Linde Aktiengesellschaft

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Dietrich Rottmann

Horst Corduan

Christian Kunz

Alfred Wanner

Karl Heinrich Schweigert

Karl Leibl

Juergen Voit

Wolfgang Haag

A plate heat exchanger for indirect heat exchange of several fluid flows () with a heat transfer medium/cooling medium () in a heat exchanger core () has a plurality of heat exchange passages within the core for the heat transfer medium/cooling medium (), a first fluid flow () and a second fluid flow (). All heat exchange passages for the first fluid flow () are located In a first component area, and all heat exchange passages for the second fluid flow () 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 (). The heat exchanger is particularly suitable for use in air-separation processes.

Plate heat exchanger

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

Multistory bath condenser

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

Low-temperature air fractionation process

A process and apparatus for low-temperature fractionation of air in a distillation column system for nitrogen-oxygen separation ( ) introduces into first feed air stream ( ) into a distillation column system for nitrogen-oxygen separation. An oxygen-rich fraction ( ) from the distillation column system for nitrogen-oxygen separation is pressurized ( ) in liquid form and is added ( ) to a mixing column ( ). A heat transfer medium stream is introduced into the lower region of the mixing column ( ) and is brought into countercurrent contact with the oxygen-rich fraction ( ). Gaseous top product ( ) from the upper region of the mixing column ( ) is introduced into an additional column ( ). A liquid ( ) from the lower or middle region of the mixing column is introduced into the distillation column system. A krypton- and xenon-containing oxygen stream ( ) from the distillation column system is introduced into a krypton-xenon enriching column ( ) from which a krypton- and xenon-enriched fraction ( ) is obtained. A krypton- and xenon-depleted top fraction ( ) is obtained from the upper region of the additional column ( ).

Air fractionation process and installation with mixing column and krypton-xenon recovery

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. Indirect heat exchange is carried out for vaporization of the liquid-pressurized product fraction in the main heat exchanger system.

Process and device for obtaining a compressed product by low temperature separation of air

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

Process and apparatus for heat exchange

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 ( ) and in which liquid from the bottom of the high pressure column is directed into the low pressure column ( ), the amount of liquid that is removed from the bottom of high pressure and fed to the low pressure column ( ) is controlled via flow adjustment ( ), wherein a nominal value for flow adjustment ( ) is set to a desired amount of flow, and the liquid level of the liquid at the bottom of column ( ) that operates at higher pressure is fixed without a set nominal value corresponding to the amount of liquid that is removed.

Adjustment process for a low-temperature rectification unit

In a single column distillation system for obtaining gaseous and liquid nitrogen with a variable proportions of liquid product by low-temperature separation from air, a first portion ( ) of nitrogen-rich fraction ( ) is fed downstream of circulation compressor ( ) to the liquefaction chamber of a condenser-evaporator ( ) associated with the single column and condensed under a pressure higher than the operating pressure of the single column ( ). A liquid oxygen-enriched fraction ( ) from the distillation column system is at least partially evaporated in the evaporation chamber of condenser-evaporator ( ). A portion ( ) of nitrogen-rich liquid ( ) from condenser-evaporator ( ) is drawn off at least at times as liquid product. A second oxygen-enriched gas ( ) is removed from one of columns ( ) of the distillation system and/or from the evaporation chamber of condenser-evaporator ( ), machine expanded( ), and heated in main heat exchanger ( ).

Process for obtaining gaseous and liquid nitrogen with a variable proportion of liquid product

For obtaining gaseous nitrogen by low-temperature separation from air, a distillation column system has a single column ( ). Compressed air ( ) is cooled in a main heat exchanger ( ) and fed ( ) to single column ( ). A nitrogen-rich fraction ( ) is drawn off from the distillation column system and compressed at least in part in a circulation compressor ( ). A first part ( ) of nitrogen-rich fraction ( ) is fed downstream from circulation compressor ( ) to the liquefaction chamber of a condenser-evaporator ( ) and is condensed under a pressure higher than the operating pressure of single column ( ), so to form nitrogen-rich liquid ( ). A liquid oxygen-enriched fraction ( ) from the distillation column system is at least partially evaporated in the evaporation chamber of condenser-evaporator ( ). A first oxygen-enriched gas ( ) formed in the evaporation chamber of condenser-evaporator ( ), is introduced into single column ( ). A second portion ( ) of the nitrogen-rich fraction ( ) is drawn off at least at times as gaseous nitrogen product. A second oxygen-enriched gas ( ) is removed from the evaporation chamber of condenser-evaporator ( ), work expanded ( ), and heated in main heat exchanger ( ).

Process for obtaining gaseous nitrogen

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 (,) and a low-pressure column (,). Feed air (,) is passed into the pressure column (,). An oxygen-containing liquid fraction (,) is taken off from the pressure column (,) and fed into the low-pressure column (,). Gaseous nitrogen (,) from the low-pressure column (,) is at least partially condensed in a top condenser (,) by indirect heat exchange with an evaporating liquid (,). Nitrogen from the low-pressure column is produced as gaseous pressurized nitrogen product (,) at a pressure which is higher than the operating pressure of the low-pressure column (,). Liquid nitrogen (,) withdrawn from the low-pressure column is brought (,) in the liquid state to a pressure which exceeds the pressure of the low-pressure column (,). The pressurized liquid (,) is evaporated in a product evaporator (,) by indirect heat exchange with a heat-transfer medium (,) and is subsequently produced as gaseous pressurized nitrogen product (,). (FIG.,)

Method and device for producing compressed nitrogen

In the method and device, nitrogen is obtained by two-stage rectification of air in a double column. Double column contains a high-pressure column and a medium-pressure column that are in a heat-exchange relationship with each other. Entering air is compressed, purified, cooled in a main heat exchanger against separation products, and fed to rectification. At least one nitrogen product fraction is taken from high-pressure column. A nitrogen gas fraction from double column is heated, expanded, and brought into indirect heat exchange with an oxygen-enriched liquid from the lower region of medium-pressure column. In this way, the nitrogen gas fraction is at least partially condensed and the oxygen-enriched liquid is at least partially evaporated. The condensate formed in the indirect heat exchange is at least partially fed to medium-pressure column. The nitrogen gas fraction is heated upstream of expansion to an intermediate temperature that is between the temperatures at the cold end and the warm end of main heat exchanger.

Method and device for obtaining nitrogen by low-temperature separation

The method and the apparatus are used to obtain oxygen and nitrogen at superatmospheric pressure by low-temperature separation of air in a rectification column system. Compressed and purified feed air (1, 3) is introduced into a pressure column (4). Liquids (5, 8) from the lower region and, respectively, from the upper or middle region of the pressure column (4) are fed into the low-pressure column (7). A third liquid fraction (17) from the lower region of the low-pressure column (7) is evaporated in indirect heat exchange (12) with condensing vapour (11) from the upper region of the pressure column (4), at least a portion of the vapour (22, 24, 26, 27) obtained in the process being introduced into the low-pressure column (7). Condensate (13) is fed into the pressure column (4); A pressurized nitrogen fraction (10, 14, 15) is extracted as product from the upper region of the pressure column (4). The pressure of the third liquid fraction (17) from the lower region of the low-pressure column (17) is increased upstream of the indirect heat exchange (12); that portion (24) of the vapor which is obtained during the indirect heat exchange and led back into the low-pressure column is expanded (25) before being introduced (27) into the low-pressure column (7).

Method and device for obtaining oxygen and nitrogen at superatmospheric

For air fractionation by two-stage rectification with subsequent production of crude argon, a component stream of the crude argon stream (25, 31) withdrawn from the crude argon column (2) is condensed (35) in indirect heat exchange (34) with a liquid oxygen product stream (40) from the medium pressure column (4), the oxygen product stream (40) being partially vaporized. The condensed crude argon (35) is then recycled into the crude argon column (20). A second component stream of the crude argon is obtained as the product (24).

Process and apparatus for air fractionation by rectification

A process and an apparatus are disclosed for air fractionation by means of rectification. Nitrogen (16) withdrawn from the process is heated to an intermediate temperature, withdrawn, in part (30), out of the primary heat exchanger (17), and engine-expanded (31). The resultant expanded gas (32) transfers its cold in the primary heat exchanger (17) to air to be fractionated (1) and is then recompressed (33, 36).

An air separation system is provided comprising a double rectification column associated with a raw argon column, the latter being operated at a pressure substantially lower than the low-pressure part of the double column. A coupled turbine-compressor system is used: (a) to lower the pressure of the argon-containing gas entering a raw argon column from the low-pressure column; and (b) to compress evaporated liquid stemming from the high-pressure column which has been used to indirectly condense raw argon product at the top of the raw argon column. Also, a pump is employed to remove liquid from the bottom of the raw argon column and recycle it to the low-pressure column.

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Munich, Germany

Dietrich Rottmann