Gas-liquid contactor for capturing carbon dioxide

Abstract

A system for removing carbon dioxide from a gas includes: an injector; a CO2 lean gas outlet, the CO2 lean gas outlet being fluidly coupled to the injector; a fan, the fan being fluidly coupled to the CO2 lean gas outlet, the fan being rotatable to discharge CO2 lean gas from the CO2 lean gas outlet; and a capture solution tank. The ejector includes: a capture solution inlet operable to receive a lean capture solution; a gas inlet operable to receive a gas comprising carbon dioxide; a mixing zone configured to react the lean capture solution and a gas comprising carbon dioxide; and an ejector outlet operable to discharge a mixed fluid comprising the rich capture solution and a CO2 lean gas. The capture solution tank is fluidly coupled to the ejector outlet and to the CO2 lean gas outlet, and the capture solution tank is configured to collect the rich capture solution.

Description

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS

[0002] This application claims priority to U.S. Provisional Patent Application No. 63 / 342,864, filed on May 17, 2022, the entire contents of which are incorporated herein by reference. Technical Field

[0003] The present disclosure describes systems, apparatus and methods for gas-liquid contacting for recovering carbon dioxide from a gas. Background Art

[0004] Capturing carbon dioxide (CO2) from the atmosphere is a solution to reduce greenhouse gas emissions and mitigate climate change. However, many technologies designed to capture CO2 from point sources (such as flue gases from industrial facilities) are generally ineffective in capturing CO2 from the atmosphere due to the significantly lower CO2 concentrations and the large amount of air required for processing. In recent years, progress has been made in finding technologies that are more suitable for capturing CO2 directly from the atmosphere. Some of these direct air capture (DAC) systems use solid adsorbents in which the active agent is attached to a substrate. These DAC systems typically use a cyclic adsorption-desorption process in which, after the solid adsorbent is saturated with CO2, it releases CO2 using humidity or thermal fluctuations and is regenerated. Although solid adsorbent DAC systems have high cycle yields, large-scale deployment has become a challenge due to the maintenance requirements inherent in batch processing.

[0005] Other DAC systems use liquid adsorbents (sometimes referred to as solvents) to capture CO2 from the atmosphere. An example of such a gas-liquid contact system is a system that uses a blower to draw air through a high surface area filler wetted with a solution containing a liquid adsorbent. CO2 in the air reacts with the liquid adsorbent. The rich solution is further processed downstream to regenerate the lean solution and release a concentrated CO2 stream. Such DAC systems may be advantageous because they use some commercially available equipment and they can operate more efficiently in certain environments than in other environments. It is desirable that DAC systems are easy to maintain and flexible in operation. Summary of the invention

[0006] In an exemplary embodiment, a system for removing carbon dioxide from a gas includes: an ejector; a lean CO2 gas outlet, the lean CO2 gas outlet fluidly coupled to the ejector; a blower, the blower fluidly coupled to the lean CO2 gas outlet, the blower rotatable to discharge the lean CO2 gas from the lean CO2 gas outlet; and a capture solution tank. The ejector includes: a capture solution inlet, the capture solution inlet operable to receive a lean capture solution; a gas inlet, the gas inlet operable to receive a gas including carbon dioxide; a mixing zone, the mixing zone configured to react the lean capture solution and the gas including carbon dioxide; and an ejector outlet, the ejector outlet operable to discharge a mixed fluid including a rich capture solution and a lean CO2 gas. The capture solution tank is fluidly coupled to the ejector outlet and to the lean CO2 gas outlet, and the capture solution tank is configured to collect the rich capture solution.

[0007] In aspects that may be combined with example embodiments, the system includes a regeneration system fluidly coupled to the capture solution tank.

[0008] In another aspect that may be combined with any of the preceding aspects, the system includes a capture solution distribution line fluidly coupled to the capture solution inlet of the ejector and fluidly coupled to the regeneration system.

[0009] In another aspect that may be combined with any of the preceding aspects, the capture solution tank is fluidly coupled to the regeneration system via a capture solution circulation pump.

[0010] In another aspect that may be combined with any of the preceding aspects, the regeneration system comprises at least one of a lime causticizing system or a calciner.

[0011] In another aspect that may be combined with any of the preceding aspects, the lime causticizing system comprises at least one of a pellet reactor or a slaker.

[0012] In another aspect which may be combined with any of the preceding aspects, the calciner comprises an electric calciner.

[0013] In another aspect which may be combined with any of the preceding aspects, the regeneration system has a product conduit configured to provide carbon dioxide as the product gas.

[0014] In another aspect that may be combined with any of the preceding aspects, the system includes a demister fluidly coupled to the CO 2 lean gas outlet.

[0015] In another aspect that may be combined with any of the preceding aspects, the demister comprises a chevron-shaped demister.

[0016] In another aspect which may be combined with any of the preceding aspects, the demister is positioned upstream of the fan.

[0017] In another aspect that may be combined with any of the preceding aspects, the system includes a mixing chamber fluidly coupled to the ejector outlet.

[0018] In another aspect which may be combined with any of the preceding aspects, the mixing chamber comprises a static mixer.

[0019] In another aspect that may be combined with any of the preceding aspects, the mixing chamber includes a coating of rate increasing material.

[0020] In another aspect which may be combined with any of the preceding aspects, the mixing chamber is positioned vertically between the ejector outlet and the capture solution tank.

[0021] In another aspect that may be combined with any of the preceding aspects, the system includes a packed bed absorber column fluidly coupled to the CO 2 lean gas outlet.

[0022] In another aspect which may be combined with any of the preceding aspects, the packed bed absorber column is positioned upstream of the blower.

[0023] In another aspect that may be combined with any of the preceding aspects, the packed bed absorption column comprises structured packing.

[0024] In another aspect that may be combined with any of the preceding aspects, the packed bed absorber column comprises a coating of rate enhancing material.

[0025] In another aspect that may be combined with any of the preceding aspects, the system includes a packed bed absorption column and a demister, wherein the demister, the packed bed absorption column, the fan and the CO2-lean gas outlet are vertically and sequentially spaced as follows from the lowest position to the highest position: the packed bed absorption column, the demister, the fan and the CO2-lean gas outlet.

[0026] In another aspect that may be combined with any of the preceding aspects, the system includes a coating of rate enhancing material on at least one of the ejector, the capture solution tank, or a wetted surface.

[0027] In another aspect which may be combined with any of the preceding aspects, the ejector is operable to flow a lean capture solution comprising a rate-enhancing additive.

[0028] In another aspect that may be combined with any of the preceding aspects, the rate enhancing additive comprises at least one of piperazine, carbonic anhydrase, or monoethanolamine.

[0029] In another aspect that may be combined with any of the preceding aspects, the system includes an auxiliary unit or an intermediate system fluidly coupled to the capture solution tank.

[0030] In another aspect combinable with any of the preceding aspects, the ejector defines an ejector axis parallel to an axis extending between the capture solution inlet and the ejector outlet, and the blower is rotatable about a blower axis parallel to the ejector axis.

[0031] In another aspect which may be combined with any of the preceding aspects, the ejector axis and the blower axis are horizontally spaced apart.

[0032] In another aspect that may be combined with any of the preceding aspects, the capture solution tank is positioned below the ejector and the blower.

[0033] In another exemplary embodiment, a system for removing carbon dioxide from a gas includes: a plurality of ejectors; at least one lean CO2 gas outlet, the at least one lean CO2 gas outlet fluidly coupled to at least one ejector of the plurality of ejectors; at least one blower, the at least one blower fluidly coupled to the at least one lean CO2 gas outlet, the at least one blower rotatable to discharge the lean CO2 gas from the at least one lean CO2 gas outlet; a capture solution tank; and a capture solution distribution line. Each ejector of the plurality of ejectors includes: a capture solution inlet operable to receive a lean capture solution; a gas inlet operable to receive a gas comprising carbon dioxide; a mixing zone configured to react the lean capture solution and the gas comprising carbon dioxide; and an ejector outlet operable to discharge a mixed fluid comprising a rich capture solution and a lean CO2 gas. The capture solution tank is fluidly coupled to the ejector outlet of each ejector of the plurality of ejectors and to the at least one lean CO2 gas outlet, and the capture solution tank is configured to collect the rich capture solution. The capture solution distribution line is fluidly coupled to a capture solution inlet of each of the plurality of injectors.

[0034] In aspects that may be combined with example embodiments, the system includes a regeneration system fluidly coupled to the capture solution tank and the capture solution distribution line.

[0035] In another aspect that may be combined with any of the preceding aspects, the capture solution tank is fluidly coupled to the regeneration system via a capture solution circulation pump.

[0036] In another aspect that may be combined with any of the preceding aspects, the regeneration system comprises at least one of a lime causticizing system or a calciner.

[0037] In another aspect that may be combined with any of the preceding aspects, the lime causticizing system comprises at least one of a pellet reactor or a lime slaker.

[0038] In another aspect which may be combined with any of the preceding aspects, the calciner comprises an electric calciner.

[0039] In another aspect which may be combined with any of the preceding aspects, the regeneration system has a product conduit configured to provide a product of the regeneration system.

[0040] In another aspect which may be combined with any of the preceding aspects, the plurality of ejectors are positioned on a perimeter of the capture solution tank.

[0041] In another aspect which may be combined with any of the preceding aspects, the at least one CO 2 lean gas outlet is fluidly coupled to each injector outlet of the plurality of injectors.

[0042] In another aspect which may be combined with any of the preceding aspects, the plurality of injectors are arranged circumferentially along a periphery around the at least one CO 2 lean gas outlet.

[0043] In another aspect which may be combined with any of the preceding aspects, the plurality of injectors are arranged in a plurality of rows of injectors.

[0044] In another aspect which may be combined with any of the preceding aspects, the plurality of ejectors are fluidly coupled to the at least one CO 2 lean gas outlet.

[0045] In another aspect that may be combined with any of the preceding aspects, the plurality of injectors includes six injectors.

[0046] In another aspect which may be combined with any of the preceding aspects, the at least one CO 2 lean gas outlet comprises six CO 2 lean gas outlets, each of the six CO 2 lean gas outlets being fluidly coupled to a respective one of the six ejectors.

[0047] In another aspect that may be combined with any of the preceding aspects, the system includes at least one demister fluidly coupled to the at least one CO 2 lean gas outlet.

[0048] In another aspect that may be combined with any of the preceding aspects, the at least one demister comprises a chevron-shaped demister.

[0049] In another aspect which may be combined with any of the preceding aspects, the at least one demister is positioned upstream of the at least one fan.

[0050] In another aspect that may be combined with any of the preceding aspects, the system includes at least one mixing chamber fluidly coupled to an injector outlet of at least one injector of the plurality of injectors.

[0051] In another aspect which may be combined with any of the preceding aspects, the at least one mixing chamber comprises a static mixer.

[0052] In another aspect that may be combined with any of the preceding aspects, the system includes at least one packed bed absorber column fluidly coupled to the at least one CO 2 lean gas outlet.

[0053] In another aspect which may be combined with any of the preceding aspects, the at least one packed bed absorber column is positioned upstream of the at least one blower.

[0054] In another aspect which may be combined with any of the preceding aspects, the at least one packed bed absorber column comprises structured packing.

[0055] In another aspect that may be combined with any of the preceding aspects, the system includes a coating of rate enhancing material on at least one of the plurality of ejectors, the capture solution tank, or a wetted surface.

[0056] In another aspect which may be combined with any of the preceding aspects, the plurality of ejectors are operable to flow a lean capture solution including a rate-enhancing additive.

[0057] In another aspect that may be combined with any of the preceding aspects, the rate enhancing additive comprises at least one of piperazine, carbonic anhydrase, or monoethanolamine.

[0058] In another aspect that may be combined with any of the preceding aspects, the system includes an auxiliary unit or an intermediate system fluidly coupled to the capture solution tank.

[0059] In another aspect which may be combined with any of the preceding aspects, the at least one CO 2 lean gas outlet is positioned to direct the CO 2 lean gas away from a gas inlet of each of the plurality of injectors.

[0060] In another exemplary embodiment, a method for removing carbon dioxide from a gas includes: flowing a lean capture solution into a capture solution inlet of an ejector to draw the gas into the gas inlet of the ejector according to a venturi effect; reacting the gas with the lean capture solution to form a mixed fluid including a rich capture solution and a CO2-lean gas; flowing the mixed fluid to a capture solution tank to collect the rich capture solution; and discharging the CO2-lean gas of the mixed fluid.

[0061] In aspects that may be combined with example embodiments, the method includes regenerating a first portion of the rich capture solution to form a regenerated capture solution.

[0062] In another aspect that may be combined with any of the preceding aspects, the method further comprises combining a second portion of the rich capture solution with the regenerated capture solution to form the lean capture solution.

[0063] In another aspect that may be combined with any of the preceding aspects, the method comprises: mixing at least a portion of the regenerated capture solution and the CO2-lean gas in an absorption column to capture carbon dioxide from the CO2-lean gas and form a rich regenerated capture solution and a CO2-lean absorber gas; and discharging the CO2-lean absorber gas.

[0064] In another aspect which may be combined with any of the preceding aspects, the method comprises reducing mist from the lean CO 2 absorber gas prior to discharging the lean CO 2 absorber gas.

[0065] In another aspect that may be combined with any of the preceding aspects, regenerating the first portion of the rich captured solution comprises flowing the first portion of the rich captured solution to at least one of a lime causticizing system, a pellet reactor, a lime slaker, or a calciner.

[0066] In another aspect that may be combined with any of the preceding aspects, regenerating the first portion of the rich capture solution includes flowing the first portion of the rich capture solution to an auxiliary unit or to an intermediate system.

[0067] In another aspect that may be combined with any of the preceding aspects, regenerating the first portion of the rich capture solution includes forming the regenerated capture solution and a concentrated carbon stream.

[0068] In another aspect that may be combined with any of the preceding aspects, the method comprises: releasing a CO2-rich gas stream from the concentrated carbon stream; and compressing the CO2-rich gas stream to form a product stream.

[0069] In another aspect that may be combined with any of the preceding aspects, the lean capture solution comprises a KOH molar concentration ranging from 1 molar to 6 molar.

[0070] In another aspect that may be combined with any of the preceding aspects, the method includes flowing a make-up capture solution into the capture solution tank.

[0071] In another aspect that may be combined with any of the preceding aspects, the compensation capture solution comprises a KOH concentration ranging from 0.1 wt % to 50 wt %.

[0072] In another aspect that may be combined with any of the preceding aspects, the method includes flowing a make-up water flow into the capture solution tank.

[0073] In another aspect that may be combined with any of the preceding aspects, the lean capture solution comprises at least one of an amine, potassium hydroxide, sodium hydroxide, potassium carbonate, bicarbonate, sodium carbonate, or water.

[0074] In another aspect that may be combined with any of the preceding aspects, the lean capture solution comprises a NaOH molarity ranging from 1 molar to 6 molar.

[0075] In another aspect which may be combined with any of the preceding aspects, the method includes reducing mist from the CO 2 lean gas prior to discharging the CO 2 lean gas.

[0076] In another aspect that may be combined with any of the preceding aspects, the method comprises mixing at least one of the lean capture solution and the rich capture solution with the CO 2 lean gas in a packed bed absorption column to capture carbon dioxide from the CO 2 lean gas.

[0077] In another aspect which may be combined with any of the preceding aspects, the method comprises flowing the gas through a pre-treatment unit before drawing the gas into the gas inlet of the ejector.

[0078] In another aspect that may be combined with any of the preceding aspects, the method includes flowing a rate increasing additive through the injector.

[0079] In another aspect that may be combined with any of the preceding aspects, the rate enhancing additive comprises at least one of piperazine, carbonic anhydrase, or monoethanolamine.

[0080] In another aspect that may be combined with any of the preceding aspects, flowing the rate increasing additive comprises flowing the rate increasing additive into the capture solution tank.

[0081] In another aspect that may be combined with any of the preceding aspects, flowing the rate-enhancing additive comprises: combining the rate-enhancing additive with the lean capture solution.

[0082] In another aspect that may be combined with any of the preceding aspects, flowing the lean capture solution into the capture solution inlet of the ejector to draw the gas into the gas inlet of the ejector comprises flowing the lean capture solution vertically downward and drawing the gas into the gas inlet in a horizontal direction. BRIEF DESCRIPTION OF THE DRAWINGS

[0083] Figure 1 is a cross-sectional view of an exemplary gas liquid contactor unit.

[0084] Figure 2 is a cross-sectional view of an exemplary supplemental gas liquid contactor unit.

[0085] Figure 3 is a plan view of an exemplary linear gas liquid contactor system.

[0086] Figure 4 is an isometric view of an exemplary perimeter gas liquid contactor system.

[0087] Figure 5 is an isometric view of an exemplary multi-row gas liquid contactor system.

[0088] Figure 6 is a block flow diagram illustrating an exemplary integrated gas capture system including a gas liquid contactor system fluidly coupled to a regeneration system.

[0089] Figure 7 is a flow chart illustrating an exemplary method for removing CO 2 from a gas.

[0090] Figure 8 is a schematic diagram of an exemplary control system for a gas liquid contactor system. DETAILED DESCRIPTION

[0091] The present disclosure describes a gas liquid contactor system in which an ejector (also known as an ejector venturi scrubber) is used in conjunction with a blower to effectively remove carbon dioxide (CO2) from a gas stream.

[0092] Ejector systems (also known as ejector venturi scrubbers) can be a useful type of gas-liquid contact system for applications where evaporative water loss is a concern, such as in arid climates, hot climates, or cold environments where low temperatures may cause the liquid sorbent to freeze. Such gas-liquid contactor systems can be used as an alternative to gas-liquid contactor systems based on cooling tower or gas scrubber designs. The use of an ejector system can have certain advantages, such as safer operation, smaller footprint, and simple maintenance.

[0093] The ejector draws gas in through the gas inlet using a lean capture solution (such as a KOH / K2CO3 solution) as the motive liquid. In some aspects of the present disclosure, "lean" can mean that the capture solution has not yet absorbed the target gas species, or that the concentration of the target gas species in the capture solution is lower than the concentration of the target gas species in the capture solution after the capture solution is exposed to the target gas species. The lean capture solution is pumped through the contraction section or throat of the ejector. As the fluid velocity increases, the contraction causes the fluid pressure to decrease. Due to the Bernoulli effect, this creates a partial vacuum on the gas inlet of the ejector that draws in the gas. The high-pressure fluid passing through the throat forms a large number of fine droplets that provide turbulent mixing of the lean capture solution and the gas. This initial mixing zone is where the lean capture solution first reacts with impurities in the gas. For example, a capture solution containing KOH will react with CO2 in the gas as follows:

[0094] CO 2(g) +2KOH (aq) →K2CO 3(aq) +H2O(k)(Eq.1)

[0095] The capture solution used in processes such as DAC and point source CO2 capture can employ capture agents other than KOH. The capture solution is selected for its performance and ability to capture at least a portion of CO2 when in contact with a gas containing CO2. For some applications, a capture solution comprising an alkaline solution is suitable, such as an aqueous solution comprising one or more of KOH (as shown in Eq. 1), NaOH, K2CO3, Na2CO3, NaHCO3, and KHCO3. For some applications, a capture solution comprising an amine-based solvent or additive is suitable, such as an aqueous solution comprising one or more of monoethanolamine (MEA) and diethanolamine (DEA). Another example of a capture solution comprising an amine-based solvent is isophorone diamine (IPDA), which can form carbamic acid when in contact with CO2 from the air. Another example of a capture solution includes an amine salt.

[0096] At least a portion of the CO2 is removed from the gas according to the above reaction (Eq. 1) or according to another reaction involving a different capture agent to produce a CO2-lean gas and a rich capture solution. In some cases, the CO2-lean gas may not be completely free of CO2, but may have less CO2 than the inlet gas. The CO2-lean gas can be discharged by a fan positioned at the CO2-lean gas outlet. The fan is used to change the ratio of capture solution to gas by controlling the gas velocity at the gas inlet of the ejector. The fan can also reduce the energy required for the motive fluid to draw the gas into the ejector because the fan can be a more efficient device for moving gas than a separate ejector. In some cases, it may also be advantageous to flow the CO2-lean gas through other components (such as a demister or dehumidifier or an absorption column) before discharging it from the system. In some cases, a portion of the rich capture solution can be sent to a regeneration system. Another portion of the rich capture solution can be circulated and combined with a fresh or regenerated capture solution to form a lean capture solution.

[0097] Throughout this disclosure, the terms "ejector venturi scrubber," "venturi flow device," and "eductor" are used interchangeably to describe components of a gas-liquid contactor system that employs the Venturi effect to draw gas into an eductor assembly using a motive liquid. The eductor may also include a spray nozzle that directs the motive liquid toward a converging section of the eductor.

[0098] Each of the configurations described herein may include unillustrated intermediate processing steps or units. At least one intermediate unit may be present between the gas-liquid contactor system and the regeneration system. For example, the capture solution may be flowed to a storage tank before flowing to the regeneration system. In another example, the filtration system may be between the gas-liquid contactor system and the regeneration system. It may be beneficial to use a rate-enhancing additive in the gas-liquid contactor system to increase the transfer rate of CO2 from gas to aqueous solution. The rate-enhancing additive may include a catalyst, a promoter, a solvent, or other types of additives. Examples of rate-enhancing additives may include, for example, carbonic anhydrase, piperazine, MEA, DEA, triazacyclic zinc, tetraazacyclic zinc, copper glycinate, hydroxypentamine cobalt perchlorate, formaldehyde hydrate, sucrose, fructose, glucose, phenols, phenolates, glycerol, arsenite, vanadium pentoxide, hypochlorite, hypobromite, or other oxygen-containing anion substances. In some embodiments, the filtration system can retain at least a portion of the rate-enhancing additive within the gas-liquid contactor system to prevent the rate-enhancing additive from being denatured or degraded in the regeneration system due to heat, pressure, shear, stress, or other process conditions that cause degradation of the promoter. In addition, some auxiliary equipment and units or intermediate systems (e.g., tanks, filters, conveyors, mixing tanks, separators, pumps) can be used as part of the overall process. These auxiliary units can form intermediate systems and / or facilitate intermediate processing steps between the gas-liquid contactor system and the regeneration system.

[0099] Each of the configurations described herein can be fluidly coupled to at least one other gas-liquid air contactor unit or gas-liquid air contactor system to form a modular system, such as a grid or a network. The modular system enables large amounts of CO2 to be captured from one or more sources. For example, a network may include multiple gas-liquid contactor systems coupled to one or more central processing facilities, which include at least one regeneration facility or a series of processing systems. The regeneration facility can be composed of multiple regeneration series, each series including a complete set of equipment to process the feedstock stream into a suitable export product stream. In a multiple series system, one or more series can be offline for maintenance without significantly affecting the overall regeneration facility capacity. In the case where an upstream capture facility requires a series of processing capacities, changing the number of series in operation can also be used to increase or decrease capacity.

[0100] Each of the configurations and methods described herein may include at least one mixed fluid stream having a corresponding gas phase and a liquid phase. Each of the mixed fluid streams may travel from the inlet of the component to the outlet, and may primarily include liquid at the inlet, but primarily include gas at the outlet. The ratio of liquid to gas and the composition of the mixed fluid depend on several factors, including reaction rate, mass transfer, and process conditions. In some embodiments, there may be more or less mixed fluid streams than the mixed fluid streams depicted.

[0101] Process streams in a gas liquid contactor system, as well as process streams within any downstream process fluidly coupled to the gas liquid contactor system, can be controlled using one or more flow control systems (e.g., Figures 1 to 6 The flow control system may include: one or more flow pumps, fans, blowers, or solid conveyors to move the process stream; one or more flow pipes through which the process stream flows; and one or more valves to regulate the flow of the stream through the pipes. Each of the configurations described herein may include at least one variable frequency drive (VFD) coupled to a corresponding pump capable of controlling at least one liquid flow rate. In some embodiments, the liquid flow rate is controlled by at least one flow control valve.

[0102] In some embodiments, the flow control system can be manually operated. For example, the operator can set the flow rate of each pump or transfer device and set the valve opening or closing position to regulate the flow of the process flow through the pipeline in the flow control system. Once the operator sets the flow rate and the valve opening or closing position for all flow control systems distributed on the system, the flow control system can make the flow flow under constant flow conditions (for example, constant volume rate or other flow conditions. In order to change the flow conditions, the operator can, for example, manually operate the flow control system by changing the pump flow rate or the valve opening or closing position.

[0103] In some embodiments, the flow control system can be operated automatically. For example, the flow control system can be connected to a computer or a control system (for example, control system 999) to operate the flow control system. The control system may include a computer-readable medium, which stores instructions (such as flow control instructions and other instructions) that can be executed by one or more processors to perform operations (such as flow control operations). The operator can use the control system to set flow rates and valve opening or closing positions for all flow control systems distributed on the facility. In such embodiments, the operator can manually change flow conditions by providing input through the control system. In addition, in such embodiments, the control system can, for example, use a feedback system connected to the control system to automatically (that is, without manual intervention) control one or more of the flow control systems. For example, a sensor (such as a pressure sensor, a temperature sensor or other sensors) can be connected to a pipeline through which the process flow flows. The sensor can monitor and provide the flow conditions (such as pressure, temperature or other flow conditions) of the process flow to the control system. In response to the flow conditions exceeding a threshold value (such as a threshold pressure value, a threshold temperature value or other threshold values), the control system can automatically perform operations. For example, if the pressure or temperature in the pipeline exceeds a threshold pressure value or a threshold temperature value, respectively, the control system may provide a signal to a pump to reduce flow rate, open a valve to relieve pressure, shut off process flow, or other signal.

[0104] Figure 1 is a view of an exemplary gas liquid contactor unit 100. The gas liquid contactor unit 100 includes an ejector 102 mounted on a capture solution tank 104. The ejector 102 can be fixed to or movably attached to the capture solution tank 104. The ejector 102 includes a gas inlet 106, a capture solution inlet 108, and an ejector outlet 110. The gas inlet 106 is operable to receive a gas 112 containing CO2. Where the ejector 102 is movably attached, the gas inlet 106 of the ejector 102 can be rotated or oriented toward the dominant wind flow, thereby reducing the energy required to pump large amounts of gas. In some cases, the ejector 102 can have multiple gas inlets 106, some of which face different angles than other gas inlets 106, and some of the gas inlets 106 can be optionally shielded, closed, or covered if they are not facing the dominant wind direction.

[0105] In some embodiments, the gas 112 may be an atmospheric gas having a dilute CO2 concentration (e.g., in the range of about 300-10,000 ppm). In other embodiments, the gas 112 may be a flue gas or an exhaust gas from an industrial or point source having a higher CO2 concentration range. The CO2 concentration of the gas 112 may depend on the type of point source. For example, in the case of a coal-fired power plant, the point source may include 10-15 v / v% CO2. In the case where the gas 112 is derived from a point source, the gas inlet 106 may be coupled to an additional pipeline that carries the gas 112 from the point source. In addition to CO2, the gas 112 may also carry pollutants such as NOx and SOx. For example, the gas 112 may be a flue gas or exhaust gas including NOx and SOx, which may adversely affect the CO2 capture mechanism in the ejector 102. In such cases, the gas 112 may be pretreated in a pretreatment unit to remove these pollutants before flowing into the gas inlet 106.

[0106] In other cases, the gas 112 may be derived from a dilute source, such as atmospheric air, and may carry moisture, dust, insects, or particles based on local weather and geographic conditions. In such cases, the gas inlet 106 may have additional components, such as a mesh, to prevent dust, insects, and particles from entering the ejector 102.

[0107] The capture solution inlet 108 is operable to receive a lean capture solution 114, which in one embodiment is an aqueous mixture comprising KOH and / or K2CO3. For example, the lean capture solution 114 may comprise a molar concentration of KOH ranging from less than 1 molar to about 6 molar. In other embodiments, the lean capture solution 114 comprises another hydroxide-carbonate mixture, such as NaOH and Na2CO3. For example, the lean capture solution 114 may comprise a molar concentration of NaOH ranging from less than 1 molar to about 6 molar. In other embodiments, the lean capture solution comprises a different aqueous mixture comprising a bicarbonate / carbonate or aqueous amine mixture. The lean capture solution 114 is employed as a motive fluid to draw the gas 112 into the gas inlet 106. The reaction of the lean capture solution 114 with the CO2 in the gas 112 occurs at least partially in an initial mixing zone 122 within the ejector 102. The initial mixing zone 122 is configured to achieve turbulent mixing to promote the reaction of the lean capture solution 114 with the CO2 in the ejector 102. In some embodiments, a spray nozzle may be employed to direct the lean capture solution 114 toward the converging section of the ejector 102 to promote turbulent mixing in the initial mixing zone 122. The reaction forms a mixed fluid 119 having a gas phase and a liquid phase.

[0108] refer to Figure 1, the lean capture solution 114 serving as the motive fluid for the ejector 102 flows in a downward direction to draw the gas 112 into the gas inlet 106 in a lateral direction (eg, substantially or primarily horizontally).

[0109] The reaction of the lean capture solution 114 with CO2 is carried out in the ejector 102, so that the concentration of hydroxide [OH - ] and the CO2 concentration in the gas phase of the mixed fluid 119 decreased, while the carbonate concentration [CO3 2- The ejector 102 has an ejector outlet 110 operable to discharge a mixed fluid 119 into the capture solution tank 104.

[0110] The liquid phase of the mixed fluid 119 can be collected in the capture solution tank 104. In some cases, the liquid phase of the mixed fluid 119 includes a rich capture solution 120 and at least a portion of the unreacted lean capture solution 114. The rich capture solution 120 has a higher concentration of carbonaceous materials, such as carbonates, than the lean capture solution 114. The capture solution tank 104 is fluidly and mechanically coupled to the vent line 144. The gas phase of the mixed fluid 119 is drawn out of the capture solution tank 104 by a fan 134 contained in the vent line 144. In some cases, the gas phase of the mixed fluid 119 includes a CO2-lean gas 116 and at least a portion of the unreacted gas 112. The CO2-lean gas 116 has a lower concentration of CO2 than the gas 112 and is a product stream produced by the gas liquid contactor unit 100. Reference Figure 1 , the capture solution tank 104 is positioned below the ejector 102 and the blower 134. In some embodiments, and with reference to Figure 1 , the fan 134 , the ventilation pipe 144 and the ejector 102 are all located above the capture solution tank 104 .

[0111] In some cases, the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ] may be higher than the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ]. For example, the ratio of [CO3 2- ] and [OH - ] may be less than about 0.4, and the [CO3 2- ] and [OH - ] can be greater than about 0.5.

[0112] In some cases, the gas liquid contactor unit 100 is relatively close to the surrounding environment. The combination of the relatively closed ejector 102 and the vent pipe 144 helps prevent or reduce evaporation losses in the gas liquid contactor unit 100. Despite these features, in some embodiments, it may be desirable to compensate for evaporation losses that may occur over time in the gas liquid contactor unit 100. In some cases, the rich capture solution 120 may include a compensation capture solution stream 118, a compensation water stream 124, or a combination of both, which are supplied to the capture solution tank 104. The compensation water stream 124 can be supplied at a rate that compensates for evaporation losses.

[0113] In some embodiments, the compensating capture solution 118 has a KOH concentration ranging from 0.1 wt % to about 50 wt %. The compensating capture solution 118 can compensate for dilution from the intake water or possible capture solution losses. In the illustrated embodiment, the rich capture solution 120 is pumped out of the capture solution tank 104 via a capture solution circulation pump 126 and can be divided into a first portion 128 of the rich capture solution and a second portion 130 of the rich capture solution. In some embodiments, the capture solution circulation pump 126 has a discharge pressure in the range of about 20 psig to about 120 psig. In some embodiments, the capture solution circulation pump 126 has a discharge pressure in the range of about 80 psig to about 100 psig. The separation of the rich capture solution 120 into the first portion 128 of the rich capture solution and the second portion 130 of the rich capture solution can be achieved by a distribution header, a manifold, or other suitable flow diversion device. For example, the distribution header can have an inlet and at least two outlets. The inlet of the distribution header may be coupled to a pipe that flows the rich capture solution 120 to the distribution header, and the distribution header may separate the rich capture solution 120 into a first portion 128 of the rich capture solution and a second portion 130 of the rich capture solution. The distribution header may discharge the first portion 128 of the rich capture solution through a first outlet and discharge the second portion 130 of the rich capture solution through a second outlet. The outlets of the distribution header may each be coupled to a corresponding pipe and a corresponding outlet valve.

[0114] The first portion 128 of the rich capture solution may be transferred to a regeneration system 138 where the CO2 is concentrated and released. For example, a capture solution comprising KOH and K2CO3 may result in the following reaction in the regeneration system 138:

[0115] K2CO 3(aq) +Ca(OH) 2(s) →2KOH aq +CaCO 3(s) (Eq.2)

[0116] CaO (s) +H2O (l) →Ca(OH)2(s) (Eq.3)

[0117] CaCO 3(s) →CaO (s) +CO 2(g) (Eq.4)

[0118] In some applications, potassium (K) in the reactions of Eq. 1 to Eq. 4 can be replaced by sodium (Na). For example, the gas-liquid contactor can use NaOH instead of KOH as the capture agent in the reaction of Eq. 1.

[0119] The reactions of Eq.2, Eq.3 and Eq.4 can be carried out in a lime causticizing system such as Figure 6The lime causticizing system 640 of the present invention may occur in a regeneration system 138 of the lime causticizing system 640 of the present invention. The lime causticizing system may include one or more reactor tanks in which the reactions of Eq. 2 and Eq. 3 occur. In some of these embodiments, the reactor tank may include a continuous stirred tank reactor. In some embodiments, the lime causticizing system includes a pellet reactor and a separate slaked lime maker, in which the reaction of Eq. 2 occurs, and in which the reaction of Eq. 3 occurs. The regeneration system 138 may also include a calciner in which the reaction of Eq. 4 occurs. In one embodiment, the calciner is an electric calciner. In other embodiments, the calciner may be a circulating fluidized bed calciner, a bubbling bed calciner, a rotary calciner, or a flash calciner. The regeneration system 138 produces a regenerated capture solution 132, which is combined with the second portion 130 of the rich capture solution to form a lean capture solution 114. The capture solution inlet 108 of the ejector 102 is configured to receive the lean capture solution 114. In one embodiment, regeneration system 138 includes an electrochemical treatment system operable to generate carbon products. For example, regeneration system 138 may include components similar to those described in U.S. Patent 8,871,008, U.S. Patent 8,119,091 and U.S. Patent Application Publication No. 2022 / 0362707A1, each of which is incorporated herein by reference, such as membrane separation treatment unit, gas stripping unit, filtration unit and gas compression and purification unit. The membrane separation unit is used to separate dissolved target substances (such as CO2) from buffer substances in aqueous streams, and may include one or more components, such as nanofiltration units, chromatographic columns, etc. The driving force of the membrane separation process may include, for example, electricity, pressure, temperature, concentration difference or salinity gradient. One or more components in the membrane separation unit may be the same or different. In some embodiments, the membrane separation unit includes an ion exchange membrane (e.g., a monovalent anion exchange membrane), which can be used in units of processes such as, for example, electrodialysis. Other components of the membrane separation unit can be used for various other processes, such as, for example, reverse osmosis, ultrafiltration, microfiltration, nanofiltration, diffusion dialysis, dialysis, Donnan dialysis, pressure dialysis, pervaporation, membrane distillation, and ion chromatography. In some cases, the gas stripping unit includes a membrane distillation unit.

[0120] In some embodiments, the capture solution tank 104 includes two outlets, each fluidly coupled to a respective pump. The first outlet discharges a first portion of the rich capture solution 120 to the first pump, which causes the first portion of the rich capture solution 120 to flow to the regeneration system 138. The second outlet discharges a second portion of the rich capture solution 120, which is combined with the regeneration solution 132 flowing from the regeneration system 138 to form a lean capture solution 114. The lean capture solution 114 then flows to the ejector 102 via the second pump.

[0121] The fan 134 is positioned at the CO2 lean gas outlet 136 of the vent pipe 144, which is fluidly coupled to the capture solution tank 104. The fan 134 can be an induced draft fan, wherein the rotation of the fan 134 draws the CO2 lean gas 116 from the upper portion of the capture solution tank 104 through the CO2 lean gas outlet 136. The CO2 lean gas 116 is discharged through the CO2 lean gas outlet 136. It may be beneficial for the CO2 lean gas outlet 136 to be positioned to discharge the CO2 lean gas 116, or to be positioned to direct the CO2 lean gas 116 away from the gas inlet 106 of the ejector 102 and away from the gas inlet of any adjacent ejector (e.g., in the multiple ejector embodiments described below). For example, the CO2 lean gas outlet 136 can be positioned to direct the CO2 lean gas 116 toward the ground, thereby avoiding the CO2 lean gas 116 from entering the gas inlet of any adjacent gas liquid contactor unit. In one embodiment, the blower 134 is sized for an outlet velocity in the range of about 1 ft. / s up to about 25 ft. / s. In some embodiments, the blower 134 is sized for an outlet velocity less than about 10 ft. / s.

[0122] refer to Figure 1 , the ejector 102 and the vent pipe 144 are vertical bodies. The ejector 102 defines an upright ejector axis 102A. The ejector axis 102A is perpendicular to the ejector axis 102A. Figure 1 The ejector axis 102A is parallel to the vertical line in FIG. The ejector axis 102A is parallel to the vertical distance measured between the capture solution inlet 108 and the ejector outlet 110. The ventilation tube 144 extends in a direction parallel to the fan axis 134A of the fan 134. The fan axis 134A is parallel to the ejector axis 102A. Figure 1 In the embodiment of the present invention, the fan axis 134A and the ejector axis 102A are horizontally spaced apart. In other embodiments, the fan axis 134A and the ejector axis 102A may be co-linear.

[0123] In some applications, it may be beneficial that the ejector 102 is as large as practical. For example, some catalog ejectors may be up to 36 feet in height and up to 96 inches in inlet diameter, but larger custom units may be designed and manufactured. In some embodiments, the gas liquid contactor unit 100 may be at least partially comprised of a caustic compatible material such as a thermoplastic, a thermosetting resin, stainless steel, or a combination thereof. Some examples of suitable thermoplastics include polyvinyl chloride (PVC), chlorinated polyvinyl chloride (CPVC), polytetrafluoroethylene (PTFE). Examples of suitable thermosetting resins are vinyl esters based on brominated bisphenol A.

[0124] In some cases, at least one of the lean capture solution 114, the rich capture solution 120, the make-up capture solution 118, and the regeneration capture solution 132 may include a rate-increasing additive capable of increasing the amount of CO2 captured. Some examples of rate-increasing additives include catalysts, promoters, or solvents, such as piperazine, carbonic anhydrase, MEA, and DEA. In some cases, the rate-increasing additive may move freely in the capture solution within the gas-liquid contactor unit 100. In some cases, the rate-increasing additive may be fixed in a capsule that moves freely in the capture solution within the gas-liquid contactor unit 100. In the case where the rate-increasing additive moves freely, the rate-increasing additive may be retained within the gas-liquid contactor unit 100 and prevented from flowing to the regeneration system 138 by a barrier or filtration system. In some cases, it may be advantageous to coat the surfaces of components of the gas-liquid contactor unit 100 with a rate-increasing material, the rate-increasing material comprising a rate-increasing additive, such as a promoter or catalyst, stabilized on a solid support by a suitable immobilization method. The gas-liquid contactor unit 100 may have a plurality of wetted surfaces coated with a rate-increasing material. For example, the sparger 102 and the capture solution tank 104 can each have a wetted surface coated with a rate-enhancing material. In particular, the interior walls, components, and surfaces within the gas liquid contactor unit 100 that are wetted by the capture solution can be coated with a rate-enhancing material. In some applications, a combination of a freely mobile rate-enhancing additive in the capture solution and a rate-enhancing material coated on a surface within the gas liquid contactor can be used to improve CO2 uptake. In some embodiments, the type and amount of rate-enhancing additive used can depend on the capture solution properties, such as composition, presence of bicarbonate or amines, temperature, or pH.

[0125] In some embodiments, the gas liquid contactor unit 100 is communicatively coupled to and controlled by a control system 999 .

[0126] The components of the gas liquid contactor unit 100 can form a modular gas liquid contactor system (such as Figure 3 System 300, Figure 4 System 400 and Figure 5 Module of system 500).

[0127] Figure 2 is a cross-sectional view of an exemplary supplemental gas-liquid contactor unit 200. The supplemental gas-liquid contactor unit 200 includes Figure 1 Some of the same components of the gas liquid contactor unit 100. For example, Figure 2 The components 202 to 236 may be connected with Figure 1 The components 102 to 136 operate or are configured in the same or similar manner. For the sake of brevity, the following Figure 2Some of the previously described functions and embodiments applicable to both the gas liquid contactor unit 100 and the supplemental gas liquid contactor unit 200 will be omitted from the description. The description of the gas liquid contactor unit 100 provided herein, as well as the description of all features and advantages associated with the gas liquid contactor unit 100, apply to the gas liquid contactor unit 200 after necessary modifications.

[0128] like Figure 2 As shown, the supplemental gas liquid contactor unit 200 includes several components, such as a mixing chamber 238, a demister 240, and a packed bed absorption column 242. In an embodiment, each of the mixing chamber 238, the demister 240, and the packed bed absorption column 242 can be used in the supplemental gas liquid contactor unit 200 independently or in combination with each other. For example, the supplemental gas liquid contactor unit 200 may include the mixing chamber 238 and the demister 240, but not the packed bed absorption column 242. In another example, the supplemental gas liquid contactor unit 200 may include the demister 240, but not the mixing chamber 238 and the packed bed absorption column 242.

[0129] The supplemental gas liquid contactor unit 200 includes an ejector 202 fluidly and mechanically coupled to a capture solution tank 204. The ejector 202 can be fixed to or removably attached to the capture solution tank 204. Where the ejector 202 is removably attached to the capture solution tank 204, the ejector 202 can be rotated or oriented toward the dominant wind flow, thereby reducing the energy required to pump large amounts of gas. The ejector 202 includes a gas inlet 206, a capture solution inlet 208, and an ejector outlet 210. The gas inlet 206 is operable to receive a gas 212 comprising CO2. In some cases, the ejector 202 can have multiple gas inlets 206, some of which face different angles than other gas inlets 206, and some of which can be optionally shielded, closed, or covered if they do not face the dominant wind direction.

[0130] The capture solution inlet 208 is operable to receive a lean capture solution 214, which in one embodiment is an aqueous mixture comprising KOH and K2CO3. The reaction of the lean capture solution 214 with the CO2 in the gas 212 occurs at least partially in an initial mixing zone 222 within the ejector 202. The initial mixing zone 222 is configured to achieve turbulent mixing to promote the reaction of the lean capture solution 214 with the CO2 in the gas 212 within the ejector 202. In some embodiments, a spray nozzle may be employed to direct the lean capture solution 214 toward a constricted portion of the ejector 202 to promote turbulent mixing in the initial mixing zone 222. The reaction in the initial mixing zone 222 forms a first mixed fluid 219 having a gas phase and a liquid phase.

[0131] The reaction of the lean capture solution 214 with CO 2 is carried out in the ejector 202 so that the hydroxyl concentration [OH - ] and the CO2 concentration in the gas phase of the first mixed fluid 219 is reduced, while the carbonate concentration [CO3 2- The ejector 202 has an ejector outlet 210 operable to discharge a first mixed fluid 219 into a mixing chamber 238 .

[0132] The ejector outlet 210 is fluidly coupled to a mixing chamber 238. In one embodiment, the mixing chamber 238 is a static mixer configured to promote turbulent mixing and shearing of the gas-liquid mixture by employing textured surfaces and / or static mixing components to achieve high tortuosity and high mass transfer. Non-limiting examples of textured surfaces and / or static mixing components include baffles and blades or present on baffles and blades. The mixing chamber 238 can enable rapid dissolution and reaching gas-liquid equilibrium. The reaction of the lean capture solution 214 and the CO2 in the first mixed fluid 219 is further carried out in the mixing chamber 238 to form a second mixed fluid 221 having a gas phase and a liquid phase. Reference Figure 2 , mixing chamber 238 is vertically positioned between injector outlet 210 and capture solution tank 204 .

[0133] The reaction is carried out in the mixing chamber 238, so that [OH - ] and the CO2 concentration in the gas phase of the second mixed fluid 221 are both reduced, while the [CO3 2- The second mixed fluid 221 is discharged from the mixing chamber 238 into the capture solution tank 204.

[0134] The mixing chamber 238 is fluidly coupled to the capture solution tank 204. The capture solution tank 204 collects the liquid phase of the mixed fluid. In some cases, the capture solution tank 204 is operable to receive a compensating capture solution flow 218, a compensating water flow 224, or a combination of the two. These flows are added to the liquid in the capture solution tank 204 to form a rich capture solution 220. The compensating capture solution 218 can compensate for dilution from the intake water or possible capture solution losses. In the illustrated embodiment, the rich regenerated capture solution 246 is received by the capture solution tank 204 and combined with the liquid phase of the mixed fluid to form the rich capture solution 220. The rich capture solution 220 is pumped out of the capture solution tank 204 via the capture solution circulation pump 226 and is divided into a first portion 228 of the rich capture solution and a second portion 230 of the rich capture solution. The division of the rich capture solution 220 into the first portion 228 of the rich capture solution and the second portion 230 of the rich capture solution can be achieved by a distribution header, a manifold, or other suitable flow diversion device. For example, a distribution header for distributing the rich capture solution 220 may have an inlet for receiving the rich capture solution 220 and at least two outlets for distributing the separated portions 228, 230 of the rich capture solution. The inlet of the distribution header may be coupled to a pipe that flows the rich capture solution 220 to the distribution header, and the distribution header may separate the rich capture solution 220 into a first portion 228 of the rich capture solution and a second portion 230 of the rich capture solution. The distribution header may then discharge the first portion 228 of the rich capture solution through the first outlet and discharge the second portion 230 of the rich capture solution through the second outlet. The outlets of the distribution header may each be coupled to a corresponding pipe and a corresponding outlet valve. After flowing out of the corresponding outlets of the distribution header, the first portion 228 of the rich capture solution may be transferred to the regeneration system 248, and the second portion 230 of the rich capture solution may be combined with the lean regenerated capture solution 232 formed in the regeneration system 248. Other configurations for fluid flow, separation, and distribution of the rich capture solution 220 are possible.

[0135] In some embodiments, the capture solution tank 204 includes two outlets, each outlet fluidly coupled to a respective pump. For example, the capture solution tank 204 may include a first outlet that discharges a first portion of the rich capture solution to a first pump that causes a first portion of the rich capture solution 220 to flow to the regeneration system 248, and a second outlet that discharges a second portion of the rich capture solution 220 that is combined with the lean regeneration solution 232 flowing from the regeneration system 248 to form the lean capture solution 214. The lean capture solution 214 then flows to the ejector 202 via the second pump.

[0136] The liquid phase of the second mixed fluid 221 may be collected in the capture solution tank 204 and combined with the rich capture solution 220. The reaction of the lean capture solution 214 with CO2 further proceeds within the capture solution tank 204 to form a third mixed fluid 223 having a gas phase and a liquid phase.

[0137] The reaction is carried out in the capture solution tank 204, so that [OH - ] and the CO2 concentration in the gas phase of the third mixed fluid 223 is reduced, while the CO3 2- The liquid phase of the third mixed fluid 223 is collected in the capture solution tank 204. The gas phase of the third mixed fluid 223 is sucked from the capture solution tank 204 to the ventilation pipe 244 by the fan 234.

[0138] The capture solution tank 204 is mechanically and fluidically coupled to the vent 244. In some embodiments, the vent 244 can accommodate at least one of a packed bed absorber column 242 and a fan 234 positioned upstream of the demister 240. Each component housed in the vent 244 can be directly or indirectly fluidly coupled to the CO2 lean gas outlet 236. In some embodiments, the vent 244 accommodates the packed bed absorber column 242 and the fan 234. In other embodiments, the vent 244 accommodates the demister 240 and the fan 234. In some embodiments, the packed bed absorber column 242 is positioned upstream of the demister 240 and the fan 234. In some embodiments, and with reference to Figure 2 , the mist eliminator 240, the packed bed absorption column 242, the fan 234 and the CO2-lean gas outlet 236 are all present in the supplementary gas liquid contactor unit 200 and are stacked one on top of the other. Figure 2 The packed bed absorption column 242, the demister 240, the fan 234 and the CO2-lean gas outlet 236 are vertically spaced apart and are arranged sequentially from the packed bed absorption column 242 at the lowest vertical position to the CO2-lean gas outlet 236 at the highest vertical position.

[0139] In some embodiments, the lean regeneration capture solution 232 is introduced into the packed bed absorption column 242. The packed bed absorption column 242 includes a packing material that is shaped to provide a large surface area for the capture solution to contact the third mixed fluid stream 223, thereby increasing the amount of captured CO2. In one embodiment, the packed bed absorption column 242 includes a structured packing (e.g., a corrugated plate). In some embodiments, the packed bed absorption column 242 includes a region of loose or random packing (e.g., a Raschig ring packing) contained within the packed bed absorption column 242. The lean regeneration capture solution 232 is introduced into the packed bed absorption column 242 from the regeneration system 248. The countercurrent flow of the gas phase of the third mixed fluid 223 and the lean regeneration capture solution 232 in the packed bed absorption column 242 enables further capture of CO2 that is not captured in the ejector 202, the mixing chamber 238, and the capture solution tank 204 from the third mixed fluid 223. For example, the lean regenerated capture solution 232 flows through the packed bed absorption column 242 toward the capture solution tank 204, and the third mixed fluid 223 flows through the packed bed absorption column 242 toward the lean CO2 gas outlet 236 and reacts with the lean regenerated capture solution 232 in the packed bed absorption column 242. The reaction forms a fourth mixed fluid 225 having a gas phase (e.g., the lean CO2 gas from the packed bed absorption column 242) and a liquid phase, and a rich regenerated capture solution 246.

[0140] The reaction is carried out in the packed bed absorption column 242, so that [OH - ] and the CO2 concentration in the gas phase of the fourth mixed fluid 225 is lower than the equivalent in the liquid phase of the third mixed fluid 223, and the [CO3 2- ] is greater than [CO3 2- ]. [CO3 in the rich regeneration capture solution 246 2- ] is greater than [CO3 2- ]. The fourth mixed fluid 225 is pumped from the packed bed absorber column 242 to the demister 240 by the fan 234, and the rich regenerated capture solution 246 is collected in the capture solution tank 204 and combined with the liquid phase of the mixed fluid to form the rich capture solution 220.

[0141] In one embodiment, the supplemental gas liquid contactor unit 200 can be used to perform a Benfield process chemistry, where K2CO3 is used to remove acid gases, including CO2. In such an embodiment, the supplemental gas liquid contactor unit 200 and the regeneration system 248 can be configured to employ a Benfield process chemistry according to the reaction of Eq. 5 below.

[0142]

[0143] For example, in a Benfield process chemical process, the supplemental gas liquid contactor unit 200 can be coupled to a regeneration system 248 capable of recovering the absorbed CO2, for example by steam stripping, and regenerating K2CO3 to return to the packed bed absorber column 242. The regeneration system 248 can be configured to process a bicarbonate solution.

[0144] The packed bed absorber column 242 is fluidly coupled to a demister 240. In some embodiments, the demister 240 is positioned upstream of the blower 234 to reduce the number of droplets entrained in the fourth mixed fluid 225 before the gas phase of the fourth mixed fluid 225 is discharged from the supplemental gas liquid contactor unit 200 as the CO2-lean gas 216. The demister 240 can be a herringbone demister, wherein droplets entrained in the fourth mixed fluid 225 adhere to the angled surfaces of the demister 240, while the gas phase of the fourth mixed fluid 225 passes through the demister 240 as the CO2-lean gas 216. In some embodiments, the demister 240 is sized for a face velocity of from about 1 ft. / s to at most about 15 ft. / s. In some embodiments, the demister 240 is sized for a face velocity of less than about 10 ft. / s.

[0145] The demister 240 is fluidly coupled to a fan 234. The fan 234 can be an induced draft fan that draws the CO2-lean gas 216 from the demister 240. In one embodiment, the fan 234 is sized to produce an outlet velocity in the range of about 1 ft. / s to about 25 ft. / s at most. In some embodiments, the fan 234 is sized to produce an outlet velocity of less than about 10 ft. / s. In some embodiments, the fan 234 is sized to match the demister face velocity. In some embodiments, the CO2-lean gas 216 has a lower CO2 concentration than the gas 212 and / or at least one or the first mixed fluid 219, the second mixed fluid 221, the third mixed fluid 223, and the fourth mixed fluid 225. The CO2-lean gas 216 is discharged through the CO2-lean gas outlet 236 as a product stream of the supplemental gas liquid contactor unit 200. It may be beneficial for the lean CO2 gas outlet 236 to be positioned to discharge the lean CO2 gas 216, or to be positioned to direct the lean CO2 gas 216 away from the gas inlet 206 of the ejector 202 and away from the gas inlet of any adjacent ejector. For example, the lean CO2 gas outlet 236 can be positioned to direct the lean CO2 gas 216 toward the ground, thereby avoiding the lean CO2 gas 216 from entering the gas inlet of any adjacent gas-liquid contactor unit.

[0146] In some embodiments, the lean regeneration capture solution 232 may be provided to the second portion of the rich capture solution 230 via a valve or connection, or directly to the top of the packed bed absorber column 242 via a valve or inlet, or a combination of both. For example, in the illustrated embodiment, the supplemental gas liquid contactor unit 200 includes a valve that controls the flow of the lean regeneration capture solution 232 from the regeneration system 248. In some embodiments, valve V-1 controls the flow of the lean regeneration capture solution 232 to the packed bed absorber column 242. In some embodiments, valve V-2 controls the flow of the lean regeneration capture solution 232 to be combined with the second portion of the rich capture solution 230. The flow rate of the lean regeneration capture solution 232 (via the position of at least one of valve V-1 and valve V-2) can determine the composition of the lean capture solution 214 returned to the capture solution inlet 208 of the ejector 202.

[0147] For example, if the first valve V-1 is open and the second valve V-2 is closed, the lean capture solution 214 will include a lower hydroxide concentration [OH - ] and higher carbonate concentrations [CO3 2- ]. For example, if the first valve V-1 is opened and the second valve V-2 is closed, the rich regeneration capture solution 246 is combined with the liquid phase of the mixed fluid in the capture solution tank 204 to form a rich capture solution 220, which is divided into a lean capture solution 214 and a first portion 228 of the rich capture solution. The lean regeneration capture solution 232 flows through the packed bed absorption column 242 and reacts with the CO2 in the third mixed fluid 223 to form a rich regeneration capture solution 246. The reaction of CO2 with the lean regeneration capture solution 232 reduces the hydroxyl concentration [OH] in the rich regeneration capture solution 246. - ] and increase the carbonate concentration [CO3 2- Then, the rich regeneration trap solution 246 is combined with the rich trap solution 220 and returned to the ejector 202 as the lean trap solution 214. In this case, since the lean regeneration trap solution 232 flows through V1, the hydroxide concentration [OH - ] and carbonate concentration [CO3 2- ] is changed by upstream reaction with CO2.

[0148] As another example, if the first valve V-1 is closed and the second valve V-2 is open, the lean regeneration capture solution 232 is combined with the second portion 230 of the rich capture solution to form the lean capture solution 214. The lean regeneration capture solution 232 does not react with CO2 before being combined with the second portion 230 of the rich capture solution and returned to the ejector 202 as the lean capture solution 214. In this case, the hydroxyl concentration [OH - ] and carbonate concentration [CO3 2- ] is not affected by the flow of lean regenerated capture solution 232 through Vl above the packed bed absorption column 242 because valve Vl is closed and therefore no lean regenerated capture solution 232 flows through Vl into the packed bed absorption column 242.

[0149] In some embodiments, the respective liquid phases of the first mixed fluid 219, the second mixed fluid 221, the third mixed fluid 223, and the fourth mixed fluid 225 may each include at least a portion of the unreacted lean capture solution 214. In some cases, the respective gas phases of the first mixed fluid 219, the second mixed fluid 221, the third mixed fluid 223, and the fourth mixed fluid 225 may each include at least a portion of the CO2 in the unreacted gas 112.

[0150] Although each of the mixed fluid streams is named in order, the order naming only indicates the position or location of the mixed fluid within the unit and / or system, and is not necessarily the order in which the mixed fluids are formed. Therefore, each of the mixed fluid streams can include at least a portion of any previous mixed fluid stream. For example, the third mixed fluid 223 can include at least a portion of the first mixed fluid 219, and does not necessarily need to form the second mixed fluid 221 in between.

[0151] In some cases, the regeneration system 248 processes the first portion 228 of the rich capture solution to increase the concentration of the carbonaceous material, and the carbon is then released as a concentrated product. In one embodiment, the regeneration system 248 includes an electrochemical processing system operable to generate a carbon product. For example, the regeneration system 248 may include components of U.S. Patent No. 8,871,008, U.S. Patent No. 8,119,091, and U.S. Patent Application Publication No. 2022 / 0362707A1, wherein a membrane separation unit is used to separate a dissolved target substance, such as CO2, from a buffer substance in an aqueous stream.

[0152] In some applications, it may be beneficial that the ejector 202 is as large as practical. For example, some catalog ejectors may be up to 36 feet in height and up to 96 inches in inlet diameter, but larger custom units may be designed and manufactured. In some embodiments, the supplemental gas liquid contactor unit 200 may be at least partially comprised of a caustic compatible material such as a thermoplastic, a thermosetting resin, stainless steel, or a combination thereof. Some examples of suitable thermoplastics include polyvinyl chloride (PVC), chlorinated polyvinyl chloride (CPVC), polytetrafluoroethylene (PTFE). Examples of suitable thermosetting resins are vinyl esters based on brominated bisphenol A.

[0153] In some cases, at least one of the lean capture solution 214, the rich capture solution 220, the make-up capture solution 218, the lean regeneration capture solution 232, and the rich regeneration capture solution 246 includes a rate-increasing additive that can increase the CO2 capture rate, such as piperazine, carbonic anhydrase, MEA, and DEA. The rate-increasing additive can move freely in the capture solution within the supplemental gas liquid contactor unit 200. In some cases, the rate-increasing additive can be fixed in a capsule that moves freely in the capture solution within the supplemental gas liquid contactor unit 200. In embodiments where the rate-increasing additive moves freely, the rate-increasing additive can be contained within the supplemental gas liquid contactor unit 200 and prevented from flowing to the regeneration system 248 by a barrier or filtration system. In some cases, it may be advantageous for the supplemental gas liquid contactor unit 200 to have multiple wetted surfaces coated with a rate-increasing material. The rate-increasing material can include a rate-increasing additive stabilized on a solid support by an immobilization method. For example, the ejector 202, capture solution tank 204, mixing chamber 238, packed bed absorber column 242, and vent pipe 244 can each have a wetted surface coated with a rate-enhancing material. In particular, the inner wall of the supplemental gas liquid contactor unit 200 can be coated with a rate-enhancing material. In some applications, a combination of a freely mobile rate-enhancing additive in the capture solution and a rate-enhancing material coated on a surface within the gas liquid contactor can be used to improve CO2 uptake.

[0154] In some embodiments, the supplemental gas liquid contactor unit 200 can be coupled to and controlled by a control system 999 .

[0155] The components of the supplemental gas liquid contactor unit 200 can be formed for use in a modular gas liquid contactor system such as Figure 3 Linear gas-liquid contactor system 300, Figure 4 Peripheral gas-liquid contactor system 400 and Figure 5 Modules of a multi-row gas liquid contactor system 500).

[0156] Figure 3304). is a plan view of an exemplary linear gas liquid contactor system 300. The linear gas liquid contactor system 300 includes a set of ejectors 302a, 302b, 302c, 302d, 302e, 302f (collectively and individually referred to as ejectors 302), which are fluidly coupled to a set of lean CO2 gas outlets 304a, 304b, 304c, 304d, 304e, 304f (collectively and individually referred to as 304). The ejectors 302 and the lean CO2 gas outlets 304 are mechanically and fluidly coupled to a capture solution tank 306. The ejectors 302 can be fixed to or removably attached to the capture solution tank 306. The removably attached ejectors 302 can be rotated or oriented toward the dominant wind flow, thereby reducing the energy required to deliver a large amount of air into the gas inlet. The CO 2 lean gas outlets 304 are each coupled to a respective blower 314 a , 314 b , 314 c , 314 d , 314 e , 314 f (collectively and individually referred to as blowers 314 ).

[0157] The linear gas liquid contactor system 300 may include Figure 1 Gas liquid contactor unit 100 or Figure 2 At least some of the components of the supplemental gas liquid contactor unit 200 of the present invention. Therefore, the description of the gas liquid contactor unit 100 and the description of the supplemental gas liquid contactor unit 200, as well as the description of all features and advantages associated with the gas liquid contactor unit 100 and the description of all features and advantages associated with the supplemental gas liquid contactor unit 200 herein, apply mutatis mutandis to the ejector 302 and to the linear gas liquid contactor system 300. The ejectors 302 can each include a gas inlet operable to receive a gas comprising CO2, a capture solution inlet operable to receive a lean capture solution 316 from the capture solution distribution line 310, and a mixing zone configured to achieve turbulent mixing to promote reaction of the gas and the lean capture solution 316. In some embodiments, a spray nozzle can be used to direct the lean capture solution 316 toward the contraction section of the ejector 302 to promote turbulent mixing in the initial mixing zone. Turbulent mixing enables CO2 from the gas to be absorbed to form a mixed fluid having a gas phase and a liquid phase.For example, the CO2 absorption reaction that may occur in the initial mixing zone of the ejector 302 is described in Eq. 1 above.

[0158] The lean capture solution 316 is reacted with the CO2 in the gas to form a mixed fluid having a gas phase and a liquid phase. As the reaction proceeds throughout the linear gas-liquid contactor system 300, the hydroxide concentration [OH - ] and the CO2 concentration in the gas phase of the mixed fluid decreased, while the carbonate concentration [CO3 2-] increases. In some cases, the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ] can be higher than the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ]. For example, if the [CO3 2- ] and [OH - ] is less than about 0.4, then the [CO 2- ] and [OH - ] can be greater than about 0.5.

[0159] The ejector 302 is fluidly coupled to the capture solution tank 306. The rich capture solution 318 flows from the ejector 302 to the capture solution tank 306. In one embodiment, an intervening mixing chamber (e.g., a static mixer) is fluidly coupled to the outlet of the ejector 302 and is fluidly coupled to the capture solution tank 306, such as Figure 2 The mixing chamber or static mixer coupled to the outlet of the ejector 302 promotes turbulent mixing and shearing of the gas-liquid mixture. In this embodiment, further mixing of the CO2 with the lean capture solution 316 can promote the reaction to form a mixed fluid. The reaction is carried out in the mixing chamber, so that [OH - ] and the CO2 concentration in the gas phase of the mixed fluid decreased, while the [CO3 2- In some cases, at least some of the ejectors 302 may have multiple gas inlets facing different angles and may be operable to be shielded, closed, or covered if not facing the dominant wind direction.

[0160] The capture solution circulation pump 308 is fluidly coupled to the capture solution tank 306. The capture solution circulation pump 308 pumps a rich capture solution 318 out of the capture solution tank 306. A first portion of the rich capture solution 318 is pumped to the regeneration system 312, and a second portion of the rich capture solution 318 is circulated back to the ejector 302 via the capture solution distribution line 310. In some embodiments, the second portion of the rich capture solution 318 is combined with the regenerated capture solution 332 to form a lean capture solution stream 316. In some embodiments, the flow rate of the lean capture solution 316 in the capture solution distribution line 310 can be varied based on a target amount of captured CO2. In one embodiment, the first portion of the rich capture solution 318 can be greater than the second portion of the rich capture solution 318. In some embodiments, the capture solution tank 306 includes two outlets, each outlet being fluidly coupled to a respective pump. For example, the first outlet may discharge a first portion of the rich capture solution 318 to a first pump that flows the first portion of the rich capture solution 318 to the regeneration system 312, and the second outlet may discharge a second portion of the rich capture solution 318 that is combined with the regenerated lean solution 332 flowing from the regeneration system 312 to form the lean capture solution 316. The lean capture solution 316 may then flow to the ejector 302 via the second pump.

[0161] The regeneration system 312 may include a lime causticization system such as Figure 6 The regeneration system 312 includes an electrochemical treatment system operable to generate a carbon product. For example, the regeneration system 638 may include components that are the same or similar to those described in U.S. Pat. No. 8,871,008, U.S. Pat. No. 8,119,091, and U.S. Patent Application Publication No. 2022 / 0362707A1, wherein a membrane separation unit is used to separate a dissolved target substance, such as CO2, from a buffer substance in an aqueous stream.

[0162] The liquid phase of the mixed fluid may be collected in capture solution tank 306 and combined with rich capture solution 318. The reaction of lean capture solution 316 with CO2 in the gas entering the gas inlet of ejector 302 may continue within capture solution tank 306 to promote the reaction to form a mixed fluid.

[0163] The reaction is carried out in the capture solution tank 306, so that [OH - ] and the CO2 concentration in the gas phase of the mixed fluid decreased, while the [CO3 2- ] increases. The liquid phase of the mixed fluid is collected in the capture solution tank 306 as it is formed. The gas phase of the mixed fluid is drawn from the capture solution tank 306 into one or more vent pipes of the ejector 302 by the fan 314.

[0164] In some embodiments, the fan 314 is an induced draft fan. The linear gas liquid contactor system 300 can include a plurality of ventilating ducts, wherein each ventilating duct includes a fan 314. In some cases, at least one ventilating duct can include a ventilating duct as described in reference Figure 2 The other components described in the vent 244 of the linear gas-liquid contactor system 300. For example, the vent in the linear gas-liquid contactor system 300 may include a corresponding demister positioned upstream of the fan 314, and / or one or more of the corresponding packed bed absorption columns.

[0165] In some embodiments, the regenerated capture solution 332 may flow through a packed bed absorber column to absorb at least a portion of any remaining CO2 in the mixed fluid that was not absorbed in the countercurrent reaction by the ejector 302 or the capture solution tank 306. The packed bed absorber column may include structured packing or loose (e.g., bulk) packing.

[0166] In one embodiment, the linear gas liquid contactor system 300 can be used to perform a Benfield process chemistry, where K2CO3 is used to remove acid gases, including CO2. In such an embodiment, the downstream unit (e.g., a regeneration system including a steam stripper) is also configured to use a Benfield process chemistry according to the reaction of Eq. 5.

[0167] System 300 may include a mist eliminator positioned upstream of fan 314 (e.g., Figure 2 The mist eliminator 240 of the linear gas-liquid contactor system 300 can be a herringbone mist eliminator that adheres to the droplets entrained in the mixed fluid. The gas phase of the mixed fluid can be sucked by the fan 314 and discharged as a lean CO2 gas (e.g., a product stream) through the lean CO2 gas outlet 304. It may be beneficial that the lean CO2 gas outlet 304 is positioned to discharge the lean CO2 gas, or is positioned to guide the lean CO2 gas away from the gas inlet of the ejector 302 and away from the gas inlet of any adjacent ejector. For example, the lean CO2 gas outlet 304 can be positioned to guide the lean CO2 gas toward the ground, thereby avoiding the lean CO2 gas from entering the gas inlet of any adjacent gas-liquid contactor unit.

[0168] The injectors 302 may be linearly aligned with one another on the capture solution tank 306. Similarly, the lean CO2 gas outlets 304 may be linearly aligned with one another on the capture solution tank 306. Each injector 302 may be positioned opposite a corresponding lean CO2 gas outlet 304 and may be fluidly coupled to the corresponding lean CO2 gas outlet 304. For example, injector 302a is fluidly coupled to the lean CO2 gas outlet 304a and is positioned opposite the lean CO2 gas outlet 304a. In an alternative embodiment, the injectors 302 may be staggered such that only certain injectors are aligned (e.g., injector 302a is aligned with injector 302c, but not with injector 302b). Although Figure 3 A linear arrangement is illustrated, but there may be embodiments in which the linear alignment of the ejectors 302 and / or the CO2-lean gas outlet 304 is not perfect. In some embodiments, the linear gas liquid contactor system 300 may include six ejectors 302, such as Figure 3 However, other embodiments are possible in which the linear gas liquid contactor system 300 includes more or less than six ejectors 302.

[0169] The ejectors 302 may also be fluidly coupled to each other via a capture solution distribution line 310. This may be useful if one or more ejectors 302 are unused, as the capture solution distribution line 310 may include one or more valves that are manually or automatically controlled to cause the lean capture solution 316 to bypass the unused ejectors 302. For example, a valve along the capture solution distribution line 310 and fluidly coupled to a particular unused ejector 302 may be closed to prevent the lean capture solution 316 from entering the unused ejector 302. The capture solution tank 306 includes an inlet that is operable to receive a make-up water flow 320, a make-up capture solution flow 322, or a combination of both, in order to maintain a specific lean capture solution concentration (e.g., a molar concentration of KOH ranging from less than 1 molar to about 6 molar, or a molar concentration of NaOH ranging from less than 1 molar to about 6 molar) or to adjust for evaporation losses. The make-up capture solution 322 may compensate for dilution from the intake water or for capture solution losses that may occur. In some embodiments, examples of these embodiments are provided in Figure 3 In the embodiment, the linear gas liquid contactor system 300 has a single capture solution tank 306 positioned below the outlets of all ejectors 302. In such an embodiment, the capture solution tank 306 is common to all ejectors 302, such that the rich capture solutions 318 from all ejectors 302 are mixed within the capture solution tank 306. In an alternative embodiment, the linear gas liquid contactor system 300 has a plurality of capture solution tanks 306, wherein at least one capture solution tank 306 is fluidly separated from at least another capture solution tank 306.

[0170] In some cases, at least one of the lean capture solution 316, the rich capture solution 318, and the make-up capture solution 322 may include a rate-increasing additive that can increase the CO2 capture rate, such as piperazine, carbonic anhydrase, MEA, and DEA. The rate-increasing additive may move freely in the capture solution within the linear gas liquid contactor system 300. The rate-increasing additive may be injected upstream of the capture solution circulation pump 308 or downstream of the stream 332. For example, the rate-increasing additive may be injected into the capture solution tank 306 and combined with the rich capture solution in the capture solution tank 306. In another example, the rate-increasing additive may be injected into the capture solution inlet of the ejector 302 and combined with the lean capture solution in the ejector 302. In another example, the rate-increasing additive may be injected into the capture solution distribution line 310. In some cases, the rate-increasing additive may be fixed in a capsule that moves freely in the capture solution within the linear gas liquid contactor system 300. In embodiments where the rate-increasing additive is free to move, the rate-increasing additive can be contained within the linear gas liquid contactor system 300 and prevented from flowing to the regeneration system 312 by a barrier or filtration system. In some cases, it may be advantageous for the linear gas liquid contactor system 300 to have multiple wetted surfaces coated with a rate-increasing material. The rate-increasing material may include a rate-increasing additive, such as a catalyst or a promoter, that is stabilized on a solid support by an immobilization method. For example, the ejector 302 and the capture solution tank 306 may each have a wetted surface coated with a rate-increasing material. In particular, the inner walls and components of the linear gas liquid contactor system 300 may be coated with a rate-increasing additive. In some applications, a combination of a freely moving rate-increasing additive in the capture solution and a rate-increasing material coated on a surface within the gas liquid contactor can be used to improve CO2 uptake.

[0171] In some applications, it may be beneficial that the ejector 302 is as large as practical. For example, some catalog ejectors may be up to 36 feet in height and up to 96 inches in inlet diameter, but larger custom units may be designed and manufactured. In some embodiments, the linear gas liquid contactor system 300 may be at least partially composed of caustic compatible materials such as thermoplastics, thermosetting resins, stainless steel, or a combination thereof. Some examples of suitable thermoplastics include polyvinyl chloride (PVC), chlorinated polyvinyl chloride (CPVC), polytetrafluoroethylene (PTFE). Examples of suitable thermosetting resins are vinyl esters based on brominated bisphenol A.

[0172] In some embodiments, the linear gas liquid contactor system 300 can be communicatively coupled to and controlled by a control system 999 .

[0173] Figure 44 is an isometric view of an exemplary perimeter gas-liquid contactor system 400. The perimeter gas-liquid contactor system 400 includes Figure 3 For the sake of brevity, the following Figure 4 Some previously described functions and embodiments applicable to both the linear gas liquid contactor system 300 and the peripheral gas liquid contactor system 400 will be omitted in the description.

[0174] The peripheral gas liquid contactor system 400 includes a set of ejectors 402a, 402b, 402c, 402d, 402e, 402f, 402g (collectively and individually referred to as ejectors 402), which are fluidly coupled to the lean CO2 gas outlet 404. The ejectors 402 and the vent pipe 444 are mechanically and fluidly coupled to the capture solution tank 406. The ejectors 402 can be fixed to or removably attached to the capture solution tank 406. The removably attached ejectors 402 can be rotated or oriented toward the dominant wind flow, thereby reducing the energy required to deliver a large amount of air to the gas inlet. The vent pipe 444 accommodates the lean CO2 gas outlet 404, which is fluidly coupled to the fan 414 and the demister 440.

[0175] The peripheral gas-liquid contactor system 400 may include Figure 1 Gas liquid contactor unit 100 or Figure 2 At least some of the components of the supplementary gas-liquid contactor unit 200 of the present invention. Therefore, the description of the gas-liquid contactor unit 100 and the description of the supplementary gas-liquid contactor unit 200, as well as the description of all features and advantages associated with the gas-liquid contactor unit 100 and the description of all features and advantages associated with the supplementary gas-liquid contactor unit 200, are applicable to the ejector 402 and to the peripheral gas-liquid contactor system 400 after the necessary changes. The ejectors 402 can each include a gas inlet, a capture solution inlet, and a mixing zone, the gas inlet being operable to receive a gas containing CO2, the capture solution inlet being operable to receive a lean capture solution from the capture solution distribution line 410, and turbulent mixing of the gas and the lean capture solution occurring in the mixing zone. The turbulent mixing enables CO2 from the gas to be absorbed to form a rich capture solution and a CO2-lean gas, which includes a lower concentration of CO2 than the gas received by the ejector 402. In some cases, at least some of ejectors 402 may have multiple gas inlets facing different angles and may be operable to be shielded, closed, or covered if not facing the dominant wind direction.

[0176] The lean capture solution 416 is reacted with the CO2 in the gas to form a mixed fluid having a gas phase and a liquid phase. As the reaction proceeds throughout the peripheral gas-liquid contactor system 400, the hydroxide concentration [OH- ] and the CO2 concentration in the gas phase of the mixed fluid decreased, while the carbonate concentration [CO3 2- ]Increase.

[0177] The ejector 402 is fluidly coupled to the capture solution tank 406. The rich capture solution flows from the ejector 402 to the capture solution tank 406. In one embodiment, an intervening mixing chamber (e.g., a static mixer) is fluidly coupled to the ejector 402 and the capture solution tank 406, such as Figure 2 The mixing chamber 238 in the supplemental gas liquid contactor unit 200. In this embodiment, further mixing of CO2 with any unreacted lean capture solution 416 can promote the reaction to form a mixed fluid. The reaction is carried out in the mixing chamber so that [OH - ] and the CO2 concentration in the gas phase of the mixed fluid decreased, while the [CO3 2- ]Increase.

[0178] In some cases, the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ] can be higher than the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ]. For example, if the [CO3 2- ] and [OH - ] is less than about 0.4, then the [CO3 2- ] and [OH - ] can be greater than about 0.5.

[0179] The capture solution circulation pump 408 is fluidly coupled to the capture solution tank 406. The capture solution circulation pump 408 pumps a rich capture solution 418 out of the capture solution tank 406. A first portion of the rich capture solution 418 is pumped to the regeneration system 412. A second portion of the rich capture solution 418 is combined with the regenerated capture solution 432 to form a lean capture solution 416, which is circulated to the ejector 402 via the capture solution distribution line 410. In some embodiments, the flow rate of the lean capture solution 416 in the capture solution distribution line 410 may be varied based on a target amount of captured CO2. In one embodiment, the first portion of the rich capture solution 418 pumped to the regeneration system 412 is greater than the second portion of the rich capture solution 418 that is combined with the regenerated capture solution 432 to form the lean capture solution 416.

[0180] In some embodiments, the capture solution tank 406 includes two outlets, each outlet fluidly coupled to a respective pump. For example, the first outlet can discharge a first portion of the rich capture solution 418 to the first pump, which causes the first portion of the rich capture solution 418 to flow to the regeneration system 412, and the second outlet can discharge a second portion of the rich capture solution 418, which is then combined with the regenerated lean solution 432 flowing from the regeneration system 412 to form the lean capture solution 416. The lean capture solution 416 then flows to the ejector 402 via the second pump.

[0181] The regeneration system 412 may include a lime causticization system such as Figure 6 causticizing system 640 to form a regenerated capture solution 432. In one embodiment, the regeneration system 412 includes an electrochemical treatment system operable to generate a carbon product. For example, the regeneration system 412 may include one or more of the components described in U.S. Patent No. 8,871,008, U.S. Patent No. 8,119,091, and U.S. Patent Application Publication No. 2022 / 0362707A1, such as a membrane separation unit for separating a dissolved target substance, such as CO2, from a buffer substance in an aqueous stream.

[0182] The liquid phase of the mixed fluid may be collected in capture solution tank 406 and combined with rich capture solution 418. The reaction of lean capture solution 416 with CO2 in the gas entering the gas inlet of ejector 402 may continue within capture solution tank 406 to promote the reaction to form a mixed fluid.

[0183] The reaction is carried out in the capture solution tank 406, so that [OH - ] and the CO2 concentration in the gas phase of the mixed fluid decreased, while the [CO3 2- ] increases. The liquid phase of the mixed fluid is collected in the capture solution tank 406 as it is formed. The gas phase of the mixed fluid is drawn from the capture solution tank 406 into one or more ventilation pipes by the fan 414.

[0184] In some embodiments, the fan 414 is an induced draft fan. The capture solution tank 406 is mechanically coupled to the vent 444, which contains Figure 2Some of the same parts of the ventilation pipe 244 of the ventilation pipe 444. In the illustrated embodiment, the ventilation pipe 444 accommodates the demister 440 upstream of the fan 414. The demister 440 can be a herringbone demister, which adheres to the droplets entrained in the mixed fluid. The demister 440 is an optional feature of the ventilation pipe 444, because other embodiments of the ventilation pipe 444 do not have a demister 440. The gas phase of the mixed fluid can be sucked upward by the fan 414 and discharged through the lean CO2 gas outlet 404 as lean CO2 gas (e.g., product flow). It may be beneficial that the lean CO2 gas outlet 404 is positioned to discharge the lean CO2 gas, or is positioned to guide the lean CO2 gas away from the gas inlet of the ejector 402 and away from the gas inlet of any adjacent gas-liquid contactor system. For example, the lean CO2 gas outlet 404 can be positioned to guide the lean CO2 gas toward the ground, thereby avoiding the lean CO2 gas from entering the gas inlet of any adjacent gas-liquid contactor unit.

[0185] In one embodiment, the vent 444 houses a packed bed absorber column positioned upstream of the blower 414, similar to the packed bed absorber column 242 of the supplemental gas liquid contactor unit 200. The packed bed absorber column may include structured packing or loose (bulk) packing and may have a similar Figure 2 The same features of the packed bed absorber column 242 of the embodiment of the present invention. In some embodiments, the regenerated capture solution 432 is not combined into the lean capture solution 416, but can be directed to flow through the packed bed absorber column to absorb residual CO2 in the mixed fluid that is not absorbed by the ejector 402 or upstream components (such as a mixing chamber). In one embodiment, the vent line 444 may include an air cooler operable to receive and discharge refrigerant. The air cooler can be positioned upstream of the demister 440 to reduce the temperature of the mixed fluid, allowing the demister 440 to remove more droplets entrained in the mixed fluid.

[0186] The ejector 402 is positioned at the periphery of the capture solution tank 406 and is fluidly coupled to the CO2 lean gas outlet 404 via the capture solution tank 406. Figure 4 , the ejectors 402 are circumferentially spaced from each other and are arranged circumferentially around the vent tube 444. The vent tube 444 is positioned at the center of the circumferential arrangement of the ejectors 402. The capture solution distribution line 410 has a ring-like shape for distributing the lean capture solution 416 to the ejectors 402. Other arrangements of the ejectors 402 are possible (see, e.g., Figure 3 and 5). Capture solution tank 406 is illustrated as being cylindrical, having a circular cross-section. In other embodiments, capture solution tank 406 may be other shapes, and ejectors 402 may be positioned at the periphery. For example, capture solution tank 406 may have a rectangular, elliptical, or polygonal cross-section, and ejectors 402 may be positioned near one or more edges of capture solution tank 406. In one embodiment, capture solution tank 406 may have a different top surface (e.g., a conical top surface, where vent tube 444 is elevated at a higher height than ejectors 402). Although Figure 4 One vent pipe 444 and seven ejectors 402 are illustrated, but the perimeter gas liquid contactor system 400 may include multiple vent pipes 444 and / or a different number of ejectors 402. For example, the perimeter gas liquid contactor system 400 may include two vent pipes 444 located in the center of the capture solution tank 406, which are surrounded by eight ejectors 402 located at the perimeter. In some embodiments, examples of these embodiments are provided in Figure 4 In the embodiment, the peripheral gas liquid contactor system 400 has a single capture solution tank 406 positioned below the outlets of all ejectors 402. In such an embodiment, the capture solution tank 406 is common to all ejectors 402, such that the rich capture solution 418 from all ejectors 402 mixes within the capture solution tank 406. In an alternative embodiment, the peripheral gas liquid contactor system 400 has a plurality of capture solution tanks 406, wherein at least one capture solution tank 406 is fluidly separated from at least another capture solution tank 406.

[0187] The ejectors 402 may also be fluidly coupled to each other via the capture solution distribution line 410. This may be useful if one or more ejectors 402 are unused, as the capture solution distribution line 410 may include one or more valves that are manually or automatically controlled to allow the lean capture solution 416 to bypass the unused ejectors 402. For example, a valve fluidly coupling the unused ejectors 402 to the capture solution distribution line 410 may be closed to prevent the lean capture solution 416 from being provided to the unused ejectors 402.

[0188] The capture solution tank 406 includes an inlet operable to receive a make-up water stream 420, a make-up capture solution stream 422, or a combination of both, in order to maintain a specific lean capture solution 416 concentration or adjust for evaporation losses. The make-up capture solution 422 can compensate for dilution from the intake water or possible capture solution losses. The peripheral gas liquid contactor system 400 can be at least partially composed of caustic compatible materials such as thermoplastics, thermosetting resins, stainless steel, or combinations thereof. Some examples of suitable thermoplastics include polyvinyl chloride (PVC), chlorinated polyvinyl chloride (CPVC), polytetrafluoroethylene (PTFE). Examples of suitable thermosetting resins are vinyl esters based on brominated bisphenol A.

[0189] In some cases, at least one of the lean capture solution 416, the rich capture solution 418, and the make-up capture solution 422 may include a rate-increasing additive that can increase the CO2 capture rate, such as piperazine, carbonic anhydrase, MEA, and DEA. The rate-increasing additive can move freely in the capture solution within the peripheral gas liquid contactor system 400. In some cases, the rate-increasing additive can be fixed in a capsule that moves freely in the capture solution within the peripheral gas liquid contactor system 400. The rate-increasing additive can be injected upstream of the capture solution circulation pump 408 or downstream of the regenerated capture solution 432. For example, the rate-increasing additive can be injected into the capture solution tank 406 and combined with the rich capture solution in the capture solution tank 406. In another example, the rate-increasing additive can be injected into the capture solution inlet of the ejector 402 and combined with the lean capture solution in the ejector 402. In another example, the rate-increasing additive can be injected into the capture solution distribution line 410. In an embodiment where the rate-enhancing additive is free to move, the rate-enhancing additive can be contained within the peripheral gas liquid contactor system 400 and prevented from flowing to the regeneration system 412 by a barrier or filtration system. In some cases, it may be advantageous for the peripheral gas liquid contactor system 400 to have multiple wetted surfaces coated with rate-enhancing materials. The rate-enhancing material can include a rate-enhancing additive, such as a catalyst or a promoter, that is stabilized on a solid support by an immobilization method. For example, the ejector 402, the capture solution tank 406, and the vent pipe 444 can each have a wetted surface coated with a rate-enhancing material. In particular, the inner walls and components of the peripheral gas liquid contactor system 400 can be coated with a rate-enhancing material agent. In some applications, a combination of a freely moving rate-enhancing additive in the capture solution and a rate-enhancing material coated on a surface within the gas liquid contactor can be used to improve CO2 uptake.

[0190] In some embodiments, the peripheral gas liquid contactor system 400 can be communicatively coupled to and controlled by a control system 999.

[0191] Figure 5 is an isometric view of an exemplary multi-row gas liquid contactor system 500. The multi-row gas liquid contactor system 500 includes Figure 4 Some of the same or similar components of the peripheral gas-liquid contactor system 400 and Figure 3 For the sake of brevity, the following Figure 5 The description of Figure 3 Some of the previously described functions and embodiments of the linear gas liquid contactor system 300, the peripheral gas liquid contactor system 400, and the multi-row gas liquid contactor system 500.

[0192] The multi-row gas liquid contactor system 500 includes a group of ejectors 502a, 502b, 502c, 502d, 502e, 502f, 502g, 502h, 502i, 502j (collectively and individually referred to as ejectors 502) that are fluidly coupled to a CO2-lean gas outlet 504. In the illustrated embodiment, the first ejector row includes ejectors 502a and 502b, the second ejector row includes ejectors 502c and 502j, the third ejector row includes ejectors 502d and 502i, the fourth ejector row includes ejectors 502e and 502h, and the fifth ejector row includes ejectors 502f and 502g. The ejectors 502 and the vent 544 are mechanically and fluidly coupled to the capture solution tank 506. The vent 544 houses a fan 514 that is fluidly coupled to the CO2-lean gas outlet 504. The ejectors 502 may be fixed to or removably attached to the capture solution tank 506. The ejectors 502 removably attached to the capture solution tank 506 may be rotated or oriented toward the dominant wind flow, thereby reducing the energy required to deliver a large volume of air into the gas inlet. In some cases, at least some of the ejectors 502 have multiple gas inlets facing different angles and are operable to be shielded, closed, or covered if not facing the dominant wind direction.

[0193] The multi-row gas liquid contactor system 500 may include Figure 1 Gas liquid contactor unit 100 or Figure 2At least some of the components of the supplemental gas liquid contactor unit 200 of the present invention. Therefore, the description of the gas liquid contactor unit 100 and the description of the supplemental gas liquid contactor unit 200, as well as the description of all features and advantages associated with the gas liquid contactor unit 100 and the description of all features and advantages associated with the supplemental gas liquid contactor unit 200, apply mutatis mutandis to the ejector 502 and to the multi-row gas liquid contactor system 500. The ejectors 502 can each include a gas inlet operable to receive a gas containing CO2, a capture solution inlet operable to receive a lean capture solution 516 from the capture solution distribution line 510, and a mixing zone in which turbulent mixing of the gas and the lean capture solution 516 occurs. The turbulent mixing allows CO2 from the gas to be absorbed to form a mixed fluid having a gas phase and a liquid phase.

[0194] The lean capture solution 516 is reacted with the CO2 in the gas to form a mixed fluid having a gas phase and a liquid phase. As the reaction proceeds throughout the multi-row gas-liquid contactor system 500, the hydroxide concentration [OH - ] and the CO2 concentration in the gas phase of the mixed fluid decreased, while the carbonate concentration [CO3 2- In some cases, the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ] can be higher than the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ]. For example, if the [CO3 2- ] and [OH - ] is less than about 0.4, then the [CO3 2- ] and [OH - ] can be greater than about 0.5.

[0195] The ejector 502 is fluidly coupled to the capture solution tank 506. The mixed fluid flows from the ejector 502 to the capture solution tank 506. In one embodiment, an intervening mixing chamber (e.g., a static mixer) is fluidly coupled to the ejector 502 and the capture solution tank 506, such as Figure 2 In this embodiment, further mixing of CO2 with any unreacted lean capture solution can promote the reaction to form a mixed fluid. The reaction is carried out in the mixing chamber so that [OH - ] and the CO2 concentration in the gas phase of the mixed fluid decreased, while the [CO32- In some cases, at least some of the ejectors 502 may have multiple gas inlets facing different angles and may be operable to be shielded, closed, or covered if not facing the dominant wind direction.

[0196] In the illustrated embodiment, the capture solution tank 506 includes a first outlet for a first portion 518 of the rich capture solution and a second outlet for a second portion 519 of the rich capture solution. The second portion 519 of the rich capture solution and the first portion 518 of the rich capture solution can be similar in chemical composition but different in flow rate, temperature, and / or pressure. The first portion 518 of the rich capture solution is pumped to the regeneration system 534 via the rich capture solution pump 524. In some embodiments, the regeneration system 534 may include a lime causticizing system and a calciner, such as Figure 6 The regeneration system 534 may include an electrochemical treatment system. The second portion 519 of the rich capture solution may be combined with the regenerated capture solution 532 to form a lean capture solution 516 that is circulated back to the ejector 502 via the circulation pump 508 and the capture solution distribution line 510.

[0197] In other embodiments, the capture solution tank 506 includes only one outlet for the rich capture solution. For example, the rich capture solution may exit the single outlet of the capture solution tank, be pumped using a circulation pump, and then be split into a first stream and a second stream, the first stream being pumped to the regeneration system 534, and the second stream being combined with the regenerated capture solution 532 to form the lean capture solution 516.

[0198] The liquid phase of the mixed fluid may be collected in capture solution tank 506 and combined with first portion 518 of rich capture solution and second portion 519 of rich capture solution. The reaction of lean capture solution 516 with CO2 in the gas entering the gas inlet of ejector 502 may continue within capture solution tank 506 to promote the reaction to form the mixed fluid.

[0199] The reaction is carried out in the capture solution tank 506, so that [OH - ] and the CO2 concentration in the gas phase of the mixed fluid decreased, while the [CO3 2- ] increases. The liquid phase of the mixed fluid is collected in the capture solution tank 506 as it is formed. The gas phase of the mixed fluid is drawn from the capture solution tank 506 into one or more ventilation pipes by the fan 514.

[0200] In some embodiments, the fan 514 is an induced draft fan. The capture solution tank 506 is mechanically and fluidly coupled to the vent duct 544, which includes a Figure 2In one embodiment, the vent 544 houses a packed bed absorber column positioned upstream of the blower 514, similar to the packed bed absorber column 242 of the supplemental gas liquid contactor unit 200. The packed bed absorber column may include structured packing or loose (bulk) packing and may have the same Figure 2 The same or similar features of the packed bed absorption column 242 of the invention. In some embodiments, the regenerated capture solution 532 is not mixed with the second portion 519 of the rich capture solution, but the regenerated capture solution 532 can be directed to flow through the packed bed absorption column to absorb at least a portion of any remaining CO2 in the mixed fluid that was not absorbed by the ejector 502, the capture solution tank 506, or an upstream unit (such as a mixing chamber) in the countercurrent reaction. In one embodiment, the vent duct 544 accommodates an optional demister (e.g., similar to the demister 440 of the peripheral gas-liquid contactor system 400) upstream of the fan 514. The demister can be a herringbone demister that adheres to droplets entrained in the mixed fluid. The gas phase of the mixed fluid can be drawn upward by the fan 514 and discharged through the lean CO2 gas outlet 504 as a lean CO2 gas (e.g., a product stream). It may be beneficial for the lean CO2 gas outlet 504 to be positioned to discharge the lean CO2 gas, or to be positioned to direct the lean CO2 gas away from the gas inlet of the ejector 502 and away from the gas inlet of any adjacent gas-liquid contactor system. For example, the lean CO2 gas outlet 504 can be positioned to direct the lean CO2 gas toward the ground, thereby avoiding the lean CO2 gas from entering the gas inlet of any adjacent gas-liquid contactor unit.

[0201] The ejectors 502 are positioned in a row on the capture solution tank 506 and are fluidly coupled to the CO2-lean gas outlet 504 via the capture solution tank 506. In embodiments where a multi-row gas liquid contactor system 500 is used to capture CO2 from air, at least some of the ejectors 502 can be oriented toward the prevailing wind to take advantage of increased gas (air) flow.

[0202] The multi-row gas liquid contactor system 500 is illustrated as including two rows of five ejectors 502 (or five rows of two ejectors 502) and one vent 544, which is fluidly and mechanically coupled to the capture solution tank 506. In other embodiments, the multi-row gas liquid contactor system 500 can include rows containing more or less than two or five ejectors 502 per row, and in some cases, the multi-row gas liquid contactor system 500 can include more than two rows of ejectors 502. In some embodiments, the multi-row gas liquid contactor system 500 can include more than one vent 544. For example, the multi-row gas liquid contactor system 500 can include two rows of six ejectors 502, an intervening row of five ejectors 502, and two vents 544. The number and orientation of ejectors 502 and vent tubes 544 in the multi-row gas liquid contactor system 500 can be selected based on wind direction, prevailing wind speed, target amount of CO2 captured, footprint size limitations, structural limitations of the capture solution tank 506, or a combination thereof.

[0203] The ejectors 502 are fluidly coupled to each other via a capture solution distribution line 510. This may be useful if one or more ejectors 502 are unused, as the capture solution distribution line 510 may include one or more valves that are manually or automatically controlled to allow lean capture solution 516 to bypass the unused ejectors 502. For example, a valve that fluidly couples the unused ejectors 502 to the capture solution distribution line 510 may be closed to prevent lean capture solution 516 from being provided to the unused ejectors 502. In some embodiments, the flow rate of lean capture solution in the capture solution distribution line 510 may vary based on a target amount of captured CO2. The capture solution tank 506 includes an inlet that is operable to receive a make-up water flow 520, a make-up capture solution flow 522, or a combination of both, in order to maintain a specific lean capture solution 516 concentration or adjust for evaporation losses. The make-up capture solution 522 may compensate for dilution from the intake water or possible capture solution losses. The multi-row gas liquid contactor system 500 may be constructed at least in part of a caustic compatible material such as a thermoplastic, a thermosetting resin, stainless steel, or a combination thereof. Some examples of suitable thermoplastics include polyvinyl chloride (PVC), chlorinated polyvinyl chloride (CPVC), polytetrafluoroethylene (PTFE).An example of a suitable thermosetting resin is brominated bisphenol A based vinyl ester.

[0204] In some cases, at least one of the lean capture solution 516, the first portion 518 of the rich capture solution, the second portion 519 of the rich capture solution, the compensating capture solution 522, and the regenerated capture solution 532 may contain a rate-enhancing additive, such as piperazine, carbonic anhydrase, MEA, and DEA. The rate-enhancing additive may be free to move in the capture solution, or may be fixed in a capsule that moves freely in the capture solution. In an embodiment where the rate-enhancing additive moves freely, the rate-enhancing additive may be contained within the multi-row gas-liquid contactor system 500 and prevented from flowing to the regeneration system 534 by a barrier or filtration system. In some cases, it may be advantageous for the multi-row gas-liquid contactor system 500 to have multiple wetted surfaces coated with a rate-enhancing material. The rate-enhancing material may include a rate-enhancing additive, such as a catalyst or a promoter, that is stabilized on a solid support by an immobilization method. For example, the ejector 502, the capture solution tank 506, and the vent pipe 544 may each have a wetted surface coated with a rate-enhancing material. In some applications, a combination of freely mobile rate-enhancing additives in the capture solution and rate-enhancing materials coated on surfaces within the gas liquid contactor can be used to improve CO 2 uptake.

[0205] In some embodiments, the multi-row gas liquid contactor system 500 can be communicatively coupled to and controlled by a control system 999 .

[0206] Figure 6 6 is a block flow diagram illustrating an exemplary integrated gas capture system 600 including a gas-liquid contactor system 660 fluidly coupled to a regeneration system 638. In the gas-liquid contactor system 660, an ejector 602 receives a gas 612 containing a dilute concentration of CO2. The gas 612 may include other components such as N2, O2, and impurities. The ejector 602 reacts the CO2 in the gas 612 by mixing it with a lean capture solution 614 to form a first mixed fluid 619 having a gas phase and a liquid phase.

[0207] The reaction of the lean capture solution 614 with CO 2 is carried out in the ejector 602 so that the hydroxyl concentration [OH - ] and the CO2 concentration in the gas phase of the first mixed fluid 619 is reduced, while the carbonate concentration [CO3 2- The ejector 602 discharges the first mixed fluid 619 into the capture solution tank 604.

[0208] In one embodiment, mixing may be supplemented by a mixing chamber downstream of the ejector 602. For example, a static mixer positioned downstream of the ejector 602 may increase turbulent mixing to further react the gas 612 with the lean capture solution 614 in the first mixed fluid 619. In some embodiments, the rich capture solution 620 and the lean capture solution 614 may each include different ratios of KOH, K2CO3, KHCO3, NaOH, Na2CO3, H2O, or combinations thereof. In some cases, the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ] can be higher than the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ]. For example, if the [CO3 2- ] and [OH - ] is less than about 0.4, then the [CO3 2- ] and [OH - ] can be greater than about 0.5.

[0209] The first mixed fluid 619 is discharged from the ejector 602 into the capture solution tank 604. The capture solution tank 604 collects the liquid phase of the first mixed fluid 619. The reaction of the lean capture solution 614 with the CO2 in the gas 612 is further performed in the capture solution tank 604 to form a second mixed fluid 623 having a gas phase and a liquid phase. The reaction is performed in the capture solution tank 604, so that [OH - ] and the CO2 concentration in the gas phase of the second mixed fluid 623 are both reduced, while the [CO3 2- ] increases. The liquid phase of the second mixed fluid 623 is collected in the capture solution tank 604 as it is formed. The gas phase of the second mixed fluid 623 is sucked from the capture solution tank 604 by the fan 634. The fan 634 causes the gas phase of the second mixed fluid 623 to flow to the CO2-lean gas outlet 636, where the CO2-lean gas 616 is discharged as a product stream.

[0210] In one embodiment, the second mixed fluid 623 is discharged from the capture solution tank 604 to a packed bed absorber column. The packed bed absorber column can accommodate structured packing or loose packing. In some embodiments, the regenerated capture solution 632 is sent directly to the top of the packed bed absorber column from the regeneration system 638. The countercurrent flow of the second mixed fluid 623 and the regenerated capture solution 632 enables further capture of CO2. In such an embodiment, at least a portion of the unreacted CO2 in the ejector 602 can be removed by reacting with the regenerated capture solution 632.

[0211] In one embodiment, the integrated dilution gas capture system 600 is used to employ a Benfield process where K2CO3 is used to remove acid gases, including CO2. For example, if the downstream unit is configured to employ a Benfield process according to the reaction of Eq. 5 (e.g., if the regeneration system includes a steam stripper), the integrated dilution gas capture system 600 can be used to perform a Benfield process where K2CO3 is used to remove acid gases, including CO2. The regeneration tower can be configured to process a bicarbonate solution.

[0212] In one embodiment, the second mixed fluid 623 is drawn from the capture solution tank 604 to a demister that captures droplets entrained in the second mixed fluid 623 before being discharged as the CO 2 lean gas 616 at the CO 2 lean gas outlet 636 .

[0213] Rich capture solution 620 is collected in capture solution tank 604. A first portion 622a of rich capture solution 620 is pumped to an exemplary regeneration system 638, and a second portion 622b of rich capture solution 620 is combined with regenerated capture solution 632 to form lean capture solution 614. Regeneration system 638 includes lime causticizing system 640 and calciner 642.

[0214] In some embodiments, the lime causticizing system 640 comprises a mixed tank reactor in which the causticizing reaction and the digestion reaction occur simultaneously in the same reactor. For example, the potassium-based reactions defined by Eq. 2 and Eq. 3 can occur simultaneously in a mixed tank reactor. The digestion reaction produces hydrated lime (Ca(OH)2) by the reaction of water with quicklime CaO. The causticizing reaction produces a concentrated carbon stream, such as a CaCO3 solid stream 650, and a regenerated capture solution 632 from the reactants i) carbonates in the first portion of the rich capture solution 620 and ii) hydrated lime Ca(OH)2. For example, the potassium-based reactions defined by Eq. 2 and Eq. 3 can occur simultaneously in a mixed tank reactor.

[0215] In some embodiments, the lime causticizing system 640 includes a pellet reactor fluidly coupled to a slaked lime. In this embodiment, the causticizing reaction (e.g., Eq. 2) occurs in the pellet reactor and the digestion reaction (e.g., Eq. 3) occurs in the slaked lime. In the slaked lime, water reacts with quicklime to produce hydrated lime, which is sent to the pellet reactor. A first portion 622a of the rich capture solution 620 reacts with the hydrated lime in the pellet reactor to produce CaCO3 solids and a regenerated capture solution 632. In some embodiments, the pellet reactor forms CaCO3 solids in the form of pellets and fine particles. The fine particles of CaCO3 can be separated in a filtration system downstream of the lime causticizing system 640.

[0216] The CaCO3 solid stream 650 is transferred to a calciner 642, and the regenerated capture solution 632 is sent to a gas liquid contactor system 660. The calciner 642 calcines the CaCO3 solids using a high temperature calcination process, thereby releasing a CO2-rich gas stream (such as CO2 stream 648) and forming a quicklime (CaO solid) stream 646. In some embodiments, the calciner 642 can be an electric calciner driven by a power generation system. In some embodiments, the calciner 642 can be an oxy-combustion calciner that is operable to receive an oxygen stream to combust with a fuel (such as natural gas, hydrogen, biogas, or biomethane) to produce a temperature high enough for calcination (e.g., 900°C). In other embodiments, the calciner can be a circulating fluidized bed calciner, a bubbling bed calciner, a rotary calciner, or a flash calciner. The CO2 stream 648 can include H2O, O2, N2, impurities, or a combination thereof. The CO2 stream 648 can be discharged from the regeneration system 638 and sent to a downstream unit or system for further processing. For example, the CO2 stream 648 can be further processed to remove at least some impurities (e.g., O2, water), and then compressed for downstream applications or pipeline transfer. Before or after processing, the CO2 stream 648 can flow from the calciner 642 in the product conduit 644 extending from the calciner 642. The product conduit 644 can be used to provide the CO2 stream 648 as a product stream or product gas for downstream applications, or as an independent product for export or as a raw material. In some embodiments, after processing to remove impurities, the CO2 stream 648 is provided as a substantially pure CO2 product stream for downstream applications, or is provided as an independent product for export or is provided as a raw material. In other embodiments of the regeneration system 638, the product conduit 644 is configured to provide different products. Non-limiting examples of products delivered via product conduit 644 in various embodiments of regeneration system 638 include carbon products such as CO, ethylene, fuels, methanol, hydrocarbons, and CaCO3 solids, and non-carbon products such as quicklime (CaO solids).

[0217] The quicklime stream 646 is transferred to the lime causticizing system 640. In one embodiment, the quicklime stream 646 is transferred to a slaked lime plant (which may be part of the lime causticizing system 640) where the CaO is hydrated to form hydrated lime Ca(OH)2 solid according to the reaction defined by Eq. 3 reproduced below.

[0218] CaO (s) +H2O (l) →Ca(OH) 2(s) (Eq.3)

[0219] In such an embodiment, the hydrated lime Ca(OH)2 solids may be further hydrated to form a slurry which is then transferred to a pellet reactor to form CaCO3 solids 650 and a regenerated capture solution 632 according to the reaction defined by Eq. 2 below:

[0220] K2CO 3(aq) +Ca(OH) 2(s) →2KOH aq +CaCO 3(s) (Eq.2)

[0221] The regenerated capture solution 632 is combined with the rich capture solution 620 from the capture solution tank 604 to form the lean capture solution 614 , which is returned to the ejector 602 .

[0222] In some embodiments, the lean capture solution 614 may further include a hydroxide reagent such as NaOH instead of KOH. In other embodiments, the lean capture solution 614 may include an amine-based CO2 capture reagent. In such cases, the regeneration system 638 may include a system other than the lime causticizing system 640 and the calciner 642 for forming the regenerated capture solution 632 and releasing CO2 648.

[0223] In one embodiment, the regeneration system 638 includes an electrochemical processing system operable to generate a carbon product. For example, the regeneration system 638 may include some of the components described in U.S. Patent No. 8,871,008; U.S. Patent No. 8,119,091; and U.S. Patent Application Publication No. 2022 / 0362707A1, such as a membrane separation unit for separating dissolved target substances, such as CO2, from buffer substances in an aqueous stream. In some embodiments, at least one of the lean capture solution 614, the rich capture solution 620, the compensation capture solution 618, and the regeneration capture solution 632 may include a rate-increasing additive that can increase the CO2 capture rate, such as piperazine, carbonic anhydrase, MEA, and DEA. The rate-increasing additive may be injected upstream of the capture solution circulation pump or downstream of the stream 632. For example, the rate-increasing additive may be injected into the capture solution tank 604 and combined with the rich capture solution in the capture solution tank 604. In another example, the rate-increasing additive may be injected into the capture solution inlet of the eductor 602 and combined with the lean capture solution in the eductor 602 .

[0224] The integrated dilution gas capture system 600 may include a gas-liquid contactor system 660 including a plurality of ejectors 602. For example, the gas-liquid contactor system 660 may include Figure 3 Linear gas-liquid contactor system 300, Figure 4 Peripheral gas-liquid contactor system 400 or Figure 5 The integrated gas capture system 600 may be communicatively coupled to and controlled by a control system 999 .

[0225] Figure 7 is a flow chart illustrating a method 700 for removing CO2 from a gas including a diluent gaseous source (such as atmospheric gas) according to at least one embodiment of the present disclosure. The method 700 includes steps 702-708, but in other embodiments, certain steps may be omitted and / or additional steps may be added. Steps 702-708 may be performed sequentially as shown or may be performed in a different order than the illustrated method.

[0226] At 702, a lean capture solution is flowed into a capture solution inlet of an ejector. A lean capture solution comprising KOH, K2CO3, H2O, NaOH, Na2CO3, or a combination thereof may be flowed into the ejector. In some cases, the lean capture solution may include a rate enhancing additive such as piperazine, carbonic anhydrase, MEA, or DEA. In some cases, the lean capture solution flows into the capture solution inlet of the ejector via a capture solution distribution line.

[0227] The lean captured solution at 702 is caused to flow to draw gas into the gas inlet of the ejector. The gas may be an atmospheric gas containing a dilute concentration of CO2. The gas is drawn into the gas inlet of the ejector via a venturi effect, which is achieved by using the lean captured solution as the motive fluid in the ejector. In some cases, the venturi effect of the motive fluid is supplemented by a fan (such as an induced draft fan) to draw the gas into the gas inlet. In some embodiments, the gas may include O2, H2O, N2, impurities, or combinations thereof. For example, the gas may contain a CO2 concentration between 300 ppm and 10,000 ppm. In some embodiments, the gas may include exhaust gas from an industrial process containing a CO2 concentration greater than 10,000 ppm, and may also include H2S, NO x , O2, impurities or a combination thereof.

[0228] At 704, the lean capture solution and the gas are mixed in a mixing zone within the ejector. The mixing may occur partially in the mixing zone and partially at the outlet of the ejector. The mixing zone of the ejector may be configured for turbulent mixing to promote the reaction of the lean capture solution with the CO2 in the gas. For example, the ejector may have a textured surface to increase turbulent mixing. Where a rate-enhancing additive is included in the lean capture solution, the rate-enhancing additive may catalyze or promote the reaction of the CO2 with the reagent in the lean capture solution.

[0229] The gas is reacted with the lean capture solution in the mixing zone. For example, some of the CO2 in the gas may react with the KOH or NaOH in the lean capture solution to form K2CO3 or Na2CO3, respectively. A portion of the gas may remain unreacted.

[0230] A mixed fluid is formed including a rich captured solution and a CO2-lean gas stream. The mixed fluid has a gas phase and a liquid phase. The mixed fluid may also include a lean captured solution and gas that was not reacted in the previous steps of method 700. As the reaction proceeds, in the mixed fluid, the concentrations of the rich captured solution and the CO2-lean gas increase, while the concentrations of the lean captured solution and the gas decrease. The mixed fluid may include some of the unreacted lean captured solution. The CO2-lean gas in the gaseous portion of the mixed fluid may include less CO2 than the gas in step 704. As subsequent steps proceed, the mixed fluid may be continuously formed. In some cases, the carbonate concentration [CO3 2- ] and hydroxide concentration [OH - ] can be higher than the carbonate concentration in the lean capture solution [CO3 2- ] and hydroxide concentration [OH - ]. For example, if the [CO3 2- ] and [OH -] is less than about 0.4, then the [CO3 2- ] and [OH - ] can be greater than about 0.5. In some cases, the rich capture solution or the lean capture solution can include a rate-enhancing additive, such as piperazine, carbonic anhydrase, MEA, or DEA. Where a rate-enhancing additive is included, the rate-enhancing additive can catalyze or promote the reaction of CO2 with a reagent in the rich capture solution or the lean capture solution.

[0231] At 706, the mixed fluid is flowed to a capture solution tank. In one embodiment, a previous step may be performed where the mixed fluid is flowed to a mixing chamber (e.g., a static mixer) to further react the CO2 remaining in the mixed fluid from the previous step of method 700 with at least some of the lean capture solution.

[0232] At 708, the CO2-lean gas of the mixed fluid is discharged, for example, from an outlet for the CO2-lean gas by operating a blower. The outlet for the CO2-lean gas can be positioned downstream of the blower. The CO2-lean gas can be the gas phase of the mixed fluid of 704. In one embodiment, the induced draft fan draws the gas phase of the mixed fluid from the capture solution tank. In some embodiments, the previous step can be performed in which the mixed fluid is caused to flow through a demister to remove droplets entrained in the mixed fluid. In some embodiments, the previous step can be performed in which the mixed fluid is caused to flow through a packed bed absorption column and react with a regenerated capture solution. In some embodiments, the packed bed absorption column can be designed for countercurrent absorption (e.g., the mixed fluid and the regenerated capture solution can flow in opposite directions as they react).

[0233] In some embodiments, method 700 includes further processing the rich capture solution to regenerate the rich capture solution. Figure 7 At 710, a first portion of the rich capture solution is flowed to a regeneration system. The regeneration system may include Figure 6 Regeneration system 638 or Figure 6 At least some of the same or similar components as any of the above-described embodiments of the regeneration system 638. For example, the regeneration system may include a lime causticizing system and a calciner, the lime causticizing system forming CaCO3 solids, and the calciner heating the pellets and releasing CO2. In one embodiment, the regeneration system may be an electrochemical regeneration system. In some embodiments, the regeneration system may include a membrane separation unit to separate, increase and / or purify the concentration of carbonaceous matter.

[0234] At 712, a regeneration capture solution is formed in the regeneration system. The regeneration capture solution may be formed using at least a first portion of the rich capture solution. For example, the first portion of the rich capture solution may be sent to a pellet reactor to form CaCO solids and a regeneration capture solution. In some cases, the regeneration capture solution may include a rate-enhancing additive such as piperazine, carbonic anhydrase, MEA, or DEA.

[0235] At 714, the regenerated trap solution is combined with a second portion of the rich trap solution to form a lean trap solution. For example, the regenerated trap solution may be combined with the rich trap solution to achieve a molar concentration of KOH in the lean trap solution ranging from less than 1 molar to about 6 molar. The lean trap solution may be returned to the ejector to repeat the method 700 starting at 702.

[0236] Optionally, method 700 includes the step of flowing a make-up capture solution, a make-up water flow, a rate-enhancing additive, or a combination thereof, to the ejector or capture solution tank. Each of the above steps can be modified to accommodate CO2 capture via a different chemical process. For example, a Benfield chemical process or an amine wash can replace the KOH-based reaction described in method 700.

[0237] The method 700 may include flowing a stream (e.g., mixed fluid, clean gas, rich capture solution, lean capture solution, regenerated capture solution) to at least one auxiliary unit or auxiliary equipment, such as a filtration system, storage tank, mixing tank, settler, clarifier, conveyor, or other unit that facilitates performance of the method 700. In the event that the gas carries pollutants such as NOx and SOx, the gas may be flowed through a pre-treatment unit prior to performing the method 700. For example, the gas may be flowed through an amine scrubber prior to step 704 of the method 700.

[0238] Figure 8 is a schematic diagram of a control system (or controller) 800 for a gas-liquid contactor system, which is used for Figure 1 and 2 The units 100 and 200 shown in and / or Figure 3-6 The system 800 may be used for the operations described in association with any of the previously described computer-implemented methods, such as as a control system 999 or other controllers described herein, or as a part of a control system 999 or other controllers described herein.

[0239] System 800 is intended to include various forms of digital computers, such as laptop computers, desktop computers, workstations, personal digital assistants, servers, blade servers, mainframes and other suitable computers. System 800 may also include mobile devices, such as personal digital assistants, cellular phones, smart phones and other similar computing devices. Additionally, the system may include portable storage media, such as a universal serial bus (USB) flash drive. For example, a USB flash drive may store operating systems and other applications. A USB flash drive may include input / output components, such as a wireless transmitter or a USB connector that may be inserted into a USB port of another computing device.

[0240] The system 800 includes a processor 810, a memory 820, a storage device 830, and an input / output device 840. Each of the components 810, 820, 830, and 840 is interconnected using a system bus 850. The processor 810 is capable of processing instructions for execution within the system 800. The processor can be designed using any of a variety of architectures. For example, the processor 810 can be a CISC (Complex Instruction Set Computer) processor, a RISC (Reduced Instruction Set Computer) processor, or a MISC (Minimum Instruction Set Computer) processor.

[0241] In one embodiment, the processor 810 is a single-threaded processor. In one embodiment, the processor 810 is a multi-threaded processor. The processor 810 is capable of processing instructions stored in the memory 820 or stored on the storage device 830 to display graphical information of the user interface on the input / output device 840.

[0242] The memory 820 stores information within the system 800. In one embodiment, the memory 820 is a computer readable medium. In one embodiment, the memory 820 is a volatile memory unit. In some embodiments, the memory 820 is a non-volatile memory unit.

[0243] The storage device 830 can provide mass storage for the system 800. In one embodiment, the storage device 830 is a computer-readable medium. In various embodiments, the storage device 830 can be a floppy disk device, a hard disk device, an optical disk device, or a tape device.

[0244] The input / output device 840 provides input / output operations for the system 800. In one embodiment, the input / output device 840 includes a keyboard and / or a pointing device. In some embodiments, the input / output device 840 includes a display unit for displaying a graphical user interface.

[0245] Certain features described may be implemented in digital electronic circuitry, or in computer hardware, firmware, software, or in a combination thereof. The apparatus may be implemented in a computer program product tangibly embodied in an information carrier, for example, in a machine-readable storage device executed by a programmable processor; and the method steps may be performed by a programmable processor executing a program of instructions to perform the functions of the described embodiments by operating on input data and generating output. The described features may advantageously be implemented in one or more computer programs executable on a programmable system comprising at least one programmable processor coupled to receive data and instructions from and transmit data and instructions to a data storage system, at least one input device, and at least one output device. A computer program is a set of instructions that can be used directly or indirectly in a computer to perform a specific activity or cause a specific result. Computer programs may be written in any form of programming language, including compiled or interpreted languages, and may be deployed in any form, including as a stand-alone program or as a module, component, subroutine, or other unit suitable for a computing environment.

[0246] Suitable processors for executing instruction programs include, for example, both general-purpose and special-purpose microprocessors, and the sole processor or one of multiple processors of any type of computer. Typically, the processor will receive instructions and data from a read-only memory or a random access memory or both. The basic components of a computer are a processor for executing instructions, and one or more memories for storing instructions and data. In general, a computer will also include one or more mass storage devices for storing data files, or be operably connected to communicate with the one or more mass storage devices; such devices include disks, such as internal hard disks and removable disks; magneto-optical disks; and optical disks. Storage devices suitable for tangibly embodying computer program instructions and data include all forms of non-volatile memory, including, for example, semiconductor memory devices, such as EPROM, EEPROM, and flash memory devices; disks, such as internal hard disks and removable disks; magneto-optical disks; and CD-ROM and DVD-ROM disks. The processor and memory may be supplemented by or incorporated into an ASIC (Application Specific Integrated Circuit).

[0247] To provide interaction with a user, these features can be implemented on a computer having a display device for displaying information to the user, such as a CRT (cathode ray tube) or LCD (liquid crystal display) monitor, and a keyboard and pointing device, such as a mouse or trackball, through which the user can provide input to the computer. In addition, such activities can be implemented via a touch screen flat panel display and other appropriate mechanisms.

[0248] These features can be implemented in a control system that includes a back-end component, such as a data server, or includes a middleware component, such as an application server or an Internet server, or includes a front-end component, such as a client computer, the client computer having a graphical user interface or an Internet browser, or any combination thereof. The components of the system can be connected by digital data communication (such as a communication network) in any form or medium. Examples of communication networks include local area networks ("LAN"), wide area networks ("WAN"), peer-to-peer networks (with self-organizing or static members), grid computing infrastructures, and the Internet.

[0249] A number of embodiments of the present disclosure have been described. However, it should be understood that various modifications may be made without departing from the spirit and scope of the present disclosure. Therefore, other embodiments fall within the scope of the following claims. In view of this description, further modifications and alternative embodiments of various aspects will be apparent to those skilled in the art. Therefore, this description is to be interpreted as being merely illustrative. It should be understood that the forms shown and described herein should be considered as examples of embodiments. Components and materials may replace the components and materials illustrated and described herein, parts and processes may be reversed, and certain features may be utilized independently, all of which will be apparent to those skilled in the art after having benefited from this description. Changes may be made to the components described herein without departing from the spirit and scope as described in the following claims.

Claims

1. A system for removing carbon dioxide from a gas, the system comprising: An injector, the injector comprising: a capture solution inlet operable to receive a lean capture solution; a gas inlet operable to receive a gas comprising carbon dioxide; a mixing zone configured to react the lean capture solution and the gas comprising carbon dioxide; and an ejector outlet operable to discharge a mixed fluid comprising a rich capture solution and a CO2-lean gas; a CO2 lean gas outlet, the CO2 lean gas outlet fluidly coupled to the ejector; a blower, the blower fluidly coupled to the CO2-lean gas outlet, the blower rotatable to discharge the CO2-lean gas from the CO2-lean gas outlet; as well as A capture solution tank is fluidly coupled to the ejector outlet and to the CO 2 lean gas outlet, the capture solution tank being configured to collect the rich capture solution. 2 . The system of claim 1 , further comprising a regeneration system fluidly coupled to the capture solution tank.

3. The system of claim 2, further comprising a capture solution distribution line fluidly coupled to the capture solution inlet of the ejector and to the regeneration system.

4. The system of claim 2, wherein the capture solution tank is fluidly coupled to the regeneration system via a capture solution circulation pump.

5. The system of claim 2, wherein the regeneration system comprises at least one of a lime causticizing system or a calciner.

6. The system of claim 5, wherein the lime causticizing system comprises at least one of a pellet reactor or a lime slaker.

7. The system of claim 5, wherein the calciner comprises an electric calciner.

8. The system of any one of claims 2 to 7, wherein the regeneration system has a product conduit configured to provide the carbon dioxide as a product gas.

9. The system of any one of claims 1 to 8, further comprising a demister fluidly coupled to the CO2 lean gas outlet.

10. The system of claim 9, wherein the mist eliminator comprises a chevron-shaped mist eliminator.

11. The system of claim 9, wherein the mist eliminator is positioned upstream of the blower.

12. The system of any one of claims 1 to 11, further comprising a mixing chamber fluidly coupled to the injector outlet.

13. The system of claim 12, wherein the mixing chamber comprises a static mixer.

14. The system of claim 12, wherein the mixing chamber comprises a coating of a rate enhancing material.

15. The system of any one of claims 12 to 14, wherein the mixing chamber is positioned vertically between the eductor outlet and the capture solution tank.

16. The system of any one of claims 1 to 15, further comprising a packed bed absorption column fluidly coupled to the CO2-lean gas outlet.

17. The system of claim 16, wherein the packed bed absorber column is positioned upstream of the blower.

18. The system of claim 16, wherein the packed bed absorber column comprises structured packing.

19. The system of claim 16, wherein the packed bed absorber column comprises a coating of a rate enhancing material.

20. The system according to claim 1, further comprising a packed bed absorption column and a demister, wherein the demister, the packed bed absorption column, the fan and the CO2-lean gas outlet are vertically and sequentially spaced as follows from the lowest position to the highest position: the packed bed absorption column, the demister, the fan and the CO2-lean gas outlet.

21. The system of any one of claims 1 to 20, further comprising a coating of a rate enhancing material on at least one of the eductor, the capture solution tank, or a wetted surface.

22. The system of any one of claims 1 to 21, wherein the ejector is operable to flow a lean capture solution comprising a rate enhancing additive.

23. The system of claim 22, wherein the rate-enhancing additive comprises at least one of piperazine, carbonic anhydrase, or monoethanolamine.

24. The system of any one of claims 1 to 23, further comprising an auxiliary unit or an intermediate system fluidly coupled to the capture solution tank.

25. A system according to any one of claims 1 to 24, wherein: The sparger defines an sparger axis parallel to an axis extending between the capture solution inlet and the sparger outlet; and The fan is rotatable about a fan axis parallel to the ejector axis.

26. The system of claim 25, wherein the ejector axis and the blower axis are horizontally spaced apart.

27. The system of any one of claims 1 to 26, wherein the capture solution tank is positioned below the ejector and the blower.

28. A system for removing carbon dioxide from a gas, the system comprising: A plurality of injectors, each of the plurality of injectors comprising: a capture solution inlet operable to receive a lean capture solution; a gas inlet operable to receive a gas comprising carbon dioxide; a mixing zone configured to react the lean capture solution and the gas comprising carbon dioxide; and an ejector outlet operable to discharge a mixed fluid comprising a rich capture solution and a CO2-lean gas; at least one CO2 lean gas outlet, the at least one CO2 lean gas outlet fluidly coupled to at least one injector of the plurality of injectors; at least one blower, the at least one blower fluidly coupled to the at least one CO2 lean gas outlet, the at least one blower rotatable to discharge the CO2 lean gas from the at least one CO2 lean gas outlet; a capture solution tank fluidly coupled to the injector outlet of each of the plurality of injectors and to the at least one CO2 lean gas outlet, the capture solution tank configured to collect the rich capture solution; as well as A catch solution distribution line is fluidly coupled to the catch solution inlet of each of the plurality of ejectors.

29. The system of claim 28, further comprising a regeneration system fluidly coupled to the capture solution tank and the capture solution distribution line.

30. The system of claim 29, wherein the capture solution tank is fluidly coupled to the regeneration system via a capture solution circulation pump.

31. The system of claim 29, wherein the regeneration system comprises at least one of a lime causticizing system or a calciner.

32. The system of claim 31, wherein the lime causticizing system comprises at least one of a pellet reactor or a lime slaker.

33. The system of claim 31, wherein the calciner comprises an electric calciner.

34. The system of any one of claims 29 to 33, wherein the regeneration system has a product conduit configured to provide a product of the regeneration system.

35. The system of any one of claims 28 to 34, wherein the plurality of ejectors are positioned on a perimeter of the capture solution tank.

36. The system of claim 35, wherein the at least one CO2 lean gas outlet is fluidly coupled to each injector outlet of the plurality of injectors.

37. The system of claim 36, wherein the plurality of injectors are arranged circumferentially along a perimeter around the at least one CO2 lean gas outlet.

38. The system of any one of claims 28 to 37, wherein the plurality of injectors are arranged in rows of injectors.

39. The system of any one of claims 28 to 38, wherein the plurality of ejectors are fluidly coupled to the at least one CO2 lean gas outlet.

40. The system of any one of claims 28 to 39, wherein the plurality of injectors comprises six injectors.

41. The system of claim 40, wherein the at least one CO2 lean gas outlet comprises six CO2 lean gas outlets, each of the six CO2 lean gas outlets being fluidly coupled to a respective one of the six ejectors.

42. The system of any one of claims 28 to 41, further comprising at least one demister fluidly coupled to the at least one CO2 lean gas outlet.

43. The system of claim 42, wherein the at least one mist eliminator comprises a chevron-shaped mist eliminator.

44. The system of claim 42, wherein the at least one mist eliminator is positioned upstream of the at least one fan.

45. The system of any one of claims 28 to 44, further comprising at least one mixing chamber fluidly coupled to the injector outlet of at least one injector of the plurality of injectors.

46. ​​The system of claim 45, wherein the at least one mixing chamber comprises a static mixer.

47. The system of any one of claims 28 to 46, further comprising at least one packed bed absorber column fluidly coupled to the at least one CO2 lean gas outlet.

48. The system of claim 47, wherein the at least one packed bed absorber column is positioned upstream of the at least one blower.

49. The system of claim 47, wherein the at least one packed bed absorber column comprises structured packing.

50. The system of any one of claims 28-49, further comprising a coating of a rate enhancing material on at least one of the plurality of ejectors, the capture solution tank, or a wetted surface.

51. The system of any one of claims 28 to 50, wherein the plurality of ejectors are operable to flow a lean capture solution comprising a rate enhancing additive.

52. The system of claim 51, wherein the rate-enhancing additive comprises at least one of piperazine, carbonic anhydrase, or monoethanolamine.

53. The system of any one of claims 28 to 52, further comprising an auxiliary unit or an intermediate system fluidly coupled to the capture solution tank.

54. The system of any one of claims 28 to 53, wherein the at least one CO2 lean gas outlet is positioned to direct the CO2 lean gas away from the gas inlet of each of the plurality of injectors.

55. A method for removing carbon dioxide from a gas, the method comprising: flowing a lean capture solution into a capture solution inlet of an ejector to draw the gas into a gas inlet of the ejector according to a venturi effect; reacting the gas with the lean capture solution to form a mixed fluid comprising a rich capture solution and a CO2-lean gas; allowing the mixed fluid to flow into a capture solution tank to collect the rich capture solution; and discharging the CO2-lean gas of the mixed fluid.

56. The method of claim 55, further comprising regenerating the first portion of the rich capture solution to form a regenerated capture solution.

57. The method of claim 56, further comprising combining a second portion of the rich capture solution with the regenerated capture solution to form the lean capture solution.

58. The method of claim 56, further comprising: in an absorption column, mixing at least a portion of the regenerated capture solution with the CO2 lean gas to capture carbon dioxide from the CO2 lean gas and form a rich regenerated capture solution and a CO2 lean absorber gas; and The CO2 lean absorber gas is discharged.

59. The method of claim 58, further comprising reducing mist from the lean CO2 absorber gas prior to discharging the lean CO2 absorber gas.

60. The method of claim 56, wherein regenerating the first portion of the rich capture solution comprises flowing the first portion of the rich capture solution to at least one of a lime causticizing system, a pellet reactor, a lime slaker, or a calciner.

61. The method of claim 56, wherein regenerating the first portion of the rich capture solution comprises flowing the first portion of the rich capture solution to an auxiliary unit or to an intermediate system.

62. The method of claim 56, wherein regenerating the first portion of the rich capture solution comprises forming the regenerated capture solution and a concentrated carbon stream.

63. The method of claim 62, further comprising: releasing a CO2-rich gas stream from the concentrated carbon stream; and The CO2 rich gas stream is compressed to form a product stream.

64. The method of any one of claims 55 to 63, wherein the lean capture solution comprises a molar concentration of KOH ranging from 1 molar to 6 molar.

65. The method of any one of claims 55 to 64, further comprising flowing a make-up capture solution into the capture solution tank.

66. The method of claim 65, wherein the compensation capture solution comprises a KOH concentration ranging from 0.1 wt% to 50 wt%.

67. The method of any one of claims 55 to 66, further comprising flowing a make-up water flow into the capture solution tank.

68. The method of any one of claims 55 to 67, wherein the lean capture solution comprises at least one of an amine, potassium hydroxide, sodium hydroxide, potassium carbonate, bicarbonate, sodium carbonate, or water.

69. The method of claim 68, wherein the lean capture solution comprises a NaOH molarity ranging from 1 molar to 6 molar.

70. The method of claim 55, further comprising reducing mist from the CO2 lean gas prior to exhausting the CO2 lean gas.

71. The method of claim 55, further comprising mixing at least one of the lean capture solution and the rich capture solution with the CO2-lean gas in a packed bed absorption column to capture carbon dioxide from the CO2-lean gas.

72. The method of any one of claims 55 to 71, further comprising flowing the gas through a pre-treatment unit prior to drawing the gas into the gas inlet of the ejector.

73. The method of any one of claims 55 to 72, further comprising flowing a rate enhancing additive through the injector.

74. The method of claim 73, wherein the rate-enhancing additive comprises at least one of piperazine, carbonic anhydrase, or monoethanolamine.

75. The method of claim 73, wherein flowing the rate-enhancing additive comprises flowing the rate-enhancing additive into the capture solution tank.

76. The method of claim 73, wherein flowing the rate-enhancing additive comprises combining the rate-enhancing additive with the lean capture solution.

77. A method according to any one of claims 55 to 76, wherein causing the lean capture solution to flow into the capture solution inlet of the ejector to draw the gas into the gas inlet of the ejector includes: causing the lean capture solution to flow vertically downward, and drawing the gas into the gas inlet in a horizontal direction.

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