Abstract: In a crude oil purification process including phase separators, a vapor recovery unit (VRU), and dew pointing/dehydration and CO2 removal membranes, instead of compressing the low boiling point (i.e., C1-5) 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 H2O/C3+ hydrocarbon enriched permeate from the dew pointing and dehydration membranes.

Abstract: 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.

Abstract: 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.

Abstract: A pressurized CO2 rich gas is cooled down to condense at least part of the stream in a heat exchanger. A bulk of the CO2 is separated by partial condensation and distillation in order to obtain at least one non-condensable gas from a separation vessel. The non-condensable gas is optionally heated up to a temperature lower than ?20° C. (membranes performances is greatly enhanced by low temperature operation). The non-condensable gas is introduced into a membrane permeation unit, producing a residue stream and a permeate stream (the permeate stream is enriched in CO2). The permeate stream is recycled to the process, optionally after compression. The method is auto-refrigerated, i. e. no external refrigerant is used to provide cooling below 0° C.

Abstract: The invention relates to a method for treating a hydrocarbon feed gas stream containing CO2 and H2S to recover a purified CO2 gas 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 CO2 enriched gas stream (v), and a stream enriched in sulfur compounds (vi); d. Compressing stream (v) exiting the TGTU; e. Passing the compressed CO2 enriched gas through a CO2 purification unit thereby recovering a purified CO2 gas stream (vii), and the device for carrying out said method.

Abstract: The invention relates to a method for treating a hydrocarbon feed gas stream containing CO2 and H2S to recover a purified CO2 gas 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 CO2 enriched gas stream (v), and a stream enriched in sulfur compounds (vi); d. Compressing stream (v) exiting the TGTU; e. Passing the compressed CO2 enriched gas through a CO2 purification unit thereby recovering a purified CO2 gas stream (vii), and the device for carrying out said method.

Abstract: This disclosure discusses devices to sweep the permeate side of fiber membrane permeators. Specifically, providing permeate side sweep wherein the fiber membranes comprise a bore; the feed fluid is in fluid communication with the outer surface of the fiber membrane; and the permeate is withdrawn from the bore of the fiber membrane. Permeate side sweep is used to increase the amount of permeate separated from a fluid mixture by the permeator device. The device of the subject invention includes a sweep chamber in fluid communication with the bore of the fiber membrane and in fluid communication with a suitable sweep fluid source. The sweep fluid is controllable and can be conditioned by devices known in the art.