Abstract: The distributor includes a pattern of irrigation points with advantageously substantially constant surface pitch over most of the irrigation area, the pattern being, typically, regular in a main region of the distributor and irregular, with associated surface regions which are also irregular in a junction region, the irrigation points delivering predetermined flow rates defined by calibrated orifices which have cross-sections chosen from a predetermined group of n cross-sections, n not being greater than four and advantageously not greater than two. This distributor is particularly applicable to packed air distillation columns.

Abstract: In this process for the distillation of air, of the type with a liquid oxygen pump (14) and with the vaporization of liquid oxygen under pressure, there are used, in addition to a principal compressor (1), at least three further compressors (9 to 11 ), of which two (9, 10) are mounted in series and supply the heat exchange line with air at a high pressure of the vaporization of oxygen. Air is withdrawn between these two further compressors, expanded to the medium pressure and introduced at the base of the medium pressure column (5), and at least one (11) of the three further compressors consumes the mechanical energy developed by the turbine (12).

Abstract: Process and installation for the production of gaseous oxygen and/or gaseous nitrogen under pressure, of the type in which the air is distilled in a double distillation column (10) comprising a low pressure column (12) operating under a low pressure, and a medium pressure column (11) operating under a medium pressure. All the air to be distilled is compressed (in 1,4) to at least one high pressure of air substantially greater than the medium pressure, and the compressed air is cooled to an intermediate temperature. A portion of it is expanded in a turbine (5) to the medium pressure, before introducing it into the medium pressure column (11). The non-work-expanded air is liquified, then introduced after expansion (in 19, 20), into the double column; and at least one liquid product withdrawn from the double column is brought to the production pressure, and this liquid product is vaporized by heat exchange with the air.

Abstract: A process and installation for the cryogenic purification of impure hydrogen, of the type in which impure hydrogen is cooled under a low pressure PO to a temperature sufficiently low to condense a predetermined proportion of the impurities, by heat exchange in a thermal heat exchange line (3) with purified hydrogen and with a residual fraction containing the expanded preliminarily condensed impurities (in 11, 12) to a low pressure P1. The remaining cold is supplied by the expansion of purified hydrogen in a turbine (8) with gas bearings and the expanded hydrogen is added to the light impurities expanded at the cold end of the heat exchange line. The turbine (8) is supplied with the gas leaving its bearings (17), after cooling of hydrogen at the labyrinthine seal (18) of the turbine is withdrawn under a pressure slightly less than the interstitial pressure Pi which prevails between the rotor (14) and the stator (16) of this turbine.

Abstract: The desulfurization of gaseous effluents containing contaminating amounts of objectionable sulfur compounds, typically via the Claus reaction and notably in the presence of oxygen, utilizing a support substrate, e.g., titanium dioxide, having an active catalytic phase deposited thereon, such active catalytic phase being constituted of an electroneutral solid solution having the average composition:A.sub.4.+-.y V.sub.2.+-.x O.sub.9in which A is a metal other than vanadium, e.g., magnesium, calcium or zinc, 0.ltoreq.x.ltoreq.0.2 and 0.ltoreq.y.ltoreq.0.5.

Abstract: Carbon monoxide and hydrogen are from a gaseous mixture comprising essentially these two components and methane, by the steps of i) cooling the initial gaseous mixture so as partially to condense it; ii) separating a condensed portion of the mixture from an uncondensed portion containing principally hydrogen; iii) sending the condensed portion to a stripping column (7) to produce a gaseous fraction at the head of the column comprising hydrogen and a liquid fraction at the base of the column containing carbon monoxide and methane; iv) distilling the liquid fraction in a purification column (9) to produce substantially pure carbon monoxide at the head of the column and methane at the base of the column; and v) supplying a portion of the separation energy by a refrigeration cycle using an autonomous refrigeration fluid.

Abstract: A primary flow (Q) of a carrier gas is divided into a series of flows of predetermined flow rate (q.sub.1 -q.sub.10). There is introduced into a first of these flows (q.sub.1) a predetermined quantity of gas (A) to be analyzed, so as to obtain a first mixture (M.sub.1). This first mixture (M.sub.1) is diluted with a carrier gas flow (q.sub.3) to constitute a second mixture (M.sub.2). A portion (d.sub.1) of this second mixture is diluted with a carrier gas flow (q.sub.5) to constitute a third mixture (M.sub.3), and so on. A calibrating gas (U.sub.5) that contains very little of the second gas is provided. These flows feed a series of outlets, usable in parallel, of controlled flow rates of different mixtures over different ranges from very low content to higher content of the gas to be analyzed. The invention is useful particularly for the calibration of high sensitivity hygrometers.

Abstract: A process for supplying a flow of nitrogen to a site having flowrate requirements varying between a nominal flowrate and a range situated thereabove comprising: a) passing compressed air into a main line in a separating assembly formed by at least two membrane separation lines mounted in parallel, wherein at least one of the separation lines can be shut off from the main line, the separating assembly having one of the following configurations: a1) when the flowrate requirements are situated at a level of the nominal flowrate, all of the membrane separators of the assembly are in operation, none of the separating lines being shut off; a2) when the flowrate requirements of the site exceed a predetermined flowrate, at least one of the lines of the separating assembly is shut off, keeping at least one separation line and its membrane separator in operation; b) advancing nitrogen gas obtained at the outlet side of each of the membrane separators to a collector connected downstream of the main line; c) evacuating g

Abstract: During restarting an argon column (2), two valves (15, 17) provided at the output of a pump (3) are controlled while maintaining a constant level in the base of the argon column, at the outset at a predetermined first control level (N2), then while progressively lowering the controlled value of the constant level. Use in installations for air distillation whose argon column, of the packed type, has a sufficient height to purify the argon of oxygen to an oxygen content less than 100 ppm.

Abstract: A process for restarting an adsorption receptacle which is part of an installation for the purification of hydrogen by pressure swing adsorption (PSA), which receptacle, during a hiatus in its operation, has been depressurized and then rendered inert with nitrogen. The receptacle is repressurized with practically pure hydrogen, and then the adsorption cycle is restarted in this receptacle. The repressurization is effected counter-current with respect to the adsorption direction in the receptacle. The receptacle is repressurized with hydrogen produced by the installation before the hiatus. The process can be used for the treatment of a catalytic hydrocarbon reforming gas, in which case the receptacle contains successively, in the adsorption direction, a layer of alumina, a layer of carbon and a layer of molecular sieve.

Abstract: The invention relates to a process for producing disilane from monosilane, according to which gaseous monosilane is passed into a reaction zone where it is subject to an electric discharge generated by a high-frequency current.

Abstract: To regenerate the adsorbent which serves to purify compressed air from water and carbon dioxide, there is used residual gas from an air distillation apparatus (10), heated to a substantially constant moderate regeneration temperature between the temperature of the air entering the mass of adsorbent and a temperature which is at most about 50.degree. C. higher, preferably about 10.degree. to 20.degree. C. higher, than this entering air temperature. This gas is then sent to a water refrigeration tower (16) for cooling the compressed air.

Abstract: Air is distilled in a distillation apparatus (13) associated with a heat exchange line (11) in which is circulated a heat transfer fluid under high pressure. A storage (20, 23)is supplied, at least intermittently, with gas in liquid phase; and gas in liquid phase withdrawn from the storage is raised to a vaporization pressure, and vaporized under this pressure in the heat exchange line (11). The supply of liquefied gas to the storage can be from the distillation apparatus (13) and/or from an external source such as a tank truck (29, 34). It is useful particularly for the supply of oxygen, nitrogen and argon under pressure to installations for the production of stainless steel such as electric arc furnaces.

Abstract: A reservoir for the storage of gas under high pressure comprises an enclosure portion (2) which is uninsulated and an enclosure portion (2A) which is insulated. The two portions (2A, 2B) are connected by an insulated passage (18) insulated from the enclosure portions. The uninsulated portion (2B) defines a gaseous sky limiting the instantaneous pressure drops during withdrawal of liquid from the insulated portion (2A) to decrease the response time of the heating of an external circuit to maintain pressure. Used particularly in safety installations of a principal source for the production of gas under high pressure.

Abstract: The invention relates to a process for the separation of a gaseous hydride or a mixture of gaseous hydrides from a gaseous medium containing at least one gas from the group consisting of H.sub.2, Ar, He, according to which the gaseous medium is passed on to a membrane module so that the concentration of the hydride or of the mixture of hydrides obtained at the outlet of the module is higher than their initial concentration in the gaseous medium.

Abstract: Provided is a process and an apparatus for producing ultra-high purity monosilane. In a preferred embodiment, the process comprises introducing a monosilane feed gas, which also serves as a heat source, to the lower stage of a rectification column which is sectioned into an upper stage, a middle stage and a lower stage by means of an intermediate portion reboiler-condenser and a lower portion reboiler-condenser. The monosilane feed gas is cooled in the lower portion of the reboiler-condenser so that the higher boiling point components in the feed gas are separated. The remaining lower boiling point components are then introduced into the upper stage by way of the middle stage and the intermediate portion of the reboiler-condenser. The remaining components are condensed in the top portion of the upper stage so that monosilane and the lower boiling point components are separated, with the condensed monosilane becoming a reflux liquid.

Abstract: The recompression line for the gas in the cold container (7) comprises at least one compressor (C) with which at least a first means (N.sub.1) for controlling the speed of rotation of the compressor as a function of parameters (inter alia, flow rate (D), pressure (P)) of the fluid in the line (8) is associated. In order to ensure an adequate fluid flow rate at the inlet of the compressor, the installation comprises a line (9) comprising a pilot-operated valve (V.sub.1) and by-passing the compressor, and a line (10) comprising a pilot-operated valve (V.sub.2) connecting the inlet line (4) to the compression line (8).Used, inter alia, in installations for refrigerating superconductive elements.

Abstract: A torch includes a sheath enclosing various feed streams for active cutting fluids and cooling fluid, terminated by a distribution unit in which a cutting head is removably mounted. The cutting head includes a heating unit provided with channels for ejection of a combustible oxygen mixture, an intermediate insert forming the ejection nozzle for gaseous shielding oxygen, and a central insert for ejection of liquid oxygen under pressure.

Abstract: Cooling water for compression apparatus (1) is cooled by an air-refrigerated apparatus (18). Makeup water which is cooler than the water treated by this apparatus passes first through a heat exchanger (8) mounted on the delivery conduit of the compression apparatus, then supplies the refrigeration apparatus (18). Use in air distillation installations.

Abstract: A process and installation for the production of gaseous oxygen and/or gaseous nitrogen under pressure by distillation of air in a double column (9), which comprises pumping (in 13) at least one liquid product withdrawn from the base of the low pressure column (11), and vaporization (in 8) of the compressed liquid product by heat exchange with the air brought to a high air pressure. All of the air to be distilled is brought to the high air pressure, and the excess fraction of this air is expanded in two turbines in series (5, 6) to the pressure of the medium pressure column (10), the air being partially reheated (in 22) between the two turbines.