US2909903A - Liquefaction of low-boiling gases - Google Patents

Liquefaction of low-boiling gases Download PDF

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US2909903A
US2909903A US620867A US62086756A US2909903A US 2909903 A US2909903 A US 2909903A US 620867 A US620867 A US 620867A US 62086756 A US62086756 A US 62086756A US 2909903 A US2909903 A US 2909903A
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helium
liquefaction
low
gas
pressure
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Francis J Zimmermann
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Arthur D Little Inc
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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
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
    • F25J1/0276—Laboratory or other miniature devices
    • 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
    • F25J1/001—Hydrogen
    • 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
    • F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/005—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 an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
    • 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
    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/0062—Light or noble gases, mixtures thereof
    • F25J1/0065—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
    • F25J1/02—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
    • 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
    • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
    • 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
    • F25J2270/14—External refrigeration with work-producing gas expansion loop
    • F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/42—Modularity, pre-fabrication of modules, assembling and erection, horizontal layout, i.e. plot plan, and vertical arrangement of parts of the cryogenic unit, e.g. of the cold box

Definitions

  • the Collins process and apparatus is frequently used to liquefy'hydrogen or other gases withhigher boiling points, but the amount so liquefied is relatively limited. However, I have found that by the use of a different type of heat exchange system the hourly rate of liquid hydrogen can be approximately doubled.
  • Fig. 1 is in part a cross-sectional view of a Collins- 'ty'p e cryostat. showing the connections between the heat exch nge. system, and the auxiliary liquefying system 'inakir'igup the improvements in such a cryostat embodied in this invention;
  • Fig. 2 is a cross-sectional view of a small section of the heat exchange system to show the relationship of the elements of the system;
  • Fig. 3 illustrates production rates for liquid hydrogen by the process of this invention compared with the previous method used.
  • Fig. 1 shows a cross-sectional view of the heat exchange system of a Collins cryostat embodying the improvements of this invention, along with a diagrammatical representation of auxiliary equipment.
  • the entire heat exchange system is'surr'ounded by an evacuated area 10 which is enclosed by outer jacket 11 and inside wall 12 which make up a Dewar-type flask, i.e., a doublewalled container with the space between the walls evacuated.
  • precooling coils 13 forearrying liquid nitrogen or liquid air are wound about inside wall 12 in the upper portion of the heat exchange system and around radiation shield 21 in the lower portion.
  • a double-walled flask hereinafter called the'heat exchanger with walls 14 and 15 contains helically wound finned tubing 16 through which high-pressure helium is passed.
  • the passage 17 surrounding this helically wound tubing serves as a pathway for cold, low pressure helium which is returned through 'the heat exchanger to precool the incoming helium.
  • cord packing 16a (Fig. 2) is also wound in such a manner as to touch the fins of finned tubing 16 and walls 14 and 15. This cordpacking 16a serves to hold the finned tubing 16 firmly in place and to better direct the passing of gas 17.
  • flange 22 of the heat exchanger is separated from flange 23 of the Dewar type flask by spacer flange 24 and sealed with an O ring seal 25.
  • space flange 24 has an inlet line of the gas to be liquefied.
  • gas source 28 usually a pressure flask
  • a draw-off line 32 connects finned tubing 16 with charcoal trap 33 which in turn is connected by line 34 to a first expansion engine '35.
  • the exhaust line 36 of expanslonengine 35 leads to passage17.
  • line 37 leads from finned tubing 16 to charcoal trap 38 and line 39 to a second expansion engine 40, the exhaust line 41 of which is connected with passage 17.
  • a Joule-Thomson heat'exchanger 42 and Joule-Thomson valve 43 are provided as part of the helium liquefying cycle.
  • a draw-off line 45, p removing the liquefied gas from the Dewar.
  • Heliuni' source 46 is connected by line 47, controlled by valve-4 8 to compressor 49 which in turn is connected by line 50 to the tubing 16 of the helium heat exchanger. Passage 17 surrounding finned tubing 16 is in turn connected to compressor 49 by means of line 51 controlled I by valve'52.
  • Flange 22 of the heat exchanger may contain auxiliary equipment such as sight glass 53, thermocouple connections 54 and relief valve 55.
  • the heliumrefrigeration" cycle may be described briefpressor system 49 and the warm, "high-pressure heliumis introduced into helical tubing 16 at the top of the main heat exchanger. After passing part way through tubing 16 a portion of this high-pressure helium is drawn off by line 32, passed through charcoal pot 33 and then, by way of line 34, led into the first expansion engine 35. There it is expanded and cooled to about K. and returned to passesge 17 to cool the incoming point (20.4 K.) of any by varying the wire diameter 3 high-pressure helium in finned tubing 16 by out-of-contact heat transfer.
  • a second portion of the high-pressure helium from finned tubing 16 is similarly expanded in the second expansion engine 40 and reduced to a temperature of about 12 K. and returned to passage 17.
  • the Joule-Thomson heat exchanger 42 and Joule- Thomson valve 43 are closed to prevent helium from liquefying and entering the lowest portion of the Dewar flask.
  • the recirculated low-pressure helium passing up through passage 17 flows by way of line 51 into the compressor system 49 to be compressed and recycled through the system as described.
  • Hydrogen is taken as a gas to illustrate this invention since it has the lowest boiling gas. except helium itself. It follows then that any gas having a boiling point above that of helium may be liquefied in the manner described.
  • the rate of liquefaction may be increased with the use of liquid nitrogen precooling.
  • the liquid nitrogen is circulated in tubing 13 in the top portion of the Dewar around wall 12 and in the bottom portion around radiation shield 21.
  • channel 18 may be constructed by other suitable means, it is conveniently formed by Winding a wire about the double-walled flask, using the wire as a divider between it and the vacuum jacket and also to form the helical path itself.
  • the wire is preferably one that is relatively flexible and easily soldered.
  • the width and/or thickness of channel 18 may be easily varied to suit each gas to be liquified and/or the pitch of the wire 19.
  • Fig. 3 The marked improvement in liquefaction rates may be seen in Fig. 3 in which are plotted the liters of liquid hydrogen which can be obtained by using one and two helium compressors with a cryostat such as illustrated in Fig. 1.
  • a cryostat has a normal capacity for liquefying 4 and 8 liters of helium, using one and two compressors, respectively.
  • Curve A represents the rate achieved by the process of this invention
  • curve B the rate for the system without the modification embodied in this invention. It can be seen from Fig. 3 that the liquefaction rate is almost doubled.
  • helium refrigeration is used in an efficient manner, making it possible to achieve marked improvement in liquefaction rates for hydrogen and all other gases having boiling points about helium.
  • an apparatus for liquefying a gas having a boiling point higher than that of helium comprising helium refrigeration means, a double-walled container with the space between the walls evacuated surrounding said helium refrigeration means, channel means separating said helium refrigeration means from said container, said helium refrigeration means comprising finned tubing means for carrying high pressure helium to a first and a second expansion engine and means for conducting the resulting low temperature, low pressure helium around said finned tubing means in a counter-current direction in which said high-pressure helium moves through said finned tubing means, said channel means forming a helical path to lead the gas to be liquefied in the direction of flow of said high-pressure helium in said finned tubing means of said helium refrigeration means.
  • heat exchange means for circulating low-pressure, low-temperature helium in outof-contact heat exchange with high-pressure helium, a double-walled container with the space betwen the walls evacuated surrounding said heat exchange means and channel means separating said heat exchange means from said double-walled evacuated container, said channel means being in out-of-contact heat exchange relation with said low-pressure, low-temperature helium and having a helical passageway arranged to direct said gas in the same direction of flow as said high-pressure helium.
  • precooling means are located within the evacuated area of said double walled container with the space between the walls evacuated and are in out-of-contact heatexchange relation with said channel means.
  • an apparatus for liquefying gas having a boiling point higher than that of helium means for supplying said gas, channel means for conducting said gas in a helical path in .out-of-contact heat exchange with low-temperature, low-pressure helium gas to a liquid collection area, double-walled container with the space between the walls evacuated and helium refrigeration means located within 'said double-walled container and forming therewith said channel means, said helium refrigerationmeans comprising a source for said helium, a compressor, tubing means for carrying high-pressure helium to a first and second expansion engine, and means for conducting the resulting low-temperature, low-pressure helium around said tubing means in a counter-current direction in which said highpressure helium moves through said tubing means, and

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Clinical Laboratory Science (AREA)
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Description

1959 F; J. ZIMMERMANN 2,909,903
LIQUEFACTION OF LOW-BOILING GASES 2 sheets-sheet 1 Filed Nov. 7, 1956 29 30 2 23 PR5 COOLANT 28 EXP/1 NOE IN VEN TOR.
AYTORNEY Oct. 27, 1959 F. J. ZIMMERMANN LIQUEFACTION OF LOW-BOILING GASES 2 Sheets-Sheet 2 Filed Nov. 7, 1956 um 2 a0 X HF M m? 5 R 3 M w .TO 5 56 M 10, W C mc g m Fm MA INVENTOR. FQA NC/S J Z/MMB'ZMA/ll? 8&4 1 W.
AZTORMY g Arthur D.
'tion of gases, particularly'hydrogen.
helium.
2,909,903 'LI'QUEFACTION F LOW-BOILING GASES Francis J, Zimmermann, Hamden, Comm, assignor t0 Little, Inc, Cambridge, Mass., 2: corporationof Massachusetts Application November 7 1956, Serial No. 620,867 Claims. (Cl. 62-8) This invention relates to a refrigeration system for the production of low temperatures and particularly to the liquefaction of gases. In United States Patent 2,458,894 issued January '11, 1949; to Samuel C. Collins, there is disclosed a cycle for liquefyinggases, particularly helium which has the lowest known boiling point, i.e., 42 K. or -268.9 C. In a low temperature refrigeration system, such as that of the Collins process it is desirable to have sufiicient flexibility of operation which permits the rap-id and efficient liquefaction of other gases while taking advantage of the helium refrigeration in the system. Rapid liquefaction and high thermodynamic efiiciency means a considerable saving in helium, an important factor in areas or countries where helium is expensive.
The Collins process and apparatus is frequently used to liquefy'hydrogen or other gases withhigher boiling points, but the amount so liquefied is relatively limited. However, I have found that by the use of a different type of heat exchange system the hourly rate of liquid hydrogen can be approximately doubled.
It is therefore an object of this invention to provide a highly eflicient refrigeration system for the liquefac- It is another object to provide, in a system designed primarily for liquefying helium, suflicient flexibility of operation which permits the use of helium refrigeration to liquefy other gases with boiling points above the boiling point of It is a further object to provide a system for liquefying gases which embodies the use ofhelium,and which is thermodynamically eflicient' and hence ecoiiomical to run even though helium may be expensive to procure, It is yet a further object of this invention lto' s'o modify the Collins low-temperature refrigeration cycle as to practically double the rate at which hydro- ]gen may be liquefied.
These and other 'objects'of this invention will be'apparent'in the following description.
lThe'improvemen'ts in the liquefaction rate'of hydron or other gas, are achieved in this invention 'by the e ofja heat exchanger which makes use of the outer :fjc se of the Collins-type cryostat heat exchanger and 1 -liiyputinto very efficient heat exchange relationship with innei 'Dewar wall. The gas to be liquefied is therecooled helium and nitrogen precooling gas if used. This invention is discussed below in detail and with reference to the accompanying drawings, in which Fig. 1 is in part a cross-sectional view of a Collins- 'ty'p e cryostat. showing the connections between the heat exch nge. system, and the auxiliary liquefying system 'inakir'igup the improvements in such a cryostat embodied in this invention;
Fig. 2 is a cross-sectional view of a small section of the heat exchange system to show the relationship of the elements of the system; and
Fig. 3 illustrates production rates for liquid hydrogen by the process of this invention compared with the previous method used.
The process of this invention will be described below United States hate-at V 26 drilled into permit introduction through lead line 27 "through passage changerand 'wall 12 of the Dewar-type flask, channel controlled by valve 45a, is provided for I lyf firs t befdie describing the liquefaction cycle. 'g'iny pure helium from source 46 i's' c'ompressedby' comin terms of the liquefaction of hydro-gen. However, it is obvious that the same process may also be used for all gases having boiling points above hydrogen, which means in effect all the known-gases except helium'itself.
Fig. 1 shows a cross-sectional view of the heat exchange system of a Collins cryostat embodying the improvements of this invention, along with a diagrammatical representation of auxiliary equipment. The entire heat exchange system is'surr'ounded by an evacuated area 10 which is enclosed by outer jacket 11 and inside wall 12 which make up a Dewar-type flask, i.e., a doublewalled container with the space between the walls evacuated. In this evacuated area precooling coils 13 forearrying liquid nitrogen or liquid air are wound about inside wall 12 in the upper portion of the heat exchange system and around radiation shield 21 in the lower portion. A double-walled flask hereinafter called the'heat exchanger with walls 14 and 15 contains helically wound finned tubing 16 through which high-pressure helium is passed. The passage 17 surrounding this helically wound tubing serves as a pathway for cold, low pressure helium which is returned through 'the heat exchanger to precool the incoming helium. In passage 17 cord packing 16a (Fig. 2) is also wound in such a manner as to touch the fins of finned tubing 16 and walls 14 and 15. This cordpacking 16a serves to hold the finned tubing 16 firmly in place and to better direct the passing of gas 17. Between wall 14 of the heat ex- 18 is formed by helically wound wire 19 whichsserves as a channel spacer and to create a passageway 20 within channel 18. To form channel 18, flange 22 of the heat exchanger is separated from flange 23 of the Dewar type flask by spacer flange 24 and sealed with an O ring seal 25. At one' point space flange 24 has an inlet line of the gas to be liquefied. In the line leading from gas source 28 (usually a pressure flask) there may be placed one for more reducing valves, such as 29' and 30,'if desired, and flow meter 31.
Part way down the heat exchanger a draw-off line 32 connects finned tubing 16 with charcoal trap 33 which in turn is connected by line 34 to a first expansion engine '35. The exhaust line 36 of expanslonengine 35 leads to passage17. Similarly, line 37 leads from finned tubing 16 to charcoal trap 38 and line 39 to a second expansion engine 40, the exhaust line 41 of which is connected with passage 17. A Joule-Thomson heat'exchanger 42 and Joule-Thomson valve 43 are provided as part of the helium liquefying cycle. A draw-off line 45, p removing the liquefied gas from the Dewar.
Heliuni' source 46 is connected by line 47, controlled by valve-4 8 to compressor 49 which in turn is connected by line 50 to the tubing 16 of the helium heat exchanger. Passage 17 surrounding finned tubing 16 is in turn connected to compressor 49 by means of line 51 controlled I by valve'52.
Flange 22 of the heat exchanger may contain auxiliary equipment such as sight glass 53, thermocouple connections 54 and relief valve 55. I
The heliumrefrigeration" cycle may be described briefpressor system 49 and the warm, "high-pressure heliumis introduced into helical tubing 16 at the top of the main heat exchanger. After passing part way through tubing 16 a portion of this high-pressure helium is drawn off by line 32, passed through charcoal pot 33 and then, by way of line 34, led into the first expansion engine 35. There it is expanded and cooled to about K. and returned to passege 17 to cool the incoming point (20.4 K.) of any by varying the wire diameter 3 high-pressure helium in finned tubing 16 by out-of-contact heat transfer. A second portion of the high-pressure helium from finned tubing 16 is similarly expanded in the second expansion engine 40 and reduced to a temperature of about 12 K. and returned to passage 17. The Joule-Thomson heat exchanger 42 and Joule- Thomson valve 43 are closed to prevent helium from liquefying and entering the lowest portion of the Dewar flask. The recirculated low-pressure helium passing up through passage 17 flows by way of line 51 into the compressor system 49 to be compressed and recycled through the system as described.
The liquefaction cycle may now be described using hydrogen as an example. Hydrogen is taken as a gas to illustrate this invention since it has the lowest boiling gas. except helium itself. It follows then that any gas having a boiling point above that of helium may be liquefied in the manner described.
Hydrogen from source 28, after passing through suitable pressure regulating valves 29 and 3,0 and flow .meter 31, if desired, is introduced by line 27 into heatexchanger inlet 26. This inlet 26 leads to channel 18 and then to passageway 20 formed by spacing wire 19..
As the hydrogen is forced, under pressure, spirally downward in channel 18 it is cooled by out-of-contact heat exchange by means of the cold helium in passage 17. Inasmuch as the helium from the second expansion engine 40 is about 12 K. liquefaction of hydrogen probably begins in the region where the helium from this expansion engine is returned to passage 17. By the time the hydrogen passes the cold end of the helium heat exchanger it is completely liquefied and it drops to the bottom of the Dewar flask to collect as liquid hydrogen 44. The liquefied hydrogen may then be drawn otf as desired by means of draw-off line 45.
As in the case where helium is to be liquefied, the rate of liquefaction may be increased with the use of liquid nitrogen precooling. The liquid nitrogen is circulated in tubing 13 in the top portion of the Dewar around wall 12 and in the bottom portion around radiation shield 21.
Although the helical path of channel 18 may be constructed by other suitable means, it is conveniently formed by Winding a wire about the double-walled flask, using the wire as a divider between it and the vacuum jacket and also to form the helical path itself. The wire is preferably one that is relatively flexible and easily soldered. The width and/or thickness of channel 18 may be easily varied to suit each gas to be liquified and/or the pitch of the wire 19.
The marked improvement in liquefaction rates may be seen in Fig. 3 in which are plotted the liters of liquid hydrogen which can be obtained by using one and two helium compressors with a cryostat such as illustrated in Fig. 1. Such a cryostat has a normal capacity for liquefying 4 and 8 liters of helium, using one and two compressors, respectively. Curve A represents the rate achieved by the process of this invention, curve B the rate for the system without the modification embodied in this invention. It can be seen from Fig. 3 that the liquefaction rate is almost doubled.
The performance figures shown in Fig. 3 were obtained when a 0.031-inch silver solder wire spaced about 1 /2 inches apart was wound and soldered about the heat exchanger. This lifted the main heat exchanger out of the Dewar-type flask about one inch, requiring a spacer flange 24 of this height.
Thus, by the process of this invention, helium refrigeration is used in an efficient manner, making it possible to achieve marked improvement in liquefaction rates for hydrogen and all other gases having boiling points about helium.
I claim:
1. In an apparatus for liquefying a gas having a boiling point higher than that of helium, comprising helium refrigeration means, a double-walled container with the space between the walls evacuated surrounding said helium refrigeration means, channel means separating said helium refrigeration means from said container, said helium refrigeration means comprising finned tubing means for carrying high pressure helium to a first and a second expansion engine and means for conducting the resulting low temperature, low pressure helium around said finned tubing means in a counter-current direction in which said high-pressure helium moves through said finned tubing means, said channel means forming a helical path to lead the gas to be liquefied in the direction of flow of said high-pressure helium in said finned tubing means of said helium refrigeration means.
2. In an apparatus for liquefying gas having a boiling point higher than that of helium, heat exchange means for circulating low-pressure, low-temperature helium in outof-contact heat exchange with high-pressure helium, a double-walled container with the space betwen the walls evacuated surrounding said heat exchange means and channel means separating said heat exchange means from said double-walled evacuated container, said channel means being in out-of-contact heat exchange relation with said low-pressure, low-temperature helium and having a helical passageway arranged to direct said gas in the same direction of flow as said high-pressure helium.
3. An apparatus in accordance with claim 2 wherein precooling means are located within the evacuated area of said double walled container with the space between the walls evacuated and are in out-of-contact heatexchange relation with said channel means.
4. Apparatus in accordance with claim 2 wherein said helical path of said channel means is formed by wrapping wire helically around said heat exchange means, the diameter of said wire and the width of said channel being equal.
5. In an apparatus for liquefying gas having a boiling point higher than that of helium, means for supplying said gas, channel means for conducting said gas in a helical path in .out-of-contact heat exchange with low-temperature, low-pressure helium gas to a liquid collection area, double-walled container with the space between the walls evacuated and helium refrigeration means located within 'said double-walled container and forming therewith said channel means, said helium refrigerationmeans comprising a source for said helium, a compressor, tubing means for carrying high-pressure helium to a first and second expansion engine, and means for conducting the resulting low-temperature, low-pressure helium around said tubing means in a counter-current direction in which said highpressure helium moves through said tubing means, and
means for drawing off said liquefied gas from said collecting area.
References Cited in the file of this patent UNITED STATES PATENTS 881,176 Claude Mar. 10, 1908 2,458,894 Collins Jan. 11, 1949 2,555,682 Daun June 5, 1951
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US3144316A (en) * 1960-05-31 1964-08-11 Union Carbide Corp Process and apparatus for liquefying low-boiling gases
US3194025A (en) * 1963-01-14 1965-07-13 Phillips Petroleum Co Gas liquefactions by multiple expansion refrigeration
US3205679A (en) * 1961-06-27 1965-09-14 Air Prod & Chem Low temperature refrigeration system having filter and absorber means
US3233418A (en) * 1962-07-23 1966-02-08 Philips Corp Apparatus for liquefying helium
US3237416A (en) * 1962-12-04 1966-03-01 Petrocarbon Dev Ltd Liquefaction of gases
US3250079A (en) * 1965-03-15 1966-05-10 Little Inc A Cryogenic liquefying-refrigerating method and apparatus
US3257812A (en) * 1962-04-27 1966-06-28 Philips Corp Dissociated ammonia separation plant having an adsorber in a liquid refrigerant bath
US3299646A (en) * 1964-06-17 1967-01-24 Little Inc A Cryogenic joule-thomson helium liquefier with cascade helium and nitrogen refrigeration circuits
US3355903A (en) * 1965-01-04 1967-12-05 Fleur Corp System of power-refrigeration
US3362174A (en) * 1963-10-14 1968-01-09 Air Liquide Gaseous condensation in vacuum with plural refrigerants
US3377811A (en) * 1965-12-28 1968-04-16 Air Prod & Chem Liquefaction process employing expanded feed as refrigerant
US3416324A (en) * 1967-06-12 1968-12-17 Judson S. Swearingen Liquefaction of a gaseous mixture employing work expanded gaseous mixture as refrigerant
US3473342A (en) * 1966-04-01 1969-10-21 Nautchno Izsledovatelski Sekto Method and apparatus for liquefaction of neon
US3485053A (en) * 1966-03-25 1969-12-23 Air Liquide Process for the production of a gas with a variable output by controlling the degree of refrigeration in the liquefaction of stored gas
US3521457A (en) * 1967-07-19 1970-07-21 Air Reduction Apparatus for making hydrogen slush using nitrogen and helium refrigerants
US3792591A (en) * 1970-03-24 1974-02-19 Cryogenic Technology Inc Helium purification method and apparatus
US3854913A (en) * 1971-02-25 1974-12-17 Physicheski Institute Recovery of neon and helium from air by adsorption and closed cycle helium refrigeration
US3864926A (en) * 1970-10-19 1975-02-11 Cryogenic Technology Inc Apparatus for liquefying a cryogen by isentropic expansion
WO1979001167A1 (en) * 1978-06-01 1979-12-27 Helix Tech Corp Cryogenic apparatus and method of removing freezing impurities from a cryogenic fluid
FR2486218A1 (en) * 1980-06-30 1982-01-08 Hoxan Kk METHOD FOR LIQUEFACTING A FREON GAS
DE3435229A1 (en) * 1984-09-26 1986-04-03 Kernforschungszentrum Karlsruhe Gmbh, 7500 Karlsruhe CRYSTATE FOR OPERATING A (ARROW UP) 3 (ARROW UP) HE (ARROW UP) 4 (ARROW UP) HE MIXING UNIT
US4841732A (en) * 1987-12-28 1989-06-27 Sarcia Domenico S System and apparatus for producing and storing liquid gases
US20050061028A1 (en) * 2003-09-24 2005-03-24 Darren Mennie System for liquefying or freezing xenon
US20060000223A1 (en) * 2004-07-01 2006-01-05 In-X Corporation Desiccant cartridge
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USRE43398E1 (en) 1997-06-16 2012-05-22 Respironics, Inc. Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator
US20120180899A1 (en) * 2009-09-29 2012-07-19 Koninklijke Philips Electronics N.V. Sytem and method for liquefying a fluid and storing the liquefied fluid
US20200318895A1 (en) * 2017-12-22 2020-10-08 Siemens Aktiengesellschaft Device and System for Condensing Gas

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Cited By (43)

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Publication number Priority date Publication date Assignee Title
US2991633A (en) * 1958-03-17 1961-07-11 Itt Joule-thomson effect cooling system
US3144316A (en) * 1960-05-31 1964-08-11 Union Carbide Corp Process and apparatus for liquefying low-boiling gases
US3205679A (en) * 1961-06-27 1965-09-14 Air Prod & Chem Low temperature refrigeration system having filter and absorber means
US3257812A (en) * 1962-04-27 1966-06-28 Philips Corp Dissociated ammonia separation plant having an adsorber in a liquid refrigerant bath
US3233418A (en) * 1962-07-23 1966-02-08 Philips Corp Apparatus for liquefying helium
US3237416A (en) * 1962-12-04 1966-03-01 Petrocarbon Dev Ltd Liquefaction of gases
US3194025A (en) * 1963-01-14 1965-07-13 Phillips Petroleum Co Gas liquefactions by multiple expansion refrigeration
US3362174A (en) * 1963-10-14 1968-01-09 Air Liquide Gaseous condensation in vacuum with plural refrigerants
US3299646A (en) * 1964-06-17 1967-01-24 Little Inc A Cryogenic joule-thomson helium liquefier with cascade helium and nitrogen refrigeration circuits
US3355903A (en) * 1965-01-04 1967-12-05 Fleur Corp System of power-refrigeration
US3250079A (en) * 1965-03-15 1966-05-10 Little Inc A Cryogenic liquefying-refrigerating method and apparatus
US3377811A (en) * 1965-12-28 1968-04-16 Air Prod & Chem Liquefaction process employing expanded feed as refrigerant
US3485053A (en) * 1966-03-25 1969-12-23 Air Liquide Process for the production of a gas with a variable output by controlling the degree of refrigeration in the liquefaction of stored gas
US3473342A (en) * 1966-04-01 1969-10-21 Nautchno Izsledovatelski Sekto Method and apparatus for liquefaction of neon
US3416324A (en) * 1967-06-12 1968-12-17 Judson S. Swearingen Liquefaction of a gaseous mixture employing work expanded gaseous mixture as refrigerant
US3521457A (en) * 1967-07-19 1970-07-21 Air Reduction Apparatus for making hydrogen slush using nitrogen and helium refrigerants
US3792591A (en) * 1970-03-24 1974-02-19 Cryogenic Technology Inc Helium purification method and apparatus
US3864926A (en) * 1970-10-19 1975-02-11 Cryogenic Technology Inc Apparatus for liquefying a cryogen by isentropic expansion
US3854913A (en) * 1971-02-25 1974-12-17 Physicheski Institute Recovery of neon and helium from air by adsorption and closed cycle helium refrigeration
US4192661A (en) * 1978-06-01 1980-03-11 Helix Technology Corporation Adsorbing impurities from cryogenic fluid make-up prior to admixing with feed
WO1979001167A1 (en) * 1978-06-01 1979-12-27 Helix Tech Corp Cryogenic apparatus and method of removing freezing impurities from a cryogenic fluid
FR2486218A1 (en) * 1980-06-30 1982-01-08 Hoxan Kk METHOD FOR LIQUEFACTING A FREON GAS
DE3026667A1 (en) * 1980-06-30 1982-02-04 Hoxan Corp., Sapporo, Hokkaido METHOD AND LIQUIDATION OF FREONGAS
US4333753A (en) * 1980-06-30 1982-06-08 Hoxan Corporation Method of liquefying Freon gas
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US4841732A (en) * 1987-12-28 1989-06-27 Sarcia Domenico S System and apparatus for producing and storing liquid gases
USRE43398E1 (en) 1997-06-16 2012-05-22 Respironics, Inc. Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator
US20050061028A1 (en) * 2003-09-24 2005-03-24 Darren Mennie System for liquefying or freezing xenon
WO2005031228A1 (en) * 2003-09-24 2005-04-07 The Boc Group Plc System for liquefying or freezing xenon
US7137274B2 (en) 2003-09-24 2006-11-21 The Boc Group Plc System for liquefying or freezing xenon
US7913497B2 (en) 2004-07-01 2011-03-29 Respironics, Inc. Desiccant cartridge
US20060000223A1 (en) * 2004-07-01 2006-01-05 In-X Corporation Desiccant cartridge
US20060086102A1 (en) * 2004-10-26 2006-04-27 In-X Corporation Liquefying and storing a gas
US7318327B2 (en) 2004-10-26 2008-01-15 Respironics In-X, Inc. Liquefying and storing a gas
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US20060086099A1 (en) * 2004-10-26 2006-04-27 In-X Corporation Liquefying and storing a gas
US20120180899A1 (en) * 2009-09-29 2012-07-19 Koninklijke Philips Electronics N.V. Sytem and method for liquefying a fluid and storing the liquefied fluid
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