A liquid air energy storage system comprises an air liquefier, a storage facility for storing the liquefied air, and a power recovery unit coupled to the storage facility. The air liquefier comprises an air input, an adsorption air purification unit for purifying the input air, and a cold box for liquefying the purified air. The power recovery unit comprises a pump for pressurising the liquefied air from the liquid air storage facility, an evaporator for transforming the high-pressure liquefied air into high-pressure gaseous air, an expansion turbine capable of being driven by the high-pressure gaseous air, a generator for generating electricity from the expansion turbine, and an exhaust for exhausting low-pressure gaseous air from the expansion turbine. The exhaust is coupled to the adsorption air purification unit such that at least a portion of the exhausted low-pressure gaseous air is usable to regenerate the adsorption air purification unit.

A device for drying compressed gas with an inlet for compressed gas to be dried originating from a compressor and an outlet for dried compressed gas, whereby this device comprises a number of vessels that are filled with a regeneratable drying agent and a controllable valve system that connects the aforementioned inlet and outlet to the aforementioned vessels, wherein the device comprises at least three vessels, whereby the aforementioned valve system is such that at least one vessel is always being regenerated, while the other vessels dry the compressed gas, whereby due to the control of the valve system the vessels are each successively regenerated in turn.

Disclosed herein are rapid cycle pressure swing adsorption (PSA) process for separating O.sub.2 from N.sub.2 and/or Ar. The processes use a carbon molecular sieve (CMS) adsorbent having an O.sub.2/N.sub.2 and/or O.sub.2/Ar kinetic selectivity of at least 5 and an O.sub.2 adsorption rate (1/s) of at least 0.2000 as determined by linear driving force model at 1 atma and 86 F.

Methods and systems for removing water vapor from a feed gas prior to further processing the feed gas according to a downstream PSA process are described. The feed gas can include CO.sub.2 and/or CO and/or H.sub.2 and the PSA process can be used to separate components of the feed gas from one another, for instance, for CO.sub.2 capture. Light product off of the PSA process is utilized to regenerate desiccant of a dryer used in the water vapor removal process that is carried out prior to the feed gas entering the PSA process. The water vapor removal process can be heated by providing thermal energy directly to the dryer and/or to a regenerating stream that regenerates the desiccant of the dryer. The thermal energy can be low cost energyfor instance, waste heat off of a system that provides the feed gas.

An activated carbon device for adsorbing solvent from a flow of air is regenerated by feeding heated inert gas to the activated carbon and by applying a reduced pressure to the heated activated carbon.

A carbon capture system can include a plurality of CO.sub.2 thermal swing adsorption (TSA) beds. The plurality of CO.sub.2 TSA beds can include at least a first TSA bed, a second TSA bed, and a third TSA bed configured to capture CO.sub.2 within a capture temperature range and to regenerate the captured CO.sub.2 at a regeneration temperature range above the capture temperature range. The carbon capture system can include a plurality of valves and associated flow paths configured to allow switching operational modes of each of the first, second, and third TSA beds.

The present disclosure provides a method for a mobile pressure swing adsorption oxygen production device, comprising a first PSA section, a second PSA section and a third PSA section which are operated in series; the first PSA section adsorbs oxygen in raw air by a velocity-selective adsorbent; the second PSA section adsorbs nitrogen etc. in desorption gas of the first PSA section by a nitrogen balance-selective adsorbent; the third PSA section removes nitrogen from oxygen-rich gas flowing out of the second PSA section; the first PSA section sequentially undergoes at least adsorption A and vacuumizing VC in one cycle; the second PSA section sequentially undergoes at least adsorption A, pressure-equalizing drop ED, backward discharge BD and pressure-equalizing rise ER; and the third PSA section sequentially undergoes at least adsorption A, pressure-equalizing drop ED, backward discharge BD and pressure-equalizing rise ER.

A hydrogen production apparatus including a desulfurizer, a reformer, a CO transformer a gas flow path, and a purge gas supply path which is provided where a purge gas is supplied to an upstream side of a pressure feeding apparatus in the gas flow path, prior to a stopping operation, a purging step of replacing gas within the gas flow path with the purge gas and filling the purge gas into the gas flow path is performed, and in a start-up operation in which a heating means is operated to increase the temperature of the gas within the gas flow path, which is performed prior to a hydrogen purification operation, a pressure increasing step of supplying the purge gas from the purge gas supply path to the closed circulation circuit and increasing the pressure within the closed circulation circuit is performed.

Systems and processes for use of concentric adsorbent beds with rotary valve assemblies are provided.

Biogas containing H.sub.2S and CO.sub.2 is upgraded by removing H.sub.2S using PTSA and CO.sub.2 using two stages of gas separation membranes. The first stage permeate may optionally be used a regeneration gas stream. The second stage permeate may optionally be used a cool down gas stream. The PTSA unit includes two or more adsorbent beds each selective for water, VOCs, and H.sub.2S over CO.sub.2 and for H.sub.2S over methane.