Abstract: Internally reheated sweep gas-aided membrane gas separation module in which the sweep gas is expanded retentate that is warmed through heat exchange with non-expanded retentate within the module.

Abstract: A hollow fiber membrane bundle useful for manufacturing a wide variety of hollow fiber membrane modules having different flow configurations includes hollow fiber membranes arranged around a porous support tube, a cured resin tubesheet formed at first end of the bundle, and either a cured resin nub or a cured resin tubesheet formed at a second end of the bundle. The bore(s) of the hollow fiber membranes are open at a face of the tubesheet adjacent the first end of the bundle. The tubesheet has an annular structure that encapsulates the hollow fiber membranes and the porous support tube at the first end of the bundle but which does not completely block a bore of the porous support tube, wherein the collection tube has a plurality of orifices formed therein at least at positions adjacent the nub.

Abstract: A hollow fiber membrane bundle useful for manufacturing a wide variety of hollow fiber membrane modules having different flow configurations includes hollow fiber membranes arranged around a porous support tube, a cured resin tubesheet formed at first end of the bundle, and either a cured resin nub or a cured resin tubesheet formed at a second end of the bundle. The bore(s) of the hollow fiber membranes are open at a face of the tubesheet adjacent the first end of the bundle. The tubesheet has an annular structure that encapsulates the hollow fiber membranes and the porous support tube at the first end of the bundle but which does not completely block a bore of the porous support tube, wherein the collection tube has a plurality of orifices formed therein at least at positions adjacent the nub.

Abstract: A hollow fiber membrane bundle useful for manufacturing a wide variety of hollow fiber membrane modules having different flow configurations includes hollow fiber membranes arranged around a porous support tube, a cured resin tubesheet formed at first end of the bundle, and either a cured resin nub or a cured resin tubesheet formed at a second end of the bundle. The bore(s) of the hollow fiber membranes are open at a face of the tubesheet adjacent the first end of the bundle. The tubesheet has an annular structure that encapsulates the hollow fiber membranes and the porous support tube at the first end of the bundle but which does not completely block a bore of the porous support tube, wherein the collection tube has a plurality of orifices formed therein at least at positions adjacent the nub.

Abstract: A hollow fiber membrane bundle useful for manufacturing a wide variety of hollow fiber membrane modules having different flow configurations includes hollow fiber membranes arranged around a porous support tube, a cured resin tubesheet formed at first end of the bundle, and either a cured resin nub or a cured resin tubesheet formed at a second end of the bundle. The bore(s) of the hollow fiber membranes are open at a face of the tubesheet adjacent the first end of the bundle. The tubesheet has an annular structure that encapsulates the hollow fiber membranes and the porous support tube at the first end of the bundle but which does not completely block a bore of the porous support tube, wherein the collection tube has a plurality of orifices formed therein at least at positions adjacent the nub.

Abstract: A plurality of membrane elements are arranged in series within a pressure vessel in which at least two of the elements exhibit different permeances or selectivities for a gas or gas pair respectively.

Abstract: Natural gas may be purified by removing C3+ hydrocarbons and CO2 in respective one or more separation units to yield conditioned gas lower in C3+ hydrocarbons and CO2 in comparison to the un-conditioned natural gas. Notably, the feed gas need not be subjected to joule-thomson expansion and molecular sieve dehydration performed by conventional processes. Rather, any water-rich reject stream from the separation unit(s) is dried downstream with a smaller compressor and smaller molecular sieve or gas separation membrane dehydration unit before it may be re-injected deep underground or deep under the sea bed.

Abstract: A plurality of membrane elements are arranged in series within a pressure vessel in which at least two of the elements exhibit different permeances or selectivities for a gas or gas pair respectively.

Abstract: A plurality of membrane elements are arranged in series within a pressure vessel in which at least two of the elements exhibit different permeances or selectivities for a gas or gas pair respectively.

Abstract: Natural gas may be purified by removing C3+ hydrocarbons and CO2 in respective first and second gas separation membrane stages to yield conditioned gas lower in C3+ hydrocarbons and CO2 in comparison to the un-conditioned natural gas.

Abstract: Natural gas may be purified by removing C3+ hydrocarbons and CO2 in respective first and second gas separation membrane stages to yield conditioned gas lower in C3+ hydrocarbons and CO2 in comparison to the un-conditioned natural gas.

Abstract: Parallel membrane elements are arranged in parallel within a pressure vessel. A sealing body is disposed within the pressure vessel and is compressed against an inner surface of the pressure vessel to provide a leak-right seal in between a feed gas side of the sealing body and a non-permeate side of the sealing body. The sealing body may be slid within the pressure vessel without damaging the sealing body and in all cases without requiring mechanical assistance.

Abstract: Natural gas may be purified by removing C3+hydrocarbons and CO2 in respective first and second gas separation membrane stages to yield conditioned gas lower in C3+ hydrocarbons and CO2 in comparison to the un-conditioned natural gas.

Abstract: Natural gas may be purified by removing C3+ hydrocarbons and CO2 in respective one or more separation units to yield conditioned gas lower in C3+ hydrocarbons and CO2 in comparison to the un-conditioned natural gas. Notably, the feed gas need not be subjected to joule-thomson expansion and molecular sieve dehydration performed by conventional processes. Rather, any water-rich reject stream from the separation unit(s) is dried downstream with a smaller compressor and smaller molecular sieve or gas separation membrane dehydration unit before it may be re-injected deep underground or deep under the sea bed.

Abstract: Natural gas may be purified by removing C3+ hydrocarbons and CO2 in respective first and second gas separation membrane stages to yield conditioned gas lower in C3+ hydrocarbons and CO2 in comparison to the un-conditioned natural gas.

Abstract: Parallel membrane elements are arranged in parallel within a pressure vessel. A sealing body is disposed within the pressure vessel and is compressed against an inner surface of the pressure vessel to provide a leak-right seal in between a feed gas side of the sealing body and a non-permeate side of the sealing body. The sealing body may be slid within the pressure vessel without damaging the sealing body and in all cases without requiring mechanical assistance.

Abstract: Parallel membrane elements are arranged in parallel within a pressure vessel. A sealing body is disposed within the pressure vessel and is compressed against an inner surface of the pressure vessel to provide a leak-right seal in between a feed gas side of the sealing body and a non-permeate side of the sealing body. The sealing body may be slid within the pressure vessel without damaging the sealing body and in all cases without requiring mechanical assistance.

Abstract: Helium-containing natural gas is processed with three gas separation stages to produce a natural gas product and a Helium-containing gas that may be injected into the reservoir from which the Helium-containing natural gas is obtained. A permeate from the first gas separation membrane stage is compressed and fed to the second gas membrane stage. The permeate from the second gas separation membrane stage is recovered as the Helium-containing gas that may be injected into the reservoir. The non-permeate from the second gas separation membrane stage is fed to the third gas separation membrane stage. Non-permeates from the first and third gas separation stages are combined to produce a natural gas product. A permeate from the third gas separation membrane stage is combined with a non-permeate from the first gas separation membrane stage before it is compressed and fed to the second gas separation membrane stage.

Abstract: Parallel membrane elements are arranged in parallel within a pressure vessel. A sealing body is disposed within the pressure vessel and is compressed against an inner surface of the pressure vessel to provide a leak-right seal in between a feed gas side of the sealing body and a non-permeate side of the sealing body. The sealing body may be slid within the pressure vessel without damaging the sealing body and in all cases without requiring mechanical assistance.

Abstract: Helium-containing natural gas is processed with three gas separation stages to produce a natural gas product and a Helium-containing gas that may be injected into the reservoir from which the Helium-containing natural gas is obtained. A permeate from the first gas separation membrane stage is compressed and fed to the second gas membrane stage. The permeate from the second gas separation membrane stage is recovered as the Helium-containing gas that may be injected into the reservoir. The non-permeate from the second gas separation membrane stage is fed to the third gas separation membrane stage. Non-permeates from the first and third gas separation stages are combined to produce a natural gas product. A permeate from the third gas separation membrane stage is combined with a non-permeate from the first gas separation membrane stage before it is compressed and fed to the second gas separation membrane stage.