US3688513A - Production of nitrogen and argon-free oxygen - Google Patents

Production of nitrogen and argon-free oxygen Download PDF

Info

Publication number
US3688513A
US3688513A US30208A US3688513DA US3688513A US 3688513 A US3688513 A US 3688513A US 30208 A US30208 A US 30208A US 3688513D A US3688513D A US 3688513DA US 3688513 A US3688513 A US 3688513A
Authority
US
United States
Prior art keywords
stage
rectifying
argon
nitrogen
column
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
US30208A
Other languages
English (en)
Inventor
Martin Streich
Hartmut Voigt
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.)
Individual
Original Assignee
Individual
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 Individual filed Critical Individual
Application granted granted Critical
Publication of US3688513A publication Critical patent/US3688513A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04454—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 at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another 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
    • 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
    • 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
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • 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
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% 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
    • 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
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon
    • 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
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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

  • a side stream [51] i Cl "F253 3/00 g i s g g containing argon flows from the second rectifying [58] Fleld of Search "62/2 6 stage to the third stage which yields a head product enriched in argon. This head product is pumped back into the upper portion of the second stage.
  • a side product of the second rectifying stage, containing argon, is separated in the third stage into an argon-free sump product and an argon-enriched head product.
  • the argon-free oxygen product is withdrawn partly from the sump of the second rectifying stage and partly from the sump of the third rectifying stage.
  • this classic process was modified to a three-stage rectifying process.
  • the pressures maintained in the medium and low pressure stages are the same as in the classic process.
  • the pressure in the argon rectifying stage corresponds approximately to the pressure in the low pressure stage.
  • argon recovery is about 30 to 60 percent.
  • a mixture of about 45 percent argon, percent oxygen, and 5 percent nitrogen leaves the head of the argon column.
  • the energy consumption for this process is about the same as for the classic process which is considered a special advantage.
  • the energy consumption for air separation can be lowered considerably by using, in the third rectifying stage, a rectifying pressure which is lower by 0.3 to 0.5 atm (atmosphere) than the pressure in the second rectifying stage, and by withdrawing the head product of the third rectifying stage and pumping it into the top portion of the second rectifying stage at a point which is already low in oxygen concentration.
  • the first rectifying stage also can operate at a lower pressure.
  • the compression pressure of the feed air can be 15 atm lower than usual.
  • the energy saving, based on gaseous product, is approximately 10 percent and remains significant, even after mathematical conversion to the product data of the classic process.
  • oxygen losses are reduced considerably. It is particularly surprising that, in spite of the reduced rectifying pressures, an argon-free oxygen product of 99.5 percent purity is recovered.
  • FIGURE of the accompanying drawing is a schematic flow diagram illustrating a preferred embodiment of the invention.
  • the first rectifying stage is represented by column 1, the second stage by column 2, and the third stage by column 3.
  • the major portion of the compressed, precooled air enters rectifying column 1 through line 6 and is separated into nitrogen and an oxygen-enriched fraction.
  • the sump of the second rectifying column 2 yields a practically argonand nitrogen-free oxygen product.
  • a side stream 9, containing argon is withdrawn from rectifying column 2 and separated in rectifying column 3 into an argon-free oxygen sump product and an argon-rich head product.
  • the argon-free oxygen product is withdrawn partly through line 10 from the sump of column 2 being desirably passed in heat exchange with the head product of column 1 in heat exchanger 5, and partly through line 11 from the sump of column 3.
  • the rectifying pressure in column 3 is lower by 0.3 to 0.5 atm than the pressure in column 2.
  • the head product of column 3 is withdrawn through line 4 and introduced by pump 12 into the top portion of column 2 at an upper level which is already low in oxygen concentration.
  • the drawing also shows how the heat input and heat withdrawal at column 3, and the heat input to column 2 can be achieved in an advantageous manner.
  • column 3 it is furthermore advantageous to operate column 3 at an absolute pressure between 0.8 and 1.1 atm.
  • Feed air cooled to a temperature ofl76 C and at an absolute pressure of 4.24 atm, is supplied to the process via line 6.
  • a partial air stream of 13 nm /hr is passed via line 7 through a conventional reheater R and heat exchanger 56 to expansion engine 8 and fed to column 2 at a temperature of 168 C.
  • the main air stream After passing through heat exchanger 5C at the sump of column 2, the main air stream enters column 1 at l78 C. From the head of column 1, 32.8 nm /hr of overhead vapor, after heat exchange with the head product of column 2 in heat exchanger 5D, flows into the upper portion of column 2.
  • the inlet temperature is 1 89 C.
  • a side stream of 14.2 nm /hr, containing argon, is fed via line 9 to column 3.
  • column 3 a head temperature of 1 855 C and a sump temperature of 183 C are maintained.
  • a head product of 2 nm /hr from column 3 is pumped into the upper portion of column 2 by way ofline 4 and pump 12.
  • Liquid product is withdrawn at a rate equivalent to 7.8 nm /hr from the sump of column 2 by line 10, and at a rate of 12.2 nm lhr as 99.5 percent pure oxygen from column 3 by line 11.
  • the argon-contaminated nitrogen leaves overhead of column 2 at a rate of nm /hr.
  • the oxygen product is recovered by way of lines 10 and 1] at 183 C and atmospheric pressure, and the nitrogen at l78 C and at an absolute pressure of 1.2 atm after leaving heat exchan er 5G.
  • the pressures o the process may be varied within the given limits. This process however is also suitable for application of the method of balancing refrigeration losses in the classic process by work-performing nitrogen expansion.
  • the recovery of pure nitrogen is not shown in the flow diagram or described in the process example but could be done in the conventional manner without essentially changing the pressure conditions.
  • a process for the recovery of substantially nitrogen-and argon-free oxygen by rectification of air in three rectifying stages which comprises separating air into a nitrogen fraction and an oxygen-enriched fraction in the first rectifying stage, passing entirely said nitrogen fraction to the top portion of the second rectifying stage and said oxygen-enriched fraction to the middle portion of said second stage, passing an argon-containing stream from the bottom portion of said second stage to the middle portion of the third rectifying stage, pumping entirely an argon-rich head product from said third stage to said second stage at a level between the introduction of said nitrogen fraction and said oxygen-enriched fraction, the pressure of said third stage being lower by 0.3 to 0.5 atmosphere than the pressure of said second stage, discharging a nitrogen head product from said second stage, and recovering said oxygen from the bottom portions of said second and third stages.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US30208A 1969-05-06 1970-04-20 Production of nitrogen and argon-free oxygen Expired - Lifetime US3688513A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE1922956 1969-05-06

Publications (1)

Publication Number Publication Date
US3688513A true US3688513A (en) 1972-09-05

Family

ID=5733336

Family Applications (1)

Application Number Title Priority Date Filing Date
US30208A Expired - Lifetime US3688513A (en) 1969-05-06 1970-04-20 Production of nitrogen and argon-free oxygen

Country Status (6)

Country Link
US (1) US3688513A (fr)
BE (1) BE748971A (fr)
DE (1) DE1922956B1 (fr)
FR (1) FR2042419B1 (fr)
GB (1) GB1260624A (fr)
NL (1) NL7004606A (fr)

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1984003934A1 (fr) * 1983-03-31 1984-10-11 Donald C Erickson Distillation de recyclage cryogenique avec echange de chaleur latente multiple
WO1984004957A1 (fr) * 1983-06-06 1984-12-20 Donald C Erickson Separation d'air cryogenique a triple pression avec echange de chaleur latente de basse pression a pression moyenne
WO1986001283A1 (fr) * 1984-08-20 1986-02-27 Erickson Donald C Oxygene et argon de grande purete et a energie reduite
WO1987005098A1 (fr) * 1986-02-20 1987-08-27 Erickson Donald C Production d'oxygene et d'argon par distillation a contre pression
US4723975A (en) * 1985-05-17 1988-02-09 The Boc Group Plc Air separation method and apparatus
US4747859A (en) * 1986-09-12 1988-05-31 The Boc Group Plc Air separation
US4747860A (en) * 1986-08-28 1988-05-31 The Boc Group Plc Air separation
WO1988006705A1 (fr) * 1987-02-26 1988-09-07 Donald Erickson Pression accrue d'alimentation en oxygene tres pur a faible consommation d'energie
US4775399A (en) * 1987-11-17 1988-10-04 Erickson Donald C Air fractionation improvements for nitrogen production
US4824453A (en) * 1987-07-09 1989-04-25 Linde Aktiengesellschaft Process and apparatus for air separation by rectification
US4932212A (en) * 1988-10-12 1990-06-12 Linde Aktiengesellschaft Process for the production of crude argon
US5049173A (en) * 1990-03-06 1991-09-17 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants
US5235816A (en) * 1991-10-10 1993-08-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
US5245832A (en) * 1992-04-20 1993-09-21 Praxair Technology, Inc. Triple column cryogenic rectification system
US6295840B1 (en) * 2000-11-15 2001-10-02 Air Products And Chemicals, Inc. Pressurized liquid cryogen process
US6397631B1 (en) 2001-06-12 2002-06-04 Air Products And Chemicals, Inc. Air separation process
FR2831250A1 (fr) * 2002-02-25 2003-04-25 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
US20100242538A1 (en) * 2009-03-26 2010-09-30 Neil Mark Prosser Cryogenic rectification method
US10852061B2 (en) 2017-05-16 2020-12-01 Terrence J. Ebert Apparatus and process for liquefying gases

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4842625A (en) * 1988-04-29 1989-06-27 Air Products And Chemicals, Inc. Control method to maximize argon recovery from cryogenic air separation units
CN1025067C (zh) * 1989-02-23 1994-06-15 琳德股份公司 精馏分离空气的方法及装置
US5305611A (en) * 1992-10-23 1994-04-26 Praxair Technology, Inc. Cryogenic rectification system with thermally integrated argon column

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1880981A (en) * 1930-02-07 1932-10-04 Pollitzer Franz Separation of oxygen, nitrogen, and argon from air
US3039274A (en) * 1958-03-28 1962-06-19 Union Carbide Corp Process and apparatus for purifying and separating compressed gas mixtures
US3123457A (en) * 1960-12-22 1964-03-03 E smith
US3127260A (en) * 1964-03-31 Separation of air into nitrogen
US3210948A (en) * 1958-05-19 1965-10-12 Air Prod & Chem Method for fractionating gaseous mixtures
US3264830A (en) * 1963-08-09 1966-08-09 Air Reduction Separation of the elements of air
US3363427A (en) * 1964-06-02 1968-01-16 Air Reduction Production of ultrahigh purity oxygen with removal of hydrocarbon impurities

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3127260A (en) * 1964-03-31 Separation of air into nitrogen
US1880981A (en) * 1930-02-07 1932-10-04 Pollitzer Franz Separation of oxygen, nitrogen, and argon from air
US3039274A (en) * 1958-03-28 1962-06-19 Union Carbide Corp Process and apparatus for purifying and separating compressed gas mixtures
US3210948A (en) * 1958-05-19 1965-10-12 Air Prod & Chem Method for fractionating gaseous mixtures
US3123457A (en) * 1960-12-22 1964-03-03 E smith
US3264830A (en) * 1963-08-09 1966-08-09 Air Reduction Separation of the elements of air
US3363427A (en) * 1964-06-02 1968-01-16 Air Reduction Production of ultrahigh purity oxygen with removal of hydrocarbon impurities

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4605427A (en) * 1983-03-31 1986-08-12 Erickson Donald C Cryogenic triple-pressure air separation with LP-to-MP latent-heat-exchange
WO1984003934A1 (fr) * 1983-03-31 1984-10-11 Donald C Erickson Distillation de recyclage cryogenique avec echange de chaleur latente multiple
WO1984004957A1 (fr) * 1983-06-06 1984-12-20 Donald C Erickson Separation d'air cryogenique a triple pression avec echange de chaleur latente de basse pression a pression moyenne
AU568140B2 (en) * 1983-06-06 1987-12-17 Donald C. Erickson Cryogenic triple-pressure air separation with lp-to-mp latent-heat-exchange
US4578095A (en) * 1984-08-20 1986-03-25 Erickson Donald C Low energy high purity oxygen plus argon
WO1986001283A1 (fr) * 1984-08-20 1986-02-27 Erickson Donald C Oxygene et argon de grande purete et a energie reduite
AU578311B2 (en) * 1984-08-20 1988-10-20 Donald C. Erickson Low energy high purity oxygen plus argon
US4781739A (en) * 1984-08-20 1988-11-01 Erickson Donald C Low energy high purity oxygen increased delivery pressure
US4723975A (en) * 1985-05-17 1988-02-09 The Boc Group Plc Air separation method and apparatus
WO1987005098A1 (fr) * 1986-02-20 1987-08-27 Erickson Donald C Production d'oxygene et d'argon par distillation a contre pression
US4756731A (en) * 1986-02-20 1988-07-12 Erickson Donald C Oxygen and argon by back-pressured distillation
US4747860A (en) * 1986-08-28 1988-05-31 The Boc Group Plc Air separation
US4747859A (en) * 1986-09-12 1988-05-31 The Boc Group Plc Air separation
WO1988006705A1 (fr) * 1987-02-26 1988-09-07 Donald Erickson Pression accrue d'alimentation en oxygene tres pur a faible consommation d'energie
US4824453A (en) * 1987-07-09 1989-04-25 Linde Aktiengesellschaft Process and apparatus for air separation by rectification
US4775399A (en) * 1987-11-17 1988-10-04 Erickson Donald C Air fractionation improvements for nitrogen production
WO1989004942A1 (fr) * 1987-11-17 1989-06-01 Erickson Donald C Fractionnement d'air ameliore a des fins de production d'azote
US4932212A (en) * 1988-10-12 1990-06-12 Linde Aktiengesellschaft Process for the production of crude argon
US5049173A (en) * 1990-03-06 1991-09-17 Air Products And Chemicals, Inc. Production of ultra-high purity oxygen from cryogenic air separation plants
US5235816A (en) * 1991-10-10 1993-08-17 Praxair Technology, Inc. Cryogenic rectification system for producing high purity oxygen
US5245832A (en) * 1992-04-20 1993-09-21 Praxair Technology, Inc. Triple column cryogenic rectification system
US6295840B1 (en) * 2000-11-15 2001-10-02 Air Products And Chemicals, Inc. Pressurized liquid cryogen process
US6397631B1 (en) 2001-06-12 2002-06-04 Air Products And Chemicals, Inc. Air separation process
FR2831250A1 (fr) * 2002-02-25 2003-04-25 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
US20100242538A1 (en) * 2009-03-26 2010-09-30 Neil Mark Prosser Cryogenic rectification method
US8448463B2 (en) 2009-03-26 2013-05-28 Praxair Technology, Inc. Cryogenic rectification method
US10852061B2 (en) 2017-05-16 2020-12-01 Terrence J. Ebert Apparatus and process for liquefying gases

Also Published As

Publication number Publication date
FR2042419A1 (fr) 1971-02-12
FR2042419B1 (fr) 1973-10-19
GB1260624A (en) 1972-01-19
DE1922956B1 (de) 1970-11-26
BE748971A (fr) 1970-09-16
NL7004606A (fr) 1970-11-10

Similar Documents

Publication Publication Date Title
US4222756A (en) Tonnage nitrogen generator
US4615716A (en) Process for producing ultra high purity oxygen
EP0697576B1 (fr) Procédé et dispositif de séparation d'air
US4717410A (en) Process and installation for producing nitrogen under pressure
US5331818A (en) Air separation
US5123249A (en) Air separation
US5896755A (en) Cryogenic rectification system with modular cold boxes
US5546766A (en) Air separation
US5485729A (en) Air separation
EP0341512A1 (fr) Système de régulation pour maximiser la récupération de l'argon des unités cryogéniques de séparation d'air
US5305611A (en) Cryogenic rectification system with thermally integrated argon column
US5546767A (en) Cryogenic rectification system for producing dual purity oxygen
EP0338022B1 (fr) Refroidissement d'air par detente partielle pour la separation cryogenique de l'air
US5934104A (en) Multiple column nitrogen generators with oxygen coproduction
US5893276A (en) Air separation
US4783208A (en) Air separation
JPH08271141A (ja) 空気の分離
US3375673A (en) Air separation process employing work expansion of high and low pressure nitrogen
US5692398A (en) Production of argon
US4604117A (en) Hybrid nitrogen generator with auxiliary column drive
US6536232B2 (en) Method for plant and separating air by cryogenic distillation
US5092132A (en) Separation of air: improved heylandt cycle
US4356013A (en) Split pressure feed for the selective production of pure oxygen from air
US3108867A (en) Separation of the elements of air
US5586451A (en) Process and installation for the production of oxygen by distillation of air