Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
  • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
  • F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
  • F28D7/1684—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation the conduits having a non-circular cross-section
• • 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
  • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
  • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
  • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
  • F25J5/005—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger in a reboiler-condenser, e.g. within a 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
  • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
  • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
  • F25J5/007—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger combined with mass exchange, i.e. in a so-called dephlegmator
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
  • F28F1/00—Tubular elements; Assemblies of tubular elements
  • F28F1/10—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
  • F28F1/12—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element
  • F28F1/126—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element consisting of zig-zag shaped fins
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
  • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
  • F28F9/02—Header boxes; End plates
• • 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
  • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
  • F25B2339/00—Details of evaporators; Details of condensers
  • F25B2339/04—Details of condensers
  • F25B2339/041—Details of condensers of evaporative condensers
• • 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
  • F25J2200/00—Processes or apparatus using separation by rectification
  • F25J2200/80—Processes or apparatus using separation by rectification using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
• • 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
  • F25J2210/18—H2/CO mixtures, i.e. synthesis gas; Water gas, shifted synthesis gas or purge gas from HYCO synthesis
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2250/00—Details related to the use of reboiler-condensers
  • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2250/00—Details related to the use of reboiler-condensers
  • F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
  • F25J2290/44—Particular materials used, e.g. copper, steel or alloys thereof or surface treatments used, e.g. enhanced surface
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
  • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
  • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
  • F28D2021/0033—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for cryogenic applications
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F28—HEAT EXCHANGE IN GENERAL
  • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
  • F28F21/00—Constructions of heat-exchange apparatus characterised by the selection of particular materials
  • F28F21/08—Constructions of heat-exchange apparatus characterised by the selection of particular materials of metal

Definitions

• the present invention relates to a method of vaporization and optionally of condensation of fluid in a heat exchanger and to a system for separating a mixture of fluids by cryogenic distillation comprising at least one heat exchanger operating according to such a method.
• it relates to a method of vaporization and possibly condensation of air gas in an installation for separating air gases by cryogenic distillation.
• Air separation units have for a very long time been using brazed aluminum plate heat exchangers for the reboiler / condenser functions of the distillation columns, including the double column reboiler / condenser with condensing nitrogen. and oxygen spraying.
• Two principles of operation of these reboilers / condensers have been proposed: in thermosiphon: it is the oldest solution with two variants:
• the body of the vaporizer can be arranged vertically and completely (or partially) immersed in a bath of liquid oxygen. This liquid oxygen enters the bottom of the vaporizer is warmed to its bubble point and is partially vaporized.
• the recirculation rate (excess flow of liquid output on vaporized flow) is very high, ranging from 5 to 100.
• the dimensions of the bodies can be of the order of 1220 mm wide x 1200 mm stacking x 2000 mm length.
• the body of the vaporizer is disposed horizontally and completely (or partially) immersed in a bath of liquid oxygen.
• the operation is identical to that of the vertically installed vaporizer.
• the oxygen side operation is improved.
• the design of the nitrogen passages is not obvious.
• EP-A-1008826 proposes a film vaporizer in which the exchanger comprises passages defined by parallel plates.
• the liquid vaporization passages contain auxiliary passages comprising only curved surfaces, for example cylindrical tubes.
• the object of the invention is to propose a method of condensation and / or vaporization using a heat exchanger which overcomes the defects of the art
• the subject of the invention is a method of vaporizing and / or condensing at least one fluid in a heat exchanger consisting of a stack of at least one tube and at least one folded wave, the wave and the tube being preferably brazed with each other, and in which a first fluid, possibly to be condensed, circulates inside at least one tube, and a second fluid, possibly to vaporize, circulates around the wave in which a) the first fluid condenses and the second fluid vaporizes or b) the first fluid vaporizes and the second fluid condenses.
• the folding of the waves is substantially parallel to the axis of the tubes;
• the tubes and waves are made of aluminum, pure or alloyed;
• the tubes and waves are made of copper alloy
• the tubes and waves are made of iron-based alloy
• the tubes are oblong and / or flattened
• the tube has parallel channels inside comprising two parallel flat walls and internal walls connected to the two flat walls and defining the parallel channels;
• the exchange surface inside the tubes is obtained by folding, extrusion or brazed preference inserts for example waves; and the waves are perforated, straight, serrated and / or louvered.
• the vaporization is carried out in the tubes and the invention would then relate to a method of vaporization and possibly condensation of at least one fluid in a heat exchanger consisting of a stack of at least one tube and at least one wave folded, the wave and the tube being preferably brazed with each other, and wherein a fluid, to be vaporized, circulates inside at least one tube and another possibly sprayable fluid circulates in channels generated by waves.
• the invention more particularly relates to a method of vaporizing at least one liquid derived from air and optionally of condensation of at least one gas derived from air, or which is air, as described above.
• the invention also relates to a method of vaporization of at least one liquid having, as main component, methane and / or carbon monoxide and / or hydrogen, and optionally of condensation of at least one gas whose main component is methane and / or carbon monoxide and / or hydrogen, as previously described.
• the invention finally relates to an installation for separating a fluid mixture by cryogenic distillation in at least one column having at least one heat exchanger operating according to a heat exchange method in a heat exchanger consisting of a stack of at least one tube and at least one folded wave, the wave and the tube being preferably brazed to one another, and wherein a fluid circulates within at least one tube and a Another fluid circulates around the wave, one warming while the other is cooling. .
• At least one of the heat exchangers of such an installation is of one of the following types: i) a vaporizer-condenser allowing the vaporization of a liquid by heat exchange with a gas which is condensing inside or outside a distillation column or; ii) a subcooler or; iii) a regeneration gas heater of a purification unit used to purify the mixture to be distilled or; iv) a dephlegmator or; v) a heat exchanger having passages for cooling the mixture to be distilled at a cryogenic temperature or; vi) a cooling exchanger of an inter-stage of a compressor of the mixture to be distilled or a product of the distillation.
• thermosiphon-type reboiler-condenser in which the direction of the fluid in condensation in the tubes is counter-current to the direction of the fluid vaporizing in the channels generated by the waves, because of the condensation in the tubes, it will be placed the gas collector at the top and the liquid collector at the bottom, so as to facilitate the gravity flow of the liquid.
• the direction of the condensing fluid in the tubes is co-current of the direction of the fluid vaporizing in the channels generated by the waves and a device for supplying the liquid to be vaporized must be added at the top of the waves.
• Such a structure could also work as a dephlegmator.
• exchangers derived from automotive radiator technology in cryogenic distillation gas separation is not limited to vaporizers-condensers, which vaporize a fluid by heat exchange with another fluid that condenses, but can also be used for:
• FIG. 1 is a front elevational view of a heat exchanger of a first type according to the invention
• FIG. 2 is a schematic perspective view of a heat exchanger for carrying out the method according to the invention
• FIG. 3 is a perspective view, on a larger scale and in the same direction, of a portion of the exchanger shown in Figure 1, according to a first embodiment
• FIG. 4 is a perspective view showing a tube section of the exchanger of Figure 2, according to a second embodiment
• FIG. 5 is a sectional view, in a vertical plane, of a stack of tubes and waves of a heat exchanger according to a third embodiment.
• FIGS. 6 and 7 are diagrammatic views, respectively from above and from the front, of a reboiler-condenser of an installation according to the invention, which contains exchangers of a second type, similar to the first one shown in FIGS. 1 and 2.
• Figure 1 there is shown schematically a heat exchanger
• FIGS. 1 to 5 will be oriented along the orthogonal coordinate system X, Y, Z, in which: the axes X and Z define the vertical plane of FIG. 1 and the principal directions in which extends the heat exchanger 1, the X axis being assumed horizontal, and the Z axis being assumed vertical; and
• the exchanger shown in FIG. 1 essentially comprises on the one hand a stack of elongated tubes 3, spaced apart and parallel to one another, and extending horizontally along the X axis, and on the other hand folded oblong fins (not visible in Figure 1), arranged in the intervals between two consecutive tubes 3.
• the tubes 3 are connected, at one of their ends, to a distribution column 5, and at their other end to a collecting column 7.
• the two columns 5, 7 are formed of vertical tubular conduits in fluid communication with each tubes 3.
• the tubes 3 are brazed on the columns 5, 7 which have been previously formed to allow the tubes 3 to fit into said columns. These columns are not necessarily cylindrical. It may be a tubular plate stamped to allow the tubes to be interlocked on which the tubes will have been preferably brazed and on which a box of typically half-cylindrical shape will be attached for example by welding after the operation of brazing.
• the distribution column 5 is equipped, in an upper part, with a fluid inlet connector 9 for supplying the exchanger 1 with a first fluid.
• the collecting column 7 is correspondingly provided, in a lower part, with an outlet connection 11 ensuring the evacuation of the first fluid of the exchanger 1.
• the exchanger shown in FIG. 2 essentially comprises, on the one hand, a stack of elongate tubes 3 spaced apart and parallel to one another, and on the other hand folded oblong fins (not visible in Figure 2), arranged in the intervals between two consecutive tubes 3.
• the elongate tubes 3 extend vertically along the axis Z and the direction of waviness or folding of the fins 17 of Figure 2 is parallel to the longitudinal axis of the tubes 3, that is to say the Y axis;
• the tubes 3 are connected, at their upper end, to a distribution column 5, and at their other end to a collecting column 7.
• the two columns 5, 7 are formed of vertical tubular pipes placed horizontally and in fluid communication with each tubes 3.
• the tubes 3 are brazed on the columns 5, 7 which have been previously formed to allow the tubes 3 to fit into said columns. These columns are not necessarily cylindrical. It may be a tubular plate stamped to allow the tubes to be interlocked on which the tubes will have been preferably brazed and on which a box of typically half-cylindrical shape will be attached for example by welding after the operation of brazing.
• the distribution column 7 is equipped, on the left, with an inlet connector 11 making it possible to supply the exchanger 1 with a first fluid in gaseous form.
• the connection extends perpendicularly to the axis of the distribution column and to the axis of the tubes. This connection could nevertheless extend in another direction, for example along the Z axis or possibly Y.
• the collecting column 5 is correspondingly provided, in a lower part, with an outlet connection 9 ensuring the evacuation of the first fluid of the exchanger 1.
• the connection extends perpendicular to the axis of the column of distribution and to the axis of the tubes. This connection could nevertheless extend in another direction, for example along the Z axis or possibly Y.
• the connectors 9, 11 have been schematically represented in FIG. 2.
• thermosiphon vaporization a fluid to be vaporized (a second fluid) circulates through the vane 17, in an upward vertical direction (that is to say that the fluid to be vaporized is circulated). in the channels generated by the waves), and a fluid of higher temperature (first fluid) is circulated inside the tubes 3 in a downward vertical direction.
• a fluid possibly to be condensed circulates through the fin 17, in a downward vertical direction (that is to say that the fluid is circulated to be condensed in the channels generated by the waves), and a lower temperature fluid to be vaporized is circulated inside the tubes 3 in a downward vertical direction.
• FIG 3 there is shown a portion of a portion of the exchanger 1 of Figure 1, consisting of two consecutive tubes 3, and a corrugated fin 17 formed between these two tubes.
• the tubes 3 have a current section, in the vertical plane XY, of elongated shape transversely along the axis X, so that they each have two opposite faces substantially flat and parallel.
• the tubes 3 have an oblong section along the transverse axis X, and of flattened shape.
• the fin 17 is corrugated in a direction of corrugation or folding Y, perpendicular to the longitudinal axis of the tubes 3.
• the fin 17 is fixed to the tubes 3, preferably by soldering, at its vertices 19. This brazing operation may be concomitant with the brazing of the tubes 3 on the columns 5.7.
• the fins 17 may be of any suitable type, for example one of the following types, commonly used in plate heat exchangers, namely: perforated, straight, “serrated” (partially offset) fins, " herringbone “(zigzag) and louvers.
• the fins 17 may have, in section in the YZ plane, a sinusoidal, crenellated or triangular shape, or may have any other suitable type of geometric pattern.
• the hydraulic diameter of the channels formed by the fins 17 is typically between 100 microns and 10 mm.
• These fins may be solid sheets, perforated sheets, sintered metal or any other metal structure (foam, ).
• the tubes 3 and the fins 17 may be made of pure aluminum or alloyed. Alternatively, the tubes 3 and the fins 17 may be made of copper-based alloy.
• the tubes 3 and the fins 17 may be made of iron-based alloy.
• the exchanger 1 of FIG. 2 comprises fins 17 oriented no longer along the X axis but along the Z axis.
• each tube is divided in two longitudinally.
• the tube 103 has its upper face cut along a median longitudinal line, the two edges 21, 22 separated by this line being folded towards the inside of the tube and welded to the bottom wall.
• the strips thus folded are contiguous and form a double partition wall between the two longitudinal compartments 103A, 103B thus defined. These compartments are called channels.
• the welding of the edges 21, 22 on the bottom wall can for example be performed by laser.
• a heat exchanger formed from tubes of this type is likely to withstand the pressure of the fluid flowing in the channels 103A, 103B because it is smaller in size than the tube 3. Such a design can be used to generate a number of channels greater than 2. Additionally, a heat exchanger formed from tubes of this type is likely to operate with three different fluids, one circulating around the fins, another flowing in one of the 103A channels, and the last flowing in the other 103B channels.
• FIG 5 there is illustrated another embodiment of a stack of tubes and fins, adapted for carrying out the method according to the invention.
• the tubes 203 are also cross-sectionally elongate tubes with opposite flat and parallel faces. Their internal volume is, however, divided into a plurality of parallel longitudinal channels 203A, separated by plane walls 23 parallel to each other, here vertical. The hydraulic diameter of these channels is typically between 100 ⁇ m and 10 mm.
• the walls 23 may be integral with the outer walls of the tube 203, for example by extrusion, or may consist of inserts, preferably brazed. These inserts can be very similar to the fins 17.
• each layer of tubes consists of two adjacent parallel tubes arranged in the same plane.
• a wall 204 surrounds the tubes 203 and the fins 17 so as to make the heat exchanger vis-à-vis its environment.
• This wall can be brazed on the tubes 203 or simply circled around the tubes 203.
• the fluid to be vaporized circulating around the wave 17 circulates in parallel with the fluids to be condensed circulating in the tubes 20.
• the fluids to be condensed on the one hand, and the fluid to be vaporized on the other hand will be circulated in opposite directions.
• FIGS. 6 and 7 show schematically a part of the installation according to the invention, which comprises, inside a ferrule 31 of generally cylindrical shape, a series of heat exchangers 301a-301 n of same type, similar to that of Figures 1 and 2.
• orthogonal coordinate system X 0 , Y 0 , Z 0 is defined as follows:
• the axis Z 0 is the vertical axis oriented from bottom to top;
• the axis X 0 is the horizontal axis defining with the axis Z 0 the principal planes in which the exchangers 301 extend; and the axis Y 0 is the horizontal axis orthogonal to the axis X 0 .
• the exchangers 301a-301 n are all arranged parallel and centered on a diametral plane of the cylindrical shell 31, as can be seen in FIG. 6.
• the length of each exchanger 301 year is adjusted to the length, along the axis X 0 of the vertical section of the shell 31 on the axis Y 0 .
• the length along the axis X 0 of the exchangers 301a-301 n increases towards the central axis Z 0 of the cylindrical shell 31.
• the orientation of the exchangers 301 an is such that the distribution columns 305a-n extend horizontally on the upper side of the ferrule 31, whereas the collector columns 307a-n extend from the lower side of the ferrule 31, also horizontally.
• the stacks of tubes 303 extend between the columns 305a-n, 307a-n, along the vertical axis Z.
• a gas collector 41 provided for supplying gas to the group of exchangers 301a-n.
• the illustrated installation further comprises a liquid collector 43, arranged under the collecting columns 307a-n, and designed to collect the liquid phase from the group of exchangers 301a-n.
• the fins stop before the columns 307a-n and 305a-n so as to allow entry and exit of the fluid.
• the outer wall as shown in Figure 5 (204) substantially stops at the same levels as the fins also to allow fluid entry and exit.
• the vaporization and condensation method which has been described above, as well as the installation described with reference to FIGS. 6 and 7, applies to the vaporization of at least one liquid derived from air or a liquid which is the liquefied air and the condensation of at least one gas derived from the air, this gas can also be air itself.
• the method and the installation also apply to the vaporization of at least one liquid having as main component methane and / or carbon monoxide and / or hydrogen, and the condensation of at least one gas having as main component methane and / or carbon monoxide and / or hydrogen.
• Such a method can be applied to many types of fluid mixing separation facilities, operating by cryogenic distillation, in at least one column having one or more heat exchangers, as described above.
• the installation can be:
• a vaporizer-condenser allowing the vaporization of a liquid by heat exchange with a gas that condenses inside or outside a distillation column, or
• a dephlegmator or a heat exchanger having passages allowing the cooling of the mixture to be distilled at a cryogenic temperature
• a cooling exchanger of an inter-stage of a compressor of the mixture to be distilled or of a product of the distillation is a cooling exchanger of an inter-stage of a compressor of the mixture to be distilled or of a product of the distillation.

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• Engineering & Computer Science (AREA)
• Physics & Mathematics (AREA)
• Thermal Sciences (AREA)
• Mechanical Engineering (AREA)
• General Engineering & Computer Science (AREA)
• Geometry (AREA)
• Separation By Low-Temperature Treatments (AREA)
• Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

Priority Applications (3)

Applications Claiming Priority (2)

Publications (1)

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Family Applications (1)

Country Status (6)

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Citations (9)

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• 2005
  • 2005-10-06 FR FR0553028A patent/FR2891901B1/fr not_active Expired - Fee Related
• 2006
  • 2006-09-29 CN CN200680036668A patent/CN100587382C/zh not_active Expired - Fee Related
  • 2006-09-29 US US12/089,092 patent/US20090211733A1/en not_active Abandoned
  • 2006-09-29 EP EP06831249A patent/EP1931929A1/fr not_active Withdrawn
  • 2006-09-29 WO PCT/FR2006/050962 patent/WO2007042698A1/fr active Application Filing
  • 2006-09-29 JP JP2008534053A patent/JP2009511849A/ja active Pending

Patent Citations (9)

Non-Patent Citations (1)

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