Disclosed herein is a porous membrane comprising a porous substrate; a porous ceramic coating disposed on the porous substrate; where an average pore size of pores in the porous substrate are larger than an average pore size of pores in the porous coating. Disclosed herein is a method of manufacturing a porous membrane comprising disposing upon a porous substrate a porous ceramic coating, where the porous ceramic coating has an average pore size that is less than an average pore size of the porous substrate.

Disclosed are a CMS membrane, characterized in that it is obtainable by pyrolysis of a polyimide composed of the monomers 1-(4-aminophenyl)-1,3,3-trimethyl-2H-inden-5-amine and 5-(1,3-dioxo-2-benzofuran-5-carbonyl-2-benzofuran-1,3-dione of the following formulae: ##STR00001##
preferably by pyrolysis of the polyimide having the CAS number 62929-02-6, and a supported CMS membrane comprising a CMS membrane obtainable from a polyimide by pyrolysis and a porous support, characterized in that a mesoporous intermediate layer is provided between the CMS membrane and the porous support. Further disclosed are a process for preparing the supported membrane, the use of the membranes for separating gas mixtures or liquid mixtures, an apparatus for gas separation or for liquid separation, and the use of the polyimide for preparing a CMS membrane by pyrolysis.

The invention relates to an apparatus and a method for the manufacture of at least one hollow fiber membrane, wherein a spinning mass is extruded via a spinning unit to form a spinning thread and precipitated in a precipitation bath to form a hollow fiber membrane and the hollow fiber membrane is optionally rinsed in a rinsing bath, wherein furthermore the hollow fiber membrane is passed through at least one drying unit, wherein the drying unit comprises a pressure section which is constructed in such a way that a positive pressure compared with atmospheric pressure can be set in the pressure section, and at least part of the precipitating agent or rinsing agent contained in the at least one hollow fiber membrane (104) is separated from the at least one hollow fiber membrane.

A composition of matter including a two-dimensional covalent organic imidazole framework (COF) polymer having an aromatic backbone and ordered nanometer sized pores that may be functionalized with a variety of functional groups. A filtration membrane having both high throughput and highly selective transport or rejection of a species of interest based on size, charge or other molecular properties is readily formed of the two-dimensional COF polymer. The filtration membrane being formed by providing a substrate, such as anodic aluminum oxide (AAO), and then depositing exfoliated carboxyl COF onto the substrate.

The invention relates to an apparatus and a method for the manufacture of at least one hollow fiber membrane, wherein a spinning mass is extruded via a spinning unit to form a spinning thread and precipitated in a precipitation bath to form a hollow fiber membrane and the hollow fiber membrane is optionally rinsed in a rinsing bath, wherein furthermore the hollow fiber membrane is passed through at least one drying unit, wherein the drying unit comprises a pressure section which is constructed in such a way that a positive pressure compared with atmospheric pressure can be set in the pressure section, and at least part of the precipitating agent or rinsing agent contained in the at least one hollow fiber membrane (104) is separated from the at least one hollow fiber membrane.

A semipermeable membrane support having a thickness difference between measurement thickness at 0.80 N/cm.sup.2 and measurement thickness at 1.27 N/cm.sup.2 of 1.0 to 5.0% is excellent in adhesion to a semipermeable membrane and also adhesion between a raw water spacer and the semipermeable membrane and thereby can be expected to maintain high water permeability after modulation. A method of producing a semipermeable membrane support comprises the step of carrying out hot-press processing by using an elastic roll, which has(have) a hardness between a type A durometer hardness of 60 or more and a type D durometer hardness of 95 or less.

The present invention is concerned with a dielectric material comprising a fluoropolymer, wherein at least part of the crystalline region of the fluoropolymer is in the β-phase. The dielectric material of the present invention may show relaxor-like ferroelectricity. The present invention also relates to a novel method of producing such a material, and the use of such a material in a high energy density capacitor. The method comprises layering sheets of PVDF on one another and applying pressure to the multilayer under a temperature which is preferably within 40° C. of the temperature of fusion. Further, the film is preferably quenched.

A reverse osmosis membrane of the present invention includes a porous support substrate (2) and a separation active layer (3) formed on a surface of the porous support substrate (2) and formed of a carbon film containing organized carbon.

A method for making a graphene membrane includes applying a suspension of graphene platelets in a fluid onto a porous substrate, and applying a pressure differential to force the fluid through the substrate to yield a filtered fluid while retaining the graphene platelets on the substrate. The graphene platelets and the substrate form the graphene membrane.

Provided is a method of producing a zeolite film continuously and efficiently. Zeolite is formed on a surface of a support using a method including: a first step of attaching zeolite fine crystals to a surface of a support; a second step of preparing synthetic gel for growing the fine crystals; a third step of putting the support and the synthetic gel into a reactor and performing hydrothermal synthesis; and a fourth step of cleaning the support subjected to the hydrothermal synthesis, in which in the third step, multiple containers arranged to be movable in a constant-temperature apparatus are each used as the reactor, the temperature and pressure for the hydrothermal synthesis is adjusted by the temperature and pressure in the constant-temperature apparatus, and the reaction time of the hydrothermal synthesis is adjusted by setting the time from when the reactor enters the constant-temperature apparatus to when the reactor exits the constant-temperature apparatus.