Abstract: A method of controlling a plant for processing a gas by adsorption, with N adsorbers R1 to R0 and variable N phase times. The method utilizes a mobile parameter for identifying the operating state of N adsorber which is in each successive phase time of the cycle. For a given phase time, a parameterized sequence (S, S′) of control steps for the plant are defined. A control sequencer of the plant is generated by matching an adsorber (R1 to R0) with each mobile parameter of the parameterized sequence during each phase time of the cycle, causing the succession of phase times of the cycle to be followed at all the adsorbers in operation.

Abstract: The plant (10) has N adsorbers (R1 to R0) operating according to a cycle with at most N phase times. For the method of controlling this plant, a mobile parameter for identifying the operating state of the adsorber which is in each successive phase time of the cycle is firstly associated with the said phase time. For a given phase time, a parameterized sequence (S, S′) of control steps of the plant (10) during the said given phase time is then defined, each adsorber controlled by the steps of the said sequence being denoted by the parameter for identifying the operating state of the said adsorber. A control sequencer of the plant (10) is lastly generated by matching an adsorber (R1 to R0) with each mobile parameter of the parameterized sequence during each phase time of the cycle, so as to cause the succession of phase times of the cycle to be followed at all the adsorbers in operation.

Abstract: This installation comprises subgroups of permeators (SG1 to SG3), each subgroup comprising a permeator (4A to 4C) or several permeators mounted in parallel, and having an inlet (12A to 12C), a permeate outlet (14A to 14C) and a non-permeate outlet (16A to 16C). The non-permeate outlet of a first subgroup (SG1, SG2) is connected to the inlet of a second subgroup (SG2, SG3), and at least one of the subgroups has closure elements (22A to 22C) for its permeate outlet when the real feed flow rate is below the nominal feed flow rate by a predetermined quantity.

Abstract: This installation comprises subgroups of permeators (SG1 to SG3), each subgroup comprising a permeator (4A to 4C) or several permeators mounted in parallel, and having an inlet (12A to 12C), a permeate outlet (14A to 14C) and a non-permeate outlet (16A to 16C). The non-permeate outlet of a first subgroup (SG1, SG2) is connected to the inlet of a second subgroup (SG2, SG3), and at least one of the subgroups has closure means (22A to 22C) for its permeate outlet when the real feed flow rate is below the nominal feed flow rate by a predetermined quantity.

Abstract: A process for separation of a gas mixture by pressure swing adsorption, in which a pressure swing cycle comprising a sequence of steps which define adsorption, decompression/regeneration and pressure rise phases is employed for the or each adsorber. The cycle furthermore comprises at least temporarily at least one step of isolating the adsorber (II; IV) during which the pressure variation in the isolated adsorber is recorded.

Abstract: Process and apparatus for the separation of at least one gas from an entering gaseous mixture (1), of the type in which a membrane separation is conducted with at least two successive membrane separators in the following manner: the entering mixture is passed through a first membrane separator (2) operating at a first operating temperature and all or a portion of the residual mixture (5) from this first membrane separator is passed through a second membrane separator (3) operating at a second operating temperature. A mixture enriched in the gas is obtained from the permeate outlet (6, 4) of each of these two separators. Two separators are used whose selectivities for the gas are different. These may be membranes of different type, or membranes of the same type, if the first operating temperature is different from the second operating temperature.