An air channel membrane distiller (1) comprises a hot surface (12), a cooling section (20) and a hydrophobic membrane (30). The hot surface and the hydrophobic membrane define a sealed evaporation channel (40). A surface (22) of the cooling section and the hydrophobic membrane define a sealed condensation channel (50). A water supply tubing (42) is connected to the evaporation channel. A water discharge tubing (46) is connected to the evaporation channel. A purified-water discharge tubing (56) is connected to the condensation channel. The surface of the cooling section is given a temperature lower than a temperature of water in the evaporation channel. A gas supply arrangement (60) for inert gas comprises a heater (62). A gas pipe system (64) is arranged to a gas inlet (55) of the condensation channel for enabling flushing of at least the condensation channel with the inert gas.

A nonwoven web obtained by electrospinning, suitable for the filtration of nano- and/or submicron aerosols, including a multiplicity of fibers of composition C1, the composition C1 including at least 50% by weight of at least one polymer P1 based on the repeat unit resulting from vinylidene fluoride (VDF), the fibers of composition C1 having a degree of crystallinity in polar phase(s), preferentially in solely beta phase, of at least 65% by weight, with respect to their total weight. Also, a process for the manufacture of the web, to a membrane including the web and also to a process for the washing/sterilization of the web or of the membrane.

A hydrophilic graphitic material is provided that may be formed by heating a graphitic material to a temperature between about 150° C. to about 1400° C. for an extended period of time under an inert atmosphere. Annealing CNT film at 500 to 1400 removes amorphous carbon to produce purified CNT film. The purified CNT film can be further densified with the treatment of alkylphosphonic acid or alkyldiphophonic acid and heating to produce a hydrophilic, densified CNT film which is mechanically robust and does not adhere to other solid surfaces. These films can be used as filtration membranes with superior membrane fouling resistance among other uses.

A system for and method of cleaning polymeric and ceramic microfiltration and ultrafiltration membranes in hollow fiber, flat sheet, and tubular membrane units is provided. The method includes using a reducing agent, specifically ascorbic acid, based formulation. The method also includes certain protocols useful in conducting such cleanings. The system includes features for facilitating the method of the present invention.

A ceramic separation membrane structure in which a zeolite separation membrane formed on a ceramic porous body is repaired, and a repair method thereof. In the ceramic separation membrane structure, a zeolite separation membrane is disposed on a ceramic porous body, and defects of the zeolite separation membrane are repaired by zeolite repaired portions containing zeolite of structure different from the structure of zeolite of the zeolite separation membrane. The zeolite separation membrane and the zeolite repaired portions are made of a hydrophobic zeolite having a ratio of SiO.sub.2/Al.sub.2O.sub.3=100 or more.

Methods of cleaning and sanitizing membrane modules within a membrane system are provided. A cleaning solution is circulated through the membrane system for about 2 to about 30 minutes. The cleaning solution includes organic acid and surfactant. A sanitizing solution is added to the cleaning solution to produce a boosted antimicrobial solution comprising an oxidizer. The boosted antimicrobial solution is then circulated through the membrane system for about 1 to about 20 minutes. The methods described are effective for reducing and removing bacterial spores and biofilms from membranes and improving membrane compatibility of effective cleaning and sanitizing solutions.

A process for the regeneration of a membrane wall in a distillation apparatus, wherein a distillation apparatus having one or more evaporation and condensation stages is provided, each evaporation and condensation stage having at least one flow channel conducting a liquid, said flow channel being at least partially confined by a vapor-permeable and liquid-impermeable membrane wall, wherein vapor emerging from the liquid passes through the membrane wall. The liquid is removed from the at least one flow channel, wherein, after the removal of the liquid, the membrane wall is surrounded on both sides by a gas atmosphere, but is still wetted with liquid, and this liquid is removed by adjusting the gas atmosphere surrounding the membrane wall such that the partial pressure of the liquid in the gas atmosphere is lower than the vapor pressure of the liquid wetting the membrane wall.

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.

A disposable filtration device includes a plurality of disposable filter capsules connected with each other by lines, which are carried by a rigid holder. At least the holder and the lines between the filter capsules preferably are formed of a sterilizable material, so that the filtration device can be sterilized in the pre-mounted, i.e. ready-to-connect condition, and can be packed and transported without a risk of damage.

A membrane heat treatment method includes a process of raising the temperature of a membrane to an intermediate heating temperature (step S21), a process of heating and keeping the membrane at the intermediate heating temperature (step S22), a process of raising the temperature of the membrane to a main heating temperature higher than the intermediate heating temperature (step S23), and the process of heating and keeping the membrane at the main heating temperature (step S24). A first recovery amount R1 that is a difference in permeability of the membrane between after step S22 and before step S21 is 50% or more and 95% or less of a second recovery amount R2 that is a difference in permeability of the membrane between after step S24 and before step S21.