Atmospheric water generation system and method

Abstract

The atmospheric water generating system comprises a water vapor consolidation system configured to increase the relative humidity of the controlled air stream prior to condensing water from the controlled air stream. The water vapor consolidation system comprises a fluid desiccant flow system configured to reduce the temperature of the desiccant to facilitate absorption of water vapor by the desiccant from the atmospheric air stream. The desiccant flow is then heated to facilitate evaporation of water vapor from the desiccant flow into the controlled air stream circulating within the system. The humidity of the controlled air stream is thereby increased above the relative humidity of the atmosphere to facilitate condensation of the water vapor into usable liquid water.

Description

[Technical Field]

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS This patent application claims priority to U.S. Provisional Patent Application No. 63 / 126,860, filed December 17, 2020, the entire contents of which are incorporated herein by reference.

[0002] This patent application is additionally related to U.S. Provisional Patent Application No. 16 / 782,808, filed February 5, 2020, which is a continuation of U.S. Provisional Patent Application No. 15 / 850,870, filed December 21, 2017, which claims priority from U.S. Provisional Patent Application No. 62 / 437,471, filed December 21, 2016, U.S. Provisional Patent Application No. 62 / 459,462, filed February 15, 2017, and U.S. Provisional Patent Application No. 62 / 459,478, filed February 15, 2017, the entire contents of all of which are incorporated herein by reference. [Background technology]

[0003] The amount of freshwater available for human consumption, plant irrigation, livestock herd maintenance, commercial and / or industrial use, and other purposes is generally outpaced by the amount of freshwater required for such purposes. Maintaining sufficient amounts of water for human and / or animal consumption and use has become increasingly costly in recent years, particularly in arid climates characterized by minimal regular rainfall and inaccessible other freshwater sources. Processes such as desalination, water filtration and / or purification, groundwater (e.g., aquifer) utilization, and other processes are often used in combination to supply freshwater to various geographic regions, depending on the relative availability and cost of each water-sourcing process.

[0004] Water shortages in certain geographic regions are also, at least in part, the cause of food shortages in certain areas of the globe. When water is not readily available for agricultural irrigation and livestock watering, basic nutritious foods may be difficult to grow and may be difficult or expensive to obtain on the free market.

[0005] Therefore, there is a need in general for processes to increase the availability of fresh water, especially in arid geographic regions and / or areas where there is no access to stored water or groundwater, or where the water is contaminated. Summary of the Invention

[0006] Certain embodiments are directed to a method for extracting water from air, comprising intersecting an atmospheric air stream with a desiccant-rich fluid flowing along a desiccant circulation loop in an absorber, extracting water vapor from the atmospheric air stream and absorbing the extracted water vapor to dilute the desiccant-rich fluid to form a diluted desiccant fluid; and distributing the diluted desiccant fluid along a solution flow path to an evaporator vessel. and directing the evaporated water vapor stream through a compressor to a condenser to form condensed water, the condenser defining at least a portion of a solution flow path, the condenser being configured to utilize sensible and / or latent heat transfer between the dilute desiccant fluid and the evaporated water vapor stream to reduce the temperature of the evaporated water vapor and condense the water vapor into condensed water, wherein the evaporated desiccant fluid stream is returned to the absorber as a desiccant-rich fluid. In certain embodiments, evaporated water vapor is directed from the MVC evaporator vessel through a compressor to a condenser to form condensed water, the condenser defining at least a portion of the solution flow path downstream of the at least one heat exchanger, the condenser configured to utilize sensible and / or latent heat transfer between the dilute desiccant fluid flowing through the condenser and the evaporated water vapor stream to reduce the temperature of the evaporated water vapor and condense the water vapor into condensed water, and the evaporated desiccant fluid stream is returned to the absorber as a desiccant-rich fluid.

[0007] In various embodiments, crossing the atmospheric air flow with the desiccant-rich fluid in the absorber includes providing the atmospheric air flow and the desiccant-rich fluid to the absorber in a counter-flow configuration, such that the atmospheric air flow flows from a lower portion of the absorber to an upper portion of the absorber, and the desiccant-rich fluid flows from the upper portion of the absorber to the lower portion of the absorber. In certain embodiments, the desiccant-rich fluid flows through a packing configuration in the absorber. In various embodiments, crossing the atmospheric air flow with the desiccant-rich fluid in the absorber includes providing the atmospheric air flow and the desiccant-rich fluid to the absorber in a cross-flow configuration, such that the atmospheric air flow flows from a first side of the absorber to an opposite second side of the absorber, and the desiccant-rich fluid flows from the upper portion of the absorber to the lower portion of the absorber at least substantially perpendicular to the atmospheric air flow. In certain embodiments, the atmospheric air flow flows from an air inlet adjacent the upper portion of the absorber on the first side of the absorber to an air outlet adjacent the lower portion of the absorber on the second side of the absorber. In various embodiments, the atmospheric air flow flows from an air inlet on a first side of the absorber adjacent a lower portion of the absorber to an outlet on a second side of the absorber adjacent an upper portion of the absorber. In certain embodiments, the method further includes, before crossing the atmospheric air flow with the desiccant-rich fluid, passing the desiccant-rich fluid through a heat exchanger cooled by a cold water stream, the cold water stream being cooled via at least one of a geothermal cooling system or a chiller before being introduced into the heat exchanger.

[0008] In various embodiments, the one or more heating subsystems include a heater positioned downstream of the at least one heat exchanger, and the method further includes heating the diluted desiccant fluid via the heater. In certain embodiments, the desiccant circulation loop includes a plurality of valves for reconfiguring a flow path of the desiccant fluid, and the method includes configuring the plurality of valves to redirect the diluted desiccant fluid to an absorber inlet as a desiccant-rich fluid for one or more fluid flow cycles before flowing the diluted desiccant fluid along the solution flow path, and configuring the plurality of valves to flow the diluted desiccant fluid along the solution flow path.

[0009] In certain embodiments, the method further includes directing the evaporated desiccant fluid stream to a second evaporator vessel to evaporate additional water vapor from the evaporated desiccant fluid stream before returning the evaporated desiccant fluid stream to the absorber.

[0010] Various embodiments provide a system for extracting water from atmospheric air, the system comprising: an absorber configured to dilute the desiccant fluid from a desiccant-rich fluid state to a dilute desiccant fluid state by absorbing water vapor from the atmospheric air passing through the desiccant fluid in the absorber; an evaporator vessel configured to condense the desiccant fluid from the dilute desiccant fluid by evaporating water vapor from the desiccant fluid and direct the evaporated water vapor toward a compressor; and a desiccant flow path from the absorber to the evaporator vessel for providing desiccant fluid from the absorber to the evaporator vessel, the desiccant flow path being one or and a condenser configured to condense water vapor after the compressor increases the vapor pressure of the water vapor, the condenser defining at least a portion of the desiccant flow path and configured to utilize sensible and / or latent heat transfer between the desiccant fluid and the water vapor stream flowing through the condenser to reduce the temperature of the water vapor and condense the water vapor into condensed water. In certain embodiments, the evaporated water vapor is directed from the evaporator vessel through the compressor to the condenser to form condensed water, the condenser defining at least a portion of the solution flow path downstream of the at least one heat exchanger, the condenser configured to utilize sensible and / or latent heat transfer between the dilute desiccant fluid flowing through the condenser and the evaporated water vapor stream to reduce the temperature of the evaporated water vapor and condense the water vapor into condensed water. The evaporated desiccant fluid stream is returned to the absorber as a desiccant-rich fluid.

[0011] In certain embodiments, the absorber interior defines a plurality of packing components, a desiccant inlet proximate an upper end of the absorber, and a desiccant outlet proximate a lower end of the absorber, the packing components configured so that liquid desiccant flowing from the desiccant inlet to the desiccant outlet flows across the plurality of packing components. In various embodiments, the absorber additionally defines an atmospheric inlet proximate a lower end of the absorber and an atmospheric outlet proximate an upper end of the absorber. In various embodiments, the method further includes an input heat exchanger in a portion of the desiccant flow path upstream of the absorber, the input heat exchanger being cooled by a cold water stream, the cold water stream being cooled via a geothermal cooling system before being introduced into the heat exchanger. In certain embodiments, the one or more heating subsystems include a heater positioned downstream of at least one heat exchanger. In various embodiments, the desiccant flow path is configurable via multiple valves between a first configuration in which the desiccant fluid leaving the absorber in a dilute state is diverted to the absorber inlet to be provided to the absorber as a rich desiccant fluid, a second configuration in which the desiccant fluid leaving the absorber is directed to the evaporator vessel, a third configuration in which the desiccant fluid leaving the evaporator vessel is diverted to the evaporator vessel inlet, and a fourth configuration in which the desiccant fluid leaving the evaporator vessel is directed to the absorber inlet to be provided to the absorber as a rich desiccant solution.

[0012] In certain embodiments, the evaporator vessel is a first evaporator vessel, and the system further includes a second evaporator vessel connected downstream relative to the first evaporator vessel such that desiccant solution exiting the first evaporator vessel is directed into the second evaporator vessel. In various embodiments, the system further includes a second set of one or more heating subsystems located between the first evaporator vessel and the second evaporator vessel, the second set of one or more heating subsystems including a second heat exchanger for exchanging heat from the desiccant fluid exiting the second evaporator vessel with the desiccant fluid passing to the second evaporator vessel. In various embodiments, the system further includes a water tank for holding condensed water.

[0013] Reference is now made to the accompanying drawings, which are not necessarily drawn to scale. [Brief explanation of the drawings]

[0014] [Figure 1] FIG. 1 is a schematic diagram of an air preconditioning system and a condenser according to one embodiment. [Figure 2A] FIG. 1 is a schematic diagram of a batch vapor consolidation system in series with a vapor condensation system according to one embodiment. [Figure 2B] FIG. 1 is a schematic diagram of a batch steam consolidation system in series with a steam condensation system according to one embodiment. [Figure 3A] FIG. 1 is a schematic diagram of a continuous steam consolidation system in series with a water vapor condensation system according to one embodiment. [Figure 3B] FIG. 1 is a schematic diagram of a continuous steam consolidation system in series with a water vapor condensation system according to one embodiment. [Figure 4] FIG. 1 is a diagram of an exemplary implementation of a steam consolidation system with an agriculture module, according to one embodiment. [Figure 5] FIG. 10 is a diagram of another exemplary implementation of a steam consolidation system with an agriculture module, according to one embodiment. [Figure 6] FIG. 1 illustrates an automatic planting mechanism according to one embodiment. [Figure 7] FIG. 1 is an exploded view of a surface overlay according to one embodiment. [Figure 8] 1 is an exemplary diagram of a surface covering panel secured to a support frame. [Figure 9] FIG. 1 is a schematic diagram of a steam consolidation system including mechanical steam consolidation according to one embodiment. [Figure 10] FIG. 1 is a schematic diagram of a steam consolidation system including mechanical steam consolidation according to one embodiment. [Figure 11] FIG. 10 illustrates an alternative fluid flow path surrounding an MVC evaporator vessel in accordance with certain embodiments. [Figure 12] 10A-10C illustrate alternative fluid flow paths surrounding an MVC evaporator vessel in accordance with certain embodiments. [Figure 13] 10A-10C illustrate alternative fluid flow paths surrounding an absorber in accordance with certain embodiments. [Figure 14] 10A-10C illustrate alternative fluid flow paths surrounding an absorber in accordance with certain embodiments. [Figure 15] 10A-10C illustrate alternative fluid flow paths surrounding an absorber in accordance with certain embodiments. [Figure 16A] FIG. 1 illustrates exemplary packing components for use as a structured packing arrangement according to one embodiment. [Figure 16B] FIG. 1 illustrates an exemplary packing component for use in a collection of multiple packing components in a random packing configuration according to one embodiment. DETAILED DESCRIPTION OF THE INVENTION

[0015] The present disclosure will more fully describe various embodiments with reference to the accompanying drawings. It should be understood that some, but not all, embodiments are shown and described herein. Indeed, embodiments may take many different forms, and thus, the present disclosure should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will satisfy applicable legal requirements. Like reference numerals refer to like elements throughout.

[0016] Overview AWG systems utilize condensing coils and / or plate systems to extract water from the air. During the water extraction process of an integrated AWG process, moist air (having humidity greater than 0%) is passed over / across / through cooled condensing surfaces (e.g., coils, plates, etc.) to reduce the temperature of the moist air below the dew point, thus causing water vapor in the moist air to condense on the condensing surfaces. The condensed water is then directed into a collection chamber (e.g., a tank, basin, etc.) for storage and use.

[0017] In certain embodiments, the AWG system additionally includes one or more air compression mechanisms, air cooling mechanisms, or air humidity increasing mechanisms to optimize the amount of water extracted from the air (per unit source air intake into the AWG system).

[0018] In certain embodiments, the AWG system may be integrated with one or more carbon dioxide filtration / capture modules, one or more greenhouse modules, one or more power generation modules, etc. For example, source intake air to the AWG system may be routed through a carbon dioxide capture system before exhausting the dry, dehumidified air to the surrounding environment. The captured carbon dioxide may be stored in a tank for later processing or may be released (e.g., in monitored amounts) into one or more greenhouse modules to increase the carbon dioxide concentration within the greenhouse, thereby increasing crop growth efficiency.

[0019] Additionally, a power generation module, which may include one or more renewable energy power generation systems, such as solar / photovoltaic, geothermal, etc., or hydrocarbon fuel-based power generation systems, may be integrated with the AWG system to provide the electrical and / or thermal energy input required for the AWG process. If such a power generation module produces carbon dioxide or other exhaust gases, the power generation module exhaust gases can be routed through a carbon dioxide capture module to reduce the carbon dioxide production of the integrated system.

[0020] Atmospheric Water Resources The atmosphere is about 3,100 cubic miles (mi 3 ) or 12,900 cubic kilometers (km 3) of water. This amount, by volume, is roughly equal to the total amount of water held by the Great Lakes. As a natural resource, water vapor is constantly replenished by the natural closed-loop water cycle, which provides a nearly unlimited supply of water that can be extracted from the air without adverse environmental effects.

[0021] Atmospheric Water Generation The AWG process includes systems and methods for extracting water vapor from atmospheric source air by condensing the water vapor and recovering the condensed liquid water. Certain embodiments can be combined with carbon dioxide capture systems as discussed herein. Certain embodiments include preconditioning and / or compressing raw source air (e.g., at atmospheric conditions) to facilitate the water extraction process, and / or condensing water vapor trapped in the raw source air (e.g., by increasing the humidity of at least a portion of the raw source air) to maximize the amount of water vapor that can be extracted from a given unit volume of source air. As discussed herein, treated source air can be compressed, compacted, and / or otherwise manipulated through one or more processes, for example, to facilitate the water extraction process.

[0022] Finally, various embodiments of the AWG process include a condensation mechanism that can direct source air (untreated source air and / or treated source air as discussed herein) over one or more condensing surfaces, each having a surface temperature below the dew point of the source air. As the source air flows over and / or around the condensing surfaces, the temperature of the source air adjacent the condensing surfaces drops (through convective heat transfer), water vapor in the source air condenses on the condensing surfaces, and the condensed liquid water flows into a storage vessel (e.g., a collection tank) and / or to one or more associated modules (e.g., greenhouse modules) for immediate use.

[0023] Air preconditioning As mentioned above, raw source air can be preconditioned to facilitate a water extraction process that ultimately condenses the water vapor into usable liquid water. In certain embodiments, the preconditioning process can include compressing the air to increase the vapor pressure of the air (thereby biasing a larger volume of water toward the liquid state rather than the vapor state) and / or to reduce the temperature of the source air to a temperature closer to the dew point. In certain embodiments, the air preconditioning systems described herein may be utilized before and / or after a humidity augmentation system, such as a desiccant-based humidity augmentation system as described herein. Certain air preconditioning systems may be utilized before and / or after a carbon dioxide capture system as discussed herein.

[0024] By way of example only, the air preconditioning process may include a series of compressors / pumps, venturi valves, vortex valves, manifolds, etc. collectively configured to reduce the temperature of the source air closer to the air dew point and / or increase the pressure of the air before removing water vapor from the air (e.g., through condensation or desiccant absorption). For example, raw source air may be drawn into the air preconditioning system via a vacuum created at the inlet through compressor 101 (e.g., a turbine / blower compressor having multiple stators or variable-pitch turbine blades controllable via a servo motor) and / or a centrifugal fan configured to increase the pressure of the raw air entering the air preconditioning system. In certain embodiments, compressor 101 and / or centrifugal fan may be rotated via one or more electric motors (which may receive input power from one or more power systems in communication with the air preconditioning system) mechanically coupled to compressor 101 and / or centrifugal fan via gear transmissions, belt drives, chain drives, etc.

[0025] In embodiments including a centrifugal fan, particles, dust, and other heavy air contaminants are rotated toward the outermost edge of the centrifugal fan, where they are removed from the airflow and expelled from the air pre-conditioning system.

[0026] 1, the filtered air may be directed into a carbon dioxide capture column 102 where it is passed over a fixed absorption bed configured to absorb carbon dioxide from the air, as discussed in more detail herein. The carbon dioxide may be separated via a compressor 103 and directed outwardly from the air stream.

[0027] In certain embodiments, the filtered air (with reduced carbon dioxide content) can then be directed further through an air preconditioning system into a primary manifold where the air is split in a ratio selected by a variable plenum / valve. From the primary manifold, a first air stream continues along with the bulk air stream, and a second air stream is directed to a vortex tube manifold as discussed herein.

[0028] The bulk airflow may proceed through one or more venturi valves, each configured to reduce the pressure and temperature of the bulk airflow (the volume and amount of air remains constant across each venturi valve while the pressure is reduced, thereby reducing the temperature of the airflow proportionally), and / or through a precooler 104 (e.g., a heat exchanger through which a cooling fluid is passed). After processing through the one or more venturi valves and / or precooler 104, the bulk airflow may proceed to a temperature measurement section, where the temperature (e.g., dry-bulb and wet-bulb temperatures) of the bulk airflow are measured by one or more temperature measurement devices (e.g., thermometers) to determine the dew point of the bulk airflow. Output from the temperature measurement devices may be utilized by a controller to mix the bulk airflow with at least a portion of the vortex-cooled airflow to lower the temperature of the bulk air to closer to the air dew point. For example, the controller may be in electrical communication with an electromechanical mixing valve that can be selectably opened and closed to vary the amount of vortex-cooled air introduced into the bulk airflow. Based on the determined dry-bulb and / or wet-bulb temperatures (as monitored by the controller), the controller may send a signal to a motor to move the electromechanical valve to a desired position to obtain a desired mix of vortex-cooled air with the bulk airflow.

[0029] The vortex-cooled air begins as a second air stream exiting the primary manifold. The second air stream exits the primary manifold and proceeds to a vortex tube manifold, where it is pressurized (e.g., via a compressor 105) to a pressure sufficient to achieve a temperature drop of approximately 70 to 150 degrees Fahrenheit for the air traveling through one or more vortex tubes 106. For example, the air may be pressurized to at least approximately 70 to 120 PSI before being directed into one or more vortex tubes 106. Each vortex tube 106 includes an inlet port that directs the airflow tangentially into the interior spin chamber. As the air enters the spin chamber, it gains some angular momentum, causing dense warm air to move toward the outer edges of the spin chamber and exit through the exhaust valve. In certain embodiments, the warm air can be utilized to heat the carbon dioxide capture column 102, as shown in FIG. 1. The remaining vortex-cooled air moves toward the center of the spin chamber and exits through the vortex outlet. As mentioned above, the vortex-cooled air can mix with the bulk air flow to lower the temperature of the bulk air flow closer to the air dew point. As yet another alternative, the vortex-cooled air may be utilized to cool the precooler 104 through which the bulk air passes.

[0030] In certain embodiments, the mixed and cooled bulk air stream is then directed into condensation chamber 107, where water vapor in the air condenses into liquid water. By way of example only, the bulk air stream may be directed over a series of condensation surfaces (e.g., cold plates, screens, tubes, etc.) configured to reduce the local temperature of the air at the condensing surfaces below the air dew point, thereby causing water vapor to condense on the condensing surfaces. The condensed water may then be routed from the condensing surfaces into holding chamber 108 for collection and later use. However, it should be understood that any of a variety of condensation mechanisms may be used. For example, as discussed herein, one or more desiccant-based condensation mechanisms may be utilized to more effectively remove water vapor from the bulk air stream. Moreover, in certain embodiments, an air preconditioning system may be omitted, and untreated air may be filtered and / or directly directed to the condensation chamber. Such embodiments may have lower input power requirements and therefore reduce the amount of power needed to generate water.

[0031] Certain air preconditioning system embodiments may include, instead of or in addition to the vortex and venturi valve mechanisms discussed herein, one or more filters (e.g., woven-based air filters, nonwoven-based air filters, etc.), one or more refrigeration systems (e.g., warm air is passed through a heat exchanger to lower the temperature of the air closer to the dew point), etc.

[0032] Desiccant-based air humidity enhancement system As noted above, certain embodiments include one or more subsystems configured to increase the humidity of a portion of the source air to increase the amount of water that can be extracted from the source air. Specifically, water vapor can be extracted from a first larger volume of source air and reintroduced into a second, smaller volume of source air, thereby increasing the humidity of the second volume of source air before the water vapor in the source air compacts and the water vapor in the second volume of source air condenses into liquid water.

[0033] The desiccant-based air humidity augmentation system includes at least one air scrubber containing a column of aqueous desiccant. The desiccant may be selected from any of a variety of ionic solutions capable of absorbing water, such as lithium chloride (LiCl), lithium bromide (LiBr), calcium chloride (CaCl), triethylene glycol, etc. In certain embodiments, the desiccant fluid may include a mixture of ionic solutions, such as a mixture of LiCl and CaCl solutions. The desiccant may be dissolved in water to provide a concentrated desiccant fluid that can be pumped (e.g., via a liquid pump) through at least one desiccant column.

[0034] Moreover, the amount of water vapor that can be absorbed by the desiccant (and / or released into the air by the desiccant) depends on the vapor pressure and temperature of the closed system containing the aqueous desiccant and air adjacent to the desiccant column. Thus, various embodiments are configured to absorb water from the air into the aqueous desiccant while the vapor pressure and temperature within the closed system are high and low, and those same embodiments are configured to evaporate water from the desiccant while the vapor pressure and temperature are low and high.

[0035] Single-stage batch steam consolidation A single-stage batch vapor consolidation system utilizes a single desiccant column that is configurable between an absorption phase and an evaporation phase. Because the function of the desiccant column between the absorption phase and the evaporation phase depends at least in part on the temperature of the closed system, the desiccant column can be switched between the absorption phase and the evaporation phase based on the ambient temperature surrounding the system. For example, the system can operate in the absorption phase during cooler periods (e.g., overnight) and in the evaporation phase during warmer periods (e.g., daytime).

[0036] 2A and 2B illustrate a single-stage batch vapor consolidation system according to various embodiments. Each figure highlights the fluid flow path between the absorption and evaporation phases, respectively. The single-stage batch vapor consolidation system includes an aqueous desiccant column 201, a desiccant swing tank 202 configured to hold excess desiccant fluid, a water tank 203 configured to hold removed water, and an air scrubber including one or more liquid and / or air heat exchangers.

[0037] During low-temperature ambient periods (e.g., nighttime hours between sunset and sunrise), the single-stage vapor consolidation system can operate in an absorption phase, during which water vapor from the ambient air is absorbed by the aqueous desiccant fluid passing through the desiccant column. Before the absorption phase begins, the desiccant fluid is highly concentrated, making it highly receptive to absorbing additional water. As the absorption phase progresses, air carrying water vapor passes (e.g., by turbulence) through the desiccant column 201, bringing the air into contact with the desiccant fluid. The water vapor in the air is absorbed by the desiccant fluid, thereby decreasing the humidity of the air (resulting in drier air exiting the desiccant column), increasing the volume of the desiccant fluid, and reducing the concentration of the desiccant fluid. Excess desiccant fluid from the desiccant column 201 is stored in a swing tank 202, which has an available volume greater than the volume of the desiccant column 201.

[0038] In certain embodiments, the desiccant column 201 can be embodied as a membrane-separated desiccant column, with a desiccant flow path on a first side of the porous membrane and an air flow path on an opposite second side of the porous membrane. By separating the air flow path from the desiccant flow path, the desiccant salt itself can enter the air flow path and prevent undesirable mass flow ultimately exiting the AWG system. Based on osmotic water flow from the air through the membrane into the desiccant fluid, water can be absorbed from the air by the desiccant fluid. Water vapor condenses on the second side of the membrane, travels through the membrane pores by capillary action, and can be absorbed by the high-salt-content concentrated desiccant fluid.

[0039] As water is absorbed, the temperature of the desiccant fluid increases due to mass and heat transfer from the air to the desiccant fluid. Accordingly, the desiccant fluid is circulated through an absorption loop, highlighted in FIG. 2B, which includes a desiccant column 201, and a refrigeration recirculation loop configured to maintain the temperature of the desiccant fluid below the ambient temperature of the system. In certain embodiments, the desiccant fluid may be circulated through a swing tank 202 as part of the refrigeration recirculation loop.

[0040] Any of a variety of cooling mechanisms may be utilized in the cooling recirculation loop. For example, the cooling recirculation loop may include a dual-fluid heat exchanger 204 (e.g., a shell-and-tube heat exchanger, a counterflow heat exchanger, etc.) in which a liquid desiccant fluid flows through a first fluid flow path and a cooling fluid (e.g., a refrigerant, chilled air, etc.) can pass through a second fluid flow path, thereby transferring heat from the liquid desiccant to the cooling fluid. The cooling fluid may be maintained at a desired cooling temperature via a conventional refrigeration cycle, geothermal cooling, etc. As yet another example, the liquid desiccant may pass through a geothermal cooling loop 205 (e.g., by directing the liquid desiccant through a series of underground conduction tubes that allow heat to pass from the liquid desiccant to the soil), etc.

[0041] The absorption phase of the single-stage vapor compression system may be stopped when the ambient temperature begins to rise (e.g., around sunrise) and / or the desiccant fluid becomes supersaturated, resulting in the desiccant fluid substantially ceasing to absorb additional water from the air passing at least partially through the desiccant column 201. In certain embodiments, the concentration of the desiccant fluid may be monitored by a control system, which may interrupt the absorption phase by ceasing various fluid pumps, air fans, etc. from moving various fluids through the system upon determining that a trigger event has occurred. In certain embodiments, the trigger event may be identified as a threshold desiccant concentration in the desiccant fluid (e.g., the controller may stop the absorption phase when the desiccant fluid concentration drops below a threshold), a threshold rate of concentration change (e.g., the desiccant fluid concentration decreases by less than a threshold amount over a set period of time), etc. The triggering event may be based on other characteristics of the single stage vapor consolidation system, such as the temperature of the desiccant fluid (e.g., the temperature of the desiccant fluid increases above a threshold), the temperature of the source air (dry bulb and / or wet bulb) (e.g., the temperature of the ambient air surrounding the system increases above a threshold), the amount of desiccant fluid increasing above a threshold, etc.

[0042] When the absorption phase is stopped, the single-stage vapor consolidation system moves the desiccant fluid out of the refrigeration recirculation loop and into swing tank 202. In certain embodiments, at least a portion of the desiccant fluid in desiccant column 201 is pumped into the swing tank, such that after the absorption phase is stopped, the majority of the desiccant fluid is in the swing tank. In certain embodiments, after the absorption phase is stopped, at least 85% of the desiccant fluid is pumped into swing tank 202.

[0043] The single-stage vapor compression system can switch to the evaporation phase. In certain embodiments, the single-stage vapor compression system can switch to the evaporation phase upon detection of a trigger event by the controller. For example, the single-stage vapor compression system can switch to the evaporation phase in response to the ambient air temperature surrounding the single-stage vapor compression system increasing above a threshold temperature, the concentration of the desiccant fluid decreasing below a threshold concentration, etc. In various embodiments, the single-stage vapor compression system is configured to switch directly between the absorption phase and the evaporation phase. Thus, it should be understood that any of the trigger events referenced above as being used to determine the end of the absorption phase may also be used (e.g., simultaneously and / or sequentially) to initiate the evaporation phase.

[0044] However, it should be understood that in certain embodiments, the single-stage vapor compression system may be configured to enter a waiting phase between the end of the absorption phase and the beginning of the evaporation phase. For example, the single-stage vapor compression system may be configured to enter the waiting phase upon detection of a first trigger event (e.g., a decrease in the concentration of the desiccant fluid below a threshold level), and the single-stage vapor compression system may be configured to initiate the evaporation phase (and thus terminate the waiting phase) upon the occurrence of a second trigger event (e.g., an increase in the ambient temperature surrounding the single-stage vapor compression system above a threshold level).

[0045] During the evaporation phase, the air within the single-stage vapor consolidation system is circulated in a closed loop as shown in FIG. 2B, so that water vapor evaporating from the liquid desiccant does not exit the single-stage vapor consolidation system.

[0046] As air circulates through the closed loop of the single-stage vapor compression system, dilute desiccant fluid is pumped through the closed loop from swing tank 202, past / through heater 206, and through desiccant column 201 of the scrubber. In certain embodiments, swing tank 202 and / or desiccant column 202 can include heater 206 as shown in FIG. 2B, thereby eliminating the need for a separate heating mechanism. Accordingly, it should be understood that the heater mechanism may be embodied in any of a variety of forms, which may be implemented as part of swing tank 202, as part of desiccant column 201, or as a separate mechanism located within the closed loop of the desiccant flow. For example, the heater may include a resistance heater having a heating element positioned within the flow path of the liquid desiccant. As yet another example, the heater may include a dual-fluid heat exchanger in which a liquid desiccant flows through a first fluid flow path and a heating fluid (e.g., a heated gas, a heated liquid, etc.) flows through a second fluid flow path such that heat from the heating fluid is transferred to the liquid desiccant (e.g., via conductive heat transfer). As particular examples, the heat exchanger may include a shell-and-tube heat exchanger, a plate heat exchanger, or a counterflow heat exchanger. In such embodiments, the heating fluid may be heated using any of a variety of heating mechanisms, such as a resistive heater having a heater element within the fluid flow of the heating fluid, a solar heater in which the heating fluid flows through a series of solar heating tubes that absorb radiant and / or convective ambient heat, etc.

[0047] As yet another example, the desiccant fluid may flow through a solar heater 207 comprising a series of solar heating tubes that absorb radiant and / or convective ambient heat to heat the desiccant fluid to a desired temperature.

[0048] The heating mechanism of the closed-loop desiccant flow path may be configured to heat the temperature of the liquid desiccant fluid to reduce the vapor pressure of the closed system of air and liquid within the desiccant column. In certain embodiments, the heating mechanism is configured to heat the desiccant fluid to a steady-state temperature of at least about 65-95 degrees Celsius.

[0049] The evaporative phase of the single-stage batch vapor consolidation system may operate as a desalination system to remove water from the desiccant fluid. As the air and heated desiccant fluid pass through the desiccant column 201, water from the desiccant fluid evaporates into the air, thereby increasing the concentration of the desiccant fluid while simultaneously increasing the humidity of the air. This mass transfer reduces the temperature of the desiccant fluid, and a heating mechanism is configured to maintain the desiccant fluid at the desired elevated temperature.

[0050] As discussed in more detail herein, the increased humidity air can be directed through a condensation chamber 208 as part of a closed-loop air flow path to condense water from the air, reducing the humidity of the air and collecting the water as a usable liquid in the water tank 203. This simultaneously allows for the collection of usable water and maintains the humidity level of the air at a desired low level, maintaining a low vapor pressure within the desiccant column and encouraging the evaporation of water from the desiccant fluid.

[0051] In certain embodiments, the condensation chamber 208 may include a heat exchanger configured to receive the air entering the condensation chamber 208 and reduce the temperature of the increased humidity air exiting the desiccant column 201 to closer to the dew point of the air to increase the rate of condensation.

[0052] Various embodiments may additionally include a membrane desalination system 209 in series with the desiccant closed-loop flow path. In the membrane desalination system 209, the desiccant flow path can flow past a first side of a membrane, such that the desiccant fluid contacts the membrane as it travels along the desiccant flow path. The membrane can separate the desiccant fluid flow path from a water flow path for water collected from the condensation process described herein. The water flow path can pass through a second side of the membrane, such that the water contacts the second side of the membrane as it flows along the water flow path. In certain embodiments, mass transfer across the membrane can be driven by increasing the vapor pressure of the desiccant. This can be achieved by heating the liquid before contacting the membrane, using a vacuum to reduce the pressure on the second side of the membrane, or a combination of both. The water in the desiccant begins to permeate the membrane in a liquid state and exits the membrane in a vapor state. The water is then condensed using a heat exchanger (e.g., a condenser) and / or by contact with a cooler fluid (e.g., condensed water).

[0053] The membrane may comprise a porous membrane, such as a nonwoven membrane with small pore sizes. By way of example only, the membrane may comprise expanded polytetrafluoroethylene (ePTFE). As the desiccant fluid and water flow past opposite sides of the membrane, water molecules migrate (via capillary action) from the high salt content desiccant fluid through the membrane and into the water flow.

[0054] The membrane desalination system 209 can be positioned between the swing tank 202 and the desiccant column 201, such that the desiccant fluid first passes through the membrane system before entering the desiccant column 201. Thus, a first amount of water can be removed from the desiccant fluid in the membrane system before the desiccant fluid enters the desiccant column for additional water to evaporate therefrom.

[0055] Moreover, as mentioned above, the single-stage batch steam compression system may be part of an AWG system that includes one or more air preconditioning systems and / or carbon dioxide capture systems. For example, the air preconditioning system may be located upstream of the single-stage batch steam compression system, such that source air entering the AWG system first passes through the air preconditioning system before entering the single-stage batch steam compression system.

[0056] In certain embodiments, the AWG system may include an air preconditioning system as described above between the single stage batch steam consolidation system and the condensation chamber.

[0057] Single-stage continuous steam consolidation 3A-3B illustrate a single-stage continuous vapor consolidation system according to an exemplary embodiment, configured to continuously absorb water from air in an absorption desiccant column 500 and simultaneously evaporate the water into air in a second evaporative desiccant column 550. Absorption desiccant column 500 is fluidly connected to evaporative desiccant column 550 (e.g., via a series of closeable valves) so that desiccant fluid can flow between absorption desiccant column 500 and evaporative desiccant column 550 as needed. Briefly, while in absorption column 500, the desiccant fluid absorbs water from air entering the system via air input 501; the dilute desiccant fluid then exits the absorption column at solution outlet 502, passes through a series of fluid conduits, and enters evaporative column 550 at dilute input 551, where the water in the desiccant fluid is evaporated into a closed air stream. The desiccant-rich fluid exits the evaporative desiccant column at rich solution outlet 552 and proceeds into the absorption column at rich solution inlet 503 for another cycle. As shown, various conduits may be optionally closed to create closed-loop systems in absorber 500 and evaporative column 550, respectively.

[0058] As mentioned, the single-stage continuous vapor consolidation system comprises an absorption scrubber including an absorption desiccant column 500 and an evaporative scrubber including an evaporative desiccant column 550. In certain embodiments, the absorption desiccant column 500 operates at low temperatures (e.g., below ambient temperature) to facilitate absorption of water vapor from air (passing through the absorption desiccant column 500 from air inlet 501 to air outlet 504) into a desiccant fluid. Thus, as the desiccant-rich fluid is moved toward the absorption column 500, the desiccant fluid may pass through a refrigeration recirculation loop to maintain the temperature of the desiccant fluid at a desired temperature (e.g., ambient temperature or below ambient temperature). The refrigeration recirculation loop may have a configuration similar to the refrigeration recirculation loop described above.

[0059] By way of example only, the desiccant-rich fluid traveling toward the absorption column 500 (e.g., exiting the evaporator column) can be directed through a series of geothermal pipes that have heat transfer characteristics with the surrounding soil below the AWG system. The desiccant-rich fluid may pass directly through the series of geothermal pipes, or the desiccant-rich fluid may pass through a dual-fluid heat exchanger against a cooling fluid that is maintained at a desired low temperature via geothermal cooling. As yet another example, as shown in FIG. 3A, the desiccant fluid may pass through a heat exchanger (e.g., a shell-and-tube heat exchanger) to cool the desiccant fluid. The heat exchanger may be cooled via a cooling solution passing through a refrigeration circuit and / or other fluid cooling device 506 to absorb heat from the desiccant fluid before it enters the absorption column 500.

[0060] As yet another example, a single-stage water consolidation system may be located in proximity to a high-pressure gas well, such as a natural gas well, an oil well (where natural gas is extracted simultaneously with oil), etc. The high-pressure gas can be directed through one or more expansion valves to regulate and / or reduce the pressure of the incoming gas, which undergoes a rapid temperature reduction through the Joule-Thomson effect (according to the ideal gas equation of state, the pressure of the gas rapidly reduces across the valve while the volume and amount of gas remains substantially constant, thereby causing a proportionally rapid temperature reduction across the expansion valve). As described in the cited U.S. Provisional Patent Application No. 62 / 459,462, filed February 15, 2017, which is incorporated herein by reference in its entirety, the expanded, sub-cooled gas can pass through a heat exchanger 505 against a desiccant-rich fluid, thereby absorbing heat from the desiccant-rich fluid and reducing the temperature of the desiccant fluid before entering the absorption column 500. The expanded gases can then be directed outward from the AWG system, where they may be collected for their own use, combusted, utilized to generate electricity (e.g., via a steam turbine), and / or utilized to heat desiccant fluid entering an evaporator column, as discussed herein.

[0061] The absorption column 500 of the single-stage continuous vapor consolidation system may operate similarly to the absorption phase of the single-stage batch vapor consolidation system described above. As noted, the desiccant fluid is highly concentrated before entering the absorption column 500, making it highly receptive to absorbing additional water. As the desiccant fluid passes through the absorption column 500, air carrying water vapor simultaneously passes through the absorption column (e.g., by turbulence) and contacts the air with the desiccant fluid. The water vapor in the air is absorbed by the desiccant fluid, thereby decreasing the humidity of the air (resulting in drier air exiting the desiccant column), increasing the volume of the desiccant fluid, and decreasing the concentration of the desiccant fluid. As the volume of the desiccant fluid increases (and its concentration decreases), excess desiccant fluid is directed toward the evaporation column 550, as discussed herein. In certain embodiments, the absorption column 500 can be configured to create a concentration gradient of desiccant fluid therein such that a highly desiccant-rich fluid enters through a solution input 503 near a first end of the absorption column 500 (e.g., the top of the absorption column 500), travels through the absorption column 500, simultaneously absorbing water (thereby reducing the concentration of the desiccant fluid as it travels), and finally exits the absorption column 500 at a lower concentration at a solution outlet 502 near a second end of the absorption column 500 opposite the first end (e.g., the bottom of the absorption column 500). The absorption column 500 thereby has a concentration gradient between a high concentration portion at the first end and a lower concentration portion at the second end, such that a low concentration desiccant fluid exits the absorption column 500 and is directed to the evaporation column 550, while the desiccant fluid is constantly replenished with a high concentration desiccant fluid within the absorption column 500.

[0062] 3A, absorption column 500 may be part of a selectively closed loop of desiccant fluid that may be pumped through absorption column 500 and cooling heat exchanger 505 in a continuous loop without entering evaporator column 550. The closed loop may be configured to allow the desiccant fluid to absorb more water before entering evaporator column 550. In such an embodiment, the closed loop may be opened (e.g., by a controller system) upon the occurrence of a trigger event (e.g., upon measurement of a desired desiccant fluid concentration within the closed loop), as discussed in more detail herein, to allow the desiccant fluid to move into evaporator column 550.

[0063] Similar to the desiccant column discussed in the single-stage batch vapor consolidation system, the absorption column 500 can be embodied as a membrane-separated absorption column with a desiccant flow path on a first side of a porous membrane and an air flow path on a second, opposite side of the porous membrane. By separating the air flow path from the desiccant flow path, the desiccant salt itself can enter the air flow path and prevent unwanted mass flow ultimately exiting the AWG system. Water can be absorbed from the air by the desiccant fluid based on osmotic water flow from the air through the membrane into the desiccant fluid. Water vapor condenses on the second side of the membrane, travels through the membrane pores by capillary action, and can be absorbed by the high-salt desiccant-rich fluid.

[0064] As yet another example, the absorption column 500 can have a structured packing configuration defined by multiple corrugated baffles stacked within the column and positioned in alternating orientations (each orientation rotated 90 degrees relative to the adjacent orientation). The corrugated baffles create highly intricate fluid flow paths for the desiccant fluid and air, thereby increasing the overall available surface area of ​​the desiccant fluid exposed to the air within the column. This configuration maximizes the amount of water vapor absorbed by the desiccant fluid passing through the absorption column 500.

[0065] As described above, the absorption column 500 can be selectably operated in a closed loop, such that the desiccant fluid can be repeatedly recirculated through the cooling loop and the absorption column 500 until the desiccant fluid reaches a threshold concentration. Accordingly, a control mechanism can communicate with one or more sensors within the absorption column 500 (or external to the absorption column but within the closed absorption column loop) to monitor the concentration of the desiccant fluid within the absorption column loop. When the controller determines that the desiccant fluid concentration has dropped below a threshold concentration level, the controller can send operational signals to one or more valves to direct at least a portion of the desiccant fluid from the absorption column loop toward the evaporator column 550 and to direct more concentrated desiccant fluid from the evaporator column 550 into the absorption column loop. The controller can be configured to maintain the various valves in an open configuration until the measured concentration of the desiccant fluid in the absorption column 500 rises above the threshold concentration level, at which point the controller can send operational signals to the various valves to close them and re-establish the closed absorption loop. In certain embodiments, air can be directed continuously through the absorption column 500 regardless of whether the absorption loop is closed or open. However, in certain embodiments, air flow can be passed through the absorption column 500 only while the absorption loop is closed, and air flow can be prevented from entering the absorption column 500 while the absorption loop is in an open configuration. In such embodiments in which the absorption column 500 can be selectively operated in a closed loop, the single-stage continuous vapor consolidation system can further include a swing tank configured to support excess desiccant fluid when the concentration of the desiccant fluid is reduced and the absorption loop remains closed.

[0066] The diluted desiccant fluid exiting the absorption column 500 (or absorption loop) is directed toward an evaporation column 550, where water is evaporated from the desiccant fluid into a closed-air system. To facilitate evaporation of water from the desiccant fluid, the diluted desiccant fluid can be heated before and / or while in the evaporation column 550. For example, the evaporation column 550 may include an embedded heater 553 (e.g., a resistive heater) configured to maintain the desiccant fluid at a desired minimum temperature that facilitates evaporation of water from the desiccant fluid. As yet another example, the desiccant fluid may pass through a heating system before entering the evaporation column. For example, the heating system may include a solar thermal heating system 560 configured to utilize radiant and / or convective heat from the ambient environment to heat the desiccant fluid to facilitate water evaporation upon entry into the evaporation column 550. In certain embodiments, the desiccant fluid can be passed through a series of solar heated tubes (e.g., tubes having one or more associated solar collectors for heating the tubes and the fluid within the tubes based on collected radiant solar energy), or the desiccant fluid can be passed through a dual fluid heat exchanger 561 (e.g., a shell-and-tube heat exchanger) against a heating fluid, the heating fluid being heated from the series of solar heated tubes. In certain embodiments, the solar heating mechanism 560 may be supplemented by an electric heater, a combustion heater (e.g., using expanded gas from the gas expansion cooling mechanism described above), or the like, particularly during nighttime system use or when solar power is otherwise not available.

[0067] In various embodiments, the heating mechanism of the desiccant flow path may be configured to heat the temperature of the diluted desiccant fluid to reduce the vapor pressure of the fluid while the desiccant is present in the evaporation column 550. In certain embodiments, the heating mechanism is configured to heat the desiccant fluid to a steady-state temperature of at least about 65-95 degrees Celsius.

[0068] Evaporation column 550 may operate as a desalination column to remove water from the desiccant fluid. As the air and heated desiccant fluid pass through desiccant column 550, water from the desiccant fluid evaporates into the air, thereby increasing the concentration of the desiccant fluid while simultaneously increasing the humidity of the air. The air passing through the evaporation column may be part of a closed air loop (air does not enter or exit the closed loop) such that evaporated water from the diluted desiccant fluid does not fall into the surrounding environment. In such an embodiment, air in the closed loop enters at dry air inlet 554, passes through evaporation column 550, and exits at wet air outlet 555 as moist air.

[0069] In certain embodiments, the absorption column 500 and the evaporation column 550 may be part of a continuous loop of desiccant fluid, such that the desiccant fluid always flows from the first end of the absorption column 500 (where it enters as a concentrated solution), through the absorption column 500 (thereby absorbing water as it passes), and out the second end of the absorption column 500 as a dilute desiccant fluid. The dilute desiccant fluid may then flow through a heating mechanism, where it is heated, and then flow into the first end of the evaporation column 550. The dilute desiccant fluid may then flow through the evaporation column 550, where it becomes concentrated due to water evaporation, and then flow out the second end of the evaporation column 550 as a concentrated solution. The desiccant fluid may then pass through a cooling mechanism and return to the first end of the absorption column 500. As the desiccant fluid is circulated between the absorption column 500 and the evaporation column 550, two air streams may pass through each column. The first, open air stream can always be circulated through the absorption column 500, where source air is drawn from the ambient environment, passed through the absorption column 500, and discharged to the environment as dried, treated air. At the same time, the closed air stream can be passed through the evaporation column 550, where it absorbs water from the diluted desiccant, and then circulated through the condensation chamber 570 (as discussed herein), where the water is condensed from the moist air and ultimately collected in the water tank 571.

[0070] In certain embodiments, the single-stage continuous vapor consolidation system may include an evaporation column 550 or, alternatively, a membrane desalination system upstream of and in series with the evaporation column 550. In a membrane desalination system, a desiccant flow path may flow past a first side of a membrane such that the desiccant fluid contacts the membrane as it travels along the desiccant flow path. The membrane may separate the desiccant fluid flow path from a water flow path for water collected from the condensation process described herein. The water flow path may pass through a second side of the membrane such that the water contacts the second side of the membrane as it flows along the water flow path.

[0071] The membrane may comprise a porous membrane, such as a nonwoven membrane with small pore sizes. By way of example only, the membrane may comprise ePTFE. As the desiccant fluid and water flow past opposite sides of the membrane, water molecules migrate from the high-salt desiccant fluid through the membrane (via capillary action) into the water stream. Thus, when the dilute desiccant fluid passes through the membrane system before entering the evaporation column 550, a first amount of water is removed from the desiccant fluid in the membrane system before the desiccant fluid enters the evaporation column 550 to evaporate additional water therefrom. In certain embodiments, mass transfer across the membrane can be driven by increasing the vapor pressure of the desiccant. This can be achieved by heating the liquid before contacting the membrane, or by using a vacuum to reduce the pressure on the second side of the membrane, or a combination of both. The water in the desiccant begins to permeate the membrane in a liquid state and exits the membrane in a vapor state. The water is then condensed using a heat exchanger (e.g., a condenser) and / or by contact with a cooler fluid (e.g., condensed water).

[0072] Similar to the absorption column 550, the evaporator column 500 can optionally be operated in a closed loop, such that the desiccant fluid can be repeatedly recirculated through the heating system and the evaporator column 550 until the desiccant fluid reaches a threshold concentration. Accordingly, a control mechanism can be in communication with one or more sensors within the evaporator column 550 (or external to the evaporator column but within the evaporator column closed loop) to monitor the concentration of the desiccant fluid within the evaporator column loop. When the controller determines that the desiccant fluid concentration has risen above a threshold concentration level, the controller can send an operating signal to one or more valves to direct at least a portion of the desiccant fluid from the evaporator column loop toward the absorption column 500 and to direct less concentrated desiccant fluid from the absorption column 500 (e.g., the absorption column loop) into the evaporator column loop. The controller can be configured to maintain the various valves in an open configuration until the measured concentration of desiccant fluid through the evaporative column 550 drops below a threshold concentration level, at which point the controller can send operational signals to the various valves to close them and re-establish a closed evaporative loop. In certain embodiments, air can be continuously directed through the evaporative column regardless of whether the evaporative column loop is closed or open. However, in certain embodiments, air flow can be passed through the evaporative column only while the evaporative column loop is closed, and air flow can be prevented from entering the evaporative column while the evaporative column loop is in an open configuration.

[0073] Moreover, in certain embodiments, the operation of the various valves for opening and closing the absorption column loop and the evaporation column loop can be synchronized, resulting in the loops being simultaneously in an open configuration or simultaneously in a closed configuration. In such embodiments, the triggering event for opening and closing the evaporation and absorption column loops can be based on a concentration measured in only one of the column loops (e.g., based on the measured concentration of the desiccant fluid in the absorption loop or based on the measured concentration of the desiccant fluid in the evaporation loop). In other embodiments, the triggering event for opening and closing the various valves can be based on the measured concentrations of the desiccant fluid in both the absorption loop and the evaporation loop. For example, the controller can be configured to open the valves to pass the desiccant fluid between the evaporation column 550 and the absorption column 500 upon determining that either the solution concentration in the evaporation column has risen above a threshold value or the solution concentration in the absorption column has fallen below a threshold value. As yet another example, the controller can be configured to open the valves to pass the desiccant fluid between the evaporation column 550 and the absorption column 500 upon determining that the solution concentrations in both the evaporation column and the absorption column have met their respective threshold values.

[0074] Similarly, the controller may rely on measurements of one or both solution concentrations in the evaporation loop and / or absorption loop when determining when to close valves to isolate the desiccant fluid between the respective absorption and evaporation loops.

[0075] In certain embodiments, the single-stage continuous vapor consolidation system may be part of an AWG system that includes one or more air preconditioning systems. For example, the air preconditioning system may be located upstream of the absorption column, such that source air entering the AWG system first passes through the air preconditioning system before entering the absorption column. Additionally, the AWG system may include an air preconditioning system, as discussed herein, between the evaporation column and the condensation chamber.

[0076] An exemplary system can be configured to produce at least about 180 gallons of water per day based on an ambient air temperature of 95°F and an ambient relative humidity level of 30%. Ambient air can be provided to the absorption column at a flow rate of at least about 2800 cubic feet per minute to pass through the packed column directing a rich lithium chloride solution having a concentration of about 38-45% by weight (e.g., about 40% by weight). Water can be absorbed by the lithium chloride solution, and the concentration of the lithium chloride solution can drop to a lean concentration level of about 38-40% by weight (e.g., about 38.6% by weight) before the desiccant fluid is directed out of the absorption column. During the absorption process, the absorption column can be maintained at a temperature of at least about 80-90°F.

[0077] The lean desiccant fluid can be heated and directed to an evaporation column operating at a temperature of at least about 180-190 degrees Fahrenheit to evaporate the absorbed water into a closed air loop. The air can then be passed through a condensation chamber where the water vapor is condensed into liquid water at a rate of at least about 180 gallons per day.

[0078] The exemplary system referenced above may additionally include a carbon dioxide capture system as discussed in more detail herein. In such an embodiment, an air flow of approximately 2800 cubic feet per minute can be passed through the carbon dioxide capture column, capturing at least approximately 1.1 tons of carbon dioxide per day. The amount of carbon dioxide generated, the amount of water produced, and the air flow rate are interrelated, so that adjusting any one of these rates will change the others.

[0079] Multi-stage continuous steam consolidation Similar to those described above, a multi-stage continuous vapor consolidation system is configured to absorb water from air in one or more absorption desiccant columns and simultaneously evaporate the water into air in one or more evaporative desiccant columns. For example, a multi-stage continuous vapor consolidation system may be configured as two or more single-stage continuous vapor consolidation systems operating in parallel and with a single condensation system. In certain embodiments, a single evaporator column may be in fluid communication with two or more absorption columns, such that a single desiccant fluid may pass through all the absorption columns in series and / or parallel. The multiple absorption columns may include a first high-concentration absorption column and a second low-concentration absorption column. The high-concentration absorption column may contain a high-concentration desiccant fluid (e.g., desiccant fluid passed directly from the evaporator column), while the low-concentration absorption column may contain a lower-concentration desiccant fluid (e.g., at least a portion of the desiccant fluid from the high-concentration absorption column may pass through the lower-concentration absorption column).

[0080] Furthermore, multiple absorption columns can be arranged in series within the air flow path, such that source air can be drawn from the environment and passed through multiple absorption columns in series before being discharged back to the environment as dry air. For example, source air can first pass through a low-concentration absorption column to absorb a first amount of water from the air, and then through a high-concentration absorption column to absorb a second amount of water from the air. Because initial absorption requires less energy (and does not require low vapor pressure between the air and the liquid desiccant), initial absorption using a lower concentration of desiccant fluid allows for the absorption of the first amount of water from the air. After the initial low-energy requirement absorption process is complete, the air (still containing water vapor) passes through a second absorption column with a higher concentration of desiccant fluid, resulting in the absorption of the second amount of water from the air. The now dry (e.g., low humidity) air can then be discharged from the system to the environment.

[0081] On the desiccant side, as the dilute desiccant exits the low concentration absorption column, the desiccant fluid passes to an evaporation system as discussed herein where it is heated and passed through an evaporation column where the water evaporates into a closed airflow loop.

[0082] In certain embodiments, each absorption column can be in fluid communication with a corresponding evaporation column, and each pair of absorption and evaporation columns can include a separate desiccant flow loop. For example, a first amount of desiccant fluid can flow between the first absorption column and the first evaporation column, and a second amount of desiccant fluid can flow between the second absorption column and the second evaporation column, where the first amount of desiccant fluid is immiscible with the second amount of desiccant. In certain embodiments, the first amount of desiccant fluid can include a first desiccant (e.g., LiCl), and the second amount of desiccant fluid can include a second desiccant (e.g., CaCl).

[0083] Moreover, in embodiments including multiple independent desiccant streams, each desiccant stream can have a different concentration range. For example, a first desiccant stream (e.g., corresponding to a first absorption column through which source air passes) can have a first concentration range measured between a high concentration value at the outlet of the evaporation column and a low concentration value at the outlet of the absorption column, and a second desiccant stream can have a second concentration range. When source air is directed through a series of absorption columns, the air can be directed first through the low concentration range absorption column and second through the high concentration range absorption column.

[0084] In various embodiments, each of the absorption column and evaporation column combinations may operate similarly to that described above in connection with the single-stage continuous vapor consolidation system.

[0085] Condensation Process Treated air (which may include air exiting a preconditioning system and / or air exiting one or more humidity augmentation systems) may be passed through a condensation chamber as discussed herein to condense water vapor in the air into usable liquid water.

[0086] The condensation chamber may be embodied as a heat exchanger (e.g., a cross-flow heat exchanger) or another chamber having a series of cooled condensing surfaces through which water vapor condenses into liquid water. For example, the condensation chamber may include a series of tubes and / or coils (e.g., metal tubes and / or coils) through which the treated air passes. The outer surfaces of the tubes and / or coils are cooled (e.g., by a refrigerant, subcooled gas, coolant, etc.) so that water in the treated air condenses on the inner surfaces of the tubes and / or coils. In such embodiments, the tubes and / or coils may be angled to allow the condensed water to flow out of the tubes and / or coils and into the retention chamber.

[0087] As yet another example, the condensation chamber may include a series of cooling tubes and / or coils (e.g., flowing a subcooled gas, refrigerant, cooling liquid, etc., through the interior of the cooling tubes and / or coils), and the treated air may cross the exterior surfaces of the cooling tubes and / or coils, resulting in water condensing on the exterior surfaces of the tubes and / or coils.

[0088] It should be appreciated that the condensation surface may have any of a variety of shapes and / or configurations.

[0089] As mentioned, the condensed water flows off the condensation surface and into a retention chamber. The retention chamber can include one or more collection trays positioned below the condensation surface and configured to collect water dripping from the condensation surface. The collection trays can be angled toward a retention reservoir configured to hold a volume of water collected via the condensation process. In certain embodiments, the retention reservoir can include one or more water outlets in fluid communication with a liquid conduit to one or more external systems, such as an agricultural system, a drinking water system, etc.

[0090] Carbon Dioxide Process Treated air (which may include air exiting a water consolidation system as discussed herein) may be passed through a carbon dioxide capture system before being discharged to the atmosphere. Carbon dioxide may be captured from the air for filtration and / or disposal (e.g., through one or more chemical processes to convert the carbon dioxide into water, oxygen, and / or solid or liquid compositions that can be disposed of, capturing the carbon dioxide in a filtration medium, etc.).

[0091] As shown in the example of Figure 1, the carbon dioxide capture system can include a carbon dioxide capture column 102 having a fixed bed of carbon dioxide absorbent material (e.g., sodium hydroxide solution). When air is passed over the carbon dioxide absorbent material, the carbon dioxide is absorbed by the material. Additionally, as shown in Figure 1, the carbon dioxide capture column 102 can be heated (e.g., by a hot fluid jacket) to facilitate increased carbon dioxide absorption by the absorbent material.

[0092] As yet another example, the carbon dioxide capture material can be configured to reversibly absorb carbon dioxide such that the captured carbon dioxide can be compressed and stored as a gas for later use.

[0093] In certain embodiments, the recovered carbon dioxide gas can be directed to a greenhouse to optimize the greenhouse environment for plant growth. As discussed herein, the greenhouse can be supplied with water produced by the AWG system discussed herein.

[0094] Power Generation Process Certain embodiments of the AWG systems described above may incorporate one or more power-consuming components, such as blowers, gas / air compressors, liquid fluid pumps, resistive heaters, supervisory computing devices, etc. These components (and other power-consuming components of various embodiments) may receive power from one or more integrated power generation mechanisms of the described systems. As mentioned above, certain embodiments may operate in proximity to hydrocarbon fuel wells, and off-gas (e.g., natural gas) from these fuel wells may be combusted and utilized to generate electricity through energy-generating turbines (e.g., steam turbines). As yet another example, various embodiments may include one or more solar thermal generating mechanisms as described above, which may additionally include one or more electrical energy generating mechanisms for converting solar energy into stored electrical energy (which may be stored via one or more batteries, an uninterruptible power supply (UPS), etc.).

[0095] Additionally, the AWG system and / or power generating aspects of the AWG system may be associated with a greenhouse or other agricultural system to facilitate plant growth (e.g., consumer plant growth). Accordingly, the power generating system may be configured to provide power to various aspects of the agricultural system, such as heating / cooling mechanisms for air within the greenhouse, air circulation fans within the greenhouse, artificial grow lights within the greenhouse, water / irrigation pumps within the greenhouse, agricultural robots (e.g., planters, harvesters, etc.) within the greenhouse, etc.

[0096] By way of example only, the solar canopy material 10 may be provided as a covering material for a plant growth environment, as discussed in more detail herein. The solar canopy 10 may be embodied as a transparent or translucent sheet configured to allow sunlight to pass through the solar canopy 10. However, it should be understood that the sheet may be opaque in certain embodiments to prevent external light from passing through the solar canopy material 10. As shown in FIGS. 7-8 , the solar canopy may additionally include photovoltaic elements 13 (e.g., patches, strips, etc.) embedded within the solar canopy 10. The photovoltaic elements 13 may be configured to convert radiant sunlight into electrical energy, which may ultimately be stored via one or more batteries or utilized in one or more electrical circuits that may be embedded within the solar canopy 10. For example, the solar canopy may additionally include one or more light-emitting diode (LED) light sources 12 embedded therein that may be configured to provide light (e.g., ultraviolet light) to plants within the plant growth environment. The LEDs may be directional, such that they provide light in a fixed direction relative to the LED, or they may be omnidirectional, such that light is emitted all around the LED.

[0097] As a particular example, the solar canopy material 10 may be embodied as a multi-layer flexible sheet (e.g., a plastic sheet, a woven fabric sheet, etc.) that can be draped or otherwise secured over the growth environment frame 20. The solar canopy material 10 may be at least substantially transparent or translucent and configured to allow ultraviolet light to pass through the solar canopy 10. The solar canopy material 10 may have high tensile strength and may be tear and / or puncture resistant. In particular embodiments, the solar canopy material 10 may include one or more reinforcing threads, tapes, etc. embedded within the solar canopy material. For example, the reinforcing threads, tapes, etc. may include Kevlar® threads, metal threads, etc.

[0098] In certain embodiments, solar canopy material 10 includes a first protective sheet 11 that defines a top surface of solar canopy material 10, and / or a second protective sheet 14 that defines a bottom surface of solar canopy material 10. In certain embodiments, first protective sheet 11 and / or second protective sheet 14 may include a woven material (e.g., woven cloth, woven carbon fiber, etc.), a nonwoven material (e.g., high-strength plastic film), etc. In certain embodiments, first protective sheet 11 and / or second protective sheet 14 may individually include multiple layers including, for example, one or more covering layers that define the outermost layer of solar canopy material 10, a reinforcing layer (e.g., one or more reinforcing threads, tapes, etc.), etc.

[0099] First protective layer 11 and / or second protective layer 14 can cover one or more electrical layers of solar canopy material 10. For example, the electrical layer may include a layer including multiple LED elements 12 and / or a layer including one or more photovoltaic elements 13. These layers may be separate layers that are secured to each other via an adhesive material, or these electrical systems may be incorporated into a single layer of solar canopy material 10 that is secured to first protective layer 11 and / or second protective layer 14 via an adhesive material.

[0100] In certain embodiments, photovoltaic elements 13 (e.g., strips, patches, etc.) may be embedded within the solar canopy material 10 as an array of photovoltaic elements 13 or may be configured to collect sunlight. Thus, the photovoltaic elements 13 may have a collecting surface facing the exterior surface of the solar canopy material 10. The photovoltaic elements 13 may be spaced apart from one another within the solar canopy material 10 as desired to allow sunlight to pass between the photovoltaic elements 13 and through the solar canopy material 10. For example, the photovoltaic elements 13 may be spaced apart at periodic intervals within the solar canopy material 10.

[0101] The photovoltaic elements 13 may be electrically connected to conductors embedded within the solar canopy material 10 configured to direct electricity outward from the photovoltaic elements 13. In certain embodiments, the electricity may be directed to a storage device, such as a battery and / or UPS, for subsequent use by various parts of the AWG system, the plant growth environment, etc. In certain embodiments, the electricity may be provided as direct current (DC) for storage and / or use. In certain embodiments, the generated DC electricity may be provided to a power converter configured to convert the DC electricity to alternating current (AC) energy for use by various components and / or supply to a connected power grid.

[0102] As mentioned above, the solar canopy material 10 may additionally comprise one or more embedded LEDs 12 connected in an LED array configured to emit light from and / or through at least a portion of the solar canopy material 10. In certain embodiments, the embedded LEDs 12 may be oriented through the outside of the solar canopy material 10 facing the outside of the solar canopy material 10 (e.g., through the second protective layer 14) such that the LEDs 12 emit light through the inside of the solar canopy material 10. In certain embodiments, the LEDs may be aligned with one or more photovoltaic elements 13 and configured to emit light toward the back side of the photovoltaic elements 13 such that the light is reflected from the back side of the photovoltaic elements 13 through the inside of the solar canopy 10. The LEDs 12 may additionally be connected to one or more conductors (which may be provided in series with the photovoltaic elements 13, in parallel with the photovoltaic elements 13, or in a circuit separate from the photovoltaic elements 13).

[0103] As yet another example embodiment, various LEDs may be suspended from the solar canopy 10. For example, LEDs may be suspended within the growing environment of the agricultural module 1000 surrounded by one or more solar canopies 10, such that the LEDs provide additional illumination to plants growing therein from additional angles (e.g., in proximity to the growing medium in which the plants are growing).

[0104] In certain embodiments, the solar canopy material 10 may be embodied as separate solar canopy panels having finished edges. The finished edges may include smooth edges configured to prevent fraying and / or tearing. For example, the edges may be sewn, welded, etc. In certain embodiments, the finished edges may include one or more grommets or other attachment mechanisms 15 proximate each of the finished edges. The attachment mechanisms 15 may be configured to attach the solar canopy panel 10 to the frame 20 (e.g., via one or more fasteners 22 secured to the mounting plate 21) and / or to adjacent solar canopy panels 10. The attachment mechanisms 15 may be spaced a fixed distance (e.g., 1 inch) from the finished edges or along a line parallel to each of the finished edges. In certain embodiments, the attachment mechanisms 15 for adjacent solar canopy panels 10 may be configured for engagement therebetween such that the adjacent solar canopy panels 10 can be joined via one or more fastening mechanisms 15. In certain embodiments, the solar canopy panels may additionally include one or more electrical connection mechanisms 16 configured to allow the conductors of adjacent solar canopy panels 10 to be connected in series. In certain embodiments, the solar canopy panels 10 may include a first set of electrical connectors 16 configured to connect to the conductors of the photovoltaic subcircuit of the adjacent solar canopy panel 10 and a second set of electrical connectors 16 configured to connect to the conductors of the LED lighting circuit of the adjacent solar canopy panel 10.

[0105] The solar canopy panel 10 may additionally include one or more overlap flaps (not shown) configured to extend beyond the smooth finished edge. The overlap flaps extend beyond the attachment mechanism 15 to provide a sealing overlap that extends across the joint between adjacent and connected solar canopy panels 10. The sealing overlap is configured to minimize the amount of air that can flow between adjacent and connected solar canopy panels 10, for example, to prevent air from escaping from within a plant growth environment sealed by the multiple connected solar canopy panels 10. In certain embodiments, the sealing overlap may include a material that is shared with the rest of the solar canopy panel 10. However, the sealing overlap may include a material that is different from the material of the solar canopy panel 10. For example, the sealing overlap may include an adhesive surface configured to detachably adhere to a surface of the solar canopy panel 10 to provide additional sealing against undesired air leakage between the secured solar canopy panels 10.

[0106] In certain embodiments, the solar canopy material 10 may be configured for use with a translucent cover layer configured to allow only low levels of light to pass through to the solar canopy material. For example, the solar canopy material 10 may be utilized to underlie visual advertising, such as a billboard having a printed translucent advertising sheet disposed on top of the solar canopy material. The photovoltaic elements 13 of the solar canopy material 10 may be configured to collect light when filtered through the overlying advertising sheet.

[0107] Agriculture Module The AWG system may be utilized to generate water and / or power to be supplied to an agricultural module, which may include a greenhouse, a plant growth environment, and / or other structure that may be utilized to promote plant growth within controlled atmospheric conditions. FIGS. 4-5 illustrate various embodiments of an agricultural module 1000 associated with an AWG system 100 housed within a shipping container according to one embodiment. As shown, the agricultural module 1000 may define a plant growth environment having at least a substantially rectangular shape or a shape with multiple distinct lobes (e.g., to form a star shape as shown in FIG. 5). In embodiments including distinct lobes, the volume within each lobe may be isolated from the remainder of the growth environment, such that each lobe may be provided with a unique growth environment (e.g., different temperatures, carbon dioxide levels, humidity levels, etc.) to promote different agricultural product growth.

[0108] FIG. 6 shows a schematic detailed view of a portion of a growing environment of an agricultural module 1000 according to one embodiment. The growing environment of the agricultural module 1000 may include one or more stackable structures 1001, each having one or more bases 1002 configured to support a growing medium (e.g., soil, a hydroponic support, etc.), one or more sidewalls, and a ceiling. The stackable structures 1001 may be suspended from a support frame of the growing environment, stacked such that the supports of the upper structure are supported by the lower structure, etc. The one or more sidewalls and ceiling may be configured to contain controlled atmospheric conditions within the structure (e.g., ambient air with controlled oxygen and carbon dioxide levels, controlled temperature, controlled humidity, etc.). The one or more sidewalls and ceiling may include a covering material, such as a flexible covering material, a rigid covering material, etc. In certain embodiments, the covering material may include integrated grow lights (e.g., light-emitting diode grow lights) and / or integrated electrical circuitry and / or may be configured to allow natural sunlight to pass through the covering material to the contained environment. In certain embodiments, the integrated grow lights may be spaced at periodic intervals throughout the flexible covering material and may be electrically connected to each other and / or to one or more power sources via an electrical circuit. For example, in the illustrated embodiment of Figure 6, the covering material includes a solar canopy 10 as discussed herein incorporating LEDs 12 spaced across the surface of the canopy 10.

[0109] In embodiments comprising a flexible cover material, the agriculture module may comprise one or more rigid supports that collectively form a rigid support frame for the flexible cover material.

[0110] In certain embodiments, the agriculture module 1000 may be embodied as a portable system configured to be quickly set up at a desired agricultural site. The agriculture module 1000 may additionally include one or more sensors 1003 that can be provided within the growth medium of the growth environment. These sensors may be embodied as part of a flexible bundle of electrical circuitry, including conductors, sensors, etc., that can be quickly deployed within the growth environment by unrolling the bundle onto a support surface of the growth environment before providing the growth medium therein. In certain embodiments, the various sensors may be electrically connected to each other, to the control computing system 1004, and / or to a power source via one or more conductors (e.g., flexible conductors). The various sensors may include a moisture sensor, a temperature sensor, a carbon dioxide content sensor, an oxygen sensor, a humidity sensor, etc. It should be understood that some of the described sensors may be configured for wireless data transmission to the control computing system via one or more wireless communication technologies, such as Wi-Fi, Bluetooth, Internet of Things (IoT) technologies, etc.

[0111] In certain embodiments, sensor outputs (e.g., indicative of measured environmental aspects within the growth environment) can be utilized by the control computing system 1004 to adjust environmental conditions within the growth environment. For example, the control computing system 1004 can include data indicative of one or more target environmental conditions, such as a target temperature, a target carbon dioxide content, etc. Based on monitored data outputs from various sensors 1003 within the growth environment, the control computing system 1004 can be configured to compare the monitored data outputs against the target environmental conditions and adjust water flow, carbon dioxide flow, etc. from the AWG 100 to the growth environment. For example, the control computing system 1004 can be configured to automatically activate a sprinkler (or drip irrigation) system (which may be incorporated into the stackable structure 1001) within the growth environment to water plants within the growth environment in response to predetermined conditions, to increase or decrease the amount of carbon dioxide flowing into the growth environment from a carbon dioxide capture system of the AWG system 100, etc.

[0112] Additionally, the growing environment may include one or more automated planting and harvesting mechanisms configured to autonomously plant new plant seeds and / or automatically harvest fruits and / or vegetables grown within the growing environment (this includes the use of agricultural robots and drones).

[0113] For example, seed planting / management may be provided by a planting probe 1010 operable to move along a grid / track system 1011 elevated above the support frame of the growing environment. In certain embodiments, the grid / track system 1011 may be raised and lowered via a support mechanism (e.g., a pneumatic and / or hydraulic support mechanism). The planting probe 1010 may be operable in response to signals received from a control computing system 1004, including data indicative of the planting medium within the growing environment and / or an internal mapping of the base 1002. The control computing system 1004 may additionally include data indicative of desired crops for planting within the growing environment, crop spacing, etc., and may provide movement signals to the planting probe 1010 to insert seeds into the planting medium according to a desired planting plan.

[0114] The planting probe 1010 itself may include a hopper 1012 configured to hold a quantity of seeds and an insertion probe 1013 (e.g., a wedge-shaped insertion probe) configured to deposit the seeds at an appropriate depth within the planting medium (as determined by the control computing system 1004). The planting probe 1010 additionally includes a motion mechanism (e.g., one or more motors) configured to move the planting probe 1010 along a track / grid to implant the seeds within the planting medium. Moreover, the planting probe 1010 may be configured to periodically return to a reloading position within the growing environment to retrieve additional seeds into the included hopper 1012. The reloading position may be located within the growing environment in proximity to a loading chute containing additional seeds that can be selectably provided to the planting probe 1010 as needed. In certain embodiments, the filling chute may be embodied as a container supported (e.g., suspended) above the path of movement of the planting probe such that the planting probe 1010 can move below the filling chute to be refilled by gravity, moving seeds from the filling chute into the planting probe 1010. Moreover, in certain embodiments, the filling chute may include an actuatable input door (e.g., a servo-actuated input door) configured to open in response to a signal received from the control computing system 1004 to allow seeds to flow out of the input chute. Thus, when the planting probe 1010 is positioned below the input chute, the control computing system 1004 can be configured to open the input door to allow seeds to flow from the input chute into the planting probe 1010. Once an appropriate amount of seeds has been provided to the planting probe 1010, the control computing system 1004 can send a second signal to cause the input door to close.

[0115] The planting probe 1010 may additionally include a harvesting mechanism that may be detachably secured to the movable planting probe 1010. The harvesting mechanism may include a mechanically movable cutting / harvesting arm 1014 and a holding basket / tray 1015. When the planting probe 1010 receives a signal from the control computing system 1004 to initiate the harvesting process, the planting probe 1010 may process to harvest and / or cut crops / plants from various plants in the growing environment and deposit the cut crops / plants in the holding basket / tray 1015. When the holding basket / tray 1015 is full, the planting probe 1010 may return to a docking position, where the holding basket / tray 1015 may deposit the harvested items in a holding bin from which the harvested items may be removed from the growing environment. Moreover, in certain embodiments, the holding bin may include one or more level sensors configured to monitor the amount of harvested items in the holding bin to avoid overflowing the holding bin. When the holding box fill level is detected to be above a threshold level, the control computing system 1004 can be configured to send a signal to the planting probe 1010 to suspend harvesting operations until the holding box is empty.

[0116] Although described above with reference to track-based planting and harvesting probe configurations, various embodiments may be configured to plant seeds and / or harvest crops via unmanned aerial vehicles (UAVs) equipped with planting and / or harvesting probes having configurations similar to those described above. The UAVs may be autonomous and configured to navigate within a growing environment according to a prescribed planting plan. In certain embodiments, the planting plan may define a map of intended seed planting locations, such that the autonomous UAV can be configured to autonomously navigate between multiple intended seed planting locations to deposit seeds into a growing medium.

[0117] The autonomous UAV may additionally comprise a harvest probe configuration similar to that described herein. A UAV with a harvest probe configuration may be configured to autonomously navigate within a growing environment to harvest crops grown therein.

[0118] The irrigation system of the growing environment may be embodied as one or more tubes that can be connected to a water distribution mechanism such as a spray sprinkler, drip irrigation tubing, etc. The tubes may include plastic flexible piping and may be embodied as a self-healing material configured to self-seal cracks, cuts, and / or perforations through the tube wall. These tubes may be connected to a water outlet of a condensation system of the AWG system, a water holding tank of the AWG system, etc.

[0119] Additionally, the irrigation system may include a fertilizer delivery mechanism configured to automatically mix a metered amount of fertilizer (e.g., liquid fertilizer) into the water supplied to the irrigation system. The fertilizer delivery mechanism may be in electrical communication with a control computing system 1004, which may be configured to provide a signal to the fertilizer delivery mechanism to modify the amount of liquid fertilizer introduced into the water flow.

[0120] Mechanical Vapor Compression-Based Embodiments Certain embodiments as discussed herein may additionally include one or more components for implementing mechanical vapor compression (MVC), also known as mechanical vapor recompression (MVR). FIGS. 9-10 show schematic diagrams of an exemplary system 600 embodiment incorporating MVC components, and FIGS. 11-12 show alternative embodiments that may be implemented in place of the configuration of FIG. 10. FIGS. 13-14 show alternative embodiments that may be implemented in place of the configuration surrounding absorber 610 of FIG. 9. As shown at reference numeral 601, ambient air (at ambient temperature and humidity levels) is directed into absorber 610 (although not shown, a blower may be implemented at the air inlet to absorber 610 to increase the volumetric flow rate of the ambient air entering absorber 610). Within absorber 610, ambient air contacts a desiccant-rich (concentrated) fluid provided to absorber 610 at a low temperature at 621 to increase the vapor pressure within the absorber to encourage water vapor in the moist ambient air to condense and be absorbed by the desiccant fluid while the moist air is in contact with the desiccant-rich fluid. As the ambient air and desiccant fluid flow through absorber 610, humidity in the air condenses and / or is otherwise absorbed into the desiccant fluid, diluting the desiccant fluid and drying the air. The dry air then exits the absorber and returns to the atmosphere, as shown at 602. As shown, a blower 603 may be incorporated at the ambient air outlet of absorber 610 to increase the volumetric flow rate of air passing through absorber 610. The blower 603 may be provided in addition to, or as an alternative to, the above-mentioned blower located at the ambient air inlet of absorber 610. Moreover, as the desiccant fluid passes through absorber 610 , diluted but still cool desiccant fluid exits absorber 610 , as shown at 622 .

[0121] In certain embodiments, absorber 610 is configured in a counterflow configuration in which ambient air enters absorber 610 near the bottom of absorber 610. Dry ambient air then exits absorber 610 near the top of absorber 610 via flow paths 602-604 (with pump / blower 603 utilized to move the air through absorber 610). Desiccant-rich fluid enters absorber 610 near the top via flow path 621 and flows down through the interior of absorber 610 due to gravity. Water is absorbed from the ambient air into the desiccant fluid, and the resulting dilute desiccant fluid exits the absorber along flow path 622 near the bottom of absorber 610. In certain embodiments, flow modifiers, such as barriers, mesh, and / or bends in the outlet piping from absorber 610, can be used to reduce carryover of desiccant fluid in the air outlet of absorber 610. In certain embodiments, the flow modification means may be positioned inside the absorber 610 adjacent to the top of the absorber 610 (e.g., at the mouth of the outlet port through which dry ambient air exits the absorber via flow path 602).

[0122] In a particular embodiment similar to that reflected in FIG. 15, the absorber 610a operates in a cross-flow configuration in which air enters from one side of the absorber 610a and traverses (e.g., at least substantially horizontally) to the other side. The desiccant-rich fluid enters the top of the absorber 610a and absorbs water from the ambient air as it flows to a low point within the absorber 610a, where the dilute desiccant fluid exits near the bottom. In this configuration, the air flow is at least substantially perpendicular to the flow of desiccant fluid within the absorber 610a. In this configuration, the air inlet and air outlet are at approximately the same height above the absorber 610a.

[0123] In a particular configuration, the absorber 610a operates in a cross-flow counterflow configuration in which air enters the absorber 610a from one side and traverses to the other side. The desiccant-rich fluid enters near the top of the absorber 610a and absorbs water from the ambient air as it flows to a low point within the absorber 610a, where the dilute desiccant fluid exits near the bottom of the absorber 610a. In this configuration, the air inlet and air outlet are offset in height, as shown in the example of FIG. 15. In this configuration, the air inlet can be on a side of the absorber 610a in a location near the top of the absorber 610a, and the air outlet is on a side of the absorber 610a near the bottom. In another orientation of this configuration, the air inlet is positioned on a side of the absorber 610a near the bottom of the absorber 610a, and the air outlet is positioned on the opposite side of the absorber 610a near the top of the absorber 610a (as shown in FIG. 15). Thus, the air path travels at an angle through the absorber 610a from the top to the bottom of the absorber 610a or from the bottom to the top of the absorber 610a.

[0124] In certain embodiments, the interior of absorber 610 comprises multiple packing elements through which the desiccant-rich fluid flows as it absorbs water extracted from the humid ambient air. The packing elements are provided to increase the surface area of ​​the rich liquid desiccant flowing within absorber 610 and to provide a highly tortuous flow path for the ambient air flowing through absorber 610, resulting in turbulent air flow through the interior of absorber 610. Absorber 610 may be embodied as a counterflow column as described above, where the desiccant-rich fluid enters absorber 610 at a desiccant column inlet located at or near the top of absorber 610 and an ambient air inlet is located at the bottom of absorber 610. Ambient air flows upward to a dry air outlet located at or near the top of absorber 610, and desiccant fluid flows downward across the packing elements to a diluted desiccant outlet of absorber 610. By way of example, the packing components may include individual blocks, balls, trays, baffles, and / or any other shape, slits, holes, mesh, and / or other flow-modifying components that define a plurality of baffles that can be positioned within the absorber 610 to collectively define a highly tortuous path for ambient air and desiccant fluid to pass through the absorber 610. The packing components may include (or be formed from) a material that is non-reactive with the desiccant fluid. Exemplary packing components are shown in FIGS. 16A-16B. In certain embodiments, multiple packing components (such as the unstructured packing component shown in FIG. 16B) may be positioned within the absorber 610 without the packing components physically connecting to one another. In other embodiments, a single packing component (such as the structured packing example of FIG. 16A) specifically sized and shaped for the interior of the absorber 610 may be provided and positioned within the absorber 610.

[0125] The packing components of certain embodiments may be arranged in a structured configuration to define channels set at different angles relative to one another, with or without holes, that collectively define structured flow paths for ambient air and desiccant fluid flowing through the absorber 610. To provide a structured packing configuration, the packing components are arranged within the absorber 610 in an ordered, stacked manner. The packing components can also be randomly positioned, where multiple geometrically shaped components (such as balls shown in FIG. 16B) are randomly positioned within the absorber 610 to increase surface area. While discussed as a packing-based absorber, it should be understood that the desiccant fluid can pass through the absorber 610 via other configurations, such as atomization of liquid desiccant fluid, spraying of desiccant fluid within the absorber, etc.

[0126] According to certain embodiments, the diluted desiccant fluid (e.g., liquid) exits absorber 610 toward pump 623. In certain operations, absorber 610 can operate in a batch configuration in which a series of valves can be configured to recirculate the diluted desiccant fluid (on the other side of the heat exchanger is cooling water collected from the overall system, as discussed in more detail herein) through a pre-absorber heat exchanger 625 (e.g., a shell-and-tube heat exchanger, a plate heat exchanger, etc.) along flow path 624 (while preventing additional desiccant-rich fluid from entering the closed loop via flow path 637 while appropriate valves remain closed) to cool the diluted desiccant fluid before it is passed back to the top of absorber 610 as shown at 621. In this way, the amount of water absorbed into the desiccant fluid can be increased (thereby increasing the level of dilution of the desiccant fluid) before it is directed toward the evaporative portion of the overall system.

[0127] In certain embodiments, the pre-absorber heat exchanger 625 is cooled by using a chiller, where a refrigerant such as water, glycol, or the like is used on the other side of the heat exchanger 625 to cool the desiccant-rich fluid along flow path 624. In this embodiment of Figure 9, the illustrated components 662, 664, 625 may all be part of a refrigeration cooling system.

[0128] In certain embodiments, absorber 610 can be operated in a serial configuration in which valves are configured to simultaneously recirculate a quantity of dilute desiccant fluid along flow path 624 and through flow path 626. In this configuration, a quantity of dilute desiccant fluid flows along flow path 624 through a pre-absorber heat exchanger 625 (e.g., a shell-and-tube heat exchanger, a plate heat exchanger, etc.) to cool the dilute desiccant fluid before passing it back through the top of absorber 610 as shown at 621 (the other side of heat exchanger 625 is cooled using water collected from throughout the system, as discussed in more detail herein). The dilute desiccant fluid simultaneously traverses along flow path 626 to MVC evaporator vessel 633.

[0129] In certain embodiments, absorber 610 is configured so that the desiccant-rich fluid is not cooled in a heat exchanger, as shown, for example, in the exemplary embodiment of Figure 13. In this embodiment, cooling of the desiccant fluid can be provided via conductive heat exchange with ambient air through conduction pipes along flow paths (637, 622, and 621). Fluid cooling can be provided in absorber 610 as sensible heat is exchanged with the atmosphere, provided that the air temperature is lower than the temperature of the incoming desiccant fluid.

[0130] In certain embodiments, absorber 610 is configured such that the diluted desiccant fluid exits absorber 610 without a recirculation path and is sent to MVC evaporator vessel 633, as shown in the example of Figure 14. The desiccant-rich fluid returning from MVC evaporator vessel 633 may or may not be cooled by a heat exchanger and / or chiller and / or geothermal cooling on flow path 621 before entering absorber 610.

[0131] 9 , the diluted desiccant fluid exiting absorber 610 at 622 is pumped (via pump 623) along flow path 626 (extending to FIG. 10 ) with appropriate valves closed to prevent the diluted desiccant fluid from recirculating to absorber 610 as described above, constituting batch operation. The diluted desiccant fluid passes through one or more heating subsystems between absorber 610 and MVC evaporator vessel 633. The one or more heating subsystems may include one or more of condenser 627, pre-evaporator heat exchanger 629, and / or heater 631. It should be understood that the one or more heating subsystems may be provided in any order relative to the flow of the desiccant fluid. In the illustrated example, the diluted desiccant fluid, which remains cool after passing through absorber 610, passes through condenser 627, which takes advantage of the generally lower temperature of the diluted desiccant fluid to facilitate condensation of water vapor from the compressed water vapor exiting MVC evaporator vessel 633, as discussed below. In certain embodiments, the condenser 627 is a shell-and-tube heat exchanger, where the diluted desiccant fluid passes through the tubes and the water vapor condenses on the outside of the tubes within the shell of the heat exchanger. In another embodiment, the condenser 627 is a plate-and-frame heat exchanger, where the diluted desiccant fluid passes through one set of plates and the water vapor passes through the other set of plates, where the water vapor condenses within the heat exchanger as it traverses through the heat exchanger to warm the diluted desiccant fluid. In another embodiment, the condenser 627 is a dual-pipe heat exchanger, where the diluted desiccant fluid passes through the inner pipe and the water vapor passes through the outer pipe, allowing the water vapor to condense on the outer surface of the inner pipe. In certain embodiments, the condenser 627 may have a counterflow configuration (where the diluted desiccant fluid flows in the opposite direction to the water vapor). In other embodiments, the condenser 627 may have a parallel, co-flow configuration, where the diluted desiccant fluid and the water vapor flow in the same direction through the condenser 627.

[0132] The diluted desiccant fluid exiting the condenser 627 via the flow path represented at 628 has an increased temperature due to a certain amount of heat transfer from the compressed water vapor to the diluted desiccant fluid within the condenser 627. The diluted desiccant fluid then passes through a pre-evaporator heat exchanger 629 (e.g., a shell-and-tube heat exchanger, a plate-and-frame heat exchanger, a dual-tube heat exchanger (having concentric tubes), etc.) and / or a heater 631 (e.g., an externally powered heater such as an electric heater, a natural gas heater, a solar heater, etc.) to increase the temperature of the diluted desiccant fluid to or near the evaporation temperature. In certain embodiments, the heater may be a series electric heater having a heating element bundle for heating the diluted desiccant fluid. The heater may have an orientation that reduces the possibility of fluid gushing over the elements. The heater 631 may be positioned within the MVC evaporator vessel 633. In certain embodiments, the heater is a heat exchanger (e.g., a shell-and-tube heat exchanger, a plate-and-frame heat exchanger, etc.). In certain embodiments, heater 631 is a solar heater that utilizes photovoltaic panels to generate electrical energy to drive an electric heating element (e.g., a resistive heating element). In certain embodiments, heater 631 is a Fresnel lens heater that utilizes solar energy to generate thermal energy in the form of heat. In certain embodiments, heater 631 includes a geothermal heater mechanism that includes a series of pipes extending to the ground to utilize geothermal energy to heat the diluted desiccant fluid. In other embodiments, heater 631 is a furnace that utilizes a hydrocarbon fuel source (e.g., natural gas, oil, wood, biomass, etc.) combined with oxygen (supplied from ambient air) to generate heat from combustion.

[0133] 10 , which includes both a pre-evaporator heat exchanger 629 and a heater 631, the diluted desiccant fluid first exits the pre-evaporator heat exchanger 629 via a flow path represented at 630 before entering the heater 631. Additionally, the opposite side of the pre-evaporator heat exchanger 629 is provided with heated desiccant-rich fluid that exits the MVC evaporator vessel 633, as discussed in more detail herein.

[0134] The diluted desiccant fluid exiting heater 631 along flow path 632 then enters MVC evaporator vessel 633. In certain embodiments, MVC evaporator vessel 633 is configured to apply a vacuum thereto (e.g., via a vacuum pump) to reduce the vapor pressure within MVC evaporator vessel 633 and lower the evaporation temperature (boiling point) of water particles trapped within the diluted desiccant fluid within MVC evaporator vessel 633. By way of example only, MVC evaporator vessel 633 may include a pressure reducing orifice where flow path 632 enters MVC evaporator vessel 633 to reduce the pressure of the incoming diluted desiccant fluid. In other embodiments, the pressure reducing orifice may be located upstream of one or more heating subsystems. In other embodiments, MVC evaporator vessel 633 includes a heater to increase the temperature therein to the evaporation temperature (boiling point), thereby reducing the vapor pressure within MVC evaporator vessel 633 and promoting evaporation of water from the desiccant fluid. The MVC evaporator vessel 633 in certain embodiments is embodied as a tank into which the diluted desiccant fluid is pumped, sprayed, atomized, or otherwise provided to promote evaporation of water entrapped therein. As the diluted desiccant fluid is pumped into the MVC evaporator vessel 633, it can pass through an orifice, as described above, causing water molecules to rush through the orifice due to reduced pressure across the orifice. In certain embodiments, the fluid is directed below the liquid level within the MVC evaporator vessel 633 to promote sealing of the vacuum pressure within the MVC evaporator vessel 633. In another configuration, the diluted desiccant fluid is sprayed into the MVC evaporator vessel 633 from the top and / or sides of the vessel and / or through the bottom of the vessel. In embodiments in which atomization is used, an atomizer is positioned within the MVC evaporator vessel 633 to impart energy to the diluted desiccant fluid to further assist in the separation of water molecules from the diluted desiccant fluid. An example of positioning may include placing the atomizer adjacent to the top of the MVC evaporator vessel 633 and flowing the desiccant fluid through the atomizer to create a shower effect of atomized fluid particles entering the MVC evaporator vessel 633. Another example of positioning may be atomizing the fluid from the surface above the surface of the diluted desiccant fluid.Other orientations that promote separation of water from the diluted desiccant fluid may also be used with the atomizer.

[0135] 10 , the diluted solution may pass through a series of heat exchangers and / or heaters before reaching the MVC evaporator vessel 633. Water in the diluted desiccant fluid vaporizes in the MVC evaporator vessel 633 due to the increased temperature of the diluted desiccant fluid entering the MVC evaporator vessel 633 and the reduced pressure within the MVC evaporator vessel 633, thereby concentrating the desiccant fluid, resulting in a desiccant-rich fluid exiting the MVC evaporator vessel 633 at flow path 634 (e.g., at the bottom of the MVC evaporator vessel 633). The rich, warm desiccant fluid is pumped (e.g., via pump 635) along flow path 636 to the pre-evaporator heat exchanger 629, where heat is transferred from the desiccant-rich fluid entering the heat exchanger 629 via flow path 636 to the diluted desiccant fluid entering the pre-evaporator heat exchanger 629 via flow path 628. The desiccant-rich fluid exits pre-evaporator heat exchanger 629 in flow path 637, where the fluid is returned to pump 623 in FIG. 9 (by opening appropriate valves to allow the desiccant-rich fluid to enter the flow circulation path surrounding absorber 610). By appropriately configuring the valves, the desiccant-rich fluid exiting pump 623 is then passed through flow path 624 and into pre-absorber heat exchanger 625, similar to that described above with respect to the recirculation of diluted desiccant fluid. The desiccant-rich fluid is cooled via pre-absorber heat exchanger 625 before being passed via flow path 621 to the top of absorber 610 to collect additional water vapor from the ambient air (as noted, the other side of pre-absorber heat exchanger 625 holds a stream of cold water that is collected as part of the process, as discussed below).

[0136] Referring again to MVC evaporator vessel 633 shown in FIG. 10 , water vapor evaporating from the diluted desiccant fluid exits MVC evaporator vessel 633 via flow path 651. The water vapor passes through compressor 652, which increases the pressure of the water vapor, thereby increasing the saturation temperature of the water vapor exiting the compressor at flow path 653. In certain embodiments, a liquid entrapment device is installed upstream of compressor 652 to minimize the amount of entrained liquid in the vapor reaching compressor 652. Moreover, the compressor may additionally or alternatively have a water injection mechanism to reduce the superheat temperature of the water vapor (and / or to generally cool compressor 652). The vapor exiting compressor 652 is then passed through a series of pipes (defining flow path 653) and / or another heat exchanger (e.g., as shown in FIG. 11 ) within MVC evaporator vessel 633, or another process line, such as that shown in FIG. 10 , that allows latent heat to be transferred to the original desiccant liquid entering MVC evaporator vessel 633. For example, the compressed water vapor passes through condenser 627, which utilizes sensible and latent heat transfer (from the water vapor to the dilute desiccant fluid) as part of the condensation process to condense the water vapor into liquid water. In certain embodiments, the condensed water exiting flow path 654 may then pass through another heat exchanger (not shown) that also utilizes sensible heat transfer before the liquid water is stored in storage tank 655 or used as potable water therein. It should be understood that additional heat exchangers may be provided either upstream or downstream of the condenser. As shown in FIG. 10, storage tank 655 has a drain line (along flow paths 656-658, including an optional pump 657 (e.g., centrifugal pump, positive displacement pump, etc.) between flow paths 656 and 658) to allow for water use. Certain embodiments need not include a pump if storage tank 655 is elevated above the use area (thereby allowing water to be drawn from storage tank 655 using potential energy as needed). Additionally, storage tank 655 has a gas vent 659 to ensure that non-condensable gases (e.g., O, N, CO, etc.) dissolved in the water can be removed.In certain embodiments, a vacuum pump and / or blower on flow path 659 is used to remove non-condensable gases from the water in storage tank 655. In certain embodiments, storage tank 655, drain lines 656-658, and / or flow path 654 may additionally include one or more water purification mechanisms, such as a carbon-based water filter. Note that the water condensed from the water vapor extracted from the diluted desiccant fluid is at least substantially distilled water, even if not purified, and therefore, a remineralization process may be included in storage tank 655, drain lines 656-658, and / or flow path 654 to add various minerals (e.g., fluoride, calcium, iron, etc.) to the water prior to use, depending on the water's intended end use.

[0137] Figures 11-12 reflect alternative fluid routing configurations that may be implemented in place of the configuration shown in Figure 10. In other words, the embodiment of either Figure 11 or Figure 12 may be implemented in combination with Figure 9 (e.g., flow from Figure 9 may proceed to Figure 11, or flow from Figure 9 may proceed to Figure 12).

[0138] Referring first to FIG. 11 , the dilute desiccant fluid exiting absorber 610 in flow path 622 is pumped (via pump 623 shown in FIG. 9 ) along flow path 626 (extending to FIG. 11 ) with appropriate valves closed to prevent the dilute desiccant fluid from recirculating to absorber 610 as described above for batch operation of absorber 610. Absorber 610 can also be operated with dilute desiccant fluid flowing through flow paths 624 and 626 simultaneously, as described above. Absorber 610 can also be operated with dilute desiccant fluid flowing from absorber 610 to MVC evaporator vessel 633, as described above. The dilute desiccant fluid passes through one or more heating subsystems between absorber 610 and MVC evaporator vessel 633. In the illustrated embodiment of FIG. 11 , the one or more heating subsystems comprise a pre-evaporator heat exchanger 629 (e.g., a shell-and-tube heat exchanger, a plate-and-frame heat exchanger, a dual-tube heat exchanger (with concentric tubes), etc.). The diluted desiccant fluid entering pre-evaporator heat exchanger 629 is heated by sensible heat transfer with the previously heated desiccant-rich fluid exiting MVC evaporator vessel 633. Thus, the diluted desiccant fluid exiting pre-evaporator heat exchanger 629 via flow path 630 has an increased temperature due to the amount of heat transferred from the desiccant-rich fluid to the diluted desiccant fluid within pre-evaporator heat exchanger 629.

[0139] In the embodiment of FIG. 11 , diluted desiccant fluid enters MVC evaporator vessel 633 via flow path 630. In certain embodiments, MVC evaporator vessel 633 is configured to apply a vacuum thereto (e.g., via a vacuum pump) to reduce the vapor pressure within MVC evaporator vessel 633 and lower the evaporation temperature (boiling point) of water particles trapped within the diluted desiccant fluid within MVC evaporator vessel 633. By way of example only, MVC evaporator vessel 633 may include a pressure-reducing orifice through which flow path 632 enters MVC evaporator vessel 633 to reduce the pressure of the incoming diluted desiccant fluid. In other embodiments, the pressure-reducing orifice may be positioned upstream of one or more heating subsystems. In other embodiments, MVC evaporator vessel 633 includes heater 633 a (which may have a configuration similar to heater 631 described above) to increase the temperature therein to the evaporation temperature (boiling point), thereby reducing the vapor pressure within MVC evaporator vessel 633 and promoting evaporation of water from the desiccant fluid. The heater 633a may be positioned to heat the diluted desiccant fluid if the heat exchange provided is insufficient to vaporize the water therein. In certain embodiments, the MVC evaporator vessel 633 is embodied as a tank into which the diluted desiccant fluid is pumped, sprayed, atomized, or otherwise provided to promote evaporation of water entrained therein. For example, the embodiment of FIG. 11 specifically depicts the MVC evaporator vessel 633 as containing a plurality of at least substantially vertical tubes therein through which the diluted desiccant fluid flows from an upper “head” of the MVC evaporator vessel 633 toward a bottom “sump” of the MVC evaporator vessel 633. In such embodiments, water vapor is introduced into a shell portion located outside the contained tubes and within the MVC evaporator vessel 633. The water vapor passing around the tubes inside the MVC evaporator vessel 633 is at a higher temperature than the desiccant fluid, and therefore the water vapor serves to increase the temperature inside the MVC evaporator vessel 633 (particularly inside the tubes through which the desiccant fluid flows) to promote evaporation of water from the diluted desiccant fluid.As the concentrated desiccant-rich fluid flows downward inside the tubes, evaporated water extracted from the desiccant fluid flows to the top of the tubes. It should be understood that the tube side of the MVC evaporator vessel 633 and / or the shell side of the MVC evaporator vessel 633 may be subjected to vacuum pressure.

[0140] In certain embodiments, the MVC evaporator vessel 633 additionally includes an actuated wiper mechanism to ensure that the film of desiccant fluid (e.g., or the film of salts that precipitate from the desiccant fluid as its concentration increases) remains thin. The actuated wiper mechanism can be operated by a motor that mechanically moves the wiper to wipe the inner surface of the tubes. In certain embodiments, a similar wiper mechanism may be utilized to wipe condensed water from the outer surface of the tubes.

[0141] As water evaporates from the diluted desiccant fluid in MVC evaporator vessel 633, the concentration of the desiccant fluid increases, and desiccant-rich fluid exits MVC evaporator vessel 633 in flow path 634 (e.g., at the bottom of MVC evaporator vessel 633). The rich, warm desiccant fluid is pumped (e.g., via pump 635) along flow path 636 to pre-evaporator heat exchanger 629, where heat is transferred from the desiccant-rich fluid entering heat exchanger 629 via flow path 636 to the diluted desiccant fluid entering pre-evaporator heat exchanger 629 via flow path 626. The desiccant-rich fluid exits pre-evaporator heat exchanger 629 via flow path 637, where the fluid is returned to pump 623 of FIG. 9 (by opening appropriate valves to allow the desiccant-rich fluid to enter the flow circulation path surrounding absorber 610 during batch operation, or by leaving all valves open to an appropriate extent to allow continuous flow). By appropriately configuring the valves, the desiccant-rich fluid exiting pump 623 is then passed through flow path 624 and into pre-absorber heat exchanger 625, similar to that described above for recirculation of dilute desiccant fluid in both batch and continuous operation. The desiccant-rich fluid is cooled through pre-absorber heat exchanger 625 before being passed via flow path 621 to the top of absorber 610 to collect additional water vapor from the ambient air. (As noted, in certain embodiments, the other side of pre-absorber heat exchanger 625 holds a stream of cold water that is collected as part of the process, as discussed below.)

[0142] Referring again to the MVC evaporator vessel 633 shown in FIG. 11 , water vapor evaporated from the dilute desiccant fluid exits the MVC evaporator vessel 633 via flow path 651. The water vapor passes through a series of compressors 652, each configured to successively increase the pressure of the water vapor, thereby increasing the saturation temperature of the water vapor exiting the series of compressors in flow path 653. While six compressors are shown in FIG. 11 , it should be understood that any number of compressors may be implemented, such as a single compressor, two compressors, three compressors, four compressors, five compressors, six compressors, seven compressors, etc. In certain embodiments, a liquid entrapment device is installed upstream of the series of compressors 652 (or a liquid entrapment device may be installed upstream of each individual compressor in the series of compressors 652) to minimize the amount of entrained liquid in the vapor reaching the compressor 652. Additionally, each of the multiple compressors may additionally or alternatively have a water injection mechanism to reduce the superheat temperature of the steam (and / or generally cool each of the compressors 652). Steam exiting the series of compressors 652 is then passed through a series of pipes (defining flow path 653) to a heat exchanger embodied within the MVC evaporator vessel 633. As noted above, the heat exchanger within the MVC evaporator vessel 633 may be embodied as a series of at least substantially vertical tubes within the MVC evaporator vessel 633, such that the MVC evaporator vessel 633 is embodied as a shell-and-tube heat exchanger. In the embodiment of FIG. 11 , compressed steam is introduced to the shell side of the MVC evaporator vessel 633. In certain embodiments, the compressed steam is introduced proximate the bottom of the MVC evaporator vessel 633 to provide countercurrent heat exchange with the desiccant fluid passing through the interior of the tubes. The water vapor can then condense on the exterior of the tubes and flow down the exterior of the tubes within the MVC evaporator vessel 633 toward the bottom of the MVC evaporator vessel 633 (referred to as the sump of the MVC evaporator vessel 633), exiting the sump of the MVC evaporator vessel 633 via flow path 654.Although not shown, flow path 654 can direct the condensed water (and water vapor) through one or more cooling mechanisms, such as a geothermal cooling mechanism, to more completely condense the water vapor into liquid water before introducing it into storage tank 655. As shown in FIG. 11 , the storage tank has a drain line (along flow paths 656-658, including an optional pump 657 (e.g., centrifugal pump, positive displacement pump, etc.) between flow paths 656 and 658) to enable use of the water. Certain embodiments need not include a pump if storage tank 655 is elevated above the use area (thereby allowing water to be drawn from storage tank 655 using potential energy as needed). Additionally, storage tank 655 has gas vents 659a-659c to actively ensure that pressure within the storage tank remains near or below atmospheric pressure (e.g., via pump 659b, which maintains a negative pressure within storage tank 655 to draw water along flow path 654 into the storage tank). In certain embodiments, storage tank 655, drain lines 656-658, and / or flow path 654 may additionally include one or more water purification mechanisms, such as a carbon-based water filter. Note that the water condensed from the water vapor extracted from the diluted desiccant fluid is at least substantially distilled water, even if not purified, and therefore, a remineralization process may be included in storage tank 655, drain lines 656-658, and / or flow path 654 to add various minerals (e.g., fluoride, calcium, iron, etc.) to the water prior to use, depending on the water's intended end use.

[0143] 12 , the diluted desiccant fluid exiting absorber 610 in flow path 622 is pumped (via pump 623 shown in FIG. 9 ) along flow path 626 (extending to FIG. 12 ) with appropriate valves closed to prevent recirculation to absorber 610 during batch operation as described above, or when valves are open to allow simultaneous flow in paths 624 and 626. The diluted desiccant fluid passes through one or more heating subsystems between absorber 610 and MVC evaporator vessel 633. In the illustrated embodiment of FIG. 12 , the one or more heating subsystems include a pre-evaporator heat exchanger 629 (e.g., a shell-and-tube heat exchanger, a plate-and-frame heat exchanger, a double-tube heat exchanger (having concentric tubes), etc.), a condenser 627, and a heater 631 (e.g., an externally powered heater such as an electric heater, a natural gas heater, a solar heater, etc.) to increase the temperature of the diluted desiccant fluid to or near the evaporation temperature. In certain embodiments, the heater 631 may be a series electric heater having a heating element bundle for heating the diluted desiccant fluid. The heater 631 may be oriented to reduce the likelihood of fluid spurting over the elements. The heater 631 may be positioned within the MVC evaporator vessel 633. In certain embodiments, the heater 631 is a heat exchanger (e.g., a shell-and-tube heat exchanger, a plate-and-frame heat exchanger, etc.). In certain embodiments, the heater 631 is a solar heater that utilizes photovoltaic panels to generate electrical energy to drive electric heating elements (e.g., resistive heating elements). In certain embodiments, the heater 631 is a Fresnel lens heater that utilizes solar energy to generate thermal energy in the form of heat. In certain embodiments, the heater 631 includes a geothermal heater mechanism comprising a series of pipes extending to the ground to utilize geothermal energy to heat the diluted desiccant fluid. In another embodiment, heater 631 is a furnace that utilizes a hydrocarbon fuel source (e.g., natural gas, oil, wood, biomass, etc.) combined with oxygen (supplied from ambient air) to generate heat from combustion.

[0144] 12, the diluted desiccant fluid entering the pre-evaporator heat exchanger 629 is heated by sensible heat transfer with the previously heated desiccant-rich fluid exiting the MVC evaporator vessel 633. Thus, the diluted desiccant fluid exiting the pre-evaporator heat exchanger 629 via flow path 628 has an increased temperature due to the amount of heat transferred from the desiccant-rich fluid to the diluted desiccant fluid within the pre-evaporator heat exchanger 629.

[0145] The diluted desiccant fluid exiting the pre-evaporator heat exchanger 629 remains below the condensation temperature of the water vapor; therefore, the diluted desiccant fluid is passed through the condenser 627, which utilizes the relatively lower temperature of the diluted desiccant fluid to facilitate condensation of water from the compressed water vapor exiting the MVC evaporator vessel 633, as discussed below. In certain embodiments, the condenser 627 is a shell-and-tube heat exchanger, where the diluted desiccant fluid passes through the tubes and the water vapor condenses on the outside of the tubes within the shell of the heat exchanger. In another embodiment, the condenser 627 is a plate-and-frame heat exchanger, where the diluted desiccant fluid passes through one set of plates and the water vapor passes through the other set of plates, where the water vapor condenses within the heat exchanger as it traverses through the heat exchanger to warm the diluted desiccant fluid. In another embodiment, the condenser 627 is a dual-pipe heat exchanger, where the diluted desiccant fluid passes through the inner pipe and the water vapor passes through the outer pipe, allowing the water vapor to condense on the outer surface of the inner pipe. In certain embodiments, the condenser 627 may have a counter-flow configuration (where the diluted desiccant fluid flows in the opposite direction to the water vapor). In other embodiments, the condenser 627 may have a parallel co-flow configuration where the diluted desiccant fluid and water vapor flow in the same direction through the condenser 627.

[0146] As will be appreciated by a comparison between Figures 10 and 12, the locations of the pre-evaporator heat exchanger 629 and the condenser 627 can be reversed to modify how sensible heat transfer is utilized to heat the diluted desiccant fluid and cool the water vapor and desiccant-rich fluid. Specifically, with reference to Figure 12, the diluted desiccant fluid first exits the pre-evaporator heat exchanger 629 via flow path 628 before entering the condenser 627, and then enters the heater 631 after exiting the condenser 627.

[0147] The diluted desiccant fluid exiting heater 631 is then passed through flow path 632 to MVC evaporator vessel 633. In certain embodiments, MVC evaporator vessel 633 is configured to apply vacuum pressure to its interior via vacuum pump arrangement 633b-633d (including tubing 633b leading to the interior of MVC evaporator vessel 633, vacuum pump 633c, and exhaust 633d to atmosphere). Reducing the pressure within MVC evaporator vessel 633 reduces the evaporation temperature (boiling point) of water particles trapped within the desiccant fluid, facilitating evaporation of water from the desiccant fluid. As another example, MVC evaporator vessel 633 may include a pressure-reducing orifice where flow path 632 enters MVC evaporator vessel 633 to reduce the pressure of the incoming diluted desiccant fluid. In other embodiments, the pressure-reducing orifice may be positioned upstream of one or more heating subsystems. In other embodiments, the MVC evaporator vessel 633 includes a heater (such as heater 633a in FIG. 11) to increase the temperature therein to the evaporation temperature (boiling point), thereby reducing the vapor pressure within the MVC evaporator vessel 633 and promoting evaporation of water from the desiccant fluid. The MVC evaporator vessel 633 in certain embodiments is embodied as a tank into which diluted desiccant fluid is pumped, sprayed, atomized, or otherwise provided to promote evaporation of water entrained within the diluted desiccant fluid.

[0148] As water evaporates from the diluted desiccant fluid in MVC evaporator vessel 633, the concentration of the desiccant fluid increases and desiccant-rich fluid exits MVC evaporator vessel 633 at flow path 634 (e.g., at the bottom of MVC evaporator vessel 633). The rich, warm desiccant fluid is pumped (e.g., via pump 635) along flow path 636 to pre-evaporator heat exchanger 629, where heat is transferred from the desiccant-rich fluid entering heat exchanger 629 via flow path 626 to the diluted desiccant fluid entering pre-evaporator heat exchanger 629 via flow path 626. The desiccant-rich fluid exits pre-evaporator heat exchanger 629 via flow path 637, where the fluid is returned to pump 623 of FIG. 9 (by opening appropriate valves to allow the desiccant-rich fluid to enter the flow circulation path surrounding absorber 610). By appropriately configuring the valves, the desiccant-rich fluid exiting pump 623 is then passed through flow path 624 and into pre-absorber heat exchanger 625, similar to that described above for recirculation of dilute desiccant fluid in both batch and continuous operation. The desiccant-rich fluid is cooled through pre-absorber heat exchanger 625 before being passed via flow path 621 to the top of absorber 610 to collect additional water vapor from the ambient air. (As noted, in certain embodiments, the other side of pre-absorber heat exchanger 625 holds a stream of cold water that is collected as part of the process, as discussed below.)

[0149] Referring again to the MVC evaporator vessel 633 shown in FIG. 12 , water vapor evaporated from the diluted desiccant fluid exits the MVC evaporator vessel via flow path 651. The water vapor passes through a series of compressors 652, each configured to successively increase the pressure of the water vapor, thereby increasing the saturation temperature of the water vapor exiting the series of compressors in flow path 653. While six compressors are shown in FIG. 12 , it should be understood that any number of compressors may be implemented, such as a single compressor, two compressors, three compressors, four compressors, five compressors, six compressors, seven compressors, etc. In certain embodiments, a liquid entrapment device is installed upstream of the series of compressors 652 (or a liquid entrapment device may be installed upstream of each individual compressor in the series of compressors 652) to minimize the amount of entrained liquid in the vapor reaching the compressor 652. Additionally, each of the multiple compressors may additionally or alternatively have a water injection mechanism to reduce the superheat temperature of the water vapor (and / or generally cool each of the compressors 652). The vapor exiting the series of compressors 652 is then passed through a series of pipes (defining flow path 653) and / or another heat exchanger (e.g., as shown in FIG. 11 ) within MVC evaporator vessel 633, or another process line, as shown in FIG. 12 , that allows latent heat to be transferred to the original desiccant fluid entering MVC evaporator vessel 633. For example, the compressed water vapor passes through condenser 627, which utilizes sensible heat transfer (from the water vapor to the dilute desiccant fluid) as part of the condensation process to condense the water vapor into liquid water. In certain embodiments, the condensed water exiting flow path 654 may then pass through another heat exchanger (not shown), also utilizing sensible heat transfer, before the liquid water is stored in storage tank 655 or used as potable water therein. As shown in FIG. 12, the storage tank 655 has a drain line (along with flow paths 656-658, including an optional pump 657 (e.g., a centrifugal pump, a positive displacement pump, etc.) between flow paths 656 and 658) to allow for water use.If the storage tank 655 is elevated above the area of ​​use (thereby allowing water to be drawn from the storage tank 655 using potential energy as needed), certain embodiments need not include a pump. Moreover, the storage tank 655 has a gas vent 659 to ensure that the pressure within the storage tank 655 remains near atmospheric pressure. In certain embodiments, the storage tank 655 additionally includes pressure reduction mechanisms 659a-659c to actively ensure that the pressure within the storage tank remains below atmospheric pressure via a pump 659b that maintains a negative pressure within the storage tank 655 to draw water into the storage tank along the flow path 654. In certain embodiments, the storage tank 655, the drain lines 656-658, and / or the flow path 654 may additionally include one or more water purification mechanisms, such as a carbon-based water filter. It should be noted that the water condensed from the water vapor extracted from the diluted desiccant fluid is, if not purified, at least substantially distilled water, and therefore, depending on the water's intended end use, a remineralization process may be included in storage tank 655, drain lines 656-658, and / or flow path 654 to add various minerals (e.g., fluoride, calcium, iron, etc.) to the water prior to use.

[0150] In certain embodiments, multiple MVC evaporator vessels are provided in series, such that desiccant fluid from an upstream MVC evaporator vessel is passed through a downstream MVC evaporator vessel to increase the concentration of the desiccant-rich fluid to a desired concentration. When a series setup is used, the desiccant-rich fluid is routed from the first MVC evaporator vessel to the next (downstream or “second”) MVC evaporator vessel, where the desiccant-rich fluid undergoes a similar process to evaporate water vapor from the desiccant fluid. In such embodiments, a second set of one or more heating subsystems may be positioned along the desiccant flow path between the outlet of the upstream MVC evaporator vessel and the inlet of the downstream MVC evaporator vessel. The second set of one or more heating subsystems may include one or more pre-evaporator heat exchangers and / or heaters. The desiccant-rich fluid exits the first MVC evaporator vessel and passes through a pre-evaporator heat exchanger (and / or heater) upstream of the second MVC evaporator vessel to increase the temperature of the desiccant fluid. In certain embodiments, the desiccant fluid may pass through a pre-evaporator heat exchanger upstream of both the first and second MVC evaporator vessels. The diluted desiccant fluid may also utilize a heater (e.g., an externally powered heater such as an electric heater, natural gas heater, etc.) contained within the second set of one or more heating subsystems to heat the desiccant fluid to or above the evaporation temperature before it enters the second MVC evaporator vessel. The desiccant fluid is passed into the second MVC evaporator vessel, where it is subjected to a vacuum to again lower the evaporation temperature. Additional water in the desiccant fluid is vaporized in the second MVC evaporator vessel and passed through a compressor in a manner similar to that shown in FIG. 10. The compressor (associated with the second MVC evaporator vessel) increases the pressure of the vapor and therefore the saturation temperature of the water vapor. A liquid entrapment device may be installed upstream of the compressor to minimize the amount of entrained liquid in the vapor reaching the compressor. The vapor leaving the compressor is then passed through a series of pipes or another heat exchanger in the second MVC evaporator vessel, or another process line similar to that shown in FIG. 10, which allows the latent heat to be transferred to the original liquid in the second MVC evaporator vessel.The condensed water then passes through a heat exchanger to a second MVC evaporator vessel to utilize sensible heat transfer before being stored in a storage tank 655 or used as potable water in the storage tank.

[0151] In certain embodiments, the MVC evaporator vessel 633 may be split to include two sections. One section acts as the original MVC evaporator vessel 633, and the other section acts as a condensing heat exchanger, with the dividing wall acting as the heat transfer surface, thereby allowing the location of the condensing heat exchanger to be moved to the interior of the vessel. As discussed above with reference to FIG. 11 , the MVC evaporator vessel 633 can alternatively utilize shell-and-tube heat exchange to allow condensation to occur therein, with the surfaces of the tubes inside the MVC evaporator vessel 633 acting as the heat transfer surface.

[0152] Additionally, referring again to Figures 9-10, at least a portion of the water exiting condenser 627 (or an alternative water source) may be diverted from flow path 654 (of Figure 10) to flow path 661 (shown in Figure 9) through geothermal cooling mechanism 662 to reduce the temperature of the water before it is used to cool the desiccant-rich fluid via pre-absorber heat exchanger 625, which is provided to cool the desiccant-rich fluid before introducing it into absorber 610. The cooled water exits the geothermal cooling mechanism through pump 664 in flow path 663 before passing along flow path 665 to pre-absorber heat exchanger 625. The water exiting pre-absorber heat exchanger 625 passes along flow path 666 where it may be recirculated back to flow path 661. To return water to storage tank 655 of FIG. 10, a series of valves can be configured such that water leaving pump 664 (downstream of geothermal cooling mechanism 662) is directed along flow path 667 that intersects flow path 654 of FIG. 10 (intersection not shown) and / or is otherwise provided to the input of storage tank 655.

[0153] Mechanical Vapor Compression-Based Exemplary Operation The following discussion provides an exemplary overview of the operation of an embodiment utilizing an MVC according to FIGS. 9-10 (specific callouts are provided for alternatives shown in FIGS. 11-12, where necessary) as part of an atmospheric water generation system and method. It should be noted that when the term “about” is used with reference to a numerical value (e.g., a temperature value, a pressure value, etc.), this encompasses both the value itself and deviations from that temperature value that provide the same functional operation of the described method. For example, a description of a temperature range of “about” 10°F to “about” 50°F is intended to encompass a temperature range of 10°F to 50°F, as well as slight deviations at the upper and lower limits of the temperature range that provide the same functionality as the described temperature range. Moreover, because the MVC process is independent of the desiccant fluid utilized, the MVC may be utilized with any of a variety of desiccant fluids. Any one of several desiccant fluids may be utilized, including, but not limited to, CaCl, NaCl, LiCl, KCOOH, MgCl, ionic liquids, deep eutectic solvents, organic liquids, and / or any combination thereof. The following exemplary methodology for mechanical vapor compression is described as utilizing CaCl, and the temperatures and pressures discussed herein are provided specifically for use with CaCl. Thus, it should be understood that other pressure and temperature ranges may be provided for embodiments utilizing other desiccant fluids.

[0154] The CaCl2 desiccant fluid exiting absorber 610 of FIG. 9 in flow path 622 exits the absorber at a concentration of about 10% by weight to about 50% by weight and a temperature of about 75°F to about 130°F. The desiccant fluid flows along flow path 622 through pump 623 and along flow path 626 through condenser 627. In certain embodiments, condenser 627 is a shell-and-tube type where the desiccant fluid enters the tube side of the heat exchanger. Water vapor produced as a result of the entire process enters the shell side and is condensed in condenser 627. In another embodiment, condenser 627 is a plate-and-frame heat exchanger. The desiccant fluid enters one set of plates, while water vapor enters the other set of plates. The water vapor condenses in condenser 627 as it traverses through condenser 627 to warm the desiccant fluid. In another embodiment, condenser 627 is a dual-pipe heat exchanger where the desiccant fluid enters the dual-pipe heat exchanger through the inner pipe. Steam enters the heat exchanger through the outer pipe and condenses on the outer surface of the inner pipe as it traverses through the condenser 627.

[0155] In certain embodiments, the flow pattern through condenser 627 is in a countercurrent direction. In other embodiments, the flow pattern through condenser 627 is in a cocurrent direction, depending on the shape and orientation of the heat exchanger embodying condenser 627.

[0156] Upon exiting the condenser 627 via flow path 628, the diluted desiccant fluid has a temperature of about 132°F to about 170°F. The diluted desiccant fluid is then routed to the pre-evaporator heat exchanger 629, where sensible heat transfer from the desiccant-rich fluid (flowing from 636 through heat exchangers 629-637) further heats the diluted desiccant fluid. In certain embodiments, the pre-evaporator heat exchanger 629 is a shell-and-tube type heat exchanger, with the diluted desiccant fluid entering the tube side of the pre-evaporator heat exchanger 629. The desiccant-rich fluid flow path 636 enters the shell side of the pre-evaporator heat exchanger 629. In another embodiment, the diluted desiccant fluid enters the tube side of the pre-evaporator heat exchanger 629, and the desiccant-rich fluid enters the tube side of the pre-evaporator heat exchanger 629. In another embodiment, the pre-evaporator heat exchanger 629 is a plate-and-frame heat exchanger. The dilute desiccant fluid enters one set of plates while the desiccant-rich fluid enters the other set of plates. In another embodiment, the pre-evaporator heat exchanger 629 is a dual-pipe heat exchanger, with the dilute desiccant fluid entering the dual-pipe heat exchanger through the inner pipe and the desiccant-rich fluid entering the heat exchanger through the outer pipe.

[0157] The diluted desiccant fluid exits pre-evaporator heat exchanger 629 in stream 630 at a temperature of about 140°F to about 210°F. The diluted desiccant fluid then traverses through heater 631. Heater 631 may be a series electric heater with an element bundle for heating the fluid. Heater 631 may have a different orientation to reduce the possibility of the fluid surging over the elements. In certain embodiments, heater 631 may reside within MVC evaporator vessel 633. In certain embodiments, heater 631 is a shell-and-tube or plate-and-frame type heat exchanger. In certain embodiments, heater 631 is a solar heater that utilizes photovoltaic panels to generate energy through electricity from solar capture. In certain embodiments, heater 631 is a Fresnel lens that utilizes solar energy to generate thermal energy in the form of heat. In certain embodiments, heater 631 is a geothermal heater as discussed herein. In other embodiments, heater 631 is a furnace that utilizes a hydrocarbon fuel source combined with oxygen to generate heat from combustion. In certain embodiments, oxygen from ambient air is used. Upon exiting heater 631, the diluted desiccant fluid is at a temperature of about 150°F to about 270°F.

[0158] The diluted desiccant fluid then passes along flow path 632 to MVC evaporator vessel 633. As another example, a pressure reducing orifice is provided at the interface between flow path 632 and MVC evaporator vessel 633 to reduce the pressure of the incoming diluted desiccant fluid before it enters MVC evaporator vessel 633. The reduced pressure through the orifice is between about 5 PSIG and about 30 PSIG. In certain embodiments, the pressure reducing orifice is positioned upstream of one or more heater subsystems.

[0159] The interior of MVC evaporator vessel 633 may be subjected to a vacuum of about -3 PSIG to about -14.6 PSIG. In certain embodiments, a vacuum pump is attached to MVC evaporator vessel 633. In certain embodiments, a vacuum pump is attached to storage tank 655, which applies negative pressure to the system via flow paths 654, 653, and 651 (and intervening components). In certain embodiments, a vacuum pump is attached to both storage tank 655 and MVC evaporator vessel 633 (similar to that shown in FIG. 12).

[0160] Due to the diluted desiccant fluid from heater 631 reaching its boiling point and the lower pressure in MVC evaporator vessel 633, water vapor separates from the diluted desiccant fluid. The water vapor is then routed through compressor 652, where it is compressed to about 0.1 PSIG to about 5 PSIG. The water vapor then exits compressor 652 at a temperature of about 160°F to about 370°F. The water vapor is routed to condenser 627, where the latent heat of condensation is transferred to the diluted desiccant fluid, as described above. Liquid water exits condenser 627 via flow path 54 at a temperature of about 75°F to about 180°F. The water then collects in storage tank 655. Pump 657 removes water from storage tank 655 when water is needed or when storage tank 655 is full. Pump 657 may be a centrifugal or positive displacement pump. In certain embodiments, the storage tank 655 is elevated above the final dispense point and potential energy is used to empty the storage tank 655. The stored water may be further purified through one or more purification and / or filtration mechanisms. Note that the water in the storage tank 655 is distilled and is ultra-pure. In certain embodiments, a carbon filter may be added between the storage tank 655 and the dispense point (accessible via the flow path 658). In certain embodiments, a remineralization process is added between the storage tank 655 and the dispense point.

[0161] Referring again to MVC evaporator vessel 633, after the water is separated, the desiccant-rich fluid exits the MVC evaporator vessel at 634 at a temperature between about 150°F and about 270°F. The weight percent of CaCl in the desiccant fluid is increased by about 0.1% to about 15% by weight relative to the diluted desiccant fluid. The desiccant-rich fluid passes through pump 635, which conveys the desiccant-rich fluid through pre-evaporator heat exchanger 629, where sensible heat transfer occurs from the desiccant-rich fluid to the diluted desiccant fluid. The desiccant-rich fluid then exits pre-evaporator heat exchanger 629 at a temperature between about 135°F and about 173°F. The desiccant-rich fluid is then pumped back along path 637-path 624-path 621 (through intervening pumps and heat exchangers) to the inlet of absorber 610. In certain embodiments, the desiccant-rich fluid is cooled to a temperature of about 50°F to about 80°F before entering the absorber 610, which absorbs additional water that condenses from humidity in the ambient air.

[0162] conclusion Modifications and other embodiments of the present disclosure will come to mind to one skilled in the art to which this disclosure pertains having the benefit of the teachings presented in the foregoing descriptions and the associated drawings. It is to be understood, therefore, that the disclosure is not to be limited to the specific embodiments disclosed, and that modifications and other embodiments are intended to be included within the scope of the appended claims. Although specific terms are employed herein, they are used in a generic and descriptive sense only and not for purposes of limitation.

[0163] In certain embodiments, various portions of the AWG system can be enclosed within one or more shipping containers that can be easily transported as modular system components to a desired operational location. For example, an air preconditioning system may be enclosed within a first container, one or more water consolidation systems (e.g., a single-stage batch water consolidation system and / or a continuous water consolidation system) may be enclosed within a second shipping container, with various ports / inlets extending through the walls of the shipping containers to allow connection to one or more geothermal cooling systems, solar heating systems, high-pressure gas inputs, etc. In certain embodiments, one or more condensation systems, water storage tanks, etc. may be embodied within a third storage container. However, it should be understood that certain embodiments may be configured such that the entire AWG system may be enclosed within a single storage container with one or more ports / inlets (e.g., air inlet / outlet, high-pressure gas inlet, solar heating inlet / outlet, geothermal cooling inlet / outlet, etc.) extending through its walls to allow interaction with aspects of the surrounding environment.

Claims

1. 1. A method for extracting water from air, comprising: intersecting the atmospheric air stream with a desiccant-rich fluid flowing along a desiccant circulation loop in an absorber to extract water vapor from the atmospheric air stream and absorb the extracted water vapor to dilute the desiccant-rich fluid to form a diluted desiccant fluid; flowing the diluted desiccant fluid along a solution flow path to an evaporator vessel, evaporating water from the diluted desiccant fluid to form an evaporated desiccant fluid stream and an evaporated water vapor stream; heating the diluted desiccant fluid via one or more heating subsystems prior to flowing the diluted desiccant fluid into the evaporator vessel, the one or more heating subsystems comprising at least one heat exchanger for effecting sensible heat transfer between the diluted desiccant fluid and the evaporated desiccant fluid stream; directing the evaporated water vapor to a liquid entrainment device upstream of a compressor to reduce the amount of entrained liquid in the evaporated water vapor; directing the evaporated water vapor stream through a compressor to a condenser to form condensed water, the condenser defining at least a portion of the solution flow path, the condenser configured to utilize sensible heat transfer between the dilute desiccant fluid flowing through the condenser and the evaporated water vapor stream to reduce the temperature of the evaporated water vapor and condense the water vapor into the condensed water; Including, a closed airflow loop circulating an airflow through the evaporator vessel and carrying the water vapor from the evaporator vessel to the condenser, the condenser condensing the water vapor into liquid water in the closed airflow loop, and the closed airflow loop returning from the condenser to the evaporator vessel; The method wherein the evaporated desiccant fluid stream is returned to the absorber as the desiccant-rich fluid.

2. 2. The method of claim 1, wherein intersecting the atmospheric air flow with the desiccant-rich fluid in the absorber comprises providing the atmospheric air flow and the desiccant-rich fluid to the absorber in a counter-flow configuration such that the atmospheric air flow flows from a lower portion of the absorber to an upper portion of the absorber and the desiccant-rich fluid flows from the upper portion of the absorber to the lower portion of the absorber.

3. 3. The method of claim 2, wherein the desiccant-rich fluid flows through a packing arrangement within the absorber, the packing arrangement including packing components that provide a highly tortuous flow path for the atmospheric air flow and the desiccant-rich fluid.

4. 2. The method of claim 1, wherein crossing the atmospheric air flow with the desiccant-rich fluid in the absorber comprises providing the atmospheric air flow and the desiccant-rich fluid to the absorber in a cross-flow configuration such that the atmospheric air flow flows from a first side of the absorber to an opposite second side of the absorber and the desiccant-rich fluid flows from an upper portion of the absorber to a lower portion of the absorber at least substantially perpendicular to the atmospheric air flow.

5. 5. The method of claim 4, wherein the air flow flows from an air inlet on the first side of the absorber adjacent an upper portion of the absorber to an air outlet on the second side of the absorber adjacent a lower portion of the absorber.

6. 5. The method of claim 4, wherein the air flow flows from an air inlet on the first side of the absorber adjacent a lower portion of the absorber to an air outlet on the second side of the absorber adjacent an upper portion of the absorber.

7. 10. The method of claim 1, further comprising, before crossing the atmospheric air stream with the desiccant-rich fluid, passing the desiccant-rich fluid through a heat exchanger cooled by a cold water stream, the cold water stream being cooled via at least one of a geothermal cooling system or a chiller before being introduced into the heat exchanger.

8. 10. The method of claim 1, wherein the one or more heating subsystems comprise a heater positioned downstream of the at least one heat exchanger, the method further comprising heating the diluted desiccant fluid via the heater.

9. the desiccant circulation loop includes a plurality of valves for reconfiguring a flow path of the desiccant fluid, and the method comprises: configuring the plurality of valves such that the diluted desiccant fluid is diverted to the absorber inlet as the desiccant-rich fluid for one or more fluid flow cycles prior to flowing the diluted desiccant fluid along the solution flow path; configuring the plurality of valves to allow the dilute desiccant fluid to flow along the solution flow path; The method of claim 1 , comprising:

10. 10. The method of claim 1, further comprising directing the evaporated desiccant fluid stream to a second evaporator vessel, where additional water vapor is evaporated from the evaporated desiccant fluid stream, before returning the evaporated desiccant fluid stream to the absorber.

11. 1. A system for extracting water from the atmosphere, comprising: an absorber configured to dilute the desiccant fluid from a desiccant-rich fluid state to a dilute desiccant fluid state by absorbing water vapor from the atmosphere passing through the desiccant fluid in the absorber; an evaporator vessel configured to condense the desiccant fluid from the diluted desiccant fluid by evaporating water vapor from the desiccant fluid and directing the evaporated water vapor toward a compressor; a liquid entrainment device upstream of the compressor that receives evaporated water vapor from the evaporator vessel and reduces the amount of entrained liquid in the evaporated water vapor; a desiccant flow path from the absorber to the evaporator vessel for providing the desiccant fluid from the absorber to the evaporator vessel; the desiccant flow path comprises one or more heating subsystems, the one or more heating subsystems comprising: a heat exchanger for exchanging heat from the desiccant fluid exiting the evaporator vessel with the desiccant fluid passing along the desiccant flow path between the absorber and the evaporator vessel; a condenser configured to condense the water vapor after the compressor increases the vapor pressure of the water vapor, the condenser defining at least a portion of the desiccant flow path, the condenser configured to utilize sensible heat transfer between the desiccant fluid and the water vapor flow through the condenser to reduce the temperature of the water vapor and condense the water vapor into condensed water; and Equipped with The system further comprises a closed airflow loop, wherein the closed airflow loop circulates an airflow through the evaporator vessel, carrying the water vapor from the evaporator vessel to the condenser, the condenser condensing the water vapor in the closed airflow loop into liquid water, and the closed airflow loop returning the airflow from the condenser to the evaporator vessel.

12. 12. The system of claim 11, wherein the absorber interior defines a plurality of packing elements, a desiccant inlet proximate an upper end of the absorber, and a desiccant outlet proximate a lower end of the absorber, and wherein one or more absorbent beds are configured such that liquid desiccant flowing from the desiccant inlet to the desiccant outlet flows substantially horizontally across the one or more absorbent beds.

13. 13. The system of claim 12, wherein the absorber additionally defines an atmospheric inlet adjacent the lower end of the absorber and an atmospheric outlet adjacent the upper end of the absorber.

14. 12. The system of claim 11, further comprising an input heat exchanger in a portion of the desiccant flow path upstream of the absorber, the input heat exchanger being cooled by a cold water stream, the cold water stream being cooled via a geothermal cooling system before being introduced into the heat exchanger.

15. The system of claim 11 , wherein the one or more heating subsystems comprise a heater positioned downstream of at least one heat exchanger.

16. The desiccant flow path is connected to a plurality of valves. a first configuration in which desiccant fluid exiting the absorber in a diluted desiccant fluid state is diverted to an inlet of the absorber to be provided to the absorber as the rich desiccant fluid; a second configuration in which desiccant fluid exiting the absorber is directed into the evaporator vessel; a third configuration in which desiccant fluid exiting the evaporator vessel is redirected to an inlet of the evaporator vessel; a fourth configuration in which the desiccant fluid exiting the evaporator vessel is directed to the inlet of the absorber so as to be provided to the absorber as the rich desiccant fluid; and The system of claim 11 , configurable between

17. 12. The system of claim 11, wherein the evaporator receptacle is a first evaporator receptacle, the system further comprising a second evaporator receptacle connected downstream relative to the first evaporator receptacle such that desiccant solution exiting the first evaporator receptacle is directed into the second evaporator receptacle.

18. 18. The system of claim 17, further comprising a second set of one or more heating subsystems located between the first evaporator vessel and the second evaporator vessel, the second set of one or more heating subsystems comprising a second heat exchanger for exchanging heat from the desiccant fluid exiting the second evaporator vessel with the desiccant fluid passing into the second evaporator vessel.

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