A biogas upgrading system can include a multiple stage membrane system that is configured to remove oxygen so that the biogas is upgraded to have a higher concentration of methane, a pre-selected oxygen (O.sub.2) concentration (e.g. less than or equal to 0.2 mol %, etc.), and a pre-selected carbon dioxide (CO.sub.2) concentration (e.g. less than or equal to 5 mol %, etc.). The membrane system can be configured to reject O.sub.2 by utilizing a low CO.sub.2/O.sub.2 selectivity that is within a pre-determined range (e.g. less than 5 or less than 4.5). In some embodiments, the upgraded biogas that is output from the system can be entirely made up of methane, carbon dioxide, and oxygen. In other embodiments, the biogas can be almost entirely composed of these components along with a small amount of nitrogen and a trace amount (e.g. less than or equal to 0.2%-0.1%, etc.) of other components.

Separating oxygen from a gas includes contacting an oxygen-selective sorbent with a gas stream, adsorbing oxygen in the gas stream with the sorbent, heating the sorbent to greater than 400° C., and desorbing a majority of the oxygen. The sorbent is selective for oxygen, and adsorbing occurs at a temperature between 275-325° C. An oxygen separation system includes a sorption bed, a heater configured to heat the sorption bed, an oxygen analyzer, a first conduit configured provide an input gas to the sorption bed, a second conduit configured to provide processed input gas from the sorption bed to the oxygen analyzer, a third conduit configured to provide a purge gas to the sorption bed, and a fourth conduit configured to provide processed purge gas to the oxygen analyzer. The first and third conduits are configured to flow the input gas and the purge gas flow in opposite directions through the sorption bed.

A double fluidized bed reactor system including a staircase-type helical blade is proposed. The system includes a bubbling fluidized bed gasification furnace for receiving fuel (for example, combustible waste and biomass) and steam, forming a bubbling fluidized bed through a flow of flow medium therein, and gasifying the fuel, thereby generating a resultant gas, and a high-speed fluidized bed combustion furnace for receiving char of the resultant gas and the flow medium from the bubbling fluidized bed gasification furnace, additionally receiving air, combusting the char so as to heat the flow medium, and transferring the heated flow medium back to the bubbling fluidized bed gasification furnace.

A receptacle is designed for a chamber for an active substance. The receptacle includes two main elements. A first element is a transverse wall with a first main side facing an interior of the chamber, and a peripheral wall formed with the first main side of the transverse wall. A second element includes a bottom wall and a sheath extending from the bottom wall. The peripheral wall and the sheath surround one another and are in contact with each other so that the chamber is formed between the bottom wall, the transverse wall, the peripheral wall and/or the sheath. At least one ventilation groove is provided between the peripheral wall and the sheath form a ventilation channel connecting the chamber with the outside atmosphere.

A receptacle forming a chamber partially filled with an active substance, wherein the receptacle is a body and a cap which closes the body. The cap includes a top wall with a first main side facing an interior of the chamber and a skirt formed with the first main side of the top wall. The body includes a bottom wall and a sidewall. The skirt and the sidewall surround one another in contact with each other. The walls surrounding the chamber include the bottom wall, the top wall and either the skirt or the sidewall. At least one ventilation path is provided between the skirt and the sidewall, such that the ventilation path connects the chamber with the outside atmosphere.

A method is provided for operating an active controlled atmosphere (CA) system to regulate the atmosphere in a cargo storage space. The controlled atmosphere system comprises: a plurality of gas exchange modules, each being operable to vary the level of a respective component gas in the cargo storage space, and/or at least one gas exchange module operable in a plurality of different modes to vary the level of a respective component gas in the cargo storage space; and a control module configured to control operation of each gas exchange module according to a plurality of different predetermined atmospheric control logics. Each atmospheric control logic defines operational gas exchange modules and/or operational modes for use over respective operational ranges of atmospheric conditions, and each atmospheric control logic is configured to cause operation of a different combination of gas exchange modules and/or modes over a comparable operational range, independently of any setpoints for gas component levels. The method comprises: the control module selecting an operational atmospheric control logic from the plurality of different predetermined atmospheric control logics for atmospheric control of the cargo storage space; and the control module controlling operation of each gas exchange module dependent on the selected operational atmospheric control logic to regulate the atmosphere in the cargo storage space.

The present invention relates to an adsorption process for xenon recovery from a cryogenic liquid or gas stream wherein a bed of adsorbent is contacted with a xenon-containing liquid or gas stream selectively adsorbing the xenon from said stream. The adsorption bed is operated to at least near full breakthrough with xenon to enable a deep rejection of other stream components, prior to regeneration using the temperature swing method. After the stripping step, the xenon adsorbent bed is drained to clear out the liquid residue left in the nonselective void space and the xenon molecules in those void spaces is recycled upstream to the ASU distillation column for increasing xenon recovery. The xenon adsorbent bed is optionally purged with oxygen, followed by purging with gaseous argon at cryogenic temperature (≤160 K) to displace the oxygen co-adsorbed on the AgX adsorbent due to higher selectivity of argon over oxygen on the AgX adsorbent. By the end of this step, the xenon adsorbent bed is filled with argon and xenon. Then the entire adsorbent bed is heated indirectly without utilizing any of the purge gas for direct heating. Operating the adsorption bed to near full breakthrough with xenon and displacing the adsorbed oxygen and other residues with argon, prior to regeneration, along with indirect heating of the bed, enables production of a high purity product ≥40 vol % xenon from the adsorption bed and further enables safely heating without any purge gas and ease for downstream product collection, even in cases where hydrocarbons are co-present in the feed stream.

The invention discloses a food container for preserving freshness of food, comprising a container body having a cavity adapted for containing food items; a lid detachably secured on the container body to close the cavity of the container; and one or more food preserving elements capable of absorbing food spoiling gas to preserve freshness of the food items. The one or more food preserving elements are disposed inside the cavity and/or into a material of the food container to preserve the food items for an extended period of time and remove odors.

Provided herein is a gas exchange composite membrane and methods of making the same. The gas exchange composite membrane may find use in a method of exchanging gas with blood in a subject in need of blood oxygenation support, which method is also disclosed. Also provided herein are systems and kits that find use in performing the methods of exchanging gas with blood.

Processes for reducing carbon monoxide levels in a carbon dioxide rich gaseous stream. The carbon dioxide rich stream is passed to a preferential oxidation zone to selectively convert carbon monoxide to carbon dioxide. Excess oxygen is consumed by reacting with hydrogen, which may be added or controlled based on PSA operating conditions upstream of the preferential oxidation zone. The preferential oxidation zone may be contained within a bed of a dryer.