Abstract: The process and the device are used for recovering argon by low-temperature separation of air. Process air (1) is compressed (3) and is introduced into a distilling-column system for nitrogen-oxygen separation (13, 14). An argon-containing stream (72) is removed in the distilling-column system for nitrogen-oxygen separation. The argon-containing stream (72) is sent to a crude argon column (25). The crude argon column (25) has a top condenser (24), in which a top gas from the crude argon column (25) is at least partially condensed. At least one part of the condensate that is recovered in this case is released as reflux liquid to the crude argon column (25). A crude argon stream (76, 176, 276a, 276b) is removed from the crude argon column (25) or the top condenser (24). The crude argon stream (76, 176, 276a, 276b) is sent to a pure argon column (20). A pure argon product stream (81) is removed from the pure argon column (20).

Abstract: The process serves for generating a pressurized product by low-temperature air fractionation. Feed air (1) is compressed (2), purified (4), cooled (9) and fed to a distillation column system (12) for nitrogen-oxygen separation (11, 23). A liquid product stream (13) is taken off from the distillation column system (12) for nitrogen-oxygen separation, brought (14) in the liquid state to an elevated pressure (PIV) and at this elevated pressure (PIV) vaporized or pseudovaporized (9). The (pseudo)vaporized product stream (16) is fed (17) as pressurized product to a gas pressure reservoir (19) which has a variable pressure (PA). The elevated pressure (PIV) is varied. The elevated pressure (PIV) is varied as a function of the pressure (PA) of the gas pressure reservoir (19).

Abstract: A plate heat exchanger for indirect heat exchange of several fluid flows (30, 40, 50) with a heat transfer medium/cooling medium (10, 20) in a heat exchanger core (9) has a plurality of heat exchange passages within the core for the heat transfer medium/cooling medium (10, 20), a first fluid flow (30, 40, 50) and a second fluid flow (30, 40, 50). All heat exchange passages for the first fluid flow (40) are located In a first component area, and all heat exchange passages for the second fluid flow (30) are located in a second component area. The first and the second component areas do not intersect and each extend over the entire height of the heat exchanger core (9). The heat exchanger is particularly suitable for use in air-separation processes.

Abstract: The invention relates to a bath condenser with a condenser block (1) that has evaporation passages (8) for a liquid and liquefaction passages (2) for a heating medium and at least two circulation sections (7) that are located vertically on top of one another. The evaporation passages (8) each have on the lower end of a circulation section (7) at least one entry opening (9) for the liquid and on the upper end of a circulation section (7) at least one exit opening (10), for each circulation section (7) there being a liquid storage tank (15) that is flow-connected to the entry opening (9) and the exit opening (10) of the circulation section (7) and that has a gas offtake (18). The inlet into the gas offtake (18) is not located in the area in front of the side (12) of the circulation section (7) in which the exit opening (10) of the circulation section (7) is located.

Abstract: The invention relates to a process for the low-temperature fractionation of air in a rectification unit, which comprises a pressure column (1) a low-pressure column (2) and a condenser-evaporator system having at least two falling-film evaporators (203, 204). Oxygen-rich liquid from the low-pressure column (2) is introduced into the evaporation passages of the first and second falling-film evaporators (203, 204) and is partially evaporated. Unevaporated oxygen-rich liquid from the first falling-film evaporator (203) is transferred into the evaporation passages of the second falling-film evaporator (204).

Abstract: The invention relates to a bath condenser with a condenser block (1) that has evaporation passages (8) for a liquid and liquefaction passages (2) for a heating medium and at least two circulation sections (7) that are located vertically on top of one another. The evaporation passages (8) each have on the lower end of a circulation section (7) at least one entry opening (9) for the liquid and on the upper end of a circulation section (7) at least one exit opening (10), for each circulation section (7) there being a liquid storage tank (15) that is flow-connected to the entry opening (9) and the exit opening (10) of the circulation section (7) and that has a gas offtake (18). The inlet into the gas offtake (18) is not located in the area in front of the side (12) of the circulation section (7) in which the exit opening (10) of the circulation section (7) is located.

Abstract: A plate heat exchanger for indirect heat exchange of several fluid flows (30, 40, 50) with a heat transfer medium/cooling medium (10, 20) in a heat exchanger core (9) has a plurality of heat exchange passages within the core for the heat transfer medium/cooling medium (10, 20), a first fluid flow (30, 40, 50) and a second fluid flow (30, 40, 50). All heat exchange passages for the first fluid flow (40) are located In a first component area, and all heat exchange passages for the second fluid flow (30) are located in a second component area. The first and the second component areas do not intersect and each extend over the entire height of the heat exchanger core (9). The heat exchanger is particularly suitable for use in air-separation processes.

Abstract: The invention relates to a process for the low-temperature fractionation of air in a rectification unit, which comprises a pressure column (1) a low-pressure column (2) and a condenser-evaporator system having at least two falling-film evaporators (203, 204). Oxygen-rich liquid from the low-pressure column (2) is introduced into the evaporation passages of the first and second falling-film evaporators (203, 204) and is partially evaporated. Unevaporated oxygen-rich liquid from the first falling-film evaporator (203) is transferred into the evaporation passages of the second falling-film evaporator (204).

Abstract: The process and device are used to obtain a compressed product by low temperature separation of air in a rectification system which has a pressure column and a low pressure column. A first flow of compressed and purified feedstock air is cooled in a main heat exchanger system and is fed into the pressure column. At least one fraction from the pressure column is expanded and fed into the low pressure column. An oxygen-rich fraction from the low pressure column is liquid-pressurized and delivered to a mixing column. A heat exchange medium is fed into the lower area of the mixing column and is brought into countercurrent contact with the oxygen-rich fraction. A gaseous top product is removed from the upper area of the mixing column. A product fraction is removed from the rectification system, liquid-pressurized, vaporized in indirect heat exchange with the gaseous top product of the mixing column and is withdrawn as the compressed product.

Abstract: For the indirect heat-exchange of a plurality of gas streams (14, 15, 16) with a heat-cold carrier (2, 7) in heat-exchange blocks (23a, b, c, d, e) in which the gas streams (14, 15, 16) are passed through a multiplicity of heat-exchange passages, only one of the gas streams (14, 15, 16) is passed in this case through at least one heat-exchange block (23a, b, c, d, e). The heat-exchange passages of the heat-exchange block (23a, b, c, d, e), through which this gas stream (14, 15, 16) flows end at two end surfaces of the heat-exchange block (23a, b, c, d, e). The gas stream (23a, b, c, d, e) is fed to an taken off from these heat-exchange passages via in each case a collector/distributor (41) connected to the heat-exchange block (23a, b, c, d, e), which collector/distributor extends in each case over the entire end surface of the heat-exchange block (23a, b, c, d, e).

Abstract: For adjusting the capacity of a low-temperature rectification unit having a high pressure column and a low pressure column in which a fluid is introduced into the high pressure column (1) and in which liquid from the bottom of the high pressure column is directed into the low pressure column (2), the amount of liquid that is removed from the bottom of high pressure and fed to the low pressure column (2) is controlled via flow adjustment (4), wherein a nominal value for flow adjustment (4) is set to a desired amount of flow, and the liquid level of the liquid at the bottom of column (1) that operates at higher pressure is fixed without a set nominal value corresponding to the amount of liquid that is removed.

Abstract: The process and device are used to obtain a compressed product by low temperature separation of air in a rectification system which has a pressure column and a low pressure column. A first flow of compressed and purified feedstock air is cooled in a main heat exchanger system and is fed into the pressure column. At least one fraction from the pressure column is expanded and fed into the low pressure column. An oxygen-rich fraction from the low pressure column is liquid-pressurized and delivered to a mixing column. A heat exchange medium is fed into the lower area of the mixing column and is brought into countercurrent contact with the oxygen-rich fraction. A gaseous top product is removed from the upper area of the mixing column. A product fraction is removed from the rectification system, liquid-pressurized, vaporized in indirect heat exchange with the gaseous top product of the mixing column and is withdrawn as the compressed product.

Abstract: For the indirect heat-exchange of a plurality of gas streams (14, 15, 16) with a heat-cold carrier (2, 7) in heat-exchange blocks (23a, b, c, d, e) in which the gas streams (14, 15, 16) are passed through a multiplicity of heat-exchange passages, only one of the gas streams (14, 15, 16) is passed in this case through at least one heat-exchange block (23a, b, c, d, e). The heat-exchange passages of the heat-exchange block (23a, b, c, d, e), through which this gas stream (14, 15, 16) flows end at two end surfaces of the heat-exchange block (23a, b, c, d, e). The gas stream (23a, b, c, d, e) is fed to an taken off from these heat-exchange passages via in each case a collector/distributor (41) connected to the heat-exchange block (23a, b, c, d, e), which collector/distributor extends in each case over the entire end surface of the heat-exchange block (23a, b, c, d, e).

Abstract: The process and the apparatus are used for the low-temperature fractionation of air in a three-column system which has a high-pressure column (5), a low-pressure column (7) and a medial column (6). Charge air (1, 2, 4) is introduced into the high-pressure column (5), where it is separated into a first oxygen-enriched liquid and a first nitrogen fraction (16). At least a part (19) of the first nitrogen fraction (16) is condensed in a first condenser/evaporator (8) to form a first liquid nitrogen fraction (20). A first oxygen-enriched fraction (22) from the high-pressure column (5) is introduced into the medial column (6), where it is separated into a second oxygen-enriched liquid and a second nitrogen fraction (24). At least a part of the second nitrogen fraction (24) is condensed in a second condenser/evaporator (25) to form a second liquid nitrogen fraction (26) and is added as reflux to one of the columns of the three-column system and/or is obtained as liquid product (64).

Abstract: For adjusting the capacity of a low-temperature rectification unit having a high pressure column and a low pressure column in which a fluid is introduced into the high pressure column (1) and in which liquid from the bottom of the high pressure column is directed into the low pressure column (2), the amount of liquid that is removed from the bottom of high pressure and fed to the low pressure column (2) is controlled via flow adjustment (4), wherein a nominal value for flow adjustment (4) is set to a desired amount of flow, and the liquid level of the liquid at the bottom of column (1) that operates at higher pressure is fixed without a set nominal value corresponding to the amount of liquid that is removed.

Abstract: The method and the device are used for the cryogenic separation of air. Compressed and purified application air (9, 10, 20) is cooled in a main heat exchanger (30) and is at least partially fed (12, 33) to a rectifying column (50). A first partial flow (26) of the application air is fed to the main heat exchanger (30), is at least partially withdrawn at a first intermediate temperature from the main heat exchanger (28), and is fed to a cold compression (29). The first partial flow (26) is warmed up (27) upstream of its withdrawal (28) at the first intermediate temperature in the main heat exchanger (30).

Abstract: The process and the apparatus serve to produce pressurized nitrogen by low-temperature fractionation of air in a rectification system which has a pressure column (4) and a low-pressure column (5). Feed air (1, 3) is passed into the pressure column (4). An oxygen-containing liquid fraction (11) is taken off from the pressure column (4) and fed into the low-pressure column (5). Gaseous nitrogen (18) from the low-pressure column (5) is at least partially condensed in a top condenser (17) by indirect heat exchange with an evaporating liquid (13). Nitrogen from the low-pressure column is produced as gaseous pressurized nitrogen product (24, 25, 29) at a pressure which is higher than the operating pressure of the low-pressure column (5). Liquid nitrogen (20) withdrawn from the low-pressure column is brought (21) in the liquid state to a pressure which exceeds the pressure of the low-pressure column (5).

Abstract: A process and a system for the low-temperature separation of air by rectification is provided. A liquid fraction is obtained in a rectifying system, stored in a tank and at least a portion of the liquid fraction taken out of the tank and brought to an increased pressure. During normal operation, the liquid fraction, which was brought to an increased pressure, is heated in a preheat exchanger and evaporated in the main heat exchanger. During an operating disturbance, at least a portion of the liquid product is removed from the tank, evaporated and used for an emergency supply.

Abstract: Feed air is fed to a rectifying system (14, 15) for low-temperature separation, from which a liquid fraction (31, 32) is taken off and introduced into a first reservoir tank (33). The pressure of a variable rate of the liquid fraction (34) is increased (35). The liquid fraction (36) is evaporated under the elevated pressure by indirect heat exchange (12) and obtained as a gaseous pressurized product (37). A heat-transport medium circulates in a refrigeration cycle which has a cycle compressor (41, 42). A first partial stream (45) of the heat-transport medium (44) compressed in the cycle compressor (41, 42) is fed to the indirect heat exchange (12) to evaporate the liquid fraction (36) and is liquefied, at least in part, in the course of this. A second partial stream (59) of the heat-transport medium (44) compressed in the cycle compressor (41, 42) is expanded (43) so as to perform work. Liquefied heat-transport medium (45, 48) is buffered in a second reservoir tank (49).

Abstract: A process and apparatus for recovery of pure argon from air utilize a rectification system comprising at least one air separating column (9) and a pure argon column (25). An argon-enriched mixture (24) of air gases is introduced into the pure argon column (25) in the lower region of which an essentially nitrogen-free argon product (26) is recovered. The head fraction (28) of the pure argon column (25), is liquefied at least partly by indirect heat exchange (29) using the evaporating cooling medium (11, 30). The condensate (28a) formed thereby is returned into the pure argon column. The indirect heat exchange (29) is carried out by means of a cooling medium (11, 30) which has an oxygen content of at least 10%. Independently thereof, the lower region of the pure argon column (25) is heated by indirect heat exchange (27) by means of a heating medium (11) in a liquid state, for example, with sump liquid from a pressure column (8).