EP3812675A1 - Verfahren und anlage zur luftzerlegung durch kryogene destillation - Google Patents

Verfahren und anlage zur luftzerlegung durch kryogene destillation Download PDF

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Publication number
EP3812675A1
EP3812675A1 EP20203664.6A EP20203664A EP3812675A1 EP 3812675 A1 EP3812675 A1 EP 3812675A1 EP 20203664 A EP20203664 A EP 20203664A EP 3812675 A1 EP3812675 A1 EP 3812675A1
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EP
European Patent Office
Prior art keywords
column
enriched
liquid
oxygen
argon
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.)
Pending
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EP20203664.6A
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English (en)
French (fr)
Inventor
Bertrand DEMOLLIENS
Patrick Le Bot
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
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP3812675A1 publication Critical patent/EP3812675A1/de
Pending legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
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    • 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
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    • 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
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
    • 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
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • 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
    • F25J2250/50—One 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
    • 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
    • F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude 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
    • 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
    • F25J2250/58—One fluid 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/44—Particular materials used, e.g. copper, steel or alloys thereof or surface treatments used, e.g. enhanced surface
    • 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
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection

Definitions

  • a method and an apparatus for separating air by cryogenic distillation The process is carried out using a double air distillation column, well known per se, associated or not with an argon separation column.
  • purified and cooled air is sent to a first column operating at a cryogenic temperature in order to be separated into a gas enriched in nitrogen and a liquid enriched in oxygen.
  • the liquid is withdrawn from the first column and sent to a second column operating at a lower pressure than the first column, after expansion in a valve.
  • Air separation devices often include an argon separation column in addition to the double column.
  • This argon separation column can obviously be used to produce argon but in some cases it is installed primarily for the purpose of increasing the oxygen yield and / or increasing the nitrogen production at a pressure high and / or to allow a lot of air intended for the second column to be expanded to increase the production of frigories and therefore the production of liquid or to improve energy performance.
  • An aim of the present invention is to improve the energy performance of air separation units, with or without the presence of the argon separation column.
  • the invention aims to reduce the additional cost associated with it. to the presence of this column.
  • the gain in energy performance brought about by the invention can be totally or partially achieved at a lower cost.
  • a method according to the characterizing part of claim 1 is known from EP-A-0860670 .
  • the liquid feeding the top condenser of the argon column does not come directly from the first column, but has previously undergone partial vaporization to condense the argon mixture.
  • the liquid thus concentrates in oxygen its vaporization temperature increases.
  • the temperature difference in the argon column condenser is then excessively small and requires a very large exchanger volume. This has the consequence of enlarging the cold box.
  • an apparatus for separating air by cryogenic distillation comprising a first column operating at a first pressure, a second column thermally connected to the first column and operating at a second pressure lower than the first pressure, a heat exchanger, means for sending air cooled and purified of water to the first column operating at a first pressure where it is separated into a gas enriched in nitrogen and a liquid enriched in oxygen, means for withdrawing a liquid enriched in nitrogen relative to the air of the first column, means for sending the enriched liquid nitrogen at the top of the second column, means for withdrawing an oxygen-enriched liquid from the air in the first column, optionally means for sending a first part of the oxygen-enriched liquid to an intermediate level of the second column , optionally after having enriched it with oxygen, means for withdrawing a gas enriched in argon from the air of the second column, means for sending part of the liquid enriched in oxygen to the heat exchanger in order to vaporize at least partially by heat exchange with the gas enriched in argon and means
  • a double air separation column comprising a first column K1 operating at a first pressure and a second column K2 operating at a second pressure, lower than the first pressure.
  • the two columns are connected together thermally, for example by a condenser-reboiler C which vaporizes the bottom oxygen of the second column K2 by heat exchange with the gaseous nitrogen of the first column K1.
  • a nitrogen-rich liquid 11 is sent from the top of the first column K1 to the top of the second column K2.
  • the first column is supplied with gaseous air by an air flow 1 cooled and purified of water and CO2. Air can also be supplied to the second column K2.
  • An oxygen-enriched liquid is withdrawn from the bottom of the first column K1 and divided into two. A part 3 is sent to the heat exchanger E where it is totally vaporized to form a gas 5.
  • the gas 5 is expanded in a turbine T and sent to an intermediate point of the first column K1. The refrigeration production generated at very low temperature by this expansion therefore leads to a gain in the energy consumption of the unit, compared to what would be consumed in the absence of this expansion.
  • the remainder of the oxygen-enriched liquid withdrawn from the tank is expanded in a valve and sent as flow 12 above the arrival points of the flows 5 and 9.
  • the exchanger E contained in an enclosure B, also serves to liquefy an intermediate gas flow 7 from the second column K2.
  • This gas 7 will be withdrawn at a position such that its condensation temperature (bubble point) will be higher than the vaporization temperature of the oxygen-enriched liquid 3 in the exchanger E.
  • its composition will be that of the feed gas of an argon production column.
  • An oxygen-rich liquid 15 is withdrawn from the bottom of the second column K2 and an overhead gas enriched in nitrogen 13 is withdrawn from the top of the same column.
  • FIG. 1b all the tank liquid can be sent to exchanger E where it partially vaporizes.
  • the partially condensed flow is separated in a phase separator 8 to produce a gas 5 and a liquid 100 enriched in oxygen relative to the liquid 3.
  • the formed gas 5 is expanded in a turbine T and the remaining liquid 10 is expanded and sent to the column as fluid 12.
  • the liquid enters the column K2 at a level above the gas of the turbine T since it has been enriched in oxygen.
  • the Figure 1B illustrates only a modified part of the Figure 1a .
  • the oxygen enriched liquid 3 is divided into three parts 3,17,19.
  • Part 17 is sent directly to the second column K2 in liquid form.
  • Part 3, as for Figure 1 heat exchange with a flow enriched in argon 7 which is part of the gas enriched in argon withdrawn from the second column, the rest of the gas 7A being sent directly to feed the argon separation column K3.
  • Part 3 is vaporized to form the gas flow 5 at 2.1 bars, then expanded in the turbine T and sent to the column K2.
  • the flow rate 7 condenses in the exchanger E contained in an enclosure B, and the liquid 9 formed feeds the column K3, preferably a few stages above the gas inlet 7A.
  • the enclosure B is preferably arranged above the point of arrival of the liquid 9 in the column K3.
  • Part 19 of the oxygen-enriched liquid feeds the head condenser N of column K3 without having been enriched in oxygen and vaporizes there to form a gas 23.
  • the gas 23 is mixed with the gas expanded in the turbine T to form a gas 25 which feeds the second column K2.
  • the oxygen-enriched liquid feeds the exchanger E and the head condenser N in parallel.
  • the argon yield is of the order of 80%, if the oxygen purified argon (flow rate 21) is recovered as product. If the flow 21 is not recovered as a pure product, the column K3 can be very small, containing only a few tens of theoretical stages ( ⁇ 50), or even less than 10 theoretical stages.
  • the oxygen-enriched liquid is only divided into two parts 3.3A.
  • Part 3A feeds column K2 and part 3 is partially vaporized in heat exchanger E.
  • the remaining liquid 3B feeds the overhead condenser N of column K3 and the gas 23 formed in the condenser feeds column K2.
  • the gas 7A formed in the exchanger E feeds the turbine T at an inlet pressure of 2.7 bars.
  • the argon yield is of the order of 75 to 76%, if the argon is recovered (flow rate 21).
  • the argon column has a liquid feed in addition to the usual gas feed.
  • the diameter of the column K3 can be reduced by about 20%, for the section above the inlet of the liquid 9, reducing its cost. Since the argon column is the highest column of the apparatus, it is important to be able to reduce its volume and thus reduce the dimensions of the cold box which contains it (not illustrated).
  • column K3 of the Figures 2 and 3 can be inside column K2, arranged concentrically with the shell of column K2.
  • Column K3 can contain structured packings or bulk packings.
  • the gas rising in column K2 will pass either in column K3 or in the annular part surrounding column K2.
  • the top condenser N of column K3 will be used in this case to heat a liquid bath located at mid-height of column K2.
  • the gas from the top of column K3 will pass through a pipe in the top condenser N through a barrier forming a tank halfway up the column K2 and the liquid condensed in the condenser N will pass in the same way in another driving through the barrier to return to column K2.
  • a valve can regulate the quantity of liquid returned from condenser N to column K2.
  • Column K3 is surrounded by an annular section of column K2 where packings are located.
  • the gas separated at the top of the annular section is sent to the column section K2 passing through the barrier in a pipe or will be sent outside the column below the barrier to enter the column above of the barrier.
  • the bottom liquid accumulated above the barrier will be sent to the top of the annular section either by a pipe passing through the barrier or by a pipe connected to the outside of the column.
  • the exchanger E in its enclosure B is still located outside the column K2 and outside the column K3.
  • the flow rate 7 is withdrawn directly from the column K2, without being divided since the flow rate equivalent to 7A rises directly in the column K2 towards the column K3.
  • liquid 3B is injected into column K2 to be directed to condenser N.
  • a metal with better conductivity can be used for the upper part of the shell than for the upper part (for example aluminum at the top of the shell of the K3 column and stainless steel at the bottom of the column) .
  • Another possibility is to use a full aluminum K3 ferrule and apply a coating in the lower section to reduce heat exchange.
  • an argon separation column having an overhead condenser in a second column (low pressure column).
  • One possibility is to position the overhead column so that the overhead gas of the argon column condenses partly in the overhead condenser of the argon column and partly in an overhead condenser of the low pressure column. by heat exchange with oxygen-rich liquid from the bottom of the first column (medium pressure column)
  • the liquid formed in the top condenser of the second column is sent to the top of the second column and the vaporized liquid is sent to a level above the top condenser of the argon column.
  • the overhead condenser can be a film vaporizer.
  • the turbine T can be replaced by a mixing column K4 operating for example at between 2.2 and 2.7 bars, as illustrated in Figure 4 .
  • This mixing column will be fed to the tank by the rich liquid vaporized 5 vaporized by the exchanger E.
  • At the top of the column K4 arrives a flow of impure liquid oxygen. containing about 90 mol% oxygen.
  • the rich vaporized liquid contains 34% oxygen for the case of the Figure 2 and 20% oxygen for the case of Figure 3 .
  • a liquid 31 is withdrawn from the bottom of column K4 containing 65% oxygen (in the case of Figure 2 ) or 50% oxygen (case of Figure 3 ).
  • a gas flow 43 is withdrawn in the middle of the column K4.
  • the gas 35 can replace the gaseous nitrogen coming from the first column in the condenser C of the Figure 2 or 3 . This makes it possible to increase the argon yield by approximately 5% or to increase the production of nitrogen gas at the top of the first column.
  • the Figure 5 further illustrates a variant of Figures 2 and 3 where the oxygen-enriched liquid 3 from the bottom of the first column is enriched with oxygen in an Etienne K5 column, the bottom reboiler E of which corresponds to the exchanger 3 of the preceding figures.
  • the reboiler E is reheated by a gas flow 7 enriched in argon coming from the second argon column.
  • the liquid flow product 9 serves as a second feed to the argon column K3 in addition to the gas feed.
  • the liquid 3 expanded in a valve descends the stages of column K5 and is enriched with oxygen to produce a flow 53 rich in oxygen (75% oxygen), a vessel flow rate and an overhead gas containing only 16% oxygen.
  • the flow 53 feeds the column K2 and allows a gain in argon yield of 3%.
EP20203664.6A 2019-10-24 2020-10-23 Verfahren und anlage zur luftzerlegung durch kryogene destillation Pending EP3812675A1 (de)

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Application Number Priority Date Filing Date Title
FR1911900A FR3102548B1 (fr) 2019-10-24 2019-10-24 Procédé et appareil de séparation d’air par distillation cryogénique

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EP (1) EP3812675A1 (de)
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CN113654302B (zh) * 2021-08-12 2023-02-24 乔治洛德方法研究和开发液化空气有限公司 一种低温空气分离的装置和方法

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JPS54126672A (en) * 1978-03-27 1979-10-02 Hitachi Ltd Air separator
EP0538520A1 (de) * 1991-10-22 1993-04-28 Odessky Institut Nizkotemperaturnoi Tekhniki I Energetiki Lufttrennungsverfahren
EP0841525A2 (de) * 1996-11-11 1998-05-13 The BOC Group plc Lufttrennung
EP0860670A2 (de) 1997-02-11 1998-08-26 Air Products And Chemicals, Inc. Lufttrennung mit Verdampfung und Expansion eines Fluidiums unter mittlerem Druck
EP1108965A1 (de) * 1999-12-13 2001-06-20 Air Products And Chemicals, Inc. Mehrkomponenten-Fluid-Destillationsverfahren zur Herstellung eines Argon-angereicherten Stroms in einem Tieftemperaturluftzerlegungsverfahren

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US4832719A (en) * 1987-06-02 1989-05-23 Erickson Donald C Enhanced argon recovery from intermediate linboil
US4994098A (en) * 1990-02-02 1991-02-19 Air Products And Chemicals, Inc. Production of oxygen-lean argon from air
GB9609099D0 (en) * 1996-05-01 1996-07-03 Boc Group Plc Oxygen steelmaking
DE10113791A1 (de) * 2001-03-21 2002-10-17 Linde Ag Argongewinnung mit einem Drei-Säulen-System zur Luftzerlegung und einer Rohargonsäule
US7487648B2 (en) * 2006-03-10 2009-02-10 Praxair Technology, Inc. Cryogenic air separation method with temperature controlled condensed feed air
US20130019634A1 (en) * 2011-07-18 2013-01-24 Henry Edward Howard Air separation method and apparatus
US10401083B2 (en) * 2015-03-13 2019-09-03 Linde Aktiengesellschaft Plant for producing oxygen by cryogenic air separation
EP3343158A1 (de) * 2016-12-28 2018-07-04 Linde Aktiengesellschaft Verfahren zur herstellung eines oder mehrerer luftprodukte und luftzerlegungsanlage

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS54126672A (en) * 1978-03-27 1979-10-02 Hitachi Ltd Air separator
EP0538520A1 (de) * 1991-10-22 1993-04-28 Odessky Institut Nizkotemperaturnoi Tekhniki I Energetiki Lufttrennungsverfahren
EP0841525A2 (de) * 1996-11-11 1998-05-13 The BOC Group plc Lufttrennung
EP0860670A2 (de) 1997-02-11 1998-08-26 Air Products And Chemicals, Inc. Lufttrennung mit Verdampfung und Expansion eines Fluidiums unter mittlerem Druck
EP1108965A1 (de) * 1999-12-13 2001-06-20 Air Products And Chemicals, Inc. Mehrkomponenten-Fluid-Destillationsverfahren zur Herstellung eines Argon-angereicherten Stroms in einem Tieftemperaturluftzerlegungsverfahren

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US20210123671A1 (en) 2021-04-29
CN112710125A (zh) 2021-04-27
FR3102548A1 (fr) 2021-04-30

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