EP1202013B3 - Vorrichtung und Verfahren zur Herstellung von gasförmigem Sauerstoff unter niedrigem Druck - Google Patents

Vorrichtung und Verfahren zur Herstellung von gasförmigem Sauerstoff unter niedrigem Druck Download PDF

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Publication number
EP1202013B3
EP1202013B3 EP20010308922 EP01308922A EP1202013B3 EP 1202013 B3 EP1202013 B3 EP 1202013B3 EP 20010308922 EP20010308922 EP 20010308922 EP 01308922 A EP01308922 A EP 01308922A EP 1202013 B3 EP1202013 B3 EP 1202013B3
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Prior art keywords
lox
heat exchange
exchange means
refrigerant
product
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EP20010308922
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English (en)
French (fr)
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EP1202013B1 (de
EP1202013A1 (de
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Rodney J. Allam
Alan Lindsay Prentice
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Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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Priority claimed from EP00309320A external-priority patent/EP1207362A1/de
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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
    • F25J3/04151—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
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • 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
    • F25J3/04006—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
    • F25J3/04103—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 using solely hydrostatic liquid head
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
    • 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
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—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
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen

Definitions

  • the present invention relates generally to the production of oxygen gas ("GOX”) and, in particular, to the production of low pressure GOX by the cryogenic distillation of air.
  • GOX oxygen gas
  • VSA vacuum swing absorption
  • LOX liquid oxygen
  • the column system in US-A-5408831 is back-pressurised.
  • the air pressure is necessarily higher, at a pressure from 8 to 16 bar absolute (0.8 to 1.6 MPa), than that in processes without column back-pressurisation giving a significant power penalty of about 12% for a given air flow.
  • Such a penalty represents an undesirable increase in operating cost especially when it is considered that power is the main operating cost of an air separation plant.
  • US-A-5505052 discloses a process for the cryogenic distillation of air using a double column system having a high pressure ("HP") column and a LP column to produce GOX at a pressure of about 25 bar (2.5 MPa) for use in installations comprising, for example, electric arc furnaces adapted to produce stainless steel.
  • Oxygen is withdrawn in liquid form from the base of the LP column, brought to the utilisation pressure by a pump and vaporised and reheated to about ambient temperature in the heat exchange line against the feed air. The gaseous oxygen is then fed to the installation.
  • a portion of the LOX withdrawn from the base of the column may be sent to storage, for example, during periods of low demand for GOX in the installation where it is kept until such time as the demand for GOX at the installation becomes high whereupon it is pumped to the utilisation pressure and vaporised and reheated to about ambient temperature in the heat exchange line against the feed air.
  • the LOX from storage may travel through the same vaporisation passages through the heat exchange line as the LOX from the column system or it may travel through separate vaporisation passages. The gaseous oxygen is then fed to the installation.
  • LOX may be added to the LOX in storage from tank trucks, for example, during prolonged periods of high demand for GOX.
  • the storage facility may not be connected to the double column system and may be supplied only by tank trucks.
  • LOX whether from the double column system or from storage, enters the heat exchange line at the cold end, i.e. the end at which cooled feed air exits the line.
  • both the LOX product from the distillation column and the additional LOX from storage are pumped to a pressure (about 25 bar (2.5 MPa)) that is substantially higher that the pressure (about 5 to 6 bar (0.5 to 0.6 MPa)) of the LP column.
  • a portion of the total refrigeration duty requirement of the process is provided by an expander and a further portion is provided by the warming and evaporation of a stream of liquid argon.
  • a process for the production of GOX comprising:
  • the heat exchange means comprises a "warm end” (or “hot end”) and a “cold end".
  • the warm end (or hot end) is the end at which the feed air enters the heat exchange means and the cold end is the end at which the cooled and at least partially condensed feed air leaves the heat exchange means.
  • the terms “warm end” (or “hot end”) and “cold end” are commonly used in the art to distinguish the two ends of heat exchange means by their relative temperatures.
  • GOX may be produced at a slightly elevated pressure by a known technique in which LOX product is withdrawn from the LP column of a double column system.
  • LOX is withdrawn from the distillation column system and is vaporised and warmed by heat exchange against the feed air.
  • a fraction of the feed air is condensed by heat exchange against the withdrawn LOX and, thus, there is less air vapour entering the distillation column system than there would otherwise be if the feed air were to be subjected to indirect heat exchange with GOX withdrawn from the column system.
  • This has the effect of reducing the efficiency of the distillation when compared to a process in which GOX is withdrawn from the distillation column system.
  • there is no performance penalty as about 99.7 % of the O 2 becomes product. Therefore, the process is surprisingly efficient.
  • LOX LOX refrigerant
  • the vaporised LOX refrigerant may be combined with the GOX produced by the vaporisation of the LOX product to produce GOX product. In this way, there is no wastage of vaporised refrigerant.
  • the distillation column system comprises a multiple column system having a higher pressure (“HP") column and a lower pressure (“LP”) column thermally integrated by the condensation of nitrogen overhead from the HP column against liquid bottoms in the LP column.
  • HP higher pressure
  • LP lower pressure
  • a portion of the condensed HP column nitrogen overhead may be subcooled by heat exchange to produce a subcooled nitrogen stream which can be fed to the LP column.
  • substantially all of the refrigeration duty required to keep the plant in energy balance is provided by the LOX refrigerant.
  • no refrigeration duty is provided by expansion of a process stream. Any heat leak into the process via the insulation and the fact that the product streams leave the heat exchanger at a temperature that is slightly lower then the entry temperature of the feed air is taken into account in calculating the amount of LOX refrigerant required.
  • vaporising and warming LOX refrigerant separately from the product LOX has little effect on the temperature profiles of the main heat exchanger and causes only a very small increase in the amount of the refrigerant.
  • the LOX refrigerant is vaporised separately from the LOX product to reduce the risk of any problems resulting from the build up of hydrocarbon impurities such as ethylene due to deposition of CO 2 and N 2 O on the interior wall surfaces of the boiling passages through the heat exchanger.
  • LOX refrigerant e.g. produced by an air separation plant
  • hydrocarbons CO 2 and N 2 O impurities.
  • concentration of these impurities in the LOX refrigerant will vary depending on the plant producing it, the mode of operation of the plant and the ratio of LOX produced to feed air entering the plant. Concentrations of about 1500 ppb (vol.) CO 2 and about 3000 ppb (vol.) N 2 O are typical.
  • the vapour phase solubility of CO 2 and N 2 O impurities is about 50 ppb (vol.) and about 500 ppb (vol.) respectively. If the LOX refrigerant were to be introduced directly into the LOX product stream, the impurity concentration of the combined LOX stream would be sufficiently increased to warrant concern about the unwanted and dangerous build up of impurity deposits in the heat exchanger. Even a very small amount of "slippage" of CO 2 and N 2 O from the air purification will cause the concentration of CO 2 and/or N 2 O to exceed the vapour phase solubility limit and result in at least partial blockage of the heat exchanger by deposited CO 2 and N 2 O.
  • vaporising LOX refrigerant without causing blockage of the heat exchanger by CO 2 and N 2 O deposits is achieved by vaporising the refrigerant at a greater pressure than the LOX product such that, at the boiling temperature of the LOX refrigerant, the CO 2 and N 2 O impurity concentrations are below the vapour phase solubility limits.
  • blockage of the heat exchanger by unwanted impurity deposits is avoided by injecting the LOX refrigerant into the heat exchange means at a pressure that is substantially equal to the pressure of the LOX product as it enters the heat exchange means, provided that the point of injection is between the warm and cold ends of the heat exchange means.
  • the temperature of the heat exchange means at the intermediate point of injection is from -165°C to -80°C, i.e. substantially above the O 2 boiling temperature.
  • the pressure of the LOX product leaving the distillation column system is usually about 1.4 bar absolute (0.14 MPa).
  • the pressure of the LOX refrigerant is preferably from 4 bar absolute (0.4 MPa) to 10 bar absolute (1.0 MPa).
  • the pressure of the GOX product is from 1.5 bar absolute (0.15 MPa) to 3.0 bar absolute (0.3 MPa), preferably from 1.8 bar absolute (0.18 MPa) to 2.5 bar absolute (0.25 MPa).
  • the process may further comprise combining LOX refrigerant with the cooled and at least partially condensed feed air to further cool the feed air, preferably during plant cooldown.
  • the process may also comprise introducing LOX refrigerant to the distillation column system under level control.
  • the LOX refrigerant is provided by an air separation plant.
  • the process may further comprise withdrawing at least one nitrogen gas product stream from the distillation column system.
  • the feed air is preferably purified before heat exchange to reduce the CO 2 and N 2 O impurity concentrations to a level which ensures that these impurity concentrations in the LOX product are below their vapour phase solubilities at the vaporising pressure and temperature heat exchange conditions.
  • the feed air may be purified using, for example, either a temperature swing absorber system using alumina and CaX or a pressure swing adsorber system using alumina and 13X.
  • apparatus for carrying out the process of the first aspect of the present invention for producing gaseous oxygen comprising:
  • the apparatus is preferably adapted or constructed to carry out any combination of the preferred features of the process discussed above.
  • NTU transfer units
  • the heat exchange means of the apparatus may have at least 55 NTU, preferably from 70 to 90 NTU and more preferably about 80 NTU.
  • the amount of LOX refrigerant consumed in the process is also very dependent on the heat gain through the insulation.
  • the cryogenic portion of the apparatus i.e. the distillation column system and the heat exchange means, is vacuum insulated to reduce heat loss.
  • the LOX refrigerant passes through the heat exchange means via a separate circuit to the LOX product.
  • the LOX refrigerant preferably passes through the heat exchange means via a single passage.
  • the LOX refrigerant is preferably introduced into the heat exchange means at an intermediate point between the cold and warm ends of the heat exchange means where the temperature of the metal of the heat exchange means is above the boiling temperature of the refrigerant.
  • An at least partially condensed feed airstream 2 is removed from the main heat exchanger E1 and fed to the high pressurecolumn C1 in an double distillation column system C1, C2 having a reboiler condenser E2.
  • the feed air stream 2 is distilled in the high pressure column C1 and a nitrogen-rich vapour stream 3 is condensed in the condenser E2 to produce a condensed nitrogen-rich stream 13.
  • a portion 5 of the condensed nitrogen-rich stream 13 is returned to the high pressure column C1 as reflux to purify gas rising and the remaining portion 4 is sent to the top of the low pressure column C2 via the main heat exchanger E1 where it is subcooled.
  • An oxygen-rich stream 6 is removed from the high pressure column C1 and fed to the low pressure column C2 at an intermediate location optionally via a heat exchanger to subcool the stream.
  • the two liquid streams 4, 6 entering the low pressure column C2 are distilled due to vapour rising from the reboiler E2.
  • a low pressure waste nitrogen vapour stream 7 is withdrawn from the top of the low pressure column and warmed to ambient temperature in the main heat exchanger E1.
  • a LOX product stream 8 is withdrawn from the bottom of the low pressure column C2 and piped to a lower elevation to gain static pressure before being vaporised and then warmed to ambient temperature in the main heat exchanger E1 to form GOX stream 9.
  • GOX at a pressure typically from 1.8 to 2.5 bar absolute (0.18 to 0.25MPa) may be obtained directly from the plant.
  • a LOX refrigerant stream 10 is introduced to a separate circuit of the main heat exchanger E1 at an intermediate point between the warm and cold ends and at a pressure equal to or higher than that for the LOX product stream 8 in a manner to avoid the deposition of CO 2 and N 2 O.
  • the LOX refrigerant stream 10 is vaporised and warming to ambient temperature to produce a stream 11 of vaporised LOX refrigerant which is combined with the GOX stream 9 to form a GOX product stream 12.
  • an airflow of 10000 Nm 3 / h (167 Nm 3 /s) is compressed to about 6 bar absolute (0.6 MPa), purified,-cooled in the main heat exchanger E1 and fed to the H P column C1 at5.5 bar absolute (0.55 MPa).
  • LOX refrigerant from an external source at a purity of about 99.8 % O 2 is injected into the main heat exchanger E1 at a flow rate of about 50 Nm 3 /h (0.8 Nm 3 / s) where it is vaporised and warmed to ambient temperature.
  • LOX product at about 95 % O 2 purity and at a contained O 2 flow of 2090 Nm 3 /h (35 Nm 3 /s) leaves the low pressure column C2 at about 1.4 bar absolute (0.14 MPa).
  • the pressure of the LOX product stream is increased by about 0.8 bar absolute (0.08 MPa) due to static head and after vaporisation and warming leaves the main heat exchanger at 2.0 bar absolute (0.2 MPa).
  • the two warmed GOX streams are combined giving a contained O 2 flow of 2140 Nm 3 /h (36 Nm 3 /s) of GOX.
  • the economics of the present invention compare favourably with those of O 2 VSA plants at product flows above 870 Nm 3 /h (15 Nm 3 /s).
  • the present invention has the same or lower gas cost without the much higher capital cost or reliability issues of the O 2 VSA plants.
  • the economics of the present invention also compare favourably with those of a cryogenic plant with an expander at a capacity of about 3480 Nm 3 / h (58 Nm 3 /s). Again, the present invention is economic having the same gas cost and lower capital cost.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Claims (20)

  1. Verfahren für die Herstellung von gasförmigem Sauerstoff ("GOX" für "gaseous oxygen") mit:
    Kühlen und wenigstens teilweise Kondensieren von Speiseluft (1) durch Wärmeaustausch unter Verwendung einer Wärmeaustauscheranordnung (E1) mit einem warmen Ende und einem kalten Ende, um gekühlte und wenigstens teilweise kondensierte Speiseluft (2) zu erzeugen;
    Destillieren der gekühlten und wenigstens teilweise kondensierten Speiseluft (2) in einem Destillationssäulensystem (C1, C2), um ein Flüssigsauerstoff- ("LOX" für "liquid oxygen") Produkt zu erzeugen;
    Entnehmen eines Stroms (8) des LOX-Produktes aus dem Destillationssäulensystem (C1, C2), Unterdrucksetzen des Stroms (8) nur durch hydrostatischen Druck und Verdampfen des unter Druck stehenden LOX-Produkt-Stroms (8) durch Wärmeaustausch (E1) gegen die Speiseluft (1), um GOX bei einem Druck von 0,15 MPa (1,5 bar absolut) bis 0,3 MPa (3,0 bar absolut) zu erzeugen; und
    Verdampfen - getrennt von dem LOX-Produkt - von LOX-Kühl- bzw. Kältemittel (10) aus einer externen Quelle durch Wärmeaustausch (E1) gegen die Speiseluft (1), um verdampftes Kühlmittel (11) zu erzeugen, wobei dadurch ein Teil der Kühlleistung zur Verfügung gestellt wird, der zum Kühlen und zum wenigstens teilweise Kondensieren der Speiseluft benötigt wird;
    wobei das Verfahren den Schritt aufweist, dass das LOX-Kühlmittel in die Wärmeaustauscheranordnung (E1) injiziert wird entweder:
    (a) bei einem Druck, der größer als der des LOX-Produktes ist, das in die Wärmeaustauscheranordnung eintritt; oder
    (b) bei einem Druck, der im Wesentlichen gleich dem des LOX-Produktes ist, das in die Wärmeaustauscheranordnung eintritt, und zwar an einem Zwischenpunkt zwischen den warmen und kalten Enden, an dem die Temperatur der Wärmeaustauscheranordnung (E1) sich über der Siedetemperatur des LOX-Kühlmittels befindet.
  2. Verfahren nach Anspruch 1, wobei die Temperatur der Wärmeaustauscheranordnung (E1) an dem Zwischenpunkt, an dem das LOX-Kühlmittel injiziert wird, von -165°C bis -80°C beträgt.
  3. Verfahren nach Anspruch 1 oder Anspruch 2, wobei das verdampfte LOX-Kühlmittel (10) mit dem GOX (9) kombiniert wird, das durch die Verdampfung des LOX-Produktes hergestellt wird, um das GOX-Produkt (12) herzustellen.
  4. Verfahren nach einem der Ansprüche 1 bis 3, wobei das Destillationssäulensystem ein Mehrfachsäulensystem mit einer Säule (C1) mit höherem Druck ("HP" für "higher pressure") und einer Säule (C2) mit niedrigerem Druck ("LP" für "lower pressure") aufweist, die durch die Kondensation des Stickstoff-Kopfproduktes von der HP-Säule gegen das flüssige Bodenprodukt in der LP-Säule thermisch integriert sind.
  5. Verfahren nach einem der Ansprüche 1 bis 4, wobei keine Kühlleistung durch die Expansion eines Verfahrensstroms zur Verfügung gestellt wird.
  6. Verfahren nach einem der Ansprüche 1 bis 5, wobei das LOX-Kühlmittel (10) die gesamte externe Kühlleistung zur Verfügung stellt, die benötigt wird, um das Verfahren im Energie-Gleichgewicht zu halten.
  7. Verfahren nach einem der Ansprüche 1 bis 6, wobei der Druck des LOX-Kühlmittels (10) von 0,4 MPa (4 bar absolut) bis 1,0 MPa (10 bar absolut) beträgt.
  8. Verfahren nach einem der Ansprüche 1 bis 7, wobei der Druck des GOX-Produktes (12) von 0,18 MPa (1,8 bar absolut) bis 0,25 MPa (2,5 bar absolut) beträgt.
  9. Verfahren nach einem der Ansprüche 1 bis 8, weiterhin mit Kombinieren des LOX-Kühlmittels mit der gekühlten und wenigstens teilweise kondensierten Speiseluft, um die Speiseluft weiter zu kühlen.
  10. Verfahren nach einem der Ansprüche 1 bis 9, weiterhin mit Einführen des LOX-Kühlmittels in das Destillationssäulensystem unter Niveau-Steuerung bzw. -Regelung.
  11. Verfahren nach einem der Ansprüche 1 bis 10, wobei das LOX-Kühlmittel durch eine Luftzerlegungsanlage zur Verfügung gestellt wird.
  12. Vorrichtung zur Durchführung des Verfahrens nach Anspruch 1 zur Erzeugung von gasförmigem Sauerstoff, wobei die Vorrichtung umfasst:
    eine Wärmeaustauscheranordnung (E1) zum Kühlen und wenigstens teilweise Kondensieren von Speiseluft (1), um gekühlte und wenigstens teilweise kondensierte Speiseluft (2) zu erzeugen, wobei die Wärmeaustauscheranordnung (E1) ein warmes Ende und ein kaltes Ende hat;
    ein Destillationssäulensystem (C1, C2) zum Destillieren der gekühlten und wenigstens teilweise kondensierten Speiseluft (2), um ein LOX-Produkt (8) zu erzeugen;
    eine Leitungsanordnung zur Führung der gekühlten und wenigstens teilweise kondensierten Speiseluft (2) von der Wärmeaustauscheranordnung (E1) zu dem Destillationssäulensystem (C1, C2); und
    eine Leitungsanordnung zur Führung des LOX-Produktes (8) von dem Destillationssäulensystem (C1, C2) zu der Wärmeaustauscheranordnung (E1);
    wobei die Vorrichtung keine Anordnung zum Pumpen des LOX-Produktstroms hat, wobei dadurch der Strom während des Durchlaufs vom Destillationssäulensystem zur Wärmeaustauscheranordnung (E1) durch hydrostatischen Druck unter Druck gesetzt wird und die Vorrichtung weiterhin aufweist entweder
    (a) eine Leitungsanordnung zur Führung des LOX-Kühlmittels (10) bei einem höheren Druck als der Druck des LOX-Produktes, das in die Wärmeaustauscheranordnung eintritt, von einem externen Vorrat zu der Wärmeaustauscheranordnung (E1), jedoch keinen Expander zum Expandieren eines Prozessstroms aufweist, um Kühlleistung zur Verfügung zu stellen; oder
    (b) eine Leitungsanordnung zur Führung des LOX-Kühlmittels (10) bei einem Druck, der im Wesentlichen gleich dem Druck des LOX-Produktes ist, das in die Wärmeaustauscheranordnung eintritt, von einem externen Vorrat zu einem Zwischenpunkt zwischen dem warmen und dem kalten Ende der Wärmeaustauscheranordnung, wo die Temperatur der Wärmeaustauscheranordnung sich über der Siedetemperatur des LOX-Kühlmittels befindet und die Wärmeaustauscheranordnung getrennte Kreisläufe für das LOX-Kühlmittel und das LOX-Produkt hat.
  13. Vorrichtung nach Anspruch 12, angepasst oder aufgebaut, um das Verfahren von Option (b) nach einem der Ansprüche 2 bis 11 durchzuführen.
  14. Vorrichtung nach Anspruch 12 oder Anspruch 13, wobei der Kryogen- bzw. Tieftemperatur-Teil der Vorrichtung vakuumisoliert ist, um Wärmeverluste zu reduzieren.
  15. Vorrichtung nach einem der Ansprüche 12 bis 14, wobei die Wärmeaustauscheranordnung (E1) wenigstens 55 NTU hat.
  16. Vorrichtung nach einem der Ansprüche 12 bis 15, wobei die Wärmeaustauscheranordnung (E1) von 70 bis 90 NTU hat.
  17. Vorrichtung nach einem der Ansprüche 12 bis 16, wobei die Wärmeaustauscheranordnung (E1) ungefähr 80 NTU hat.
  18. Vorrichtung nach einem der Ansprüche 13 bis 17, wobei bei der Option (a) die Wärmeaustauscheranordnung getrennte Kreisläufe für das LOX-Kühlmittel und das LOX-Produkt hat.
  19. Vorrichtung nach einem der Ansprüche 12 bis 18, wobei bei der Option (b) die Vorrichtung keinen Expander zum Expandieren eines Prozessstroms aufweist, um Kühlleistung zur Verfügung zu stellen.
  20. Vorrichtung nach einem der Ansprüche 12 bis 19, wobei das LOX-Kühlmittel (10) über einen einzigen Durchgang durch die Wärmeaustauscheranordnung (E1) verläuft.
EP20010308922 2000-10-23 2001-10-19 Vorrichtung und Verfahren zur Herstellung von gasförmigem Sauerstoff unter niedrigem Druck Expired - Lifetime EP1202013B3 (de)

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EP20010308922 EP1202013B3 (de) 2000-10-23 2001-10-19 Vorrichtung und Verfahren zur Herstellung von gasförmigem Sauerstoff unter niedrigem Druck

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Application Number Priority Date Filing Date Title
EP00309320 2000-10-23
EP00309320A EP1207362A1 (de) 2000-10-23 2000-10-23 Verfahren und Vorrichtung zur Herstellung von gasförmigem Niederdrucksauerstoff
EP20010308922 EP1202013B3 (de) 2000-10-23 2001-10-19 Vorrichtung und Verfahren zur Herstellung von gasförmigem Sauerstoff unter niedrigem Druck

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Publication number Priority date Publication date Assignee Title
FR2706195B1 (fr) * 1993-06-07 1995-07-28 Air Liquide Procédé et unité de fourniture d'un gaz sous pression à une installation consommatrice d'un constituant de l'air.
FR2757282B1 (fr) * 1996-12-12 2006-06-23 Air Liquide Procede et installation de fourniture d'un debit variable d'un gaz de l'air

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