US3389565A - Process for liquefaction of helium by expansion - Google Patents

Process for liquefaction of helium by expansion Download PDF

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US3389565A
US3389565A US449744A US44974465A US3389565A US 3389565 A US3389565 A US 3389565A US 449744 A US449744 A US 449744A US 44974465 A US44974465 A US 44974465A US 3389565 A US3389565 A US 3389565A
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gas
temperature
pressure
expansion
liquefaction
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Ergenc Sahabettin
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Sulzer AG
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Sulzer AG
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
    • F25J1/0224—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an internal quasi-closed refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0005—Light or noble gases
    • F25J1/0007—Helium
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops

Definitions

  • One stream is returned through one or more of the heat exchangers through which the compressed gas flows prior to throttling, and is raised in temperature in the process.
  • This one stream is then passed through an expansion turbine wherein its pressure is lowered to the vicinity of the liquefaction pressure of the gas, whereafter it is heated substantially to room temperature by heat exchange with compressed gas which has not been throttled, being then recycled to the compressor.
  • the other stream of gas after further cooling, is further expanded in a second throttling step, undergoing partial liquefaction in the process. Unliqueed gas and liquefied gas which undergoes revaporization is combined with that flowing through the expansion turbine for return to the compressor.
  • the present invention pertains to a process and apparatus for the liquefaction of a gas having a low boiling point, such as helium.
  • a gas having a low boiling point such as helium.
  • the gas is first compressed to a high pressure, preferably above its critical pressure. It is then cooled by a heat exchange process and thereupon partially liquefied by'expansion in a throttling step. Processes of this kind are employed either for production of low temperatures or for the purpose of obtaining the liquefied gas as an end product.
  • the Joule-Thomson effect becomes positive if the enthalpy of the gas at high pressure and at the intermediate temperature just referred to is less than the enthalpy of the gas throttled to lower pressure but at the same temperature.
  • the throttling effect i.e. the difference in enthalpy between the gas stream throttled to lower pressure and the compressed gas at the intermediate temperature, corresponds to the quantity of heat which can be removed from the gas when it is in the range of temperatures from the intermediate temperature downward. This quantity of heat is, in the most ⁇ favorable case, equivalent to the amount of thermal energy removed in that range of temperatures 3,389,565 Patented June 25, 1968 example, through introduction of heat from the outside.
  • the magnitude of. the enthalpy difference is determinative for the cooling achieved.
  • the magnitude of the enthalpy difference depends in the first instance on the value of the intermediate temperature with which it is associated and additionally on the pressure values before and after throttling.
  • the enthalpy difference increases with declining temperature and, generally, with increase in difference in pressure between the pressures prior to and after the throttling, as may be Seen from the usual graphic plots such as the temperature-entropy diagrams of, for example, helium.
  • the first stream abstracts heat from high pressure gas not having undergone the expansion step, before being aspirated, in the range of ambient temperatures, by a compressor.
  • the second partial stream is subjected to further expansion in a second throttling valve, and the liquefied fraction so obtained is separated 0E.
  • the remainder including any revaporized gas, passes as a heat absorption medium in heat exchange relation with gas at high pressure until it is rewarmed to the vicinity of ambient temperature.
  • the quantity of heat, which must be withdrawn from the gas to achieve the said intermediate temperature below the inversion temperature of the gas corresponds to the so-called cooling energy requirement in this range of temperatures, i.e. between the ambient temperature and the said intermediate temperature.
  • a portion of the energy required to be removed from the gas in order to cool it is so removed, after initial compression of the gas, by expansion of the gas in expansion turbines with performance of external work.
  • a portion of the energy required to be removed from a gas for cooling is removed therefrom by exterior sources of cold, in place of the expansion with performance of external work. That is to say., energy is removed lfrom the gas to be cooled by transfer thereof to those sources of cold acting as a heat sink.
  • the second partial stream is cooled by heat exchange with non-liquefied gas expanded in said second throttling step.
  • the first partial stream after being raised in temperature by heat exchange in at least one exchanger with gas at high pressure, is expanded with performance of work in an expansion stage and is thus brought down approximately to the pressure at which part of the second partial stream is liquefied.
  • the rst partial stream can undergo cooling by heat exchange between two successive stages of such expansion.
  • This third partial gas stream is then cooled by heat exchange and by expansion with performance of Work, from ambient temperature down approximately to that exhibited by the rst partial stream after being warmed by heat exchange Iwith gas at high pressure which has not undergone the first throttling expansion.
  • This third partial stream is then expanded, together with the gas in the first partial stream, down to the pressure exhibited by the second partial stream after the separate throttling undergone by that second partial stream.
  • Another mode of achieving part of the necessary energy removal which can be employed is ,one in which part of the high pressure gas is expanded with performance of work down to the intermediate pressure and is then cornbined with the first partial stream after the latter has passed through the heat exchanger immediately upstream of the throttling step for the high pressure gas.
  • the two streams so combined are then raised in temperature subsantially to ambient by heat exchange with high pressure gas and are compressed to high pressure.
  • a particularly advantageous application of the process of the invention resides in the liquefaction of helium.
  • FIGS. 1 to 5 are schematic diagrams of various forms of apparatus according to the invention suitable for carrying out the process of the invention.
  • the gas to be liquefied is compressed in a compressor 1, preferably to supercritical pressure.
  • the compressed gas then passes through an after cooler 2 for removal of the heat of compression. It then passes through heat exchangers 4, 5, 6 and 7 which may advantageously be of so-called plate-fin type.
  • the gas is cooled by heat exchange with cooler gas flowing counter-current therewith, the operation of these heat exchangers being explained in greater detail hereinafter.
  • the gas so cooled conveniently called high pressure gas in View of its subsequent reduction in pressure, is thereupon passed through one or the other of two adsorbers 8 and 9 for removal of residual impurities.
  • the adsorbers 8 and 9 are used alternately, the one not in use undergoing regeneration.
  • the high pressure gas has by now been cooled to what has hereinabove been referred to as the intermediate temperature, to be designed TVI, which lies below the inversion temperature of the gas.
  • the high pressure gas is then further cooled in a heat exchanger 10 and is then expanded by passing through the throttling valve 11 down to an intermediate pressure.
  • the value of this intermediate pressure is so chosen that in being expanded thereto the gas undergoes a cooling, to a temperature TVH below TVI, but no liquefaction.
  • the iiow channel from compressor 1 to the low pressure side of throttling valve 11 will be designated 2l.
  • a junction 22 from which one line 23 leads back through exchangers 10 and 7 to a junction 24, while another line 25 leads through an exchanger 16 and second throttling valve 17 into a liquid gas reservoir vessel 18.
  • the gas expanded in valve 11 is divided at junction 22 into two streams. The first of these is led vvia line v23 back through the heat exchanger 1i). In passing through exchanger 10 this stream absorbs heat from the gas flowing from the loutlet end of the adsorbers S and 9 toward the throttling valve 11 and is raised in temperature to the vicinity of the precooling temperature TVI. It then flows on back through the heat exchanger 7 where it also absorbs heat.
  • the first partial stream is combined with another stream owing in a channel 26 from compressor 12 to junction 24.
  • the gas stream flowing in channel 26 has been raised by compressor 12 to a pressure intermediate the inlet and outlet pressures at the throttling valve 11.
  • the gas stream then passes through an after cooler 13 for dissipation of the heat of compression and through the heat exchanger 4 in which it is cooled. It thereupon ows through the expansion turbine 14 and lastly through the exchanger 6 where it undergoes further cooling to a temperature close to that of the first partial gas stream arriving at junction 24.
  • the two gas streams so combined are then passed through expansion turbine 15 in which they are reduced to a pressure close to that of liquefaction for the gas in question.
  • the second partial gas stream divided off at this outlet passes at a precooling temperature TVH via channel 25 into a heat exchanger 16 in which it is further cooled.
  • a throttling valve 17 Upon emerging from the exchanger 16 it is further expanded in a throttling valve 17 whereupon it undergoes partial liquefaction.
  • the liquefied fraction is captured in a container 18 from which the liquefied product passes through a withdrawal line 19 having a valve 20 therein.
  • the helium may be compressed in compressor 1 to a pressure of approximately 18 atmospheres, and it may be reduced at the throttling valve 11 to an intermediate pressure of about 3 atmospheres, which latter pressure it will be noted is still above the critical pressure for helium.
  • atmospheres means atmospheres absolute.
  • helium is compressed to about 7 atmospheres and it is expanded in the turbine 14 to about 3 atmospheres, and in the turbine l5 to a pressure somewhat below the liquefaction pressure of helium, which is about 1.25 atmospheres.
  • the intermediate temperature TVI amounts in this example to about y6" Kelvin and the temperature TVH downstream of the first throttling valve 11 is about 5.4" Kelvin, whereas the liquefaction temperature in the container 18 amounts for the assumed pressure of 1.25 atmospheres to some 4.5a Kelvin.
  • a 'portion of the energy required to be removed from the gas to effect cooling is delivered by the gas to exterior sources of cold, in place of the expansion of the gas with performance of external work which is employed in the embodiment of FIG. l.
  • the elements in the system of FIG. 2 corresponding to those of FIG. 1 are identified with similar reference characters.
  • the embodiment of 'FIG. 2 is likewise adapted to the liquefaction of helium.
  • a vessel containing liquid nitrogen and a vessel 31 containing "liquid hydrogen are provided as sources of cold or low temperature.
  • Liquid nitrogen is supplied to the container 30 ⁇ via line 32.
  • Vaporized nitrogen passes from the container 3d through a heat exchanger 33, absorbing heat therein, and thence via a line 34 out of the system.
  • the vessel 31 is fed with liquid hydrogen through aline 35, and from this vessel vaporized hydrogen passes through heat exchangers 36 and 33, also absorbing heat therein, and thence via a line 37 out of the system.
  • the helium compressed in the compressor 1 is, after dissipation of its heat of compression in an after cooler 2, passed through the heat exchanger 33.
  • the high lpress-ure gas thus further cooled is thereupon -passed through the heat exchanger 36 where it fiows in heat exchange relation with vaporized hydrogen developed in the vessel 31, and with vaporized helium in channel 51 ⁇ from the vessel 18 and with the first partial gas stream in channel 23.
  • After purification in one of the adsorbers 8 and 9 it passes through a heat exchange -coil 39l in the liquid space of the hydrogen vessel 31 so that its temperature is reduced to the first intermediate temperature TV1.
  • the remaining steps of the process so far as corresponding to that of the embodiment of FIG. l will not be restated.
  • the first partial gas stream beginning at the intermediate pressure at the outlet valve 11, is not thereafter expanded with performance of work. Rather, after heating in the exchangers 1f), 36 and 33, it is returned to channel 211 downstream of the first stage 1a of the compressor' and upstream of the second stage 1.
  • the after cooler for dissipation of compressor heat downstream of the first stage ofthe compressor is identified by reference 2a.
  • the gas is raised to the selected high pressure in a single stage compressor 1.
  • a single stage compressor 1 After precooling in an after cooler 2 it is reduced in temperature to the first intermediate ⁇ or precooling temperature T VI in exchangers 40, 41 and '42 of channel 21, where it passes in heat exchange relation with a first partial 4stream owing in a channel 53.
  • the gas in channel 21 is then further cooled7 in exchanger 43, by the counter-flowing gas in channel 53, and is then reduced in v the throttling valve 11.
  • the first partial stream is fed Iback by channel 53 through the exchangers 43, 42 and 41 and is heated thereby. It is then expanded in the expansion turbine 44.
  • the gas so cooled in turbine 44 is further cooled in exchanger 41 and is lastly reduced in pressure by expansion in expansion turbine 45 to a pressure below the liquefaction pressure in the vessel 1S.
  • the gas vaporizing out of the vessel 18 flows through a channel 54 where it is heated substantially to the initial intermediate temperature TVI in heat exchangers 16 and 43, this Ibeing the temperature of the high pressure gas in channel 21 at its outlet from exchanger 42.
  • the gas in channel 54 is then combined at a junction S5 with the ⁇ gas expanded in the expansion turbine 4S and is passed via a channel 55 through the exchangers 42, 41 and 4d in which it is raised to ambient temperature before being supplied to the input side of compressor 1.
  • the cooling energy requirement corresponding to passage from the initial intermediate temperature TVI up to ambient i.e. the thermal energy required to be removed fro-m the gas, is supplied essentially by expansion of the first partial stream with performance of work.
  • FIG. 4 illustrates a further embodiment of the invention constituting a variant on the embodiment of FIG. 3 as regards the initial cooling of the gas to be liquefied from ambient down to the first intermediate temperature TV1.
  • the four heat exchangers upstream of the first throttling ofI the high pressure gas are identified with reference characters 4t) to 43.
  • the cooling load to be met in reducing the temperature of the gas to be liquefied from ambient to the first intermediate temperature TVI is supplied by expansion with performance of work of a portion of the high pressure gas compressed in compressor 1.
  • a portion of the gas compressed in compressor 1 and cooled in the exchanger 4t) down below ambient temperature is split off from channel 21 at a junction 53 and sent through a channel 59, wherein it is expanded in an expansion turbine 46 approximately to the intermediate pressure of the tirst partial stream in channel 60. It is then further cooled in the exchanger 41 approximately to the temperature of the first partial stream upon the emergence of the latter from exchanger 42. It is thereupon combined with that first partial stream at a junction 61 of the channels 59 and 60,
  • the gas streams so combined are thereupon expanded in an expansion turbine 47 substantially to the liquefaction pressure of the gas in the container 18 and are combined at a junction 62 with gas vaporizing out of that container through a channel 63, after heating of the latter in the exchangers 16 and 43 substantially to the precooling temperature TVI.
  • the gas streams combining at junction 62 are fed together to the compressor 1 through a channel 64, in which they are raised substantially to ambient temperature in the exchangers 42, 41 and 40.
  • the cooling from ambient down to the first intermediate temperature TVI is, as in the embodiment of FIG. 4, effected by expansion, with the performance of work, of a portion of the high pressure gas.
  • This gas is in the embodiment of FIG. 5 compressed in a two-stage cornpressor.
  • the fraction of the gas led off downstream of the exchanger 443 is passed through two successive stages of expansion with performance of work in the turbines 48 and 49 and is thereby brought down to the intermediate pressure characterizing the high pressure gas after initial throttling and expansion thereof.
  • expansion turbines have been shown, piston machines may be used to the same end. Between the two expansions in turbines 48 and 49 the gas is cooled in a heat exchanger 41.
  • the gas so expanded which has been reduced in temperature approximately to the initial lintermediate temperature TVI, is combined at a junction 65 with the .first partial stream upstream of exchanger i3 and is conducted together with this partial stream through the exchangers 42, 41 and 40 to the suction side of compressor 1.
  • the gas to be liquefied is first compressed. It is then initially cooled to a first intermediate temperature TVI below the inversion temperature of the gas. This initial cooling is effected by expansion of the gas with performance of external work in expansion turbines, or by cooling with the aid of external cooling means to which heat of the gas is transferred by conduction or convection. The gas is then further cooled by heat exchange and is thereafter throttled to a rst intermediate pressure higher than that of liquefaction. By this first throttling there is achieved for the gas a second intermediate temperature TVH which is however above the liquefaction temperature of the gas.
  • a fraction of the gas thus cooled to the second intermediate temperature is then subjected to a second throttling step in the course of which it is at least partially liquefied.
  • the cooling effected on the basis of the Joule-Thomson effect increases, the lower temperature at which it is carried out, as has been already stated. This means that for the achievement of a given cooling, down to the lowest temperature required to be achieved, there is required a smaller expenditure of energy in compression of the gas than would be the case if the gas were throttled directly from the first intermediate temperature to the liquefaction pressure thereof in order to achieve such liquefaction.
  • FIGS. l, 3 and 5 which employ expansion turbines for cooling of the gas, that the thermodynamic losses of such turbines are lower at higher temperature ranges than at lower temperature ranges.
  • the invention provides a process for the liquefaction of a gas of low boiling point, such as helium, comprising the steps of compressing the gas to be liquefied to a high pressure preferably above critical, cooling the compressed gas to a temperature below its inversion temperature, further cooling the gas, expanding the gas without liquefaction thereof in a first throttling step, dividing the gas so expanded into two partial streams, passing a first one of those streams in heat exchange relation with the compressed gas prior to the first throttling step for abstraction of heat therefrom and thereafter recycling the gas in the first stream together with make-up gas, expanding the second stream with partial liquefaction thereof in a second throttling step, and returning the fraction of the gas subjected to the second throttling step and remaining in gaseous condition in counter-current fiow heat exchange relation with the compressed gas prior to said first throttling step.
  • a gas of low boiling point such as helium
  • the invention also provides apparatus for the liquefaction of such a gas comprising means to compress the gas to be liquefied to a high pressure preferably above critical, means to cool the compressed gas to a temperature below the inversion temperature thereof, means to further cool the gas, means to throttle the gas so further cooled, means to conduct a part of the gas so throttled in counter-current -fiow heat exchange relation with the gas so compressed, means to subject to a second throttling a part of the gas so throttled, and means to conduct the gas remaining in a gaseous state after the second throttling in counter-current fiow heat exchange relation with the compressed gas.
  • a process for the liquefaction of helium gas comprising ythe steps of compressing the gas to be liquefied, cooling th-e compressed gas to a temperature below its inversion temperature, expanding all of the gas so cooled without liquefaction of any part thereof in a first throttling step, dividing the gas so expanded into two partial streams, passing a first one of said partial streams in heat exchange relation with the compressed gas prior to said first throttling step for abstraction of heat from such compressed gas, expanding said second partial stream of gas in a second throttling step, and returning the fraction of the gas subjected to said second throttling step remaining in gaseous condition in heat exchange relation With .the compressed gas prior to said rst throttling step for abstraction of heat from such compressed gas.
  • Process according to claim 1 including the further step of subjecting the second partial gas stream, prior to the second throttling thereof, to cooling by heat exchange with nonliquified gas expanded in said second throttling step.
  • Process according to claim 1 including the further step, after passage of the first partial gas stream through at least one stage of heat exchange with said compressed gas, of expanding the gas in the first partial stream with performance of external work substantially to the pressure at which the second partial stream emerges from the second throttling step.
  • Process according to claim 1 comprising the further step of compressing additional gas to a pressure below that of said compressed gas to be liquefied but higher than that to which said compressed gas is reduced in said first throttling step, and cooling said additional gas by heat exchange and by expansion with performance of external Work substantially to the pressure of the gas in the first partial stream after initial heating thereof by heat exchange with said compressed gas, combining said additional gas with the gas in said first partial stream after such initial heating thereof, and expanding said combined gases with performance of external work substantially to the pressure of the gas in said second partial stream after said second throttling step.
  • Process according to claim 1 including the step of expanding a portion of the compressed gas with performance of externa-l work, combining the so-expanded gas with gas in the first partial stream after initial heating thereof in heat exchange relation with said compressed gas, raising the temperature of ythe socombined gas streams substantially to ambient by passing them in counter-current flow heat exchange relation with said compressed gas, and recycling the combined gas streams so raised in temperature.
  • a process for the liquefaction of helium gas comprising the steps of compressing .the gas to be liquefied, cooling the compressed gas to a temperature below its inversion temperature, further cooling the gas, expanding all of the gas so cooled and further cooled without liquefaction of any part thereof in a first .throttling step, dividing the gas so expanded into two partial streams, passing a first one of said partial streams through plural stages of counter-current flow heat exchange relation with the compressed gas prior to said first throttling step for absorption of heat from such compressed gas and thereafter recycling the gas in said first partial stream together with make-up gas, expanding said second partial stream with partial liquefaction thereof in a second throttling step, and returning the fraction of the gas subjected to said second throttling step remaining in gaseous condition in counter-current flow heat exchange relation with the compressed gas prior to said first throttling step for absorption of heat from such compressed gas.
  • a process for the lquefaction of helium gas comprising the steps of compressing the gas to supercritical pressure, cooling the compressed gas below its inversion temperature by passing it in heat exchange relation with previously compressed and cooled gas, expanding the cooled gas to a pressure above the liquefaction pressure thereof in a irst throttling step without liquefaction of any part of .the gas so expanded, dividing the gas so expanded into two streams, passing one of said streams in heat exchange relation with compressed gas, thereafter expanding said one stream with performance of external Work down to the vicinity of the liquefaction pressure of the gas, thereafter heating said one stream substantially to ambient temperature by passage in heat exchange relation with compressed gas, recycling to said compression step the gas in said one stream so heated, further expand- 10 ing the other of said two streams in a second throttling step with partial liquefaction thereof, and heating the gas in said second stream not liquefied upon said second throttling step substantially to ambient temperature by passing it in heat exchange relation with compressed gas.

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  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
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  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US449744A 1964-04-29 1965-04-21 Process for liquefaction of helium by expansion Expired - Lifetime US3389565A (en)

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CH562864A CH411957A (de) 1964-04-29 1964-04-29 Verfahren zur Verflüssigung eines tiefsiedenden Gases, insbesondere von Helium

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CH (1) CH411957A (fr)
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Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3677019A (en) * 1969-08-01 1972-07-18 Union Carbide Corp Gas liquefaction process and apparatus
US3828564A (en) * 1970-02-27 1974-08-13 Linde Ag Closed refrigerant cycle for the liquefaction of low-boiling gases
US3864926A (en) * 1970-10-19 1975-02-11 Cryogenic Technology Inc Apparatus for liquefying a cryogen by isentropic expansion
US3992167A (en) * 1975-04-02 1976-11-16 Union Carbide Corporation Low temperature refrigeration process for helium or hydrogen mixtures using mixed refrigerant
US4055961A (en) * 1973-08-21 1977-11-01 U.S. Philips Corporation Device for liquefying gases
WO1979001167A1 (fr) * 1978-06-01 1979-12-27 Helix Tech Corp Appareil et methode cryogenique pour eliminer des impuretes congelees d'un liquide cryogenique
US4195979A (en) * 1978-05-12 1980-04-01 Phillips Petroleum Company Liquefaction of high pressure gas
US4701200A (en) * 1986-09-24 1987-10-20 Union Carbide Corporation Process to produce helium gas
US4701201A (en) * 1986-09-24 1987-10-20 Union Carbide Corporation Process to produce cold helium gas for liquefaction
EP0875725A2 (fr) * 1997-05-01 1998-11-04 Praxair Technology, Inc. Système pour la production d'un fluide cryogénique
US6170290B1 (en) * 1998-03-02 2001-01-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Refrigeration process and plant using a thermal cycle of a fluid having a low boiling point
US7278280B1 (en) * 2005-03-10 2007-10-09 Jefferson Science Associates, Llc Helium process cycle
US20070251266A1 (en) * 2004-11-15 2007-11-01 Mayekawa Mfg. Co., Ltd. Cryogenic liquefying/refrigerating method and system
US20080184722A1 (en) * 2007-02-01 2008-08-07 Linde Aktiengesellschaft Method and apparatus for a refrigeration circuit
US7409834B1 (en) * 2005-03-10 2008-08-12 Jefferson Science Associates Llc Helium process cycle
US20120227418A1 (en) * 2011-03-08 2012-09-13 Linde Aktiengesellschaft Cooling unit
US20130061607A1 (en) * 2011-09-08 2013-03-14 Linde Aktiengesellschaft Cooling system
CN104792113A (zh) * 2014-01-22 2015-07-22 中国科学院理化技术研究所 氦液化器及其控制方法
KR20150103020A (ko) * 2013-01-03 2015-09-09 레르 리키드 쏘시에떼 아노님 뿌르 레？드 에렉스뿔라따시옹 데 프로세데 조르즈 클로드 냉동 및/또는 액화 장치 및 대응 방법

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US6141973A (en) * 1998-09-15 2000-11-07 Yukon Pacific Corporation Apparatus and process for cooling gas flow in a pressurized pipeline
FR3057941B1 (fr) * 2016-10-20 2020-02-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Dispositif et procede de refrigeration et/ou de liquefaction d'un fluide cryogenique
CN109764637B (zh) * 2018-12-28 2020-09-25 中国科学院理化技术研究所 一种氦液化器流程装置

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US2895303A (en) * 1956-05-17 1959-07-21 Little Inc A Purification of low-boiling gases
US2957318A (en) * 1956-06-13 1960-10-25 Liquefreeze Company Inc Control for refrigerating system
US3095274A (en) * 1958-07-01 1963-06-25 Air Prod & Chem Hydrogen liquefaction and conversion systems
US3182461A (en) * 1961-09-19 1965-05-11 Hydrocarbon Research Inc Natural gas liquefaction and separation

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DE1036282B (de) * 1956-08-17 1958-08-14 Sulzer Ag Kuehlanlage
US3094390A (en) * 1958-07-09 1963-06-18 Air Prod & Chem Production and storage of converted hydrogen

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Publication number Priority date Publication date Assignee Title
US2895303A (en) * 1956-05-17 1959-07-21 Little Inc A Purification of low-boiling gases
US2957318A (en) * 1956-06-13 1960-10-25 Liquefreeze Company Inc Control for refrigerating system
US3095274A (en) * 1958-07-01 1963-06-25 Air Prod & Chem Hydrogen liquefaction and conversion systems
US3182461A (en) * 1961-09-19 1965-05-11 Hydrocarbon Research Inc Natural gas liquefaction and separation

Cited By (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3677019A (en) * 1969-08-01 1972-07-18 Union Carbide Corp Gas liquefaction process and apparatus
US3828564A (en) * 1970-02-27 1974-08-13 Linde Ag Closed refrigerant cycle for the liquefaction of low-boiling gases
US3864926A (en) * 1970-10-19 1975-02-11 Cryogenic Technology Inc Apparatus for liquefying a cryogen by isentropic expansion
US4055961A (en) * 1973-08-21 1977-11-01 U.S. Philips Corporation Device for liquefying gases
US3992167A (en) * 1975-04-02 1976-11-16 Union Carbide Corporation Low temperature refrigeration process for helium or hydrogen mixtures using mixed refrigerant
US4195979A (en) * 1978-05-12 1980-04-01 Phillips Petroleum Company Liquefaction of high pressure gas
WO1979001167A1 (fr) * 1978-06-01 1979-12-27 Helix Tech Corp Appareil et methode cryogenique pour eliminer des impuretes congelees d'un liquide cryogenique
US4192661A (en) * 1978-06-01 1980-03-11 Helix Technology Corporation Adsorbing impurities from cryogenic fluid make-up prior to admixing with feed
US4701200A (en) * 1986-09-24 1987-10-20 Union Carbide Corporation Process to produce helium gas
US4701201A (en) * 1986-09-24 1987-10-20 Union Carbide Corporation Process to produce cold helium gas for liquefaction
EP0875725A2 (fr) * 1997-05-01 1998-11-04 Praxair Technology, Inc. Système pour la production d'un fluide cryogénique
EP0875725A3 (fr) * 1997-05-01 1999-04-14 Praxair Technology, Inc. Système pour la production d'un fluide cryogénique
US6170290B1 (en) * 1998-03-02 2001-01-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Refrigeration process and plant using a thermal cycle of a fluid having a low boiling point
US20070251266A1 (en) * 2004-11-15 2007-11-01 Mayekawa Mfg. Co., Ltd. Cryogenic liquefying/refrigerating method and system
US7540171B2 (en) * 2004-11-15 2009-06-02 Mayekawa Mfg. Co., Ltd. Cryogenic liquefying/refrigerating method and system
US7278280B1 (en) * 2005-03-10 2007-10-09 Jefferson Science Associates, Llc Helium process cycle
US7409834B1 (en) * 2005-03-10 2008-08-12 Jefferson Science Associates Llc Helium process cycle
US20080184722A1 (en) * 2007-02-01 2008-08-07 Linde Aktiengesellschaft Method and apparatus for a refrigeration circuit
US20120227418A1 (en) * 2011-03-08 2012-09-13 Linde Aktiengesellschaft Cooling unit
US20130061607A1 (en) * 2011-09-08 2013-03-14 Linde Aktiengesellschaft Cooling system
KR20150103020A (ko) * 2013-01-03 2015-09-09 레르 리키드 쏘시에떼 아노님 뿌르 레？드 에렉스뿔라따시옹 데 프로세데 조르즈 클로드 냉동 및/또는 액화 장치 및 대응 방법
US20150345834A1 (en) * 2013-01-03 2015-12-03 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Refrigeration and/or liquefaction device, and corresponding method
US10520225B2 (en) * 2013-01-03 2019-12-31 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Refrigeration and/or liquefaction device using selective pre-cooling, and corresponding method
KR102124677B1 (ko) 2013-01-03 2020-06-23 레르 리키드 쏘시에떼 아노님 뿌르 레드 에렉스뿔라따시옹 데 프로세데 조르즈 클로드 냉동 및/또는 액화 장치 및 대응 방법
CN104792113A (zh) * 2014-01-22 2015-07-22 中国科学院理化技术研究所 氦液化器及其控制方法
CN104792113B (zh) * 2014-01-22 2018-09-28 北京中科富海低温科技有限公司 氦液化器及其控制方法

Also Published As

Publication number Publication date
GB1030600A (en) 1966-05-25
NL125897C (fr)
FR1428851A (fr) 1966-02-18
CH411957A (de) 1966-04-30
NL6406768A (fr) 1965-11-01
DE1259914B (de) 1968-02-01

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