two or more absorption stages in the multiplicity of absorption stages are in gaseous communication.

10. The system of claim 9, wherein the two or more absorption stages are not in gaseous communication.

11. The system of any one of claims 1-10, wherein one or more of the absorption stages are configured to receive a carbon dioxide-containing gas stream.

12. The system of any one of claims 1-11, wherein one or more of the absorption stages comprise counterflow absorbers.

13. The system of any one of claims 1-12, wherein the sorbent comprises a protic medium and / or an aprotic medium. #14498906v114. The system of any one of claims 1-13, wherein one or more electrochemical cells within the multiplicity of electrochemical cells is configured to facilitate a liquid-solid electrochemical reaction.

15. The system of any one of claims 1-14, wherein one or more electrochemical cells within the multiplicity of electrochemical cells is configured to facilitate a gas-liquid electrochemical reaction.

16. The system of any one of claims 1-15, wherein one or more electrochemical cells within the multiplicity of electrochemical cells is configured to facilitate a liquid-liquid electrochemical reaction.

17. A method, comprising: in a first absorption stage, reacting carbon dioxide with a sorbent within a sorbent stream having a first total CO2loading to form a sorbent stream having a second total CO2 loading that is greater than the first total CO2 loading; in a cathodic chamber of a first electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the second total CO2 loading; in a second absorption stage, reacting carbon dioxide with the sorbent within the sorbent stream having the second total CO2loading to form a sorbent stream having a third total CO2 loading that is greater than the second total CO2 loading; in an anodic chamber of the first electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the third total CO2loading; in a desorption stage, releasing carbon dioxide from the sorbent stream having the third total CO2 loading to form a sorbent stream having a fourth total CO2 loading that is less than the third total CO2loading and that may optionally be equal to the first total CO2 loading; and in a cathodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the fourth total CO2 loading. #14498906v118. A method, comprising: in a first absorption stage, reacting carbon dioxide with a sorbent within a sorbent stream having a first total CO2loading to form a sorbent stream having a second total CO2loading that is greater than the first total CO2loading; in a cathodic chamber of a first electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the second total CO2loading; in a second absorption stage, reacting carbon dioxide with the sorbent within the sorbent stream having the second total CO2 loading to form a sorbent stream having a third total CO2loading that is greater than the second total CO2loading; in an anodic chamber of the first electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the third total CO2loading; in an anodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the third total CO2 loading; in a desorption stage, releasing carbon dioxide from the sorbent stream having the third total CO2 loading to form a sorbent stream having a fourth total CO2 loading that is less than the third total CO2 loading and that may optionally be equal to the first total CO2loading; and in a cathodic chamber of the second electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the fourth total CO2loading.

19. A method, comprising: in a first absorption stage, reacting carbon dioxide with a sorbent within a sorbent stream having a first total CO2loading to form a sorbent stream having a second total CO2 loading that is greater than the first total CO2 loading; in a cathodic chamber of a first electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the second total CO2 loading; #14498906v1in a second absorption stage, reacting carbon dioxide with sorbent within the sorbent stream having the second total CO2 loading to form a sorbent stream having a third total CO2 loading that is greater than the second total CO2 loading; in an anodic chamber of the first electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the third total CO2 loading; in a first desorption stage, releasing carbon dioxide from the sorbent stream having the third total CO2loading to form a sorbent stream having a fourth total CO2loading that is less than the third total CO2 loading; in an anodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the fourth total CO2 loading; in a second desorption stage, releasing carbon dioxide from the sorbent stream having the fourth total CO2loading to form a sorbent stream having a fifth total CO2loading that is less than the fourth total CO2loading and that may optionally be equal to the first total CO2 loading; and in a cathodic chamber of the second electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the fifth total CO2 loading.

20. A method, comprising: in an absorption stage, reacting carbon dioxide with a sorbent within a sorbent stream having a first total CO2 loading to form a sorbent stream having a second total CO2loading that is greater than the first total CO2loading; in an anodic chamber of a first electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the second total CO2 loading; in a first desorption stage, releasing CO2from the sorbent stream having the second total CO2 loading to form a sorbent stream having a third total CO2 loading that is less than the second total CO2 loading; #14498906v1in an anodic chamber of a second electrochemical cell, performing one or more electrochemical reactions to deactivate sorbent within the sorbent stream having the third total CO2 loading; in a second desorption stage, releasing CO2from the sorbent stream having the third total CO2loading to form a sorbent stream having a fourth total CO2loading that is less than the third total CO2 loading and may optionally be equal to the first total CO2 loading; and in a cathodic chamber of the second electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the fourth total CO2 loading.

21. The method of claim 20, further comprising, in a cathodic chamber of the first electrochemical cell, performing one or more electrochemical reactions to activate sorbent within the sorbent stream having the fourth total CO2loading.

22. A system and / or method for separating (capturing) CO2 comprising: a. one or more pumps for moving CO2; b. a power supply for the one or more pumps; c. tubing and a valve; d. a feed gas comprising CO2; e. an absorber that captures CO2; f. a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2absorption in stages, followed by sequential deactivation and desorption; wherein activation and absorption are concurrent or sequential; g. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and h. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell.

23. The system of claim 22, wherein sequential activation and absorption followed by electrochemical deactivation and CO2 desorption occurs in four or more stages. #14498906v124. A system and / or method for separating (capturing) CO2 comprising: a. one or more pumps for moving CO2; b. a power supply for the one or more pumps; c. tubing and a valve; d. a feed gas comprising CO2; e. an absorber that captures CO2; f. a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in stages; wherein activation and absorption are concurrent or sequential; g. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and h. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell.

25. The system of claim 24, wherein sequential activation and absorption followed by electrochemical deactivation and CO2desorption in stages occurs in four or more stages.

26. A system and / or method for separating (capturing) CO2comprising: a. one or more pumps for moving CO2; b. a power supply for the one or more pumps; c. tubing and a valve; d. a feed gas comprising CO2; e. an absorber that captures CO2; f. a multiplicity of electrochemical cells, wherein i. one or more electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2 absorption in stages, followed by sequential deactivation and desorption in stages; and #14498906v1ii. one or more electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in stages , g. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and h. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell.

27. The system of any one of claims 22-26, wherein the feed gas comprises air, flue gas, or an aqueous medium comprising CO2.

28. The system of any one of claims 22-27, wherein the electrochemical cells comprise an electrochemical sorbent.

29. A system for separating CO2comprising: a. an absorber that captures CO2; b. a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2 absorption in stages, followed by sequential deactivation and desorption; wherein activation and absorption are concurrent or sequential; c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell.

30. The system of claim 29, wherein sequential activation and absorption followed by electrochemical deactivation and CO2 desorption occurs in four or more stages.

31. A system for separating CO2 comprising: a. an absorber that captures CO2; b. a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes sequential activation and #14498906v1absorption followed by electrochemical deactivation and CO2desorption in stages; wherein activation and absorption are concurrent or sequential; c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell.

32. The system of claim 31, wherein sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in stages occurs in four or more stages.

33. A system for separating CO2 comprising: a. an absorber that captures CO2; b. a multiplicity of electrochemical cells, wherein i. one or more electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2 absorption in stages, followed by sequential deactivation and desorption in stages; and ii. one or more electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in stages , c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell.

34. The system of any one of claims 29-33, further comprising a feed gas comprising air, flue gas, or an aqueous medium comprising CO2.

35. The system of any one of claims 29-34, wherein the electrochemical cells comprise an electrochemical sorbent.

36. A method for separating CO2 comprising: #14498906v1a. providing a feed gas comprising CO2to an absorber that captures CO2; b. providing the absorbed CO2 to a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2absorption in stages, followed by sequential deactivation and desorption; wherein activation and absorption are concurrent or sequential; c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell.

37. The method of claim 36, wherein sequential activation and absorption followed by electrochemical deactivation and CO2 desorption occurs in four or more stages.

38. A method for separating CO2comprising: a. providing a feed gas comprising CO2 to an absorber that captures CO2; b. providing the absorbed CO2 to a multiplicity of electrochemical cells, wherein each electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2 desorption in stages; wherein activation and absorption are concurrent or sequential; c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell.

39. The method of claim 38, wherein sequential activation and absorption followed by electrochemical deactivation and CO2desorption in stages occurs in four or more stages.

40. A method for separating CO2comprising: a. providing a feed gas comprising CO2 to an absorber that captures CO2; #14498906v1b. providing the absorbed CO2to a multiplicity of electrochemical cells, wherein i. one or more electrochemical cell upon exposure to an electrical potential undergoes electrochemical activation and CO2absorption in stages, followed by sequential deactivation and desorption in stages; and ii. one or more electrochemical cell upon exposure to an electrical potential undergoes sequential activation and absorption followed by electrochemical deactivation and CO2desorption in stages, c. a cathode and an anode for controlling electrochemical potential of the electrochemical cells; and d. a power supply for creating an electrical current between an anode and a cathode of the electrochemical cell.

41. The method of any one of claims 36-40, further comprising a feed gas comprising air, flue gas, or an aqueous medium comprising CO2.

42. The method of any one of claims 36-41, wherein the electrochemical cells comprise an electrochemical sorbent. #14498906v1

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