SYSTEMS AND METHODS FOR DIRECT AIR CARBON DIOXIDE CAPTURE

Abstract

A method for capturing and sequestering carbon dioxide (CO.sub.2) includes receiving and performing an electrochemical process on the input liquid including water and a salt to produce at least one hydroxide-rich stream, and then capturing CO.sub.2 from air using the hydroxide-rich stream and a passive air capture system, thereby producing a liquid carbonate solution containing air-captured CO.sub.2. Optional steps include disposing of the liquid carbonate solution, precipitating air-captured CO.sub.2 from the liquid carbonate solution as solid carbonate and/or a slurry of carbonate, and mixing the liquid carbonate solution with a hydrogen-rich stream produced by the electrochemical process to generate gaseous CO.sub.2. Various integrations and synergies among CO.sub.2 capture, renewable energy, water desalination, and metal and mineral extraction are provided.

Claims

1. A method for capturing and sequestering carbon dioxide (CO.sub.2), comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; and capturing CO.sub.2 from air using the hydroxide-rich stream and a passive air capture system, thereby producing a liquid carbonate solution containing air-captured CO.sub.2.

2. The method of claim 1, further comprising precipitating air-captured CO.sub.2 from the liquid carbonate solution as solid carbonate and/or a slurry of carbonate.

3. The method of claim 1, further comprising directly disposing of the liquid carbonate solution from the air capture system in a body of water or on land.

4. The method of claim 1, further comprising mixing the liquid carbonate solution with a hydrogen-rich stream produced by the electrochemical process to generate gaseous CO.sub.2.

5. The method of claim 1, further comprising: producing a hydrogen-rich stream at least in part with the electrochemical process; dissolving a metal and/or mineral into the hydrogen-rich stream to produce a metal and/or mineral solution; mixing carbonates from the liquid carbonate solution with the metal and/or mineral solution to produce a metal and/or mineral carbonate mixture; precipitating metal and/or mineral carbonates from the metal and/or mineral carbonate mixture; and recycling a salt solution from the metal and/or mineral carbonate mixture by mixing the salt solution with the input liquid upstream from the electrochemical process.

6. The method of claim 5, further comprising pretreating the input liquid with carbonates from the liquid carbonate solution.

7. The method of claim 1, further comprising: mixing CO.sub.2 from a desalination facility with the liquid carbonate solution; precipitating carbonates from the liquid carbonate solution; pretreating the input liquid with the precipitated carbonates, upstream from the electrochemical process; and processing the pretreated input liquid with a reverse osmosis system to recover water from the pretreated input liquid prior to the electrochemical process.

8. The method of claim 7, further comprising treating the input liquid and/or the recovered water with a hydrogen-rich stream produced at least in part by the electrochemical process.

9. The method of claim 1, further comprising processing the input liquid with a pretreatment stage before performing the electrochemical process, the pretreatment stage comprising one or more of a filtration system, a reverse osmosis concentration system, and an ion exchange system.

10. The method of claim 1, further comprising capturing CO.sub.2 from an industrial CO.sub.2 source with the liquid carbonate solution from the passive air capture system.sub.2 to produce a bicarbonate solution.

11. The method of claim 10, further comprising mixing the liquid carbonate solution and the bicarbonate solution with hydrochloric acid to neutralize the liquid carbonate solution and the bicarbonate solution, and to form carbon dioxide gas and a salt solution before recycling the salt solution back to the electrochemical process.

12. The method according to claim 1, further comprising producing hydrogen with the electrochemical process, neutralizing carbonates from the liquid carbonate solution with hydrochloric acid to generate CO.sub.2, and combining the CO.sub.2 with the hydrogen in presence of a catalyst, at high temperatures and pressures, to produce methanol.

13. A method for capturing and sequestering carbon dioxide (CO.sub.2), comprising: receiving an input liquid comprising salt water and at least one of a mineral and a metal; performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream; capturing CO.sub.2 from air using the hydroxide-rich stream and a passive air capture system, thereby producing a liquid carbonate solution containing air-captured CO.sub.2; precipitating the at least one of the mineral and metal from the at least one hydroxide-rich stream; and precipitating air-captured CO.sub.2 from the liquid carbonate solution.

14. The method of claim 13, wherein the at least one precipitated mineral or metal is lithium.

15. The method of claim 13, wherein the electrochemical process comprises bipolar electrodialysis.

16. The method of claim 13, further comprising absorbing lithium (Li) ions from the input liquid with an absorber, producing an hydrogen-rich stream with the electrochemical process, extracting Li from the absorber using the hydrogen-rich stream and precipitating Li as lithium carbonate.

17. A method for capturing and sequestering carbon dioxide (CO.sub.2), comprising: receiving an input liquid comprising water and a salt; performing an electrochemical process comprising electrolysis with an electrolysis unit to produce at least one hydroxide-rich stream; capturing CO.sub.2 from air using the hydroxide-rich stream and a passive air capture system, thereby producing a liquid carbonate solution containing air-captured CO.sub.2; and precipitating air-captured CO.sub.2 from the liquid carbonate solution.

18. The method of claim 17, further comprising producing the at least one hydroxide-rich stream, hydrogen gas, and chlorine gas with the electrolysis unit.

19. The method of claim 18, further comprising combining the hydrogen and chlorine to produce hydrochloric acid.

20. The method of claim 17, wherein the electrolysis unit is powered by renewable energy.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0184] FIG. 1 shows a flow chart of a carbon capture process, according to one implementation.

[0185] FIG. 2 shows a flow chart of the capture process, according to one implementation.

[0186] FIG. 3 shows potential pretreatment steps prior to electrodialysis, including nanofiltration and microfiltration, according to one implementation.

[0187] FIG. 4 shows an alternate process that pre-concentrates the feed streams, according to one implementation.

[0188] FIG. 5 is a flow chart depicting a carbon capture process, according to one implementation.

[0189] FIG. 6 depicts a further implementation of the system configured to capture carbon dioxide in gas form.

[0190] FIG. 7 depicts a flow chart depicting a carbon capture process, according to an implementation featuring the precipitation of lithium or another metal.

[0191] FIG. 8 shows a summary flow chart of one implementation of the disclosed system.

[0192] FIG. 9 shows a detailed flow chart of a carbon capture process, according to one implementation.

[0193] FIG. 10 shows detail of the particulate matter portion of the carbon capture process, according to one implementation of the disclosed system.

[0194] FIG. 11 is a flow chart depicting the capture process, according to an implementation featuring the production of green hydrogen gas and other byproducts such as green chlorine gas.

[0195] FIG. 12 is a flow chart depicting the capture process, according to an implementation featuring the production of hydrochloric acid.

[0196] FIG. 13 shows a summary flow chart of one implementation of the disclosed system.

[0197] FIG. 14 shows a flow chart of the full process, according to one implementation.

[0198] FIG. 15 depicts a further implementation of the system configured to capture carbon dioxide in gas form.

[0199] FIG. 16 shows a flow chart depicting a carbon capture process, according to one implementation of the system.

[0200] FIG. 17 shows a flow chart of the combined carbon capture and lithium extraction process, according to one implementation.

[0201] FIG. 18 depicts a flow chart depicting the carbon capture process and lithium extraction, according to an implementation featuring the production of green hydrogen gas and other byproducts such as green chlorine gas and hydrochloric acid.

[0202] FIG. 19 shows a summary flow chart of one implementation of the disclosed system using the bipolar membrane electrodialysis.

[0203] FIG. 20 shows a flow chart of one implementation of the disclosed system using the electrolysis unit to produce green hydrogen gas.

[0204] FIG. 21 depicts a further implementation of the system configured to capture carbon dioxide in gas form and use it partially or fully for lithium extraction.

[0205] FIG. 22 is a flow chart depicting a carbon capture process according to one implementation.

[0206] FIG. 23 shows a flow chart of the capture process, according to one implementation featuring the direct disposal of air-captured CO.sub.2 carbonate in addition to the precipitated carbonate.

[0207] FIG. 24 depicts a flow chart depicting the capture process, according to an implementation featuring the recycling of the hydroxide-rich stream from the precipitator and the hydrogen-rich stream from the acid neutralization over Olivine-like rocks process.

[0208] FIG. 25 depicts a flow chart depicting the capture process, according to an implementation featuring the recycling of the salt solution by neutralization of air-captured CO.sub.2 carbonates with the hydrogen-rich stream.

[0209] FIG. 26 depicts a flow chart wherein the neutralization of air-capture CO.sub.2 carbonates is done indirectly, employing a liquid solution such as calcium chloride. The liquid solution can be sourced, either fully or partially, within the system by reacting the divalent ion rejects from ion exchange with a hydrogen-rich stream or can be sourced from outside.

[0210] FIG. 27 shows a summary flow chart of one implementation of the disclosed system featuring direct disposal of sodium carbonates into the ocean.

[0211] FIG. 28 shows a flow chart of the full process, according to one implementation of the disclosed system featuring the acid neutralization over olivine rocks and the recycling of the sodium hydroxide and hydrochloric acid streams.

[0212] FIG. 29 depicts a further implementation of the system configured to capture carbon dioxide in gas form and recycling of the salt solution back to the electrochemical process step.

[0213] FIG. 30 depicts an alternate implementation of the system configured to recycling of the salt solution back to the electrochemical process step while precipitating calcium carbonate that is ultimately disposed of in the ocean or on land.

[0214] FIG. 31 is a flow chart depicting a carbon capture process, according to one implementation.

[0215] FIG. 32 is a flow chart depicting a carbon capture process, according to one implementation.

[0216] FIG. 33 depicts a flow chart wherein CO.sub.2 is captured from air in the form of carbonate which is further used to absorb CO.sub.2 from an industrial source to form bicarbonate.

[0217] FIG. 34 depicts a flow chart depicting the capture process, according to an implementation featuring the recycling of the salt solution by neutralization of carbonates formed from absorbing CO.sub.2 from the air and industrial sources with the hydrogen-rich stream.

[0218] FIG. 35 shows a summary flow chart of one implementation of the disclosed system featuring the disposal of sodium carbonates and sodium bicarbonates on land or in the ocean.

[0219] FIG. 36 depicts a further implementation of the system configured to capture carbon dioxide in gas form and recycling of the salt solution back to the electrochemical process step.

[0220] FIG. 37 depicts a flow chart depicting the carbon capture process, according to an implementation featuring the bipolar electrodialysis unit producing multiple output streams including one hydroxide-rich stream, one hydrogen-rich stream, and one hydrogen gas stream.

[0221] FIG. 38 shows a summary flow chart of one implementation of the disclosed system featuring the use of bipolar electrodialysis for products used for the mineralization of carbon dioxide.

[0222] FIG. 39 shows details of the section of a BPED unit, including the arrangement of the ion exchange membranes, and the electrodes to produce multiple streams including hydrogen gas, dilute hydrochloric acid, and concentrated sodium hydroxide according to an implementation.

[0223] FIG. 40 shows a flow chart of the combined carbon capture, desalination, and mineral extraction process, according to one implementation.

[0224] FIG. 41 shows a summary block diagram of one implementation of the disclosed system using including the synergies and interdependencies between carbon dioxide capture and sequestration, desalination, and mineral extraction.

[0225] FIG. 42 is a flow chart depicting a carbon capture process, according to one implementation.

[0226] FIG. 43 shows a flow chart of the combined carbon capture, desalination, and mineral extraction process, according to one implementation.

[0227] FIG. 44 shows a summary block diagram of one implementation of the disclosed system using including the synergies and interdependencies between carbon dioxide capture and sequestration, desalination, and mineral extraction.

[0228] FIG. 45 shows is a flow chart depicting a carbon capture process, according to one implementation.

[0229] FIG. 46 shows a flow chart of the combined carbon capture and hydrogenation process to form methanol, according to one implementation.

[0230] FIG. 47 shows a flow chart of the combined carbon capture and hydrogenation process to form methanol, according to one implementation.

[0231] FIG. 48 shows a summary block diagram of the system using carbon dioxide capture and hydrogenation of the re-released CO.sub.2 gas to form methanol, according to an implementation.

[0232] FIG. 49 shows a summary block diagram of the system using carbon dioxide capture and hydrogenation of the mineral carbonates to form methanol, according to an implementations.

[0233] FIG. 50 is a flow chart depicting a carbon capture process, according to an implementation.

DETAILED DESCRIPTION

One

[0234] The various examples and implementations disclosed or contemplated herein relate to methods, systems and devices for the capture and sequestration of carbon dioxide. Various implementations use an electrochemical process such as, for example, electrodialysis (ED) or electrolysis, to produce a hydroxide-rich flow from an input liquid such as a saline water. The hydroxide-rich stream can be used along with passive airflow over packing structures to directly capture CO.sub.2 from the air. In various implementations solid carbonates are precipitated from the resulting liquid carbonate solution and then deposited in a body of water or otherwise stored. In some implementations the liquid carbonate solution is also or instead processed to release and store the captured CO.sub.2 as a gas.

[0235] Additional liquid input can be used to continue the process, so as to operate the process in a continuous fashion. In various cases the input liquid is saline water, i.e., water with one or more dissolved salts such as, for example, sodium chloride. In some cases the input liquid is a saline water such as seawater. In various cases the input liquid is desalination brine, brackish water, brine effluent or another salt water.

[0236] As described herein, the disclosed technologies are often referred to broadly as a system 10, a capture system 10, or a carbon capture system 10, though it is understood that this is for brevity and is in no way intended to be limiting to any specific modality.

[0237] One object of various implementations of the capture system 10 is to minimize the energy use associated with CO.sub.2 extraction methods. In various implementations the system does not rely on the use of calciners or boilers, and thus does not require constant power. This in turn means that various implementations can be powered exclusively via intermittent/renewable power. Another object of the disclosed system 10 according to various implementations is to maximize the collection of CO.sub.2 by collecting CO.sub.2 both in the creation of a solvent and directly from the air. Further, an object of various implementations is to provide air capture methods that eliminate the typical steps of heating a solvent or sorbent to extract CO.sub.2 before capturing and sequestering the CO.sub.2 by creating a stream of solid carbonates and depositing them in the ocean or other body of water, or on land. These and other objects are described in detail below.

[0238] Certain implementations of the capture system 10 relate to the sequestration of CO.sub.2 using only saline water-such as seawater—and electricity. In these implementations, electricity is applied to saline water via an electrochemical process (e.g., electrodialysis or electrolysis) to create hydroxide-rich solvents which can be used to directly capture CO.sub.2 from the air. The resulting precipitated solid carbonates are then deposited into a body of water, for example, an ocean, or on land. Additional saline water is used to continue the process, which can in some cases facilitate a continuous process for CO.sub.2 capturing and sequestering, especially in locations with ready access to saline water.

[0239] In various representative implementations, the capture system 10 is performed offshore because such locations enable consistent wind flow, easy access to saline water such as seawater and easy depositing of precipitated carbonates back into the ocean. It is further appreciated that such locations minimize costs by avoiding or reducing the electrical costs of fans for air capture, can avoid or reduce transport costs for depositing carbonates in the ocean, and can reduce the pumping costs for seawater inputs.

[0240] In various alternative implementations, the capture system 10 can be employed onshore and can include various process modifications. These modifications can include, for example, 1) locating the system 10 near a source of saline water such as seawater, desalination brine, brackish water, brine effluent, or water with added salt, 2) locating the system 10 near a location with sustained winds and/or solar radiation, and/or 3) locating the capture system 10 near a site for the accumulation of solid carbonates.

[0241] FIG. 1 depicts an implementation of the carbon capture system 10 and various of its operational flows according to aspects of the disclosed technology. In this implementation, a variety of optional steps are performed. For example, in various implementations the system comprises a process having steps such as receiving an input liquid (box 100) and performing an electrochemical process such as, for example, electrolysis or electrodialysis on the input liquid to produce at least one hydroxide-rich stream (box 110). The process also includes capturing CO.sub.2 from air using the hydroxide-rich stream and a passive air capture system (box 120), and precipitating air-captured CO.sub.2 (box 130) as, for example, carbonates.

[0242] Turning to FIGS. 2-4, in various implementations of the capture system 10, an input liquid 12 such as seawater or other saline liquid is fed into the capture system 10 to produce an hydroxide-rich stream 14 containing salts such as NaOH and/or MgOH and/or CaOH and/or other hydroxides. It is understood that the capture system 10 and other implementations and examples described herein comprise one or more fluidic and/or electrical connections (shown generally at the lines) between a variety of optional components that can be arranged in a wide variety of arrangements, such that the various fluids/gases and electricity described herein are able to flow as described.

[0243] In various implementations, after the liquid input 12 enters the system 10, some portion of the input liquid 12 is exposed to an electrochemical processor 16. In various implementations the electrochemical process 16 includes electrodialysis (ED), as shown in FIGS. 2-4. In such cases the electrochemical processor includes an electrodialysis unit such as an ED stack that is configured to perform electrodialysis on the liquid 12. In various implementations, the ED stack comprises a stack of membranes 18 disposed between a positively charged plate and a negatively charged plate for bipolar electrodialysis (BPED). In such cases, the ED stack may also be referred to as an electrodialysis bipolar membrane (EDBM). In various implementations, the ED stack is configured or otherwise comprises a set of repeating ED-cells 18 in a 3-chamber pattern. This pattern includes repeating bipolar membranes and anion and cation permeable membranes.

[0244] Optionally, maintaining a sufficient flow rate through the electrodialysis unit can largely avoid the common problem in water purification systems of membrane fouling. As an example, in some cases the electrodialysis unit receives a continuous, high-velocity feed of the input liquid, e.g., water. Periodic reversing of the polarity of the system also serves to protect the membranes.

[0245] In various implementations, the electrochemical process 16 includes electrolysis, as will be described in greater detail further herein. In such cases the electrochemical processor 16 may include, for example, an electrolyzer to process the input liquid 12.

[0246] Returning to FIGS. 2-4, in use according to certain implementations, application of electricity via the electrochemical processor 16 causes the creation of the hydroxide-rich stream 14 from the input liquid 12. The hydroxides in this stream 14 are then available to capture CO.sub.2 from the air 25 using a direct air CO.sub.2 capture mechanism 22.

[0247] Certain of the saline water 12 that provided Ca+, Na+ and Mg+ ions to the ED stack 16 is now partially desalinated and of neutral pH. This seawater 800 can be returned to the ocean or used to balance pH of other waste streams before return.

[0248] Some or all of the hydroxide solution 14 is then sent to a direct air CO.sub.2 capture mechanism 22 for the capture of carbon dioxide as carbonates. This mechanism can be one of many existing approaches. Once this stream 14 has progressed through the CO.sub.2 capture system and becomes saturated with carbon, it is preferably sent to a precipitation system 20 to extract carbonates. In various implementations, the direct air capture system is preferably sited in a location with sustained wind speeds (shown at 25) to minimize flow time through the capture mechanism and energy cost.

[0249] In various implementations, the precipitation system includes a precipitation tank 20 in fluidic communication with the direct air CO.sub.2 capture mechanism 22 and, optionally, one or more of the other system 10 components as described herein. As shown in FIGS. 2-4, in various implementations the precipitation tank 20 is connected upstream of the electrochemical processor 16. In some cases the tank 20 is coupled with a pretreatment stage, such as a nanofiltration stage 15A as shown in FIG. 3 or a reverse osmosis stage 15B as shown in FIG. 4. Additionally, in various implementations the precipitation tank 20 is coupled with the electrochemical processor 16, thus providing a recycling loop for the outflow from the air capture mechanism 22 after carbonates have precipitated from the stream in the tank.

[0250] In various implementations, the capture system 10 utilizes a method for the extraction of inorganic hydroxides that is given by:

X.sub.a(O.sub.bH.sub.c).sub.m [0251] where X represents any element or combination of elements that can chemically bond with oxygen and hydrogen or its multiple; [0252] where at least one element in X is a group IA, IIA, IIIA, IVA, IB, IIB, IIIB, IVB, VB, VIIIB, VIIB, or VIIIB element of the periodic table; and [0253] where a, b, and c are stoichiometrically determined positive integers.

[0254] According to certain implementations, the capture and sequestration of CO.sub.2 described above by using an input liquid 12 such as saline water and electricity (via the electrochemical process 16, e.g., ED stack) as inputs. In these implementations, electrochemistry and water are used to create hydroxides of the form of the hydroxide-rich stream 14 specified above, and these hydroxides can then be used to directly capture CO.sub.2 from the air.

[0255] As shown and discussed, the system 10 allows for the precipitation of solid carbonates after capturing CO.sub.2 from the air. According to various implementations, the precipitation is given by:

X(CO.sub.3).sub.m [0256] where X is any element or combination of elements that can chemically bond with a carbonate group or its multiple; [0257] where at least one said element is a group IA, IIA, IIIA, IVA, IB, IIB, IIIB, IVB, VB, VIIB, VIIB, or VIIIB element of the periodic table; and [0258] where m is a stoichiometrically determined positive integer.
Following such precipitation, solid carbonates can be placed into the ocean or other body of water to facilitate increased alkalinity.

[0259] Carbonates recovered from throughout the process can be returned to the ocean as shown in these implementations at 30, or to another body of water. As anthropogenic atmospheric carbon has increased, the air/water equilibrium has shifted and an increasing fraction of CO.sub.2 is absorbed into the ocean as carbonic acid and bicarbonates. This has led to an increase in ocean acidity. Depositing carbonates from the process described herein into the ocean helps to counteract ocean acidification and support certain sea life dependent on carbonates.

[0260] The depositing of carbonates is, in certain implementations, performed in a location where these deposited carbonates will sink below the carbonate compensation depth and dissolve. Below this depth, the cool temperature and high pressure leads calcium carbonate to dissolve. Once dissolved, the Ca+ ions and carbonate ions can disperse through the ocean.

[0261] As noted above, in certain implementations, the input liquid 12 passes through one or more optional pretreatment stages 15 before entering the electrochemical processor 16. As one example, in some cases an optional filtration system 15A is utilized, such as a nanofiltration and/or a microfiltration system, as would be appreciated. In various cases the nanofiltration and/or microfiltration helps remove divalent ions from the concentrated sodium chloride solution making up at least part of the input liquid 12.

[0262] As shown in the implementation of FIG. 4, an optional reverse osmosis concentration system 15B is used to pre-concentrate a saline input liquid 12 (e.g., seawater) for use in the electrochemical processor 16 in some cases. In various implementations the efficiency of the electrochemical processor 16 (e.g., an ED bipolar membrane as shown in FIG. 4) increases with concentration of seawater, and so there are cost efficiencies in adding a standard reverse osmosis (RO) stage or an additional electrodialysis step prior to the electrochemical processor 16. Seawater is typically 30-35 g/l NaCl and other dissolved solids. In various implementations additional concentration by RO or ED can increase the concentration of brine to 70-100 g/l.

[0263] Another example of an optional pretreatment stage is shown as part of the carbon capture process and system 10 in FIG. 5. The pretreatment stage in this case includes a filtration system 15A and an ion exchange package 15C upstream from the electrochemical processor 16, the optional ion exchange system 15C can be useful for removing divalent ions from the input liquid to improve the feed composition for an electrochemical processor such as, for example, an electrodialysis bipolar membrane (EDBM).

[0264] Continuing with FIG. 5, the illustrated flow diagram provides a detailed depiction of the carbon capture process and system 10, according to one possible implementation. The detailed diagram depicts a number of pumps, vessels, and other components of the system, in addition to fluid connections between relevant components. It will be appreciated that the system may include fewer and/or additional components and aspects that are not shown in various cases.

[0265] Beginning at the left of the flow diagram, an input liquid 12 (in this example salt water) is pumped into an expansion vessel (V-001) before flowing to a pretreatment stage. The pretreatment stage in this case includes a nano-filtration unit (15A) and an ion exchange unit (15C) to remove divalent ions such as, for example, calcium and magnesium. The output from this pretreatment stage (e.g., filtrate) is stored in a vessel (V-005) before sending it to an electrochemical processor 16. In this example the electrochemical processor is implemented by an electrodialysis bipolar membrane (EDBM-001).

[0266] In the electrochemical processor 16, the treated input liquid 12 (e.g., salt stream) is split into an hydroxide-rich stream (14) and a hydrogen-rich stream (79). The hydroxide-rich stream 14 is then passed through an air contactor (22) wherein the stream absorbs carbon dioxide from an air stream (25) to form carbonates. The carbonates stream (72) are then pumped to a precipitator or a settling tank (20) where they are mixed with divalent ion streams from the nano-filtration 15A and the ion exchange package 15C to form calcium carbonate. The calcium carbonate solution is then separated into a slurry of calcium carbonate solids (30). In some cases a centrifugal dryer CG-001 is used to separate out the slurry of solid carbonates 30 and water (802), which is recycled back into the system.

[0267] As will be appreciated, in this example the main input into the capture process 10 is salt water (12) and the main outputs are carbonate solids (30) and hydrochloric acid (79). In various implementations the process/system 10 uses one or more additional inputs and may generate one or more additional outputs. In various implementations one or more ancillary inputs and/or outputs are largely recycled within the system. For example, in some cases an output from the electrochemical process 16 is processed (e.g., by reverse-osmosis) and provides low total dissolved solids (TDS) water (804), which can be used as a makeup liquid for the EDBM unit. In some cases an HCl make-up stream and/or NaOH make-up stream are also used to facilitate the EDBM unit. In various implementations a regen stream 806 including, for example, some amount of HCl, is used to regenerate the ion exchange pretreatment stage 15C. As will be appreciated, additional inputs and/or outputs may be present in various implementations of the system 10.

[0268] Turning to FIG. 6, in various implementations the capture system 10 is configured to capture CO.sub.2 in gas form. As shown in FIG. 6, the system 10 is similar to the examples shown in FIGS. 2-5 with some modifications. The first is the mixing (shown generally at 48) of sodium carbonate (Na.sub.2CO.sub.3) produced by the direct air CO.sub.2 capture mechanism 22 with a hydrogen-rich stream 79. This combination creates CO.sub.2 in gas form 52 and saltwater 50. The salt water 50 can be returned to the electrochemical process 16 via the input liquid 12 for reuse in the process, and the gaseous CO.sub.2 is stored.

[0269] The electrochemical process 16 in the system 10 of FIG. 6 can in some cases include an electrodialysis stack (e.g., an EDBM). In such cases, the electrodialysis stack receives the saltwater input liquid 12 and produces the hydrogen-rich stream 79, which is illustrated in this example as hydrochloric acid (HCl). The HCl can then be mixed with the sodium carbonate from the capture mechanism 16 to produce gaseous CO.sub.2.

[0270] As one possible alternative, in various implementations the electrochemical process 16 includes an electrolysis unit. In such cases, the electrolysis unit produces, for example, hydrogen and chlorine gases in addition to a hydroxide-rich stream. The hydrogen and chlorine gases can then be combined in an HCl oven and a deionized water absorber to produce the hydrochloric acid 79, which can in turn be used to produce the gaseous CO.sub.2 52 when mixed with the Na.sub.2CO.sub.3 from the air capture system 22. Thus, various examples of the capture systems 10 providing a hydrogen-rich stream such as HCl may be equipped with an electrochemical process 16 implemented by either an electrodialysis stack or an electrolysis unit in combination with an HCl oven and deionized water absorber.

[0271] Further implementations of the disclosed systems and methods can be combined or otherwise utilized with the following additional examples, and the teachings of each of the disclosed implementations outlined herein can make use of the technologies disclosed in the other examples and aspects, such that the teachings contained herein all relate to variations on the implementations disclosed elsewhere herein. One of skill in the art would readily appreciate that in certain implementations, features or other aspects disclosed in any specific example detailed herein can be combined with additional features outlined in alternate examples, such that the instant disclosure contemplates combining various features for individual applications of the disclosed technology.

Two

[0272] Additional embodiments disclosed or contemplated herein relate to methods, systems and devices for the extraction, concentration and precipitation of various metals and mineral hydroxides as part of a capture and sequestration of CO.sub.2 using containing water and salt inputs, electrochemical production of hydroxides, and airflow over packing structures.

[0273] FIG. 7 depicts an implementation of the carbon capture system 10 and various of its operational flows according to aspects of the disclosed technology. In this implementation, a variety of optional steps are performed. For example, in various implementations the system comprises a process having steps such as receiving an input liquid (box 100), performing an electrochemical process, on the inputted liquid (box 105) to produce at least one hydroxide-rich stream (box 110), capturing CO.sub.2 from air using the hydroxide-rich stream and a passive air capture system (box 120), and precipitating air-captured CO.sub.2 (box 130). As shown in FIG. 7, in various implementations the electrochemical process is electrolysis. In various implementations the electrochemical process includes electrodialysis performed via an electrodialysis stack (box 105), such as an ED stack configured for bipolar electrodialysis (BPED). In certain implementations the capture system 10 further allows for the precipitation of minerals or metals, such as lithium (box 135).

[0274] As discussed above, additional carbon capture system 10 implementations disclosed or contemplated herein relate to methods, systems and devices for the extraction, concentration and precipitation of various metals and mineral hydroxides. The metals and mineral hydroxide processes can in various cases be implemented as part of the capture and sequestration of CO.sub.2 using containing water and salt inputs, electrochemical production of hydroxides, and airflow over packing structures, as described herein.

[0275] In certain implementations, in addition to the permanent CO.sub.2 capture described above, the capture system 10 is also able to produce lithium, as shown in FIGS. 8-10, and in various cases can also reduce particulate matter concentrations in ambient air, as described herein. It is also understood that an object of various implementations of the capture system 10 described herein is to minimize the energy use and environmental impact associated with lithium and other metals extraction. Minimizing energy use itself is beneficial to the environment, plus the methods described have lower use of water and toxic chemicals than existing methods.

[0276] To that end, a capture system 10 according to certain implementations utilizes a method for the extraction of inorganic hydroxides that is given by:

X.sub.a(O.sub.bH.sub.c).sub.m [0277] where X represents any element or combination of elements that can chemically bond with oxygen and hydrogen or its multiple; [0278] where at least one element in X is a group IA, IIA, IIIA, IVA, IB, IIB, IIIB, IVB, VB, VIIB, VIIB, or VIIIB element of the periodic table; and [0279] where a, b, and c are stoichiometrically determined positive integers.

[0280] The extraction according to certain implementations is done in combination with the capture and sequestration of CO.sub.2 described above by using a metal- and/or mineral-containing input liquid 12 such as saline water 12 and electricity (via the electrochemical process 16, e.g., ED stack) as inputs, as is shown variously in FIGS. 8-10. In these implementations, electrochemistry and water are used to create hydroxides of the form of the hydroxide-rich stream 14 specified above, and these hydroxides can then be used to precipitate metal and mineral hydroxide solids and directly capture CO.sub.2 from the air.

[0281] In these implementations, after capturing CO.sub.2 from the air, the system 10 allows for the precipitation of solid carbonates as given by:

X(CO.sub.3).sub.m [0282] where X is any element or combination of elements that can chemically bond with a carbonate group or its multiple; [0283] where at least one said element is a group IA, IIA, IIIA, IVA, IB, IIB, IIIB, IVB, VB, VIIB, VIIB, or VIIIB element of the periodic table; and [0284] where m is a stoichiometrically determined positive integer.

[0285] Following such precipitation, solid carbonates can be collected and/or deposited into the ocean or other body of water to facilitate increased alkalinity, as shown in FIGS. 8-10.

[0286] Continuing with reference to FIGS. 8-10, the system 10 comprises a variety of optional steps and sub-steps. In certain implementations, the system 10 comprises feeding mineral containing saline water as an input liquid 12 to an electrochemical process 16 such as a bipolar electrodialysis membrane/ED stack to produce a hydroxide-rich stream 14, as described above.

[0287] It is understood that in these implementations, the stream 14 can be divided into a number of discrete portions for varying uses. For example, in certain of these implementations of the system 10, portions of the hydroxide-rich stream 14 are used for capturing and precipitating air-captured CO.sub.2 as carbonates and/or precipitating air-captured particulate matter, metals, and minerals such as lithium for use.

[0288] In these implementations of the system 10, certain of the minerals contained in the hydroxide-rich stream 14 are precipitated for extraction, while the other portions of the hydroxide-rich stream 14 are utilized for capturing CO.sub.2 as described above.

[0289] As shown in FIG. 9, the input liquid 12 is run through a pretreatment stage 15 that includes one or more various filtration and/or concentration systems, such as the filtration and concentration examples discussed above with respect to FIGS. 2-5. The filtered input liquid 12A is optionally mixed 17 with the recycled waste streams 19 and with a low pH solution 13, and then run through an electrochemical process 16 to create the hydroxide-rich stream 14, as previously described. As shown in FIG. 9, in various implementations the low pH solution 13 is a generated output from the electrochemical process 16.

[0290] In these implementations, solids, such as LiOH, can be precipitated out 60 and collected for the minerals or metals, such as lithium.

[0291] The electrochemical process 16 according to certain implementations is configured to ensure that the hydroxide-rich stream 14 is a high pH alkaline solution. This hydroxide-rich, alkaline solution 14 produced by the electrochemical process 16 is subsequently sent to a precipitation system (as shown in FIG. 9 at 60) to remove 62 metal and mineral hydroxides, such as lithium. Precipitation is utilized in certain implementations of this step to gather the solid metal and mineral hydroxides and retain portions of the hydroxide solution to be used for carbon capture. The process of increasing the alkalinity also converts the bicarbonates, carbonic acid and trapped CO.sub.2 into carbonate ions. It is appreciated that these will increasingly precipitate as pH increases.

[0292] The remainder of the stream 14A can be used for direct air carbon dioxide capture, as described above, via the optional introduction of concentrated CO.sub.2 28 and exposure to air 25, which is optionally filtered 32 for example in a cooling tower 40. That is, certain capture systems can utilize an air filter system 32 such as a HEPA filter 32 to filter particulate matter from the air 25 in the cooling tower 40, and the system can be further configured to capture additional particulate matter in the stream 14A during CO.sub.2 capture (shown at 22). The resulting stream 72, with particulate matter and captured CO.sub.2, contains liquid carbonates, which can then be precipitated 20 as solid metal oxides 70, CaCO.sub.3 and other compounds as would be readily appreciated.

[0293] As is also shown in the implementation of FIG. 9, certain systems can utilize a filter system to introduce further liquids with particulate matter 72 into the precipitate 20.

[0294] The output liquid stream 74 from the sequential precipitation 20 of solids can be further purified via various desalination 3 methods (such as via nanofilter (NF) 15A and/or reverse osmosis (RO) 15B) to produce clean water 1 as one output and concentrated brine 2 as a second output, which can be recirculated as would be understood.

[0295] FIG. 10 depicts a further, simplified implementation, wherein the system 10 utilizes a filter 32, such as a HEPA filter for air inputs and an additional treatment stage 15 (including reverse osmosis and nanofiltration) for water/liquid inputs, though one of skill in the art would appreciate that further filtering techniques could easily be used.

[0296] As previously noted, according to certain implementations, the system 10 uses saline water 12 that contains metals and minerals such as those described above and are readily appreciated by those of skill in the art. In further implementations of the system 10, the system is operated or performed near non-saline water containing minerals and includes various process modifications, as would also be appreciated. In various implementations these modifications can include 1) adding sodium to the non-saline water, and 2) introducing minerals into the water at the beginning of the process.

Three

[0297] As discussed above, the various embodiments disclosed or contemplated herein relate to methods, systems, and devices allowing for the capture and sequestration of CO.sub.2 using a liquid input such as saline water like seawater, brine, or other salty water with an electrochemical process and passive airflow over packing structures. According to another aspect of the disclosed technology, additional examples disclosed or contemplated herein relate to methods, systems, and devices for the production of byproducts such as, for example, green hydrogen and other gases such as chlorine gas or hydrochloric acid as part of the capture and sequestration of CO.sub.2. As in various other described examples, the capture and sequestration of CO.sub.2 from CO.sub.2-containing water and salt inputs can occur through the electrochemical production of hydroxides and airflow over packing structures.

[0298] As discussed elsewhere herein, various implementations of the carbon capture system 10 according to the disclosed technology relate to the sequestration of CO.sub.2 using an input liquid (e.g., saline water, such as seawater) and electricity. In these implementations, electricity is applied to saline water via an electrochemical process such as, for example, electrodialysis or electrolysis) to create hydroxide-rich solvents which can be used to directly capture CO.sub.2 from the air. In various implementations resulting precipitated solid carbonates are then deposited into in a body of water such as the ocean, and additional saline water is used to continue the process in a continuous manner.

[0299] FIGS. 11-12 depict various implementations of the carbon capture system 10 and various of its operational flows according to the disclosed technology. In these implementations, a variety of optional steps are performed, including steps depicted and discussed previously, such as with respect to FIG. 1. For example, in various implementations the capture system 10 comprises a process having steps such as receiving an input liquid (box 100) and performing an electrochemical process on the input liquid to produce at least one hydroxide-rich stream (box 110). The process also includes capturing CO.sub.2 from air using the hydroxide-rich stream and a passive air capture system (box 120), and precipitating air-captured CO.sub.2 (box 130) as, for example, solid carbonates.

[0300] In various implementations, the electrochemical process is configured to produce one or more byproducts in addition to the hydroxide-rich stream(s). For example, in various cases the electrochemical process includes an electrolyzing process that produces hydrogen gas and other gases such as chlorine gas. As shown in FIGS. 11 and 12, in various implementations, the electrochemical process (e.g., electrolysis) uses renewable energy (box 105) to thereby produce green hydrogen gas and other gases such as green chlorine gas (box 140) in addition to the hydroxide-rich stream(s). The system's operational flow 10 in FIG. 11 further allows for the storage of byproduct gases, such as hydrogen and chlorine, in pressurized vessels (box 150). The example operational process 10 in FIG. 12 includes the direct combination of the hydrogen and chlorine gases to produce hydrochloric acid (box 160). For example, in various implementations the hydrogen and chlorine gases are combined in an HCl oven and a deionized water absorber, and then stored in a vessel for further processing or selling (box 170).

[0301] As shown in FIGS. 13-15, various implementations of the carbon capture system 10 produce green hydrogen and other gases or byproducts as part of capturing and sequestrating CO.sub.2 according to the disclosed technology. As with the implementations of the system 10 shown in FIGS. 2-4, in various implementations of the capture system 10 depicted in FIGS. 13-15, an input liquid 12 such as seawater or other saline liquid is fed into the capture system 10 to produce a hydroxide-rich stream 14 containing salts such as NaOH and/or MgOH and/or CaOH and/or other hydroxides. As described herein, it is understood that implementations of the capture system 10, including those implementations shown in FIGS. 13-15, comprise one or more fluidic and/or electrical connections (shown generally at the lines) between a variety of optional components that can be arranged in a wide variety of arrangements, such that the various fluids/gasses and electricity described herein are able to flow as described.

[0302] Returning to FIGS. 13-15, in various implementations, after the liquid input 12 enters the capture system 10, some portion of the input liquid 12 is exposed to an electrochemical processor 16, which in this example is an electrolysis unit configured to perform electrolysis on the input liquid 12. In various implementations an optional pretreatment stage 15 is utilized, such as a nanofiltration and microfiltration system, an ion-exchange stage, and/or a reverse osmosis concentration stage, as would be appreciated. In various implementations, the electrolysis unit comprises a stack of ion-permeable membranes 18A disposed between a positively charged electrode 18B and a negatively charged electrode 18C. In various implementations, the electrochemical processor 16 is configured or otherwise comprises a set of electrolysis units connected in series or in parallel. Various other configurations of the electrochemical processor 16 can also be employed.

[0303] In use according to certain implementations, the application of electricity via the electrolysis unit causes the creation of the hydroxide-rich stream 14 from the input liquid 12. These hydroxides are then available to capture 22 CO.sub.2 from the air 25. In various implementations, an optional precipitation tank 20 is provided as a part of the system 10. As shown in FIG. 13, the precipitation tank 20 is in fluidic communication with one or more of the other system components as described herein.

[0304] Certain of the saline water 12 that provided Ca+, Na+, and Mg+ ions to the electrolysis unit is now partially desalinated 317 and of neutral pH. This seawater can be returned to the ocean or used to balance the pH of other waste streams before return.

[0305] Some or all of the hydroxide solution 14 is then sent to a direct air CO.sub.2 capture mechanism 22 for the capture of carbon dioxide as carbonates. This mechanism can be one of many existing approaches. Once this stream 14 has progressed through the CO.sub.2 capture system and becomes saturated with carbon, it is, in various cases, sent to a precipitation system 20 to extract carbonates. In various implementations, the direct air capture system 22 is preferably sited in a location with sustained wind speeds (shown at 25) to minimize flow time through the capture mechanism and energy cost.

[0306] Accordingly, the example capture systems depicted in FIGS. 13-15 relate to the capture and sequestration of CO.sub.2 using water and salt inputs, electrochemical production of hydroxides, and airflow over packing structures, as described herein. In addition to the permanent CO.sub.2 capture described above, various capture systems (e.g., such as those in FIGS. 13-15) are also able to produce hydrogen and chlorine gases, and can in some cases also reduce particulate matter concentrations in ambient air, as described herein. It is also understood that an object of various systems is to use renewable energy to minimize the environmental impact associated with the production of hydrogen gas. Renewable energy use itself is beneficial to the environment. In addition, various methods described herein have multiple uses for the chemicals produced, in some cases more than existing methods.

[0307] In various implementations, the capture system 10 utilizes a method for the extraction of inorganic hydroxides that is given by:

X.sub.a(O.sub.bH.sub.c).sub.m [0308] where X represents any element or combination of elements that can chemically bond with oxygen and hydrogen or its multiple; [0309] where at least one element in X is a group IA, IIA, IIIA, IVA, IB, 11B, IIIB, IVB, VB, VIIB, VIIB, or VIIIB element of the periodic table; and [0310] where a, b, and c are stoichiometrically determined positive integers.

[0311] The production of hydrogen gas according to certain implementations is done in combination with the capture and sequestration of CO.sub.2 described above by receiving an input saline liquid 12 such as seawater and renewable electricity to power the electrolysis unit, as is shown variously in FIGS. 13-15. In these implementations, electrochemistry and water are used to create hydroxides in the form of the hydroxide-rich stream 14 specified above, and simultaneously produce hydrogen gas 16B and chlorine gas 16C as byproducts. The hydroxide-rich stream is used to directly capture CO.sub.2 from the air.

[0312] In these implementations, after capturing CO.sub.2 from the air, the system 10 allows for the precipitation of solid carbonates as given by:

X(CO.sub.3).sub.m [0313] where X is any element or combination of elements that can chemically bond with a carbonate group or its multiple; [0314] where at least one said element is a group IA, IIA, IIIA, IVA, IB, IIB, IIIB, IVB, VB, VIIB, VIIB, or VIIIB element of the periodic table; and [0315] where m is a stoichiometrically determined positive integer.

[0316] Following such precipitation, solid carbonates can be placed into the ocean or other bodies of water to facilitate increased alkalinity.

[0317] In various implementations, the capture systems and methods 10 in FIGS. 13-15 comprise a variety of optional steps and sub-steps. In certain implementations, the capture system 10 includes feeding mineral-containing saline water as an input liquid 12 to an electrolysis unit to produce a hydroxide-rich stream 14, as described above.

[0318] In various implementations, a hydrogen-rich stream is produced at least in part with the electrochemical process 16. For example, the byproduct gas streams of hydrogen gas (16B) and chlorine gas (16C) from the electrochemical process 16 can be combined in a combustion chamber and passed through a deionized water absorber (16D) to form hydrochloric acid (16E) of various concentrations, as shown in the implementation of FIG. 15. In certain implementations, the byproduct gas streams of hydrogen gas (16B) and chlorine gas (16C) from the electrochemical process 16 can be stored in pressurized vessels for further processing and sale.

[0319] In various implementations of the capture system 10, certain of the minerals contained in the hydroxide-rich stream 14 are precipitated for extraction, while the other portions of the hydroxide-rich stream 14 are utilized for capturing CO.sub.2 as described above. As an example, in various implementations one or more mineral hydroxides (e.g., lithium hydroxide) are precipitated from the hydroxide-rich stream 14 as shown in FIG. 14.

[0320] Turning back to FIG. 15, in certain implementations, the system 10 can capture CO.sub.2 in gas form 52. As shown in FIG. 15, the system 10 is similar to the examples in FIGS. 13 and 14 with some modifications. The first is the mixing 48 of Na.sub.2CO.sub.3 produced via the direct air CO.sub.2 capture mechanism 22 with the low pH hydrochloric acid stream 16E produced from the hydrogen gas 16B and chlorine gas 16C generated by the electrochemical process 16. This combination creates CO.sub.2 in gas form 52 and saltwater 50. The saltwater 50 can be returned to the electrochemical process 16 for reuse in the process, and the gaseous CO.sub.2 is stored, as previously described.

[0321] According to certain implementations, the system 10 uses saline water 12 that contains metals and minerals such as those described above. In further implementations, the capture system and/or process 10 is operated or performed near non-saline water containing the minerals and including various process modifications, as would also be appreciated. These modifications can include, for example, 1) adding sodium to the non-saline water, and 2) introducing the minerals into the water at the beginning of the process.

[0322] FIG. 16 is a flow chart providing a detailed depiction of a carbon capture process and system 10, according to one possible implementation. The detailed diagram depicts a number of pumps, vessels, and other components of the system, in addition to fluid connections between relevant components. It will be appreciated that the system may include fewer and/or additional components and aspects that are not shown in various cases.

[0323] Continuing with reference to FIG. 16, in this example the system 10 receives a saltwater input liquid 12 that is then pumped into an expansion vessel (V-001) before sending it to a pretreatment stage. The pretreatment stage in this example includes a nano-filtration unit (15A) and an ion exchange unit (15C) to remove divalent ions such as, for example, calcium and magnesium. The output from this pretreatment stage, (e.g., filtrate) is stored in vessel (V-002) before sending it to an electrochemical processor 16. In various implementations, the electrochemical processor is an electrolysis unit as shown in FIG. 16.

[0324] The electrochemical processor 16 (e.g., electrolysis unit) splits the pretreated input liquid into a hydroxide-rich stream 14, a hydrogen gas stream (16B), and a chlorine gas stream (16C). The hydroxide-rich stream is then passed through an air contactor (22) wherein it absorbs carbon dioxide from an air stream (25) to form carbonates. These carbonates (stream 72) are then pumped to a precipitator or a settling tank (20) where they are mixed with divalent ion streams from the nano-filtration 15A and ion exchange package 15C to form calcium carbonate. The calcium carbonate solution is then separated into a slurry of calcium carbonate solids (stream 30). In some cases a centrifugal dryer CG-001 is used to separate out the slurry of solid carbonates 30 and water (802), which is recycled back into the system.

[0325] According to various implementations, the input liquid 12 received by the capture system 10 is an artificial brine. In some cases the artificial brine is different than seawater brine or a brine reject obtained from seawater reverse osmosis and is instead made by adding salt to fresh water.

[0326] In various implementations the process/system 10 in FIG. 16 uses one or more additional inputs and may generate one or more additional outputs. As just one possible example, in various implementations a regen stream 806 including, for example, some amount of HCl, is used to regenerate the ion exchange pretreatment stage 15C. As will be appreciated, additional inputs and/or outputs may be present in various implementations of the system 10.

Four

[0327] Turning to FIGS. 17-22, some implementations are related to another aspect of the disclosed technology including one or more of capture and sequestration of CO.sub.2, extraction of lithium compounds, and production of byproducts such as green hydrogen and other gases such as chlorine gas or hydrochloric acid. Various implementations disclosed or contemplated herein relate to methods, systems, and devices allowing for the simultaneous capture and sequestration of CO.sub.2 in an air contactor and extraction of lithium compounds in an absorber using a liquid input such as saline water like seawater, brine, or other salty water with electrolysis.

[0328] Additional implementations disclosed or contemplated herein relate to methods, systems, and devices for the production of byproducts—green hydrogen and other gases such as chlorine gas or hydrochloric acid as part of combined capture and sequestration of CO.sub.2 in an air contactor and lithium extraction in an absorber using containing water and salt inputs, electrochemical production of hydroxide-rich and hydrogen-rich streams.

[0329] Additional implementations disclosed or contemplated herein relate to methods, systems, and devices for the sequestration of CO.sub.2 in a gas form by using the hydroxide-rich stream to capture CO.sub.2 as carbonates in an air contactor and regenerating the CO.sub.2 using the hydrogen-rich stream. The collected CO.sub.2 gas is then used in combination with the lithium absorber to form lithium carbonate.

[0330] As previously discussed, and also described herein with respect to FIGS. 17-22, the disclosed technologies are referred to broadly as an operational flow 10 and/or capture system 10, though it is understood that this is for brevity and in no way intended to be limiting to any specific modality.

[0331] Certain implementations of the disclosed capture system 10 relate to the sequestration of CO.sub.2 and extraction of Li using only saline water-such as geothermal or seawater—and electricity. In these implementations, electricity is applied to saline water via electrolysis to create hydroxide-rich solvents which can be used to directly capture CO.sub.2 from the air. The electrolysis also creates hydrogen-rich solvents which can be used to recover Li from an absorber. The resulting precipitated lithium carbonate is recovered for post-processing/selling and other solid carbonates such as calcium carbonate are then deposited into the ocean, and additional saline water is used to continue the process, so as to make it continuous.

[0332] FIGS. 17 and 18 depict various implementations of the carbon capture system 10 described herein. In these implementations, a variety of optional steps are performed. For example, in various implementations the system 10 comprises a process as shown in FIG. 17 having steps such as receiving an input liquid (box 100), which is pretreated and filtered (box 210) prior to performing an electrochemical process on the inputted liquid. In the illustrated example, the electrochemical process includes electrodialysis, which produces at least one hydroxide-rich stream and one hydrogen-rich stream (box 220). The process further includes capturing CO.sub.2 from air using the hydroxide-rich stream and a passive air capture system (box 120) and extracting Li from an absorber using the hydrogen-rich stream (box 240). The process also includes precipitating air-captured CO.sub.2 and Li from the absorber as carbonates (box 250).

[0333] As shown in FIG. 18, in various implementations, the electrochemical process includes electrolysis. In various cases the electrolysis is performed using renewable energy (box 105) to produce hydrogen gas and other gases such as chlorine gas (box 140) in addition to the hydroxide-rich stream(s) (box 110). In certain implementations, the operational flow of the system 10 further allows for the direct combination of the hydrogen and chlorine gases in a HCl oven and a deionized water absorber to produce hydrochloric acid (box 160). The hydrochloric acid is used in the Li absorber to form soluble Li compounds (box 240) that are precipitated as carbonates (box 250).

[0334] As shown in FIG. 19, in various implementations of the system 10, an input liquid 12 such as seawater or other saline liquid is fed into the capture system 10, pretreated and filtered to remove coarse particles and divalent ions such as calcium and magnesium 15A, and passed through the Li absorber 80. The input liquid 12 coming out of the Li absorber is then passed into an electrochemical processor 16. In this example the processor 16 includes a bipolar membrane electrodialysis stack 16 that produces a hydroxide-rich stream 14 containing salts such as NaOH and/or MgOH and/or CaOH and/or other hydroxides, as well as a hydrogen-rich stream containing acids such as HCl 79. As described herein, it is understood that the capture system 10 comprises one or more fluidic and/or electrical connections (shown generally at the lines) between a variety of optional components that can be arranged in a wide variety of arrangements, such that the various fluids/gasses and electricity described herein are able to flow as described.

[0335] As shown in FIG. 20, in various implementations, after the liquid input 12 enters the system 10, and is passed through pretreatment 15A and Li absorption steps 80, some portion of the input liquid 12 is exposed to an electrochemical processor 16 that includes an electrolysis unit that is configured to perform electrolysis on the input liquid 12. In various implementations, the electrolysis unit comprises a stack of ion-permeable membranes 18A disposed between a positively charged electrode 18B and a negatively charged electrode 18C. In various implementations, the electrolysis unit is configured or otherwise comprises a set of electrolysis units connected in series or in parallel. Various other configurations of the electrolysis units can also be employed.

[0336] In use according to certain implementations, the application of electricity via the electrolysis unit causes the creation of the hydroxide-rich stream 14 from the input liquid 12. In various implementations, a hydrogen-rich stream is produced at least in part with the electrochemical process 16. As shown in FIG. 20, in certain implementations, the byproduct gas streams of hydrogen gas (16B) and chlorine gas (16C) are combined in a combustion chamber and deionized water absorber (16D) to form the hydrogen-rich stream of hydrochloric acid (16E) of various concentrations. The hydroxide-rich stream is used to capture 22 CO.sub.2 from the air 25. The hydrogen-rich stream is used to extract Li from the Li absorber 80.

[0337] Some or all of the hydroxide solution 14 is then sent to a direct air CO.sub.2 capture mechanism 22 for the capture of carbon dioxide as carbonates. This mechanism can be one of many existing approaches. Once this stream 14 has progressed through the CO.sub.2 capture system and becomes saturated with carbon, it is again preferably sent to a precipitation system 20 to extract carbonates. The direct air capture system is preferably sited in a location with sustained wind speeds to minimize flow time through the capture mechanism and energy cost.

[0338] As shown in FIG. 19, in various implementations some or all of the hydrogen-rich solution 79 from the bipolar membrane electrodialysis stack is sent to the Li absorber 80 to extract Li from the sorbent in form of Li compound. As shown in FIG. 20, in various implementations some or all of the hydrogen-rich solution 16E from the electrolysis unit is sent to the Li absorber 80. In both examples, one of the output streams from the lithium absorber 80 is then sent to a precipitation system 20 which contains sodium carbonate generated through the direct air capture system. Lithium compound, in one such manifestation, is then precipitated as lithium carbonate.

[0339] To that end, the system 10 according to certain implementations utilizes a method for the extraction of inorganic hydroxides that is given by:

X.sub.a(O.sub.bH.sub.c).sub.m [0340] where X represents any element or combination of elements that can chemically bond with oxygen and hydrogen or its multiple; [0341] where at least one element in X is a group IA, IIA, IIIA, IVA, IB, IIB, IIIB, IVB, VB, VIIB, VIIB, or VIIIB element of the periodic table; and [0342] where a, b, and c are stoichiometrically determined positive integers.

[0343] In these implementations, after capturing CO.sub.2 from the air, the system 10 allows for the precipitation of solid carbonates as given by:

X(CO.sub.3).sub.m [0344] where X is any element or combination of elements that can chemically bond with a carbonate group or its multiple; [0345] where at least one said element is a group IA, IIA, IIIA, IVA, IB, IIB, IIIB, IVB, VB, VIIB, VIIB, or VIIIB element of the periodic table; and [0346] where m is a stoichiometrically determined positive integer.

[0347] Following such precipitation, value add carbonates such as lithium carbonates are separated and processed further for sale and storage while other solid carbonates such as calcium carbonate can be placed into the ocean or other bodies of water to facilitate increased alkalinity.

[0348] Various implementations of the system 10 as illustrated in FIGS. 19-22 include a variety of optional steps and sub-steps. In certain implementations, some or all of the hydrogen-rich solution 79 from the electrochemical processor 16 (e.g., bipolar membrane electrodialysis stack) in FIG. 19 or the stream 16E in the case of the electrochemical processor 16 (e.g., electrolysis unit) in FIG. 20 is neutralized over rocks such as olivine to enhance weathering and further increase the amount of carbon dioxide removal.

[0349] As shown in the implementation of FIG. 21, in certain implementations, the system 10 can capture CO.sub.2 in gas form. This approach uses the same process described herein with two modifications. The first is the mixing of Na.sub.2CO.sub.3 produced via the direct air CO.sub.2 capture mechanism 22 with the low pH hydroxide-rich stream produced via the electrochemical process 16 (see, e.g., discussion of FIG. 6 herein). In various implementations the Na.sub.2CO.sub.3 is mixed with the low pH hydrochloric acid produced from the hydrogen and chlorine gases generated by the electrochemical processor 16 (in this case an electrolysis unit) and discussed further with respect to FIG. 15. The combination in each case creates CO.sub.2 in gas form 52 and saltwater (not shown). The saltwater can be returned to the electrochemical process 16 for reuse in the process, and the gaseous CO.sub.2 is stored, as previously described, or used in Li absorber 80 to directly convert Li-ions absorbed on the sorbent into lithium carbonate, which is stored and post-processed for sale, as previously described.

[0350] FIG. 22 is a flow chart providing a detailed depiction of a carbon capture process and system 10, according to one possible implementation. The detailed diagram depicts a number of vessels, and other components of the system, in addition to fluid connections between relevant components. It will be appreciated that the system may include fewer and/or additional components and aspects that are not shown in various cases.

[0351] As is shown in FIG. 22, in this example the system 10 receives an input liquid 12 including salt water, that flows to a pretreatment stage. The pretreatment stage in this example includes a nano-filtration unit (15A) to remove divalent ions such as, for example, calcium and magnesium. The filtrate output from the pretreatment stage is then passed through a lithium extraction vessel (V-001) to selectively absorb lithium ions from the saltwater input liquid 12.

[0352] The absorbed lithium ions are extracted in stream 808 using hydrochloric acid (79) from an electrochemical processor 16. Carbonates 72 from the air contactor 22 are fed along with the lithium-ion stream 808 (e.g., lithium chloride) into a lithium precipitation vessel (V-002). The carbonates mix with the lithium-ion stream in the precipitation vessel to produce a lithium carbonates stream 810. The input liquid (e.g., saltwater stream) 12, which is now depleted of lithium, is output from the lithium extraction vessel (V-001) and fed to the electrochemical processor 16. In this example the electrochemical processor 16 is an electrodialysis bipolar membrane unit (EDBM-001).

[0353] According to various implementations, the EDBM unit splits the salt stream 12 into an hydroxide-rich stream (14) and a hydrogen-rich stream (79). In various cases the hydrogen-rich stream is hydrochloric acid, which is optionally made available as an output, and also fed to the lithium extraction vessel as previously noted. The hydroxide-rich stream is passed through the air contactor (22) wherein it absorbs carbon dioxide from an air stream (25) to form carbonates. These carbonates (72) are then fed to a sparger or a bubble column reactor (V-003) wherein concentrated CO.sub.2 (28) from industrial gases is passed through to form bicarbonates (814). The bicarbonates and other carbonate precipitates are separated in the centrifuge dryer (CG-001) as stream 30.

[0354] As will be appreciated, in this example one of the main inputs into the capture process 10 is the input saltwater liquid (12). In various implementations another input is concentrated CO.sub.2 28 from, for example, various industrial processes and plants. In the depicted example, some of the outputs are carbonate and bicarbonate solids (30), hydrochloric acid (79), and lithium carbonates 810.

[0355] In various implementations the process/system 10 uses one or more additional inputs and may generate one or more additional outputs. In various implementations one or more ancillary inputs and/or outputs are largely recycled within the system. For example, in some cases an output from the electrochemical process 16 is processed (e.g., by reverse-osmosis) and provides low total dissolved solids (TDS) water (804), which can be used as a makeup liquid for the EDBM unit. In some cases an HCl make-up stream and/or NaOH make-up stream are also used to facilitate the EDBM unit. As will be appreciated, additional inputs and/or outputs may be present in various implementations of the system 10.

Five

[0356] Turning now to FIGS. 23-30, various systems, methods and devices implement another aspect of the disclosed technology relating to post-processing and sequestration in Direct Air CO.sub.2 Capture and/or storing or handling of various elements and compounds. Various embodiments disclosed or contemplated herein allow for the capture and sequestration of CO.sub.2 using a liquid input such as saline water like seawater, brine, or other salty water with an electrochemical process and passive airflow over an air contactor. Additional embodiments relate to post-processing of the air-captured CO.sub.2 carbonates, the recycling of the hydroxide-rich liquid solution, the neutralization, over olivine rocks, and the recycling of the hydrogen-rich liquid solution, and the storing of CO.sub.2 in gas form while recycling the salt solutions back to the electrochemical process.

[0357] As previously described herein, examples and implementations of the disclosed technologies, including the implementations in FIGS. 23-30 are referred to broadly as a capture system 10 with various operational processes, though it is understood that this is for brevity and in no way intended to be limiting to any specific modality.

[0358] As discussed elsewhere herein, certain implementations of the capture system 10 relate to the sequestration of CO.sub.2 using an input liquid with only saline water-such as seawater—and electricity. In these implementations, electricity is applied to saline water via electrolysis to create hydroxide-rich solvents which can be used to directly capture CO.sub.2 from the air. The resulting liquid carbonate solution or the further processed precipitated solid carbonates are then deposited into the ocean, or stored on land, and additional saline water is used to continue the process, so as to make it continuous.

[0359] FIGS. 23-26 depict various implementations of the capture system 10 described herein. In these implementations, a variety of optional post-processing steps are performed after the capture of carbon dioxide from the air via hydroxide-rich streams. For example, as shown in FIGS. 23, 24, and 26, in various implementations the liquid carbonate solution from the air contactor is directly stored in an ocean or on land (box 340). In some cases the hydrogen-rich stream is neutralized over olivine rocks (box 335), as shown in FIGS. 24 and 25. In various implementations, the hydroxide-rich stream (box 350) and the hydrogen-rich stream (box 355) are recycled back to the electrochemical process step 310 as depicted in the example of FIG. 24. In some cases the salt solution is recycled back (box 360) to the electrochemical process step either through a direct neutralization step (box 335) as shown in FIG. 25 or indirectly using liquid solutions (box 380) as shown in FIG. 26. Further, in various implementations the system 10 stores CO.sub.2 in gas form (box 370) as depicted n FIG. 25.

[0360] Various implementations of the capture system 10 with various post-processing steps are depicted in FIGS. 27-30 according to the disclosed technology. As shown in FIG. 27, in various post-processing implementations of the air-captured CO.sub.2, the carbonate solution 72 leaving the air contactor 22 is directly deposited in a large water body such as an ocean or first converted into another carbonate in a precipitator 20 and the precipitate is then deposited in an ocean or stored on land. In various implementations, the air contactor 22 is a static pond wherein a rich-hydroxide solution is exposed to air for a certain time before being disposed of. In another implementation, the air contactor 22 is a cooling tower or a system with fans or other energy-supported units to help the convection of air and increase the contact with the hydroxide-rich solution.

[0361] As shown in FIG. 28, in various implementations, the hydroxide-rich liquid 14A from the precipitator 20 is recycled back to the electrochemical process 16. In various implementations, the hydrogen-rich liquid 79 from the electrochemical process 16 is neutralized in a solid-liquid mixer with Olivine rocks 82, and the neutralized mixture 83 is either stored in an ocean or on land while the unused hydrogen-rich solution 79A is recycled back to the electrochemical process 16. Various other configurations of the acid-neutralization process can also be employed.

[0362] In use according to certain implementations, the application of heat or cooling via a heat exchanger may be required for enhancing the kinetics of certain reactions and processes.

[0363] As shown in FIGS. 29 and 30, in various implementations, the liquid carbonate solution 72 from the air-capture unit 22 is directly or indirectly neutralized with a hydrogen-rich stream such as hydrochloric acid 79 in a mixer/bubbler 48. The direct neutralization reaction releases carbon dioxide gas 52 which is then captured for storage in pressurized vessels 52A. The resulting sodium chloride solution 50 is recycled back to the electrochemical process step 16.

[0364] In various implementations, as shown in FIG. 30, the hydrogen-rich stream 79 reacts with the divalent rejects from a pretreatment system 15 including, for example, filtration, concentration, and ion exchange stages), in a mixer bubbler 48A to form liquid solutions 48B, e.g., calcium chloride solution. This calcium chloride solution 48B combines with the sodium carbonate solution 72 from the air capture system 22 in a precipitator 20 to form a precipitate-calcium carbonate which is then disposed of in the ocean or on land. The liquid solution from the precipitator is the sodium chloride salt solution 50 which is then recycled back to the electrochemical process step.

[0365] In various implementations, as shown in FIG. 30, a calcium-rich stream or stream of other similar compounds 15D obtained from an external source is used in the mixer/bubbler 48A along with the hydrogen-rich stream 79 to form a chloride solution 48B which reacts with sodium carbonate from the air contactor 22 in the precipitator 20 to form a precipitate that is disposed of in the ocean or on land and a liquid salt solution 50 that is recycled back to the electrochemical process step.

[0366] FIG. 31 is a flow chart providing a detailed depiction of a carbon capture process and system 10, according to one possible implementation. The detailed diagram depicts a number of pumps, vessels, and other components of the system, in addition to fluid connections between relevant components. It will be appreciated that the system may include fewer and/or additional components and aspects that are not shown in various cases.

[0367] As is shown in FIG. 31, in this example the system 10 receives an input liquid 12 that includes salt water. The input liquid 12 is pumped into an expansion vessel (V-001) before sending it to a pretreatment system that includes a nano-filtration unit (15A) and an ion exchange unit (15C) to remove divalent ions such as calcium and magnesium. The filtrate output from the pretreatment stage is stored in a vessel (V-005) before sending it (pump, P-005) to an electrochemical processor 16.

[0368] In various implementations the electrochemical processor 16 includes an electrodialysis bipolar membrane (EDBM-001) unit as shown in FIG. 31. The EDBM unit splits the input salt liquid 12 into an hydroxide-rich stream (14) and a hydrogen-rich stream (79). The hydroxide-rich stream 14 is then passed through an air contactor (22) wherein it absorbs carbon dioxide from air stream (25) to form carbonates. These carbonates (72) are then fed to a sparger or a bubble column reactor or a carbonation tower (V-006) wherein concentrated CO.sub.2 (stream 18) from industrial gases is passed through the carbonate solution to form bicarbonates (814). The bicarbonates along with other carbonates (30) are dried in a centrifuge dryer (CG-001) to separate out a slurry of solids (30) and recycle back the additional water (802).

[0369] FIG. 32 is a flow chart providing a detailed depiction of a carbon capture process and system 10, according to one possible implementation. The detailed diagram depicts a number of pumps, vessels, and other components of the system, in addition to fluid connections between relevant components. It will be appreciated that the system may include fewer and/or additional components and aspects that are not shown in various cases.

[0370] As is shown in FIG. 32, in this example the system 10 receives an input liquid 12 that includes salt water (12) that is pumped into an expansion vessel (V-001) before sending it to a pretreatment stage that includes, for example, a nano-filtration unit (15A) and an ion exchange unit (15C) to remove divalent ions such as calcium and magnesium. The output from the pretreatment stage (e.g., filtrate) is stored in vessel (V-004) and mixed with recycled salt water (50) before sending it to an electrochemical processor 16.

[0371] In the various implementations, the electrochemical processor 16 is an electrodialysis bipolar membrane (EDBM-001) unit. The EDBM unit in this example splits the salt input liquid into an hydroxide-rich stream (14) and a hydrogen-rich stream (79). The hydroxide-rich stream is then passed through an air contactor (22) wherein it absorbs carbon dioxide from air stream (25) to form carbonates. These carbonates (72) are then fed to, e.g., a continuous stirred tank reactor (CSTR, V005), and mixed with hydrochloric acid (79) to form carbon dioxide gas (52) which in some cases is compressed and stored for further processing. In various implementations the salt solution 50 remaining in the CSTR is recycled back to the EDBM unit.

[0372] Turning now to FIGS. 33-36, various systems, methods and devices implement another aspect of the disclosed technology relating to post-processing of hydroxide-rich and hydrogen-rich liquid solutions in ways, among other things, that include optimizing the process, increasing the amount of carbon dioxide captured, and reducing the cost. The various embodiments disclosed or contemplated herein allow for the capture and sequestration of CO.sub.2 using a liquid input such as saline water like seawater, brine, or other salty water with an electrochemical process and passive airflow over an air contactor.

[0373] As described herein elsewhere, examples and implementations of the disclosed technologies are referred to broadly as a capture system 10 with various operational flows or processes, though it is understood that this is for brevity and in no way intended to be limiting to any specific modality.

[0374] FIGS. 33 and 34 depict various implementations of the capture system 10 and associated operational flows. In these implementations, a variety of optional post-processing steps are performed after the capture of carbon dioxide from the air via hydroxide-rich streams. For example, in various implementations, the liquid carbonate solution (box 410) from the air contactor is exposed to additional carbon dioxide gas from an industrial source (box 400) to form and precipitate bicarbonates (box 420) before storing it on land or in a large water body (box 340).

[0375] FIG. 34 depicts an implementation of the capture system 10 in which the hydrogen-rich stream is neutralized on carbonate (box 335) releasing CO.sub.2 gas. The resulting salt solution is recycled back (box 360) to the electrochemical process step 310. In various implementations the CO.sub.2 is stored in gas form (box 370).

[0376] Various implementations of the capture system 10 are depicted in FIGS. 35-36 according to the disclosed technology. As shown in FIG. 35, in various post-processing implementations of the air-captured CO.sub.2, the carbonate solution 72 leaving the air contactor 22 is exposed to additional carbon dioxide gas 28 from an industrial source in a reactor 80 to form bicarbonate precipitate that is ultimately stored on land or in a large water body.

[0377] In another implementation, as shown in FIG. 36, the liquid carbonate solution 72 from the air-capture unit 22 and the resulting bicarbonate solution 72A from the reactor 80 with industrial carbon dioxide gas is directly or indirectly neutralized with a hydrogen-rich stream such as hydrochloric acid 79 in a mixer/bubbler 48. The direct neutralization reaction releases carbon dioxide gas 52 which is then captured for storage in pressurized vessels 52A. The resulting sodium chloride solution 50 is recycled back to the electrochemical process step 16.

Six

[0378] Turning to FIGS. 37-39, some implementations are related to another aspect of the disclosed technology relating to methods, systems, and devices for the production of multiple products streams such as green hydrogen gas, hydrochloric acid, and sodium hydroxide as part of capture and sequestration of CO.sub.2 using containing water and salt inputs, electrochemical production of hydroxides, and airflow over packing structures.

[0379] As previously discussed, and also described herein with respect to FIGS. 37-39, the disclosed technologies are referred to broadly as a capture system 10 with various operational processes or flows. It should be understood that this is for brevity and in no way intended to be limiting to any specific modality.

[0380] Certain implementations of the disclosed capture system 10 relate to the sequestration of CO.sub.2 using only an input liquid 12 (e.g., saline water, such as seawater) and electricity. In these implementations, electricity is applied to saline water via an electrochemical processor. In various cases the electrochemical processor is a bipolar membrane electrodialysis (BPED) unit configured to create hydroxide-rich streams which can be used to directly capture CO.sub.2 from the air. The resulting precipitated solid carbonates are then deposited into the ocean, and additional saline water is used to continue the process, so as to make it continuous. In various implementations, additional products, such as hydrogen gas and a hydrogen-rich solvent, are created in the BPED unit during the production of hydroxide-rich solvents.

[0381] FIG. 37 depicts various implementations of the capture system 10 and operational flow described herein. In these implementations, a variety of optional steps are performed. For example, in various implementations the system 10 comprises a process having steps such as receiving an input liquid (box 100) and performing an electrochemical process on the input liquid. In the illustrated example, the electrochemical process includes electrodialysis, which produces at least one hydroxide-rich stream and one hydrogen-rich stream (box 310). The system and process 10 also includes capturing CO.sub.2 from air using the hydroxide-rich stream and a passive air capture system (box 120) and precipitating air-captured CO.sub.2 (box 130). In various implementations, electrodialysis is performed using renewable energy to produce hydrogen gas in addition to the hydroxide-rich and hydrogen-rich solvent streams (box 145). In certain implementations, the system 10 further allows for the storage of byproduct gases, such as hydrogen, in pressurized vessels (box 150).

[0382] As shown in FIG. 38, in various cases a capture system 10 has an electrochemical process 16 that is used to split salts in the input liquid 12 to form a hydroxide-rich stream 14 (e.g., with NaOH) and a hydrogen-rich stream containing acids such as HCl (not shown). The NaOH stream 14, when exposed to ambient air or industrial gases in an air-capture unit 22, captures CO.sub.2 to form carbonates that are stored on land or in water. In certain implementations, the electrochemical process includes a bipolar membrane electrodialysis (BPED) unit, which produces hydrogen gas in addition to the hydroxide- and hydrogen-rich (e.g., NaOH and HCl) streams.

[0383] FIG. 39 provides a detailed picture of a section of an electrochemical processor 16 according to various implementations. In various cases the electrochemical processor 16 is configured as a bipolar electrodialysis (BPED) unit that produces multiple product streams according to various implementations. As is shown, feed water 12 enters into the BPED unit, which has a cathode 85 and an anode 86. The unit includes multiple membranes stacked in a predetermined manner to produce the streams needed. These membranes include a cation exchange membrane (CEM) 87 and an anion exchange membrane (AEM) 88.

[0384] In various implementations the CEM 87 allows hydrogen ions generated from the splitting of the water molecule to pass through while the AEM 88 allows the hydroxyl ion to pass through. The hydrogen ions are consumed at the cathode to form hydrogen gas 91. Other electrochemical reactions on the electrode surface are also possible, though a proper selection of electrode materials and the use of electrocatalysts may increase selectivity for hydrogen evolution reactions. The remaining hydrogen ions compose a dilute hydrochloric acid 90.

[0385] The anion exchange layer 88 allows the hydroxyl ions to pass through, which are then protected by an adjacent CEM 87 to form a relatively concentrated sodium hydroxide 89 (compared to the dilute HCl generated). To further increase sodium hydroxide concentration, partial recycle may be implemented in various cases.

Seven

[0386] Various implementations disclosed or contemplated herein relate to methods, systems, and devices allowing for the simultaneous capture and sequestration of CO.sub.2, desalination of water, and value-add mineral extraction. In various cases carbon dioxide is captured and sequestered from ambient air (e.g., in an air contactor) and also from industrial sources (e.g., in a bubble column or sparger reactor). Desalinated water can be provided for industrial and residential uses in some cases. The combined processes are closely integrated, with several interdependencies and synergies, leading to an efficient system wherein products are used interchangeably between the processes, resulting in advantages such as low carbon emissions and reduced waste stream.

[0387] Additional implementations disclosed or contemplated herein relate to methods, systems, and devices for the extraction of value-add minerals such as, among others, chromium, bromine, and lithium, the recovery of low total dissolved solids (TDS) water for use in residential or industrial purposes, and the capture of carbon dioxide. In various implementations, carbon dioxide is absorbed from fossil fuel energy generated for, among others, reverse osmosis and desalination of salty water and/or captured from ambient air using processes such as, among others, nanofiltration, ion exchange, and electrolysis or electrodialysis to manufacture the solvent from high-salinity brine.

[0388] As previously discussed, and also described herein with respect to FIGS. 40-41, the disclosed technologies are referred to broadly as a capture system 10 with various operational processes or flows, though it is understood that this is for brevity and in no way intended to be limiting to any specific modality.

[0389] Certain implementations of the capture system 10 shown in FIGS. 40-41 relate to the sequestration of CO.sub.2 and simultaneous extraction of value-add minerals along with recovery of low TDS water for residential and industrial purposes using only saline water, such as seawater or brackish groundwater, and electricity. In these implementations, electricity is applied to the input saline water via an electrochemical process. In various implementations the electrochemical process includes electrolysis, which creates hydroxide-rich solvents which can be used to directly capture CO.sub.2 from the air. In various implementations the electrochemical process (e.g., electrodialysis or electrolysis) also creates a hydrogen-rich and chlorine-rich solvent stream that can be used for mineral extraction and for disinfecting the low TDS water for its use.

[0390] FIGS. 40-41 depict various synergistic and interdependencies among carbon capture, mineral extraction, and desalination processes according to various implementations of the capture system and process 10. In the depicted implementation, a variety of optional steps are performed. For example, in various implementations the system 10 comprises a process having steps such as receiving input liquid (box 100) and disinfecting the input liquid with chlorine-based products (box 510) obtained from the electrochemical reaction used to produce solvent for the carbon capture process (box 310).

[0391] The disinfected product is then passed through a pretreatment stage that variously includes nanofiltration and ion exchange. The product is further pretreated with carbonates such as sodium carbonate and sodium bicarbonate (box 520) which are obtained from the carbon capture process (box 580). The pretreated solution is then processed through hydrogen-rich solvents from the electrochemical process, such as hydrochloric acid, to dissolve metals and minerals and the dissolved materials are precipitated as carbonates for extraction (box 530).

[0392] The resulting water stream is passed through reverse osmosis and other processes involved in the desalination of the water (box 550) to obtain a low TDS stream for residential and industrial use (box 560). The concentrated, high-salinity brine is then passed through an electrochemical process such as electrolysis or electrodialysis for producing solvents (box 310) including, for example, hydrogen-rich and/or hydroxide-rich solvents. A solvent, such as sodium hydroxide, is used to capture CO.sub.2 (box 580) from ambient air as well as from an industrial source, such as a fossil fuel energy generator (box 540) used to power the metal extraction and desalination processes.

[0393] As shown in FIG. 41, in various implementations of the system 10, an input liquid 12 such as seawater 12 or other saline liquid 12 is fed into the capture system 10. The input liquid 12 is pretreated and filtered to remove coarse particles 15A and divalent ions such as calcium and magnesium 15C. The input liquid 12 is then passed through a metal and mineral extraction process, such as in an absorber 80A, before precipitating the metal and minerals for further purification 80B. The input liquid 12 coming out of the metal and mineral extraction process 80A is also passed through a reverse osmosis unit 120 which uses energy from a fossil fuel generator 121. The reverse osmosis unit 120 separates the water into a low TDS water stream 122 that can be further disinfected with hydrogen and chlorine-rich disinfectant before sending it for residential and industrial use 123. In addition, the concentrate from the reverse osmosis stage 120 is filtered 15A, if needed, before being passed into a bipolar membrane electrodialysis stack 16 to produce a hydroxide-rich stream 14 containing salts such as NaOH and/or other hydroxides and/or a hydrogen-rich stream containing acids such as HCl.

[0394] As described herein, it is understood that the capture system 10 shown in FIG. 41 comprises one or more fluidic and/or electrical connections (shown generally at the lines) between a variety of optional components that can be arranged in a wide variety of arrangements, such that the various fluids/gasses and electricity described herein are able to flow as described.

[0395] Some or all of the hydroxide solution 14 is then sent to a direct air CO.sub.2 capture mechanism 22 for capturing carbon dioxide and an industrial gas CO.sub.2 capture mechanism 48 for capturing an industrial source of carbon dioxide 28 as carbonates. This mechanism can be one of many existing approaches. Once this stream 14 has progressed through the CO.sub.2 capture systems and becomes saturated with carbon, it is again preferably sent to a precipitation system 20 to extract carbonates.

[0396] FIG. 42 is a flow chart providing a detailed depiction of a carbon capture process, according to one possible implementation. The detailed diagram depicts a number of vessels and other components of the system, in addition to fluid connections between relevant components. It will be appreciated that the system may include fewer and/or additional components and aspects that are not shown in various cases.

[0397] Continuing with FIG. 42, in various implementations, a capture system and method 10 receives an input liquid 12, such as, for example, sea water, which is then sent through a pretreatment stage. In the illustrated example, the pretreatment stage includes a reverse osmosis unit (15B) in which the input liquid 12 is concentrated. Following the concentration, the resulting permeate (818) which contains reduced dissolved salts (low TDS) is returned back for residential and industrial use. The concentrated input liquid 12 from the reverse osmosis unit (15B) is then fed to a nano-filtration unit (15A) and an ion exchange unit (15C) to remove divalent ions such as calcium and magnesium. The output of the pretreatment stage (e.g., filtrate) is then sent to an electrochemical processor 16.

[0398] In various implementations, the electrochemical processor 16 includes an electrodialysis bipolar membrane (EDBM-001). The EDBM unit is configured to split the input liquid salt stream into a hydroxide-rich stream (14) and a hydrogen-rich stream (79). The hydroxide-rich stream is then passed through an air contactor (22) wherein it absorbs carbon dioxide from an air stream (25) to form carbonates. These carbonates (72) are then pumped to a reactor (V-002) which absorbs CO.sub.2 from industrial gases (28) and from a desalination facility (820) to form bicarbonates (stream 814). In various implementations the solid bicarbonate slurry (814) is separated in a centrifuge dryer (CG-001) into a solid carbonate/bicarbonate precipitant stream 30, an aqueous carbonate 822 stream, and water, which in some cases is recycled back into the system (802), sent to desalination facility (824), or both.

[0399] As will be appreciated, in various implementations the process/system 10 uses one or more additional inputs and may generate one or more additional outputs, In various implementations one or more ancillary inputs and/or outputs are largely recycled within the system. For example, in some cases an output from the electrochemical process 16 is processed (e.g., by reverse-osmosis) and provides low total dissolved solids (TDS) water (804), which can be used as a makeup liquid for the EDBM unit. In some cases an HCl make-up stream and/or NaOH make-up stream are also used to facilitate the EDBM unit.

[0400] As will be appreciated, additional inputs and/or outputs may be present in various implementations of the system 10, especially when the capture system 10 is integrated with another industrial process such as, for example, desalination. In various implementations the capture system/process 10 is configured to provide the following a number of outputs to a desalination facility. As shown in FIG. 42, examples include Low TDS water 818 collected upstream from the electrochemical process as a RO permeate (e.g., up to 50%) and sent to the desalination facility; dilute HCl 79 sent to the desalination facility for disinfectant and pH control; water 826 recovered from concentrating HCl; and an aqueous carbonate solution 822 separated in the centrifuge dryer and sent to the desalination facility for removing hardness and pH control.

[0401] In addition, in various implementations the system/process 10 is configured to receive and process CO.sub.2 emissions from the desalination facility, thus providing an efficient way of handling emissions.

[0402] The various implementations disclosed or contemplated herein relate to methods, systems, and devices allowing for the simultaneous capture and sequestration of CO.sub.2 from ambient air in an air contactor and that from industrial sources in a bubble column or sparger reactor, and mineral extraction from mined rock materials or from waste rock materials. In various implementations the combined process is closely integrated, with several interdependencies and synergies, leading to an efficient system wherein products are used interchangeably between them resulting in low carbon emissions, and reduced waste stream.

[0403] As described herein, the disclosed technologies will be referred to broadly as a system 10, though it is understood that this is for brevity and in no way intended to be limiting to any specific modality.

[0404] Certain implementations of the capture system 10 relate to the sequestration of CO.sub.2 and simultaneous extraction of metal and minerals from mined rock or waste rock materials using only saline water and electricity. In these implementations, electricity is applied to saline water via electrodialysis to create hydroxide-rich solvents which can be used to directly capture CO.sub.2 from the air. The electrodialysis process also creates a hydrogen-rich acid stream that can be used for dissolving mined or waste rocks and the subsequent metal or mineral extraction.

[0405] FIG. 43 depicts various synergies and interdependencies according to various implementations of a carbon capture and mineral extraction system 10. In the depicted implementation, a variety of optional steps are performed. For example, in various implementations the system includes a process having steps such as receiving an input liquid (box 100), performing an electrochemical reaction (box 310) to produce a hydroxide-rich solvent for the carbon capture process and a hydrogen-rich solvent for mineral extractions.

[0406] In various cases the hydroxide-rich solvent is passed through an air contactor or other similar medium to convert carbon dioxide from ambient air and industrial sources into carbonates (box 120). In some cases the hydrogen-rich solvent is mixed with fine rock powder (box 725) to dissolve the metals and minerals of interest. The fine rock powder is obtained from mined rock or rock waste (box 705) which is ground in a dry or a wet medium (box 715).

[0407] The dissolved metal and mineral compounds (box 380), such as metal chlorides obtained by mixing fine rock powder with hydrochloric acid, are mixed with carbonates to form metal and mineral carbonates (box 355) that are then precipitated out for storage on land or in water (box 340). In some cases the salt solution that is obtained from the reaction is recycled back to the front of the process (box 360).

[0408] As shown in FIGS. 44, in various implementations of a carbon capture system 70, coarse rock, obtained from a mine or from waste feed stream 730 is first ground to fine particles in a wet or a dry grinder 732 and then dissolved using a hydrogen-rich stream, such as hydrochloric acid 79, from the direct air capture system. The direct air capture system uses saline liquid as an input liquid 12 into the electrochemical process to form a hydroxide-rich stream 14 and a hydrogen-rich stream 79. The input liquid 12 is first pretreated 15 through nanofiltration and ion exchange to remove divalent ions such as calcium and magnesium.

[0409] The hydroxide-rich stream is used to remove carbon dioxide from ambient air and from industrial gases to form carbonates such as sodium carbonate and bicarbonates 72. The dissolved metal/mineral rock particles 734 are then mixed with the carbonates in a precipitator 20 to form mineral carbonates that are stored on land or in water and the salt solution 50 that remains in the precipitator is recycled back to the electrochemical step.

[0410] As described herein, it is understood that the capture system 10 comprises one or more fluidic connections (shown generally at the lines) between a variety of optional components that can be arranged in a wide variety of arrangements, such that the various fluids/gasses and electricity described herein are able to flow as described.

[0411] FIG. 45 is a flow chart providing a detailed depiction of a carbon capture process 10, according to one possible implementation. The detailed diagram depicts a number of vessels and other components of the system, in addition to fluid connections between relevant components. It will be appreciated that the system may include fewer and/or additional components and aspects that are not shown in various cases.

[0412] Continuing with FIG. 45, in various implementations, a capture system and method 10 receives an input liquid 12, such as, for example, sea water, which is then sent through a pretreatment stage. In the illustrated example, the pretreatment stage includes a nano-filtration unit (15A) and an ion exchange unit (15C) to remove divalent ions such as calcium and magnesium. The output of the pretreatment stage (e.g., filtrate) is then sent to an electrochemical processor 16.

[0413] In various implementations, the electrochemical processor 16 includes an electrodialysis bipolar membrane (EDBM-001). The EDBM unit is configured to split the input liquid salt stream into a hydroxide-rich stream (14) and a hydrogen-rich stream (79). The hydroxide-rich stream is then passed through an air contactor (22) wherein it absorbs carbon dioxide from an air stream (25) to form carbonates. These carbonates (72) are then pumped to a reactor (V-001) which absorbs CO.sub.2 from industrial gases (28) to form bicarbonates (stream 814). In various implementations the solid bicarbonate slurry (814) is separated in a centrifuge dryer (CG-001) into a solid carbonate/bicarbonate precipitant stream 30 and water, which in some cases is recycled back into the system (802).

[0414] In various implementations, the integration with mineral extraction makes use of the hydrogen-rich stream 79 (e.g., HCl) produced by the electrochemical processor 16. As shown in FIG. 45, the system/process 10 receives mineral rock 130A, which is crushed in a dry grinder (G-001) and then dissolved into the hydrogen-rich stream 79 in a leaching tank (V-003). The resulting mixture 830 is then sent to a precipitation vessel (V-003) and mixed with the carbonates and bicarbonates 30. The resulting mixture forms metal and mineral carbonates 832, which are then precipitated out for storage on land or in water.

[0415] As will be appreciated, additional inputs and/or outputs may be present in various implementations of the system 10.

Eight

[0416] As previously discussed, and also described herein with respect to FIGS. 46-50, the disclosed technologies are referred to broadly as a system 10, though it is understood that this is for brevity and in no way intended to be limiting to any specific modality.

[0417] Certain implementations of the capture system 10 relate to the sequestration of CO.sub.2 in the form of mineral carbonates, re-releasing the captured CO.sub.2 using hydrochloric acid from an electrochemical unit (e.g., electrolysis or electrodialysis unit), and combining the released CO.sub.2 with hydrogen produced from the electrochemical process to form methanol. In these implementations, electricity is applied to saline water via the electrochemical process to create hydroxide-rich solvents which can be used to directly capture CO.sub.2 from the air. The electrodialysis or electrolysis process also creates a hydrogen-rich and chlorine-rich solvent stream that can be used for re-releasing captured CO.sub.2 and its synthesis to methanol.

[0418] In certain other implementations of the capture system 10, hydrogenation is performed on the carbonates in the presence of a catalyst to form methanol. The energy used in the process is renewable energy resulting in green hydrogen which in turn results in green methanol production. Green methanol can be used for storing carbon dioxide in its form or further processed into other derivative green products.

[0419] FIG. 46 depicts various steps in the process of carbon capture and hydrogenation to methanol in various implementations of the capture system 10. In this implementation, the system comprises a process having steps such as receiving an input saline liquid (box 100) and passing the liquid through an electrochemical process (box 610) such as, for example, electrolysis or electrodialysis, to produce a hydroxide-rich solvent stream (box 110), such as sodium hydroxide. The process also includes using the solvent to capture CO.sub.2 (box 580) from ambient air as well as from an industrial source and precipitating the captured CO.sub.2 in the form of carbonates (box 130).

[0420] In various implementations the process 10 further includes using the electrochemical process at least in part to produce chlorine gas (box 140B) and hydrogen gas (box 140A). The process also includes neutralizing the carbonates with the hydrogen-rich stream, such as hydrochloric acid (box 160). The hydrochloric acid can be formed by combustion of the chlorine gas (box 140B) with the hydrogen gas (box 140A). If needed, CO.sub.2 re-released from the combustion can be hydrogenated with hydrogen from the electrochemical process in the presence of a catalyst for methanol synthesis (box 680). The process also includes storing methanol for sale and further production of derivative products (box 695). The neutralization of carbonates produces salt, such as sodium chloride, which is recycled back (box 690) to include with the input liquid 100.

[0421] FIG. 47 depicts various steps in the system's process of producing methanol using the carbon capture and hydrogenation steps forming part of the system 10. In this example mineral carbonates are hydrogenated directly to form methanol (box 685). The process also includes storing methanol for sale and further production of derivative products (box 695). Further, the system 10 produces chlorine-based byproducts such as, for example, chlorine gas and/or hydrochloric acid, which can be stored for subsequent sale (box 675).

[0422] As shown in FIG. 48, in one implementation of the system 10, an input liquid 12 such as seawater is pretreated and filtered to remove coarse particles 15 and passed into an electrochemical processor 16 (e.g., an electrolysis unit in the illustrated example) to produce a hydroxide-rich stream 14 containing salts such as NaOH and/or other hydroxides and byproduct gases such as hydrogen 16B and chlorine 16C. The byproduct gases can be combined in a combustion chamber 16D to produce a hydrogen-rich acid stream such as hydrochloric acid 16E. The hydroxide-rich stream is used to capture CO.sub.2 from ambient air in an air contactor 22 and from industrial gases 28 in a reactor 80 to form mineral carbonates. The mineral carbonates are then neutralized with hydrochloric acid in a mixer/bubbler 48 to re-release pure CO.sub.2 gas 52 and recycle the salt 50. In a methanol processing unit 124 the re-released CO.sub.2 52 is combined with the hydrogen gas 16B from the electrolysis unit to form methanol 125 at high temperatures and pressures in the presence of a catalyst in a chamber and is stored for sale or further processing 126.

[0423] In another implementation, as shown in FIG. 49, the carbonates are directly hydrogenated using hydrogen gas 16B for the synthesis 124 of methanol. The direct hydrogenation of carbonates is performed in presence of catalysts such as a ruthenium (Ru) catalyst and other chemicals including alcohols such as ethylene glycols to form methanol. The direct air capture of CO.sub.2 and methanol synthesis 124 can be performed in a single reactor. The byproduct, in this implementation, chlorine gas 16C, is stored in pressurized vessel for sale or further processing.

[0424] As described herein, it is understood that the capture system 10 comprises one or more fluidic and/or electrical connections (shown generally at the lines) between a variety of optional components that can be arranged in a wide variety of arrangements, such that the various fluids/gasses and electricity described herein are able to flow as described.

[0425] FIG. 50 is a flow chart providing a detailed depiction of a carbon capture process, according to one possible implementation. The detailed diagram depicts a number of vessels and other components of the system, in addition to fluid connections between relevant components. It will be appreciated that the system may include fewer and/or additional components and aspects that are not shown in various cases.

[0426] According to various implementations, the system 10 receives an input liquid 12, which in some cases is an artificial brine that is formed by mixing salt with water. The input liquid is fed to pretreatment system that in this case includes nano-filtration unit (15A) and an ion exchange unit (15C) to remove divalent ions such as calcium and magnesium. The filtrate output by the pretreatment stage is then sent to an electrochemical processor 16.

[0427] In various implementations the electrochemical processor is an electrolysis unit (EZ-001) wherein the salt and water solution is split into a hydroxide-rich stream (14), hydrogen gas stream (16B), and a chlorine gas stream (16C). A portion of the hydrogen gas (16B) and chlorine gas (16C) are combusted in an HCl oven (V-001) to form HCl (79). The hydroxide stream (14) is passed through air contactor 22 wherein the hydroxide combines with ambient CO.sub.2 to form a carbonate solution (72). The carbonate solution 72 is exposed to industrial CO.sub.2 (28) to form bicarbonates in a reactor (V-002). The bicarbonate solution (814) is mixed with the HCl (79) in a mixer/bubbler reactor (V-003) to release gaseous CO.sub.2 (52). The CO.sub.2 (52) and the H2 (16B) gases are then sent to a methanol reactor 840 for the synthesis of methanol 842.

[0428] In various implementations, the main inputs for the capture process and system 10 in FIG. 50 are the liquid input 12 (e.g., artificial brine in this example), air 25, and CO.sub.2 from industrial emissions. In various implementations, the main outputs are methanol 842, Cl.sub.2 gas 16C, and carbonate products 30.

[0429] In various implementations the process/system 10 in FIG. 50 uses one or more additional inputs and may generate one or more additional outputs. As just one possible example, in various implementations a regen stream 806 including, for example, some amount of HCl, is used to regenerate the ion exchange pretreatment stage 15C. As will be appreciated, additional inputs and/or outputs may be present in various implementations of the system 10.

[0430] Although the disclosure has been described with reference to preferred embodiments, persons skilled in the art will recognize that changes may be made in form and detail without departing from the spirit and scope of the disclosed apparatus, systems, and methods.