US3754406A - The production of oxygen - Google Patents

The production of oxygen Download PDF

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US3754406A
US3754406A US00124253A US3754406DA US3754406A US 3754406 A US3754406 A US 3754406A US 00124253 A US00124253 A US 00124253A US 3754406D A US3754406D A US 3754406DA US 3754406 A US3754406 A US 3754406A
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pressure column
low pressure
liquid
stream
nitrogen
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R Allam
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Air Products and Chemicals Inc
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04854—Safety aspects of operation
    • F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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    • 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
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    • 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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
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    • 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
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    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04424—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system without thermally coupled high and low pressure columns, i.e. a so-called split columns
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884—Arrangement of reboiler-condensers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • 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
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • 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
    • F25J2235/02—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pump in general or hydrostatic pressure increase
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream 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
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream 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
    • F25J2250/02—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
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    • 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
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    • 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
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • 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

Definitions

  • ABSTRACT (22] Filed: Man 5 1971 A plant for the production of low purity oxygen, in which a low pressure stream of incoming air is cooled PP 124,253 against outgoing gas streams and fed into a high pressure fractionating column, and a high pressure stream [30] Foreign Appucauon Prim-y of incoming air is cooled against outgoing gas streams, Mar. 16 1970 Great Britain 12 586/70 partially 9 bmlmg net in a product vaporizer, and separated into gas and 52 US. Cl. 62/41 62/14 62/30 liquid stream the liquid stream being summed and 62/38 62/29 expanded into a low pressure fractionating column s 1 1 rm. c1.
  • Oxygen enrichment may also be economically benficial in glass melting furnaces, the fire refining of copper and numerous processes associated with the petrochemical and petroleum cracking industries.
  • the oxygen from the air separation unit is often mixed with varying quantities of air to produce an enriched air stream which may contain from 25 to 35 oxygen.
  • the purity of the oxygen producedfrom the air separation plant determines the amount of air which must be added to produce a final enriched air stream.
  • the overall cost of producing the enriched air stream is thus a function of the cost of oxygen from the air separation unit, the cost of compressing the oxygen to the enriched air delivery pressure and the cost of com.- pressing the air which is mixed with the oxygen to the enriched air delivery pressure.
  • the pressure at which the enrichedair is used is usually less than 50 psia, for example, when. oxygen enriched air is blown into a blast furnace producing iron,
  • low purity oxygen is obtained from the fractionation of air in a plant operating according to a split pressure cycle, with a low pressure air feed passing, after cooling, to a high pres.- sure fractionating column, and a high pressure feed passing, after cooling, to a product vaporizer inwhich it is partially condensed against boilingoxygenproduct, the liquid fraction then being sub-cooled and flashed down to low pressure column pressure for admission to a low pressure fractionating column.
  • a major portion of the vapour fraction of the high pressure feed may be reheated and expanded to provide plant refrigeration, and a minor portion condensed against waste nitrogen and combined with the subcooled liquid fraction.
  • An important preferred feature of the cycle is that a first external reboiler/condenser supplies the vapour boil-up for the low pressure column when crude liquid from the base of the high pressure column vaporizes against condensing nitrogen, and a second external reboiler/condenser condenses the remaining nitrogen from the high pressure column against a boiling liquid.
  • a liquid oxygen stream can be withdrawn from the base of the low pressure distillation column and passed through a pump'where its pressure is raised to therequired oxygen product delivery pressure, and the .oxy-
  • gen product can be vaporized in a reboiler-condenser with heat transferred from the condensing high pressure air stream.
  • Such a plant can produce oxygen product at up to 70 oxygen content.
  • the pressure of oxygen is fixed by the pressure of the high pressure air stream, for example, 50 psia oxygen can be produced with a high pressure air pressure of 109 psia entering the cold box.
  • the limit of oxygen purity is fixed by the equilibrium between liquid and vapour at the bottom tray of the low pressure distillation column and the mass balance around the base of the low pressure column.
  • the use of the vaporized crude oxygen stream as the vapour feed to the base of the low pressure column sets an upper limit of about 70 oxygen on the liquid collecting in the sump of the low pressure column.
  • FIG. 1 is a flow diagram of the complete plant
  • FIG. 2 illustrates a modification of the plant of FIG.
  • the reversing heat exchangers are a well known means of cooling down the feed stream to a low temperature plant against warming product streams and at the same time causing high boiling point impurities to beremoved from the cooling stream and sublimed into one of the low pressure warming streams by switching the cooling stream and the particular warming stream passages at regular intervals.
  • This switching of the two streams between identical sets of passages in the heat exchanger is accomplished by means of switch valves at the warm end of the heat exchanger and self-acting check valves at the cold end of the heat exchanger.
  • the air and waste nitrogen streams are switched at regular intervals to remove water and carbon dioxide from the air streams.
  • the rest of the plant air is delivered at 109.0 psia. It is cooled in high pressure reversing heat exchanger cores E103 and E104 and enters a product vapourizer E109 where it is partially condensed against boiling product liquid oxygen.
  • the resulting two-phase air mixture passes into a phase separator C110.
  • the liquid air fraction about of the total high pressure air stream, is passed through a subcooler E108 where it is cooled against the product liquid oxygen stream then flashed down to low pressure column. pressure and fed into a separator C107.
  • the liquid portion of the streain'from' the separator C107 passes through an external reboiler/condenser E106 in which'about 88 of the-stream is vaporized against condensing nitrogen from the top of the high pressure column C101.
  • the liquid and vapour air fractions from the separator C107 then enter a low pressure fractionating column-C102.
  • the operating pressure of the low pressure column is 21.5 psia at the base. 1 I
  • Crude liquid oxygen containing 44 oxygen withdrawn from the bottom of the high pressure column C101, is sub-cooled against waste nitrogen from the top of the low pressure column in a main sub-cooler E105. Hydrocarbons are then removed in adsorbers C and the crude liquid is flashed down to low pressure column pressure and fed into a separator C108.
  • the liquid stream from the separator C108 is mostly vaporized in an external reboiler/condenser E107 against condensing nitrogen from the top of the high pressure column,
  • a small liquid purge stream is taken from the separator C108 to the sump of the column C102, by-passing the reboiler/condenser E107, to prevent possible hydrocarbon buildup.
  • the operating pressure of the high pressure column C101 is 48.3 psia at the top. Nitrogen gas leaving the top of the high pressure column C101 is totally condensed in the external reboiler/condensers E106 and E107 and part of it provides the reflux for the high pressure column C101. The remaining part is subcooled against waste nitrogen from the top of the low pressure column C102 in the main sub-cooler E105 and flashed down to low pressure column pressure to provide the reflux for the low pressure column C102.
  • vapour about 25 of the total high pressure air stream leaves the separator C110 as vapour. 90% of this vapour fraction is used as a reheat stream for the high and low pressure heat exchanger cold cores E102 and E104.
  • This method of controlling the temperature difference at the cold ends of the reversing heat exchangers E102 and E104 ensures that the solid carbon dioxide deposited from the air stream on to the surface of the heat exchangers is sublimed into the waste nitrogen stream when the exchangers are switched.
  • the remaining of vapour is condensed in a nitrogen superheater E110 against that fraction of waste nitrogen from the sub-cooler E105 which leaves the plant through the high pressure reversing heat exchangers E103 and E104.
  • the liquid air stream leaving the superheater E110 rejoins the main liquid air stream from the subcooler E108.
  • the function of the nitrogen superheater E110 is to warm the outgoing nitrogen sufficiently to ensure that the high pressure air feed is not liquefied in the cold cores E104 of the high pressure reversing heat exchanger. This is necessary for proper removal of CO, in the reversing heat exchangers E103 and E104.
  • the fraction of the high pressure air which has been reheated in the reversing heat exchangers is expanded through a turbo-expander K103 and provides the plant refrigeration requirement.
  • a by-pass is available to pass more high pressure air through the turbine should additional refrigeration be required.
  • the expander exhaust is cooled in the main sub-cooler E105 and enters the low pressure column C102 slightly superheated.
  • Outgoing waste nitrogen from the low pressure column C102 is warmed against liquid nitrogen from the high pressure column, the crude liquid from the high pressure column, and the turbo-expander exhaust stream, in the main sub-cooler E105. It leaves the plant via the high and low pressure reversing heat exchangers E101 to E104.
  • Liquid containing 68 oxygen is withdrawn from the low pressure column sump and raised in pressure-by a pump G101 to 55 psia.
  • the total stream is passed through hydrocarbon adsorbers C106, warmed to its bubble point against liquid air in the sub-cooler E108 and fed to a separator C109.
  • a small liquid bleed from this separator is flashed down to low pressure column pressure and returned to the low pressure column to prevent possible hydrocarbon buildup.
  • the remaining liquid oxygen is totally vaporized against condensing high pressure air in the product vaporizer E109. This, the product stream, passes through the reversing heat exchangers Emil-E104, and leaves the plant at 50 psia.
  • the concentration of CO in the high pressure air leaving the high pressure reversing heat exchanger E104 is about 0.3 ppm, and in addition, there may be some solid CO carryover from the heat exchanger E104.
  • This CD would tend to deposit in the air channels at the top end of the product vaporizer E109 where no liquefaction takes place unless special methods were used to prevent this.
  • meth ods are available to prevent this deposition.
  • the high pressure air may be fed into the vaporizer E109 at a point part way down its length as indicated in FIG. 1. This arrangement leaves some free surface area above the feed point where condensation will take place providing a falling liquid film to wash away any CO deposited on the surface area below or near the feed point.
  • Another method is to pump a small liquid bleed from the bottom of the separator C110 to the top of the vaporizer E109 by a pump as shown in FIG. 2. This arrangement will also ensure that the incoming air meets a falling liquid film to dissolve and wash away any CO deposition.
  • a further method is to pass the high pressure air stream leaving the high pressure reversing heat exchangers through carbon dioxide absorbers. These will also remove any hydrocarbons in the stream.
  • the CO concentration in the vapour fraction leaving the separator C1 10 is so low that there is no risk of CO deposition in the expander K103 or in the main subcooler E105. Also, the vapour leaving the separator is at its dewpoint and will immediately condense in the nitrogen superheater E110 giving no deposition problem in that unit.
  • the plant described has been designed to eliminate problems of CO, deposition and hydrocarbon build-up which are often critical in low purity oxygen plants.
  • Variations on the design described above may be considered which use other means than reversing heat exchangers such as plate-fin heat exchangers, to cool the air and remove water and carbon dioxide impurities. These would include regenerators filled with stones or other types of packing and having air sidestreams instead of reheat streams for temperature difference control.
  • Plant for the production of low purity oxygen by the fractionation of air comprising a low pressure compressor compressing a first air feed stream in a first feed line, a high pressure compressor compressing a second air feed stream in a second feed line, a first heat exchanger in which said first feed stream from said low pressure compressor is cooled against outgoing gas streams, a high pressure fractionating column receiving the cooled first feed stream from said first heat exchanger as feed, a second heat exchanger in which said second feed stream from said high pressure compressor is cooled against outgoing gas streams, a product vaporizer in which said cooled second feed stream from said second heat exchanger is partially condensed against boiling oxygen product, a first separator receiving said partially condensed second feed stream from said product vaporizer and separating it into a liquid fraction stream, a first sub-cooler receiving said liquid fraction stream from said first separator and cooling it against outgoing liquid oxygen, a low pressure fractionating column receiving said cooled liquid fraction stream from said sub-cooler as feed after flashing of said cooled liquid fraction stream down to low
  • Plant according to claim 1 further comprising passages in said second heat exchanger receiving a major proportion of said vapour fraction stream from said first separator and reheating said major proportion of said vapour fraction stream, an expander receiving saidreheated major proportion of said vapour fraction stream from said passages and expanding it to provide plant refrigeration, and an expander exhaust line delivering the exhaust from said expander to said low pressure column as feed.
  • Plant according to claim 2 further comprising a nitrogen superheater in which a minor proportion of said vapour fraction stream from said first separator is condensed against outgoing waste nitrogen in said waste nitrogen line, the condensed minor proportion of said vapour fraction stream from said nitrogen superheater being combined with said cooled liquid fraction stream from said sub-cooler for delivery to said low pressure column.
  • Plant according to claim 1 further comprising a first external reboiler/condenser receiving crude liquid oxygen from the bottom of said high pressure column after it has been flashed down to low pressure column 'pressure, and partially vaporizing it against a condensportion of tne nitrogen from the top of the high pressure column is condensed against the boiling cooled liquid fraction stream from said sub-cooler before said fraction stream enters the low pressure column, the condensed nitrogen from said reboiler/condensers providing reflux streams for both columns.
  • a first external reboiler/condenser receiving crude liquid oxygen from the bottom of said high pressure column after it has been flashed down to low pressure column 'pressure, and partially vaporizing it against a condensportion of tne nitrogen from the top of the high pressure column is condensed against the boiling cooled liquid fraction stream from said sub-cooler before said fraction stream enters the low pressure column, the condensed nitrogen from said reboiler/condensers providing reflux streams
  • Plant according to claim 5 further comprising a second sub-cooler in which the nitrogen reflux stream for the low pressure column is sub-cooled against the waste nitrogen stream from the top of that column.
  • said expander exhaust line includes a cooler in which the expander exhaust is cooled against the waste nitrogen from the top of the low pressure column.
  • Plant according to claim 1 further comprising a pump in said outgoing liquid product line which pumps the liquid oxygen to a higher pressure before it enters said product vaporizer.
  • Plant according to claim 10 further comprising a bleed line withdrawing a small liquid bleed from said liquid fraction stream leaving said separator and delivering it to said product vaporizer passages at the top of said vaporizer.
  • Plant according to claim 1 further comprising a second separator receiving the product oxygen from said product vaporizer and separating it into a vaporized product fraction and a liquid product fraction, a line returning said liquid product fraction tosaid product vaporizer, a gaseous product line delivering said vaporized product fraction to said first and second heat exchangers, and a bleed line delivering a small amount of said liquid product fraction to said low pressure column.
  • Plant according to claim 13 comprising further separators respectively receiving the crude liquid oxygenfrom said first reboiler/condenser and said feed liquid fraction stream from said second reboiler/condenser, each of said further separators having a liquid delivery line returning separated liquid to the respective reboiler/condenser, a gas delivery line feeding separated vapour to said low pressure volumn, and a bleed line delivering a small portion of separated liquid to said low pressure column.

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US4407135A (en) * 1981-12-09 1983-10-04 Union Carbide Corporation Air separation process with turbine exhaust desuperheat
US4702757A (en) * 1986-08-20 1987-10-27 Air Products And Chemicals, Inc. Dual air pressure cycle to produce low purity oxygen
US4704147A (en) * 1986-08-20 1987-11-03 Air Products And Chemicals, Inc. Dual air pressure cycle to produce low purity oxygen
US4704148A (en) * 1986-08-20 1987-11-03 Air Products And Chemicals, Inc. Cycle to produce low purity oxygen
US4783210A (en) * 1987-12-14 1988-11-08 Air Products And Chemicals, Inc. Air separation process with modified single distillation column nitrogen generator
US4848996A (en) * 1988-10-06 1989-07-18 Air Products And Chemicals, Inc. Nitrogen generator with waste distillation and recycle of waste distillation overhead
US4869742A (en) * 1988-10-06 1989-09-26 Air Products And Chemicals, Inc. Air separation process with waste recycle for nitrogen and oxygen production
US5098456A (en) * 1990-06-27 1992-03-24 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with dual feed air side condensers
US5108476A (en) * 1990-06-27 1992-04-28 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with dual temperature feed turboexpansion
US5114452A (en) * 1990-06-27 1992-05-19 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system for producing elevated pressure product gas
US5148680A (en) * 1990-06-27 1992-09-22 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with dual product side condenser
US5337570A (en) * 1993-07-22 1994-08-16 Praxair Technology, Inc. Cryogenic rectification system for producing lower purity oxygen
US5456083A (en) * 1994-05-26 1995-10-10 The Boc Group, Inc. Air separation apparatus and method
US5471842A (en) * 1994-08-17 1995-12-05 The Boc Group, Inc. Cryogenic rectification method and apparatus
US5655388A (en) * 1995-07-27 1997-08-12 Praxair Technology, Inc. Cryogenic rectification system for producing high pressure gaseous oxygen and liquid product
US5792523A (en) * 1996-03-14 1998-08-11 Aga Aktiebolag Krypton gas mixture for insulated windows
EP0959313A2 (en) * 1998-05-18 1999-11-24 Praxair Technology, Inc. Cryogenic rectification system with integral product boiler
EP1098152A1 (fr) * 1999-11-05 2001-05-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d'air par distillation cryogénique
US20090277220A1 (en) * 2008-05-07 2009-11-12 Henry Edward Howard Method and apparatus for separating air
US20130086940A1 (en) * 2010-06-18 2013-04-11 L'Air Liquide Societe Anonyme pout l'Etude et l'Exploitation des Procedes Georges Claude Air separation plant and process operating by cryogenic distillation
US20160010551A1 (en) * 2014-07-08 2016-01-14 8 Rivers Capital, Llc Method and system for power production wtih improved efficiency
EP2686628B1 (fr) * 2011-03-18 2021-01-13 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Appareil et procede de separation d'air par distillation cryogenique
US10914232B2 (en) 2018-03-02 2021-02-09 8 Rivers Capital, Llc Systems and methods for power production using a carbon dioxide working fluid
US20220252345A1 (en) * 2019-04-05 2022-08-11 Linde Gmbh Method for operating a heat exchanger, arrangement with a heat exchanger, and system with a corresponding arrangement
US11441841B2 (en) * 2018-12-28 2022-09-13 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Heat exchanger assembly and method for assembling same

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JPS55152375A (en) * 1979-05-17 1980-11-27 Union Carbide Corp Low temperature production system of low purity oxygen
US4895583A (en) * 1989-01-12 1990-01-23 The Boc Group, Inc. Apparatus and method for separating air
US5829271A (en) * 1997-10-14 1998-11-03 Praxair Technology, Inc. Cryogenic rectification system for producing high pressure oxygen

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Publication number Priority date Publication date Assignee Title
US4372765A (en) * 1980-02-26 1983-02-08 Kabushiki Kaisha Kobe Seiko Sho Air liquefaction and separation process and equipment
US4407135A (en) * 1981-12-09 1983-10-04 Union Carbide Corporation Air separation process with turbine exhaust desuperheat
US4702757A (en) * 1986-08-20 1987-10-27 Air Products And Chemicals, Inc. Dual air pressure cycle to produce low purity oxygen
US4704147A (en) * 1986-08-20 1987-11-03 Air Products And Chemicals, Inc. Dual air pressure cycle to produce low purity oxygen
US4704148A (en) * 1986-08-20 1987-11-03 Air Products And Chemicals, Inc. Cycle to produce low purity oxygen
US4783210A (en) * 1987-12-14 1988-11-08 Air Products And Chemicals, Inc. Air separation process with modified single distillation column nitrogen generator
US4848996A (en) * 1988-10-06 1989-07-18 Air Products And Chemicals, Inc. Nitrogen generator with waste distillation and recycle of waste distillation overhead
US4869742A (en) * 1988-10-06 1989-09-26 Air Products And Chemicals, Inc. Air separation process with waste recycle for nitrogen and oxygen production
US5098456A (en) * 1990-06-27 1992-03-24 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with dual feed air side condensers
US5108476A (en) * 1990-06-27 1992-04-28 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with dual temperature feed turboexpansion
US5114452A (en) * 1990-06-27 1992-05-19 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system for producing elevated pressure product gas
US5148680A (en) * 1990-06-27 1992-09-22 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with dual product side condenser
US5337570A (en) * 1993-07-22 1994-08-16 Praxair Technology, Inc. Cryogenic rectification system for producing lower purity oxygen
US5456083A (en) * 1994-05-26 1995-10-10 The Boc Group, Inc. Air separation apparatus and method
US5471842A (en) * 1994-08-17 1995-12-05 The Boc Group, Inc. Cryogenic rectification method and apparatus
US5655388A (en) * 1995-07-27 1997-08-12 Praxair Technology, Inc. Cryogenic rectification system for producing high pressure gaseous oxygen and liquid product
US5792523A (en) * 1996-03-14 1998-08-11 Aga Aktiebolag Krypton gas mixture for insulated windows
EP0959313A3 (en) * 1998-05-18 2000-07-12 Praxair Technology, Inc. Cryogenic rectification system with integral product boiler
EP0959313A2 (en) * 1998-05-18 1999-11-24 Praxair Technology, Inc. Cryogenic rectification system with integral product boiler
EP1098152A1 (fr) * 1999-11-05 2001-05-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé et appareil de séparation d'air par distillation cryogénique
FR2800859A1 (fr) * 1999-11-05 2001-05-11 Air Liquide Procede et appareil de separation d'air par distillation cryogenique
US20090277220A1 (en) * 2008-05-07 2009-11-12 Henry Edward Howard Method and apparatus for separating air
US8286446B2 (en) * 2008-05-07 2012-10-16 Praxair Technology, Inc. Method and apparatus for separating air
US20130086940A1 (en) * 2010-06-18 2013-04-11 L'Air Liquide Societe Anonyme pout l'Etude et l'Exploitation des Procedes Georges Claude Air separation plant and process operating by cryogenic distillation
US9534836B2 (en) * 2010-06-18 2017-01-03 L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude Air separation plant and process operating by cryogenic distillation
EP2686628B1 (fr) * 2011-03-18 2021-01-13 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Appareil et procede de separation d'air par distillation cryogenique
CN106662014B (zh) * 2014-07-08 2018-08-10 八河流资产有限责任公司 用于加热再循环气流的方法及发电的方法和系统
US9850815B2 (en) * 2014-07-08 2017-12-26 8 Rivers Capital, Llc Method and system for power production with improved efficiency
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US10711695B2 (en) 2014-07-08 2020-07-14 8 Rivers Capital, Llc Method and system for power production with improved efficiency
AU2019201409B2 (en) * 2014-07-08 2020-07-16 8 Rivers Capital, Llc Method and system for power production with improved efficiency
US20160010551A1 (en) * 2014-07-08 2016-01-14 8 Rivers Capital, Llc Method and system for power production wtih improved efficiency
KR20210148397A (ko) * 2014-07-08 2021-12-07 8 리버스 캐피탈, 엘엘씨 향상된 효율을 갖는 동력 생산을 위한 방법 및 시스템
US11365679B2 (en) 2014-07-08 2022-06-21 8 Rivers Capital, Llc Method and system for power production with improved efficiency
US10914232B2 (en) 2018-03-02 2021-02-09 8 Rivers Capital, Llc Systems and methods for power production using a carbon dioxide working fluid
US11560838B2 (en) 2018-03-02 2023-01-24 8 Rivers Capital, Llc Systems and methods for power production using a carbon dioxide working fluid
US11441841B2 (en) * 2018-12-28 2022-09-13 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Heat exchanger assembly and method for assembling same
US20220252345A1 (en) * 2019-04-05 2022-08-11 Linde Gmbh Method for operating a heat exchanger, arrangement with a heat exchanger, and system with a corresponding arrangement
US12044471B2 (en) * 2019-04-05 2024-07-23 Linde Gmbh Method for operating a heat exchanger, arrangement with a heat exchanger, and system with a corresponding arrangement

Also Published As

Publication number Publication date
GB1314347A (en) 1973-04-18
FR2085610B1 (ja) 1975-01-17
NL7103408A (ja) 1971-09-20
FR2085610A1 (ja) 1971-12-24
BE764315A (fr) 1971-08-16
DE2113539A1 (de) 1971-10-07

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