WO2024243699A1

WO2024243699A1 - Integrated self-sufficient water generation, carbon capture and sustainable fuel production system

Info

Publication number: WO2024243699A1
Application number: PCT/CA2024/050727
Authority: WO
Inventors: Reza RASOOLI; Nader MOHEBBI
Original assignee: Climate Assist Technologies Inc
Current assignee: Climate Assist Technologies Inc
Priority date: 2023-05-30
Filing date: 2024-05-30
Publication date: 2024-12-05
Anticipated expiration: 2025-11-30

Abstract

A method for water generation and carbon capture from atmospheric air and exhaust gas comprises the steps of introducing the atmospheric air into an evaporator, wherein the evaporator is configured to extract water from the atmospheric air; transferring at least some of the water extracted by the evaporator to a water conditioning tank; introducing the exhaust gas to a flash drum, wherein the flash drum is configured to cool the exhaust gas; transferring the exhaust gas from the flash drum to an air cooler, wherein the air cooler is configured to further cool the exhaust gas; transferring the exhaust gas between the air cooler and a compressor, wherein the compressor is configured to increase a pressure of the exhaust gas; transferring the exhaust gas from the compressor to an absorber; transferring at least a portion of the water from the water conditioning tank to the absorber, wherein the absorber is configured to effect a dissolution of carbon dioxide from the exhaust gas into the water; and transferring the water from the absorber to the flash drum, wherein the flash drum is configured to separate the carbon dioxide from the water.

Description

TITLE

Integrated Self-Sufficient Water Generation, Carbon Capture and Sustainable Fuel Production System

TECHNICAL FIELD

[0001] The present disclosure relates to water generation systems. In particular, the present disclosure relates to systems for integrated water generation from atmospheric air and/or exhaust gas from combustion and/or syngas sources with carbon capture, hydrogen generation, and sustainable fuel production capabilities.

BACKGROUND

[0002] Climate change is exacerbating droughts and desertification worldwide, significantly impacting water availability. According to a United Nations report, natural disasters related to weather, climate, and water have affected 55 million people annually since 1970, with 2.3 billion people experiencing water stress each year. This scarcity puts severe constraints on industries, particularly renewable energy solutions, which require substantial water resources for operation.

[0003] Water scarcity particularly affects technologies such as hydrogen production through electrolysis, which requires significant pure water inputs. This limitation hampers the development and scalability of such technologies, impeding their adoption and effectiveness in transitioning to a low-carbon economy. A new approach is needed that can reduce the impact of climate change but does not create new problems.

[0004] Atmospheric Water Generation (AWG) may be used to address this issue. AWG uses technology to produce water from the surrounding air. This provides the potential to expand water availability during shortages, contamination events, and other situations that can interrupt typical drinking water services. However, such technology has limitations. [0005] AWG depends on the humidity and temperature in the geographical location the AWG system is located. The output increases with an increase in temperature, and vice versa. As a result, systems that only rely on AWG systems do not provide meaningful output in lower temperatures. This is because cold air does not contain as much moisture as warm air.

[0006] Industrial exhaust gases contain considerable amounts of water, which can be recovered during the CO2 capture process. This not only reduces greenhouse gas emissions but also provides an additional source of water, helping alleviate water scarcity issues faced by industries. Currently, existing CO2 capture technologies do not generate and utilize exhaust gas water simultaneously for CO2 capture or hydrogen generation.

[0007] In the absence of adequate infrastructure and the risks associated with conventional methods of utilizing captured CO2, transforming captured CO2 into sustainable fuel has emerged as the optimal utilization method. By converting captured CO2 into sustainable fuel, not only are greenhouse gas emissions reduced, but this also contributes positively to combating global warming and related environmental issues.

[0008] Sustainable fuel production is crucial for reducing reliance on fossil fuels and mitigating carbon emissions. Utilizing renewable energy sources and carbon-neutral processes, such as biomass conversion or electrolysis, can yield sustainable fuels like biofuels.

[0009] Sustainable fuel, derived from organic materials like plant biomass or waste, offer a renewable alternative to traditional fossil fuels. Their production can be carbon- neutral or even carbon-negative when coupled with carbon capture technologies.

[0010] Integrating sustainable fuel production into water generation and carbon capture systems creates a holistic approach to addressing climate change, energy security, and environmental sustainability. [0011] The aviation industry is recognized as a sector where reducing emissions is particularly challenging, and there is an urgent need for innovative solutions to meet global reduction goals. Sustainable aviation fuel (SAF) could offer a viable solution. According to the International Civil Aviation Organization (ICAO), SAF is defined as renewable or waste-derived aviation fuels that meets sustainability criteria under Carbon Offsetting and Reduction Scheme for International Aviation (CORSIA) rules. Technical analysis done at the ICAO shows that SAF has the greatest potential to reduce CO2 emissions from international aviation. However, its production is also hampered by water scarcity. Traditional methods such as sourcing water from rivers and lakes or using desalination impose additional environmental and economic challenges, making them less sustainable. Moreover, these methods are not practical for facilities located away from coastal areas.

[0012] Sustainable fuel production primarily involves the synthetic fuel generation process, which depends on hydrogen production to maintain the correct CO/H2 ratio for the synthetic fuel production process or to convert CO2 to CO upstream of the synthetic fuel process. Consequently, hydrogen generation, which is predominantly carried out through electrolysis, requires pure water and can be impacted by water shortage issues.

[0013] The increasing urgency for innovative techniques that support CO2 capture and sustainable fuel without exacerbating water scarcity is clear. Technologies like AWG, which extracts water from the air, offer potential solutions for mitigating water shortages. However, the utility of AWG is limited by regional and climatic factors, emphasizing the need for solutions that are adaptable to varying conditions.

[0014] Additionally, significant amounts of water present in industrial exhaust gases could be harvested during the CO2 capture process. This approach is not constrained by environmental conditions and could be more energy-efficient in cooler climates. Using this method in conjunction with AWG could enhance both the system's availability and its effectiveness. Such techniques not only reduce greenhouse gas emissions but also augment alternative water resources, addressing the water scarcity issues that industries face. Despite these promising methods, the industry still lacks a comprehensive solution that integrates both AWG and water recovery from exhaust gases for efficient carbon capture and sustainable fuel production.

[0015] There is therefore a need for a new approach to address the above issues. These and other objects will be better understood by reference to this specification as a whole. Not all of the objects are necessarily met by all embodiments described below.

SUMMARY

[0016] An integrated system combining water generation and carbon capture with capability to produce hydrogen and sustainable fuel is provided. This system features several subsystems, such as an interface module (which includes inlet metering, filtration units, and a cooling system), a water generation module, a water polishing module, a CO2 removal module, an H2 generation module, and a sustainable fuel generation module (capable of producing SAF, diesel, naphtha, wax, etc.), along with a control system module.

[0017] Power to operate the system may be generated using utility grid or renewable energy sources, such as solar, wind, fuel cell, etc.

[0018] In accordance with one embodiment, a method for water generation and carbon capture from atmospheric air and exhaust gas comprises the steps of introducing the atmospheric air into an evaporator, wherein the evaporator is configured to extract water from the atmospheric air; transferring at least some of the water extracted by the evaporator to a water conditioning tank; introducing the exhaust gas to a flash drum, wherein the flash drum is configured to cool the exhaust gas; transferring the exhaust gas from the flash drum to an aircooler, wherein the aircooler is configured to further cool the exhaust gas; transferring the exhaust gas between the air cooler and a compressor, wherein the compressor is configured to increase a pressure of the exhaust gas; transferring the exhaust gas from the compressor to an absorber; transferring at least a portion of the water from the water conditioning tank to the absorber, wherein the absorber is configured to effect a dissolution of CO2 from the exhaust gas into the water; and transferring the water from the absorber to the flash drum, wherein the flash drum is configured to separate the CO2 from the water.

[0019] In a further embodiment, the method further comprises the step of transferring at least some of the water extracted by the evaporator to a water storage tank.

[0020] In still a further embodiment, the method further comprises the step of transferring at least some of the water extracted by the evaporator to a main water storage tank.

[0021] In still yet a further embodiment, the method further comprises the step of transferring at least a portion of the exhaust gas from the air cooler to the evaporator, wherein the evaporator is configured to extract water from the exhaust gas.

[0022] In another embodiment, the compressor comprises a plurality of stages.

[0023] In still another embodiment, the air cooler comprises a plurality of bundles.

[0024] In still yet another embodiment, the step of transferring the exhaust gas between the air cooler and the compressor comprises transferring the exhaust gas between one of the plurality of bundles of the air cooler and one of the plurality of stages of the compressor.

[0025] In a further embodiment, the compressor comprises one or more suction scrubbers.

[0026] In still a further embodiment, the step of transferring the exhaust gas from the compressor to the absorber further comprises transferring the exhaust gas through a gas cooling coil in the water conditioning tank, wherein the gas cooling coil is configured to cool the exhaust gas.

[0027] In yet still a further embodiment, the water conditioning tank comprises a water cooling coil configured to cool the water within the water conditioning tank. [0028] In still further embodiment, the method further comprises the step of transferring the CO2 separated by the flash drum to a synthetic fuel generation unit configured to generate synthetic fuel using the CO2.

[0029] In another embodiment, a system for water generation and carbon capture from atmospheric air and exhaust gas comprises an evaporator, a water conditioning tank, a flash drum, an air cooler, and a compressor. The evaporator is configured to accept the atmospheric air and to extract water from the atmospheric air. The water conditioning tank is configured to accept at least some of the water extracted by the evaporator. The flash drum is configured to accept the exhaust gas and to cool the exhaust gas. The air cooler is configured to accept the exhaust gas from the flash drum and to further cool the exhaust gas. The compressor is configured to accept the exhaust gas from the air cooler and to increase a pressure of the exhaust gas. The absorber is configured to accept the exhaust gas from the compressor. The absorber is further configured to accept at least a portion of the water from the water conditioning tank and to effect a dissolution of CO2 from the exhaust gas into the water. The flash drum is further configured to separate the CO2 from the water.

[0030] In still another embodiment, the evaporator is further configured to accept at least a portion of the exhaust gas from the air cooler and to extract water from the exhaust gas.

[0031] In still yet another embodiment, the water conditioning tank comprises a gas cooling coil configured to cool the exhaust gas from the compressor and a water cooling coil configured to cool the water within the water conditioning tank.

[0032] The foregoing was intended as a summary only, and of only some of the aspects of the invention. It was not intended to define the limits or requirements of the invention. Other aspects of the invention will be appreciated by reference to the detailed description of the embodiments. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] The embodiments of the invention will be described by reference to the drawings thereof, in which:

[0034] Fig. 1 depicts a block diagram for Configuration 1 of the system;

[0035] Fig. 2 depicts a block diagram for Configuration 2 of the system;

[0036] Fig. 3 depicts a block diagram for Configuration 3 of the system;

[0037] Fig. 4 depicts the boundary limits for the inputs and outputs for the system across the various configurations;

[0038] Fig. 5 depicts an overall flow and controls diagram for all systems configurations;

[0039] Fig. 6A depicts a portion from Fig. 5, depicting the components for water generation;

[0040] Fig. 6B depicts a portion from Fig. 5, depicting the components for water generation and further including control lines;

[0041] Fig. 7A depicts a portion from Fig. 5, depicting the components for CO2 capture;

[0042] Fig. 7B depicts a portion from Fig. 5, depicting the components for CO2 capture and further including control lines; and

[0043] Fig. 8 illustrates the different operating modes for the system. DETAILED DESCRIPTION

[0044] A system 10 for water generation and carbon capture with hydrogen and sustainable fuel generation capabilities in accordance with one embodiment is shown in Fig. 5. The system 10 is an integrated modular solution that provides the features described as follows.

[0045] The technology discussed in this document applies to System 10 when it is fed by exhaust gas (such as biogenic exhaust gas and stack gas) from industrial or manufacturing processes. The system 10 also features an integrated AWG subsystem that enhances water production from exhaust gases. Furthermore, it includes applications for using at least some of the produced water to generate hydrogen through electrolysis, as well as the ability to use the generated hydrogen for sustainable fuel production.

[0046] The system 10 is adaptable and can be utilized to produce any custom production rates depending on application requirements and system feed characteristics. In addition, the technology of the system 10 may be scalable, meaning several smaller units could be bundled or stacked to produce higher rates.

[0047] The innovative integration of atmospheric air and exhaust gas water generation capabilities with high-pressure water-based carbon removal in a single system has led to the development of a new technology. This technology is more efficient and consumes less energy than traditional methods, effectively addressing two major climate-related challenges: water scarcity and carbon emissions. Furthermore, using a portion of the water generated by the system 10 for hydrogen production through electrolysis, either alone or in conjunction with external water sources, avoids additional strain on limited water resources. The use of this produced hydrogen for sustainable fuel generation in such an integrated system enhances the benefits of what would otherwise be multiple separate systems, overcoming their individual limitations when used in isolation. [0048] Unlike some of the available solutions, the feed of the system 10 can have any temperatures, any humidity level, and any carbon content percentages. This is the result of integrating and meeting the needs of these three diverse technologies in a novel self-sufficient way.

[0049] The system 10 comprises control logic 70 that is configured to control and monitor various components of the system 10. The control and monitoring techniques for the components outlined herein can be implemented within the control logic 70 using a variety of commercially available programming software platforms and languages. Although the control and monitoring techniques presented herein are unique, the hardware of the control logic 70 may employ products like programmable logic controllers (PLC), distributed control systems (DCS), and/or other types of control systems used in the process industry. They may be tailored specifically to execute the features of the system 10. While the embodiment shown in Figs. 5 to 7 uses a PLC as an illustrative example, this does not restrict the control logic 70 to only using PLCs. It is understood that other types of control systems can also be employed.

[0050] The system 10 may further comprise a human machine interface (HMI) 116 that is configured to allow for the system 10 to be controlled and monitored locally. Alternatively, or in addition, the system 10 may be equipped with cellular or satellite communication capabilities to facilitate controlling and monitoring the system 10 remotely. This remote control may include starting or stopping the system 10, or changing the setpoints for one or more of the control loops. Furthermore, automatic warnings or alerts may be set up to provide live unit status of the system 10.

[0051] Depending on the type of feed gas that is available for the system, the system 10 can function in one of three different main configurations, namely Configuration 1 (CONFIG-1 ), Configuration 2 (CONFIG-2), and Configuration 3 (CONFIG-3). These configurations allow for generating water from atmospheric air and/or exhaust gas with the possibility for removing CO2, generating hydrogen, and utilizing CO2 by producing sustainable fuel when required by utilizing different combination of modules.

[0052] Figs. 1 to 3 show the various subsystems involved in each configuration, while Fig. 4 illustrates the different combinations of input and output streams for each of the configurations. As it is illustrated in Fig. 8, each of configurations above may operate in three modes.

[0053] Mode 1 (“AWG Only”) operates by utilizing atmospheric air for AWG. This mode may be selected for generating water from atmospheric air when there is either a lack of reliable nearby water sources or when the available exhaust gas volume is too low to produce enough water for carbon capture. This option is particularly effective during summertime or when the unit is operating in tropical or subtropical regions, where the ambient temperature and humidity are typically high.

[0054] Mode 2 (“Exhaust Gas Only”) relies solely on exhaust gas as the input for the system 10. This mode may be employed when there is access to exhaust gas from another industrial process, such as biomass gasification or combustion stacks. Here, the exhaust gas itself is used to produce the necessary water for carbon capture. The excess water, either alone or combined with external water sources, may also be utilized for hydrogen production. This hydrogen can then potentially be used to create sustainable fuels. Depending on the required water volume for these processes and the power availability at the site, Mode 2 may operate in three sub-modes: Mode 2A, Mode 2B, and Mode 2C.

[0055] Mode 3 (“AWG Plus Exhaust Gas”) combines the use of atmospheric air and exhaust gas for water generation and carbon capture simultaneously. Mode 3 encompasses all the applications of Mode 1 , but with the added benefit of carbon capture functionality. This mode is particularly well-suited for systems situated in tropical regions, or during the summer in other climates, especially in coastal areas, near facilities with exhaust gas stacks requiring carbon capture technology. This is particularly advantageous when local water sources are scarce or difficult to access, and the produced water is intended for hydrogen generation and/or sustainable fuel production, provided there are no constraints on power availability.

[0056] As illustrated in Fig. 1 , CONFIG-1 involves processing exhaust gas 200 and atmospheric air 100 to produce pure water. This water can be used fully or partially, either independently or in conjunction with an external water supply 150, for carbon capture. Additionally, some of the water may be used for hydrogen generation 172 or other industrial needs. In this configuration, the captured CO2, along with the produced water and hydrogen, will be sent to third parties for utilization. The exhaust gas may pass through a cleaning module that removes the emissions such as SOx and NOx.

[0057] Referring to Fig. 1 , in some embodiments, water from the external water supply 150 is treated by a water conditioning module 500, which may be external to the system 10, before entering a water storage module 506. The exhaust gas 200 may be fed into a gas cooling module 502 configured to cool the exhaust gas 200 before it enters a water generation module 504. The atmospheric air 100 may also be fed into the water generation module 504. The water generation module 504 is configured to generate water from the atmospheric air 100 and/or the exhaust gas 200 from the gas cooling module 502. The water generated from the water generation module 504 is fed into the water storage module 506.

[0058] At least some of the water from the water storage module 506 may be fed into a water utilization module 516, which is configured to provide for water to be used for various desired purposes. Alternatively, at least some of the water from the water storage module 506 may be fed into an electrolyzer unit 518 to generate H2 for use by a H2 utilization unit 520. The electrolyzer unit 518 and the H2 utilization unit 520 may be external to the system 10 or may be integrated within the system 10.

[0059] In some embodiments, at least some of the water from the water storage module 506 may be fed into a water cooling module 508 configured to cool the water. The water may also be subjected to a water pumping module 510 that is configured to increase the water pressure.

[0060] The exhaust gas 200 exiting the gas cooling module 502 may then be fed into a gas compression module 512 that is configured to compress the exhaust gas 200 (i.e. increase its pressure). The exhaust gas 200 from the gas compression module 512 may then be mixed into the high-pressure cold water from the water pumping module 510 within a CO2 removal module 514 to dissolve CO2 into the water. The CO2 removal module 514 is configured to remove the CO2 from the water and exhaust gas 200 mixture. The CO2 may then be fed into a CO2 utilization unit 522. The CO2 utilization unit 522 may be external to the system 10. [0061] As shown in Fig. 2, CONFIG-2 includes all the components of CONFIG-1 but also includes the following: the captured CO2 and generated hydrogen are routed to a synthetic fuel generation unit 254 that is configured to generate synthetic fuels, such as, for example, SAF, naphtha, diesel, and/or wax. The synthetic fuel generation unit 254 may feature additional subsystems like the reverse water-gas-shift, which internally converts CO2 to CO. Subsequently, CO and H2 are mixed in precise ratios for use in downstream subsystems that facilitate the synthetic fuel production process. This adjustment facilitates the production of synthetic fuels using technologies like the Fischer-Tropsch process. In some embodiments, the boundary of the system 10 is established where CO2 and H2 are transferred to the synthetic fuel generation unit 524 (i.e. the synthetic fuel generation unit 524 is external to the system 10). Beyond this boundary, the synthetic fuel generation process continues within an external system, which may be available commercially. In other embodiments, the system 10 may comprise the synthetic fuel generation unit 524, such that the system 10 is designed as an integrated system, capable of being delivered as a unified package.

[0062] In CONFIG-2, if the exhaust gas 200 used as feed for the system 10 originates from biogenic sources, such as the exhaust from a biomass-based power generation system, the system 10 can produce SAF, along with bio-based naphtha, diesel, and wax. Utilizing renewable power sources for this configuration enables the produced SAF to be classified as eSAF. Conversely, if the exhaust gas 200 is derived from a non-biogenic source, such as the exhaust from a fossil fuel driven power generation system, the produced synthetic fuel is classified as LCAF (Lower Carbon Aviation Fuel). LCAF is a fossil-based aviation fuel that complies with the CORSIA Sustainability Criteria.

[0063] CONFIG-2 represents a complete CCUS (Carbon Capture, Utilization, and Storage) solution that captures, stores, and utilizes CO2 in a self-sufficient manner. This has resulted in a new CCUS technology and implementation approach that operates independently of sequestration and requires minimal or no reliance on external resources such as water, CO2, and hydrogen. Additionally, the combined system enhances energy and electricity efficiency by sharing resources across different components, eliminating interface points and gaps that would typically result in the wastage of valuable resources within the subsystems. [0064] As depicted in Fig. 3, CONFIG-3 resembles CONFIG-2 in terms of the outputs it generates, but it differs by utilizing syngas 526 at the inlet of the system 10. The syngas 526, or synthesis gas, is a fuel gas mixture primarily composed of hydrogen (H2) and carbon monoxide (CO) and is used as an intermediary in the production of synthetic fuels and chemicals. Additionally, the syngas 526 contains CO2 and water. The system 10 is designed to remove the CO2 and water from the syngas 526, thus preparing it for processing in downstream synthetic fuel generation systems (e.g. the synthetic fuel generation unit 524). These systems may include additional subsystems such as the reverse water-gas-shift, water-gas-shift, and partial oxidation, which internally adjust the CO and H2 in specific ratios. This adjustment facilitates the production of synthetic fuels using technologies like the Fischer-Tropsch process.

[0065] Since the composition of the syngas 526 is already more favorable for processing in synthetic fuel generation systems compared to combustion-based exhaust gases, which contain significantly higher levels of CO2 and require the conversion of CO2 to CO, CONFIG-3 may be more efficient. The syngas 526 also naturally contains H2, reducing the need for additional hydrogen generation. As a result, CONFIG-3 may be more energy-efficient, consuming less energy and requiring less electricity, which potentially leads to higher production rates than CONFIG-2.

[0066] As illustrated in Fig. 8, each of the configurations (i.e. CONFIG-1 , CONFIG-

2, and CONFIG-3) can operate in three different modes: Mode 1 , Mode 2, and Mode

3. One difference between these configurations, as shown in Fig. 8 and previously described, lies in the available inputs and outputs from and to the system 10.

[0067] Referring to Figs. 5 to 7, the system 10 comprises an air cooler 214, an evaporator unit 15, a condenser 50, and a refrigeration loop compressor 60. The evaporator unit 15 comprises an evaporator 16 connected to an evaporator collecting tank 38, which in turn is connected to a water separator 74. The system 10 further comprises a water storage tank 34. These components may be used for water generation, as generally shown in Figs. 6A and 6B. [0068] With respect to CO2 capture, as generally shown in Figs. 7A and 7B, the system 10 further comprises a water conditioning tank 322, a main water storage tank 156, a compressor 248, a flash drum 390, an absorber 360, and a cooler 334.

[0069] Referring to Figs. 6A and 6B, the air cooler 214 is connected to the evaporator unit 15. An air cooler valve 232 is configured to control the flow of the exhaust gas 200 (or syngas 526) through the evaporator unit 15. In Mode 1 , when the system 10 is configured to use AWG for water generation, the air cooler valve 232 is closed. The air cooler valve 232 is configured to isolate the air cooler 214 from the evaporator unit 15, as the air cooler 214 will not be used in this mode of operation. The evaporator gas inlet isolation valve 68 and the evaporator bypass isolation valve 72, which help regulate the flow of the exhaust gas 200, may be provided, but they remain closed in Mode 1 .

[0070] The system 10 comprises a main intake louver 12 configured to accept the atmospheric air 100 into the system 10. The main intake louver 12 is configured to be in the open position in Mode 1 . A damper valve 62 may be provided to direct the output from the evaporator unit 15 entirely to the condenser 50. In addition, a block valve 76 may be provided and may be closed in Mode 1 , as the compressor 248, as fed through a suction line 64, will be in idle mode or will be shut down.

[0071] In Mode 1 , the atmospheric air 100 may be drawn into the system 10 through the main intake louver 12 and then passes through one or more intake filters 14, driven by the draft produced from an air blower 78. The air blower 78 may have variable speed capabilities. A secondary louver 106 may be provided and is configured to allow incoming air for optimal operation of the condenser 50. When the evaporator 16 is in service, the secondary louver 106 is configured to remain in an open position, allowing incoming air to pass through one or more secondary filters 42. The movement of the incoming air may be aided by a fan 44, which directs the incoming air over the condenser 50 before exiting through an air output 48. The speed of the fan 44 and the air blower 78 may be set by a refrigeration coolant temperature element 52 operatively connected to the condenser 50 to ensure the condenser 50 operates in optimum operating conditions. [0072] A temperature of the atmospheric air 100 entering the evaporator unit 15 may be measured by an inlet air temperature element 18. Additionally, a relative humidity of the atmospheric air 100 may be measured by an air humidity sensor 104 before the atmospheric air 100 enters the evaporator unit 15. These measurements from the inlet air temperature element 18 and the air humidity sensor 104 may be recorded in the control logic 70 and may be used to assess production rates and/or adjust the speed of the air blower 78 based on pre-set logic in the control logic 70.

[0073] The atmospheric air 100 passes through the evaporator 16. The evaporator 16 may comprise a plurality of finned evaporator tubes that operate between roughly 1 °C and 5°C. An evaporator outlet temperature element 40 may be provided to control the speed of operation of the refrigeration loop compressor 60. The speed of the operation of the refrigeration loop compressor 60 may dictate the circulation flow rate of refrigerant in the evaporator unit 15. In some embodiments, an expansion valve 56 may be provided between the evaporator unit 15 and the condenser 50. The expansion valve 56 may be controlled by an expansion valve temperature element 58. A condenser pressure element 54 may be provided to monitor a pressure of the refrigerant. The differential pressure across the expansion valve 56 ensures the cold refrigerant remain between the desired temperatures of roughly 1 °C and 5°C.

[0074] When atmospheric air 100 comes into contact with the cold evaporator tubes of the evaporator 16, the atmospheric air 100 may condense, forming water droplets. These droplets collect in the evaporator water collecting tank 38. A water transfer isolation valve 66 is provided between the evaporator collecting tank 38 and the water separator 74 and may remain open in any mode that uses the evaporator 16. Water may then move from evaporator water collecting tank 38 to the water separator 74 (i.e. through the first isolation valve 66) via gravity. An evaporator tank level transmitter 20 may be provided for monitoring a water level within the evaporator collecting tank 38.

[0075] Furthermore, a separator temperature element 86 and/or a separator level transmitter 88 may be provided to monitor a water temperature and/or a water level within the water separator 74, respectively. If the separator level transmitter 88 detects a high water level, the control logic 70 may be configured to activate a pump 22 to distribute water to one or more of three potential destinations: the water utilization module 516, the electrolyzer unit 518, and/or the CO2 removal module 514. The rates of water produced may recorded in the control logic 70 based on measurements made by a flow totalizer 24.

[0076] The pure water produced by the system 10 can be utilized in one or more of the following ways: for drinking, for high-pressure CO2 removal, and/or for industrial applications such as hydrogen generation via electrolysis. The choice of use depends on the moisture content of the air (gas) and the flow rate. A polishing isolation valve 102 may be provided between the water separator 74 and the water storage tank 34. A storage isolation valve 90 may be provided between the water separator 74 and the main water storage tank 156. A conditioning tank isolation valve 84 may be provided between the water separator 74 and the water conditioning tank 322 to control a flow of water from the water separator 74 to the water conditioning tank 322 through a conditioning tank line 80. A conditioning tank flowmeter 82 may be provided to measure a flow of water into the water conditioning tank 322. Accordingly, the positions of the polishing isolation valve 102, the storage isolation valve 90, and/or the conditioning tank isolation valve 84 may vary, being either open or closed based on the specific need for the produced water.

[0077] Referring to Figs. 6A and 6B, if there is an intention to use at least some of the produced pure water for drinking purposes, the polishing isolation valve 102 may be either fully or partially open to allow the water to then flow through one or more water filters 26 for filtering out impurities. The water may then undergo mineralization at a mineralization station 28 and may then be sanitized by ultraviolet (UV) treatment at UV treatment station 30. The treated water may then be stored in the water storage tank 34. A water level in the water storage tank 34 may be monitored by a water storage level transmitter 36. A flow of water into the water storage tank 34 may be monitored by a water storage flowmeter 32. Should the water storage level transmitter 36 detect a high water level within the water storage tank 34, it may be configured to trigger a shutdown through the control logic 70, resulting in a closure of the polishing isolation valve 102. [0078] Referring to Figs. 7A and 7B, if there is an intention to use at least some of the produced pure water for industrial purposes, the storage isolation valve 90 may be either fully or partially open to allow for a flow of water through a main water storage tank line 94 to the main water storage tank 156. The flow of water may be monitored by a storage tank flowmeter 92. A water level in the main water storage tank 156 may be monitored by a storage tank level transmitter 160. If the storage tank level transmitter 160 detects a high water level within the main water storage tank 156, it may be configured to instruct the control logic 70 to close the storage isolation valve 90. Additionally, the storage tank level transmitter 160 may be configured to control a storage tank pump 166, which is configured to pump water out of the main water storage tank 156. The storage tank pump 166 may be configured to stop pumping water when there is insufficient water in the tank (as detected by the storage tank level transmitter 160). The flow of water out of the main water storage tank 156 may be measured by a tank output flowmeter 168. An output valve 170 may be provided to control a flow of water from the main water storage tank 156. The output valve 170 may be used for either isolation or flow control. The main water storage tank 156 may also be equipped with a conductivity meter 162 to monitor water quality and with a storage tank temperature sensor 164 to measure a water temperature within the main water storage tank 156.

[0079] The main water storage tank 156 may also be filled with water from the external water supply 150 regardless of the mode of operation (i.e. Mode 1 , Mode 2, Mode 3) orthe inlet and outlet configuration (i.e. CONFIG-1 , CONFIG-2, and CONFIG- 3). An external water isolation valve 178 may be provided between the external water supply 150 and the main water storage tank 156. If water from the external water supply 150 is to be used, the external water isolation valve 178 may remain open, with the water flow rate being actively measured and monitored by external water flowmeter 154. A percentage of an opening of the external water isolation valve 178 may be set by the control logic 70 in relation to a percentage of an opening of the storage isolation valve 90 and a reading of the storage tank flowmeter 92. Both the external water isolation valve 178 and the storage tank isolation valve 90 may also be regulated by the storage tank level transmitter 160 to prevent low or high water levels in the main water storage tank 156. [0080] A decision to use water from the external water supply 150 may depend on the availability of external water, atmospheric air and exhaust gas water generation limits, or available electricity due to load management purposes. Although the system 10 is designed to be self-sufficient, utilizing external water from the external water supply 150 is a flexible option, employed only under specific operational circumstances as described.

[0081] Any external water introduced into the system 10 (i.e. through the external water supply 150) may already have been purified to the quality needed for electrolysis. However, if necessary, the water conditioning module 500 may also be included as part of the system 10 on an as-needed basis.

[0082] In Mode 2, the exhaust gas 200 enters the system 10 through an exhaust input line 201 for water generation and carbon capture purposes. The main features of water generation though the evaporator path is explained in Mode 1 for the atmospheric air 100 previously. Water generation from the exhaust gas 200 is similar to that for the atmospheric air 100, but the exhaust gas 200 is typically at higher temperatures than the atmospheric air 100. When the exhaust gas 200 is sent directly to the suction line 64, the water generation concept is based on cooling the hot gas at the air cooler 214 to condense the water content.

[0083] The core principle of carbon capture in this disclosure hinges on the fact that CO2 exhibits higher solubility in water under elevated pressure and lower temperatures. Conversely, the solubility of CO2 decreases significantly with higher temperatures and reduced pressure, as occurs in the flash drum 390.

[0084] Referring to Figs. 7A and 7B, upon entry, a flow rate of the exhaust gas 200 may be metered by an inlet flowmeter 206 at the receiving point. A relative humidity of the exhaust gas 200 may also be measured by an exhaust humidity sensor 202, and a temperature of the exhaust gas 200 may be measured by an exhaust temperature sensor 204. Additionally, a composition of the exhaust gas 200 may be analyzed by analyzer 208. Data from the inlet flowmeter 206, exhaust humidity sensor 202, the exhaust temperature sensor 204, and/or the analyzer 208 may be transmitted to the control logic 70 for recording and control purposes. [0085] The flash drum 390 is a component of the carbon capture subsystem and comprises a heating coil 316. The heating coil 316 may be an immersed heat exchanger. The exhaust gas 200 is directed to the heating coil 316. The exhaust gas 200 passes through the heating coil 316, with the flow of the exhaust gas 200 through the heating coil 316 controlled by an inlet control valve 256 and a flash drum heating coil bypass control valve 246. Relative openings for the inlet control valve 256 and the flash drum heating coil bypass control valve 246 are ratio-controlled by a flash drum temperature element 392, which is configured to adjust the operating temperature of the flash drum 390. The temperature setpoint may be selected based on system performance to maximize CO2 recovery in the flash drum 390.

[0086] Passing the exhaust gas 200 through the heating coil 316 of the flash drum 390 offers two primary advantages. Firstly, it enhances the efficiency of the CO2 removal process by increasing the temperature of the flash drum 390. Secondly, it lowers the temperature of the exhaust gas 200, consequently reducing the heat duty of the air cooler 214.

[0087] The exhaust gas 200, having lost some of its heat, exits the heating coil 316 of the flash drum 390 via a heating coil outlet line 210 and then enters the air cooler 214. The air cooler 214 comprises a plurality of bundles, with the exhaust gas 200 entering a first bundle 220. An outlet line temperature element 212 is provided to measure a temperature of the exhaust gas 200 exiting the heating coil 316. A difference in temperature of the exhaust gas 200 between a temperature measured by the exhaust temperature element 204 and a temperature as measured by the outlet line temperature element 212 reflects the amount of temperature reduction achieved in the flash drum 390, demonstrating the effectiveness of the heat recovery loop, as shown in Fig. 5.

[0088] The path of the exhaust gas 200 is shared among Mode 2A, Mode 2B, and Mode 2C until the air cooler 214, but each mode follows a different path within the system 10 after the exhaust gas exits the first bundle 220 of the air cooler 214. As depicted in Figs. 5, 6A, and 6B, the arrangement of various ones of the valves differs for each mode (i.e. for Mode 2A, Mode 2B, and Mode 2C). [0089] Regardless of the variations in Mode 2, the exhaust gas 200 enters the carbon capture system by arriving at the compressor 248 through the suction line 64. The compressor 248 may be a multistage compressor. In some embodiments, the compressor 248 may be a two-stage compressor, comprising first and second stages 248a, 248b, as shown in Figs. 7A and 7B. In practice, the number of stages in the compressor 248 may be different based on available options in the market or CO2 removal requirements (e.g. pressure). The logic for operation of the compressor 248 may be the same even if more stages are deployed.

[0090] The compressor 248 is configured to provide enough draft force to pull the exhaust gas 200 from its source.

[0091] The exhaust gas 200 enters the first stage 248a from the suction line 64 and exits the first stage 248a through the first stage discharge line 224. The temperature and pressure of the exhaust gas 200 before the first stage 248a may be measured and monitored at the suction line 64 by a suction line temperature element 240 and a suction line pressure transmitter 242, respectively. The temperature and pressure of the exhaust gas 200 after the first stage 248a may be measured and monitored at the first stage discharge line 224 by a first stage discharge line temperature element 258 and a first stage discharge line pressure transmitter 244, respectively. The differences in pressure and temperature across these points may indicate the performance of the compressor 248 and may be used to monitor and control the operation of the first stage 248a (e.g. using the control logic 70).

[0092] The exhaust gas 200 enters a second bundle 218 of the air cooler 214 through the first stage discharge line 224, thereby further reducing the temperature of the exhaust gas 200. The exhaust gas 200 then exits the second bundle 218 through a first scrubber inlet line 230. A temperature of the exhaust gas 200 before the second bundle 218 may be monitored by the first stage discharge line temperature element 258. A temperature of the exhaust gas 200 after the second bundle 218 may be monitored by a first scrubber inlet temperature element 234 on the first scrubber inlet line 230. The temperatures of the exhaust gas 200 before and after the second bundle 218 may be used by the control logic 70 to adjust operation of the air cooler 214. For example, in some embodiments, the air cooler 214 may comprise an air cooler fan 215, which may be configured to operate at different speeds by the control logic 70 depending on the temperatures of the exhaust gas before and after the second bundle 218.

[0093] After cooling, the exhaust gas 200, having lost further of its temperature, moves on to second stage 248b of the compressor 248. In some embodiments, one or more suction scrubbers may be provided. For example, in the embodiment shown in Figs. 7A and 7B, the suction scrubbers comprise first and second stage suction scrubbers 268, 278.

[0094] The first stage suction scrubber 268 may comprise a first stage scrubber level transmitter 264 to measure a level of condensed water separated in the first stage suction scrubber 268, with the water directed to the water conditioning tank 322 through a first stage scrubber control valve 266. The exhaust gas 200 enters the first stage scrubber 268 through the first scrubber inlet line 230 and exits through a second stage inlet line 225. The exhaust gas 200 then enters the second stage 248b through the second stage inlet line 225 and exits the second stage 248b through a second stage discharge line 226. A pressure at the suction of the second stage 248b may be regulated by a first stage scrubber pressure transmitter 262 and by a first control valve 260.

[0095] A temperature of the exhaust gas 200 before and after the second stage 248b may be measured and monitored by a second stage inlet temperature element 250 and a second stage discharge temperature element 280, respectively. A pressure of the exhaust gas 200 before and after the second stage 248b may be measured and monitored by a second stage inlet pressure transmitter 252 and a second stage discharge pressure transmitter 254, respectively. The differences in pressure and temperature across these points may be used to determine the performance of the compressor 248 and may be used (e.g. by the control logic 70) to monitor and control operation of the second stage 248b. [0096] The exhaust gas 200 exits from the second stage 248b through the second stage discharge line 226 and enters a third bundle 216 of the air cooler 21 to further lower its temperature. The exhaust gas 200 exits from the third bundle 216 through a second scrubber inlet line 228 before proceeding to the second stage suction scrubber 278. A temperature of the exhaust gas 200 before the third bundle 216 may be monitored by the second stage discharge temperature element 280. A temperature of the exhaust gas 200 after the third bundle 216 may be monitored a second scrubber inlet temperature element 236. The temperatures of the exhaust gas 200 before and after the third bundle 216 may be used to adjust a speed of the air cooler fan 215 to adjust its operation.

[0097] After cooling, the exhaust gas 200, having lost further of its temperature, moves on to the second stage suction scrubber 278 through the second scrubber inlet line 228. The second stage suction scrubber 278 may comprise a second stage level transmitter 274 to measure a level of condensed water separated in the second stage suction scrubber 278, with the water directed to the water conditioning tank 322 through a second stage scrubber control valve 276. The exhaust gas 200 exits the second stage suction scrubber 278 through a conditioning tank inlet line 271. A pressure at the discharge of the second stage 248b may be regulated by a second stage scrubber pressure transmitter 272 and by a second control valve 270.

[0098] The water from the first and second stage scrubbers 268 and 278 may be directed to the water conditioning tank 322 via a shared line 281 .

[0099] If the compressor 248 comprises more than two stages, the same approach applies. Additional ones of the bundles may be added to the air cooler 214 to manage the temperature of the exhaust gas 200 between successive stages of the compressor 248.

[0100] The compressor 248 is configured to boost the pressure of the exhaust gas 200 to between approximately 2.5 Mpa and 10 Mpa, depending on the operating temperature of the absorber 360. To enhance the solubility of CO2 in water, it may be necessary not only to increase the pressure of the exhaust gas 200 but also to lower its temperature before it enters the absorber 360, which is configured for dissolving CO2 in water.

[0101] Once the exhaust gas 200 exits the air cooler 216, the high-pressure exhaust gas 200, having shed some of its heat at the air cooler 216 and reduced in volume by losing most of its water through water generation, moves into a gas cooling coil 320, which may be submerged in the water conditioning tank 322. The gas cooling coil 320 is an immersed heat exchanger and is configured to lower the temperature of the exhaust gas 200 down to between approximately 5°C and 23°C.

[0102] A water cooling coil 330 may also be submerged in the water conditioning tank 322. The water cooling coil 330 is an immersed heat exchanger that cools the water within the water conditioning tank 322 to a temperature ranging from approximately 3°C to 23°C. A conditioning tank temperature element 328 on the water conditioning tank 322 is configured to regulate a speed of a positive displacement refrigeration compressor 332 to maintain the water temperature within this range. As a speed of the positive displacement refrigeration compressor 332 is increased, so does a circulation rate of refrigerant. A coolant pressure transmitter 340 may ensure that the outlet pressure of the positive displacement refrigeration compressor 332 is maintained and does not exceed the discharge piping's rated capacity. A coolant temperature element 342 is configured to modulate a speed of a condenser air cooler 334 to maintain it operating within optimal limits. Additionally, an expansion valve temperature sensor 346 is configured to control an expansion valve 344 to lower the pressure, thereby achieving a desired temperature at the water cooling coil 330.

[0103] The exhaust gas 200, with a temperature ranging from about 5°C to 23°C, enters the absorber 360 from the gas cooling coil 320 through an absorber gas inlet line 361 . The exhaust gas 200 may enter the absorber 360 through a lower connection.

[0104] Cold water may be drawn from the water conditioning tank 322 to the absorber 360 by a booster pump 352 through an absorber water inlet line 351. The booster pump 352 may be of a fixed or variable speed type. If the booster pump 352 is of variable speed, its speed may be controlled by a booster pump suction flow element 350 and a booster pump discharge pressure transmitter 354. The discharge of the booster pump 352 may be connected to the suction of a main pump 356. A speed of the main pump 356 may be adjusted based on the pressure setpoint of a main pump discharge pressure transmitter 358. This is to ensure that water enters the absorber 360 at a pressure of between approximately 2.5 Mpa and 10 Mpa. The water may enter the absorber 360 through an upper connection.

[0105] The absorber 360 comprises two sets of packings 362, although more may be used depending on the performance and efficiency of available packings. The exhaust gas 200 may enter the absorber 360 at pressures ranging from approximately 2.5 Mpa to 10 Mpa and temperatures between about 5°C to 23°C. The pressure and temperature are chosen within these ranges to maintain CO2 solubility between approximately 5.0-6.5 kg CO2/IOO kg H2O.

[0106] In some embodiments, the exhaust gas 200 entering the absorber 360 should maintain a pressure that is at least 50 kPa higher than that of the water entering the absorber 360. The pressure and temperature within the absorber 360 may be monitored by an absorber pressure transmitter 372 and an absorber temperature element 366, respectively. A back pressure control valve 368 may be used to regulate the pressure within the absorber 360, keeping it between approximately 2.5 Mpa and 10 Mpa, based on the temperature recorded by absorber temperature element 366. The control logic 70 may be configured to manage the pressure and temperature within the absorber 360 to optimize the solubility of CO2 in water.

[0107] The exhaust gas 200 exiting the absorber 360 may be either CO2-free air, which is released into the atmosphere in CONFIG-2, or CO2-free syngas in CONFIG- 3, which may be directed to a synthetic fuel generation unit 524 via an absorber gas discharge line 310. The composition of the syngas 526 in the absorber gas discharge line 310 may be examined by a gas discharge analyzer 304 to assess the effectiveness of the CO2 removal process, while a gas discharge flowmeter 370 is configured to track the volume of exhaust gas 200 exiting the absorber 360.

[0108] The CO2-rich water exits the absorber 360 through an absorber water discharge line 381 . The absorber water discharge line 381 may exit the absorber 360 from a bottom connection. An absorber water discharge flowmeter 380 is configured to measure a flow rate of the water from the absorber 360 to the flash drum 390, and an absorber water discharge temperature element 382 is configured to monitor a temperature of the water within the absorber water discharge line 381 . An absorber level transmitter 364 may be configured to control an absorber water discharge control valve 384 to maintain the water level within the absorber 360.

[0109] A flash drum level transmitter 386 may be configured to measure a water level within the flash drum 390. If the flash drum level transmitter 386 detects a water level within the flash drum 390 above a predetermined high setpoint, it may be configured to increase the speed of a circulation pump 400 to reduce the water level within the flash drum 390. The circulation pump 400 is configured to pump water out of the flash drum 390 through a flash drum water discharge line 391 . If the circulation pump 400 is at its maximum speed but still cannot reduce the water level within the flash drum 390 below the predetermined high setpoint, the flash drum level transmitter 386 may be configured to close the absorber water discharge control valve 384, thereby restricting the flow of water from the absorber 360 to the flash drum 390. If the flash drum level transmitter 386 detects a water level within the flash drum 390 below a predetermined low setpoint, the flash drum level transmitter 386 may be configured to stop the circulation pump 400.

[0110] The captured CO2, in gas form, exits the flash drum 390 through a flash drum gas discharge line 301. A flash drum pressure transmitter 388 is configured to maintain a pressure within the flash drum 390 at approximately 140 kPa by adjusting a flash drum gas discharge control valve 394 on the flash drum gas discharge line 301. The temperature within the flash drum 390 may be regulated by the flash drum temperature element 392, which may be configured to adjust the heating coil bypass control valve 246 and the heating coil inlet control valve 256. Operating at approximately 140 kPa enables the flash drum 390 to separate CO2 from water at various temperatures, with higher temperatures improving CO2 recovery efficiency. The heating coil 316 is configured to cool the exhaust gas 200 by transferring heat to the water in the flash drum 390 before exhaust gas 200 enters the first bundle 220 of the air cooler 214, thereby reducing the thermal load on the air cooler 214 and potentially allowing for a smaller size for the air cooler 214. This heat recovery scheme may aid in overall energy savings and enhancing CO2 extraction efficiency.

[0111] The pH of water at the discharge of the circulation pump 400 may be measured by a pH meter 404. The control logic 70 may be configured to maintain the pH of the water downstream of the circulation pump 400 between approximately 6 and approximately 9. If the pH meter 404 detects that the pH is outside of this range, the control logic 70 may be configured to close a return control valve 406 between the water conditioning tank 322 and the circulation pump 400. At the same time, the control logic 70 may be configured to open a purge water line control valve 410 to allow water to flow from the circulation pump 400 to a vaporizer 416. The total flow rate of the purge water that leaves the system 10 may be metered by a purge flowmeter 412. The conditioning tank isolation valve 84 may be opened to let the same flow of water to enter the water conditioning tank 322 to compensate for the amount of water that has left the system 10.

[0112] In some embodiments, once the water level inside the vaporizer416 reaches approximately 40%, a vaporizer heater 420 may be turned on. Once the water level inside the vaporizer 416 drops to approximately 10%, the vaporizer heater 420 may be turned off. The setpoints for turning on and off the vaporizer heater 420 may be adjusted. Once the pH returns back to the acceptable range (e.g. between approximately 6 and 9), the control logic 70 may be configured to close the purge water line control valve 410 and the conditioning tank isolation valve 84.

[0113] If the pH inside the water conditioning tank 322, as measured by a tank pH meter 326, exceeds approximately 9 or falls below approximately 6, the control logic 70 may be configured to respond by closing the return control valve 406, thereby preventing water from returning from the flash drum 390 to the water conditioning tank 322. The control logic 70 may then be configured to open the purge water line control valve 410 to direct the purge water to the vaporizer 416. The tank pH meter 326 may use the same logic as the pH meter 404, opening and closing the same valves to maintain the pH value between approximately 6 and approximately 9. [0114] The pH monitoring and control, combined with the integrated water generation system and water makeup logic for CO2 absorption and recovery, add a unique feature to the control logic 70.

[0115] The captured CO2, in gas phase, flows through the flash drum gas discharge line 301 and exits the carbon capture subsystem. The flow rate through the flash drum gas discharge line 301 may be monitored by a flash drum gas discharge flowmeter 396 and the purity of the captured CO2 may be assessed by a CO2 analyzer 302. In CONFIG-1 , the CO2 may be sent to the CO2 utilization unit 522 for utilization and storage. In CONFIG-2 and CONFIG-3, the CO2 may be directed to the synthetic fuel generation unit 524. Although the synthetic fuel generation unit 524 in CONFIG-2 and CONFIG-3 may be provided by a third party, it may also be integrated into the system 10, sharing resources with other components to boost productivity by improving energy saving and efficiency. Fig. 8 depicts the boundaries for the system 10.

[0116] As discussed above, each of the configurations may be operated in three modes (i.e. Mode 1 , Mode 2, and Mode 3). In addition, Mode 2 may operate in three sub-modes (i.e. Mode 2A, Mode 2B, and Mode 2C).

[0117] In Mode 1 , the atmospheric air 100 is utilized for AWG, with the air cooler valve 232, the block valve 76, and the evaporator gas inlet isolation valve 68 maintained in the closed position.

[0118] In Mode 2, the exhaust gas 200 is relied upon solely as the input for the system 10. In this mode, the main intake louver 12 is closed, and the damper valve 62 channels all of the exhaust gas 200 directly to the suction line 64, bypassing the condenser 50.

[0119] In Mode 2A, the exhaust gas 200 is directed through the evaporator 16 for additional cooling and to maximize water extraction from the exhaust gas 200. In this arrangement, the evaporator bypass valve 72 is closed. The water transfer valve 66 and the evaporator gas inlet isolation valve 68 are kept open. In addition, the block valve 76 is kept open. This mode is optimal for scenarios with lower volumes of the exhaust gas 200 and when there is sufficient power availability at the site. [0120] In Mode 2B, the exhaust gas 200 is directed straight to the compressor 248 through the suction line 64. For this mode, the water transfer valve 66 and the evaporator gas inlet isolation valve 68 are closed, along with the block valve 76. The evaporator bypass isolation valve 72 remains open. This configuration is ideal for processing large volumes of the exhaust gas 200, particularly when the moisture content is high enough to produce the necessary water for carbon capture.

[0121] In Mode 2C, a portion of the exhaust gas 200 is routed through the evaporator 16, while the remainder is sent directly to the compressor 248 via the suction line 64. The two pathways converge upstream of the suction line temperature element 240 before entering the suction of the compressor 248. In this setup, the air cooler valve 232 and the water transfer valve 66 are fully open. The opening percentage of the evaporator gas inlet isolation valve 68, the evaporator bypass isolation valve 72, and the block valve 76 are adjusted based on the setpoints provided to first and second flow control loops 108, 110 at control logic 70. The distribution between the first and second control loops 108, 110 determines the proportion of gas passing through each line. Mode 2C is particularly useful when power availability at the site is inconsistent or when the volume or properties of the gas vary regularly. This flexibility allows the system 10 to operate at optimal load, maximizing water generation and carbon capture according to the available utilities.

[0122] In Mode 3, the main intake louver 12 and the water transfer valve 66 are open, allowing air to flow, while the evaporator gas inlet isolation valve 68 is closed. The damper valve 62 is set to direct all the air to the condenser 50. Additionally, the air cooler valve 232 and the evaporator bypass isolation valve 72 are open, while the block valve 76 is closed.

[0123] It will be appreciated by those skilled in the art that the preferred embodiment has been described in some detail but that certain modifications may be practiced without departing from the principles of the invention.

Claims

1. A method for water generation and carbon capture from atmospheric air and exhaust gas, the method comprising the steps of: introducing the atmospheric air into an evaporator, wherein the evaporator is configured to extract water from the atmospheric air; transferring at least some of the water extracted by the evaporator to a water conditioning tank; introducing the exhaust gas to a flash drum, wherein the flash drum is configured to cool the exhaust gas; transferring the exhaust gas from the flash drum to an air cooler, wherein the air cooler is configured to further cool the exhaust gas; transferring the exhaust gas between the air cooler and a compressor, wherein the compressor is configured to increase a pressure of the exhaust gas; transferring the exhaust gas from the compressor to an absorber; transferring at least a portion of the water from the water conditioning tank to the absorber, wherein the absorber is configured to effect a dissolution of CO2 from the exhaust gas into the water; and transferring the water from the absorber to the flash drum, wherein the flash drum is configured to separate the CO2 from the water.

2. The method of claim 1 , further comprising the step of transferring at least some of the water extracted by the evaporator to a water storage tank.

3. The method of claim 1 , further comprising the step of transferring at least some of the water extracted by the evaporator to a main water storage tank.

4. The method of claim 1 , further comprising the step of transferring at least a portion of the exhaust gas from the air cooler to the evaporator, wherein the evaporator is configured to extract water from the exhaust gas.

5. The method of claim 1 , wherein the compressor comprises a plurality of stages.

6. The method of claim 5, wherein the air cooler comprises a plurality of bundles.

7. The method of claim 6, wherein the step of transferring the exhaust gas between the air cooler and the compressor comprises transferring the exhaust gas between one of the plurality of bundles of the air cooler and one of the plurality of stages of the compressor.

8. The method of claim 5, wherein the compressor comprises one or more suction scrubbers.

9. The method of claim 1 , wherein the step of transferring the exhaust gas from the compressor to the absorber further comprises transferring the exhaust gas through an gas cooling coil in the water conditioning tank, wherein the gas cooling coil is configured to cool the exhaust gas.

10. The method of claim 9, wherein the water conditioning tank comprises a water cooling coil configured to cool the water within the water conditioning tank.

11 . The method of claim 1 , further comprising the step of transferring the CO2 separated by the flash drum to a synthetic fuel generation unit configured to generate synthetic fuel using the CO2.

12. A system for water generation and carbon capture from atmospheric air and exhaust gas, the system comprising: an evaporator configured to accept the atmospheric air and to extract water from the atmospheric air; a water conditioning tank configured to accept at least some of the water extracted by the evaporator; a flash drum configured to accept the exhaust gas and to cool the exhaust gas; an air cooler configured to accept the exhaust gas from the flash drum and to further cool the exhaust gas; a compressor configured to accept the exhaust gas from the air cooler and to increase a pressure of the exhaust gas; and an absorber configured to accept the exhaust gas from the compressor, wherein the absorber is further configured to accept at least a portion of the water from the water conditioning tank and to effect a dissolution of CO2 from the exhaust gas into the water; wherein the flash drum is further configured to separate the CO2 from the water.

13. The system of claim 12, wherein the evaporator is further configured to accept at least a portion of the exhaust gas from the air cooler and to extract water from the exhaust gas.

14. The system of claim 12, wherein the compressor comprises a plurality of stages.

15. The system of claim 14, wherein the air cooler comprises a plurality of bundles.

16. The system of claim 15, wherein the compressor and the air cooler are configured to exchange the exhaust air between one of the plurality of bundles of the air cooler and one of the plurality of stages of the compressor.

17. The system of claim 12, wherein the water conditioning tank comprises a gas cooling coil configured to cool the exhaust gas from the compressor.

18. The system of claim 17, wherein the water conditioning tank further comprises a water cooling coil configured to cool the water within the water conditioning tank.