Embodiments of methods and associate system for removing acid gas from a sour gas stream are provided. The method includes (1) passing the sour gas stream in a counter-flow arrangement with an encapsulated phase change material and a lean amine based sorbent liquid configured to absorb the acid gas from the sour gas stream in an absorber; (2) separating the rich amine based sorbent liquid and the encapsulated phase change material; (3) passing the rich amine based sorbent liquid to an amine regenerator wherein the rich amine based sorbent liquid is heated to release the absorbed sour gas and regenerate the lean amine based sorbent liquid; and (4) passing the encapsulated phase change material and the regenerated lean amine based sorbent liquid through a cooler to reduce the temperature of the encapsulated phase change material such that the phase change material in the encapsulated phase change material solidifies.

Embodiments of methods and associate system for removing acid gas from a sour gas stream are provided. The method includes (1) passing the sour gas stream in a counter-flow arrangement with an encapsulated phase change material and a lean amine based sorbent liquid configured to absorb the acid gas from the sour gas stream in an absorber; (2) separating the rich amine based sorbent liquid and the encapsulated phase change material; (3) passing the rich amine based sorbent liquid to an amine regenerator wherein the rich amine based sorbent liquid is heated to release the absorbed sour gas and regenerate the lean amine based sorbent liquid; and (4) passing the encapsulated phase change material and the regenerated lean amine based sorbent liquid through a cooler to reduce the temperature of the encapsulated phase change material such that the phase change material in the encapsulated phase change material solidifies.

In one embodiment, a carbon dioxide capturing system includes an absorber to absorb CO2 from first gas into lean liquid, and produce rich liquid that is the lean liquid absorbing the CO2 and second gas that is the first gas removing the CO2, and a regenerator to separate third gas including the CO2 from the rich liquid flowing from the absorber, and provide the lean liquid and the third gas. The system further includes a flowmeter to measure a flow rate of the third gas, a liquid level gauge to measure a liquid level of the lean liquid and/or the rich liquid, and a controller to regulate a quantity of heat energy supplied to the regenerator based on the flow rate of the third gas, and regulate a total amount of the lean liquid and the rich liquid in the system based on the liquid level.

A sulfur dioxide absorbent that is an ionic liquid including a solvent; and a salt of a diamine compound that is substituted with a hydroxyl group and has a chemical formula 1 to 3 below dissolved in the solvent: ##STR00001## where, in Chemical Formula 1 and 2, R.sub.1-R.sub.4 are the same or different and each is independently selected from the group consisting of H, a C1-C6 alkyl, and a C1-C6 alkoxy; and where, in Chemical Formula 1 to 3, X is selected from the group consisting of Cl, Br, I, MeSO.sub.3, CF.sub.3SO.sub.3, HCO.sub.2, CF.sub.3CO.sub.2 and CH.sub.3CO.sub.2; and n is an integer of 1-10. The sulfur dioxide absorbent is constituted to selectively absorb sulfur dioxide and sulfurous acid (H.sub.2SO.sub.3) formed by combination of sulfur dioxide with water, not CO.sub.2.

A packing device for mass and heat transfer with a subject fluid includes a housing having opposing ends, and subject fluid openings at each opposing end defining a subject fluid flow path for at least one subject fluid flowing through the packing device. A plurality of mass and heat transfer plates each include an interior heat exchange fluid channel disposed between interior heat transfer surfaces of the mass and heat transfer plates. A heat exchange fluid inlet and fluid outlet can supply and remove heat exchange fluid to the heat exchange fluid channels of the mass and heat transfer plates. The mass and heat transfer plates can be oriented to define there between fluid flow channels for the subject fluid. A method and system for mass and heat transfer with a subject fluid, and a method and system for the removal of CO.sub.2 from a gas stream are disclosed.

A system and a process for capturing Carbon Dioxide (CO.sub.2) from flue gases are disclosed. The process comprises feeding a flue gas comprising CO.sub.2 to at least one Rotary Packed Bed (RPB) absorber rotating circularly. A solvent may be provided through an inner radius of the RPB absorber. The solvent may move towards an outer radius of the RPB absorber. The solvent may react with the flue gas in a counter-current flow. The process further includes passing the flue gas through at least one of a water wash and an acid wash to remove traces of the solvent present in the flue gas. Finally, the solvent reacted with the CO.sub.2 may be thermally regenerated for re-utilizing the solvent back in the process.

Disclosed herein is a rotating packed bed, RPB, for mass transfer between a sorbent and a gas, the RPB comprising: a central chamber arranged to receive a flow of a sorbent that is a liquid; and a flow path for the sorbent between the central chamber and a region for mass transfer between a gas and the sorbent; wherein, in use, the flow of sorbent through the region for mass transfer is substantially in cross-flow with the flow of gas through the region for mass transfer. Advantageously, mass transfer between a liquid sorbent and a gas is improved.

An absorbent liquid which absorbs at least one of CO.sub.2 and H.sub.2S from a gas, including a secondary linear monoamine; a tertiary linear monoamine or a sterically hindered primary monoamine; and a secondary cyclic diamine, wherein a concentration of each of the secondary linear monoamine, the tertiary linear monoamine or the sterically hindered primary monoamine; and the secondary cyclic diamine is less than 30% by weight.

A system for processing a gas stream can include a physical solvent unit, an acid gas removal unit upstream or downstream of the physical solvent unit, and an LNG liquefaction unit downstream of the acid gas removal unit. The physical solvent unit is configured to receive a feed gas, remove at least a portion of any C.sub.5+ hydrocarbons in the feed gas stream using a physical solvent, and produce a cleaned gas stream comprising the feed gas stream with the portion of the C.sub.5+ hydrocarbons removed. The acid gas removal unit is configured to receive the cleaned gas stream, remove at least a portion of any acid gases present in the cleaned gas stream, and produce a treated gas stream. The LNG liquefaction unit is configured to receive the treated gas stream and liquefy at least a portion of the hydrocarbons in the treated gas stream.

A system and method for removing one or more predetermined gases from an environment is herein disclosed. An embodiment of the system and method will now be described. A means for conveying a fluid and a means for flowing the fluid is combined with adsorber and desorber sections. The fluid flows in the means for conveying the fluid by the means for flowing the fluid. Comparably, the fluid flows in the adsorber and desorber sections not by the means for flowing the fluid, but rather by capillary action. In the adsorber section, the environment is in direct contact with the fluid. The fluid is capable for adsorbing one or more gases from the environment. The fluid exits the adsorber section and subsequently flows into the desorber section. The desorber section is self-contained wherein an inner portion of the desorber section is not in direct contact with the environment. In the desorber section, the one or more gases are desorbed from the fluid into the inner portion of the desorber section. In an embodiment, the one or more gases exit the desorber section and the system as a whole.