Air Liquide Advanced Technologies U.S. LLC

L'air Liquide,societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude

Total Sa

Totalenergies Onetech

Sandeep K Karode

Yong Ding

Karl S Beers

Benjamin Bikson

Sudhir S Kulkarni

Paul Terrien

Claire Weiss

Nicolas Chambron

Kamlesh Ghodasara

Sylvain Gerard

Cyril Defaye

Wolfgang Nehb

Fan Z Worley

Frédéric Pousse

Michael E Bailey

Manuel Arruda

Ed Sanders, Jr

Tim Poludniak

Stefan Fraenkle

Eckhard Jungst

Frederic Pousse

Eckhard JÜNGST

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.

Gas separation membrane bundle with convertible flow configurations

In a crude oil purification process including phase separators, a vapor recovery unit (VRU), and dew pointing/dehydration and COremoval membranes, instead of compressing the low boiling point (i.e., C) hydrocarbon vapor stream from the VRU along with the main portion of gas from the separation train and feeding it to the membranes, it is compressed and dehydrated along with the HO/Chydrocarbon enriched permeate from the dew pointing and dehydration membranes.

System and method for recovery of fuel gas from crude oil purification

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.

Membrane sweep with internal reheat of sweep gas

A single compressor is used to separately compress permeate from cascaded first and second gas separation membrane-based separation units and residue from a fourth gas separation membrane-based separation unit in order to avoid too high a CO2 partial pressure in the compressed permeate. After the permeates from the first and second stages are compressed, the compressed stream is fed to a third gas separation membrane-based separation unit.

Integrated compression and membrane separation process for removal of CO2 from raw natural gas

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.

Gas separation membrane module with membrane elements arranged in series

Natural gas may be purified by removing Chydrocarbons and COin respective one or more separation units to yield conditioned gas lower in Chydrocarbons and COin 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.

Method and system for purification of natural gas using membranes

Natural gas may be purified by removing Chydrocarbons and COin respective first and second gas separation membrane stages to yield conditioned gas lower in Chydrocarbons and COin comparison to the un-conditioned natural gas.

The invention relates to a method for treating a hydrocarbon feed gas stream containing COand HS to recover a purified COgas stream (vii), comprising: a. Separating said feed gas stream into a sweetened gas stream (i), and an acid gas stream (ii); b. Introducing stream (ii) into a Claus unit wherein an oxygen-rich stream is used as a combustive agent in the Claus furnace, thereby recovering a liquid stream of elemental sulfur (iii) and a tail gas stream (iv); c. Introducing the stream (iv) into a Tail Gas Treatment Unit (TGTU) thereby separating said tail gas stream into a COenriched gas stream (v), and a stream enriched in sulfur compounds (vi); d. Compressing stream (v) exiting the TGTU; e. Passing the compressed COenriched gas through a COpurification unit thereby recovering a purified COgas stream (vii), and the device for carrying out said method.

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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.

Gas separation membrane module with improved gas seal

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.

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Boothwyn, PA, United States of America

Sandeep K Karode