Abstract: Nitrogen is rejected from a pressurized feed gas stream comprising methane and nitrogen by cooling the feed gas stream in a main heat exchanger and rectifying the cooled feed gas stream in a double rectification column comprising a higher pressure rectification column, a lower pressure rectification column, and a condenser-reboiler placing the higher pressure column in heat exchange relationship with the lower pressure column. A pump withdraws a methane product stream from the column. The methane product stream is pressurized by the pump and is vaporized in the main heat exchanger. The pressurized feed gas stream is expanded with the performance of external work in an expansion turbine 6 upstream of the main heat exchanger.

Abstract: In order to provide `ultra high purity` nitrogen having diminished concentrations of light and heavy impurities in comparison with nitrogen produced by conventional cryogenic air separation, the nitrogen product from a conventional cryogenic air separation column is introduced into the bottom of a liquid-vapor contract column 2 fitted with a condenser 8 to provide reflux. A liquid nitrogen stream having a reduced concentration of heavy impurities is withdrawn from the column 2 through an outlet 22 situated at a level a few trays below the top tray in the column 2. The liquid nitrogen is then subjected to two stages of flash separation. In the first stage the liquid is passed through valve 24 into a phase separator 26. In the second stage, the resulting liquid from the first stage, having a reduced concentration of light impurities, is passed through valve 32 into a phase separator 34. Liquid nitrogen product is withdrawn from the phase separator 34 through outlet 38.

Abstract: Air is fractionated in a double distillation column comprising lower pressure and higher pressure columns. A condenser/reboiler provides reboiled oxygen to the bottom of the column. Liquid nitrogen reflux is introduced into the top of the column. Oxygen, nitrogen and argon-enriched streams are withdrawn from the column. The argon-enriched stream is separated in a further distillation column and a product argon stream is withdrawn therefrom. A liquid stream comprising oxygen and nitrogen is withdrawn from an intermediate level of the column, is at least partially reboiled in a heat exchanger, and is returned to the column at a level where the composition of the vapor corresponds approximately to that of the reboiled liquid. Heating for the heat exchanger is provided by a fluid stream withdrawn from the second distillation column. The fluid stream is returned to the second column.

Abstract: A method of liquefying a permanent gas stream includes the step of reducing the temperature of the permanent gas stream at elevated pressure to below its critical temperature. The reduction in temperature is effected at least in part by countercurrent heat exchange with work expanded working fluid, at least some of which is at a temperature below the critical temperature of the permanent gas when it is brought into heat exchange relationship with the permanent gas stream. The permanent gas stream after being cooled to below its critical temperature is then subjected to at least three successive isenthalpic expansions. Resulting flash gas is separated from the resulting liquid. At least some of the flash gas is heat exchanged with the permanent gas stream at elevated pressure.

Abstract: A method of liquefying a permanent gas stream, includes the steps of reducing the temperature of the permanent gas stream at elevated pressure to below its critical pressure and performing at least two working fluid cycles to provide at least part of the refrigeration necessary to reduce the temperature of the permanent gas to below its critical temperature. Each working fluid cycle comprises work-expanding the cooled working fluid in countercurrent heat exchange with the permanent gas stream and with the working fluid being cooled, refrigeration thereby being provided for the permanent gas stream. In at least one working fluid cycle, work-expanded working fluid is brought into countercurrent heat exchange relationship with the permanent gas stream at a temperature below the critical temperature of the permanent gas and in the or each such cycle on completion of the work expansion the working fluid is at a pressure of at least 10 atmospheres.