System and method for generating atmospheric water by absorption using ultrasound or microwave for solvent regeneration

Abstract

The atmospheric water generating system includes a water vapor integration system configured to increase the relative humidity of the controlled air stream prior to condensing water from the controlled air stream. The water vapor integration system includes a fluid-desiccant flow system configured to reduce the temperature of the desiccant to promote absorption of water vapor by the desiccant from the atmospheric air stream. Heating of the desiccant flow then promotes evaporation of water vapor from the desiccant flow into the controlled air stream circulating through the system. This increases the humidity of the controlled air stream relative to the atmospheric relative humidity, promoting 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 / 203,064, filed July 7, 2021, the entire contents of which are incorporated herein by reference.

[0002] This patent application is also related to U.S. Patent Application No. 17 / 552,173, filed December 15, 2021, which claims priority to U.S. Provisional Patent Application No. 63 / 126,860, filed December 17, 2020. This patent application is also related to U.S. Patent Application No. 16 / 782,808, filed February 5, 2020, which is a continuation of U.S. Patent Application No. 15 / 850,870, filed December 21, 2017, which claims priority to 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 which are incorporated herein by reference. [Background technology]

[0003] The amount of freshwater available for human consumption, plant irrigation, livestock and herd rearing, commercial and / or industrial use, and other purposes has largely outpaced the amount of freshwater required for such purposes. Maintaining sufficient quantities of water for human and / or animal consumption and use has become increasingly expensive in recent years, particularly in arid climates with minimal annual precipitation and inaccessible other freshwater sources. Processes such as seawater desalination, water filtration and / or purification, groundwater (e.g., aquifer) exploitation, and other processes are often used in combination to provide freshwater to various geographic regions, depending on the relative availability and cost of each water-sourcing process.

[0004] Water shortages in certain geographic areas are also at least partly responsible for food shortages in certain parts of the globe. Where water is not readily available to irrigate crops and hydrate livestock, basic nutritional foods are difficult to grow and may be difficult or expensive to obtain on the open market.

[0005] Therefore, there is a general need for processes to increase the availability of freshwater, especially in arid geographical areas and / or areas where stored or underground waters are inaccessible or contaminated. Summary of the Invention

[0006] Various embodiments are directed to an atmospheric water generating system comprising: an absorbent configured to intersect an atmospheric air flow with a desiccant flowing along a closed desiccant circulation loop, extract water vapor from the atmospheric air flow, and absorb the extracted water vapor into the desiccant; and at least one water extraction device configured to extract water from the desiccant in a liquid desiccant and collect it in a permeate water flow path, the water extraction device comprising at least one excitation component and at least one water separation component. The excitation component comprises at least one heating system for increasing the temperature of the liquid desiccant before it enters the at least one water separation component. In certain embodiments, the excitation component comprises a device utilizing at least one excitation system selected from the group consisting of ultrasound, microwave, or a combination thereof.

[0007] Certain embodiments are directed to a method of extracting water from atmospheric air, comprising intersecting the atmospheric air flow with a desiccant in an absorbent material to extract water vapor from the atmospheric air flow and absorbing the extracted water vapor into the desiccant. In the embodiments described herein, the desiccant flows along a closed desiccant circulation loop to a water excitation component that heats a hygroscopic feed, and then to a water separation component, where the heated liquid desiccant is separated into entrained water vapor and concentrated liquid desiccant, which is circulated back to the atmospheric water absorption component.

[0008] Certain embodiments described herein are directed to a water extraction apparatus comprising: an ultrasonic excitation component disposed between an atmospheric water collection component and a water separation component, the ultrasonic excitation component comprising a housing having an inlet configured to receive liquid desiccant from the atmospheric water collection component and an outlet for channeling the liquid desiccant to a water separation system, the liquid desiccant comprising a hygroscopic feed solution; and one or more ultrasonic nozzles disposed within the housing and configured to excite water molecules in the liquid desiccant by applying ultrasonic waves to the liquid desiccant within the housing.

[0009] Certain embodiments described herein are directed to a water extraction apparatus comprising: a microwave excitation component disposed between an atmospheric water collection component and a water separation component, the microwave excitation component comprising a housing having an inlet configured to receive liquid desiccant from the atmospheric water collection component and an outlet for flowing the liquid desiccant to a water separation system, the liquid desiccant comprising a hygroscopic feed solution; and one or more microwave generators and waveguides disposed within the housing and configured to excite water molecules in the liquid desiccant by applying microwaves to the liquid desiccant within the housing.

[0010] Embodiments described herein are further directed to a method of water extraction that includes separating water from a liquid desiccant using an ultrasonic water extraction device, wherein the liquid desiccant flows from an atmospheric water collection component to an excited component, the liquid desiccant in the excited component is ultrasonically excited and heated to produce high humidity water vapor, and the heated liquid desiccant then flows from the excited component to a water separation system to separate the water from the desiccant.

[0011] Embodiments described herein are further directed to a method of water extraction that includes separating water from a liquid desiccant using a microwave water extraction device, wherein the liquid desiccant flows from an atmospheric water collection component to an excited component, the liquid desiccant in the excited component is excited and heated by microwaves to produce high humidity water vapor, and the heated liquid desiccant then flows from the excited component to a water separation system to separate the water from the desiccant.

[0012] Reference will now be made to the accompanying drawings, which are not necessarily drawn to scale. [Brief explanation of the drawings]

[0013] [Figure 1] FIG. 1 is a schematic diagram of an ultrasonic water extraction system, according to one embodiment. [Figure 2] FIG. 1 is a schematic diagram of a microwave water extraction system, according to one embodiment. [Figure 3] FIG. 2 is a schematic diagram of an air preconditioning system and a condenser, according to one embodiment. [Figure 4A] FIG. 2 is a schematic diagram of an air preconditioning system and a condenser according to another embodiment. [Figure 4B] FIG. 2 is a schematic diagram of an air preconditioning system and a condenser according to another embodiment. [Figure 5A] 1 illustrates exemplary packing components within an absorbent material, according to certain embodiments. [Figure 5B]1 illustrates exemplary packing components within an absorbent material, according to certain embodiments. [Figure 6A] FIG. 1 illustrates an exemplary configuration of a membrane-based water extraction device, according to various embodiments. [Figure 6B] FIG. 1 illustrates an exemplary configuration of a membrane-based water extraction device, according to various embodiments. [Figure 6C] FIG. 1 illustrates an exemplary configuration of a membrane-based water extraction device, according to various embodiments. [Figure 6D] FIG. 1 illustrates an exemplary configuration of a membrane-based water extraction device, according to various embodiments. [Figure 6E] FIG. 1 illustrates an exemplary configuration of a membrane-based water extraction device, according to various embodiments. [Figure 7A] FIG. 1 is a schematic diagram of a batch steam integration system alongside a steam condensation system, according to one embodiment. [Figure 7B] FIG. 1 is a schematic diagram of a batch steam integration system alongside a steam condensation system, according to one embodiment. [Figure 8A] FIG. 1 is a schematic diagram of a continuous steam integration system alongside a water vapor condensation system, according to one embodiment. [Figure 8B] FIG. 1 is a schematic diagram of a continuous steam integration system alongside a water vapor condensation system, according to one embodiment. [Figure 9] FIG. 1 illustrates an exemplary implementation of a steam integration system with an agricultural module, according to one embodiment. [Figure 10] FIG. 1 illustrates another exemplary implementation of a steam integration system with an agricultural module, according to an embodiment. [Figure 11] FIG. 1 illustrates an automated planting mechanism according to one embodiment. [Figure 12] FIG. 1 is an exploded view of a surface overlay, according to one embodiment. [Figure 13] 1 is an exemplary diagram of a surface covering panel secured to a support frame. DETAILED DESCRIPTION OF THE INVENTION

[0014] The present disclosure will now more particularly describe various embodiments with reference to the accompanying drawings. It should be understood that while some embodiments have been shown and described herein, not all are fully described. Indeed, these embodiments may take many different forms, and this 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 numbers refer to like elements throughout.

[0015] Overview

[0016] The performance of an atmospheric water generation (AWG) system is primarily determined by the local atmospheric conditions and the hygroscopic desiccant medium. Specifically, the hygroscopic desiccant medium in the absorbent column is initially used to capture water vapor from the ambient air. The absorbed water is then extracted from the dilute desiccant solution by external energy input during regeneration, which is classified as a high-energy-demand unit operation of the AWG. Conventional heat-only methods are often implemented for water separation during regeneration, but these methods always increase the cost of water production by the AWG system. Therefore, alternative innovative technologies are needed to improve the efficiency of the AWG system and regenerate the liquid desiccant in an energy-efficient manner.

[0017] Atmospheric water generation (AWG) systems utilize an absorption system to extract water from the atmosphere. Even with low-humidity atmosphere (air with humidity greater than zero), a certain amount of water can be extracted from the air, at least in part, by contacting the air with a concentrated desiccant solution under controlled conditions that promote mass transfer of water from the air (where water is present in vapor form) to the diluent of the desiccant solution (where water is present in liquid form). The controlled conditions can increase the vapor pressure present in the controlled environment by prescribing specific temperature and / or pressure conditions. Aspects of controlling the environment to promote condensation of water vapor from the air into the desiccant solution include controlling the temperature (e.g., lowering the temperature of the air in contact with the desiccant solution), controlling the pressure (e.g., increasing the pressure of the air in contact with the desiccant solution), controlling the surface area of ​​the desiccant solution in contact with the air (e.g., flowing the desiccant solution across various high-surface-area plates to increase the surface area of ​​the desiccant solution), and / or controlling the flow rate and / or flow path of the air and / or desiccant solution (e.g., creating turbulent air flow in contact with the desiccant solution). In certain embodiments, air compression, cooling, or humidity increasing mechanisms are incorporated to optimize the amount of water extracted from the air (per unit of intake air drawn into the AWG system).

[0018] In one embodiment, the AWG system utilizes a condensing coil and / or plate system to extract water from the air. In the water extraction process of the integrated AWG process, moist air (with humidity greater than 0%) passes over / around / through cooled condensing surfaces (e.g., coils, plates, and / or the like) until the temperature of the moist air drops below its dew point, causing water vapor from the moist air to condense on the condensing surfaces. The condensed water is then directed to a collection chamber (e.g., a tank, bowl, and / or the like) for storage and use.

[0019] As another example of an embodiment, an AWG system may utilize a liquid desiccant, such as a hygroscopic feed solution, to absorb water from the air. The hygroscopic feed solution may be passed through an excitation system, where an excitation signal, such as ultrasound (FIG. 1) or microwave (FIG. 2), is applied to the liquid desiccant, exciting the liquid desiccant and causing the water within the liquid desiccant to be released as water vapor, which can then be cooled and collected as liquid water. The excitation system may be used alone to extract water from the liquid desiccant, or may be used in conjunction with one or more additional water extraction systems, such as membrane-based water separation systems and / or the like.

[0020] In certain embodiments, the AWG system may include one or more additional air compression mechanisms, air cooling mechanisms, or air humidity increasing mechanisms to optimize the amount of water extracted from the air (per unit of air intake taken into the AWG system).

[0021] In certain embodiments, the AWG system may be integrated with one or more carbon dioxide filtering / capture modules, one or more greenhouse modules, one or more power generation modules, and / or the like. For example, the intake air into the AWG system may be passed through a carbon dioxide capture system before the dehumidified, dry air is discharged 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 carbon dioxide concentrations within the greenhouse and thereby improve crop growth efficiency.

[0022] Additionally, the power generation module may include one or more renewable energy power generation systems, such as solar / photovoltaic, geothermal, and / or the like, or hydrocarbon fuel-based power generation systems, that can 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 generates carbon dioxide or other exhaust gases, the power generation module exhaust gases may be passed through a carbon dioxide capture module to reduce carbon dioxide production of the integrated system.

[0023] definition

[0024] As used herein, the term "liquid desiccant" refers to a hygroscopic feed solution comprising a hygroscopic material and water. The liquid desiccant absorbs and retains water from the atmosphere. In embodiments described herein, the hygroscopic material can be selected from the group consisting of CaCl, NaCl, LiCl, MgCl, KCOOH, CHCOOK, colloids, nanomaterials, and ionic liquids, or any combination thereof.

[0025] As used herein, the term "separation system" refers to various processes that may be used to extract water from heated liquid desiccant. In certain embodiments described herein, the liquid desiccant is separated by one or more of electrodialysis, mechanical vapor compression, or distillation, including but not limited to membrane distillation, vacuum membrane distillation, single-effect distillation, or any combination thereof. Electrodialysis refers to an electrochemical separation process that removes salts from a feed solution by using DC power to move ions across a selective ion-exchange membrane. Mechanical vapor compression refers to a process in which the pressure and temperature of a liquid desiccant are increased prior to condensation. Distillation refers to a process in which a liquid desiccant is heated to form vapor, and the vapor is then condensed to separate the liquid distillate (i.e., water). Membrane distillation separates vapor from an aqueous feed solution by applying a microporous hydrophobic membrane, which condenses on the other side of the membrane. Single-effect distillation refers to a process in which a liquid desiccant is heated in an evaporation tank, and the vapor is cooled in a condensation tank and stored as fresh water.

[0026] As used herein, the term "sensible heating" refers to heat that can be felt (the amount of heat that can be measured with a thermometer).

[0027] atmospheric water resources

[0028] The atmosphere is about 3,100 cubic miles (mi 3 ) or 12,900 cubic kilometers (km 3 ) of water. This amount is roughly equivalent to the total volume of the Great Lakes. As a natural resource, water vapor is constantly replenished through nature's closed-loop water cycle, providing a nearly limitless supply of water that can be extracted from the air without adverse environmental impact.

[0029] Atmospheric Water Generation

[0030] AWG processes include systems and methods for extracting water vapor by condensing water vapor from atmospheric source air and capturing the condensed liquid water. Certain embodiments may be adapted to be combined with a carbon dioxide capture system as discussed herein. Certain embodiments include preconditioning and / or compressing the original air supply (e.g., air at atmospheric conditions) to facilitate the water extraction process, and / or maximizing the amount of water vapor extractable from a given unit volume of air supply by condensing the water vapor captured in the original air supply (e.g., by increasing the humidity of at least a portion of the original air supply). As discussed herein, the treated air supply may be compressed, consolidated, and / or manipulated through one or more processes to facilitate the water extraction process.

[0031] Air preconditioning

[0032] As mentioned above, the original supply air may be preconditioned to facilitate the water extraction process utilized in the eventual condensation of water vapor into usable liquid water. In certain embodiments, the preconditioning process may include compressing the air to increase the vapor pressure of the air (thereby forcing more water into a liquid state rather than a vapor state) and / or lowering the temperature of the supply air to a temperature closer to the dew point. In certain embodiments, the air preconditioning system described herein may be utilized before and / or after a humidification system, such as a desiccant-based humidification system as described herein. Additionally, the air preconditioning system may be utilized before and / or after a carbon dioxide capture system as discussed herein.

[0033] By way of example only, the air preconditioning process may include a series of compressors / pumps, venturi valves, vortex valves, manifolds, and / or the like configured to collectively lower the temperature of the supply air to approach the air dew point and / or increase the pressure of the air before removing water vapor from the air (e.g., by condensation or desiccant absorption). For example, the original supply air may be drawn into the air preconditioning system by a vacuum created at the inlet by 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 original air pressure entering the air preconditioning system. In certain embodiments, the compressor and / or centrifugal fan may be rotated by one or more electric motors (which may receive input power from one or more electrical power grids in communication with the air preconditioning system) mechanically connected to the compressor and / or centrifugal fan via a gear transmission, belt drive, chain drive, and / or the like.

[0034] In embodiments including a centrifugal fan, particulates, dust, and other heavy air contaminants are directed to the outermost edge of the centrifugal fan where they are removed from the airflow and expelled from the air pre-conditioning system.

[0035] In certain embodiments, the filtered air may be directed to a carbon dioxide capture column, as discussed in more detail herein, where it passes over a fixed sorbent bed configured to absorb carbon dioxide from the air. The carbon dioxide may be separated and directed away from the air stream by a compressor.

[0036] In certain embodiments, the filtered (carbon dioxide reduced) air may be further directed through an air pre-conditioning system to a primary manifold, where a variable plenum / valve splits the air in a selected ratio, from which a first air stream continues along with the bulk air flow and a second air stream is directed to a vortex tube manifold as described herein.

[0037] The bulk airflow may proceed through one or more venturi valves (e.g., a heat exchanger through which a cooling fluid passes) each configured to reduce the pressure and temperature of the bulk airflow (pressure is reduced on both sides of each venturi valve while the volume and amount of air remains constant, thereby reducing the temperature of the airflow proportionally to the temperature) and / or a precooler (e.g., a heat exchanger through which a cooling fluid passes). After passing through the one or more venturi valves and / or precoolers, the bulk airflow may proceed to a temperature measurement section, where one or more temperature measurement devices (e.g., thermometers) measure the temperature (e.g., dry-bulb and wet-bulb temperatures) of the bulk airflow to determine the dew point of the bulk airflow. The output of the temperature measurement devices may be used by a controller to mix the bulk airflow with at least a portion of the vortex-cooled airflow to reduce the temperature of the bulk air and bring it closer to the air dew point. For example, the controller may be in electronic communication with an electromechanical mixing valve that can be selectively opened or 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 (monitored by the controller), the controller may send a signal to the motor to move the electromechanical valve to a desired position to achieve a desired mixture of vortex cooling air and bulk airflow.

[0038] The vortex-cooled air begins flowing 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., by a compressor) to a pressure sufficient to achieve a temperature drop (approximately 70-150°F) of the air through one or more vortex tubes 106. For example, the air may be pressurized to at least approximately 70-120 PSI before being directed into one or more vortex tubes. Each vortex tube includes an inlet port that directs the airflow tangentially into the internal spin chamber. As the air gains angular momentum upon entering the spin chamber, denser, warmer air moves toward the periphery of the spin chamber and is discharged through the exhaust valve. In certain embodiments, this warmer air may be used to heat the carbon dioxide capture column. Other vortex-cooled air moves toward the center of the spin chamber and is discharged through the vortex outlet. As previously mentioned, the vortex-cooled air can mix with the bulk air stream to lower the temperature of the bulk air stream, bringing it closer to its dew point. As yet another alternative, the vortex cooling air may be used to cool a precooler through which the bulk air passes.

[0039] In certain embodiments, the mixed and cooled bulk air stream is then directed to a condensation chamber 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., cooling plates, screens, tubes, and / or the like configured to reduce the local temperature of the air at the condensation surface below the air dew point, thereby causing water vapor to condense onto the condensation surface). The condensed water may then be passed from the condensation surface to a holding chamber for collection and subsequent 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 efficiently remove water vapor from the bulk air stream. Furthermore, in certain embodiments, the air preconditioning system may be omitted, and raw air may be filtered and / or introduced directly into the condensation chamber. In such embodiments, the required input power may be lower, thereby reducing the amount of power required to generate water.

[0040] It should also be understood that certain embodiments of the pre-conditioning system may include one or more filters (e.g., woven-based air filters, non-woven-based air filters, and / or the like), one or more refrigerant systems (e.g., passing warm air through a heat exchanger to reduce its temperature and bring it closer to the dew point), and / or the like, instead of or in addition to the vortex and venturi valve mechanisms discussed herein.

[0041] Use of desiccants in atmospheric water generation systems.

[0042] As previously discussed, certain embodiments include one or more subsystems configured to increase the humidity of a portion of the supply air to increase the amount of water that can be extracted from the supply air. Specifically, water vapor may be extracted from a first, larger volume of supply air and reintroduced into a second, smaller volume of supply air, thereby consolidating the water vapor in the supply air and increasing the humidity of the second volume of supply air before the water vapor in the second volume of supply air condenses into liquid water.

[0043] An AWG system as discussed herein includes at least one air scrubber with a column for contacting atmospheric air (e.g., after humidifying the air) with a desiccant. In certain embodiments, the desiccant solution may be a fluid, gel, and / or the like within the typical operating temperature range discussed herein. The desiccant may be selected from lithium chloride (LiCl), lithium bromide (LiBr), calcium chloride (CaCl), triethylene glycol, and / or the like, as well as various ionic solutions capable of absorbing water. Other, unlisted compounds with hygroscopic properties may be provided for use as the desiccant solution in certain embodiments. In embodiments described herein, the liquid desiccant includes a hygroscopic feed solution. The liquid desiccant may also be comprised of a surfactant and / or a nanofluid. In certain embodiments, the desiccant solution 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 solution that can be pumped (e.g., by a liquid pump) through at least one desiccant column. In certain embodiments, other materials may be utilized in place of the desiccant solution, including gels, aerogels, desiccant granules that can flow according to granular flow principles, and / or the like.

[0044] Furthermore, the amount of water vapor that a desiccant can absorb (and / or release) depends on the vapor pressure and temperature of the closed system containing the desiccant. Thus, various embodiments are configured to absorb water from the air into the desiccant when the closed system has high vapor pressure and low temperature, and to extract water from the desiccant when the closed system has low vapor pressure and high temperature.

[0045] Absorption of water from the atmosphere

[0046] Water can be extracted from the air by one or more absorbent modules. An AWG system (an example of which is shown in FIGS. 3A and 3B as system 600) can incorporate a single absorbent module or multiple absorbent modules. The absorbent module can be connected to additional modules in the AWG system (including the water extraction module, discussed in more detail below) so that desiccant can flow between the water absorbent module and the additional modules in the AWG system. The flow paths to and from the absorbent module throughout the AWG system can be configurable (e.g., configurable with valves between open and closed configurations) so that the absorbent module can operate as a closed module (desiccant flows only within and / or between multiple absorbent modules) in a batch operating mode before transferring the desiccant to the water extraction module. In other embodiments (e.g., embodiments with open valves or no valves), the desiccant flows freely between the absorbent module and the water extraction module, such as in a continuous-flow operating configuration.

[0047] Additionally, as previously mentioned, the air entering the absorption module (e.g., entering absorber 610 via air flow path 601 as shown in FIG. 4A and exiting the absorber as dry air via flow paths 602-604) may come from a pre-conditioning module configured to increase the humidity of the air prior to water extraction from the air in absorber 610. In other embodiments, air may flow directly into the absorption module from the ambient atmosphere external to the AWG system.

[0048] Certain embodiments of the absorption module include absorbent 610 configured to contact ambient air / atmospheric air (e.g., after preconditioning) with the desiccant (flowing through absorbent 610 along flow paths 621 and 622) to absorb water from the ambient air into the desiccant. Absorbent 610 may be embodied as a container through which the desiccant flows between an inlet (via flow path 621) and an outlet (via flow path 622) and through which the ambient air / atmospheric air flows between an air inlet (flow path 601) and an air outlet (flow paths 602-604, including blower 603). Within the container, the ambient air contacts the desiccant, enabling mass transfer of water vapor from the ambient air to the desiccant. In certain embodiments, one or more baffles, flow interrupters, or packing (e.g., structured or random packing) may be disposed within the absorbent to increase the surface area of ​​the desiccant and / or increase the contact time between the ambient air and the desiccant.

[0049] In certain embodiments, the absorber 610 is configured in a counterflow configuration, with ambient air entering the absorber 610 near its bottom. Dry ambient air then exits the absorber 610 near its top via a specific flow path (using a pump / blower 603 to move air through the absorber 610). Concentrated desiccant (e.g., desiccant fluid) enters the absorber 610 near its top via inlet flow path 621 and flows down the interior of the absorber 610 by gravity. Absorption of water from the ambient air into the desiccant causes dilute desiccant to exit the absorber 610 near its bottom along outlet flow path 622. In certain embodiments, flow modifiers, such as barriers, mesh, packing components, and / or turns, may be used in the outlet piping from the absorber 610 to reduce desiccant carryover at the air outlet of the absorber 610. In certain embodiments, the flow modifier may be located inside the absorbent 610 near the top of the absorbent 610 (e.g., at the mouth of the exhaust port where dry ambient air exits the absorbent via the exhaust air flow path).

[0050] In certain embodiments, the absorber 610 operates in a cross-flow configuration, where air enters one side of the absorber 610 and crosses (e.g., at least substantially horizontally) to the other side. Concentrated desiccant (e.g., desiccant fluid) enters the top of the absorber 610 and flows to the bottom of the absorber 610, absorbing water from the ambient air, where diluted desiccant exits near the bottom. In this configuration, the air flow is at least substantially perpendicular to the flow of desiccant within the absorber 610. In this configuration, the air inlet and air outlet are at approximately the same height in the absorber 610.

[0051] In certain configurations, the absorbent 610 operates in a cross-counterflow configuration, where air enters one side of the absorbent 610 and crosses to the other side. Concentrated desiccant (e.g., desiccant fluid) enters near the top of the absorbent 610 and flows to the bottom of the absorbent 610, absorbing water from the ambient air, where diluted desiccant exits near the bottom of the absorbent 610. In this configuration, the air inlet and air outlet levels are offset from one another. In this configuration, the air inlet can be on a side of the absorbent 610 closer to the top, and the air outlet is on a side of the absorbent 610 closer to the bottom. In another orientation of this configuration, the air inlet is located on a side of the absorbent 610 closer to the bottom, and the air outlet is located on an opposite side of the absorbent 610 closer to the top. The air travels along a path that extends at an angle through the absorbent 610 from the top to the bottom of the absorbent 610 or from the bottom to the top of the absorbent 610 .

[0052] In certain embodiments, the absorbent 610 includes a plurality of packing components around which the concentrated desiccant flows while absorbing water extracted from the moist ambient air. The packing components are provided to increase the surface area of ​​the concentrated desiccant flowing within the absorbent 610 and to provide a highly tortuous flow path for the ambient air flowing through the absorbent 610, resulting in turbulent air flow within the absorbent 610. The absorbent 610 may be embodied as a counterflow vessel, as described above, in which concentrated desiccant (e.g., desiccant fluid) enters the absorbent 610 at a desiccant vessel inlet located at or near the top of the absorbent 610, with the ambient air inlet located at the bottom of the absorbent 610. The ambient air flows upward to a dry air outlet located at or near the top of the absorbent 610, and the desiccant fluid flows downward across the packing components to the diluted desiccant outlet of the absorbent 610. By way of example, the packing components may include individual blocks, balls, trays, baffles, and / or other shapes defining multiple baffles, slits, holes, mesh, and / or other flow-modifying components disposed within the absorbent 610 that may collectively define highly intricate paths for ambient air and desiccant fluid to pass through the absorbent 610. The packing components may include (or be formed from) materials that are non-reactive with the desiccant fluid. Exemplary packing components are shown in FIGS. 5A and 5B. In certain embodiments, multiple packing components (such as the unstructured packing component shown in FIG. 5B) may be disposed within the absorbent 610 without the packing components being physically connected to one another. In other embodiments, a single packing component (such as the structured packing example of FIG. 5A) specifically sized and shaped for the interior of the absorbent 610 may be provided and disposed within the absorbent 610.

[0053] The packing components of certain embodiments may be arranged in a structured configuration to define channels set at different angles to one another, with or without holes, that collectively define structured flow paths for ambient air and desiccant fluid through the absorbent 610. To provide a structured packing configuration, the packing components may be arranged in the absorbent 610 in a stacked manner. The packing components may also be arranged randomly, with multiple geometrically shaped components randomly arranged in the absorbent 610 to increase surface area. While discussed herein as a packing-based absorbent, it should be understood that the desiccant fluid may be passed through the absorbent 610 in other configurations (e.g., by atomizing the liquid desiccant fluid, by spraying the desiccant fluid within the absorbent and / or the like).

[0054] During operation of the entire AWG system, ambient air (at ambient temperature and humidity levels) is directed through the absorber 610. (Although not shown, a blower may be implemented at the intake of the absorber 610 to increase the volumetric flow rate of ambient air entering the absorber 610.) In the absorber 610, the ambient air contacts a concentrated desiccant (e.g., desiccant fluid) applied to the absorber 610 at a low temperature, increasing the vapor pressure within the absorber. This promotes condensation of water vapor from the moist ambient air and its absorption by the desiccant fluid while the moist air is in contact with the concentrated desiccant. As the ambient air and desiccant fluid flow through the absorber 610, the condensation and / or absorption of moisture from the air into the desiccant fluid dilutes the desiccant fluid and dries the air. The dried air then exits the absorber and returns to the atmosphere, as indicated at 602. As shown, a blower 603 may be incorporated at the ambient air outlet of the absorber 610 to increase the volumetric flow rate of air passing through the absorber 610. Blower 603 may be provided in addition to or as an alternative to the previously described blower positioned at the ambient air intake of absorbent 610. Furthermore, as the desiccant fluid passes through absorbent 610, diluted but still cool desiccant fluid exits absorbent 610 as indicated by reference numeral 622.

[0055] According to certain embodiments, diluted desiccant (e.g., desiccant fluid) exits absorber 610 and is directed to pump 623. In certain operations, the absorber module can be operated in a batch configuration where a series of valves can be configured to recirculate the diluted desiccant along a recirculation flow path (with appropriate valves closed to prevent separate concentrated desiccant fluid from entering the closed loop via flow path 637) through a pre-absorber heat exchanger 625 (e.g., a shell-and-tube heat exchanger, a plate heat exchanger, and / or the like) to cool it (on the other side of the heat exchanger is cooling water collected from the overall system, as discussed in more detail herein) and then return it to the top of absorber 610, as shown at 621, by isolating the absorber module from the rest of the AWG system. In this way, the amount of water absorbed by the desiccant fluid can be increased (thereby allowing for a higher level of desiccant dilution) before the desiccant is directed to the evaporator portion of the overall system.

[0056] In certain embodiments, the absorption module includes a pre-absorber heat exchanger 625 that is cooled through the use of a cooling device (e.g., where the cooling medium is separated from the desiccant, such as on both sides of the heat exchanger) that uses a cooling medium (e.g., water, glycol, and / or the like) to cool the concentrated desiccant that flows into the pre-absorber heat exchanger via flow path 624 before entering the absorber 610.

[0057] In certain operations, the absorption module can be operated in a serial configuration, with valves configured to recirculate a certain amount of dilute desiccant fluid along the recirculation path, and a certain amount of dilute desiccant fluid flowing toward the water extraction module through a separate flow path (flow path 626) connecting the absorption module and the water extraction module. In this configuration, a certain amount of dilute desiccant fluid flows along the recirculation path through a pre-absorber heat exchanger 625 (e.g., a shell-and-tube heat exchanger, a plate heat exchanger, and / or the like) where it is cooled (the other side of heat exchanger 625 is cooled by water collected from the entire system) and then returned to the top of the absorber 610, as shown at 621. The dilute desiccant fluid simultaneously travels along separate flow path 626 to the water extraction module. The cooled fluid passes through flow paths 661-667, which comprise a fluid recirculation loop, as well as a cooling system 662 and a pump 664, which ensure sufficient fluid flow through pre-absorber heat exchanger 625. A portion of the fluid then returns to the fluid reservoir via flow path 667.

[0058] In certain embodiments, the absorbent 610 is configured so that the concentrated desiccant is not cooled in a heat exchanger. In this embodiment, the desiccant fluid may be cooled by conductive heat exchange with the ambient air through conductive piping along a specific flow path leading to the absorbent's intake. The absorbent 610 may also cool the fluid by exchanging sensible heat with the ambient air, provided that the air temperature is lower than the temperature of the incoming desiccant fluid.

[0059] By way of example only, the concentrated desiccant fluid moving toward the absorber 610 may be directed through a series of geothermal pipes that have heat transfer characteristics with the surrounding ground directly below the AWG system. The concentrated desiccant fluid may pass directly through the series of geothermal pipes, or it may pass through a two-fluid heat exchanger opposite a cooling fluid maintained at a desired low temperature by geothermal cooling. As yet another example, the desiccant may pass through a heat exchanger (e.g., a shell-and-tube heat exchanger) that cools the desiccant fluid. The heat exchanger may be cooled by a cooling solution that passes through a refrigeration circuit and / or other fluid cooling device to absorb heat from the desiccant fluid before entering the absorber 610.

[0060] As yet another example, a single-stage water integration system may be located near a high-pressure gas well, such as a natural gas well, an oil well (where natural gas is co-extracted with oil), and / or the like. The high-pressure gas may be directed through one or more expansion valves to regulate and / or reduce the pressure of the inlet gas, which experiences a rapid temperature drop due to the Joule-Thompson effect (according to the gas law equation, the volume and quantity of gas remains substantially constant, and a rapid drop in gas pressure across the valve results in a proportionally rapid drop in temperature across the expansion valve). The expanded and subcooled gas may pass through a heat exchanger opposite the concentrated desiccant fluid to absorb heat from the concentrated desiccant fluid and reduce the temperature of the desiccant fluid before entering the absorbent 610. The expanded gas may then be directed away from the AWG system for future use, for example, for collection, combustion, generation of electricity (e.g., via a steam turbine), and / or for heating the desiccant fluid entering the water extraction module, as discussed herein.

[0061] In certain embodiments, absorber 610 is configured so that the diluted desiccant fluid exits absorber 610 and is sent to the water extraction module without a recirculation path. The concentrated desiccant fluid returning from the water extraction module may or may not be cooled by a heat exchanger, chiller, and / or geothermal cooling before entering absorber 610. For example, if an appropriate valve is closed to prevent the diluted desiccant from being recirculated to absorber 610 as described above, the diluted desiccant exiting absorber 610 is pumped along a flow path extending between the absorption module and the water extraction module.

[0062] In certain embodiments, the absorbent material 610 may be embodied as a membrane-separated absorbent material having a desiccant flow path on a first side of the porous membrane and an air flow path on a second, opposite side of the porous membrane. Separating the air flow path from the desiccant solution flow path can prevent undesirable mass flow of the desiccant salt (e.g., aqueous desiccant salt) itself toward the air flow path and ultimately out of the AWG system. Also, water can be absorbed from the air by the desiccant based on the flow of water permeating through the membrane 610 from the air to the desiccant solution. Water vapor can then condense on the second side of the membrane, pass through the membrane pores by capillary action, and be absorbed by the concentrated desiccant solution with a high salt content. In certain embodiments, the membrane is embodied as a porous membrane with pores of appropriate size (e.g., average pore size, maximum pore size, and / or similar size) to allow water molecules to pass through the membrane while preventing the desiccant salt from passing through the membrane. By way of example, the porous membrane may be a nonwoven material such as polytetrafluoroethylene (PTFE), expanded polytetrafluoroethylene (ePTFE), polypropylene (PP), polyvinylidene fluoride (PVDF), and / or the like. Other materials (including nylon and / or other synthetic materials) may also be used in certain embodiments. Synthetic and / or natural materials may be utilized in various embodiments. In certain embodiments, the porous membrane may be at least partially woven. In certain embodiments, the membrane may be organic, inorganic, polymeric, mesoporous, ceramic, and / or the like. In certain embodiments, the membrane may comprise a metal-organic framework, carbon nanotubes, and / or combinations thereof. The membrane may be hydrophilic and / or hydrophobic, or may be treated (e.g., with a coating) to render it hydrophilic and / or hydrophobic. Exemplary membrane geometries include spiral wound, flat plate and frame, or tubular. As the desiccant solution and water pass across the membrane, water molecules move (by capillary action) from the desiccant solution through the membrane and into the permeate stream (e.g., water vapor and / or liquid water).In certain embodiments, the membrane may be provided with mechanical support by being supported within a frame via spacers such as lattices, grids, and / or the like to maintain a desired orientation within the housing.

[0063] Various embodiments of the absorbent module include a multi-tiered absorbent configuration that includes multiple absorbents arranged in series (such that the desiccant flows from a first absorbent through a second absorbent and then through additional absorbents in the multi-tiered absorbent configuration), or a multi-tiered absorbent configuration that includes multiple absorbents arranged in parallel such that the desiccant is divided and flows through the multiple absorbents in parallel.

[0064] Additionally, multiple absorbents may be arranged in series within the air flow path, allowing supply air to be drawn from the environment, pass through the multiple absorbents in series, and then be discharged to the environment as dry air. For example, the supply air may first pass through a low-concentration absorbent to absorb a first amount of water from the air, and then pass through a high-concentration absorbent to absorb a second amount of water from the air. The initial absorption process using a low concentration of desiccant fluid requires less energy (and thus does not require a low vapor pressure between the air and the liquid desiccant) to absorb the first amount of water from the air. After the initial absorption process, which requires less energy, the air (still containing water vapor) passes through a second absorbent having a high concentration of desiccant fluid to absorb the second amount of water from the air. This dry (e.g., low humidity) air may then be discharged from the system to the environment.

[0065] On the desiccant side, once the diluted desiccant leaves the low concentration absorbent, the desiccant fluid is passed to a water extraction module as discussed herein, where water is extracted therefrom (resulting in the desiccant being re-concentrated).

[0066] In certain embodiments, each absorbent material may be in fluid communication with a corresponding water extraction module such that each absorbent material is associated with a separate and independent desiccant flow path loop. For example, a first amount of desiccant fluid may flow between the first absorbent material and the first water extraction module, and a second amount of desiccant fluid may flow between the second absorbent material and the second water extraction module, where the first amount of desiccant fluid is immiscible with the second amount of desiccant fluid. In certain embodiments, the first amount of desiccant fluid may include a first desiccant (e.g., LiCl) and the second amount of desiccant fluid may include a second desiccant (e.g., CaCl).

[0067] Furthermore, in embodiments including multiple independent desiccant streams, each desiccant stream may have a different concentration range. For example, a first desiccant stream (e.g., corresponding to a first absorbent material through which the feed air passes) may have a first concentration range measured between a high concentration value at the outlet of the water extraction module and a low concentration value at the outlet of the absorbent material, and a second desiccant stream may have a second concentration range. If the feed air is directed through a series of absorption columns, the air may first be directed through the absorption column with the lower concentration range and then through the absorption column with the higher concentration range.

[0068] Membrane-based water extraction from desiccants

[0069] The water extraction module is configured to remove water from the diluted desiccant (e.g., diluted desiccant fluid) and store it for use as drinking water or other clean liquid water. The water extraction module includes one or more membrane-based water extractors (e.g., connected in series or parallel) and is connected to the absorption module via various flow paths to allow the desiccant (e.g., diluted desiccant and concentrated desiccant) to flow between the absorption module and the water extraction module. The membrane-based water extractors (also referred to as fluid separators) also serve to concentrate the desiccant solution to obtain a concentrated desiccant retentate solution that can be reprocessed through the atmospheric water generation system.

[0070] The water extraction module comprises at least one membrane-based water extraction device 633 (FIG. 4B) that defines two flow paths separated by a permeable membrane 633a. On a first side of the permeable membrane 633a, the desiccant flows along the desiccant flow path (between flow path 632 and flow path 634), and on the opposite second side of the permeable membrane, the permeate fluid (e.g., water vapor) is entrained and then migrates (into portion 633c disposed within the water extraction device between flow path 650 and flow path 651). Both the desiccant (on first side 633b of the permeable membrane 633a) and the entrapped permeate fluid (on second side 633c of the permeable membrane 633a) contact both sides of the permeable membrane 633a while passing through it. This allows the membrane 633a to separate the desiccant flow path from the capture permeate (water vapor) flow path, which contains water vapor (e.g., water vapor moving through the porous membrane 633a) that is collected and condenses into a liquid permeate stream (e.g., downstream of the membrane-based water extraction device) during the water collection / fluid separation process. In certain embodiments, increasing the vapor pressure of the desiccant can enhance water vapor mass transfer across the membrane 633a. This can be achieved by heating the desiccant prior to contact with the membrane 633a (at the desiccant side 633b of the membrane). Reducing the pressure on the permeate side 633c of the membrane 633a (e.g., by using a vacuum mechanism) can also induce water vapor mass transfer across the membrane. As the desiccant passes through the porous membrane 633a (the first desiccant side 633b of the membrane), the water in the desiccant begins to permeate across the membrane 633a in a vapor state and exits the membrane 633a (the second side) in a vapor state. The water vapor then condenses upon cooling (eg, at least partially by application of a heat exchanger (eg, condenser 627) and / or contact with a cooler fluid (eg, condensed water)) and flows along the water flow path.

[0071] In certain embodiments, the desiccant side 633b may be heated by a heating fluid (e.g., heated oil, steam, glycol, and / or the like) separated from the desiccant flow path via a thermally conductive layer (e.g., a thermally conductive non-porous film, metal sheet, and / or the like) within the membrane-based water extraction device. In certain embodiments, the desiccant side 633b may be embodied as a shell / tube heat exchanger, with the heating fluid flowing through the tubes and the desiccant flowing through the shell, certain walls of the shell embodied as porous membranes 633a. In certain embodiments, the heating fluid may be a product of the AWG system, which may utilize sensible heat transfer to heat the desiccant fluid and facilitate the movement of water vapor across the membrane. In other embodiments, the heating fluid may be a product (e.g., a final product, waste product, or intermediate product) of a spatially nearby process, such as mining, gas extraction, power generation, and / or similar processes.

[0072] As discussed in more detail herein, the permeate side 633c may similarly comprise a heat exchanger configuration that reduces the temperature of the permeate fluid to promote its condensation. For example, a cooling fluid (e.g., liquid water extracted from the liquid water storage tank 655, a coolant (e.g., glycol), and / or the like) may be separated from the permeate flow path by a thermally conductive layer (e.g., a thermally conductive nonporous film, a metal sheet, and / or the like). The cooling fluid cools the thermally conductive layer, thereby providing a surface within the permeate fluid stream upon which water vapor may condense. In certain embodiments, the permeate side 633c may be embodied as a shell / tube heat exchanger, with the cooling fluid flowing through the tubes and the permeate fluid flowing through the shell, certain walls of the shell embodied as porous membranes 633a. In such embodiments, the outer surfaces of the tubes provide the condensation surface for water vapor. In certain embodiments, the cooling fluid may be a product of the AWG system (e.g., liquid water) and may cool the permeate by utilizing sensible heat transfer to promote water vapor transport across the membrane and promote condensation of the water vapor.

[0073] The membrane 633a may include a hydrophobic porous membrane, such as a nonwoven membrane with small pore sizes. By way of example only, the membrane may include PTFE, ePTFE, PP, PVDF, and / or the like, which are hydrophobic by design. In certain embodiments, the membrane may be organic, inorganic, polymeric, mesoporous, ceramic, and / or the like. In certain embodiments, the membrane may include metal-organic frameworks, carbon nanotubes, and / or combinations thereof, such as by layering layers of materials. The membrane may be hydrophilic or hydrophobic, or may be treated (e.g., with a coating) to render it hydrophilic and / or hydrophobic. The use of a hydrophobic material (or a material with a hydrophobic coating) encourages water vapor to selectively pass through the membrane and be retained on the permeate side 633c of the membrane. Applying a layer of hydrophobic material to the membrane on the desiccant side 633b allows only volatile vapors to pass through, while retaining the liquid fluid on the desiccant side 633b of the membrane. As examples of membrane shapes, the membrane may be spiral wound, flat plate and frame, or hollow tubular. As the desiccant solution flows across the desiccant side 633b of the membrane, water molecules (by capillary action) migrate in vapor form from the desiccant solution through the membrane to the permeate side 633c, leaving a concentrated desiccant solution on the desiccant side 633b of the membrane 633a.

[0074] The membrane-based water extraction device 633 is embodied as a housing having a desiccant inlet and a desiccant outlet on the desiccant side 633b of the membrane 633a and a permeate inlet and a permeate outlet on the permeate side 633c of the membrane 633a. In other exemplary embodiments, the membrane-based water extraction device 633 may utilize gravity to remove permeate fluid from the membrane-based water extraction device; in such embodiments, the permeate flow path need not include an inlet (because gravity alone is sufficient to move the permeate fluid through the device's outlet). For example, as the desiccant fluid flows from the inlet to the outlet of the membrane-based water extraction device, water vapor travels through the membrane and forms vapor on the permeate side of the membrane. The permeate side of the membrane may be cooled (e.g., by a cooling fluid separated from the permeate side of the membrane by a thermally conductive film), and water may condense on the permeate side of the membrane-based water extraction device and fall (under gravity) through an outlet port located at the lower end of the permeate side of the membrane.

[0075] The desiccant flow channel extends between the desiccant inlet and the desiccant outlet. The permeate (water) flow channel extends between the permeate inlet and the permeate outlet. In certain embodiments, the permeate outlet may be located below the permeate inlet (and at the opposite end of the membrane-based water extraction device) to utilize gravity to facilitate permeate flow from the membrane-based water extraction device. As previously mentioned, the desiccant and permeate flow channels are each bounded on either side by a porous membrane 633a. By separating the desiccant fluid from the permeate stream, the membrane 633a prevents mass transfer of dissolved solids from the desiccant to the resulting permeate stream, preserving the desiccant for continued use and maintaining the purity of the captured water. Similarly, the membrane 633a prevents the transfer of gas (e.g., sweep gas) on the permeate side of the membrane from the permeate stream to the desiccant stream.

[0076] In certain embodiments, the housing defines two parallel flow paths contacting opposite sides of the porous membrane 633a in a countercross-flow manner, as shown in FIG. 6A , where a first flow path is a desiccant flow path 633b and a second flow path is a permeate flow path 633c, and the porous membrane 633a is embodied as a planar membrane (e.g., defined within a frame) separating the desiccant flow path 633b from the permeate flow path 633c. In certain embodiments, the housing may be configured to permit access to the membrane for maintenance purposes, such as replacing the porous membrane as needed. In other embodiments, a first flow path (e.g., a desiccant flow path) may flow horizontally across the surface of the membrane 633a, and a second flow path (e.g., a permeate flow path) may flow vertically across the opposite surface of the membrane, e.g., the permeate flow outlet may be below the permeate flow inlet.

[0077] In other embodiments, the desiccant flow path may be defined by a desiccant inlet that directs the desiccant toward the membrane (e.g., at an angle or at least substantially perpendicular to the first side of the membrane), and after contacting the membrane, the desiccant is directed toward an outlet. This embodiment is a dead-end flow, where the influent desiccant interfaces with the membrane in a direction at least substantially normal (perpendicular) to the permeate flow path on the opposite side of the porous membrane. In this embodiment, the permeate flow path flows parallel to the porous membrane. An example of this configuration is shown in Figure 6B.

[0078] Additionally, in other embodiments, such as that shown in FIG. 6C, the housing may define a lumen-like flow path, with the first flow path at least substantially concentric with the second flow path. The wall of the first flow path (separating the first and second flow paths) may be defined at least in part by a porous membrane. In certain embodiments, the porous membrane may extend partially around the first flow path. In other embodiments, the porous membrane may extend the entire circumference of the first flow path. By way of example only, the first inner flow path may be a desiccant flow path and the second outer flow path may be a permeate flow path, with permeate moving from the inner flow path to the outer flow path through the porous membrane. As another example, the first inner flow path may be a permeate flow path and the second outer flow path may be a desiccant flow path, with permeate moving from the outer flow path to the inner flow path through the porous membrane.

[0079] In a lumenal flow membrane-based water separation device, the permeate and desiccant channels may run in the same cocurrent or countercurrent direction. In certain embodiments, these flows may be horizontal or vertical. In a vertical orientation, the permeate side may flow downward, thereby utilizing gravity to facilitate the flow of water (after condensation) out of the membrane-based water separation device.

[0080] To achieve separation of water from the desiccant solution, a chemical potential difference is introduced. This may be achieved by a transmembrane temperature gradient, a transmembrane pressure gradient, and / or a transmembrane concentration gradient between the desiccant channel 633b, the membrane 633a, and the permeate channel 633c. The transmembrane temperature gradient may be achieved by heating the desiccant fluid channel 633b and / or cooling the permeate liquid water channel 633c. The temperature of the desiccant fluid and / or liquid water can be manipulated using any heating / cooling source, including, but not limited to, heat exchangers, heating elements, waste heat, geothermal heat, solar heat, geothermal cooling, cooling ponds, cooling streams, sweep gases, and / or the like. For example, a membrane-based water extraction device can incorporate a heat exchange arrangement across a non-porous film on the desiccant side of the membrane (e.g., a heating fluid can heat the desiccant fluid as it flows across the surface of the membrane) and / or a cooling arrangement on the permeate side of the membrane (e.g., a cooling fluid separated from the permeate fluid across a non-porous film can cool the permeate fluid). The pressure gradient across the membrane can be achieved by a higher pressure on the desiccant side of the membrane and / or a lower pressure on the liquid water side of the membrane. The pressure difference between the desiccant side of the membrane and the permeate side of the membrane can be induced by mechanisms such as, but not limited to, a high-pressure pump, a pump, a blower, a compressor, a vacuum pump, a Venturi vacuum induction mechanism, and / or the like. Additionally, the use of one or more pumps and / or agitators on the desiccant or permeate side may ensure uniformity of the desiccant and / or liquid water properties. Finally, the pressure and / or temperature difference can result in a vapor pressure difference on both sides of the membrane, facilitating the movement of water vapor through the membrane from the desiccant side to the permeate / water vapor side of the membrane. Specifically, the vapor pressure on the permeate side of the membrane can be lower than the vapor pressure on the desiccant side of the membrane (e.g., thereby facilitating water permeation through the membrane using an induced vacuum).

[0081] In certain embodiments, the membrane-based water extraction apparatus is configured to utilize the aforementioned mechanisms to enhance the chemical potential. In one example incorporating vacuum membrane distillation (VMD), a pressure gradient across the membrane 633 is introduced by pressurizing the permeate outlet path 651 to a vacuum pressure (e.g., by utilizing one or more vacuum pumps, such as compressor 652, positioned downstream of the membrane-based water extraction apparatus 633 along the permeate flow path). By way of example only, a vacuum pump can be located in the permeate storage tank 655 and / or along the gas vent flow path 659 from the water storage tank 655. In this embodiment, the absolute pressure on the desiccant side 633b is greater than the absolute pressure on the permeate side 633c. The interior of the membrane-based water extraction apparatus may be similar to that shown in Figures 5A-5C. In certain embodiments, additional components, such as heating and / or cooling fluid streams (as described below), may be incorporated into the VMD configuration of the membrane-based water extraction apparatus to further enhance the efficiency of the water extraction process.

[0082] In another exemplary embodiment, an air gap membrane distillation (AGMD) process is utilized to facilitate water vapor permeation across membrane 633a to permeate side 633c of membrane 633a. Exemplary AGMD configurations are shown in Figures 5D and 5E, each of which convey a cooling fluid (e.g., cooling water directed from storage tank 655 along flow path 658 to flow path 650 on permeate side 633c of membrane 633a and thus to membrane-based water extraction device 633) along a cooling fluid flow path separated from permeate flow path 633c by a thermally conductive, non-porous film on the permeate side 633c of the membrane. Cooling fluid flowing along flow path 633d sandwiches an air gap between non-porous membrane 633e (which separates cooling fluid flow path 633d from permeate side 633c of the membrane) and porous membrane 633a. The resulting air gap contains non-porous membrane 633e, which facilitates condensation via heat transfer. This air gap serves as a pathway for condensate separated from the desiccant through the porous membrane. Because the cooling fluid is at a temperature below the heated desiccant fluid, a temperature gradient is created from the heated desiccant side 633b of the module to the cold, non-porous membrane that holds the cooling fluid. The cold side also condenses the transported vapor to a liquid state. The greater the temperature gradient (difference between the heated desiccant fluid and the cooling fluid), the greater the driving force created to separate the desiccant-rich water molecules across the porous membrane, thereby improving the separation performance of the membrane-based water extraction device. As described above, the water vapor within the cavity may be directed out of the housing of the membrane-based water extraction device based on a vacuum created within the cavity, a sweep gas flowing through the cavity, and / or gravity, which drives the condensed water downward and out an outlet located at the lower end of the cavity. In certain embodiments, the housing defines three outlets: a desiccant outlet (to flow path 634), a permeate outlet (to flow path 651), and a cooling fluid outlet (for recirculating the cooling fluid along the cooling fluid flow path). In certain embodiments, the housing defines at least two inlets, including a desiccant inlet (from flow path 632) and a cooling fluid inlet (e.g., from flow path 650) (in cases where the permeate fluid does not require an inlet, such as when gravity is used to direct the permeate fluid out of the void).In other embodiments, the housing defines at least three inlets, including a desiccant fluid inlet (from flow path 632) (if a permeate fluid inlet is needed, such as when vacuum pressure or a sweep gas is used to direct the permeate out of the housing), a permeate fluid inlet (e.g., allowing gas flow through the permeate side 633c of the membrane), and a cooling fluid inlet (e.g., from flow path 650).

[0083] Although shown as a flat, imperforate membrane 633d, it is understood that the permeate side of membrane 633a may be embodied as a shell-and-tube heat exchanger configuration (with the walls of the tubes embodying imperforate film 633e and the cooling fluid flowing inside the tubes).

[0084] Additionally, in certain embodiments, a similar configuration may be implemented on the desiccant side of the membrane by utilizing a heating fluid separated from the desiccant by a non-porous thermally conductive film, as shown in FIG. 6E. In such embodiments, a heating fluid (e.g., heating oil, steam, heated coolant, and / or the like) passes along the heating fluid flow path 633f from the desiccant fluid 633b on the opposite side of the non-porous film 633g. The heating fluid transfers heat to the desiccant flowing through the desiccant flow path 633b, which promotes water vapor permeation across the porous membrane 633a. In particular, when the configuration of the heating fluid flow 633f is integrated with the configuration of the cooling fluid flow 633d, a large chemical potential difference is introduced between the desiccant flow 633b and the permeate flow 633c, promoting water transport across the membrane 633a. As described above, water vapor within the void may be directed out of the housing of the membrane-based water extraction device based on a vacuum created within the void, a sweep gas flowing through the void, and / or gravity, which causes condensed water to flow downward and exit through an outlet located at the lower end of the void. In certain embodiments, the housing defines three outlets: a desiccant outlet (to flow path 634), a permeate outlet (to flow path 651), a heating fluid outlet (e.g., for recirculating the heating fluid along the heating fluid flow path), and a cooling fluid outlet (for recirculating the cooling fluid along the cooling fluid flow path). In certain embodiments, the housing defines at least three inlets, including a desiccant inlet (from flow path 632), a heating fluid inlet, and a cooling fluid inlet (e.g., from flow path 650) (for cases in which the permeate fluid does not require an inlet, such as when gravity is used to direct the permeate fluid out of the void). In other embodiments, the housing defines at least four inlets, including a desiccant fluid inlet (from flow path 632) (if a permeate fluid inlet is required, such as when vacuum pressure or a sweep gas is used to direct the permeate out of the housing), a permeate fluid inlet (e.g., allowing gas flow through the permeate side 633c of the membrane), a heating fluid inlet, and a cooling fluid inlet (e.g., from flow path 650).

[0085] As shown in either Figure 6D or Figure 6E, separating the permeate stream 633c from the cooling fluid 633d can reduce the vapor pressure on the permeate side 633c of the membrane, thereby increasing the efficiency of water permeation through the membrane. The implementation of vacuum pressure, sweep gas, and / or other flow-enhancing mechanisms in the permeate stream 633c can encourage the water vapor on the permeate side 633c of the membrane to exit through the permeate outlet of the membrane-based water extraction apparatus 633 and then be guided to one or more compressors (which can incorporate the beneficial features of mechanical vapor compression, similar to U.S. Patent Application No. 17 / 552,173, filed December 15, 2021, the entire contents of which are incorporated herein by reference). The water vapor exiting the permeate outlet of the membrane-based water extraction apparatus can flow to one or more heat exchangers and / or one or more condensers 627, where it condenses to liquid water and is then stored in a storage tank 655.

[0086] In another embodiment, a chemical potential across the membrane 633a is driven by implementing a direct contact membrane distillation (DCMD) process. In a DCMD configuration, the permeate side 633c of the porous membrane 633a carries a cooling fluid (e.g., cooling water) that directly contacts the membrane 633a. In such a configuration, water is directed directly from the storage tank 655 to the permeate stream 633c, maintaining a low temperature on the permeate side 633c of the membrane 633a. The cooling fluid is cooler than the desiccant fluid, creating a temperature gradient across the membrane 633a from the heated desiccant side 633b to the direct contact cooling fluid on the permeate side 633c of the membrane 633a. The cooling fluid may be withdrawn from the storage tank 655 and directed along flow paths 658, 650, and 633c to the membrane-based water extractor 633 (and exits the membrane-based water extractor via flow path 651). In certain embodiments, a portion of the water exiting storage tank 655 along flow path 658 may be directed to an external system for use as liquid water. A cooling fluid (e.g., liquid water from storage tank 655) is supplied to permeate side 633c of membrane 633a, which condenses the water vapor that permeates membrane 633a and displaces the water vapor separated from the desiccant-rich fluid. The greater the temperature gradient (difference between the heated desiccant fluid and the cooling fluid), the greater the driving force generated to separate the desiccant-rich water molecules across the porous membrane, thereby improving the separation performance of the membrane-based water extraction device.

[0087] As yet another example, a sweep gas membrane distillation (SGMD) process may be utilized to create a chemical potential across the membrane 633a. The SGMD configuration can be combined with AGMD and / or DCMD to further improve the efficiency of such configurations. In an SGMD configuration, the permeate side 633c of the membrane 633a carries a sweep gas (e.g., nitrogen gas, humid air, inert gas, and / or the like) that carries the permeate fluid (e.g., water vapor) that has permeated the porous membrane away from the porous membrane 633a. In certain embodiments, the sweep gas can carry the permeate water vapor to the compressor 652 and / or the condenser 627, where the water vapor condenses to liquid water. The sweep gas can be separated from the permeate water vapor by bringing the mixture to the water dew point, and ultimately flows away from the liquid water along flow path 659 and out of the storage tank 655. The sweep gas can be returned to the storage tank and recycled to the system along flow path 660, as described above. Condensing the permeate vapor to a liquid allows the water to be stored in product water tank 655. In certain embodiments, SGMD configurations utilize an inert gas-state fluid as a sweep gas that does not contaminate the product water. In certain SGMD embodiments, the gas flow to permeate channel 633c is heated to maintain the permeate's physical state (vapor state). To help maintain the vapor state, a heat tracing element can be used to prevent the fluid from becoming liquid due to cooling by the fluid pipe walls. The water vapor can then be transported to condenser 627 downstream of membrane-based water extraction device 633 to condense the water, which can then be stored in water storage tank 655. Additionally, in SGMD configurations, a sweep gas can be introduced to the membrane-based water extraction device along flow paths 660 and 650. The sweep gas can be routed away from the water storage tank, such as along flow path 659, as shown in FIG. 4B, to keep it away from the condensed liquid water.

[0088] In certain embodiments, the water extraction module includes one or more heating mechanisms along the flow path that directs the desiccant fluid (at the desiccant side 633b of the membrane 633a) to the intake air of the membrane-based water extraction device. In one exemplary embodiment, the desiccant fluid is heated to a temperature of approximately 40-80°C. This process results in adequate separation even at low temperatures (approximately 40°C). In certain embodiments, higher temperatures (e.g., approximately 60-80°C) may result in more efficient separation.

[0089] For example, the diluted desiccant exiting the absorption module passes through one or more heating subsystems between the absorption module and the membrane-based water extraction device. These heating subsystems are provided as part of the water extraction module. These one or more heating subsystems may include one or more of a condenser 627, a pre-extraction heat exchanger 629, and / or a heater 631. It is understood that these one or more heating subsystems may be provided in any order relative to the desiccant flow. In one example, the diluted desiccant, which remains at a low temperature after passing through the absorbent 610, passes through a condenser 627, which takes advantage of the generally lower temperature of the diluted desiccant to promote condensation of water from the water vapor flowing along the permeate flow paths 651-654 (e.g., the water flow paths, including the water flow path on the second side of the porous membrane). In certain embodiments, the condenser 627 is a shell-and-tube heat exchanger in which the diluted desiccant (upstream of the membrane-based water extraction device 633) passes through the tubes and the water vapor condenses on the exterior of the tubes within the shell of the heat exchanger. In another embodiment, the condenser 627 is a plate-and-frame heat exchanger in which the diluted desiccant fluid passes through one set of plates and the water vapor passes through the other set of plates. As the water vapor traverses the heat exchanger warming the diluted desiccant, it condenses in the heat exchanger. In another embodiment, the condenser 627 is a dual-pipe heat exchanger in which the diluted desiccant passes through the inner pipe and the water vapor passes through the outer pipe, allowing it to condense on the outer surface of the inner pipe. In certain embodiments, the condenser 627 may have a counterflow configuration (in which the diluted desiccant flows in the opposite direction to the water vapor). In other embodiments, the condenser 627 may have a co-flow configuration in which the diluted desiccant and the water vapor flow in the same direction through the condenser 627.

[0090] The diluted desiccant exits condenser 627 via flow path 628 at an elevated temperature due to a certain amount of heat transferred from the water vapor to the diluted desiccant within condenser 627. The diluted desiccant then passes through 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 (with concentric tubes), and / or the like) and / or a heater 631 (e.g., an externally powered heater such as an electric heater, a natural gas heater, a solar heater, and / or the like) to increase the temperature to or near the evaporation temperature. In certain embodiments, the heater may be an in-line electric heater including a bundle of heating elements for heating the diluted desiccant fluid. The heater may be oriented to reduce the likelihood of fluid spurting over the elements. The heater 631 may be located within the housing of the membrane-based water extraction device. In certain embodiments, the heater is a heat exchanger (e.g., a shell-and-tube heat exchanger, a plate-and-frame heat exchanger, and / or the like). 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 comprises a geothermal heating mechanism that includes a series of pipes that extend into the earth and utilize geothermal energy to heat the diluted desiccant fluid. In other embodiments, heater 631 is a combustion heater that combines a hydrocarbon fuel source (e.g., natural gas, oil, wood, biomass, and / or the like) with oxygen (supplied from ambient air) to generate heat by combustion.

[0091] In embodiments including both a pre-extraction heat exchanger 629 and a heater 631, the dilute desiccant fluid first exits the pre-extraction heat exchanger 629 via flow path designated 630 and then enters the heater 631. Additionally, the opposite side of the pre-extraction heat exchanger 629 is supplied with heated concentrated desiccant fluid exiting the membrane-based water extraction device, as discussed in more detail herein.

[0092] As the desiccant exits the heater 631 (if used), it flows along flow path 632 and enters the housing, specifically the desiccant inlet of the membrane-based water extraction device. In the membrane-based water extraction device, the desiccant solution directly contacts the membrane. By utilizing temperature, pressure, and / or concentration differences, water moves through the membrane and is collected on the second side. The water may move through the membrane as a liquid and / or vapor. The water may then be distributed for use and / or collected in a storage tank 655. In certain embodiments, the vapor on the liquid water side of the membrane may be collected and condensed with cold liquid water or another cryogenic fluid. The vapor on the liquid water side of the membrane may be swept away from the membrane by a sweep gas flowing through the membrane-based water extraction device on the liquid water side of the membrane. The water vapor may then condense to liquid water in another process using a heat transfer process, such as a heat exchanger or other embodiment of a heat transfer process (the opposite side of the heat exchanger and / or condenser may define a portion of the flow path of a cooled fluid, such as a diluted desiccant, before entering the desiccant side of a membrane-based water extraction apparatus). In certain embodiments, after exiting the membrane-based extractor 633, the vapor enters a heat transfer process directly on the permeate side of the membrane. The heat transfer process may be a heat exchanger 629, which condenses the water vapor to liquid water, or other embodiment of a heat transfer process. In other embodiments, a vacuum may be induced on the permeate side of the membrane to achieve a pressure differential between the desiccant and permeate sides of the membrane. Water enters the membrane as a liquid and / or vapor and exits the membrane as a vapor on the permeate side. The water flow path directs water to storage tank 655 (via flow paths 651-654, which may include a pump, heat exchanger 627, compressor 652, and / or other flow aids). Additionally, the water flow path circulates from the storage tank via flow path 650 (which in certain embodiments includes one or more pumps, not shown) to the membrane-based water extractor 633. In certain embodiments, a sweep gas (e.g., moist air) is blown into the water flow path (e.g., by a blower along the water flow path) to push water vapor from the membrane-based extractor 633 to a compressor 652 and ultimately to a condenser 627.

[0093] In certain embodiments, the permeate vapor is compressed to a high pressure by mechanical and / or thermal means (e.g., compressor 652). The vapor then passes through heat exchanger 627, allowing the latent heat to be used to heat the desiccant solution, and through which the vapor condenses into a liquid.

[0094] The membrane-based water extraction apparatus 633 may be configured for batch operation, in which the desiccant fluid repeatedly contacts the membrane (without directing the desiccant to the absorption module) by circulating the desiccant in a closed loop until the desired amount of water is separated. The valves in the water extraction module may be configured to provide a closed-loop flow of the desiccant solution. After the desired concentration of the desiccant solution is reached, the desiccant solution is returned to the absorption module by reconfiguring the valves to allow flow of desiccant from the water extraction module to the absorption module. The membrane-based water extraction apparatus 633 may include parallel subunits in which multiple membranes are contained within a single apparatus and / or systems consisting of multiple membrane-based water extraction apparatuses operating in parallel (each operating to separate water from a portion of the desiccant solution). In certain embodiments, the membrane separation subunits may also be configured in series. In this configuration, the desiccant solution contacts a first membrane, and a fixed amount of water migrates through the first membrane. The retained desiccant solution from the first membrane is fed to a second membrane as a desiccant solution, which further separates water from the desiccant solution. This process is repeated for each of the membrane separation subunits in the series. In certain embodiments, a combination of parallel and series units may be utilized.

[0095] In certain embodiments, the membrane-based water extraction device 633 is configured for continuous operation, where the desiccant stream flows in direct contact with the membrane (e.g., perpendicular, parallel, or tangential to the membrane plane) and water is continuously separated from the desiccant solution through the membrane. Continuous mode operation may utilize series and / or parallel subunits as described in the previous section. During continuous operation, the desiccant flows in a continuous loop from the absorption module to the water extraction module and back to the absorption module.

[0096] In certain embodiments, the membrane-based water extraction device may be provided in combination with an evaporation-based water extraction device (e.g., an evaporation vessel for evaporating water from a desiccant and a condenser for condensing the evaporated water into liquid potable water). For example, the membrane-based water extraction device may be provided upstream (along the desiccant flow path) of an evaporation vessel, such as the evaporation vessel described in co-pending U.S. patent application Ser. No. 17 / 552,173, filed December 15, 2021, the entire contents of which are incorporated herein by reference. Alternatively (or additionally), the membrane-based water extraction device may be located downstream (along the desiccant flow path) of the evaporation vessel described above.

[0097] Carbon dioxide capture

[0098] Treated air (which may include air from a water integration system as discussed herein) may be passed through a carbon dioxide capture system prior to being released to the atmosphere. Carbon dioxide may be captured from the air and filtered and / or disposed of (e.g., by one or more chemical processes that convert the carbon dioxide into disposable water, oxygen, and / or solid or liquid compositions, capturing the carbon dioxide in a filtering medium, and / or similar processes).

[0099] The carbon dioxide capture system may include a carbon dioxide capture column 102 having a fixed bed of carbon dioxide absorbent material (e.g., sodium hydroxide solution). As air passes over the carbon dioxide absorbent material, carbon dioxide is absorbed by the material. Additionally, heating of the carbon dioxide capture column 102 (e.g., by a hot fluid jacket) may help increase carbon dioxide absorption by the absorbent material, as shown in Figure 3.

[0100] As yet another example, the carbon dioxide capture material may be configured to reversibly absorb carbon dioxide such that the captured carbon dioxide can be compressed and stored as a gas for later use.

[0101] In certain embodiments, the captured carbon dioxide gas may be directed to a greenhouse to optimize the internal greenhouse environment for plant growth. As discussed herein, the greenhouse may be supplied with water produced by the AWG system discussed herein.

[0102] Water Pumping System

[0103] In certain embodiments, the AWG system may include a fluid excitation system (668 in FIG. 4A) for exciting molecules of a liquid desiccant solution embodied as a hygroscopic feed solution to promote evaporation of water absorbed by the liquid desiccant while minimizing any resulting mass transfer of the liquid desiccant itself to a water collection system. The fluid excitation system may be integrated with an evaporation column, a membrane separation system as discussed herein, or used alone to remove water from the liquid desiccant. In an exemplary embodiment, the fluid excitation system includes a unit configured to increase the energy level of the liquid desiccant to enable (or facilitate) separation of the liquid desiccant from the water. As shown in FIG. 4A, the fluid excitation system 668 may be located upstream of a water extraction system (e.g., membrane-based system 633). As shown, the fluid excitation system 668 is upstream of one or more heat transfer devices to further increase the temperature of the diluted desiccant before feeding it to a separation system. However, it is understood that the fluid excitation system 668 may be located immediately upstream of a water separation unit that is utilized (as may be downstream of any other heating mechanisms that are utilized). The fluid excitation system facilitates the separation of purified water from concentrated liquid desiccant. In certain embodiments, the fluid excitation system includes energy application systems, pumps, valves, compressors, and / or piping as needed to maintain the required flow of liquid desiccant into and out of the fluid excitation system, the required flow of water (and / or water vapor) into and out of the fluid excitation system, and / or similar flows.

[0104] To achieve separation of water from the liquid desiccant, excitation of water molecules absorbed in the liquid desiccant is used. In certain embodiments, excitation can be achieved by applying ultrasound to the liquid desiccant. In this embodiment, ultrasound is generated by an ultrasound generator to excite the water molecules to a high energy state, where the water molecules gain high enthalpy and entropy corresponding to the high temperature. With sufficient excitation, the water molecules transition from a liquid state in the liquid desiccant to a vapor state. In certain embodiments, ultrasound can be applied as pulses, and the frequency and amplitude of the ultrasound pulses can be adjusted to enable optimal excitation based on the composition of the liquid desiccant. In the embodiments described herein, optimal excitation refers to excitation of the liquid desiccant that promotes water extraction, such as by evaporation of water contained in diluted liquid desiccant.

[0105] As another example, application of microwaves to a liquid desiccant promotes excitation of water molecules in the liquid. In this embodiment, microwaves generated by a microwave generator excite the water molecules to a higher energy state, where the water molecules gain high enthalpy and entropy corresponding to the higher temperature, transitioning from the liquid phase to the vapor phase and enabling separation of the water from the liquid desiccant. In certain embodiments, the excitation may be induced by an electromagnetic field generator. In this embodiment, the electromagnetic field generator is used to excite the water molecules to the vapor state, enabling separation of the water from the liquid desiccant. In such embodiments, the excitation can be adjusted to enable optimal separation of the water from the liquid desiccant.

[0106] In certain embodiments, the energy application system unit does not completely vaporize the water molecules in the liquid desiccant, but combines electrodialysis, mechanical vapor compression, membrane distillation, vacuum membrane distillation, single-effect distillation, distillation, and / or another form of liquid desiccant regeneration to extract additional water from the liquid desiccant. In certain embodiments, the energy application system may assist with other forms of molecular excitation that utilize vacuum or high pressure and / or pressure changes induced by thermal changes.

[0107] The energy application system may include a container 3 (FIG. 1) for receiving liquid desiccant from the atmospheric water collection component. In some embodiments, the energy application system excites water molecules in the liquid desiccant disposed in the container until the water molecules vaporize. The water vapor is withdrawn from the system and condensed (e.g., by a condenser and / or heat exchanger) as discussed herein. The condensed liquid desiccant exits the container and is fed to an absorbent system for use in collecting additional water.

[0108] In certain embodiments, particles and / or chemicals may be added to the liquid desiccant to enhance its excitation characteristics, such as increasing the liquid desiccant temperature in the system to a desired level. Non-limiting examples of particles that can be added include conductive additives such as carbon-containing nanomaterials, boron nitride nanomaterials, and / or other nanoparticles. Such particles may respond to ultrasonically generated heat to help increase the energy of the fluid, thereby enhancing heat and mass transfer within the fluid.

[0109] In certain embodiments, the energy application system operates at least substantially continuously in a steady-state configuration. In other embodiments, the energy application system operates in a batch configuration, such that liquid desiccant enters the system (e.g., a container) and is excited, e.g., until a predetermined amount of water is extracted from the container. The resulting concentrated liquid desiccant is then fed to an absorbent material to absorb additional water from the atmosphere.

[0110] In certain embodiments, multiple pumping systems may be provided for parallel operation. In such a configuration, water from all pumping units is collected and fed to a common collection tank. The concentrated liquid desiccant is collected in a common manifold and fed to an absorber.

[0111] In certain embodiments, multiple pumping systems operate in series. In a series configuration, water from a first pumping system can be used to heat (e.g., via a heat exchanger) the liquid desiccant provided as input to a second pumping system in the series. Alternatively, water can be provided directly to a common water collection tank or condenser. Liquid desiccant from a first pumping system in a series of multiple pumping systems can pass through a heat exchanger heated by water vapor from the first pumping system or can be directed directly to a second pumping system. Each of the multiple pumping systems can use the same or different pumping technology. Once the liquid desiccant reaches a predetermined concentration level, it can be provided to an absorber from the last pumping system in the series to absorb additional water from the atmosphere.

[0112] An exemplary system may 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 may be supplied to the absorption column at a flow rate of at least about 2800 cubic feet per minute and passed through a packed column directing a concentrated lithium chloride solution having a concentration of about 38-45% by weight (e.g., about 40% by weight). Water may be absorbed by the lithium chloride solution, and the concentration of the lithium chloride solution may be reduced to a dilute concentration level of about 38-40% by weight (e.g., about 38.6% by weight) before the desiccant solution is discharged from the absorption column. During the absorption process, the absorption column may be maintained at a temperature of at least about 80-90°F.

[0113] The desiccant solution provided in the embodiments discussed herein may be embodied as a compound having hygroscopic properties. In certain embodiments, the desiccant solution may be a fluid, gel, and / or the like within the typical operating temperature ranges discussed herein. By way of non-limiting example, the desiccant solution may be embodied as lithium chloride (LiCl), lithium bromide (LiBr), calcium chloride (CaCl), triethylene glycol, and / or the like. Other unlisted compounds having hygroscopic properties may be provided for use as the desiccant solution in certain embodiments. Liquid desiccant may also be comprised of surfactants and / or nanofluids.

[0114] water extraction equipment

[0115] The water extraction unit includes an energy-addition module and associated pumps, valves, compressors, and piping. In certain embodiments, the energy-addition module includes one or more non-thermal water extraction devices (e.g., connected in series or parallel) and / or is combined with at least one heat-only system. In this embodiment, the excitation module is connected to the absorption module via various flow streams, allowing desiccant to flow between the absorption module and the water extraction module. The fluid separation device includes a device in which the desiccant medium is heated to a saturated state, enabling separation of the captured water from the hygroscopic desiccant. The resulting high concentration of diluted liquid desiccant heats the desiccant fluid by utilizing sensible heat transfer, promoting water vapor transfer. In certain embodiments, the concentrated liquid desiccant may be recycled, in whole or in part, to the absorption module within the AWG system. In this embodiment, the AWG water extraction module includes at least one or more non-thermal heating systems, including ultrasonic, microwave, and / or a combination thereof.

[0116] ultrasonic water extraction device

[0117] In certain embodiments, the water extraction apparatus described herein comprises an excitation component, as shown in FIG. 1 , positioned between an atmospheric water collection component and a water separation component in an AWG system or the like discussed herein, the excitation component comprising a housing having an inlet 1 configured to receive liquid desiccant from the atmospheric water collection component and an outlet 2 for flowing the liquid desiccant to the water separation system, the liquid desiccant medium 8 containing the liquid desiccant; and one or more ultrasonic nozzles 7 disposed within the housing and configured to excite water molecules in the liquid desiccant medium 8 by applying ultrasonic waves to the liquid desiccant within the housing.

[0118] In embodiments described herein, the separation system is configured to separate water from the liquid desiccant by one or more of electrodialysis, mechanical vapor compression, or distillation, such as, but not limited to, membrane distillation, vacuum membrane distillation, single-effect distillation, or any combination thereof.

[0119] In the embodiments described herein, the liquid desiccant is selected from the group consisting of CaCl2, NaCl, LiCl, MgCl2, KCOOH, CH3COOK, colloids, nanomaterials, and ionic liquids, or combinations thereof.

[0120] In certain embodiments, the fluid holding chamber is cylindrical, cubic, conical, or a combination thereof. In embodiments, the apparatus including one or more ultrasonic nozzles includes at least two ultrasonic nozzles 7 and further includes at least two ultrasonic generators 6 and at least two ultrasonic transducers 5, each operating a corresponding one of the at least two ultrasonic nozzles. In embodiments described herein, the nozzles extend through at least one wall of the fluid holding chamber. In some embodiments, the nozzles extend through two or more walls of the fluid holding chamber. In embodiments described herein, the nozzles are positioned to maximize the range of ultrasound. In certain embodiments, the nozzles are spaced 2 cm to 10 cm apart. In embodiments, one or more nozzles extend through the same wall of the holding chamber. In other embodiments, one or more nozzles extend through one or more walls of the fluid holding chamber. In embodiments described herein, the apparatus includes one ultrasonic nozzle, two ultrasonic nozzles, three ultrasonic nozzles, or up to six ultrasonic nozzles. In certain embodiments, the apparatus includes two ultrasonic nozzles, as shown in FIG. 1.

[0121] In the embodiments described herein, the fluid-holding chamber further comprises an outer wall 3. The outer wall of the chamber comprises plastic, metal, or any material that facilitates the containment and heating of the liquid desiccant. The inner wall of the fluid-holding chamber can be coated or modified with insulation 4 to limit the loss of heat generated by the ultrasound. The device can further comprise an acoustic enclosure to reduce user discomfort from loud noises generated by the ultrasound.

[0122] Microwave Water Extraction Equipment

[0123] In certain embodiments, the water extraction apparatus described herein includes an excitation component, as shown in FIG. 2 , disposed between the atmospheric water collection component and the water separation component, the excitation component comprising a housing having an inlet 1 configured to receive liquid desiccant from the atmospheric water collection component and an outlet 2 for flowing the liquid desiccant to the water separation system, the liquid desiccant medium 8 comprising the liquid desiccant, and one or more microwave generators 6 and waveguides 5 disposed within the housing and configured to excite water molecules in the liquid desiccant by applying microwaves to the liquid desiccant within the housing.

[0124] In embodiments described herein, the separation system is configured to separate water from the liquid desiccant by one or more of electrodialysis, mechanical vapor compression, or distillation, such as, but not limited to, membrane distillation, vacuum membrane distillation, single-effect distillation, or any combination thereof.

[0125] In the embodiments described herein, the liquid desiccant is selected from the group consisting of CaCl2, NaCl, LiCl, MgCl2, KCOOH, CH3COOK, colloids, nanomaterials, and ionic liquids, or combinations thereof.

[0126] In certain embodiments, the fluid holding chamber is cylindrical, cubic, conical, or a combination thereof. In embodiments, the apparatus includes one or more microwave generators 6, each operating a corresponding waveguide, one or more microwave waveguides 5, and one or more microwave absorbing materials for converting electromagnetic waves into thermal energy. In embodiments described herein, the waveguides are applied to at least one wall of the fluid holding chamber. In some embodiments, the waveguides are applied to two or more walls of the fluid holding chamber. In embodiments described herein, the waveguides are positioned to maximize microwave range. In certain embodiments, the waveguides are spaced 2 cm to 10 cm apart. In embodiments, two or more waveguides are applied to the same wall of the holding chamber. In other embodiments, two or more waveguides are applied to two or more walls of the fluid holding chamber. In embodiments described herein, the apparatus includes one microwave waveguide, two microwave waveguides, three microwave waveguides, or up to six microwave waveguides. In a particular embodiment, the device comprises one microwave waveguide, as shown in FIG.

[0127] In the embodiments described herein, the fluid-holding chamber further comprises an outer wall 3. The outer wall of the chamber comprises plastic, metal, or any material that facilitates the containment and heating of the liquid desiccant. The inner wall of the fluid-holding chamber can be coated or modified with insulation 4 to limit the loss of microwave-generated heat.

[0128] Method for heating a liquid desiccant medium

[0129] Ultrasonic Heating System

[0130] To achieve separation of water from liquid desiccant, ultrasonically assisted extraction of water is used, whereby ultrasonic waves propagate through the desiccant medium through a series of compression and rarefaction cycles parallel to the direction of ultrasonic wave propagation. This generates both hydrostatic and acoustic pressure. In this embodiment, ultrasonic waves are generated in the system using at least one ultrasonic transducer operatively connected to at least one ultrasonic generator. In certain embodiments, the most influential parameters of ultrasonic waves—power and frequency—can be varied to optimize sensible heating resulting from excitation of liquid desiccant molecules based on the liquid desiccant composition. In this embodiment, adjusting the ultrasonic waves may include utilizing high-power or low-frequency ultrasound (20-100 kHz), medium-power or intermediate-frequency sound (100 kHz-1 MHz), and / or low-power and high-frequency sound (1-10 MHz). In this embodiment, the ultrasonic input can be varied based on "pulse-on" or "pulse-off" modes. The pulse mode of the ultrasonic generator involves rapid on / off adjustment of the generator's ultrasonic output. Pulsed mode increases the excitation of water molecules in the liquid desiccant by promoting the formation of more cavitation bubbles and their implosion. In certain embodiments, an ultrasonic module with multiple ultrasonic nozzles (e.g., connected in series or parallel) improves system performance by orienting and / or tilting the ultrasonic nozzles in different directions relative to one another or spatially locating them at different distances from the walls of the ultrasonic chamber. In certain embodiments, the ultrasonic module may be configured with an acoustic enclosure (insulator) to reduce excessive noise levels and avoid user discomfort.

[0131] In certain embodiments, ultrasonic wave propagation induces several fluid dynamic effects, including, but not limited to, cavitation, microstreaming, mechanical vibration, acoustic streaming, and / or combinations thereof. Cavitation bubbles are generated as ultrasonic waves pass through the liquid desiccant medium present in the ultrasonic module. Like any sound wave, ultrasonic waves propagate in a series of compression and rarefaction cycles that affect the molecules of the liquid desiccant. Cavitation bubbles within the fluid form when the negative pressure of the rarefaction cycles exceeds the intermolecular attractive forces of the desiccant molecules. The cavitation bubbles continue to compress and grow through successive cycles until they completely collapse, creating an acoustic effect. In this embodiment, after at least one cavitation bubble reaches a critical size, it violently implodes in the compression region, inducing physical, chemical, and thermal effects. As a result, it is understood that this ultrasound-induced phenomenon generates extraordinary local temperatures and pressures, up to 5000 K and 1000 atmospheres, respectively, thereby heating the desiccant fluid through sensible heat transfer and promoting water vapor transport. In certain embodiments, heat transfer within a fluid is further enhanced by turbulence generated at microscopic and / or macroscopic scales by cavitation bubble collapse, microjet formation, and shock waves. Another important hydrodynamic effect of ultrasound propagation is acoustic streaming (Eckart streaming and Rayleigh streaming), which has transducer-position-dependent velocities that vary from 0.01 to 1 m / s, thereby increasing turbulence through the medium for heat and mass transfer applications. In certain embodiments, the height of the fluid medium relative to the transducer position within the chamber can be varied depending on the optimal sonication conditions.

[0132] Certain embodiments are directed to a method of water extraction that includes separating water from a liquid desiccant using an ultrasonic water extraction device described herein, where the liquid desiccant flows from an atmospheric water collection component to an excited component. The liquid desiccant in the excited component is ultrasonically excited and heated to produce high humidity water vapor. The heated liquid desiccant flows from the excited component to a water separation system, where water is separated from the liquid desiccant. For example, the heated liquid desiccant may flow into a membrane separation system, as discussed herein.

[0133] In the embodiments described herein, the water extraction method can be performed in a batch process or a continuous process. In certain embodiments, the liquid desiccant is present in the holding chamber for at least 30 minutes. In embodiments, the ultrasound described herein is adjusted to achieve sensible heating based on the composition of the liquid desiccant.

[0134] In embodiments described herein, adjusting the ultrasound waves includes changing the frequency of the ultrasound waves. In embodiments described herein, the frequency of the ultrasound waves can be changed by a controller that can operate manually or automatically. In some embodiments, the controller includes a UI that allows an operator to manually, automatically, or remotely change the frequency of the ultrasound waves. In some embodiments, the ultrasound waves are high-power, low-frequency waves, including ultrasound waves with frequencies between 20 kHz and 100 kHz. In some embodiments, the ultrasound waves are medium-power, intermediate-frequency waves, including ultrasound waves with frequencies between 100 kHz and 1 MHz. In other embodiments, the ultrasound waves are low-power, high-frequency waves, including ultrasound waves with frequencies between 1 MHz and 10 MHz.

[0135] In the embodiments described herein, the ultrasound generates a local temperature of at least 500K, at least 1000K, at least 1500K, at least 3000K, or up to at least 5000K.

[0136] Microwave Heating System

[0137] In certain embodiments, microwave-assisted water extraction from liquid desiccant can be performed, causing water molecules in the desiccant medium to undergo a phase transition from liquid to vapor. Microwave-induced heating of the desiccant medium offers potential advantages, including non-contact heating, rapid heating, targeted heating, and independence from thermal convection. In this embodiment, the microwave unit can operate based on a multimode or single-mode reactor configuration. In certain embodiments, adjusting the microwave intensity can enable optimal sensible heating as molecules absorb and convert electromagnetic energy into heat. In certain embodiments, the electromagnetic radiation can operate at a frequency of 2.45 GHz. In certain embodiments, the microwave excitation system does not completely vaporize the water molecules in the liquid desiccant by itself and may require the integration of a separate separation module, including, but not limited to, electrodialysis, mechanical vapor compression, membrane distillation, vacuum membrane distillation, single-effect distillation, distillation, and / or another form of liquid desiccant regeneration. In certain embodiments, the excitation / regeneration unit can assist with other forms of molecular excitation that utilize vacuum or high pressure and / or pressure changes induced by thermal changes.

[0138] In embodiments described herein, microwaves excite water molecules to the point of vaporization. The extracted water flows from the system into a water separation system, where the water molecules in the liquid desiccant are separated. In some embodiments, the separation system includes a condensation chamber as part of a closed-loop flow path to condense water from the heated liquid desiccant-rich air and collect it as a usable liquid in a water tank. In certain embodiments, the condensation chamber further includes a heat exchanger configured to lower the temperature of the liquid desiccant-rich air exiting the excitation component to increase the condensation rate. In embodiments described herein, the separation system further includes a membrane distillation system along the desiccant closed-loop flow path. In the membrane distillation system, the desiccant flow path can pass through a first side of a membrane such that the desiccant solution contacts the membrane as it travels along the desiccant flow path. The membrane can separate a desiccant solution flow path from a water flow path for water collected by 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, increasing the vapor pressure of the desiccant can enhance mass transfer across the membrane. This can be achieved by heating the liquid prior to contact with the membrane, reducing the pressure on the second side of the membrane by using a vacuum, or a combination of both. The water in the desiccant begins to permeate the membrane in liquid form and exits the membrane in vapor form. The water then condenses using a heat exchanger (e.g., a condenser) and / or by contact with a cooler fluid (e.g., condensed water). The concentrated liquid desiccant exiting the separation system can be recycled to the absorbent system, allowing for water vapor collection.

[0139] Microwave induction heating weakens hydrogen-bonding structures in bulk liquid desiccant, increasing molecular mobility. The material's electrical conductivity plays a major role in microwave heating. In certain embodiments, the addition of microwave-absorbing particles and / or chemicals with different electrical conductivities to the liquid desiccant can adjust the excitation and / or frequency of the fluid to a desired state. Examples of particles include ferromagnetic materials and / or carbon nanomaterials and / or nanoparticles. The penetration depth, determined by the material's dielectric constant, can be used to visualize a material's ability to be heated by microwaves. In certain embodiments, microwave induction heating can form nanobubbles, but the thermal and non-thermal effects of microwave radiation can create superheated hot spots, resulting in the formation of gas and vapor bubbles at temperatures below the boiling point. Based on the material's inherent absorption, microwave irradiation can result in intense localized heating and hot spot formation, with microwave exposure potentially reaching temperatures as high as 2000°C within minutes. In certain embodiments, the duration of microwave heating can be varied. Microwave treatment of the material's inherent absorption can result in intense heating, as well as intense light and gas evolution, enabling localized heating effects in homogeneous heat and mass transfer applications within the separation unit. In certain embodiments, the microwave chamber can be coated with a susceptor material and / or incorporates an agitator to agitate the fluid medium to increase heating efficiency and reduce heat dissipation issues. In certain embodiments, such materials can include conductive polymers, metal layers, and / or other similar heating additives. In certain embodiments, the microwave heating module can include insulation along the interior walls of the chamber to prevent microwave radiation loss, control heat dissipation, or a combination thereof.

[0140] In embodiments, described herein is a method of water extraction that includes separating water from a liquid desiccant using a microwave water extraction device, where the liquid desiccant flows from an atmospheric water collection component to an excited component. The liquid desiccant in the excited component is then excited and heated by microwaves to produce high humidity water vapor. The heated liquid desiccant flows from the excited component to a water separation system, where the water is separated from the liquid desiccant.

[0141] In embodiments described herein, the water extraction method can be performed in a batch or continuous process. In certain embodiments, the liquid desiccant is present in the holding chamber for at least 30 minutes. In certain embodiments, the microwaves described herein are adjusted to achieve sensible heating based on the composition of the liquid desiccant.

[0142] In embodiments described herein, adjusting the microwaves includes changing the microwave frequency. In some embodiments, the microwaves generated to heat the liquid desiccant include a microwave frequency between 0.5 GHz and 5 GHz. In embodiments described herein, the microwaves generated to heat the liquid desiccant are at a frequency between 1 GHz and 3 GHz. In certain embodiments, the microwaves are generated at a frequency of about 2.4 GHz.

[0143] In the embodiments described herein, the microwaves generate local temperatures of at least 100°C, at least 500°C, at least 1000°C, at least 1500°C, or up to at least 2000°C.

[0144] Continuous or batch heating methods

[0145] In certain embodiments, the pumping units may be configured to operate in a serial configuration as described above. In certain embodiments, the pumping units may be configured to operate in a batch configuration, where liquid desiccant enters the system and is pumped until a predetermined amount of water exits the unit. A high concentration of liquid desiccant is then sent to the absorber, and more fluid enters the pumping units. In certain embodiments, the pumping system operates the units in parallel. In a parallel configuration, water is collected from all units and sent to a common collection tank. The liquid desiccant is collected in a common manifold and sent back to the absorber. In certain embodiments, the pumping units operate in series. In a series configuration, water from the first unit can be used to heat the feed to the second unit through a heat exchanger. Alternatively, water can be delivered to a water collection tank or condenser. The liquid desiccant from the first pumping unit can pass through a heat exchanger heated by water vapor, or it can simply enter the second pumping unit. The pumping units may include different types of pumping technologies as described above. Once the liquid desiccant reaches a predetermined concentration, it is sent from the last pumping unit in the series to the absorber.

[0146] Use in automated agriculture

[0147] The AWG system may be adapted to generate water and / or power for agricultural modules, which may include greenhouses, plant growth habitats, and / or other structures that may be used to promote plant growth under controlled atmospheric conditions. FIGS. 8 and 9 illustrate various embodiments of an agricultural module 1000 associated with an AWG system 100 housed in a shipping container, according to one embodiment. As shown in the drawings, 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., forming a star shape, as shown in FIG. 9 ). In embodiments including distinct lobes, the volume of each lobe may be isolated from the rest of the habitat so that each lobe is provided with a unique growth environment (e.g., different temperatures, carbon dioxide levels, humidity levels, and / or similar environments) to promote the growth of different agricultural products.

[0148] FIG. 10 is a schematic detailed view of a portion of an agricultural module 1000 growing environment, according to one embodiment. The agricultural module 1000 growing environment may include one or more stackable structures 1001, each having one or more bases 1002 configured to support growing media (e.g., soil, hydroponic supports, and / or the like), 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 an upper structure are supported by a lower structure, and / or similar configurations. The one or more sidewalls and ceiling may be configured to contain controlled atmospheric conditions in the structure (e.g., ambient air with controlled oxygen and carbon dioxide levels, temperature, humidity, and / or similar conditions). The one or more sidewalls and ceiling may include a covering, such as a flexible covering, a rigid covering, and / or the like. In certain embodiments, the covering can include integrated grow lamps (e.g., light-emitting diode grow lamps) and / or integrated electrical circuitry, and / or can be configured to allow natural sunlight to pass through the covering to reach the interior environment. In certain embodiments, the integrated grow lamps can be spaced at regular intervals throughout the flexible covering and can be electrically connected to each other and / or to one or more power sources via electrical circuitry. For example, in the exemplary embodiment of FIG. 10, the covering includes a solar canopy 100 as discussed herein, with integrated LEDs 12 spaced throughout the surface of the canopy 100.

[0149] In embodiments including flexible covering, the agricultural module may include one or more rigid supports that together form a rigid support frame for the flexible covering.

[0150] In certain embodiments, the agricultural module 1000 may be embodied as a portable system configured to be quickly deployed at a desired agricultural site. The agricultural module 1000 may additionally include one or more sensors 1003 that can be provided within the growing medium of the growing environment. These sensors may be embodied as part of a flexible electrical circuit bundle including conductors, sensors, and / or the like, and can be rapidly deployed within the growing environment by unrolling the electrical circuit bundle on a supporting surface of the growing environment prior to providing the growing medium therein. In certain embodiments, the various sensors may be electrically connected to each other, the control computer system 1004, and / or a power source via one or more conductors (e.g., flexible conductors). The various sensors may include moisture sensors, temperature sensors, carbon dioxide content sensors, oxygen sensors, humidity sensors, and / or similar sensors. It is understood that some of the sensors may be configured for wireless data transmission to the control computer system via one or more wireless communication technologies, such as Wi-Fi, Bluetooth, Internet of Things (IoT) technologies, and / or similar technologies.

[0151] In certain embodiments, the control computer system 1004 may utilize sensor output (e.g., indicative of environmental measurements within the growth environment) to adjust environmental conditions within the growth environment. For example, the control computer system 1004 may include data indicative of one or more target environmental conditions, such as a target temperature, a target carbon dioxide content, and / or similar conditions. Based on monitoring data output from various sensors 1003 within the growth environment, the control computer system 1004 may be configured to compare the output monitoring data with the target environmental conditions and to adjust the flow of water, carbon dioxide, and / or the like from the AWG 100 to the growth environment. For example, the control computer system 1004 may 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, increase and / or decrease the amount of carbon dioxide flowing into the growth environment from a carbon dioxide capture system of the AWG system 100, and / or similar actions.

[0152] Additionally, the growing environment may include one or more automated planting and harvesting mechanisms configured to automatically sow new plants and / or automatically harvest fruits and / or vegetables grown within the growing environment (including using agricultural robots and drones).

[0153] For example, seeding / control may be provided by a planting probe 1010 operable to travel along a grid / track system 1011 elevated above a support surface of the growing environment. In certain embodiments, the grid / track system 1011 may be raised and / or lowered by a support mechanism (e.g., a pneumatic and / or hydraulic support mechanism). The planting probe 1010 may be operable in response to receiving signals from a control computer system 1004 including data indicative of an internal mapping of the planting media and / or base 1002 within the growing environment. The control computer system 1004 may additionally include data indicative of desired crops for planting within the growing environment, crop spacing, and / or the like, and may provide movement signals to the planting probe 1010 to insert seeds into the planting media according to a desired planting plan.

[0154] 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 inject the seeds to an appropriate depth within the planting medium (as determined by the control computer system 1004). The planting probe 1010 may additionally include a movement mechanism (e.g., one or more motors) configured to move the planting probe 1010 along a track / grid for seeding into the planting medium. Furthermore, the planting probe 1010 may be configured to periodically return to a refilling position within the growing environment to add seeds to its hopper 1012. The refilling position may be located near a filling chute within the growing environment that contains additional seeds that can be selectively supplied 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 travel of the planting probe such that the planting probe 1010 may travel down the filling chute and be refilled by gravity, which transfers seeds from the filling chute to the planting probe 1010. Furthermore, in certain embodiments, the filling chute may include an actuatable feed door (e.g., a servo-actuated feed door) configured to open and permit the flow of seeds from the feeding chute in response to a signal received from the control computer system 1004. Thus, when the planting probe 1010 is positioned directly below the feeding chute, the control computer system 1004 may be configured to open the feed door to allow seeds to flow from the feeding chute to the planting probe 1010. Once an appropriate amount of seeds has been delivered to the planting probe 1010, the control computer system 1004 may send a second signal to close the feed door.

[0155] The planting probe 1010 may additionally include a harvesting mechanism that may be removably secured to the movable planting probe 1010. The harvesting mechanism may include a mechanically movable cutting / picking arm 1014 and a holding basket / tray 1015. Upon receiving a signal from the control computer system 1004 to start the harvesting process, the planting probe 1010 may proceed to pick and / or cut produce / plants from various plants in the growing environment and store the cut produce / plants in the holding basket / tray 1015. Once the holding basket / tray 1015 is full, the planting probe 1010 may return to a docking position where the holding basket / tray 1015 may store the harvested produce in a holding crate that is removable from the growing environment. Additionally, in certain embodiments, the holding crate may include one or more level sensors configured to monitor the amount of harvested produce therein to prevent overflow of the holding crate. The control computer system 1004 may be configured, upon detecting that the fill level of the holding crate exceeds a threshold level, to send a signal to the planting probe 1010 to suspend harvesting operations until the holding crate is emptied.

[0156] While the above description refers to a track-based planting and harvesting probe configuration, various embodiments may be configured to perform seeding and / or harvesting using 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 the growing environment according to a defined planting plan. In certain embodiments, the planting plan may define a map of seeding locations such that the autonomous UAV can autonomously navigate between the seeding locations to insert seeds into the growing medium.

[0157] The autonomous UAV may additionally include a harvest probe arrangement similar to that described above. A UAV including the harvest probe arrangement may be configured for autonomous navigation within a growing environment to harvest agricultural products grown therein.

[0158] The irrigation system of the growing environment may be embodied as one or more pipes connectable to a watering mechanism, such as a spray sprinkler, drip irrigation pipes, and / or the like. The pipes may include plastic flexible tubing and may be embodied as a self-healing material configured to self-seal cracks, cuts, and / or perforations through the pipe wall. The pipes may be connected to a water outlet of a condensation system of the AWG system, a water holding tank of the AWG system, and / or the like.

[0159] Additionally, the irrigation system may include a fertilizer supply mechanism configured to automatically mix a metered amount of fertilizer (e.g., liquid fertilizer) into the water supplied to the irrigation system. The fertilizer supply mechanism may be in electrical communication with a control computer system 1004 that may be configured to provide signals to the fertilizer supply mechanism to modify the amount of liquid fertilizer introduced into the water stream.

[0160] Exemplary Operation of an Atmosphere Generating System

[0161] The following discussion provides an exemplary operation of one embodiment utilizing a membrane-based water extraction process as part of an atmospheric water generation system and method. It should be noted that the use of the term "about" in reference to a numerical value (e.g., a temperature value, a pressure value, and / or a similar value) includes the value itself as well as deviations 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 include the temperature range of 10°F to 50°F as well as slight deviations at the upper and lower ends of the temperature range that provide the same functionality as the described temperature range. Furthermore, the concepts discussed herein are applicable to any of a variety of desiccant fluids, gels, aerogels, and / or the like, as the described process is independent of the desiccant utilized. 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.

[0162] In an exemplary operation, the desiccant fluid exiting the absorbent has a concentration of about 10% to about 50% by weight and a temperature of about 75°F to about 130°F. The desiccant fluid flows along a flow path (using one or more pumps, if desired) through one or more heating mechanisms, such as a condenser (which utilizes relatively low temperature dilute desiccant on a first side of the condenser to condense water vapor flowing in the water flow path, the water flow path passing through an opposite side of the heat exchanger embodied as a condenser, as discussed in more detail herein). The water vapor condenses in the condenser as it traverses the condenser, warming the dilute desiccant fluid. In another embodiment, the condenser is a dual-pipe heat exchanger, where the dilute desiccant fluid enters the dual-pipe heat exchanger through an inner pipe. Water vapor enters the heat exchanger through an outer pipe. As the water vapor traverses the condenser, it condenses on the outer surface of the inner pipe.

[0163] In certain embodiments, the flow pattern through the condenser is a countercurrent orientation, with the dilute desiccant solution flowing in a first direction and the water flow path passing in an opposite second direction through the heat exchanger (as previously mentioned, within the condenser the dilute desiccant fluid is physically separated from the water flow path.) In other embodiments, the flow pattern through the condenser is a cocurrent orientation, depending on the shape and orientation of the heat exchanger embodying the condenser.

[0164] The temperature of the diluted desiccant fluid is between about 132°F and about 170°F upon exiting the condenser. The diluted desiccant fluid is then sent to a second heat exchanger 629 where it is further heated by sensible heat transfer from the concentrated desiccant fluid exiting the membrane-based water extraction device. In certain embodiments, the second heat exchanger is a shell-and-tube heat exchanger with the diluted desiccant fluid entering its tube side. The concentrated desiccant fluid enters the shell side of the second heat exchanger. In other embodiments, the diluted desiccant fluid enters the shell side of the second heat exchanger and the concentrated desiccant fluid enters the tube side of the second heat exchanger. In another embodiment, the second heat exchanger is a plate-and-frame heat exchanger. The diluted desiccant fluid enters one set of plates while the concentrated desiccant fluid enters the other set of plates. In another embodiment, the second heat exchanger is a dual-pipe heat exchanger where the diluted desiccant fluid enters the dual-pipe heat exchanger through an inner pipe and the concentrated desiccant fluid enters the heat exchanger through an outer pipe.

[0165] The diluted desiccant fluid exits the second heat exchanger at a temperature of about 140°F to about 210°F. The diluted desiccant fluid then traverses a heater. The heater may be an in-line electric heater including a bundle of elements for heating the fluid. The heater may be oriented differently to reduce the likelihood of the fluid surging over the elements. In certain embodiments, the heater may reside within the housing of the membrane-based water extraction device. In certain embodiments, the heater is a shell-and-tube or plate-and-frame heat exchanger. In certain embodiments, the heater is a solar heater that utilizes photovoltaic panels to capture sunlight and generate energy from electricity. In certain embodiments, the heater is a Fresnel lens that utilizes solar energy to generate thermal energy in the form of heat. In certain embodiments, the heater is a geothermal heater as discussed herein. In certain embodiments, the heater is a combustion heater that combines a hydrocarbon fuel source with oxygen to generate heat by combustion. In certain embodiments, the oxygen is from ambient air. The temperature of the diluted desiccant fluid is between about 150°F and about 270°F upon exiting the heater.

[0166] The diluted desiccant fluid then flows into a membrane-based water extraction device. In certain embodiments, the outlet of the membrane-based water extraction device is provided with a reducing orifice to increase the pressure on the desiccant side of the membrane within the housing of the membrane-based water extraction device.

[0167] The diluted desiccant stream enters the housing of the membrane-based water extraction apparatus on a first side of the membrane. The diluted desiccant stream is at high temperature (e.g., about 150°F to about 270°F) and high pressure. As the water stream flows along the water flow path, it passes through the opposite second side of the membrane. The water flow path may pass through a pressure reducing orifice at the inlet of the membrane-based water extraction apparatus to reduce the pressure on the water flow side of the membrane, thereby facilitating the passage of water through the membrane to the water flow side of the membrane. Additionally, the water stream passes through a cooling device before entering the housing of the membrane-based water extraction apparatus.

[0168] As the diluted desiccant and water flow through the membrane-based water extraction device housing on both sides of the membrane, water absorbed by the fluid desiccant migrates through the membrane (water is considered to enter the membrane as a liquid on the desiccant side of the membrane and exit the membrane as a vapor on the water side of the membrane). This re-concentrates the desiccant fluid, while the water vapor is captured in the permeate flow path for later condensation and storage as liquid water. The re-concentrated desiccant fluid then passes through one or more cooling devices to cool it before returning to the absorbent (e.g., passing through one or more heat exchangers for sensible heat transfer to the diluted desiccant solution, as described above). The entire desiccant flow path is a closed desiccant circulation loop configured for insignificant mass transfer of desiccant salt through the membrane of the membrane-based water extraction device and / or to the atmosphere in contact with the desiccant flow within the absorbent. As the desiccant flows along the flow path within the closed desiccant circulation loop, water absorption into and / or extraction from the desiccant occurs as the desiccant flows through the AWG system.

[0169] The water flow path exits the membrane-based water extraction device and passes through one or more condensers. In certain embodiments, a sweep gas (e.g., a gas with properties that reduce the likelihood of water evaporation into gas and / or humid air flowing along a closed air circulation loop coextensive with the water flow path) flows with the liquid water to drive water vapor from the membrane-based water extraction device to the condenser. In certain embodiments, the water flow passes through a compressor to increase its pressure (which increases the vapor pressure of the water vapor and promotes condensation) before passing through one or more condensers. After passing through the condenser, the water flow path enters a storage tank. A certain amount of water from the storage tank is recirculated through the water flow path (to the membrane-based water extraction device) to facilitate the extraction of additional water from the diluted desiccant fluid flowing through the membrane-based water extraction device.

[0170] conclusion

[0171] Numerous modifications and other embodiments 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 therefore to be understood that the disclosure is not limited to the particular embodiments, 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.

[0172] In certain embodiments, various portions of the AWG system may be contained in 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 housed in a first container, one or more water integration systems (e.g., a single-stage batch water integration system and / or a continuous water integration system) may be housed in a second shipping container, and various ports / inlets may extend through the walls of the shipping container to allow connection to one or more geothermal cooling systems, solar heating systems, high-pressure gas inputs, and / or the like. In certain embodiments, one or more condensation systems, water storage tanks, and / or the like may be embodied in a third storage container. However, it should be understood that certain embodiments may be configured such that the entire AWG system is housed in a single storage container, with one or more ports / inlets (e.g., air inlet / outlet, high-pressure gas inlet, solar inlet / outlet, geothermal cooling inlet / outlet, and / or the like) extending through its walls to enable interaction with aspects of the surrounding environment.

Claims

1. an ultrasonic excitation component disposed between the atmospheric water collection component and the water separation component, the ultrasonic excitation component comprising a housing having an inlet configured to receive liquid desiccant from the atmospheric water collection component and an outlet for channeling the liquid desiccant to the water separation component, the liquid desiccant comprising a hygroscopic feed solution; one or more ultrasonic nozzles disposed within the housing and configured to apply ultrasonic waves to the liquid desiccant within the housing to excite water molecules within the liquid desiccant; A water extraction device comprising:

2. 10. The apparatus of claim 1, wherein the water separation component is configured to separate water from the liquid desiccant by one or more of electrodialysis, mechanical vapor compression, or distillation, such as, but not limited to, membrane distillation, vacuum membrane distillation, single-effect distillation, or any combination thereof.

3. The hygroscopic feed solution comprises CaCl 2 , NaCl, LiCl, MgCl 2 , KCOOH, CH 3 3. The device of claim 1 or 2, wherein the catalyst is selected from the group consisting of COOK, colloids, nanomaterials, and ionic liquids, or combinations thereof.

4. The device of claim 1 or 2, wherein the housing is cylindrical, cubic, conical, or a combination thereof.

5. 3. The apparatus of claim 1, wherein the one or more ultrasonic nozzles include at least two ultrasonic nozzles, and the apparatus further comprises at least two ultrasonic generators that each operate a corresponding one of the at least two ultrasonic nozzles.

6. 3. A method of water extraction comprising separating water from the hygroscopic feed solution using the ultrasonic water extraction device of claim 1 or 2, the hygroscopic feed solution flows from the atmospheric water collection component into the excitation component; the hygroscopic feed solution in the excitation component is ultrasonically excited and heated to generate high humidity water vapor; The method wherein the heated hygroscopic feed solution flows from the excitation component into the water separation component to separate water from the desiccant.

7. 7. The method of claim 6, selected from a batch process or a continuous process.

8. 8. The method of claim 7, wherein the hygroscopic feed solution resides in the housing for at least 30 minutes.

9. 7. The method of claim 6, wherein the ultrasound is adjusted to achieve sensible heating based on the composition of the hygroscopic feed solution.

10. The method of claim 9 , wherein adjusting the ultrasound waves comprises changing the frequency of the ultrasound waves.

11. 7. The method of claim 6, wherein the ultrasound is a high power or low frequency wave, including ultrasound with a frequency between 20 kHz and 100 kHz.

12. 7. The method of claim 6, wherein the ultrasound waves are medium power or intermediate frequency waves, including ultrasound waves with frequencies between 100 kHz and 1 MHz.

13. 7. The method of claim 6, wherein the ultrasound waves are low power or high frequency waves, including ultrasound waves with frequencies between 1 MHz and 10 MHz.

14. 7. The method of claim 6, wherein the ultrasound generates a local temperature of at least 500K, at least 1000K, at least 1500K, at least 3000K, or up to at least 5000K.

15. a microwave excitation component disposed between the atmospheric water collection component and the water separation component, the microwave excitation component comprising a housing having an inlet configured to receive liquid desiccant from the atmospheric water collection component and an outlet for channeling the liquid desiccant to the water separation component, the liquid desiccant comprising a hygroscopic feed solution; one or more microwave generators and waveguides disposed within the housing and configured to apply microwaves to a liquid desiccant within the housing to excite water molecules within the liquid desiccant; A water extraction device comprising:

16. 16. The apparatus of claim 15, wherein the water separation component is configured to separate water from the liquid desiccant by one or more of electrodialysis, mechanical vapor compression, or distillation, such as, but not limited to, membrane distillation, vacuum membrane distillation, single-effect distillation, or any combination thereof.

17. The hygroscopic feed solution comprises CaCl 2 , NaCl, LiCl, MgCl 2 , KCOOH, CH 3 17. The device of claim 15 or 16, wherein the catalyst is selected from the group consisting of COOK, colloids, nanomaterials, and ionic liquids, or combinations thereof.

18. The apparatus of any one of claims 15 to 16, wherein the housing is cylindrical, cubic, conical, or a combination thereof.

19. 17. The apparatus of any one of claims 15-16, wherein the one or more microwave generators and one or more microwave waveguides comprise one or more microwave generators operating at least one waveguide each, and the apparatus further comprises one or more microwave absorbing materials that convert electromagnetic waves into thermal energy.

20. A method of water extraction comprising separating water from the hygroscopic feed solution using a microwave water extraction apparatus according to any one of claims 15 to 16, the hygroscopic feed solution flows from the atmospheric water collection component into the excitation component; the hygroscopic feed solution in the excitation component is excited and heated by microwaves to generate high humidity water vapor; The method wherein the heated hygroscopic feed solution flows from the excitation component into the water separation component to separate water from the desiccant.

21. 21. The method of claim 20, selected from a batch process or a continuous process.

22. 22. The method of claim 21, wherein the hygroscopic feed solution resides in the housing for at least 30 minutes.

23. 21. The method of claim 20, wherein the microwave is adjusted to provide sensible heating based on the composition of the hygroscopic feed solution.

24. 21. The method of claim 20, wherein the microwaves generated to heat the hygroscopic feed solution comprise a microwave frequency of 0.5 GHz to 5 GHz.

25. 25. The method of claim 24, wherein the microwaves generated to heat the hygroscopic feed solution are at a frequency of 1 GHz to 3 GHz.

26. 26. The method of claim 25, wherein the microwaves are generated at a frequency of about 2.4 GHz.

27. 21. The method of claim 20, wherein the microwaves generate a localized temperature of at least 100°C, at least 500°C, at least 1000°C, at least 1500°C, or up to at least 2000°C.

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