A hollow fiber membrane module includes: a tubular case; a hollow fiber membrane bundle; and a pair of sealing and fixing portions, in which an outside-membrane channel that passes by an outer wall of each of the hollow fiber membranes and an inside-membrane channel that passes through the hollow inside of each of the hollow fiber membranes are formed, moist air flows through the outside-membrane channel, and dry air flows through the inside-membrane channel, whereby moisture in the moist air is supplied to the dry air by a membrane separation effect of the hollow fiber membranes, wherein a plurality of spaces are disposed between the case inner wall and the hollow fiber membrane bundle, and a restriction portion that restricts the hollow fiber membrane from entering into the spaces is partially disposed between the hollow fiber membrane bundle and each of the spaces.

The present invention is directed to a method of capturing CO2 from a FCC regenerator using select membranes.

A facility and a process with four membrane separation units, where the second separation unit separates the retentate of the first unit, the third separation unit separates the permeate of the first unit, the fourth separation unit separates the retentate of the third unit, the permeate of the second unit and the retentate of the fourth unit are recycled to the feed to the first unit, the permeate of the fourth unit is passed to a methane oxidation unit and the permeate of the third unit is discharged to the atmosphere allows separating methane and carbon dioxide from a gas stream, providing a methane rich stream with the retentate of the second unit at a high methane yield and adhering to low limits for methane discharge to the atmosphere with a small size methane oxidation unit.

A gas separation membrane includes a composite membrane, the composite membrane including: a gas separation functional layer; and a compound having a composition different from a compound constituting the gas separation functional layer, wherein the presence ratio of the gas separation functional layer at at least one surface of the gas separation membrane is not less than 90% and less than 100%. Provided is a gas separation membrane capable of suppressing damage of the gas separation functional layer during the preparation process of a gas separation membrane module or during the use of a gas separation membrane module even when the gas separation functional layer includes a site having low strength.

A regenerable organic contaminant controller includes a carbon hollow fiber module that includes a passage between an inlet and an outlet, on an opposite end of the carbon hollow fiber module from the inlet, such that organic contaminants in contaminated air flowing through the passage are desorbed into pores of the carbon hollow fiber module. The regenerable organic contaminant controller also includes wires coupled to the inlet of the carbon hollow fiber module and to the outlet of the carbon hollow fiber module. The wires heat the carbon hollow fiber module based on a flow of electricity through the wires. The heat causes release of the organic contaminants from the pores of the carbon hollow fiber module.

An active CO.sub.2 capture unit for capturing CO.sub.2 from a dilute source of CO.sub.2 input gas can include an inlet through which an input gas is introduced into the unit and a non-aqueous region comprising a non-aqueous CO.sub.2 binding organic liquid containing OH.sup.− arranged to be in contact with the input gas to chemisorb CO.sub.2 from the input gas and convert the chemisorbed CO.sub.2 into HCO.sub.3.sup.− by reacting with OH.sup.−. The unit also includes an aqueous region arranged downstream of the non-aqueous region, wherein at an aqueous region interface, the HCO.sub.3.sup.− interacts with H.sub.2O and decomposes to CO.sub.2 and CO.sub.3.sup.2−. An anion exchange membrane is disposed between the non-aqueous region and the aqueous region to facilitate HCO.sub.3.sup.− diffusion and migration from the non-aqueous region to the aqueous region. A captured CO.sub.2 outlet is disposed downstream of the aqueous region.

An inerting system comprises an air separating device having an enclosure (40) having at least one air inlet (46) and one outlet (48) for oxygen-depleted air. The air separating device (18) is configured to generate, from an air inlet flow coming from the air inlet (46) of the enclosure (40), an outlet flow of oxygen-depleted air and to discharge the outlet flow of oxygen-depleted air through the outlet (48) for oxygen-depleted air. The inerting system (14) comprises a heating system (20), outside the enclosure (40), configured to heat at least one region of the enclosure (40).

Combustion systems are provided that can include a combustion assembly operatively engaged with an air intake, wherein the air intake performs air enrichment.

Methods for enriching air to a combustion assembly are also provided. The methods can include: forming an N.sub.2-rich stream and an O.sub.2-rich stream from a first air stream; supplementing a second air stream with the O.sub.2-rich stream to enrich the second air stream with O.sub.2; and combusting the enriched air stream.

Systems for separating CO.sub.2 from flue gas are also provided. The systems can include a vortex tube assembly operably coupled to a component of the system that provides pressurized N.sub.2.

Methods for heating or cooling components of a system for separating CO.sub.2 from flue gas are also provided. The methods can include: providing compressed nitrogen from one or more components of the system to a vortex tube to form a heated nitrogen stream and cooled nitrogen stream; providing the heated nitrogen stream to components benefiting from a heat source; and providing the cooled nitrogen stream to components benefiting from a cooling source.

Systems for separating CO.sub.2 from flue gas can also include a separation assembly that includes a membrane assembly configured to separate CO.sub.2 from N.sub.2.

Methods for separating CO.sub.2 from flue gas can also include providing a flue gas stream comprising CO.sub.2 and N.sub.2 to a first membrane separation system to form a CO.sub.2-rich stream and an N.sub.2-rich stream.

A fuel gauging system for a fuel tank containing fuel and an ullage gas in an ullage of the tank. The fuel gauging system pressurizes/depressurizes the ullage gas and measures changes in conditions of the ullage gas to determine ullage gas volume and thus volume of the fuel. The system may infer one or more values in the volume calculation to reduce the number of measurements involved. The inferred values may come from known operating characteristics of an inerting system integrated with the fuel gauging system. The system may use a control valve that operates within the limits of a climb-dive valve to generate the system response. The control valve may control delivering or receiving ullage gas from another tank to preserve the ullage gas. An inerting system may be integrated into such a paired-tank fuel gauging system.

The present invention relates to a process for the production of asymmetric cellulose hollow fibres and the use of such fibres in the production of asymmetric carbon hollow fibre membranes (CHFMs). In particular, the present invention provides a facile and scalable process for the preparation of asymmetric CHFMs by direct pyrolysis of polymeric precursors without the need for complex pre-pyrolysis treatment steps to prevent pore collapse. The present invention also relates to the use of asymmetric CHFMs prepared according to said process in the separation of hydrogen gas from a mixed gas source, especially in the separation of hydrogen from CO.sub.2 in the steam-methane reforming reaction.