EP1672301B1 - Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air - Google Patents

Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air Download PDF

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Publication number
EP1672301B1
EP1672301B1 EP05024947.3A EP05024947A EP1672301B1 EP 1672301 B1 EP1672301 B1 EP 1672301B1 EP 05024947 A EP05024947 A EP 05024947A EP 1672301 B1 EP1672301 B1 EP 1672301B1
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EP
European Patent Office
Prior art keywords
heat exchanger
direct contact
line
low
cooler
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EP05024947.3A
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German (de)
English (en)
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EP1672301A1 (fr
Inventor
Andreas Brox
Markus Huppenberger
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Linde GmbH
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Linde GmbH
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Priority to PL05024947T priority patent/PL1672301T3/pl
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Publication of EP1672301B1 publication Critical patent/EP1672301B1/fr
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—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
    • F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
    • 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
    • F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
    • 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
    • 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
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • 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
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F25J2205/32—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as direct contact cooling tower to produce a cooled gas stream, e.g. direct contact after cooler [DCAC]
    • 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
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F25J2205/34—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as evaporative cooling tower to produce chilled water, e.g. evaporative water chiller [EWC]
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/902—Apparatus
    • Y10S62/903—Heat exchange structure

Definitions

  • the invention relates to a device for producing a product by cryogenic separation of a gas mixture, in particular air, with a direct contact cooler for cooling the feed mixture, with a cleaning device for cleaning the cooled feed mixture and with a low temperature part, the main heat exchanger for cooling the purified feed mixture to about dew point and a distillation column for cryogenic decomposition of the feed mixture.
  • cryogenic temperature is meant here basically any temperature which is below the ambient temperature, but preferably a temperature of 200 K or less, most preferably 150 K or less, for example 100 K or less.
  • a direct contact cooler In a "direct contact cooler” the feed mixture is brought into direct heat exchange with a coolant, for example water, and thereby cooled. It is used in particular for removing heat of compression, which has arisen in a feed gas compressor, which is usually connected upstream.
  • a coolant for example water
  • a subsequent "cleaning device” is usually designed as an adsorption device and in particular has at least two switchable container, which are operated cyclically. It serves to separate unwanted components, for example those which can freeze out in the low-temperature part.
  • the feed mixture is first cooled to about dew point temperature and then decomposed in a distillation column system.
  • the low-temperature part thus contains one or more heat exchangers and one or more distillation columns.
  • the product is in Withdrawn gas or liquid form.
  • the cryogenic part is usually thermally insulated by being enclosed by one or more cold boxes.
  • the “main heat exchanger” serves to heat the gaseous product (s) in indirect heat exchange with at least one feed mixture stream.
  • the three mentioned plant components are usually arranged so that the consumption of floor space is as low as possible. This is not satisfactory in all cases.
  • the invention is therefore based on the object to further optimize the arrangement of the components of a cryogenic separation plant in order to achieve a particularly high efficiency of the system.
  • This object is achieved in that the direct contact cooler, the cleaning device and the low-temperature part are arranged in a line.
  • the arrangement “on a line” means that there must be at least one horizontal straight line, which intersects the bases of all three plant components mentioned.
  • “Base area” is understood here as the footprint that is required for the corresponding system components including the directly associated functional units such as, for example, pumps and fittings.
  • the arrangement in a line minimizes in particular the effort in the fluidic connection of the system components with each other.
  • the corresponding pipe lengths and the scope of the associated steel construction devices such as pipe bridges are minimized. For very large plants with a single-gas flow rate of 300,000 Nm, this means 3 / h or more - a noticeable reduction in investment costs.
  • the linear arrangement also has the advantage that the system components are basically accessible from both sides for assembly and maintenance. This reduces the operating and repair costs of the system.
  • the direct contact cooler is preceded by a feed gas compressor for compressing the feed mixture.
  • a feed gas compressor for compressing the feed mixture.
  • This can be arranged in the context of the invention, for example, laterally next to the group of direct contact cooler, cleaning device and low temperature part.
  • it is particularly favorable when the feed gas compressor, the direct contact cooler, the cleaning device and the low-temperature part are arranged in a line. This further enhances the above advantages.
  • connection means may be arranged, for example on the side of the cryogenic part a pipe bridge for discharging the products and / or on the compressor side a gas or steam turbine for driving the feed gas compressor with appropriate accessories, such as an air condenser, steam -, gas and / or cooling water lines for machines or the like. Nevertheless, the various system components remain easily accessible.
  • the drive shaft of the feed gas compressor runs, in this case in particular, preferably substantially perpendicular to the line on which the direct contact cooler, the cleaning device and the low-temperature part are arranged.
  • the feed gas compressor may be arranged laterally next to the other system parts.
  • the drive shaft of the feed gas compressor runs essentially parallel to the line on which the direct contact cooler, the cleaning device and the low-temperature part are arranged.
  • the base of the previously mentioned system components has a relatively elongated shape. More specifically, in this case, the ratio of the dimension of the smallest rectangle including the bases of the direct contact cooler, the purifier, and the cryogenic part and possibly the feed gas compressor in the direction of a straight line connecting direct contact cooler and low temperature part to the extension in the direction perpendicular thereto is larger than 1, in particular greater than 1.5. For example, this ratio is 2.0 or more, especially 3.0 or more.
  • the device for connecting the individual systems with each other (for example, pipe bridge for product lines) is arranged along the narrow sides and can thus be made relatively short and inexpensive.
  • the cryogenic part regularly comprises a heat exchanger box containing at least one main heat exchanger, a rectification box containing at least one distillation column, and an expansion machine located within a turbine box. It is favorable if the turbine box is arranged at a transition section of the low-temperature part, which is located between the heat exchanger box and the rectification box. Alternatively, the turbine box may be connected directly to the heat exchanger box.
  • the claims 7 to 12 contain further advantageous embodiments of the device according to the invention. Their features can be applied in a device for producing a product by cryogenic separation of a gas mixture, in particular air, as a non-inventive embodiment, independently of the features of claims 1 to 6 or according to the invention in combination with these.
  • the feed mixture line for introducing feed mixture into the main heat exchanger and the product line for drawing off the product flow from the main heat exchanger run substantially parallel to a main orientation axis and are arranged on opposite sides of the main heat exchanger.
  • the "main axis of orientation" represents an abstract straight line that runs in a horizontal direction and is not usually materialized by components of the plant or any other physical device.
  • substantially parallel are two directions if they form an angle of less than 20 °, preferably less than 10 °, most preferably less than 5 ° with each other.
  • the arrangement according to claim 7 offers the advantage that the devices for the discharge of the products, for example one or more manifolds, into which the product line (s) open, on one side of the main heat exchanger and the means for pretreatment of the feed mixture on the opposite side of the main heat exchanger can be arranged. This makes very small pipe lengths possible.
  • the arrangement also has the advantage that the system components are basically accessible from both sides for assembly and maintenance. This reduces the operating and repair costs of the system.
  • the device prefferably has a collecting line, into which the product line opens at its end facing away from the main heat exchanger, and when the collecting line runs essentially perpendicular to the main orientation axis.
  • One direction is "substantially perpendicular" to another when the respective straight lines subtend an angle of 70 ° to 110 °, preferably 80 ° to 100 °, most preferably 85 ° to 95 °.
  • One or more manifolds may connect the device and possibly other identical or similar devices (strands) to a multi-line plant, or to a tank farm and / or to an emergency supply device.
  • the manifold (s) can be arranged on a pipe bridge or on the ground. In the latter case, the manifolds are routinely routed to so-called sleepers.
  • manifold (s) are connected to a product line of one or more other cryogenic decomposition devices.
  • manifold (s) may be connected to a storage container for product.
  • the main heat exchanger is embodied exclusively as a recuperative heat exchanger, that is to say as a non-reversible heat exchanger.
  • the claims 13 to 16 contain further advantageous embodiments of the device according to the invention. Their features can be applied in a device for producing a product by cryogenic separation of a gas mixture, in particular air, as a non-inventive embodiment, independently of the features of claims 1 to 12 or according to the invention in combination with these.
  • the ratio of the distance between the evaporative cooler and the direct contact cooler to the distance between the evaporative cooler and the main heat exchanger is at least 0.5, in particular at least 1.0.
  • the evaporative cooler 15 is thus arranged comparatively close to the main heat exchanger. Although this means higher costs for the coolant piping; However, the line for the gas flow from the low-temperature part can be made very short. In the context of the invention has been found that this arrangement leads to a total of comparatively low investment costs costs. In particular, the effort for the pipelines and the associated steel construction costs is reduced. This is partly due to the very high cross section (for example 1 to 2 m) of the gas line to the evaporative cooler.
  • Atmospheric air is sucked in as "feed mixture” via an inlet filter 1 and fed via feed pipes 51, 52, 53, 54 to other plant components.
  • a main air compressor 2 which in the example represents the "feed gas compressor”
  • the compressed air 52 flows into a direct contact cooler 3 where it is cooled in direct heat exchange with cooling water flowing over a cooling water piping 61.
  • the cooled air 53 is further passed into a purifier 4 having a pair of molecular sieve adsorbers 5, 6.
  • the purified air 54 continues to flow to the cryogenic part 7.
  • the low-temperature part can consist of a single cold box, in which all cryogenic apparatus are arranged, in particular the one or more heat exchangers and the distillation column (s), or from a plurality of separate cold boxes.
  • a cylindrical rectification box 9 contains the distillation columns 9a, here a double column with high-pressure and low-pressure column and a main capacitor arranged therebetween.
  • the remaining cold parts, in particular the main heat exchanger 8a are housed in a cuboid heat exchanger box 8.
  • the two cold boxes 8, 9 insulate the respective cold parts of the apparatus against heat from the environment.
  • a transition section 10 also belongs to the low-temperature part. He is also surrounded by a coldbox; Alternatively, located in the transition section 10 piping and fittings are thermally insulated by means of a correspondingly smaller cold box.
  • the main heat exchanger is designed as exclusively recuperative heat exchanger, so not as a switchable heat exchanger (Revex). It consists, for example, of one block or a plurality of flow-connected blocks.
  • the block or blocks are preferably designed as aluminum plate heat exchangers.
  • Possible further heat exchangers, such as one or more subcooling countercurrents, may also be accommodated in the heat exchanger box; alternatively or additionally, one or more blocks of subcooling countercurrents may be arranged in the rectification box.
  • the form of the rectification box may differ from the exemplary embodiment; For example, it may be substantially cuboidal.
  • the main air compressor 2 is driven via a first shaft 11 by a drive means 12, which is designed as an electric motor, gas or steam turbine.
  • a booster 14 is for a portion of the purified air 54 intended.
  • the inlet of the booster 14 is connected to the pipe 54 for the purified air.
  • the further compressed air in the booster 14 is passed through a further, not shown in the drawing pipe in the low-temperature part 7, in particular in the heat exchanger box 8.
  • the booster 14 is also driven by a further shaft 13 of the drive means 12.
  • the booster could be driven independently of the main air compressor, for example by a separate gas or steam turbine or by a separate electric motor.
  • the products of the low-temperature part 7 are discharged via exemplary product lines 105, 106, which open here into manifolds 107 and 108, respectively.
  • the manifolds 107, 108 are arranged on a pipe bridge 109 and can connect the device and possibly other identical or similar devices (strands) to a multi-strand system or lead to a tank farm and / or to an emergency supply device.
  • an evaporative cooler 15 For cooling water before its introduction into the direct contact cooler 3, an evaporative cooler 15 is used. In it, dry residual nitrogen from the low-temperature part is brought into direct heat and mass transfer with cooling water to be cooled. About the cooling water piping 61 cold cooling water is passed to the direct contact cooler. Warm cooling water is returned directly or indirectly to the evaporative cooler. The moist nitrogen from the evaporative cooler escapes into the atmosphere.
  • the apparatus also includes utility piping 63, the location of which is schematically indicated in the drawing.
  • the equipment piping serves to transport steam, gas and / or cooling water and to dispose of condensate, cooling water, etc. It flows into resource headers (not shown), which can be arranged on the pipe bridge 109.
  • Resource and booster air tubing 63, 62 may be located on the floor (on sleepers) or on one or more pipe bridges.
  • the base surfaces of the direct contact cooler 3, the cleaning device 4 and the low-temperature part 7 have in the embodiment circular, rectangular or a complex shape. These bases are arranged in a line, for example on a main orientation axis 101. In addition, this line 101 also extends through the base area of the main air compressor 2. This results in a particularly short feed gas piping 52/53/54.
  • the product lines 105, 106 which are arranged parallel to the entrance of the insert line 54, have a particularly short length. They can even be so short that their own pipe bridge is not needed.
  • the rectangle 102 which encloses the bases of direct contact cooler 3, cleaning device 4 and low-temperature part 7, is approximately 1.7 times longer in the extent that extends vertically in the drawing than in the direction perpendicular thereto (horizontally in the drawing).
  • a factor of about 1.8 applies for the rectangle 103, which also encloses the base of the main air compressor and the apparatuses connected to it.
  • a short pipe bridge 109 and short lines 107, 108 of sufficient length for the product removal or the resource supply and removal; This is particularly advantageous in multi-strand systems. (Due to its schematic character, the drawing is not necessarily to scale in this respect either.)
  • direct contact coolers 3 and evaporative coolers 15 are arranged as a unit or at least as immediately adjacent units because of their functional relationship. In the embodiment, however, the evaporative cooler 15 is much closer to the low temperature part than the direct contact cooler.
  • the distance 104 between the evaporative cooler 15 and the main heat exchanger 8a is about one fifth of the distance between the direct contact cooler 3 and the low temperature part 7.
  • the residual nitrogen pipe between the main heat exchanger and the evaporative cooler 15 which is not shown in the drawing, only a relatively short Overcome route and can therefore be realized particularly cost effective; This saving is significant because of the very large cross-section of the residual nitrogen pipe.
  • the cooling water piping is longer, but has a much smaller cross-section and increases the cost of the apparatus only insignificantly.
  • Cryogenic air separation plants regularly have one or more expansion machines, which serve to generate cold by work-performing relaxation of one or more process streams and are usually designed as turbines.
  • the plant of the embodiment preferably has a turbine for work-performing expansion of a partial flow of the feed air or a product or intermediate product stream from the low-temperature decomposition. This turbine is seated in a turbine box 16, which is arranged in the embodiment at the transition section 10 between the heat exchanger box 8 and rectification box 9.

Claims (16)

  1. Procédé de production d'un produit par séparation cryogénique d'un mélange gazeux, en particulier d'air, avec un refroidisseur à contact direct (3) pour le refroidissement du mélange de charge, avec un dispositif de purification (4) pour purifier le mélange de charge refroidi et avec une partie cryogénique (7), qui présente un échangeur de chaleur principal (8a) pour le refroidissement du mélange de charge purifié environ à la température du point de rosée et une colonne de distillation (9a) pour la séparation cryogénique du mélange de charge, caractérisé en ce que le refroidisseur à contact direct (3), le dispositif de purification (4) et la partie cryogénique (7) sont disposés sur une ligne (101) et le dispositif est conçu pour un débit de gaz de charge de 300 000 Nm3/h ou plus, dans lequel la disposition "sur une ligne" signifie qu'il doit y avoir au moins une droite horizontale, qui coupe les faces de base de tous les trois composants de l'installation précités et par "face de base" on entend ici la face de pose qui est nécessaire pour les composants correspondants de l'installation y compris les unités fonctionnelles directement correspondantes comme par exemple des pompes et des armatures.
  2. Dispositif selon la revendication 1, caractérisé par un compresseur de gaz de charge (2) monté avant le refroidisseur à contact direct (3) pour la compression du mélange de charge, dans lequel le compresseur de gaz de charge (2), le refroidisseur à contact direct (3), le dispositif de purification (4) et la partie cryogénique (7) sont disposés sur une ligne (101).
  3. Dispositif selon la revendication 1 ou 2, caractérisé par un compresseur de gaz de charge (2) monté avant le refroidisseur à contact direct (3) pour la compression du mélange de charge, dans lequel l'arbre d'entraînement (11) du compresseur de gaz de charge (2) est essentiellement perpendiculaire à la ligne (101), sur laquelle le refroidisseur à contact direct (3), le dispositif de purification (4) et la partie cryogénique (7) sont disposés.
  4. Dispositif selon la revendication 1, caractérisé par un compresseur de gaz de charge (2) monté avant le refroidisseur à contact direct (3) pour la compression du mélange de charge, dans lequel l'arbre d'entraînement du compresseur de gaz de charge (2) est essentiellement parallèle à la ligne (101), sur laquelle le refroidisseur à contact direct (3), le dispositif de purification (4) et la partie cryogénique (7) sont disposés.
  5. Dispositif selon l'une quelconque des revendications 1 à 4, caractérisé en ce que le rapport de l'extension du plus petit rectangle (102; 103), qui entoure les faces de base du refroidisseur à contact direct (3), du dispositif de purification (4) et de la partie cryogénique (7) et éventuellement du compresseur de gaz de charge (2) dans la direction d'une droite de liaison (101) entre le refroidisseur à contact direct (3) et la partie cryogénique (7) à l'extension dans la direction perpendiculaire à celle-ci, est supérieur à 1, en particulier supérieur à 1,8.
  6. Dispositif selon l'une quelconque des revendications 1 à 5, caractérisé en ce que la partie cryogénique (7) présente un boîtier d'échangeur de chaleur (8), qui contient au moins un échangeur de chaleur principal, un boîtier de rectification (9), qui contient au moins une colonne de distillation, une section de transition (10), qui est disposée entre le boîtier d'échangeur de chaleur (8) et le boîtier de rectification (9), et un caisson de turbine (16), qui contient une machine de détente, dans lequel le caisson de turbine (16) est relié à la section de transition (10).
  7. Dispositif selon l'une quelconque des revendications 1 à 6, avec une conduite de mélange de charge (51, 52, 53, 54) pour l'introduction de mélange de charge dans l'échangeur de chaleur principal et avec une conduite de produit (105, 106) pour soutirer le courant de produit hors de l'échangeur de chaleur principal, caractérisé en ce que la conduite de mélange de charge (54) et la conduite de produit (104, 105) sont essentiellement parallèles à un axe d'orientation principal (101) et sont disposées sur des côtés opposés l'un à l'autre de l'échangeur de chaleur principal.
  8. Dispositif selon la revendication 7, caractérisé par une conduite de collecte (107, 108), dans laquelle la conduite de produit (104, 105) débouche à son extrémité éloignée de l'échangeur de chaleur principal, dans lequel la conduite de collecte (107, 108) est essentiellement perpendiculaire à l'axe d'orientation principal (101).
  9. Dispositif selon la revendication 8, caractérisé en ce que la conduite de collecte (107, 108) est disposée sur une passerelle à tubes (109) ou sur le sol.
  10. Dispositif selon la revendication 8 ou 9, caractérisé en ce que la conduite de collecte est raccordée à une conduite de produit d'une ou de plusieurs autres installations de séparation cryogénique.
  11. Dispositif selon une des revendications 8 ou 9, caractérisé en ce que la conduite de collecte est raccordée à un réservoir d'accumulation pour le produit.
  12. Dispositif selon l'une quelconque des revendications 7 à 11, caractérisé en ce que l'échangeur de chaleur principal (8a) est constitué exclusivement par un échangeur de chaleur à récupération.
  13. Dispositif selon l'une quelconque des revendications 1 à 12, avec un circuit d'agent réfrigérant (61) pour la fourniture d'agent réfrigérant pour le refroidisseur à contact direct, dans lequel le circuit d'agent réfrigérant présente un refroidisseur par évaporation (15) pour le refroidissement d'agent réfrigérant par échange de chaleur direct avec un courant de gaz provenant de la partie cryogénique, caractérisé en ce que le rapport de la distance entre le refroidisseur par évaporation (15) et le refroidisseur à contact direct (3) à la distance (104) entre le refroidisseur par évaporation (15) et l'échangeur de chaleur principal (8a) vaut au moins 0,5, en particulier au moins 1,0.
  14. Dispositif selon la revendication 13, caractérisé en ce que le rapport de la distance entre le refroidisseur par évaporation (15) et le refroidisseur à contact direct (3) à la distance (104) entre le refroidisseur par évaporation (15) et l'échangeur de chaleur principal (8a) vaut au moins 2, en particulier au moins 4.
  15. Dispositif selon la revendication 13 ou 14, caractérisé en ce que la distance (104) entre le refroidisseur par évaporation (15) et l'échangeur de chaleur principal (8a) vaut au plus 20 m, en particulier au plus 10 m.
  16. Dispositif selon l'une quelconque des revendications 13 à 15, caractérisé en ce que la distance entre le refroidisseur par évaporation et le refroidisseur à contact direct (3) vaut au moins 10 m, en particulier au moins 25 m.
EP05024947.3A 2004-12-03 2005-11-15 Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air Not-in-force EP1672301B1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP05024947.3A EP1672301B1 (fr) 2004-12-03 2005-11-15 Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air
PL05024947T PL1672301T3 (pl) 2004-12-03 2005-11-15 Urządzenie do niskotemperaturowego rozkładu mieszanki gazowej, zwłaszcza powietrza

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
EP04028683A EP1666823A1 (fr) 2004-12-03 2004-12-03 Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air
EP04028682 2004-12-03
EP04028681A EP1666822A1 (fr) 2004-12-03 2004-12-03 Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air
EP05024947.3A EP1672301B1 (fr) 2004-12-03 2005-11-15 Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air

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EP1672301A1 EP1672301A1 (fr) 2006-06-21
EP1672301B1 true EP1672301B1 (fr) 2018-08-15

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EP04028681A Withdrawn EP1666822A1 (fr) 2004-12-03 2004-12-03 Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air
EP04028683A Withdrawn EP1666823A1 (fr) 2004-12-03 2004-12-03 Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air
EP05024947.3A Not-in-force EP1672301B1 (fr) 2004-12-03 2005-11-15 Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air

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EP04028681A Withdrawn EP1666822A1 (fr) 2004-12-03 2004-12-03 Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air
EP04028683A Withdrawn EP1666823A1 (fr) 2004-12-03 2004-12-03 Installation pour la séparation cryogénique d'un mélange gazeux en particulier d'air

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US (1) US7516626B2 (fr)
EP (3) EP1666822A1 (fr)
CN (1) CN100575838C (fr)
CA (1) CA2528735C (fr)
PL (1) PL1672301T3 (fr)
RU (1) RU2382963C2 (fr)

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Publication number Publication date
CA2528735A1 (fr) 2006-06-03
PL1672301T3 (pl) 2019-01-31
EP1672301A1 (fr) 2006-06-21
EP1666822A1 (fr) 2006-06-07
CN1782644A (zh) 2006-06-07
US7516626B2 (en) 2009-04-14
EP1666823A1 (fr) 2006-06-07
RU2005137481A (ru) 2007-06-20
CA2528735C (fr) 2013-08-06
US20060156759A1 (en) 2006-07-20
RU2382963C2 (ru) 2010-02-27
CN100575838C (zh) 2009-12-30

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