Abstract: A process for operating a permeable membrane generator at above or below design conditions therefor, which entails adjusting the permeation temperature of a feed stream permeating said membrane generator by heating or cooling means, thereby providing a desired amount, purity and pressure of a product gas.

Abstract: A device for separation of gas by adsorption, of the so-called VSA or MPSA type, comprises, between a utilization line (L) and a source (S) of gaseous mixture to be separated, at least one module (M) comprising in series a reversible rotary machine (R), typically a Roots machine, an adsorber (A) and a shut-off valve (V), the rotary machine (R) being alternately actuated, in one direction during a first phase of pressurization and of production and then, in the other direction, during a second phase of depressurization and desorption. Used particularly in the production of small and medium volumes of oxygen in modular installations.

Abstract: A device for the separation of gas by adsorption, of the so-called VSA or MPSA type, comprises, between a utilization line (L) and a source (S) of gaseous mixture to be separated, at least one module (M) comprising in series a reversible rotatable machine (R), typically a Roots, an adsorber (A) and a shut-off valve (V). The rotary machine (R) is alternately actuated, in one direction during a first phase of pressurization and of production and then, in the other direction, during a second phase of depressurization and desorption. Used particularly in the production of small and medium volumes of oxygen in modular installations.

Abstract: An assembly comprising an intermediate volume of medium-pressure gas (8) in a transportable housing (3) which is advantageously combined with a user apparatus (4) and selectively connectable to a high-pressure gas supply (1) by coupling it to a filling unit (2) via a quick connection system (15, 16). The assembly is particularly useful in portable welding apparatuses.

Abstract: A membrane nitrogen generator exhibiting increased flexibility and productivity in response to changes in customer demand which entails a membrane generator capable of generating nitrogen of variable flow rate and purity, bulk storage capacity for storing nitrogen of a purity which is higher than that required by a customer and flow and purity controllers for delivery to a customer plant.

Abstract: According to this process, there is produced gaseous nitrogen of medium purity under substantially the production pressure. This nitrogen is sent to the base of a distillation column (11) provided with a head condenser (23). The head condenser is cooled by means of liquid in the base of the low pressure column and if desired the liquid nitrogen at medium purity contained in a reservoir (10). Ultra-pure nitrogen is withdrawn as a product from the head of the column, and during periods of no production of nitrogen of medium purity and during periods in which the demand for ultra-pure nitrogen exceeds this production, there is sent to the base of the column gaseous reserve nitrogen of medium purity obtained from the liquid nitrogen of the reservoir and there is sent into the head condenser a relatively large flow of liquid nitrogen from this reservoir.

Abstract: Assembly of a pressurizable beverage keg (8) and a reservoir (1) of pressurization gas containing CO.sub.2 and comprising an expansion valve (5). The reservoir (1) is a toric portion (2) disposed concentrically at one end of the keg (8). The expansion valve (5) is mounted on one of the ends (3) of the torus. The keg (8) has at one end a handling skirt (11) defining an internal space, and the reservoir (1) is entirely disposed in the internal space of the skirt (11). The expansion valve (5) is coaxial to its end (3) of the torus (2) and has a passage (6) for emptying and filling the reservoir (1), opening through the peripheral wall of the reservoir (1) adjacent the same end (3) of the torus.

Abstract: A membrane nitrogen gas generator, containing a feed stream compressor, one or more filtering membranes, each having a permeate side and a non-permeate side, in fluid connection with and downstream of the feed stream compressor, and one or more product storage containers capable of storing a product having a higher purity than is required by customer demand, and which generator is capable of generating an increased flow rate during periods of high demand.

Abstract: A membrane nitrogen generator adapted to deliver a flow rate of nitrogen gas having a purity at least equal to P.sub.0, which contains:a) a source of compressed nitrogen containing gas having a purity lower than P.sub.0, the source having a maximum flow rate Fm.sub.1 ;b) a varyer connected to the source, which is adapted to vary the flow rate of the source between Fm.sub.1 and 0;c) a nitrogen membrane fed by the source which is capable of delivering a low purity nitrogen gas having a purity P.sub.1, which purity is lower than P.sub.0 at the maximum flow rate Fm.sub.1 ;d) a source of high purity compressed nitrogen gas having a purity which is greater than P.sub.0 which has a controllable flow rate of from 0 to a maximum flow rate value of Fm.sub.2 ;e) a mixer; andf) a purity controller.

Abstract: The separation of a gaseous mixture of at least three components, by permeation, wherein a more permeable component, e.g. hydrogen, is separated from an intermediately permeable component and a less permeable component, e.g. CO.sub.2 and CO, respectively, in a first permeator. The residue from the first permeator, e.g. CO.sub.2 and CO, is introduced into a second permeator in which the intermediately permeable component, e.g. CO.sub.2, is separated from the less permeable component, e.g. CO. The less permeable component, e.g. CO, is then directly and completely introduced into the downstream side of the first permeator, where it rejoins the more permeable component, e.g. H.sub.2. The partial pressure of the more permeable component in the starting gaseous mixture, e.g. H.sub.2, is maintained higher than its partial pressure in the final mixture of e.g. H.sub.2 and CO.

Abstract: This process comprises eliminating the ammonia from a gaseous effluent of the treatment of scrubbing with a liquid essentially comprising water, regenerating the scrubbing liquid by stripping countercurrent with respect to the gas to be treated, then recycling at least most of the regenerated scrubbing liquid by putting it into thermal exchange relation with the scrubbing liquid to be regenerated.Application in the production of CO.sub.2 by the treatment of smoke with ammonia.

Abstract: Liquid oxygen and gaseous nitrogen are remixed in a roughly reversible manner in an auxiliary column (3); rich liquid without argon, withdrawn at an intermediate place of the auxiliary column is remixed in another auxiliary column section (4) with impure nitrogen of the top of a low pressure column (6), and the gas of the top of this auxiliary section constitutes a residual gas (R1) of the plant. Application in the production of argon.

Abstract: The reservoir 1 contains in its lower part a purifying vessel 2 which contains a plate 9 having a bell means communicating with the reservoir and provided with an overflow pipe 12 through which liquid overflows into a bath having a constant level. When gas is drawn off from the top of the purifying vessel, liquid taken from the lower bath is vaporized in an exterior vaporizer 3 and the gas produced passes through the two baths in succession. In this way it is possible to obtain the gases having high purity devoid of particles of dust which are required for certain applications and in particular in the electronic component industry.

Abstract: A method of and an installation for utilizing a thermal cycle by means of which a less volatile fluid can be compressed by the expansion of a more volatile fluid, is characterized in that, in the course of said cycle a less volatile fluid available in a fractionated separation zone working under a low pressure is put into liquid-vapour equilibrium in counter-flow in said separation zone at said low pressure, with one or more light fractions at most as volatile as said more volatile fluid, so as to obtain, under said low pressure, the more volatile fluid and one or more heavy fractions at least as volatile as said less volatile fluid, and in that, after compression of said heavy fraction from said low pressure to a high pressure, the more volatile fluid available in a fractionated mixture zone working under said high pressure is put into liquid-vapour equilibrium in counter-flow in said mixture zone under said high pressure with one or more heavy fractions so as to obtain said less volatile fluid at said high