Electro oxidation membrane evaporator 1 comprises sweep air handler 60; fluid tank 20 defining a fluid container; fluid contactor/separator 30; oxidation cell 40; and scrubber 80. Electro oxidation membrane evaporator 1 may allow higher percent water recovery from wastewater prior to delivering brine to a brine water recovery system and can allow O.sub.2 from air such as cabin air to continuously diffuse into the wastewater as O.sub.2 is consumed to generate oxidants, helping to eliminate the low oxidant environment at the end of the cycle that causes pH to remain high, and low pH prevents precipitates from forming for longer so more water can be evaporated from the wastewater.

This system for concentrating solvent-containing articles involves a first step in which: a supply flow (a) comprising solvent-containing articles containing a solute and a solvent (b) is caused to flow counter to or parallel with a permeant flow (d) through a forward osmosis membrane (o); the solvent (b) contained in the supply flow (a) is made to pass through the forward osmosis membrane (o) and to move into the permeant flow (d); and a concentrate flow (c) formed from the concentrated solvent-containing articles and a flow (e) formed from the diluted permeant flow (d) are obtained, wherein the permeant flow (d) is an inorganic salt solution containing multivalent cations, and the temperature of the permeant flow (d) in the aforementioned first step is 5-60 C.

Composite membrane tubing includes a porous scaffold support combined with polyether block amide copolymer. The composite membrane tubing has overlapping fusion areas that are an artifact of the manufacturing process. The methods of manufacturing above-mentioned composite membrane tubing have also been addressed. The composite membrane tubing can be reinforced with a structural mesh to further provide rigidity and strength. Composite membrane tubing or generally extruded tubing can be integrated into a multi-tube module for various applications.

The invention relates to the field of membrane gas separation. A method of removing components of gas mixtures which is based on passing the components of a gas mixture through a nanoporous membrane and subsequently selectively absorbing them with a liquid absorbent that is in contact with the nanoporous membrane, wherein to prevent the gas from getting into the liquid phase of the absorbent and the liquid phase of the absorbent from getting into the gas phase, a nanoporous membrane with homogeneous porosity (size distribution less than 50%) and a pore diameter in the range of 5-500 nm is used, and the pressure differential between the gas phase and the liquid absorbent is kept below the membrane bubble point pressure. An acid gas removal performance of more than 0.3 nm.sup.3/(m.sup.2 hour) in terms of CO.sub.2 is achieved at a hollow-fiber membrane packing density of up to 3200 m.sup.2/m.sup.3, which corresponds to a specific volumetric performance of acid gas removal of up to 1000 nm.sup.3 (m.sup.3 hour). The technical result is that of providing effective extraction of undesirable components from natural and process gas mixtures.

This document describes systems and methods for treating and recovering water from feed solutions using a membrane module that has a plurality of hollow fiber membranes encapsulated in a collection chamber and an expansion chamber that is connected to the outlet of the membrane module.

A heat and mass transfer system configured to be a passive system using gravitational force to form a thin liquid film flow on an outer surface of a flow distribution head and downstream conduit member to subject the thin liquid film to heat transfer mediums. The at least partially spherical flow distribution head creates a uniform thin flow of liquid on the outer surface increasing the efficiency of the heat and mass transfer system. The heat and mass transfer system may include a heat transfer medium supply system in fluid communication with internal aspects of the downstream conduit such that a heat transfer medium flows within the downstream conduit while the liquid film flows on the outer surface of the downstream conduit. Rather than conventional sheet flow on inner surfaces of a conduit, the flow distribution head enables sheet flow to be formed on an outside surface of a component.

A membrane evaporative condenser (MEC) includes a repeating sequence of channels for evaporation and/or condensation are arranged, each sequence of channels includes a condensation channel for condensation of a vapor to a liquid, an evaporation channel, and zero to one hundred evaporation-condensation channels. The condensation channel has walls of a non-permeable material which exterior to the condensation channel share the wall with a liquid evaporative medium (LEM) conduit that contains a LEM. The LEM conduit includes a moisture transfer membrane (MTM), where the LEM can evaporate into an evaporation channel or an evaporation-condensation channel that can amplify the effect of the heat transfer for additional mass transfer.

An air-impermeable water vapor transport membrane comprises an active layer on a microporous polymeric substrate. The active layer comprises a polyethylene-oxide containing copolymer and a polar protic solvent in an amount of about 3% to about 100% of copolymer weight in the active layer. Molecules of the protic solvent are bonded to the copolymer. The polar protic solvent reduces temperature-dependent variability in the water-vapor permeability of the membrane.

A system and method for processing unconditioned syngas first removes solids and semi-volatile organic compounds (SVOC), then removes volatile organic compounds (VOC), and then removes at least one sulfur containing compound from the syngas. Additional processing may be performed depending on such factors as the source of syngas being processed, the products, byproducts and intermediate products desired to be formed, captured or recycled and environmental considerations.

Disclosed are methods for dehydrating a water containing source of formaldehyde in which water is separated from the water containing source of formaldehyde using a zeolite membrane. In certain aspects, the water containing source of formaldehyde includes a separation enhancer having a relative static permittivity ranging from 2.5 to 20, and the water containing source of formaldehyde may further include methanol. In certain aspects, (meth)acrylic acid alkyl ester may be produced using the dehydrated source of formaldehyde.