Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
  • F23J3/00—Removing solid residues from passages or chambers beyond the fire, e.g. from flues by soot blowers
  • F23J3/02—Cleaning furnace tubes; Cleaning flues or chimneys
• • 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
  • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
  • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of 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
  • 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
• • 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
• • 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
• • 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
  • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
  • F25J3/04248—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
  • F25J3/04309—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 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
  • 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
  • F25J3/04321—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 oxygen
• • 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
  • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
  • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
• • 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
  • F25J3/0446—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 heat generated by mixing two different phases
• • 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
  • F25J3/04642—Recovering noble gases from air
  • F25J3/04648—Recovering noble gases from air argon
  • F25J3/04654—Producing crude argon in a crude argon column
  • F25J3/0466—Producing crude argon in a crude argon column as a parallel working rectification column or auxiliary column system in a single 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
  • 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
  • F25J3/04642—Recovering noble gases from air
  • F25J3/04648—Recovering noble gases from air argon
  • F25J3/04654—Producing crude argon in a crude argon column
  • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
  • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
  • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
• • 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
  • F25J3/04642—Recovering noble gases from air
  • F25J3/04648—Recovering noble gases from air argon
  • F25J3/04654—Producing crude argon in a crude argon column
  • F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual 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
  • F25J2200/00—Processes or apparatus using separation by rectification
  • F25J2200/02—Processes or apparatus using separation by rectification in a single 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
  • F25J2200/00—Processes or apparatus using separation by rectification
  • F25J2200/04—Processes or apparatus using separation by rectification in a dual 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
  • F25J2200/00—Processes or apparatus using separation by rectification
  • F25J2200/08—Processes or apparatus using separation by rectification in a triple 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
  • F25J2200/00—Processes or apparatus using separation by rectification
  • F25J2200/32—Processes or apparatus using separation by rectification using a side column fed by a stream from the 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
  • F25J2200/00—Processes or apparatus using separation by rectification
  • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low 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
  • F25J2205/00—Processes or apparatus using other separation and/or other processing means
  • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification 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
  • F25J2215/00—Processes characterised by the type or other details of the product stream
  • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity 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
  • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
  • F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
• • 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
  • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
  • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the 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
  • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
  • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
• • 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
  • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
  • F25J2235/52—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen enriched compared to air ("crude oxygen")
• • 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
  • Y10S62/923—Inert gas
  • Y10S62/924—Argon

Definitions

• the present invention relates to the air distillation technique by means of an installation provided with an argon production column.
• air distillation installations provided with an argon production column generally comprise a double column consisting of a medium pressure distillation column operating at about 6 bars, a low distillation column pressure operating a little above atmospheric pressure, and a condenser-vaporizer. The air is sent, after purification and cooling, to the bottom of the medium pressure column.
• “rich liquid” (oxygen-enriched air) collected in the bottom of the medium pressure column is sent to the feed at an intermediate point in the low pressure column, while part of the “lean liquid”, consisting almost entirely of nitrogen, collected at the head of the medium pressure column is sent to reflux at the head of the low pressure column.
• the low pressure column is connected to the argon production column by a line called "argon tapping" and a liquid return line minus the argon plug.
• the low pressure column is generally provided in the tank with gaseous oxygen and liquid oxygen withdrawal pipes, and the medium pressure column is generally provided at the head with gaseous nitrogen and liquid nitrogen withdrawal pipes.
• the vapor at the top of the low pressure column (“impure nitrogen”) consists of nitrogen containing up to a few% of oxygen and is generally discharged into the atmosphere.
• impure nitrogen consists of nitrogen containing up to a few% of oxygen and is generally discharged into the atmosphere.
• impure nitrogen gases containing up to a few% of oxygen and is generally discharged into the atmosphere.
• the oxygen is temporarily excess. This is particularly the case during periods of shutdown of the user's factories.
• FR-A-2 550 325 proposes a solution to limit this drawback. This solution has the advantage of being simple, but its effectiveness is limited.
• the distillation of a given air flow is capable of supplying approximately 21% of this oxygen flow and, under certain conditions, this quantity of oxygen is in excess compared to the real needs, while other productions, notably argon, are sought.
• the object of the invention is to make it possible in all cases to optimize the excess oxygen in order to increase the desired productions, in particular that of argon.
• the subject of the invention is a process for the distillation of air by means of an installation comprising a main distillation apparatus associated with an argon production column by an argon tapping pipe, this process being characterized in what: - one sends to the base of a first section of column, of mixture of nitrogen gas possibly impure but practically without argon, and to the sonnet of a second section of column of mixture of liquid oxygen possibly impure would practice without argon;
• At least between the base of the pranier section and the top of the second section is carried out at least one intermediate racking constituting a waste gas or from which such a gas is produced, which is a mixture of nitrogen and oxygen comprising approximately 10 to 30 % oxygen;
• the invention is also concerned with an installation intended for the implementation of such a method.
• This installation of the type comprising a main distillation apparatus associated with an argon production column by an argon tapping pipe, is characterized in that it comprises:
• FIG. 1 is a diagrarrcre which illustrates the basic principle of the invention
• FIG. 2 schematically shows an air distillation installation according to the invention
• Figure 3 schematically shows part of a variant of the installation of Figure 2;
• a “column” or “column section” is used for a material and heat exchange apparatus having the structure of a distillation column, that is to say comprising a packing or a certain number of trays of the type used for distillation.
• FIG. 1 illustrates by a diagram the manner in which a conventional air distillation installation, shown in more detail in the other figures, is modified in accordance with the invention.
• At least two sections of mixing column K1 and K2 are added to the conventional installation, operating under two pressures P1 and P2 which, as will be seen below, may or may not be equal.
• the section K1 is supplied at its base with nitrogen gas which may contain up to a few% of oxygen but which is practically devoid of argon (that is to say containing less than 1% of argon, and preferably less than 0.05% argon), while the K2 section is supplied at its top with liquid oxygen practically free of argon (with the same meaning as above) and nitrogen.
• Overhead steam from section K1 is sent to the base of the section K2, and the tank liquid of the latter is sent under reflux at the top of the section K1.
• lean LP1 liquid consisting of nitrogen containing up to a few% of oxygen, is drawn off and impure oxygen, that is to say containing, is drawn off at the sonnet of the section K2. up to about 15% of nitrogen, and preferably from 5 to 10% of about nitrogen.
• At least one intermediate withdrawal is carried out between the base of the section K1 and the top of the section K2, to constitute a residual gas from the installation composed of an oxygen-nitrogen mixture at approximately 10 to 30% d oxygen, and therefore having a composition similar to that of air but devoid of argon.
• the intermediate racking is carried out between the sections K1 and K2. It can be constituted by overhead steam from section K1, which directly supplies the residual gas R. In some cases, it may be preferable to draw tank liquid LR1 from section K2, this liquid being made up of a mixture oxygen-nitrogen with a content of approximately 40 to 75% of oxygen; this liquid is then sent to the head of a third section, of mixing column K3, fractionating under a pressure P3 and supplied at its base, like the section K1, with nitrogen gas which is possibly impure but practically without argon.
• the residual gas R1 is then drawn off at the head of the section K3, while the tank liquid of this section constitutes lean liquid LP2 consisting, like the liquid LP1, of nitrogen containing up to a few% of oxygen.
• the liquids LP1 and LP2 are sent back to the installation to improve the distillation; the impure gaseous oxygen withdrawn at the head of the section K2 can constitute a production gas, or be purified to produce pure gaseous oxygen, as will be seen below.
• the source of the liquid oxygen and of the nitrogen gas flow (s) will appear in the following description.
• This energy manifests itself in the form of a heat pump type refrigeration transfer between liquid oxygen and the lean liquid LP1 - LP2 and can be used to increase the production of the installation other than oxygen, to to know nitrogen gas under pressure, the liquid productions and especially the argon, came that will appear in the continuation of the description. It is noted that the above technical effect would also be obtained by supplying the s ⁇ met of the section K2 with liquid oxygen containing up to a few% of impurity cam nitrogen.
• FIGS 2 to 9 show several examples of implementation of the basic principle illustrated in Figure 1 with double column air distillation plants.
• the air distillation installation shown in FIG. 2 is intended to produce on the one hand iirpur oxygen containing approximately 5 to 10% of nitrogen, on the other hand of argbn, and possibly of nitrogen. It essentially comprises a double column 1, an argon production column 2, a remixing column 3 and a remixing minaret 4.
• the double column 1 comprises, in a conventional manner, a lower column 5 operating under a medium pressure MP of around 6 bars absolute, an upper column 6 operating under a low pressure BP slightly higher than atmospheric pressure, and a vaporizer-condenser 7 which puts the tank liquid in heat exchange relationship (liquid oxygen practiced pure) of the low pressure column with the overhead vapor (nitrogen practiced pure) of the medium pressure column.
• the air to be treated, compressed to 6 bars, purified and cooled near its dew point, is injected at the bottom of the medium pressure column.
• the bottom liquid of this column rich in oxygen (rich liquid LR at about 40% oxygen) contains almost all of the oxygen and argon from the incoming air; it is relaxed and injected in 8 in an intermediate location of the low pressure column, while liquid from the top of column 5 (liquid poor in oxygen, LP), is expanded and injected in 9 at the top of the low pressure column.
• a pipe 10 for argon tapping sends a gas almost free of nitrogen into column 2, and a pipe 11 makes up the tank liquid of the latter, slightly less rich in argon, about worse at the top level in the low pressure column.
• the impure argon (argon mixture) is extracted from the top of column 2 and is then purified in a conventional manner.
• purified oxygen gas oxygen containing less than 15% of nitrogen, for example 5 to 10% of nitrogen approximately
• the remixing minaret 4 constitutes the section of the mixing column K3 in FIG. 1. Its comunic base directly with the top from the low pressure column 6. It is therefore supplied at its base with impure nitrogen (nitrogen containing up to a few% of oxygen). At its end, this minaret is supplied with 13 by the rich liquid LR1 coming from column 3 and suitably expanded.
• the relatively reversible remixing of the irrigated nitrogen and the rich liquid LR1 produces an additional quantity of poor liquid LP2, consisting of nitrogen containing up to a few% of oxygen, which falls into column 6 and increases the reflux there.
• the waste gas R1 devoid of argon and whose composition is close to that of air is evacuated.
• part of the rich liquid LR or LR1 can be expanded and vaporized in a condenser at the head of column 2, then returned to column 6 near level 8.
• part of the vapor from the top of column 6 can be drawn off, for example to produce by distillation in an auxiliary column section (not shown) pure nitrogen under low pressure.
• liquid is taken from the low pressure column, a few trays above the argon tapping 10, and sent to the head of an auxiliary low pressure column 14; the latter is supplied at its base with impure oxygen from the mixing column 3, expanded at low pressure, in a turbine 15.
• the bottom liquid of the column 14 is impure oxygen without argon, which l 'is added upstream of the p ⁇ rpe 12 to the pure liquid oxygen withdrawn from the low pressure column. All the argon contained in the liquid injected at the top of the column 14 leaves with the overhead vapor of this column and is returned to the low pressure column 6, at about the same level as the withdrawal of said liquid.
• the column 3 operates in the vicinity of the low pressure and receives direct oxygen at the head from the tank of the column 6.
• the turbine 15 of FIG. 3 is eliminated and the columns 3 and 14 are combined in a single ferrule 16.
• the tank of column 3 is supplied with nitrogen obtained by expansion in a turbine 17 of medium pressure nitrogen. As shown, medium pressure nitrogen expanded in the turbine 17 and then in an expansion valve 17A can also be blown at the head of the column 6.
• FIG. 5 shows another means of supplying low pressure nitrogen at the base of column 3: the upper part of column 6 is split by an auxiliary column 18 operating at somewhat higher pressure, for example 1 , 8 bar center 1.4 bar for column 6.
• Part of the treated air flow is diverted and expanded to 1.8 bar in a turbine 19.
• Part of the turbinated flow is sent to the base of column 18, which receives at the head, cam column 6, lean liquid at the appropriate pressure.
• the rest of the turbined air is expanded to 1.4 bar in an expansion valve 20 and blown into column 6, like the tank liquid in column 18. It is pure nitrogen, containing up to 'to a few% of oxygen and practiced no argon, drawn off at the head of column 18, which is used to feed the base of column 3.
• FIG. 6 illustrates a variant of FIG. 5 which makes it possible to remove the pump (not shown) for raising the liquid LP 1.
• the section K1 is transferred above the column 18, in the same shell as that- ci, and the liquid LR 1 is shared between the top of the minaret 4 and that of the section K1.
• a second waste gas R is then produced at the head of the section K, a cam indicated in phantom in FIG. 6.
• the waste gas R1 leaves the minaret 4 at a pressure of the order of 1.3 bar, sufficient for it to be used for the regeneration of the adsorption bottles (not shown) serving purifying the incoming air.
• This is advantageous but results in a relatively high operating pressure, which is costly in terms of energy for compressing the incoming air.
• the air rolling in the valve 20 corresponds to a loss of energy.
• FIG. 7 takes up the principle of FIG. 5 but makes it possible to avoid any rolling of air and to lower the operating pressure: the column 18 is transferred under the column 3, in the same shell; it is supplied at the head by the lean liquid falling from the section K1 and by an addition of lean liquid LP drawn off at the top of the column 5 and expanded in a valve 21, and in the tank by all of the air expanded to 1.8 bar in the turbine 19.
• Came this flow provides at the head of the column 18 a flow of impure nitrogen higher than that necessary for the operation of the column 3, one can withdraw from this one an additional residual gas R, under approximately 1 , 6 bar, which can be used for the regeneration of the above-mentioned adsorption bottles.
• the gas R1 leaving the minaret 4 is then no longer used for this regeneration and need only be at a pressure slightly higher than atmospheric pressure, to overcome the pressure drops of the heat exchange line serving cooling the incoming air. The system operating pressure is thus lowered.
• FIG. 7 shows the origin and the use of the two types of rich liquid: (a) rich liquid with argon, coming on the one hand from the tank of the medium pressure column 5, on the other hand from the tank in column 18. These two streams are combined and serve both to reflux into the low pressure column 6 and to supply the head condenser 2A of column 2, in a conventional manner; and (b) rich liquid LRl without argon, taken between the sections K1 and K2 of column 3 and sent to the head of the minaret 4. Furthermore, by comparing this FIG. 7 with FIG. 1, it can be seen that one performs between the sections K1 and K2 the two withdrawals indicated in FIG. 1, namely a direct withdrawal of waste gas R and a withdrawal of liquid LR1 which, after mixing with nitrogen, also supplies waste gas R1, but at a pressure different.
• FIG. 7 also shows lines for drawing off gaseous oxygen or low pressure liquid from column 6 and nitrogen gas or medium pressure liquid from column 5.
• FIG. 8 Another possibility to avoid any loss of energy by air rolling is illustrated by the installation of FIG. 8.
• the double column 5,6 surmounted by the minaret 4 constituting the section K3 of FIG. 1
• the turbined air in turbine 19 is expanded to 1.3 bar and blown into column 6.
• two auxiliary columns are used: on the one hand a column 3A, operating at 1.4 bar, which joins the column 14 for purifying oxygen and, under it, the section K2 of FIG. 1, and on the other hand a column 3B, operating at 1.5 bar, which joins the section K1 of FIG. 1 and, under this one, a splitting 6A of the upper part of the low pressure column 6.
• the section K2 is supplied at the head by liquid oxygen withdrawn from the tank of column 6 and, in tank, by gas G withdrawn by head of column 3B, that is to say at the head of section K1.
• Rich liquid without argon LR1 withdrawn from the tank of column 3A, is sent under reflux both at the head of column 3B and minaret 4.
• Poor liquid is sent under reflux both at the head of column 6 and of section 6A, while the liquid rich with argon coming from the tank of column 5 is, in part, injected both into column 6 and in section 6A, and, for another part, vaporized in the overhead condenser 2A of column 2 and then injected into the tank of section 6A.
• the very rich liquid collected at the bottom of the latter is in turn injected into column 6.
• FIG. 8 Pressure drop considerations show that the arrangement of Figure 8 is particularly suitable in the case where at least column 2 is fitted with packings. Furthermore, it is understood that the installation of FIG. 8 could also operate by replacing the air trigger with a nitrogen trigger.
• FIG. 9 shows another installation in which the sections K1 and K3 both operate at the pressure of the low pressure column 6 and are combined.
• the double column is surmounted by a remixing column 3B supplied at the head with liquid oxygen coming from the tank of column 6 and in the tank by the purified nitrogen at the head of this same column 6.
• the liquid of tank of column 3B is sent to reflux in column 6, and impure oxygen is drawn off at the top of column 3B.
• the residual gas R is drawn between the sections K2 on the one hand, K1-K3 on the other hand.
• the invention is compatible not only with double column installations, but also with any type of air distillation installation comprising means for producing argon.
• FIG. 10 is a more complete diagram than FIGS. 2 to 9.
• the compressed and purified air is cooled and partially liquefied in a heat exchange line 20.
• the majority of the air flow is expanded to around 1.5 bar in a turbine 21 (Claude cycle), then injected into the distillation column 1A connected to the column 2 for the production of argon.
• the liquefied air, expanded in a valve 22, is injected into the same column. This produces oxygen in the tank and nitrogen at the top.
• This latter gas after heating in the exchange line 20, is partially compressed to 6 bars by a compressor 23, cooled and passes through a coil 24 provided in the tank of column 1A, where it condenses by vaporizing the liquid oxygen, then is partially expanded in a valve 25 and sent backward to the top of the column 1A.
• the rest of the condensed nitrogen is expanded in a valve 26, vaporized in the condenser at the head of column 2 and then sent to the tank of the mixing column 3, bringing together the sections K1 and K2, which operates at 2 to 3 bars.
• the liquid oxygen produced in the tank of column 1A is at least partly brought by pump to the pressure of column 3 and injected at the time of the latter.
• the purified gaseous oxygen withdrawn at the head of column 3 is condensed in a second coil 27 in the bottom of column 1A, expanded in a valve 28 and injected into this same column 1A.
• the section K3 located above the column 1A, is supplied with the s ⁇ met by the rich liquid LR1 drawn off between the sections K1 and K2 and expanded at low pressure, and in the tank by the nitrogen at the head of the column 1A.
• This section K3 produces in the tank lean liquid LP2 which, like the lean liquid LP1 coming from the tank of column 3, is sent under reflux to the s ⁇ met of column 1A; it produces the waste gas R1 at the head, which is heated in the exchange line 20 before being evacuated or, if the pressure is sufficient, used to regenerate the bottles of adsorbent used to purify the incoming air .
• the installation can also produce liquid oxygen, drawn off in the tank. column 1A, gaseous oxygen, also drawn off from the bottom of this column and reheated in the exchange line 20, and nitrogen gas, drawn off at the head of the same column and, after reheating, discharged upstream of the compressor 23.
• gaseous oxygen also drawn off from the bottom of this column and reheated in the exchange line 20
• nitrogen gas drawn off at the head of the same column and, after reheating, discharged upstream of the compressor 23.
• nitrogen can also be taken at 6 bars downstream of compressor 23.

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• 1985
  • 1985-07-15 FR FR8510796A patent/FR2584803B1/fr not_active Expired - Fee Related
• 1986
  • 1986-07-09 EP EP86904215A patent/EP0229803B1/de not_active Expired - Lifetime
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  • 1986-07-09 WO PCT/FR1986/000247 patent/WO1987000609A1/fr active IP Right Grant
  • 1986-07-09 JP JP61503742A patent/JPH0731004B2/ja not_active Expired - Lifetime
  • 1986-07-09 US US07/026,792 patent/US4818262A/en not_active Expired - Lifetime
  • 1986-07-09 DE DE8686904215T patent/DE3669392D1/de not_active Expired - Lifetime
  • 1986-07-09 AU AU61290/86A patent/AU584229B2/en not_active Ceased
  • 1986-07-10 ZA ZA865185A patent/ZA865185B/xx unknown
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• 1987
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