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US3034306A - Separation of air - Google Patents

Separation of air Download PDF

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US3034306A
US3034306A US818336A US81833659A US3034306A US 3034306 A US3034306 A US 3034306A US 818336 A US818336 A US 818336A US 81833659 A US81833659 A US 81833659A US 3034306 A US3034306 A US 3034306A
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sub
fraction
heat exchange
major
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US818336A
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Schuftan Paul Manrice
Smith Kenneth Cecil
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BOC Group Ltd
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British Oxigen Ltd
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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
    • F25J3/04006—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
    • 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
    • F25J3/04242—Cold end purification of the feed 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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

Definitions

  • This invention relates to the low temperature separation of air. More particularly it relates to a low temperature air separation process in which air is compressed, Cooled in a. reversing heat exchange zone by heat exchange with a gaseous nitrogen product fraction and subjected to rectification to produce oxygen and nitrogen fractions.
  • the oxygen fraction is frequently required to be delivered in the gaseous phase under pressure and it has been proposed to pump under pressure a liquid oxygen fraction derived from the rectification step and to vaporize the premurized liquid by heat exchange with incoming air, thus eliminating the necessity for gaseous oxygen compressors.
  • a compressed gaseous oxygen fraction which is dry and not substantially contaminated with carbon dioxide, without the use of gaseous oxygen compressors; to produce a minor part of the oxygen product as liquid, when desired, without reduction in the total oxygen yield; and to produce a gaseous nitrogen fraction, which may be substantially free from oxygen or argon, which is dry and substantially uncontaminated by carbon dioxide.
  • a process for the low temperature separation of air to produce at least the major part of the oxygen product as a compressed gaseous oxygen fraction, and a part of the gaseous nitrogen product as a gaseous nitrogen fraction uncontaminated by water and carbon dioxide comprises the steps of compressing the air to a relatively low prmsure, dividing the compressed air into a major stream and a minor stream, coolingsaid major stream with removal of condensible constituents by heat exchange with a cold gaseous nitrogen fraction of a mass flow greater than that of said major stream in a reversing heat exchange zone, further compressing said minor stream to a substantially higher pressure with removal of condensible impurities therefrom, dividing said compressed minor stream into a first and a second substream, cooling said first sub-stream by heat exchange with a pressurized liquid oxygen fraction with simultaneous vaporization of said liquid oxygen fraction to produce a compressed gaseous oxygen fraction, cooling said second sub-stream by heat exchange with a second cold gaseous nitrogen fraction, withdrawing said second gaseous nitrogen fraction
  • liquid oxygen product While the whole of the liquid oxygen product may be pumped under pressure, a minor part of the product may, if desired, be withdrawn prior to pumping and stored or utilised as liquid. It will be appreciated that when such minor part is retained as liquid, some adjustment of the relative proportions of the various air streams, and/or 'of the pressure to which the minor air stream is compressed will be required, as hereinafter more'particularly described, in order to ensure that the refrigeration re quirements of the separation process are met.
  • a third sub-stream may be withdrawn from the second sub-stream at a point in the latters heat exchange with the gaseous nitrogen fraction such that the third sub-stream is at the appropriate temperature, expanded with the production of external work and thereafter combined with the major stream leaving the reversing heat exchange zone.
  • the gaseous nitrogen fraction used to cool the second sub-stream does not pass through the reversing heat exchange zone and is therefore dry and uncontaminated with carbon dioxide.
  • the rectification step may be arranged to produce both a gaseous nitrogen fraction substantially free from oxygen and argon, and also a relatively impure gaseous nitrogen fraction, the former being used to cool the second sub ream and the latter to cool the major air stream in the reversing heat exchange zone and to volatilize condensible impurities deposited therein.
  • FIGURE 1 illustrates diagrammatically one arrangement of apparatus forpractising the process of this invention.
  • FIGURE 2 illustratesdiagrammatically a modified form of arrangement of apparatus for practicing the process of v the invention.
  • the compressed air is then cooled in a direct cooler 12 by direct contact with cooling Water to approximately the temperature of the cooling water.
  • the air leaving the cooler 12 is divided into a major stream and a minor stream, the relative proportions of the two streams being dependent on the proportion of the oxygen product to be'withdrawn as liquid.
  • the major air stream may comprise'67% by volume of the total air and the minor stream 33% by volume. Where 10% of the total oxygen product is re-.
  • the major stream may difiuoromethane.
  • the major air stream is cooled approximately to its dew point by passage through one of two regenerators 13 of conventional type, the regenerator not in use for cooling air being itself re-cooled by passage therethrough of a cold gaseous nitrogen fraction as hereinafter described.
  • the regenerators 13 are changed over automatically by timing gear after a suitable period, for example 8 minutes.
  • carbon dioxide and water vapour present in the air are deposited on the regenerator packing, from which they are volatilized during the cooling cycle by the returning nitrogen stream. Balancing of the regenerator's is achieved by ensuring that the mass flow ofthe may be 2350 p.s.i.g, and where 10% of the oxygen prod? not is required as liquid, the pressure may be increased to 2925 p.s.i.g.
  • the air is passed through a scrubbing tower in which its carbon dioxide is remove by scrubbing with caustic soda solution.
  • the high pressure minor air stream is then cooled to about 12 C. in a cooler 16 by heatexchange with an exrequired as liquid.
  • the proportion of the minor ternal refrigerant such as, for example, boiling dichloro- 7 Water condensed from the air on cooling is removed in a separator 17.
  • the remainder of the moisture in the minor air stream is then removed by passage through a drier 18 containing a suitable adsorbent such as alumina.
  • drier is provided in duplicate for. alternate use, onedrier being reactivated while the other is in use. 'Again, it will be appreciated that in accordance with conventional practice; an oil filter is inserted before the drier to'remove stream from the drier.
  • the first substream may comprise 80% of the minor air stream and I the second sub-stream only 20%, whilst where 10% of at substantially atmospheric pressure.
  • the air stream forming the third sub-stream may be as low as 4.5%, whilst where 10% of the total oxygen product is required as liquid, the refrigeration requirements are, of course, greater and the third sub-stream may comprise 21% of the minor air stream.
  • the expanded third substream is then combined with the cooled major'air stream leaving the regenerators l3.
  • the remainder of the second sub-stream after withdrawal of the'third sub-stream is further cooled to about l70' C. ina heat exchanger 24 by heat exchange with the cold gaseous nitrogen fraction subsequently passed through the precooler 21.
  • the first sub-stream leaving the exchanger 19 and the remainder of the second sub.- stream leaving the exchanger 24 are then combined and expandedthrough a valve 25, and fed to the lower column 26 of a conventional double column rectification system.
  • the column 26 operates at about 78 p.s.i.g.
  • a small proportion (for example, about 4%) of the combined first and second sub-streams is bled ofi' upstream the valve 25 and, expanded with consequent liquefaction through a valve 27 into the major air stream'leaving the regenerators l3.
  • the major air stream is then fed to an equalizer 28.
  • the equalizer 28 is shown as located apart from the rectification columns, but if desired, it may be located at the bottom of the lower column 26.
  • the equalizer 2-8 'efficient contact between the vapour and the liquid is obtained and residual higher boiling impurities, such as carbon dioxide, are precipitated.
  • Vapour from the equalizer 28 is fed into the lower column 26 at 29, while a small liquid residue containing the precipitated higher boiling impurities is withdrawn from the bottom of the equalizer 28, passed through a filter 30 and expanded through a valve 3 1 into the upper column 32 of the rectification system.
  • This upper column 32 operates A portion of the air fed to the column 26 is withdrawn, liquefied in a condenser 33 by heat exchange with a gaseous nitrogen fractionleaving the rectification system and returned to the column 26.
  • the amount of air so withdrawn and liquefied is adjusted so that the temperature of the gaseous nitrogen fraction leaving the condenser 33 is about 175 .C. a a
  • the air is separated into an oxygenenriched'liquid fraction collecting at the bottom of the column and a liquid nitrogen fraction which is tormedat the top of the column.
  • the oxygen-enriched liquid is withdrawn from the column 2.6 and passed through an adsorber 34 in which hydrocarbon impurities, such as acetylene or traces of oil from the expansion machine 23, are removed by adsorption on a suitable adsorbent such as silica gel. While for simplicity only one adsorber 34 is shown in the drawing, in practice the adsorber is provided in duplicate so that one can be regenerated while the other is on stream.
  • the oxygen-enriched'liquid is'expanded through an expansion
  • the second sub-stream is cooled to about 33 to production ofexternal work;
  • the expansion machine 23 may be a turbine or an expansion engine.
  • the amount ofair bled ed to form the third. sub-stream will again, depend on the proportion of the oxygen product valve 35 into the upper column 32 of the rectification systern.
  • lower column 26 is used as reflux liquid in both columns, a part of the liquid nitrogen being withdrawn, cooled in a heat exchanger 36 against gaseous nitrogen leaving the upper column 32, and expanded through an expansion valve 37 into thetop of theupper column 32.
  • the air is further separated into a liquid oxygen fraction collecting at the bottom of i the upperlcolumn and a gaseous nitrogen fraction withdrawn from thetop of the column.
  • the liquid oxygen product is Withdrawn from thebottom of the upper column and-fed to a pump 38 where it is pumped to a pressure of 400-600 p.s.i.g.
  • the liquid nitrogen fraction formed at the top of the" gen-fraction is then passed to the, heat exchanger 19 I where it is vaporized by heat exchange with high-pressure air as previously described.
  • liquid oxygen fraction may be withdrawn through a valve-controlled outlet 39 upstream the pump 38 and stored or used as liquid.
  • stored liquid may, for example, be used to produce compressed gaseous oxygen during periods when the separa tion plant is shut down.
  • the gaseous nitrogen fraction is withdrawn from the top of the upper column and passed successively through the exchanger 36 and the condenser 33 as hereinbefore described. After leaving the condenser, the gaseous nitrogen fraction is divided into two streams, one stream passing through the regenerators 13 and being withdrawn at 40 as waste nitrogen contaminated with water vapour and carbon dioxide. The other stream passes successively through the exchanger 24 and the precooler 21 and is withdrawn at 22 as a dry gaseous nitrogen product uncontaminated with carbon dioxide as previously described.
  • FIGURE 2 The alternative arrangement shown in FIGURE 2 is substantially identical in operation with the exception that two gaseous nitrogen fractions are withdrawn from the upper column 32.
  • One fraction consisting of nitrogen substantially free from oxygen and argon is withdrawn from the top of the upper column 32, passed through the heat exchanger 36 and condenser 33 and thence passed directly to the exchanger 24.
  • a substantially pure, dry nitrogen fraction is withdrawn at 22.
  • a second relatively impure nitrogen fraction is withdrawn from the upper column 32 at a point a few plates below the top, passed through separate paths in the exchanger 36 and condenser 33 and thence passed directly to the regenerators 13.
  • a process for the low temperature separation of air to produce at least the major part of the oxygen product as a compressed gaseous oxygen fraction and a part of the nitrogen product as a dry gaseous nitrogen fraction uncontaminated by carbon dioxide com-prising the steps of compressing the air to a relatively low pressure, dividing the compressed air into two streams, namely a major stream and a minor stream, cooling said major stream with removal of condens-ible impurities by heat exchange with a first cold gaseous nitrogen fraction of a mass flow greater than that of said major stream in a reversing heat exchange zone, further compressing said minor stream to a substantially higher pressure with removal of con densible impurities therefrom, dividing said further compressed minor stream into a first and a second sub-stream, both at said substantially higher pressure, cooling said first sub-stream by heat exchange with a pressurized liquid oxygen fraction with simultaneous vaporisation of said liquid oxygen fraction to produce a compressed gaseous oxygen fraction, cooling said second sub-stream by heat exchange with a second cold gaseous nitrogen fraction,
  • Process according to claiml including the steps of scrubbing said combined major air stream and third substream, prior to rectification with a liquid derived from said minor air stream, whereby residual higher boiling impurities in said combined major air stream and third substream are precipitated, and removing said impurities by filtration of said liquid.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
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Description

May 15, 1962 SCHUFTAN ETAL 3,034,306
SEPARATION OF AIR Filed June 5, 1959 2 Sheets-Sheet 1 Air Inventor PAUL MAURlCE S'GHUFT'AN KENNETH CECH. SMITH y M Attorney y 1962 P. M. SCHUFTAN ETAL 3,034,306
SEPARATION OF AIR Filed June 5, 1959 2 sheets-sheet 2 Air 7 Wqste Nltmgen Inventor. PAul. MAURICE scuuFrAM KENNETH czcu. H
By I 0m x WNW Unite Stts This invention relates to the low temperature separation of air. More particularly it relates to a low temperature air separation process in which air is compressed, Cooled in a. reversing heat exchange zone by heat exchange with a gaseous nitrogen product fraction and subjected to rectification to produce oxygen and nitrogen fractions.
The oxygen fraction is frequently required to be delivered in the gaseous phase under pressure and it has been proposed to pump under pressure a liquid oxygen fraction derived from the rectification step and to vaporize the premurized liquid by heat exchange with incoming air, thus eliminating the necessity for gaseous oxygen compressors.
Among the objects of the instant invention are to pro duce a compressed gaseous oxygen fraction which is dry and not substantially contaminated with carbon dioxide, without the use of gaseous oxygen compressors; to produce a minor part of the oxygen product as liquid, when desired, without reduction in the total oxygen yield; and to produce a gaseous nitrogen fraction, which may be substantially free from oxygen or argon, which is dry and substantially uncontaminated by carbon dioxide.
According to the invention, a process for the low temperature separation of air to produce at least the major part of the oxygen product as a compressed gaseous oxygen fraction, and a part of the gaseous nitrogen product as a gaseous nitrogen fraction uncontaminated by water and carbon dioxide, comprises the steps of compressing the air to a relatively low prmsure, dividing the compressed air into a major stream and a minor stream, coolingsaid major stream with removal of condensible constituents by heat exchange with a cold gaseous nitrogen fraction of a mass flow greater than that of said major stream in a reversing heat exchange zone, further compressing said minor stream to a substantially higher pressure with removal of condensible impurities therefrom, dividing said compressed minor stream into a first and a second substream, cooling said first sub-stream by heat exchange with a pressurized liquid oxygen fraction with simultaneous vaporization of said liquid oxygen fraction to produce a compressed gaseous oxygen fraction, cooling said second sub-stream by heat exchange with a second cold gaseous nitrogen fraction, withdrawing said second gaseous nitrogen fraction after such heat exchange as a gaseous nitrogen product uncontaminated by water and carbon dioxide, expanding said first and second substreams, subjecting said major stream leaving said reversing heat exchange zone and said expanded first and second sub-streams to rectification in a rectification zone, withdrawing a liquid oxygen fraction from said rectification zoneand pumping at least a major part of liquid oxygen fraction to provide said pressurized liquid oxygen fraction vaporized to produce said compressed gaseous oxygen fraction.
While the whole of the liquid oxygen product may be pumped under pressure, a minor part of the product may, if desired, be withdrawn prior to pumping and stored or utilised as liquid. It will be appreciated that when such minor part is retained as liquid, some adjustment of the relative proportions of the various air streams, and/or 'of the pressure to which the minor air stream is compressed will be required, as hereinafter more'particularly described, in order to ensure that the refrigeration re quirements of the separation process are met.
ice
In order to increase cold production to meet the demand for liquid oxygen, a third sub-stream may be withdrawn from the second sub-stream at a point in the latters heat exchange with the gaseous nitrogen fraction such that the third sub-stream is at the appropriate temperature, expanded with the production of external work and thereafter combined with the major stream leaving the reversing heat exchange zone.
It Will be appreciated that the gaseous nitrogen fraction used to cool the second sub-stream does not pass through the reversing heat exchange zone and is therefore dry and uncontaminated with carbon dioxide. If desired, the rectification step may be arranged to produce both a gaseous nitrogen fraction substantially free from oxygen and argon, and also a relatively impure gaseous nitrogen fraction, the former being used to cool the second sub ream and the latter to cool the major air stream in the reversing heat exchange zone and to volatilize condensible impurities deposited therein.
It is well known that for the eflicient operation of a reversing heat exchange zone, for example provided by regenerators or reversing heat exchangers it is necessary to ensure that all the condensible impurities deposited from the air during its' passage through the zone are completely volatilized by the gaseous nitrogen passing through the zone after reversal. Such complete volatilizetion may be efiected by ensuring that the mass flow of gaseous nitrogen through the zone is greater than that of the major air stream passing through the zone, while the minor air stream is in heat exchange with a smaller mass of separation products.
The invention will now be more particularly described with reference to theaccompanying drawings in which:
FIGURE 1 illustrates diagrammatically one arrangement of apparatus forpractising the process of this invention; and
FIGURE 2 ilustratesdiagrammatically a modified form of arrangement of apparatus for practicing the process of v the invention.
In the two figures, like parts are indicated by the same reference numeral.
It will be understood that the drawings illustrate diagrammatically preferred apparatus for practicing this inexchangers.
For the sake of clarity and to avoidundue elaboration of the description, the change-over valve system associated with the regencrators has not been shown in the drawings, but it will be appreciated that such a system must be provided.
The drawings will be described with reference to the production of oxygen, by way of example, but it Will be appreciated that the apparatus maybe used for the production of higher or lower oxygen purities.
Referring to FIGURE 1, air enters the separation systern through a filter 10 and passes into an electrically driven-multistage turbo-compressor 11 which delivers the air at a pressure of 67 p.s.i.g. The compressed air is then cooled in a direct cooler 12 by direct contact with cooling Water to approximately the temperature of the cooling water. The air leaving the cooler 12 is divided into a major stream and a minor stream, the relative proportions of the two streams being dependent on the proportion of the oxygen product to be'withdrawn as liquid. Where,
for example, all the oxygen product is required as compressed gas, the major air stream may comprise'67% by volume of the total air and the minor stream 33% by volume. Where 10% of the total oxygen product is re-.
quired to be withdrawn as liquid, the major stream may difiuoromethane.
comprise 62% of the total air and the minor stream 38% The major air stream is cooled approximately to its dew point by passage through one of two regenerators 13 of conventional type, the regenerator not in use for cooling air being itself re-cooled by passage therethrough of a cold gaseous nitrogen fraction as hereinafter described. The regenerators 13 are changed over automatically by timing gear after a suitable period, for example 8 minutes. During the passage of the major air stream through the regenerator, carbon dioxide and water vapour present in the air are deposited on the regenerator packing, from which they are volatilized during the cooling cycle by the returning nitrogen stream. Balancing of the regenerator's is achieved by ensuring that the mass flow ofthe may be 2350 p.s.i.g, and where 10% of the oxygen prod? not is required as liquid, the pressure may be increased to 2925 p.s.i.g.
'At a convenient point in the compression of the minor air stream, for example, as in the drawing between the first and second stages, the air is passed through a scrubbing tower in which its carbon dioxide is remove by scrubbing with caustic soda solution.
The high pressure minor air stream is then cooled to about 12 C. in a cooler 16 by heatexchange with an exrequired as liquid. Thus, where all the oxygen product is required as compressed gas, the proportion of the minor ternal refrigerant, such as, for example, boiling dichloro- 7 Water condensed from the air on cooling is removed in a separator 17. The remainder of the moisture in the minor air stream is then removed by passage through a drier 18 containing a suitable adsorbent such as alumina.
drier is provided in duplicate for. alternate use, onedrier being reactivated while the other is in use. 'Again, it will be appreciated that in accordance with conventional practice; an oil filter is inserted before the drier to'remove stream from the drier.
. While for the sake of simplicity, only 1 one such drier is shown in the drawing, in practice the The minor air streamis then divided into a first and a second sub-stream, the relative proportions of the substre'ams again depending on the proportion of the total oxygen product required .as liquid. 'Ihus, when all the,
oxygen is required as compressed gas, the first substream may comprise 80% of the minor air stream and I the second sub-stream only 20%, whilst where 10% of at substantially atmospheric pressure.
air stream forming the third sub-stream may be as low as 4.5%, whilst where 10% of the total oxygen product is required as liquid, the refrigeration requirements are, of course, greater and the third sub-stream may comprise 21% of the minor air stream. The expanded third substream is then combined with the cooled major'air stream leaving the regenerators l3.
The remainder of the second sub-stream after withdrawal of the'third sub-stream is further cooled to about l70' C. ina heat exchanger 24 by heat exchange with the cold gaseous nitrogen fraction subsequently passed through the precooler 21. 'The first sub-stream leaving the exchanger 19 and the remainder of the second sub.- stream leaving the exchanger 24 are then combined and expandedthrough a valve 25, and fed to the lower column 26 of a conventional double column rectification system. The column 26 operates at about 78 p.s.i.g. A small proportion (for example, about 4%) of the combined first and second sub-streams is bled ofi' upstream the valve 25 and, expanded with consequent liquefaction through a valve 27 into the major air stream'leaving the regenerators l3. i
The major air stream is then fed to an equalizer 28. In the drawings, the equalizer 28 is shown as located apart from the rectification columns, but if desired, it may be located at the bottom of the lower column 26. In the equalizer 2-8, 'efficient contact between the vapour and the liquid is obtained and residual higher boiling impurities, such as carbon dioxide, are precipitated. Vapour from the equalizer 28 is fed into the lower column 26 at 29, while a small liquid residue containing the precipitated higher boiling impurities is withdrawn from the bottom of the equalizer 28, passed through a filter 30 and expanded through a valve 3 1 into the upper column 32 of the rectification system. This upper column 32 operates A portion of the air fed to the column 26 is withdrawn, liquefied in a condenser 33 by heat exchange with a gaseous nitrogen fractionleaving the rectification system and returned to the column 26. The amount of air so withdrawn and liquefied is adjusted so that the temperature of the gaseous nitrogen fraction leaving the condenser 33 is about 175 .C. a a
In the column 26, the air is separated into an oxygenenriched'liquid fraction collecting at the bottom of the column and a liquid nitrogen fraction which is tormedat the top of the column. The oxygen-enriched liquid is withdrawn from the column 2.6 and passed through an adsorber 34 in which hydrocarbon impurities, such as acetylene or traces of oil from the expansion machine 23, are removed by adsorption on a suitable adsorbent such as silica gel. While for simplicity only one adsorber 34 is shown in the drawing, in practice the adsorber is provided in duplicate so that one can be regenerated while the other is on stream. From the adsorber 34, the oxygen-enriched'liquid is'expanded through an expansion The second sub-stream is cooled to about 33 to production ofexternal work; The expansion machine 23 'may be a turbine or an expansion engine. The amount ofair bled ed to form the third. sub-stream will again, depend on the proportion of the oxygen product valve 35 into the upper column 32 of the rectification systern.
lower column 26 is used as reflux liquid inboth columns, a part of the liquid nitrogen being withdrawn, cooled in a heat exchanger 36 against gaseous nitrogen leaving the upper column 32, and expanded through an expansion valve 37 into thetop of theupper column 32. V
'In theupper column 32, the air is further separated into a liquid oxygen fraction collecting at the bottom of i the upperlcolumn and a gaseous nitrogen fraction withdrawn from thetop of the column. The liquid oxygen product is Withdrawn from thebottom of the upper column and-fed to a pump 38 where it is pumped to a pressure of 400-600 p.s.i.g. The pressurized liquid oxy- The liquid nitrogen fraction formed at the top of the" gen-fraction is then passed to the, heat exchanger 19 I where it is vaporized by heat exchange with high-pressure air as previously described.
If required, a part of the liquid oxygen fraction may be withdrawn through a valve-controlled outlet 39 upstream the pump 38 and stored or used as liquid. Such stored liquid may, for example, be used to produce compressed gaseous oxygen during periods when the separa tion plant is shut down.
The gaseous nitrogen fraction is withdrawn from the top of the upper column and passed successively through the exchanger 36 and the condenser 33 as hereinbefore described. After leaving the condenser, the gaseous nitrogen fraction is divided into two streams, one stream passing through the regenerators 13 and being withdrawn at 40 as waste nitrogen contaminated with water vapour and carbon dioxide. The other stream passes successively through the exchanger 24 and the precooler 21 and is withdrawn at 22 as a dry gaseous nitrogen product uncontaminated with carbon dioxide as previously described.
Substantially complete volatilization of condensed deposits in the regenerator 13 through which the nitrogen stream is passing is ensured by arranging that the mass flow of this stream is greater than that of the major air stream passing through the regenerators.
The alternative arrangement shown in FIGURE 2 is substantially identical in operation with the exception that two gaseous nitrogen fractions are withdrawn from the upper column 32. One fraction consisting of nitrogen substantially free from oxygen and argon is withdrawn from the top of the upper column 32, passed through the heat exchanger 36 and condenser 33 and thence passed directly to the exchanger 24. In this way a substantially pure, dry nitrogen fraction is withdrawn at 22. A second relatively impure nitrogen fraction is withdrawn from the upper column 32 at a point a few plates below the top, passed through separate paths in the exchanger 36 and condenser 33 and thence passed directly to the regenerators 13.
It will be appreciated that the figures given in the above description for the proportions of the total air forming the various air streams and sub-streams and for the pressure to which the minor air stream is compressed are only exemplary and may be varied if required, provided that sufiicient refrigeration is produced to provide for the cold requirements of the process. Thus, by raising the pressure to which the minor air stream is compressed above the values suggested in the description, it is possible to reduce the amount of air passing through the expansion machine 23, or even to eliminate this machine completely, without substantially reducing the total refrigeration produced.
When the process of the instant invention is used for the production of oxygen of high purity, it may be desirable to withdraw an argon-containing fraction from the upper column (as indicated in the drawings at 41) and to recover the argon therefrom by conventional means.
We claim:
1. A process for the low temperature separation of air to produce at least the major part of the oxygen product as a compressed gaseous oxygen fraction and a part of the nitrogen product as a dry gaseous nitrogen fraction uncontaminated by carbon dioxide, com-prising the steps of compressing the air to a relatively low pressure, dividing the compressed air into two streams, namely a major stream and a minor stream, cooling said major stream with removal of condens-ible impurities by heat exchange with a first cold gaseous nitrogen fraction of a mass flow greater than that of said major stream in a reversing heat exchange zone, further compressing said minor stream to a substantially higher pressure with removal of con densible impurities therefrom, dividing said further compressed minor stream into a first and a second sub-stream, both at said substantially higher pressure, cooling said first sub-stream by heat exchange with a pressurized liquid oxygen fraction with simultaneous vaporisation of said liquid oxygen fraction to produce a compressed gaseous oxygen fraction, cooling said second sub-stream by heat exchange with a second cold gaseous nitrogen fraction, withdrawing said second gaseous nitrogen fraction after such heat exchange as a dry gaseous nitrogen product uncontaminated by carbon dioxide, dividing from said cooled second sub-stream a third sub-stream, expanding said third sub-stream with the performance of external work, and combining said expanded third sub-stream with the the major stream leaving said reversing heat exchange zone, further cooling the remainder of said second substream by heat exchange with said second gaseous nitrogen fraction, expanding said first sub-stream and the remainder of said second sub-stream, subjecting said combined major stream and third sub-stream and said expanded first and second sub-streams to rectification in a rectification zone, withdrawing a liquid oxygen fraction from said rectification zone and pumping at least a major part of said liquid oxygen fraction under pressure to provide said pressurized oxygen liquid oxygen fraction vaporized by heat exchange with said first sub-stream.
2. Process according to claim 1 wherein a part of said liquid oxygen fraction is withdrawn as liquid prior to pumping. I
3. Process according to claim 1 wherein said second gaseous nitrogen fraction passed in heat exchange with said second sub-stream is a relatively pure gaseous nitrogen fraction withdrawn from said rectification zone and said first gaseous nitrogen fraction passed in heat exchange with said major air stream in said reversing heat exchange zone is a relatively impure gaseous nitrogen fraction withdrawn from said rectification zone.
4. Process according to claiml, including the steps of scrubbing said combined major air stream and third substream, prior to rectification with a liquid derived from said minor air stream, whereby residual higher boiling impurities in said combined major air stream and third substream are precipitated, and removing said impurities by filtration of said liquid.
5. Process according to claim 1 wherein an argon-containing fraction is withdrawn from said rectification zone.
References Cited in the file of this patent UNITED STATES PATENTS 2,712,738 Wucherer et a1. July 12, 1955 2,822,675 Grenier Feb. 11, 1958 2,873,583 Potts et a1 Feb. 17, 1959

Claims (1)

1. A PROCESS FOR THE LOW TEMPERATURE SEPARATION OF AIR TO PRODUCE AT LEAST THE MAJOR PART OF THE OXYGEN PRODUCT AS A COMPRESSED GASEOUS OXYGEN FRACTION AND A PART OF THE NITROGEN PRODUCT AS A DRY GASEOUS NITROGEN FRACTION UNCONTAMINATED BY CARBON DIOXIDE, COMPRISING THE STEPS OF COMPRESSING THE AIR TO A RELATIVELY LOW PRESSURE, DIVIDING THE COMPRESSED AIR INTO TWO STREAMS, NAMELY A MAJOR STREAM AND A MINOR STREAM, COOLING SAID MAJOR STREAM WITH REMOVAL OF CONDENSIBLE IMPURITIES BY HEAT EXCHANGE WITH A FIRST COLD GASEOUS NITROGEN FRACTION OF A MASS FLOW GREATER THAN THAT OF SAID MAJOR STREAM IN A REVERSING HEAT EXCHANNGE ZONE, FURTHER COMPRISING SAID MINOR STREAM TO A SUBSTANTIALLY HIGHER PRESSURE WITH REMOVAL OF CONDENSIBLE IMPURITIES THEREFROM, DIVIDING SAID FURTHER COMPRESSED MINOR STREAM INTO A FIRST AND A SECOND SUB-STREAM, BOTH AT SAID SUBSTANTIALLY HIGHER PRESSURE, COOLING SAID FIRST SUB-STREAM BY HEAT EXCHANGE WITH A PRESSURIZED LIQUID OXYGEN FRACTION WITH STIMULATEOUS VAPORISATION OF SAID LIQUID OXYGEN FRACTION TO PRODUCE A COMPRESSED GASEOUS OXYGEN FRACTION, COOLING SAID SECOND SUB-STREAM BY HEAT EXCHANGE WITH A SECOND COLD GASEOUS NITROGEN FRACTION, WITHDRAWING SAID SECOND GASEOUS NITROGEN FRACTION AFTER SUCH HEAT EXCHANGE AS A DRY GASEOUS NITROGEN PRODUCT UNCONTAMINATED BY CARBON DIOXIDE, DIVIDING FROM SAID COOLED SECOND SUB-STREAM A THIRD SUB-STREAM EXPANDING SAID THIRD SUB-STREAM WITH THE PERFORMANCE OF EXTERNAL WORK, AND COMBINING SAID EXPANDED THIRD SUB-STREAM WITH THE MAJOR STREAM LEAVING SAID REVERSING HEAT EXCHANGE ZONE, FURTHER COOLING THE REMAINDER OF SAID SECOND SUBSTREAM BY HEAT EXCHANGE WITH SAID SECOND GASEOUS NITROGEN FRACTION, EXPANDING SAID FIRST SUB-STREAM AND THE REMAINDER OF SAID SECOND SUB-STREAM AND SAID COMBINED MAJOR STREAM AND THIRD SUB-STREAM AND SAID EXPANDED FIRST AND SECOND SUB-STREAMS TO RECTIFICATION IN A RECTIFICATION ZONE, WITHDRAWING A LIQUID OXYGEN FRACTION FROM SAID RECTIFICATION ZONE AND PUMPING AT LEAST A MAJOR PART OF SAID LIQUID OXYGEN FRACTION UNDER PRESSURE TO PROVIDE SAID PRESSURIZED OXYGEN LIQUID OXYGEN FRACTION VAPORIZED BY HEAT EXCHANGE WITH SAID FIRST SUB-STREAM.
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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3216206A (en) * 1961-11-29 1965-11-09 Linde Eismasch Ag Low temperature distillation of normally gaseous substances
US3500651A (en) * 1966-01-13 1970-03-17 Linde Ag Production of high pressure gaseous oxygen by low temperature rectification of air
US3754406A (en) * 1970-03-16 1973-08-28 Air Prod & Chem The production of oxygen
US3909409A (en) * 1974-06-12 1975-09-30 Chicago Bridge & Iron Co Recovery system for oxygen from waste water oxygenation
JPS5289565A (en) * 1975-12-19 1977-07-27 Linde Ag Air constituent separation method
US4202678A (en) * 1975-08-25 1980-05-13 Air Products & Chemicals, Inc. Air separation liquefaction process
JPS5741565A (en) * 1980-07-22 1982-03-08 Air Prod & Chem Production of gaseous oxygen and low temperature plant used therefor
US5410885A (en) * 1993-08-09 1995-05-02 Smolarek; James Cryogenic rectification system for lower pressure operation

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2712738A (en) * 1952-01-10 1955-07-12 Linde S Eismaschinen Ag Method for fractionating air by liquefaction and rectification
US2822675A (en) * 1954-04-23 1958-02-11 Air Liquide Production of gaseous oxygen under pressure
US2873583A (en) * 1954-05-04 1959-02-17 Union Carbide Corp Dual pressure cycle for air separation

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2712738A (en) * 1952-01-10 1955-07-12 Linde S Eismaschinen Ag Method for fractionating air by liquefaction and rectification
US2822675A (en) * 1954-04-23 1958-02-11 Air Liquide Production of gaseous oxygen under pressure
US2873583A (en) * 1954-05-04 1959-02-17 Union Carbide Corp Dual pressure cycle for air separation

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3216206A (en) * 1961-11-29 1965-11-09 Linde Eismasch Ag Low temperature distillation of normally gaseous substances
US3500651A (en) * 1966-01-13 1970-03-17 Linde Ag Production of high pressure gaseous oxygen by low temperature rectification of air
US3754406A (en) * 1970-03-16 1973-08-28 Air Prod & Chem The production of oxygen
US3909409A (en) * 1974-06-12 1975-09-30 Chicago Bridge & Iron Co Recovery system for oxygen from waste water oxygenation
US4202678A (en) * 1975-08-25 1980-05-13 Air Products & Chemicals, Inc. Air separation liquefaction process
JPS5289565A (en) * 1975-12-19 1977-07-27 Linde Ag Air constituent separation method
JPS5741565A (en) * 1980-07-22 1982-03-08 Air Prod & Chem Production of gaseous oxygen and low temperature plant used therefor
US5410885A (en) * 1993-08-09 1995-05-02 Smolarek; James Cryogenic rectification system for lower pressure operation

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