Abstract: All of the air is compressed in a single compressor, which feeds a smelter for smelting ore, a converter for converting matte coming from the smelter and an air separation unit which delivers two oxygen streams for enriching the air. A buffer tank is used to deliver a variable flow of enriched air to the converter.

Abstract: All of the air is compressed in a single compressor (1), which feeds the smelter (2) for smelting the ore, the converter (6) for converting the matte coming from the smelter (2) and an air separation unit (4) which delivers two oxygen streams (9, 10) for enriching the air. A buffer tank (7) is used to deliver a variable flow of enriched air to the converter (6). Application to the production of copper.

Abstract: Impure oxygen containing 70 to 98% oxygen and less than 2% argon is supplied to a synthesis-gas production unit (3a) which supplies hydrogen to an ammonia-production unit (7a). The same air-separation device (1a) can supply the nitrogen (9) to the ammonia-production unit and impure oxygen (2a) to the synthesis-gas production unit.

Abstract: A process and plant for air separation by cryogenic distillation. Air is cooled in a main exchanger and is sent to a distillation column in which it separates into an oxygen-enriched liquid and a nitrogen-enriched vapor. A stream of pressurized liquid coming from the apparatus vaporizes in the main exchanger. The refrigeration necessary for the process is generated by expansion of air in one or more turbines immediately downstream of the main exchanger. The turbine or turbines produces or produce, as output, a stream which is at least 95 percent liquid, preferably 100 percent liquid.

Abstract: Process and installation for the production of variable flow rates of at least one pure component by fractionation of a mixture in a distillation apparatus (15), containing structured packing (17) and dimensioned to handle a nominal flow rate of the mixture at nominal pressure. To obtain higher production than the nominal production, there is increased proportionately to the ratio of the productions, the flow rate of the mixture distilled in the apparatus (15). Also increased is the operating pressure of the apparatus so as to increase the flooding limit of the apparatus under similar proportions. Preferably, the mixture is air. There is a compressor (3) for the mixture to be fractionated designed for nominal capacity and, upstream of the latter, a blower (1). Alternatively, there can be a compressor (3) for the mixture to be fractionated designed for maximum capacity.

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 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.

Abstract: All the entering air is brought to a high pressure and then cooled to an intermediate temperature. At this temperature, a portion of the air is work expanded (in 4) to the medium pressure, and the rest is liquified. The low pressure column operates under a pressure of the order of 1.7 to 5 bars absolute, and its residual gas is expanded in a second turbine (9) after having been reheated to ambient temperature, then further heated (in 7) by heat exchange with the compressed air. Use for the production of impure oxygen under pressure and simultaneously at least one liquid product.

Abstract: Process and installation for the production of gaseous oxygen and/or gaseous nitrogen under pressure and of at least one liquid product by an installation comprising a single air distillation column (9) provided with a nitrogen refrigeration cycle. The air to be treated is compressed (in 1) to a first pressure at least equal to the pressure of the single column. At least a portion of the air is further compressed (in 4; 4, 4A) to a high pressure substantially greater than the pressure of the single column. A fraction of this air is condensed (in 7) by vaporization of liquid oxygen and/or liquid nitrogen withdrawn from the base of the column and pumped (in 14, 15) to the corresponding vaporization pressure. The gaseous oxygen and/or gaseous nitrogen is recovered (in 30, 28) under the resulting pressure, as product. The air thus condensed is subcooled (in 11), expanded to about the pressure of the column (in 20, 21), and introduced at least in part into an intermediate level of the column.

Abstract: Process and installation for the production of gaseous oxygen and/or gaseous nitrogen under pressure, of the type in which air is distilled in a double distillation column (11) comprising a low pressure column (13) operating under a so-called low pressure, and a medium pressure column (12) operating under a so-called medium pressure. All the air to be distilled is compressed (in 1, 3, 7)to at least one high air pressure substantially greater than the medium pressure, and the compressed air is cooled to an intermediate temperature, and a portion of it is expanded in a turbine (8) to the medium pressure, before introducing it into the medium pressure column (12). The air which has not been expanded is liquefied, then introduced after expansion (in 20, 21), into the double column. 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 at least one portion of the air to be distilled in the course of cooling.

Abstract: Process and apparatus for the production of gaseous oxygen under median pressure with a double distillation column (5). The low pressure column (7) of the double column (5)is operated under a pressure substantially greater than atmospheric pressure and slightly greater than the desired production pressure of oxygen, this low pressure being about 2 to 5 bars. The medium pressure column (6) of the double column (5) is under a corresponding pressure, namely, about 8 to 16 bars. The gaseous production oxygen is directly recovered from the base of the low pressure column, and the installation is maintained cold, at least in part, by free expansion of at least one gaseous product leaving the low pressure column.

Abstract: A cryogenic unit for the separation of gases includes at least one distillation column (1) is preassembled in the factory. The column (1) with added tubing elements (2) constitutes a pre-equipped subassembly which is transported and installed at the worksite. The tubing elements are disposed so as to be inscribed in at least one elongated volume (3; 3.sub.1, 3.sub.2) lateral to the column and of reduced section. The subassembly (1,2) is disposed on at least one transport cradle (4, 4') and transported to the worksite on the cradle and mounted at the worksite in a cold box (10) Preferably, all the tubing elements are disposed in the cradle. The subassembly, with or without the cradle, is mounted adjacent one side wall of the cold box (10) and is spaced by insulation (13) from at least one liquid gas reservoir (11; 12) also in the cold box (10).