An apparatus includes a housing that defines a first zone, a second zone, a third zone, and a fourth zone. The apparatus includes an inlet, a first outlet, a second outlet, and a conveyor belt. The inlet is configured to receive a carbon dioxide-containing fluid in the first zone. The first outlet is configured to discharge a carbon dioxide-depleted fluid from the first zone. The second outlet is configured to discharge a carbon dioxide-rich fluid from the third zone. The conveyor belt passes through each of the zones. The conveyor belt includes a carbon dioxide sorbent. Within the first zone, the carbon dioxide sorbent is configured to adsorb carbon dioxide from the carbon dioxide-containing fluid to produce the carbon dioxide-depleted fluid. Within the third zone, the carbon dioxide sorbent is configured to desorb the captured carbon dioxide to produce the carbon dioxide-rich fluid.

The removal of acid gases (e.g., non-carbon dioxide acid gases) using sorbents that include salts in molten form, and related systems and methods, are generally described.

A system comprises a liquid desiccant regeneration system, a first air contactor stage, and a second air contactor stage. The regeneration system has a first stage with a first concentration output and first diluted output, and a second stage with a second concentration output, different from the first concentration output, and a second diluted output. The first air contactor stage is coupled to the first concentrated output to form a first output air stream having a reduced water content and a first diluted air contactor output. The second air contactor stage is coupled to the second concentrated output to form a second output air stream having a reduced water content and a second diluted air contactor output. Both diluted air contactor outputs are recirculated into the regeneration system, and the output air streams are combined.

A method for the removal of at least one contaminant from an aqueous liquor or a gas, comprising: preparing a solution or slurry of a solid alkali reagent by supplying a solid alkali reagent into a pre-wetting chamber via a feed pipe; supplying a liquid via two or more liquid sidestreams, each through a liquid inlet positioned on a side wall of the chamber to allow the liquid sidestreams to wash an internal wall of a frusto-conical section of the chamber and flow, preferably tangentially onto the internal wall in a downward spiraling manner thereby forming a vortex, towards a fluid outlet of the chamber and to further wet the solid alkali reagent with the supplied liquid thereby forming a pre-wetted reagent; and flowing a stream though a conduit, thereby creating a suction by the eductor to draw the pre-wetted reagent out of the chamber fluid outlet and mixing it with the stream to form a slurry or solution; and directing the slurry or solution exiting the eductor to an aqueous liquor or gas treatment unit, removing at least a portion of the contaminant from the aqueous liquor or gas in the treatment unit.

The disclosure provides seven integrated methods for the chemical sequestration of carbon dioxide (CO.sub.2), nitric oxide (NO), nitrogen dioxide (NO.sub.2) (collectively NO.sub.x, where x=1, 2) and sulfur dioxide (SO.sub.2) using closed loop technology. The methods recycle process reagents and mass balance consumable reagents that can be made using electrochemical separation of sodium chloride (NaCl) or potassium chloride (KCl). The technology applies to marine and terrestrial exhaust gas sources for CO.sub.2, NOx and SO.sub.2. The integrated technology combines compatible and green processes that capture and/or convert CO.sub.2, NOx and SO.sub.2 into compounds that enhance the environment, many with commercial value.

The removal of acid gases (e.g., non-carbon dioxide acid gases) using sorbents that include salts in molten form, and related systems and methods, are generally described.

Devices, systems and methods for capturing CO.sub.2 in a form that can be stored, processed, and/or converted to usable products is desirable. Systems capture CO.sub.2 using small scale, individual devices at a vast number of locations which, in the aggregate, are capable of significantly decreasing CO.sub.2 concentrations in the atmosphere on a global scale. When such small devices are placed in areas already occupied with a structure, i.e., office buildings, apartments, homes, automobiles and the like, though the amount of CO.sub.2 removal by each individual device may be relatively small, in the aggregate, significant amounts of CO.sub.2 may be removed at a more macro or even global scale.

The present development is a method for capturing and purifying CO.sub.2 from a flue gas stream using a metal aluminate nanowire absorbent and then regenerating the absorbent. After the CO.sub.2 is adsorbed into the absorbent, the adsorbent is regenerated by subjecting the CO.sub.2 saturated adsorbent to a dielectric barrier discharge plasma or to a microwave plasma or to a radio frequency (RF) plasma while ensuring that the external temperature does not exceed 200° C.

A method of scrubbing a gas, such as flue gas or exhaust gas, comprising carbon dioxide to deplete the gas of carbon dioxide (CO.sub.2), the method comprising the steps of: —scrubbing the gas in a scrubber (210) with a first alkaline, aqueous scrubbing liquid to dissolve carbon dioxide (CO.sub.2) as hydrogen carbonate (HCO.sub.3.sub.−) and/or as carbonate (CO.sub.32-) in the first alkaline, aqueous scrubbing liquid, thereby providing a first spent aqueous scrubbing liquid comprising hydrogen carbonate (HCO.sub.3—) and/or carbonate (CO.sub.32-), the first spent aqueous scrubbing liquid having a pH from about 7 to about 9; —feeding the first spent aqueous scrubbing liquid to an anode chamber of an electrolytic cell (310) comprising the anode chamber (313) and a cathode chamber (312) separated by a membrane (311); —regenerating the first spent aqueous scrubbing liquid in the electrolytic cell (310) by electrolysis, the electrolysis increasing the pH of the first spent aqueous scrubbing liquid in the cathode chamber (312), the electrolysis further depleting the first spent aqueous scrubbing liquid of hydrogen carbonate (HCO.sub.3—) and of carbonate (CO.sub.32-) in the anode chamber (313) by decreasing the pH, the regeneration further comprising generating gaseous hydrogen in the cathode chamber (312) and a gaseous mixture of oxygen and carbon dioxide (CO.sub.2) in the anode chamber (313) by electrolysis; and—withdrawing regenerated alkaline, aqueous scrubbing liquid from the cathode chamber (312) and re-circulating it to the scrubber (210); wherein: —the gaseous hydrogen is withdrawn from the cathode chamber (312); and—the gaseous mixture of oxygen and carbon dioxide is withdrawn from the anode chamber (313).

Solar thermal units and methods of operating solar thermal units for the conversion of solar insolation to thermal energy are provided. In some examples, solar thermal units have an inlet, and a split flow of heat absorbing fluid to either side of the solar thermal unit, along a first fluid flow path and a second fluid flow path. Optionally, one or more photovoltaic panels can be provided as part of the solar thermal unit, which may convert solar insolation to electric power that may be used by a system connected to the solar thermal unit.