A tank for accumulating oxygen enriched air from an oxygen concentration device is disclosed. The oxygen concentration device includes a canister including a nitrogen-adsorbent material. A compressor is coupled to the canister. The compressor compresses air for the canister to produce oxygen enriched air in a swing adsorption process. The tank includes a closed container for collecting oxygen enriched air produced in the canister. An inlet is coupled to the container. An outlet in the container allows a patient to inhale the collected oxygen enriched air. An adsorbent material within the container adsorbs oxygen enriched air added to the tank from the canister.

Structured adsorbent beds comprising a high cell density substrate, such as greater than about 1040 cpsi, and a coating comprising adsorbent particles, such as DDR and a binder, such as SiO.sub.2 are provided herein. Methods of preparing the structured adsorbent bed and gas separation processes using the structured adsorbent bed are also provided herein.

A monolithic open cell structure apparatus including an open cell structure housing including a first side, a second side opposite the first side, a first opening located at the first side, and a second opening located opposite the first opening at a second side. The monolithic open cell structure apparatus also including a filtration portion extending from the first side to the second side within the open cell structure housing. The monolithic open cell structure apparatus further including a retaining partition that at least partially encloses the filtration portion within the open cell structure housing. The monolithic open cell structure apparatus is a single piece including a unitary structure.

A system and a method for continuously separating carbon dioxide from gas mixtures, utilizing a continuous loop of porous monoliths which support a sorbent within its pores. Continuously exposing a portion of the continuous loop of monoliths to a flow of gas mixture containing a minor proportion of carbon dioxide, to adsorb carbon dioxide from the flow. The loop passes through a sealed regeneration and carbon dioxide capture assembly located astride a portion of the loop, and which is capable of sealingly containing a monolith in relative movement through the assembly. The assembly chamber comprises a plurality of separately sealed zones, including at least one zone for purging oxygen from the monoliths, -a subsequent zone for heating the monolith to release the adsorbed carbon dioxide, and another cooling zone for cooling the monolith prior to reentering the adsorption portion of the loop where it is exposed to oxygen.

Provided is a method for manufacturing a polymer fiber adsorbent having an MOF uniformly distributed in the matrix thereof, the method comprising the steps of: spinning a spinning dope comprising a polymer matrix and a metal precursor of an MOF to prepare a polymer fiber adsorbent precursor comprising the metal precursor; and contacting the polymer fiber adsorbent precursor with an organic ligand of the MOF to form an MOF in the polymer fiber adsorbent precursor. A polymer fiber adsorbent manufacturing method provided by an aspect of the present invention offers a method capable of easy synthesis of an MOF which is sensitive to water, thereby obtaining a polymer fiber adsorbent excellent in terms of adsorption performance and long-term stability.

Contactor structures are provided that can allow for improved heat management while reducing or minimizing the potential for contamination of process gas streams with heat transfer fluids. The contactor structures can include one or more sets of flow channels for process gas flows, such as gas flows introduced to allow adsorption of components from a gas stream or gas flows introduced to facilitate desorption of previously adsorbed components into a purge gas stream. The process gas flow channels can correspond to flow channels defined by a structural material of unitary structure. The unitary structure can correspond to the entire contactor, or the unitary structure can correspond to a monolith that forms a portion of the contactor. The contactor structures can also include one or more sets of flow channels for heat transfer fluids. The heat transfer flow channels can also be defined by the structural material of a unitary structure.

Described are boron oxide-containing adsorbents that include porous adsorbent base and boron oxide on surfaces of the base, as well as devices that include the boron oxide-containing adsorbent, and related methods of preparing and using the boron oxide-containing adsorbent.

The invention generally relates to a process for purifying a hydrogen gas for use in a fuel cell. The process involves taking a hydrogen feed stream from a high-pressure tank and passing it through a purifier comprising an adsorbent to provide a purified hydrogen stream which is sent to a fuel cell. A particular adsorbent which can be used is a metal-organic framework composition. The adsorbent can be housed in a device such as a canister or cartridge having an inlet and outlet port.

An adsorption device for compressed gas, is provided with a vessel with an inlet for the supply of a compressed gas to be treated, and an outlet for treated gas and an adsorption element is affixed in the vessel. The adsorption element extends along the flow direction of the compressed gas to be treated, between the inlet and the outlet. The adsorption element has a monolithic supporting structure that is at least partially provided with a coating that contains an adsorbent.

The present disclosure relates to hydrocarbon emission control systems. More specifically, the present disclosure relates to substrates coated with hydrocarbon adsorptive coating compositions and evaporative emission control systems for controlling evaporative emissions of hydrocarbons from motor vehicle engines and fuel systems. The hydrocarbon adsorptive coating compositions include particulate carbon having a BET surface area of at least about 1300 m.sup.2/g, and at least one of (i) a butane affinity of greater than 60% at 5% butane; (ii) a butane affinity of greater than 35% at 0.5% butane; (iii) a micropore volume greater than about 0.2 mug and a mesopore volume greater than about 0.5 ml/g.