US3327490A - Recombining separated gaseous nitrogen and vaporized liquid nitrogen with air to produce a constant gaseous feed rate - Google Patents

Recombining separated gaseous nitrogen and vaporized liquid nitrogen with air to produce a constant gaseous feed rate Download PDF

Info

Publication number
US3327490A
US3327490A US396162A US39616264A US3327490A US 3327490 A US3327490 A US 3327490A US 396162 A US396162 A US 396162A US 39616264 A US39616264 A US 39616264A US 3327490 A US3327490 A US 3327490A
Authority
US
United States
Prior art keywords
nitrogen
gaseous
liquid nitrogen
cold
amount
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US396162A
Other languages
English (en)
Inventor
Grenier Maurice
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Air Liquide SA filed Critical Air Liquide SA
Application granted granted Critical
Publication of US3327490A publication Critical patent/US3327490A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B1/00—Shaft or like vertical or substantially vertical furnaces
    • F27B1/10—Details, accessories, or equipment peculiar to furnaces of these types
    • F27B1/18—Arrangements of dust collectors
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/044—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a single pressure main column system only
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high pressure column of a double pressure main column system
    • 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
    • F25J2210/04—Mixing or blending of fluids with the feed 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
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One fluid being 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/42—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery
    • F25J2260/44—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery using nitrogen for cooling purposes
    • 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
    • F25J2290/62—Details of storing a fluid in a tank
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/939—Partial feed stream expansion, air
    • Y10S62/94—High pressure column

Definitions

  • a process for the production of cold by the vaporisation of liquid nitrogen in which nitrogen vapour at low temperature, obtained by the vaporisation of liquid nitrogen, is reheated to a temperature in the region of ambient temperature, at least in part by indirect heat exchange with a gas which has a high nitrogen content and from which said liquid nitrogen is to be produced, characterised in that (a) said gas having a high nitrogen content 3,327,496 Patented June 27, 1967 is formed by the admixture of air, gaseous nitrogen separated from said gas with a high nitrogen content, and at least a part of any nitrogen vapour obtained by the vaporisation of said liquid nitrogen for the production of cold and reheated by heat exchange with the said gas having a high nitrogen content, said mixture being supplied at a constant or substantially constant delivery rate and the proportion of said nitrogen vapour in the gas with a high nitrogen content increasing or decreasing as the production of cold increases or decreases; and (b) said gas having a high nitrogen content is separated by liquefaction and rectification into
  • the process of the invention assures a close connection between the consumption of cold and the production of liquefied gas, such that any increase in the former necessarily causes an increase of the latter. It also permits the use of an installation which is only of moderate size, corresponding substantially to the mean cold consumption, and which is consequently much less costly than an installation corresponding to the desired maximum instantaneous cold production.
  • the process of the invention is modified in either one of or both of the following ways:
  • FIGURE 1 shows schematically an installation for the production of low temperatures by vaporisation of liquid nitrogen
  • FIGURE 2 shows schematically a modified arrangement of that part of the installation shown in FIGURE 1 which is disposed on the right of the axis XX in FIG- URE l;
  • FIGURE 3 shows schematically another embodiment of an installation for the production of low temperatures.
  • atmospheric air which is introduced through the pipe 1 (in the direction of the full-line arrows), is dried and the carbon dioxide removed therefrom at 2, for example by adsorption at ambient te-meprature on an adsorbent mass, e.g. activated alumina, in accordance with the process described in US. patent application Ser. No. 211,370 of July 20, 1962; the carbon dioxide may also be removed by washing with a sodium hydroxide solution, the drying then taking place, after the subsequent compression, by passing over an adsorbent mass.
  • an adsorbent mass e.g. activated alumina
  • the air then has added thereto, through a pipe 3, gaseous nitrogen at or in the neighbourhood of ambient temperature, the gaseous nitrogen originating on the one hand from gaseous nitrogen separated by rectification and on the other hand from nitrogen vaporised to ensure the production of cold.
  • the resulting gas with a high nitrogen content is then brought by a compressor 4 to a pressure of approximately 200 bars absolute, and is then passed through a pipe 5 into a heat exchanger 6, where it is cooled to about 25 C. by heat exchange with the cold nitrogen separated by rectification or vaporised in the cold consumption installation.
  • a part of the cooled gas is then sent through a pipe 7 to an expansion machine 8 to about 6 bars absolute, and is blown through a pipe 9 into the bottom of a rectifier column 10 which is at a higher pressure.
  • the other part of the cooled gas is passed through a pipe 11 into a heat exchanger 12, .in which it is cooled to a low temperature in heat exchange with separated oxygen and nitrogen vapours; it is then passed through a pipe 13 to a coil 14 disposed in the sump of the rectifier column 10 in which it is super-cooled; it is then passed through a pipe 15 into a heat exchanger 16, in which it is again supercooled by heat exchange with separated gaseous nitrogen; after passing through duct 17 it is then expanded through valves 18 and 19 and introduced into the high-pressure rectifier column 19.
  • the respective rates of flow of liquefied gas passing through the valves 18 and 19 are regulated as a function of the cold production in a device 35, as will be explained hereinafter.
  • the gas having a high nitrogen content is separated in the column 10 at a high pressure into an oxygen-enriched liquid and into a nitrogen-enriched liquid.
  • the oxygenenriched liquid is sent through a pipe 22 to a heat exchanger 23, super-cooled in the latter by heat exchange With separated gaseous nitrogen, then introduced through a pipe 24 and an expansion valve 25 at about 1.3 bars absolute into the middle Zone of a low-pressure rectification column 21.
  • Liquid nitrogen which is drawn off through a pipe 26 at the top of the high-pressure rectifier column 10, is super-cooled in a heat exchanger 27 in counter-current with the gaseous nitrogen leaving the upper end of the low-pressure rectification column 10, and then divided into two parts.
  • the first part is introduced through a pipe 29 and an expansion valve 30 at 1.3 bars absolute to the head of the low-pressure rectification column 21 as reflux liquid.
  • the second part constitutes the liquid nitrogen which is intended to ensure the production of cold, and is sent through a pipe 31 and an expansion Valve 32 in the region of atmospheric pressure into a heat-insulated reservoir 33.
  • the heat-insulated reservoir 33 is equipped with a withdrawal valve 34 which connects it to a heat exchange device, represented diagrammatically by a coil 36, placed in a chamber 35 in which it is desired to bring about the production of cold.
  • a pipe 37 permits the cold nitrogen vapours formed in the heat exchange device 36 to be sent back to the liquefaction device for the nitrogen-enriched gas. This recovery cannot be complete (as is the case, for example, when the liquid nitrogen is used for cooling products by direct contact); a line 37A represents the losses of vaporised gaseous nitrogen.
  • a pipe 38 connected to the upper part, of the heat-insulated reservoir 33 enables the cold nitrogen vapours formed in this reservoir to be recovered and for them to be recombined With the vapours formed in the heat exchange device 36.
  • the nitrogen vapours are then sent through a pipe 39 into the heat exchanger 12, where they are reheated in counter-current with the nitrogen-enriched gas, and then through a conduit 40 into the heat exchanger 6, where they are reheated to the region of ambient temperature in counter-current with the same gas. They are then combined by means of the pipe 3 with the purified air at the intake of the compressor.
  • the gaseous nitrogen separated at the head of the low-pressure rectifier column 21 passes successively through pipes 41, 42 and 43 into the exchangers 27, 23 and 16, respectively, in which it ensures the supercooling of the liquid separated in the high-pressure column 10 and of the nitrogen-enriched gas to be sepa- 4 rated. It is then combined by means of a pipe 44 with the cold nitrogen vapours at the cold end of the exchanger 12. Finally, the gaseous oxygen separated in the low-pressure column 21 is sent successively through pipes 45 and 46 into the exchangers 12 and 6, then discharged through a pipe 47.
  • the air When the consumption of cold in the chamber 35 iszero, the air only has added thereto, through the pipe'3, the gaseous nitrogen separated in the rectifier column and nitrogen vapour formed in the reservoir 33.
  • the compressor 4 compresses a mixture of air and nitrogen, with about 12% of oxygen, from which the rectifier columns produce the liquid nitrogen which is collected in the reservoir 33.
  • the quantity of liquid nitrogen vaporised in the chamber 35 becomes equal to or slightly greater than the quantity of liquid nitrogen produced (this being produced for a delivery of nitrogen which is about one-- to ensure a reflux in the low-pressure column, the rate of flow of additional air to the intake of the compressor being zero and the treated gaseous mixture being practically pure nitrogen.
  • the production of liquid nitrogen becomes greater than the quantity which can be separated in the high-pressure rectifier column 10. It is then expedient progressively to open the valve 18 so as to introduce the necessary supplement of liquid nitrogen into the head of the column 10, closing at the same time the valve 19 proportionately to the increase in the production of liquid nitrogen.
  • the apparatus then functions substantially as a nitrogen liquefier, the rectification columns no longer playing any part.
  • FIGURE 2 of the accompanying drawing there is shown a double rectifier column which operates in a manner similar to that of FIGURE 1, except as regards the reflux liquid nitrogen in the column at a low pressure.
  • the latter is no longer taken from the top of the column at a high pressure, but from the middle zone of the latter through a pipe 59; the liquid nitrogen is super-cooled in a heat exchanger 27A in counter-current with the separated gaseous nitrogen, then introduced by way of a pipe 51 and an expansion valve 52 into the head of the low-pressure rectification column 21.
  • This makes it possible to have available a higher rate of flow of the reflux liquid without causing any inconvenience.
  • the gaseous nitrogen sepa rated at the head of the low-pressure rectification column 21 is not absolutely pure, since it is intended to be recycled.
  • FIGURES 1 and 2 Installations for the production of cold by vaporisation of liquid nitrogen, such as those shown in FIGURES 1 and 2, make it possible to conform to a consumption of cold which can vary between zero and a value several times greater than that corresponding to the vaporisation of a quantity of liquid nitrogen equal to the normal pro duction of the separation apparatus (at zero cold consumption) without the purity of the liquid nitrogen decreasirn to an appreciable degree; the latter can for example constantly remain higher than 99%
  • FIGURE 3 there is shown an installation which is similar to that of FIGURES 1 and 2, but comprises only a single rectifier column. It is thus simpler than the first installation, but supplies a smaller yield of nitrogen from the liquefied gas.
  • the rectifier column 10 at high pressure has arranged above it a combined condenser and vaporiser 20 surrounded by a bath of liquefied gas fed with oxygenenriched liquid coming from the sump of the column 1%) through the pipe 22 and the expansion valve 25.
  • the nitrogen-enriched gas after having been super-cooled in the coil 14 of the sump and the exchanger 16, in countercurrent with the separated nitrogen, is introduced as betore through the expansion valves 18 and/or 19 into the high-pressure rectification column 10.
  • the liquid nitrogen is drawn off from the top of the column 10 through the pipe 31, expanded in the valve 32 and introduced into the reservoir 33.
  • the gaseous nitrogen evacuated at the dome of the condenser 20 is expanded in a valve 48 to the region of atmospheric pressure, reheated in the exchanger 16 and combined by means of the pipe 44 with the nitrogen vapours coming from the device 36 for the production of cold.
  • the oxygen-enriched gas is returned through the pipes 45 and 46 into the exchangers 12 and 6 before being discharged at 47.
  • a method for the production of cold by the vaporization of liquid nitrogen according to a variable cold demand comprising the steps of:

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US396162A 1963-09-23 1964-09-14 Recombining separated gaseous nitrogen and vaporized liquid nitrogen with air to produce a constant gaseous feed rate Expired - Lifetime US3327490A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
FR948348A FR1380546A (fr) 1963-09-23 1963-09-23 Procédé de production de froid à basse température par vaporisation d'azote liquide

Publications (1)

Publication Number Publication Date
US3327490A true US3327490A (en) 1967-06-27

Family

ID=8812888

Family Applications (1)

Application Number Title Priority Date Filing Date
US396162A Expired - Lifetime US3327490A (en) 1963-09-23 1964-09-14 Recombining separated gaseous nitrogen and vaporized liquid nitrogen with air to produce a constant gaseous feed rate

Country Status (8)

Country Link
US (1) US3327490A (nl)
BE (1) BE653054A (nl)
DE (1) DE1250459B (nl)
ES (1) ES304271A1 (nl)
FR (1) FR1380546A (nl)
GB (1) GB1031107A (nl)
LU (1) LU46947A1 (nl)
NL (1) NL143335B (nl)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3509728A (en) * 1966-02-22 1970-05-05 Petrocarbon Dev Ltd Low temperature separation of gases utilizing two distillation columns having a common condenser-evaporator
US3648471A (en) * 1969-02-14 1972-03-14 Genrikh Maxovich Basin Method of liberation of nitrogen and oxygen from air
US4083194A (en) * 1976-12-02 1978-04-11 Fluor Engineers And Constructors, Inc. Process for recovery of liquid hydrocarbons

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3062016A (en) * 1957-12-31 1962-11-06 Air Reduction Maintaining high purity argon atmosphere
US3210950A (en) * 1960-09-26 1965-10-12 Air Prod & Chem Separation of gaseous mixtures

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3062016A (en) * 1957-12-31 1962-11-06 Air Reduction Maintaining high purity argon atmosphere
US3210950A (en) * 1960-09-26 1965-10-12 Air Prod & Chem Separation of gaseous mixtures

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3509728A (en) * 1966-02-22 1970-05-05 Petrocarbon Dev Ltd Low temperature separation of gases utilizing two distillation columns having a common condenser-evaporator
US3648471A (en) * 1969-02-14 1972-03-14 Genrikh Maxovich Basin Method of liberation of nitrogen and oxygen from air
US4083194A (en) * 1976-12-02 1978-04-11 Fluor Engineers And Constructors, Inc. Process for recovery of liquid hydrocarbons

Also Published As

Publication number Publication date
ES304271A1 (es) 1964-11-01
NL6410425A (nl) 1965-03-24
BE653054A (nl) 1965-03-15
FR1380546A (fr) 1964-12-04
LU46947A1 (nl) 1964-11-14
GB1031107A (en) 1966-05-25
NL143335B (nl) 1974-09-16
DE1250459B (de) 1967-09-21

Similar Documents

Publication Publication Date Title
US2823523A (en) Separation of nitrogen from methane
US3416323A (en) Low temperature production of highly compressed gaseous and/or liquid oxygen
US4704148A (en) Cycle to produce low purity oxygen
US3210951A (en) Method for low temperature separation of gaseous mixtures
US5157926A (en) Process for refrigerating, corresponding refrigerating cycle and their application to the distillation of air
US2495549A (en) Separation of ternary gaseous mixtures containing hydrogen and methane
US3886758A (en) Processes for the production of nitrogen and oxygen
US2873583A (en) Dual pressure cycle for air separation
US2918802A (en) Process of separation of air into its elements
US5392609A (en) Process and apparatus for the production of impure oxygen
US4254629A (en) Cryogenic system for producing low-purity oxygen
US2822675A (en) Production of gaseous oxygen under pressure
US3327489A (en) Method for separating gaseous mixtures
US3209548A (en) Process for the manufacture of oxygen-enriched air
US2526996A (en) Method and apparatus for separating mixed gases
US2959021A (en) Process for air separation by liquefaction and rectification
US2146197A (en) Method of and apparatus for separating mixed gases and vapors
US3056268A (en) Method for stabilizing the operation of a plant for the low temperature rectification of gaseous mixtures
US3173778A (en) Separation of gaseous mixtures including argon
US3210947A (en) Process for purifying gaseous streams by rectification
US2433604A (en) Separation of the constituents of gaseous mixtures
US4356013A (en) Split pressure feed for the selective production of pure oxygen from air
US3058315A (en) Process for supplying a gaseous product to meet a fluctuating demand
US2779174A (en) Low temperature separation of gaseous mixtures
US2327459A (en) Process of and apparatus for separating gas mixtures