The disclosure provides a method for preparing a hollow fiber membrane by melt spinning-stretching and selective swelling, including: preparing a nascent hollow fiber by melt spinning in an inert gas protective atmosphere by using an amphiphilic block copolymer as a film forming material, and stretching the nascent hollow fiber in the cooling process, a stretch rate being controlled at 200-540 mm/min, and a stretch ratio being controlled at 150-600%; immersing the obtained hollow fiber in a swelling solvent, and treating the hollow fiber in a water bath at 65° C. for 1 h; and then transferring the hollow fiber into a long-chain alkane solvent, treating the hollow fiber at the same temperature for 1-12 h, and after the completion of the treatment, immediately taking out the hollow fiber and drying the hollow fiber to obtain the hollow fiber membrane with a bicontinuous porous structure. By combining the melt spinning-stretching and the selective swelling, the method of the disclosure can synchronously and continuously improve the permeability and selectivity of the hollow fiber membrane. The treatment in the long-chain alkane solvent can make the polar chain excessively enriched on the surface of the membrane migrate inward, thereby improving the performance of the hollow fiber membrane.

The present invention provides a separation membrane that is suitable for separating an acid gas from a gas mixture containing the acid gas and has a high acid gas permeability. A separation membrane (10) of the present invention includes: a separation functional layer (1); a porous support member (3) supporting the separation functional layer (1); and an intermediate layer (2) disposed between the separation functional layer (1) and the porous support member (3), and including a matrix (4) and nanoparticles (5) dispersed in the matrix (4).

The disclosure provides a method for preparing a hollow fiber membrane by melt spinning-stretching and selective swelling, including: preparing a nascent hollow fiber by melt spinning in an inert gas protective atmosphere by using an amphiphilic block copolymer as a film forming material, and stretching the nascent hollow fiber in the cooling process, a stretch rate being controlled at 200-540 mm/min, and a stretch ratio being controlled at 150-600%; immersing the obtained hollow fiber in a swelling solvent, and treating the hollow fiber in a water bath at 65° C. for 1 h; and then transferring the hollow fiber into a long-chain alkane solvent, treating the hollow fiber at the same temperature for 1-12 h, and after the completion of the treatment, immediately taking out the hollow fiber and drying the hollow fiber to obtain the hollow fiber membrane with a bicontinuous porous structure. By combining the melt spinning-stretching and the selective swelling, the method of the disclosure can synchronously and continuously improve the permeability and selectivity of the hollow fiber membrane. The treatment in the long-chain alkane solvent can make the polar chain excessively enriched on the surface of the membrane migrate inward, thereby improving the performance of the hollow fiber membrane.

Described herein are polymeric based composite membranes that provide selective resistance for gases while providing water vapor permeability. Such composite membranes have a high water/air selectivity in permeability. The methods for making such membranes and using the membranes for dehydrating or removing water vapor from gases are also described.

M(SiF.sub.6)(pyz).sub.3 (M=Cu, Zn, Co, or Ni) has a pore size between a size of H.sub.2 and a size of CO.sub.2, and thus exhibits prominent screening performance for H.sub.2/CO.sub.2. A strong interaction between Cu(SiF.sub.6)(bpy).sub.2 and a CO.sub.2 molecule can hinder the transport of the CO.sub.2 molecule. The above two MOFs both can achieve the H.sub.2/CO.sub.2 separation. By preparing a dense MSiF.sub.6/polymer layer, MSiF.sub.6 is uniformly dispersed in the polymer and is fixed, and subsequently, MSiF.sub.6 is converted into M(SiF.sub.6)(pyz).sub.3 or Cu(SiF.sub.6)(bpy).sub.2 by interacting with an organic ligand. Through vapor-induced in-situ conversion, MOF particles can be well dispersed without interface defects between the MOF particles and the polymer. Even at a doping amount of 80%, the mechanical flexibility and stability of the MMM can still be retained.

The invention relates to:—anion exchange blend membranes consisting the following blend components:—a halomethylated polymer (a polymer with —(CH2)x—CH2—Hal groups, Hal=F, CI, Br, I; x=0-12), which is quaternised with a tertiary or a n-alkylated/n-arylated imidazole, an N-alkylated/N-arylated benzimidazole or an N-alkylated/N-arylated pyrazol to form an anion exchanger polymer. - an inert matrix polymer in which the anion exchange polymer is embedded and which is optionally covalently crosslinked with the halomethylated precursor of the anion exchanger polymer,—a polyethyleneglycol with epoxide or halomethyl terminal groups which are anchored by reacting with N—H-groups of the base matrix polymer using convalent cross-linking—optionally an acidic polymer which forms with the anion-exchanger polymer an ionic cross-linking (negative bound ions of the acidic polymer forming ionic cross-linking positions relative to the positive cations of the anion-exchanger polymer)—optionally a sulphonated polymer (polymer with sulphate groups —SO2Me, Me=any cation), which forms with the halomethyl groups of the halomethylated polymer convalent crosslinking bridges with sulfinate S-alkylation. The invention also relates to a method for producing said membranes, to the use of said membranes in electrochemical energy conversion processes (e.g. Redox-flow batteries and other flow batteries, PEM-electrolyses, membrane fuel cells), and in other membrane methods (e.g. electrodialysis, diffusion dialysis).

A porous composite ultrafiltration membrane including a block copolymer layer having (a) one or more soft block polymer(s) having an elongation at break of greater than about 50%, as measured by ASTM D638 and an elastic modulus of between 10 MPa to 3 GPa as measured by the ASTM D638 tensile test; and (b) one or more hard block polymer(s) having an elongation at break of less than about 65%, as measured by ASTM D638, and an elastic modulus of higher than 1 GPa as measured by the ASTM D638 tensile test, and a macroporous support layer having a pore size larger than a pore size of the block copolymer layer. Also described is a method for making the porous composite membrane.

The invention relates to: —anion exchange blend membranes consisting the following blend components: —a halomethylated polymer (a polymer with —(CH.sub.2).sub.x—CH.sub.2—Hal groups, Hal=F, Cl, Br, I; x=0-12), which is quaternised with a tertiary or a n-alkylated/n-arylated imidazole, an N-alkylated/N-arylated benzimidazole or an N-alkylated/N-arylated pyrazol to form an anion exchanger polymer. —an inert matrix polymer in which the anion exchange polymer is embedded and which is optionally covalently crosslinked with the halomethylated precursor of the anion exchanger polymer, —a polyethyleneglycol with epoxide or halomethyl terminal groups which are anchored by reacting with N—H-groups of the base matrix polymer using covalent cross-linking—optionally an acidic polymer which forms with the anion-exchanger polymer an ionic cross-linking (negative bound ions of the acidic polymer forming ionic cross-linking positions relative to the positive cations of the anion-exchanger polymer)—optionally a sulphonated polymer (polymer with sulphate groups —SO.sub.2Me, Me=any cation), which forms with the halomethyl groups of the halomethylated polymer covalent crosslinking bridges with sulfinate S-alkylation. The invention also relates to a method for producing said membranes, to the use of said membranes in electrochemical energy conversion processes (e.g. Redox-flow batteries and other flow batteries, PEM-electrolyses, membrane fuel cells), and in other membrane methods (e.g. electrodialysis, diffusion dialysis).

Disclosed herein is a system for recovering carbon monoxide from an industrial by-product gas, the system including a supply unit for supplying an industrial by-product gas containing carbon dioxide, nitrogen, carbon monoxide, and hydrogen, a first membrane separation unit including a separation membrane capable of allowing carbon dioxide and hydrogen to permeate, and receiving the industrial by-product gas supplied from the supply unit to allow carbon dioxide and hydrogen to permeate, and a second membrane separation unit including a polymer membrane in which a transition metal is supported, and receiving a gas remaining in the first membrane separation unit to allow carbon monoxide to permeate.

A method for making a gas separation membrane comprises dissolving and mixing poly(ether-b-amide) (Pebax) copolymer and acrylate-terminated polyethylene glycol oligomers (PEGDA) in a solvent, casting the polymer solution into a mold, removing the solvent to form a film, adding a photoinitiator to the film and irradiating the film with ultraviolet radiation to induce crosslinking of the PEGDA in the film, producing XLPEGDA, and submerging the film after exposure in a crosslinking solution to form crosslinked Pebax (XLPebax) in the film, wherein the crosslinking solution comprises one of a diisocyanate, a diisocyanate derivative and a combination of a diiscyanate and a diisocyanate derivative.