EP0130122A1 - Device for evaporating a liquid by heat exchange with a second fluid and air distillation unit comprising such a device - Google Patents

Device for evaporating a liquid by heat exchange with a second fluid and air distillation unit comprising such a device Download PDF

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Publication number
EP0130122A1
EP0130122A1 EP84401284A EP84401284A EP0130122A1 EP 0130122 A1 EP0130122 A1 EP 0130122A1 EP 84401284 A EP84401284 A EP 84401284A EP 84401284 A EP84401284 A EP 84401284A EP 0130122 A1 EP0130122 A1 EP 0130122A1
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EP
European Patent Office
Prior art keywords
liquid
passages
heat exchanger
bath
exchanger according
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP84401284A
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German (de)
French (fr)
Other versions
EP0130122B2 (en
EP0130122B1 (en
Inventor
Pierre Petit
Maurice Grenier
Jean-François Deschamps
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Priority to AT84401284T priority Critical patent/ATE37229T1/en
Publication of EP0130122A1 publication Critical patent/EP0130122A1/en
Application granted granted Critical
Publication of EP0130122B1 publication Critical patent/EP0130122B1/en
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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
    • 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
    • F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits
    • 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
    • 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
    • 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
    • F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D9/0062—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements
    • F28D9/0068—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for one heat-exchange medium being formed by spaced plates with inserted elements with means for changing flow direction of one heat exchange medium, e.g. using deflecting zones
    • 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
    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
    • 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
    • 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 present invention relates to the vaporization of a liquid by heat exchange with a second fluid by means of a heat exchanger of the type with vertical plates. It applies in particular to air distillation installations.
  • the liquid oxygen which is in the bottom of the low pressure column is vaporized by heat exchange with. nitrogen gas taken from the top of the medium pressure column.
  • the temperature difference between oxygen and nitrogen made necessary by the structure of the heat exchanger imposes the operating pressure of the medium pressure column. It is . It is therefore desirable for this temperature difference to be as small as possible, in order to minimize the expenses linked to the compression of the air to be treated injected into the medium pressure column.
  • the invention aims to provide means for obtaining heat exchange performance at least as good but more reliably and more economically.
  • the subject of the invention is a method for vaporizing a liquid by heat exchange with a second fluid by means of a heat exchanger comprising a parallelepipedic body formed by an assembly of parallel vertical plates defining between them a multitude of flat passages, method of the type in which the liquid is sent in a first set of passages and the second fluid in the remaining passages, characterized in that the liquid is distributed in. two stages at the upper end of the passages of said first set, over the entire horizontal length thereof, the two stages comprising a rough predistribution of the liquid over the entire length of the passages of said first assembly, then a fine distribution over the entire length of these passages of the liquid thus predistributed.
  • the liquid flow rate is adapted to permanently ensure the presence of a liquid film over practically the entire extent of all the walls contained in each of the passages of said first assembly.
  • the invention also relates to a heat exchanger intended for the implementation of such a process.
  • This exchanger is characterized in that it comprises means for predistributing the liquid leading to means for fine distribution of the liquid arranged at the upper end of each of the passages of said first assembly.
  • the predistribution means comprise openings, in particular a horizontal row of holes, and retaining means for forming a bath of liquid above these openings; said fine distribution means may comprise a lining, or alternatively, when said openings are made in the plates of the exchanger, a surface for spreading the jets of liquid leaving these openings.
  • the invention also relates to an air distillation installation of the double column type, in which the liquid from the bottom of the medium pressure column is brought into heat exchange relationship with the top gas of the low pressure column at means of a heat exchanger as defined above, this installation comprising supply means for supplying the liquid to said predistribution means; and means for supplying gas to the. passages of said second set.
  • FIG. 1 illustrates a possibility of installing an oxygen-nitrogen heat exchanger in an air distillation installation of the double column type.
  • This installation comprises a medium pressure column 1 at the bottom of which the air to be treated is injected, under a pressure of the order of 6 bars absolute.
  • the oxygen-enriched liquid which is collected in the tank of column 1 is sent under reflux in the middle of the height of a second column (not rearranged), called the low pressure column, which operates slightly above atmospheric pressure.
  • the nitrogen gas which is at the head of column 1 is brought into heat exchange relationship with the liquid oxygen collected in the bottom of the low pressure column; the condensed condensing nitrogen serves as reflux in column 1 and in the low pressure column, while the resulting vaporized oxygen is returned to the bottom of the low pressure column.
  • the exchanger 2 consists of a sealed envelope 3, the main height of which contains a set of parallel plates 4 of rectangular aluminum shape, with a length of the order of 1 to 1.5 m and a height of the order of 3 to 6 m, between which waves also made of aluminum are fixed by brazing.
  • the space located above the plates 4 contains a liquid oxygen bath 5 supplied by a line 6 coming from the tank of the low pressure column and provided with a pump (not shown).
  • a bath level regulator 5 which is shown diagrammatically by a level measuring tube 6A, or, as a variant, by a flow regulator.
  • a pipe 7 for returning oxygen vaporized above the bath 5 to the bottom of the low pressure column, resulting from the heat inputs at the pump and the pipes.
  • the set of plates 4 is supplied at its upper part with gaseous nitrogen by a horizontal feed box 8 which communicates by a pipe 9 with the head of the medium pressure column 1.
  • the evacuation of the condensed nitrogen takes place at the base of the plates 4 by a horizontal collecting box 10 which communicates by a pipe 11 with a guarded channel 12 disposed at the head of the column 1.
  • On the box 10 is stuck a pipe 13 for discharging incondensable rare gases.
  • a pipe 14 connects the tank of the low pressure column to the space located in the casing 3 below the plates 4. This pipe penetrates vertically into this space through the bottom point of the casing 3, and its upper end is surmounted by a conical deflector 15. From the bottom of the casing 3 also leaves a pipe 16 intended to return to the bottom of the low pressure column the excess liquid oxygen.
  • the casing 3 has a parallelepiped shape.
  • the plates 4 define a multitude of passages intended alternately for the flow of oxygen (passages 17) and for the flow of nitrogen (passages 18). Over most of their height, the passages 17 and 18 each contain a wave 19 consisting of a corrugated perforated aluminum sheet with vertical generators.
  • each nitrogen passage comprises a liquid oxygen tank 22 containing a vertical wave 23 of perforated aluminum sheet, with vertical generators, the thickness and pitch of which are clearly greater than those of waves 19.
  • the waves 23 have only a function of spacers between the plates 4, so as to allow the assembly of the exchanger by a single brazing operation.
  • the tanks 22 are open upwards to communicate with the liquid oxygen bath 5.
  • the waves 19 of the oxygen passages 17 extend downwards to the lower end of the plates 4, so that these passages are open down. These waves extend upwards to the upper edge of the bars 21, then are extended by a lining 24.
  • the latter consists of a wave of the "serrated" type which is illustrated in more detail in FIG. 6.
  • the wave 24 is an unperforated aluminum sheet with horizontal generators (so-called "hard way” arrangement with respect to the flow of liquid oxygen).
  • each horizontal or psaudo-horizontal facet 25 of the wave 24 is provided with a puncture 26 offset upwards by a quarter of a wave step.
  • the width of the punctures 26, measured along a generatrix of the wave, is of the same order as the distance which separates each of them from the two adjacent punctures situated on the same facet 25.
  • each plate 4 comprises, above the lining 24, a horizontal row of holes 27 arranged at regular intervals over the entire length of the exchanger, the holes of the successive plates being arranged at the same height but in a staggered arrangement. As a variant, these holes could moreover be provided only in every second plate.
  • the oxygen passages are closed by horizontal bars 28, arranged at the upper end of the plates 4. To avoid the risk of obstruction of certain holes 27 by waves 23, these are interrupted for a short height at the level of said holes.
  • the regulating device of the pump for supplying the exchanger 2 with liquid oxygen maintains above the plates 4 a level of the bath 5 sufficient to overcome the various pressure drops which oppose the flow of oxygen.
  • the height liquid oxygen above the plates 4 is for example of the order of 20 cm.
  • Liquid oxygen fills the reservoirs 22 and passes through the holes 27, at a flow rate defined by the passage section of the latter and by the height of liquid which overcomes it. As this height is constant in steady state, the flow of liquid oxygen is that supplied by the pump for raising this liquid.
  • the holes 27 therefore provide a rough predistribution of the liquid oxygen along the passages 17, and the liquid oxygen thus pre-distributed appears on the lining 24, which ensures a fine distribution over the entire length of each passage 17.
  • Liquid oxygen thus approaches waves 19 by flowing in a perfectly uniform manner over all the walls (waves 19 and plates 4) of the passages which are assigned to it, that is to say by forming on these walls a continuous descending film.
  • the nitrogen gas arrives in the exchanger through the box 8 and the distribution waves 20, then flows down along the passages 18. In so doing, it gradually gives off heat to the oxygen. liquid which is in the adjacent passages 17, so that the oxygen vaporizes and that, simultaneously, the nitrogen condenses.
  • the condensed nitrogen is collected in the box 10 and flows in the pipe 11 as far as the channel 12.
  • this liquid overflows from the channel and falls into reflux in the medium pressure column after a portion has been withdrawn through a pipe 11A to ensure the reflux of the low pressure column. This creates suction in the passages 17, which ensures the circulation of nitrogen.
  • the liquid oxygen flow rate is adjusted so as to guarantee an excess of liquid oxygen over the entire height of the plates 4.
  • a total vaporization of the oxygen in a region of the passages 17 would lead to this location at a concentration of acetylene dissolved in liquid oxygen, which could cause a local explosion.
  • this risk of explosion it would also result in a drop in performance of the exchanger by neutralization of the non-wetted surface. This risk is limited thanks to the high efficiency of the fine distribution ensured by the lining 24.
  • the bars 21 which limit the upper passages 18 are arranged at the upper end of the plates 4, like the bars 28.
  • the holes 27 are eliminated and replaced by vertical holes 29 drilled at regular intervals in the bars 28, all along these.
  • the liquid oxygen in the bath 5 flows through the holes 29, at a flow rate corresponding to that of the liquid oxygen pump, and is thus predistributed over the entire length of the passages 17; these liquids then fall on the lining 24 located just below (this lining has been represented ores schematically in FIG. 3).
  • the lining 24 ensures a uniform fine distribution of the liquid oxygen over the entire length of the passages 17, and this liquid then flows along the waves 19 and the corresponding walls 4.
  • the heat exchange between oxygen and nitrogen begins during the passage of liquid oxygen through the linings 24, which are at the same level as the nitrogen gas distribution waves.
  • the holes 29 of the bars 28 instead of being of a constant diameter over the entire height of these bars, can have an enlarged diameter in most of their height by a counter-bore 29A produced from the bottom.
  • FIG. 5 shows that similar holes can also be obtained by perforating the upper core 30 of U-shaped profiles constituting the bars 28.
  • the advantage of these two embodiments lies in the fact that the useful part of the holes 29, which defines the liquid oxygen passage section is short and therefore less subject to the appearance of blockages or undesirable vaporization.
  • the vaporized oxygen is evacuated from below at the same time as the excess liquid oxygen.
  • the vaporized oxygen is free to escape both from the top and from the bottom.
  • the exchanger of FIG. 6 is identical to that of FIG. 2 from the bottom of the plates 4 to the level of the upper edge of the bars 21 which limit the nitrogen passages 18 above.
  • each plate 4 has a horizontal row of holes 31. Above these, the. plates 4 extend over a significant height, up to a level higher than that of the free surface of the liquid oxygen bath 5.
  • waves - spacers 32 with vertical generators similar to the waves 23 in FIG. 2.
  • a free space 33 is provided at the holes 31, above waves 19, and this space is overcome, from bottom to top by the lining 24 previously described, by a bar 28 with holes 29 similar to those of FIG. 3, and by a wave-spacer 34 similar to waves 32 but with generators horizontal.
  • the bath 5 is supplied laterally by a supply box 35 located above the box 8 and opening into the spaces occupied by the waves 34.
  • the bars 36 which close the passages 17 on this side of oxygen extend upward only up to the level of the upper edge of the bars 28.
  • the heat exchanger illustrated in FIG. 7 differs from that of FIG. 2 only in the way in which the oxygen is distributed and evacuated.
  • the lining 24 is eliminated; the jets of liquid oxygen 37 leaving the holes 27 strike the plate 4 opposite and spread over the latter.
  • the spacing and the diameter of these holes are chosen so that the sheets of parabolic shape thus formed meet in a continuous sheet a little above the heat exchange waves 19.
  • the predistribution of oxygen is still provided by the holes 27, while its fine distribution is provided by the plates 4 themselves.
  • This distribution method is particularly simple and has the advantage of not creating a significant obstacle to the evacuation of the oxygen vaporized from the top of the passages 17, as shown.
  • the lower end of the passages 17 can then be either closed and provided with means for collecting the excess liquid oxygen, or open to also allow the gaseous oxygen the possibility of being evacuated from below.
  • the areas for spreading the jets can be provided on additional plates 39 attached to the plates 4.
  • the exchanger region located above the bars 21 does not require any waves.
  • waves 23 made of strong sheet metal and with large pitch can be used as spacers, these ecant waves interrupted at the level of the holes 27 and in the areas of spreading of the jets.
  • FIG. 8 there is shown in the passages 17 a wave 23 in two parts, respectively above and below the holes 27, with a striated zone 40. Opposite these holes and another striated zone 41 between the wave 23 and wave 19. This figure 8 also shows that such waves 23 allow the simultaneous installation of additional plates 39.
  • holes 27 can be provided in all the plates 4, with of course a suitable offset, in order to supply each passage 17 with two layers of liquid oxygen.
  • the nitrogen circuit is conventional. It can therefore be replaced by other known types of nitrogen circuits, in particular by those described in the FR patent. 78.20.757 of the plaintiff.
  • one or more heat exchangers according to the invention can be installed inside a double air distillation column whose low pressure column is superimposed on the medium pressure column.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)

Abstract

Liquid oxygen of a low pressure column forms a bath 5 at the top of a heat exchanger 2 of the type having plates defining vertical passages 17, 18. This liquid is predistributed along every other passage 17 by a series of apertures 27 formed for example in the plates, and then is uniformly distributed in a fine manner in the same passages by a packing 24 so as to form a continuous running liquid film. The gaseous nitrogen of a medium pressure column is introduced into the remaining passages 18 and condensed by heat exchange with the oxygen which is vaporized.

Description

La présence invention est relative à la vaporisation d'un liquide par échange de chaleur avec un deuxième fluide au moyen d'un échangeur de chaleur du type à plaques verticales. Elle s'applique en particulier aux installations de distillation de l'air.The present invention relates to the vaporization of a liquid by heat exchange with a second fluid by means of a heat exchanger of the type with vertical plates. It applies in particular to air distillation installations.

Dans les installations de distillation de l'air du type à double colonne, l'oxygène liquide qui se trouve en cuve de la colonne basse pression est vaporisé par échange de chaleur avec. l'azote gazeux prélevé en tête de la colonne moyenne pression. Pour une pression de fonctionnement donnée de la colonne basse pression, l'écart de température entre l'oxygène et l'azote rendu nécessaire par la structure de l'échangeur de chaleur impose la pression de fonctionnement de la colonne moyenne pression. Il est . donc souhaitable que cet écart de température soit le plus faible possible, afin de minimiser les dépenses liées à la compression de l'air à traiter injecté dans la colonne moyenne pression.In air distillation systems of the double column type, the liquid oxygen which is in the bottom of the low pressure column is vaporized by heat exchange with. nitrogen gas taken from the top of the medium pressure column. For a given operating pressure of the low pressure column, the temperature difference between oxygen and nitrogen made necessary by the structure of the heat exchanger imposes the operating pressure of the medium pressure column. It is . It is therefore desirable for this temperature difference to be as small as possible, in order to minimize the expenses linked to the compression of the air to be treated injected into the medium pressure column.

Pour atteindre ce but; on a proposé d'alimenter l'échangeur de chaleur en oxygène liquide par le haut, en assurant le ruissellement de ce liquide le long de tubes de grande longueur (jusqu'à 6 m environ).To reach this goal; it has been proposed to supply the heat exchanger with liquid oxygen from above, ensuring the flow of this liquid along very long tubes (up to approximately 6 m).

Des performances remarquables ont ainsi été obtenues du point de vue de l'échange de chaleur, mais ceci au prix de sérieuses difficultés technologiques. En effet, notamment lorsque des débits d'oxygène importants doivent être traités, il se pose des problèmes de réalisation d'une multitude de longs tubes résistant à la pression extérieure de l'azote, ainsi que d'autres problèmes liés à la présence de plaques d'extrémité en acier inoxydable de forte épaisseur.Remarkable performance has thus been obtained from the point of view of heat exchange, but this at the cost of serious technological difficulties. In fact, in particular when large oxygen flow rates have to be treated, problems arise in producing a multitude of long tubes resistant to the external pressure of nitrogen, as well as other problems linked to the presence of thick stainless steel end plates.

L'invention a pour but de fournir des moyens pour obtenir des performances d'échange de chaleur au moins aussi bonnes mais de façon plus fiable et plus économique.The invention aims to provide means for obtaining heat exchange performance at least as good but more reliably and more economically.

A cet effet, l'invention a pour objet un procédé pour vaporiser un liquide par échange de chaleur avec un deuxième fluide au moyen d'un échangeur de chaleur comprenant un corps parallélépipédique formé d'un assemblage de plaques verticales parallèles définissant entre elles une multitude de passages plats, procédé du type dans lequel on envoie le liquide dans un premier ensemble de passages et le deuxième fluide dans les passages restants, caractérisé en ce qu'on distribue le liquide en. deux stades à l'extrémité supérieure des passages dudit premier ensemble, sur toute la longueur horizontale de ceux-ci, les deux stades comprenant une prédistribution grossière du liquide sur toute la longueur des passages dudit premier ensemble, puis uné distribution fine sur toute la longueur de ces passages du liquide ainsi prédistribué. De préférence, le débit de liquide est adapté pour assurer en permanence la présence d'un film liquide sur pratiquement toute l'étendue de toutes les parois contenues dans chacun des passages dudit premier ensemble.To this end, the subject of the invention is a method for vaporizing a liquid by heat exchange with a second fluid by means of a heat exchanger comprising a parallelepipedic body formed by an assembly of parallel vertical plates defining between them a multitude of flat passages, method of the type in which the liquid is sent in a first set of passages and the second fluid in the remaining passages, characterized in that the liquid is distributed in. two stages at the upper end of the passages of said first set, over the entire horizontal length thereof, the two stages comprising a rough predistribution of the liquid over the entire length of the passages of said first assembly, then a fine distribution over the entire length of these passages of the liquid thus predistributed. Preferably, the liquid flow rate is adapted to permanently ensure the presence of a liquid film over practically the entire extent of all the walls contained in each of the passages of said first assembly.

L'invention a également pour objet un échangeur de chaleur destiné à la mise en oeuvre d'un tel procédé. Cet échangeur est caractérisé en ce qu'il comprend des moyens de prédistributioa du liquide débouchant sur des moyens de distribution fine du liquide disposés à l'extrémité supérieure de chacun des passages dudit premier ensemble.The invention also relates to a heat exchanger intended for the implementation of such a process. This exchanger is characterized in that it comprises means for predistributing the liquid leading to means for fine distribution of the liquid arranged at the upper end of each of the passages of said first assembly.

Dans un mode de réalisation particulièrement efficace de l'échangeur suivant l'invention, les moyens de prédistribution comprennent des ouvertures, notamment une rangée horizontale de trous, et des moyens de retenue pour former un bain de liquide au-dessus de ces ouvertures ; lesdits moyens de distribution fine peuvent comprendre un garnissage, ou bien, lorsque lesdites ouvertures sont ménagées dans les plaques de l'échangeur, une surface d'étalement des jets de liquide sortant de ces ouvertures.In a particularly effective embodiment of the exchanger according to the invention, the predistribution means comprise openings, in particular a horizontal row of holes, and retaining means for forming a bath of liquid above these openings; said fine distribution means may comprise a lining, or alternatively, when said openings are made in the plates of the exchanger, a surface for spreading the jets of liquid leaving these openings.

L'invention a encore pour objet une installation de distillation d'air du type à double colonne, dans laquelle le liquide de cuve de la colonne moyenne pression est mis en relation d'échange thermique avec le gaz de tête de la colonne basse pression au moyen d'un échangeur de chaleur tel que défini ci-dessus, cette installation comprenant des moyens d'alimentation pour fournir le liquide auxdits moyens de prédistribution; et des moyens d'alimentation en gaz des. passages dudit deuxième ensemble.The invention also relates to an air distillation installation of the double column type, in which the liquid from the bottom of the medium pressure column is brought into heat exchange relationship with the top gas of the low pressure column at means of a heat exchanger as defined above, this installation comprising supply means for supplying the liquid to said predistribution means; and means for supplying gas to the. passages of said second set.

Plusieurs exemples de mise en oeuvre de l'invention vont maintenant être décrits en regard des dessins annexés. Sur ces dessins :

  • - la figure 1 est un schéma partiel d'une installation de distillation d'air conforme à l'invention ;
  • - la figure 2 est une vue schématique partielle en perspective, avec arrachement, d'un échangeur de chaleur équipant l'installation de la figure 1 ;
  • - la figure 3 est une vue analogue d'une variante de l'échangeur de chaleur de la figure 2 ;
  • - les figures 4 et 5 représentent respectivement en perspective deux variantes d'un détail de l'échangeur de la figure 3 ;
  • - la figure 6 est une vue partielle en perspective, avec arrachements, d'un autre échangeur de chaleur conforme à l'invention ;
  • - le figure 7 est une vue schématique en coupe d'une partie d'un échangeur de chaleur suivant un autre mode de réalisation de l'invention ; et
  • - la figure 8 est une vue analogue d'une variance de l'échangeur de la figure 7.
Several examples of implementation of the invention will now be described with reference to the accompanying drawings. In these drawings:
  • - Figure 1 is a partial diagram of an air distillation installation according to the invention;
  • - Figure 2 is a partial schematic perspective view, with parts broken away, of a heat exchanger fitted to the installation of Figure 1;
  • - Figure 3 is a similar view of a variant of the heat exchanger of Figure 2;
  • - Figures 4 and 5 show respectively in perspective two variants of a detail of the exchanger of Figure 3;
  • - Figure 6 is a partial perspective view, with parts broken away, of another heat exchanger according to the invention;
  • - Figure 7 is a schematic sectional view of part of a heat exchanger according to another embodiment of the invention; and
  • FIG. 8 is a similar view of a variance of the exchanger of FIG. 7.

Dans les différents modes de réalisation qui vont être décrits ci-dessous, on désignera par les mêmes références les éléments identiques ou correspondants.In the various embodiments which will be described below, the same or corresponding elements will be designated by the same references.

La figure 1 illustre une possibilité d'implantation d'un échangeur de chaleur oxygène-azote dans une installation de distillation d'air du type à double colonne. Cette installation comprend une colonne moyenne pression 1 au bas de laquelle est injecté l'air à traiter, sous une pression de l'ordre de 6 bars absolus. La liquide enrichi en oxygène qui est recueilli en cuve de la colonne 1 est envoyé en reflux au milieu de la hauteur d'une deuxième colonne (non rearésentée), dite colonne basse pression, qui fonctionne légèrement au-dessus de la pression atmosphérique. L'azote gazeux qui se trouve en tête de la colonne 1 est mis en relation d'échange de chaleur avec l'oxygène liquide recueilli en cuve de la colonne basse pression ; l'azote condensé rasultant sert de reflux dans la colonne 1 et dans la colonne basse pression, tandis que l'oxygène vaporisé résultant est renvoyé au bas de la colonne basse pression.FIG. 1 illustrates a possibility of installing an oxygen-nitrogen heat exchanger in an air distillation installation of the double column type. This installation comprises a medium pressure column 1 at the bottom of which the air to be treated is injected, under a pressure of the order of 6 bars absolute. The oxygen-enriched liquid which is collected in the tank of column 1 is sent under reflux in the middle of the height of a second column (not rearranged), called the low pressure column, which operates slightly above atmospheric pressure. The nitrogen gas which is at the head of column 1 is brought into heat exchange relationship with the liquid oxygen collected in the bottom of the low pressure column; the condensed condensing nitrogen serves as reflux in column 1 and in the low pressure column, while the resulting vaporized oxygen is returned to the bottom of the low pressure column.

L'échange de chaleur entre l'oxygène et l'azote s'opère dans un échangeur 2 qui est monté au-dessus de la colonne 1, tandis que la colonne basse pression est juxtaposée à cette dernière.The heat exchange between oxygen and nitrogen takes place in an exchanger 2 which is mounted above the column 1, while the low pressure column is juxtaposed to the latter.

L'échangeur 2 est constitué d'une enveloppe étanche 3 dont l'essentiel de la hauteur contient un ensemble de plaques parallèles 4 de forme rectangulaire en aluminium, d'une longueur de l'ordre de 1 à 1,5 m et d'une hauteur de l'ordre de 3 à 6 m, entre lesquelles des ondes également en aluminium sont fixées par brasage.The exchanger 2 consists of a sealed envelope 3, the main height of which contains a set of parallel plates 4 of rectangular aluminum shape, with a length of the order of 1 to 1.5 m and a height of the order of 3 to 6 m, between which waves also made of aluminum are fixed by brazing.

L'espace situé au-dessus des plaques 4 renferme un bain d'oxygène liquide 5 alimenté par une conduite 6 provenant de la cuve de la colonne basse pression et munie d'une pompe (non représentée). Cette dernière peut être commandée par un régulateur du niveau du bain 5, que l'on a schématisé par un tube 6A de mesure de niveau, ou, en variante, par un régulateur de débit. Au sommet de l'échangeur 2 est prévue une conduite 7 de renvoi au bas de la colonne basse pression de l'oxygène vaporisé au-dessus du bain 5, résultant des entrées de chaleur au niveau de la pompe et des tuyauteries.The space located above the plates 4 contains a liquid oxygen bath 5 supplied by a line 6 coming from the tank of the low pressure column and provided with a pump (not shown). This the latter can be controlled by a bath level regulator 5, which is shown diagrammatically by a level measuring tube 6A, or, as a variant, by a flow regulator. At the top of the exchanger 2 is provided a pipe 7 for returning oxygen vaporized above the bath 5 to the bottom of the low pressure column, resulting from the heat inputs at the pump and the pipes.

L'ensemble de plaques 4 est alimenté à sa partie supérieure en azote gazeux par une boîte d'alimentation horizontale 8 qui communique par une conduite 9 avec la tête de la colonne moyenne pression 1. L'évacuation de l'azote condense s'effectue à la base des plaques 4 par une boîte collectrice horizontale 10 qui communique par une conduite 11 avec une rigole gardée 12 disposée en tête de la colonne 1. Sur la boîte 10 est piqué un tuyau 13 d'évacuation des gaz rares incondensables.The set of plates 4 is supplied at its upper part with gaseous nitrogen by a horizontal feed box 8 which communicates by a pipe 9 with the head of the medium pressure column 1. The evacuation of the condensed nitrogen takes place at the base of the plates 4 by a horizontal collecting box 10 which communicates by a pipe 11 with a guarded channel 12 disposed at the head of the column 1. On the box 10 is stuck a pipe 13 for discharging incondensable rare gases.

Une conduite 14 relie la cuve de la colonne basse pression à l'espace situé dans l'enveloppe 3 au-dessous des plaques 4. Cette conduite pénètre verticalement dans cet espace par le point bas de l'enveloppe 3, et son extrémité supérieure est surmontée d'un déflecteur conique 15. Du fond de l'enveloppe 3 part également une conduite 16 destinée à ramener en cuve de la colonne basse pression l'oxygène liquide en excès.A pipe 14 connects the tank of the low pressure column to the space located in the casing 3 below the plates 4. This pipe penetrates vertically into this space through the bottom point of the casing 3, and its upper end is surmounted by a conical deflector 15. From the bottom of the casing 3 also leaves a pipe 16 intended to return to the bottom of the low pressure column the excess liquid oxygen.

La structure de la partie active de l'échangeur 2, c'est-à-dire de l'ensemble de plaques 4, va maintenant être décrite en regard de la figure 2.The structure of the active part of the exchanger 2, that is to say of the set of plates 4, will now be described with reference to FIG. 2.

Dans cette région de l'échangeur, l'enveloppe 3 a une forme parallélépipédique. Les plaques 4 définissent une multitude .de passages destinés alternativement à l'écoulement de l'oxygène (passages 17) et à l'écoulement de l'azote (passages 18). Sur la majeure partie de leur hauteur, les passages 17 et 18 contiennent chacun une onde 19 constituée d'une tôle d'aluminium perforée ondulée à génératrices verticales.In this region of the exchanger, the casing 3 has a parallelepiped shape. The plates 4 define a multitude of passages intended alternately for the flow of oxygen (passages 17) and for the flow of nitrogen (passages 18). Over most of their height, the passages 17 and 18 each contain a wave 19 consisting of a corrugated perforated aluminum sheet with vertical generators.

Les ondes 19 des passages d'azote se terminent, en haut comme en bas, avant les ondes 19 des passages d'oxygène. En bas des plaques 4, ces ondes des passages 18 sont prolongées par des ondes obliques de collection d'azote (non représentées) qui aboutissent à l'encrée de la boîte collectrice 10. A leur extrémité supérieure, ces mêmes ondes 19 sont prolongées par des ondes obliques 20 de distribution d'azote qui débouchent à la sortie de la boîte d'alimentation 8. Au-dessus des ondes 20, les passages 18 d'azote sont fermés par des barres horizontales 21. Des barres analogues ferment l'extrémité inférieure des passages d'azote au-dessous des zones de collection de l'azote. Au-dessus des barres 21, chaque passage d'azote comporte un réservoir d'oxygène liquide 22 contenant une onde verticale 23 en tôle d'aluminium perforée, à génératrices verticales, dont l'épaisseur et le pas sont nettement supérieurs à ceux des ondes 19. Les ondes 23 ont uniquement une fonction d'entretoises entre les plaques 4, de façon à permettre l'assemblage de l'échangeur par une unique opération de brasage. Les réservoirs 22 sont ouverts vers le haut pour communiquer avec le bain d'oxygène liquide 5. Les ondes 19 des passages d'oxygène 17 s'étendent vers le bas jusqu'à l'extrémité inférieure des plaques 4, de sorte que ces passages sont ouverts vers le bas. Ces ondes s'étendent vers le haut jusqu'au bord supérieur des barres 21, puis sont prolongées par un garnissage 24. Ce dernier est constitué par une onde du type "serrated" qui est illustrée plus en détail sur la figure 6.The waves 19 of the nitrogen passages end, above and below, before the waves 19 of the oxygen passages. At the bottom of the plates 4, these waves of the passages 18 are extended by oblique waves of nitrogen collection (not shown) which lead to the inking of the manifold 10. At their upper end, these same waves 19 are extended by oblique waves 20 of nitrogen distribution which open at the outlet of the feed box 8. Above the waves 20, the nitrogen passages 18 are closed by horizontal bars 21. Similar bars close the lower end of the nitrogen passages below the nitrogen collection areas. Above the bars 21, each nitrogen passage comprises a liquid oxygen tank 22 containing a vertical wave 23 of perforated aluminum sheet, with vertical generators, the thickness and pitch of which are clearly greater than those of waves 19. The waves 23 have only a function of spacers between the plates 4, so as to allow the assembly of the exchanger by a single brazing operation. The tanks 22 are open upwards to communicate with the liquid oxygen bath 5. The waves 19 of the oxygen passages 17 extend downwards to the lower end of the plates 4, so that these passages are open down. These waves extend upwards to the upper edge of the bars 21, then are extended by a lining 24. The latter consists of a wave of the "serrated" type which is illustrated in more detail in FIG. 6.

-Comme on le voit sur cette figure 6, l'onde 24 est une tôle d'aluminium non perforée à génératrices horizontales (disposition dite en "hard way" par rapport à l'écoulement de l'oxygène liquide). A intervalles réguliers, chaque facette horizontale ou psaudo-horizontale 25 de l'onde 24 est pourvue d'un crevé 26 décalé vers le haut d'un quart de pas d'onde. La largeur des crevé 26, mesurée le long d'une génératrice de l'onde, est du même ordre que la distance qui sépare chacun d'eux des deux crevé adjacents situés sur la même facette 25.-As seen in this figure 6, the wave 24 is an unperforated aluminum sheet with horizontal generators (so-called "hard way" arrangement with respect to the flow of liquid oxygen). At regular intervals, each horizontal or psaudo-horizontal facet 25 of the wave 24 is provided with a puncture 26 offset upwards by a quarter of a wave step. The width of the punctures 26, measured along a generatrix of the wave, is of the same order as the distance which separates each of them from the two adjacent punctures situated on the same facet 25.

En revenant à la figure 2, chaque plaque 4 comporte, au-dessus du garnissage 24, une rangée horizontale de trous 27 disposés à intervalle régulier sur toute la longueur de l'échangeur, les trous des plaques successives étant disposés à la même hauteur mais en quinconce. En variante, ces trous pourraient d'ailleurs être prévus seulement dans une plaque sur deux. Juste au-dessus de ces trous, les passages d'oxygène sont fermés par des barres horizontales 28, disposées à l'extrémité supérieure des plaques 4. Pour éviter le risque d'obstruction de certains trous 27 par des ondes 23, celles-ci sont interrompues sur une courte hauteur au niveau desdits trous.Returning to FIG. 2, each plate 4 comprises, above the lining 24, a horizontal row of holes 27 arranged at regular intervals over the entire length of the exchanger, the holes of the successive plates being arranged at the same height but in a staggered arrangement. As a variant, these holes could moreover be provided only in every second plate. Just above these holes, the oxygen passages are closed by horizontal bars 28, arranged at the upper end of the plates 4. To avoid the risk of obstruction of certain holes 27 by waves 23, these are interrupted for a short height at the level of said holes.

En fonctionnement, le dispositif de régulation de la pompe d'alimentation de l'échangeur 2 en oxygène liquide maintient au-dessus des plaques 4 un niveau du bain 5 suffisant pour vaincre les diverses pertes de charge qui s'opposent à l'écoulement de l'oxygène. La hauteur d'oxygène liquide au-dessus des plaques 4 est par exemple de l'ordre de 20 cm.In operation, the regulating device of the pump for supplying the exchanger 2 with liquid oxygen maintains above the plates 4 a level of the bath 5 sufficient to overcome the various pressure drops which oppose the flow of oxygen. The height liquid oxygen above the plates 4 is for example of the order of 20 cm.

L'oxygène liquide remplit les réservoirs 22 et passe par les trous 27, à un débit défini par la section de passage de ces derniers et par la hauteur de liquide qui le surmonte. Comme cette hauteur est constante en régime établi, le débit d'oxygène liquide est celui fourni par la pompe de remontée de ce liquide. Les trous 27 assurent donc une prédistribution grossière de l'oxygène liquide tout le long des passages 17, et l'oxygène liquide ainsi pré-distribué parrient sur le garnissage 24, lequel en assure une distribution fine sur toute la longueur de chaque passage 17. L'oxygène liquide aborde ainsi les ondes 19 en ruisselant de façon parfaitement uniforme sur toutes les parois (ondes 19 et plaques 4) des passages qui lui sont affectés, c'est-à-dire en formant sur ces parois un film continu descendant.Liquid oxygen fills the reservoirs 22 and passes through the holes 27, at a flow rate defined by the passage section of the latter and by the height of liquid which overcomes it. As this height is constant in steady state, the flow of liquid oxygen is that supplied by the pump for raising this liquid. The holes 27 therefore provide a rough predistribution of the liquid oxygen along the passages 17, and the liquid oxygen thus pre-distributed appears on the lining 24, which ensures a fine distribution over the entire length of each passage 17. Liquid oxygen thus approaches waves 19 by flowing in a perfectly uniform manner over all the walls (waves 19 and plates 4) of the passages which are assigned to it, that is to say by forming on these walls a continuous descending film.

En même temps, l'azote gazeux parvient dans l'échangeur par la boite 8 et les ondes de distribution 20, puis s'écoule vers le bas le long des passages 18. Ce faisant, il cède progressivement de la chaleur à l'oxygène liquide qui se trouve dans les passages adjacents 17, de sorte que l'oxygène se vaporise et que, simultanément, l'azote se condense.At the same time, the nitrogen gas arrives in the exchanger through the box 8 and the distribution waves 20, then flows down along the passages 18. In so doing, it gradually gives off heat to the oxygen. liquid which is in the adjacent passages 17, so that the oxygen vaporizes and that, simultaneously, the nitrogen condenses.

L'azote condense est recueilli dans la boite 10 et s'écoule dans la conduite 11 jusque dans la rigole 12. Lorsque la hauteur d'azote liquide dans la conduite 11 est suffisante pour vaincre la pression qui règne dans la colonne moyenne pression 1, ce liquide déborde de la rigole et tombe en reflux dans la colonne moyenne pression après qu'une partie ait été prélevée par une conduite 11A pour assurer le reflux de la colonne basse pression. Il se crée ainsi une aspiration dans les passages 17, ce qui assure la circulation de l'azote.The condensed nitrogen is collected in the box 10 and flows in the pipe 11 as far as the channel 12. When the height of liquid nitrogen in the pipe 11 is sufficient to overcome the pressure prevailing in the medium pressure column 1, this liquid overflows from the channel and falls into reflux in the medium pressure column after a portion has been withdrawn through a pipe 11A to ensure the reflux of the low pressure column. This creates suction in the passages 17, which ensures the circulation of nitrogen.

La débit d'oxygène liquide est réglé de façon à garantir un excès d'oxygène liquide sur toute la hauteur des plaques 4. En effet, une vaporisation totale de l'oxygène dans une région des passages 17 conduirait à cet emplacement à une concentration de l'acétylène dissous dans l'oxygène liquide, ce qui pourrait provoquer une explosion locale. Indépendamment de ce risque d'explosion, il en résulterait aussi une baisse de performance de l'échangeur par neutralisation de la surface non mouillée. Ce risque est limité grâce à la grande efficacité de la distribution fine assurée par le garnissage 24. Cependant, par sécurité, on préfère travailler avec un excès d'oxygène liquide, généralement du même ordre que le débit d'oxygène vaporisé.The liquid oxygen flow rate is adjusted so as to guarantee an excess of liquid oxygen over the entire height of the plates 4. In fact, a total vaporization of the oxygen in a region of the passages 17 would lead to this location at a concentration of acetylene dissolved in liquid oxygen, which could cause a local explosion. Independently of this risk of explosion, it would also result in a drop in performance of the exchanger by neutralization of the non-wetted surface. This risk is limited thanks to the high efficiency of the fine distribution ensured by the lining 24. However, for safety, it is preferred to work with an excess of liquid oxygen, generally of the same order as the flow of vaporized oxygen.

Par conséquent, un mélange diphasique oxygène gazeux-oxygène liquide sort par l'extrémité inférieure des passages 17 ; ce mélange se sépare dans la partie inférieure de l'enveloppe 3, les phases liquide et vapeur retournant respectivement à la cuve de la colonne basse pression par les conduites 16 et 14.Consequently, a two-phase mixture of gaseous oxygen and liquid oxygen leaves through the lower end of the passages 17; this mixture separates in the lower part of the casing 3, the liquid and vapor phases returning respectively to the tank of the low pressure column by the lines 16 and 14.

La demanderesse a constaté qu'un tel échangeur peut fonctionner de façon parfaitement fiable avec un écart de température très faible, de l'ordre de 0,5 °C, entre l'azote et l'oxygène, ce qui permet par conséquent de comprimer l'air entrant dans l'installation de distillation dans des conditions très économiques.The Applicant has found that such an exchanger can function perfectly reliably with a very small temperature difference, of the order of 0.5 ° C., between nitrogen and oxygen, which consequently makes it possible to compress the air entering the distillation plant under very economical conditions.

Dans le mode de réalisation de la figure 2, on voit que la distribution de l'oxygène liquide est entièrement réalisée lorsque le fluide arrive dans la zone d'échange de chaleur avec l'azote. Dans la variante de la figure 3, au concraire, l'oxygène est mis en relation d'échange thermique avec l'azote dès le début de l'opération de distribution fine.In the embodiment of Figure 2, we see that the distribution of liquid oxygen is fully achieved when the fluid arrives in the heat exchange zone with nitrogen. In the variant of FIG. 3, in the concierge, the oxygen is put into heat exchange relation with the nitrogen from the start of the fine distribution operation.

Pour cela, les barres 21 qui limitent supérieurement les passages 18 sont disposées à l'extrémité supérieure des plaques 4, comme les barres 28. De plus, les trous 27 sont supprimés et remplacés par des trous verticaux 29 percés à intervalles réguliers dans les barres 28, tout le long de celles-ci.For this, the bars 21 which limit the upper passages 18 are arranged at the upper end of the plates 4, like the bars 28. In addition, the holes 27 are eliminated and replaced by vertical holes 29 drilled at regular intervals in the bars 28, all along these.

Dans cette variante, l'oxygène liquide du bain 5 s'écoula par les trous 29, à un débit correspondant à celui de la pompe de racontée de l'oxygène liquide, et est ainsi prédistribué sur toute la longueur des passages 17 ; ces liquides tombent alors sur le garnissage 24 situé juste au-dessous (ce garnissage a été représenté orès schématiquement sur la figure 3). Comme précédemment, le garnissage 24 assure une distribution fine uniforme de l'oxygène liquide sur toute la longueur des passages 17, et ce liquide ruisselle ensuite le long des ondes 19 et des parois 4 correspondantes. L'échange de chaleur entre l'oxygène et l'azote commence pendant le passage de l'oxygène liquide à travers les garnissages 24, lesquels se trouvent au même niveau que lés ondes 20 de distribution de l'azote gazeux.In this variant, the liquid oxygen in the bath 5 flows through the holes 29, at a flow rate corresponding to that of the liquid oxygen pump, and is thus predistributed over the entire length of the passages 17; these liquids then fall on the lining 24 located just below (this lining has been represented ores schematically in FIG. 3). As before, the lining 24 ensures a uniform fine distribution of the liquid oxygen over the entire length of the passages 17, and this liquid then flows along the waves 19 and the corresponding walls 4. The heat exchange between oxygen and nitrogen begins during the passage of liquid oxygen through the linings 24, which are at the same level as the nitrogen gas distribution waves.

Comme illustré à la figure 4, les trous 29 des barres 28, au lieu d'être d'un diamètre constant sur toute la hauteur de ces barres, peuvent avoir un diamètre élargi dans la plus grande partie de leur hauteur par un contre-alésage 29A réalisé à partir du bas.As illustrated in FIG. 4, the holes 29 of the bars 28, instead of being of a constant diameter over the entire height of these bars, can have an enlarged diameter in most of their height by a counter-bore 29A produced from the bottom.

La figure 5 montre que des trous analogues peuvent également être obtenus par perforation de l'âme supérieure 30 de profilés en U constituant les barres 28. L'avantage de ces deux réalisations réside dans le fait que la partie utile des trous 29, qui définie la section de passage de l'oxygène liquide, est de courte longueur et donc moins sujette à l'apparition de bouchages ou de vaporisation indésirable.FIG. 5 shows that similar holes can also be obtained by perforating the upper core 30 of U-shaped profiles constituting the bars 28. The advantage of these two embodiments lies in the fact that the useful part of the holes 29, which defines the liquid oxygen passage section is short and therefore less subject to the appearance of blockages or undesirable vaporization.

Dans les échangeurs de chaleur des figures 2 et 3, l'oxygène vaporisé s'évacue par le bas en même temps que l'oxygène liquide en excès. Dans le mode de réalisation de la figure 6, au contraire, l'oxygène vaporisé est libre de s'évacuer à la fois par le haut et par le bas.In the heat exchangers of Figures 2 and 3, the vaporized oxygen is evacuated from below at the same time as the excess liquid oxygen. In the embodiment of FIG. 6, on the contrary, the vaporized oxygen is free to escape both from the top and from the bottom.

L'échangeur de la figure 6 est identique à celui de la figure 2 du bas des plaques 4 jusqu'au niveau du bord supérieur des barres 21 qui limitent supérieurement les passages d'azote 18.The exchanger of FIG. 6 is identical to that of FIG. 2 from the bottom of the plates 4 to the level of the upper edge of the bars 21 which limit the nitrogen passages 18 above.

Jusce au-dessus de ces barres 21, chaque plaque 4 comporte une rangée horizontale de trous 31. Au-dessus de ceux-ci, les. plaques 4 s'étendent sur une hauteur importante, jusqu'à un niveau supérieur à celui de la surface libre du bain 5 d'oxygène liquide. Dans les intervalles situés au-dessus des barres 21 sont disposées des ondes - entretoises 32 à génératrices verticales analogues aux ondes 23 de la figure 2. Dans les intervalles restants,.un espace libre 33 est prévu au niveau des trous 31, au-dessus des ondes 19, et cet espace est surmonté, de bas en haut par le garnissage 24 précédemment décrit, par une barre 28 à trous 29 analogue à celles de la figure 3, et par une onde-entretoise 34 analogue aux ondes 32 mais à génératrices horizontales.Up to the top of these bars 21, each plate 4 has a horizontal row of holes 31. Above these, the. plates 4 extend over a significant height, up to a level higher than that of the free surface of the liquid oxygen bath 5. In the intervals located above the bars 21 are arranged waves - spacers 32 with vertical generators similar to the waves 23 in FIG. 2. In the remaining intervals, a free space 33 is provided at the holes 31, above waves 19, and this space is overcome, from bottom to top by the lining 24 previously described, by a bar 28 with holes 29 similar to those of FIG. 3, and by a wave-spacer 34 similar to waves 32 but with generators horizontal.

L'alimentation du bain 5 s'effectue latéralement par une boîte d'alimentation 35 située au-dessus de la boite 8 et débouchant dans les espaces occupés par les ondes 34. Pour cela, les barres 36 qui ferment de ce côté les passages 17 d'oxygène ne s'étendent vers le haut que jusqu'au niveau du bord supérieur des barres 28.The bath 5 is supplied laterally by a supply box 35 located above the box 8 and opening into the spaces occupied by the waves 34. For this, the bars 36 which close the passages 17 on this side of oxygen extend upward only up to the level of the upper edge of the bars 28.

En fonctionnement, on maintient dans la botte 35 un niveau d'oxygène liquide constant approprié. Le bain 5 surmonte les barres 28 et, comme à la figure 1, l'oxygène liquide s'écoule par les trous 29 dans le garnissage 24, qui le distribue uniformément de façon fine, puis ruisselle dans les passages 17 en échange de chaleur avec l'azote contenu dans les passages 18. L'oxygène vaporisé peut s'évacuer soit vers le bas, comme précédement, soit vers la haut en passant par les trous 31 et les espaces contenant les ondes 32, comme indiqué par des flèches sur la figure 6.In operation, an appropriate constant liquid oxygen level is maintained in the boot 35. The bath 5 overcomes the bars 28 and, as in FIG. 1, the liquid oxygen flows through the holes 29 in the lining 24, which distributes it uniformly in a fine manner, then trickles through the passages 17 in exchange for heat with the nitrogen contained in the passages 18. The vaporized oxygen can be evacuated either downwards, as above, either upwards through the holes 31 and the spaces containing the waves 32, as indicated by arrows in FIG. 6.

Dans ce mode de réalisation, on peut également, en variante, fermer les passages 17 à leur extrémité inférieure et recueillir l'oxygène liquide au moyen d'une onde oblique de collection et d'une boîte collectrice horizontale reliée par une conduite au bain d'oxygène liquide situé en cuve de la colonne basse pression. Dans ce cas, la totalité de l'oxygène vaporisé sort de l'échangeur par le haut, de la façon décrite ci-dessus.In this embodiment, it is also possible, as a variant, to close the passages 17 at their lower end and to collect the liquid oxygen by means of a collection oblique wave and a horizontal collecting box connected by a pipe to the bath. liquid oxygen located in the bottom of the low pressure column. In this case, all of the vaporized oxygen leaves the exchanger from above, as described above.

L'échangeur de chaleur illustré à la figure 7 ne diffère de celui de la figure 2 que par la manière dont l'oxygène est distribué et évacué. En effet, dans chaque passage 17, le garnissage 24 est supprimé ; les jets d'oxygène liquide 37 sortant des trous 27 frappent la plaque 4 en regard et s'étalent sur celle-ci. L'espacement et le diamètre de ces trous sont choisis de manière que les nappes d'allure parabolique ainsi formées se rejoignent en une nappe continue un peu au-dessus des ondes d'échange thermique 19. Ainsi, la prédistribution de l'oxygène est encore assurée par les trous 27, tandis que sa distribution fine est assurée par les plaques 4 elles-mêmes.The heat exchanger illustrated in FIG. 7 differs from that of FIG. 2 only in the way in which the oxygen is distributed and evacuated. In fact, in each passage 17, the lining 24 is eliminated; the jets of liquid oxygen 37 leaving the holes 27 strike the plate 4 opposite and spread over the latter. The spacing and the diameter of these holes are chosen so that the sheets of parabolic shape thus formed meet in a continuous sheet a little above the heat exchange waves 19. Thus, the predistribution of oxygen is still provided by the holes 27, while its fine distribution is provided by the plates 4 themselves.

Ce mode de distribution est particulièrement simple et présente l'avantage de ne pas créer d'obstacle important à l'évacuation de l'oxygène vaporisé par le haut des passages 17, comme représenté. L'extrémité inférieure des passages 17 peut alors être soit obturée et pourvue de moyens de collection de l'excès d'oxygène liquide, soit ouverte pour laisser également à l'oxygène gazeux la possibilité de s'évacuer par le bas.This distribution method is particularly simple and has the advantage of not creating a significant obstacle to the evacuation of the oxygen vaporized from the top of the passages 17, as shown. The lower end of the passages 17 can then be either closed and provided with means for collecting the excess liquid oxygen, or open to also allow the gaseous oxygen the possibility of being evacuated from below.

Pour améliorer l'étalement des jets d'oxygène liquide sur la plaque 4, on peut modifier localement l'état de surface de celle-ci, en particulier par striage, de préférence horizontal, at/ou prévoir un obstacle horizontal 38 en saillie sur cette plaque au-dessus des jets, comme représenté en trait interrompu. L'amélioration de l'étalement des jets permet, pour un débit donné, d'utiliser des trous 27 plus grands en plus petit nombre, ce qui réduit le risque de bouchage de ces trous par des particules en suspension dans le liquide.To improve the spreading of the liquid oxygen jets on the plate 4, it is possible to locally modify the surface state of the latter, in particular by streaking, preferably horizontal, at / or providing a horizontal obstacle 38 projecting from this plate above the jets, as shown in broken lines. The improvement in the spreading of the jets makes it possible, for a given flow rate, to use larger holes 27 in smaller numbers, which reduces the risk of these holes being blocked by particles suspended in the liquid.

En variante (figure 8), les zones d'étalement des jets peuvent être prévues sur des plaques supplémentaires 39 accolées aux plaques 4.As a variant (FIG. 8), the areas for spreading the jets can be provided on additional plates 39 attached to the plates 4.

La région de l'échangeur située au-dessus des barres 21 ne nécessite aucune onde. Pour l'assemblage de l'échangeur par brasage, on peut disposer dans cette région, entre les plaques 4, des cales d'épaisseur que l'on retire ensuite, les plaques 39 étant éventuellement rapportées ultérieurement. En variante, comme représenté, on peut utiliser comme entretoises des ondes 23 en tôle forte et à grand pas, ces ondes écant interrompues au niveau des trous 27 et dans les zones d'étalement des jets. A la figure 8, on a représenté dans les passages 17 une onde 23 en deux parties, respectivement au-dessus at au-dessous des trous 27, avec une zone striée 40 .en regard de ces trous et une autre zone striée 41 entre l'onde 23 et l'onde 19. Cette figure 8 moncre par ailleurs que de telles ondes 23 permettent la mise en place simultanée des plaques supplémentaires 39.The exchanger region located above the bars 21 does not require any waves. For the assembly of the exchanger by brazing, it is possible to have in this region, between the plates 4, shims which are then removed, the plates 39 possibly being added later. As a variant, as shown, waves 23 made of strong sheet metal and with large pitch can be used as spacers, these ecant waves interrupted at the level of the holes 27 and in the areas of spreading of the jets. In FIG. 8, there is shown in the passages 17 a wave 23 in two parts, respectively above and below the holes 27, with a striated zone 40. Opposite these holes and another striated zone 41 between the wave 23 and wave 19. This figure 8 also shows that such waves 23 allow the simultaneous installation of additional plates 39.

En variante, on peut prévoir des trous 27 dans toutes les plaques 4, avec bien entendu un décalage convenable, afin d'alimenter chaque passage 17 avec deux nappes d'oxygène liquide.As a variant, holes 27 can be provided in all the plates 4, with of course a suitable offset, in order to supply each passage 17 with two layers of liquid oxygen.

Dans chaque mode de réalisation de l'échangeur suivant l'invention, le circuit d'azote est classique. On peut donc le remplacer par d'autres types connus de circuits d'azote, notamment par ceux décrits dans le brevet FR. 78.20.757 de la demanderesse.In each embodiment of the exchanger according to the invention, the nitrogen circuit is conventional. It can therefore be replaced by other known types of nitrogen circuits, in particular by those described in the FR patent. 78.20.757 of the plaintiff.

Par ailleurs, un ou plusieurs échangeurs de chaleur suivant l'invention peuvent être installés à l'intérieur d'une double colonne de distillation d'air dont la colonne basse pression est superposée à la colonne moyenne pression.Furthermore, one or more heat exchangers according to the invention can be installed inside a double air distillation column whose low pressure column is superimposed on the medium pressure column.

Claims (26)

1. - Procédé pour vaporiser un liquide par échange de chaleur avec un deuxième fluide au moyen d'un échangeur de chaleur (2) comprenant un corps parallélépipédique formé d'un assemblage de plaques verticales parallèles (4) définissant entre elles une multitude de passages plats (17,18), procédé du type dans lequel on envoie le liquide dans un premier ensemble de passages (17) et le_ deuxième fluide dans les passages restants (18), caractérisé en ce qu'on distribue le liquide en deux stades à l'extrémité supérieure des passages (17) dudit premier ensemble, sur toute la longueur horizontale de ceux-ci, les deux stades comprenant une prédistribution grossière du liquide sur toute la longueur des passages (17) dudit premier ensemble, puis une distribution fine sur toute la longueur de ces passages du liquide ainsi prédistribué.1. - Method for vaporizing a liquid by heat exchange with a second fluid by means of a heat exchanger (2) comprising a parallelepipedic body formed by an assembly of parallel vertical plates (4) defining between them a multitude of passages dishes (17,18), process of the type in which the liquid is sent in a first set of passages (17) and the second fluid in the remaining passages (18), characterized in that the liquid is distributed in two stages at the upper end of the passages (17) of said first set, over the entire horizontal length thereof, the two stages comprising a rough predistribution of the liquid over the entire length of the passages (17) of said first set, then a fine distribution over the entire length of these passages of the liquid thus predistributed. 2. - Procédé salon la revendication 1, caractérisé en ce que le débit de liquide est adapté pour assurer en permanence la présence d'un film liquide sur pratiquement toute l'étendue de toutes les parois (4,19) contenues dans chacun des passages dudit premier ensemble (17).2. - Process according to claim 1, characterized in that the liquid flow rate is adapted to permanently ensure the presence of a liquid film over practically the entire extent of all the walls (4,19) contained in each of the passages of said first set (17). 3. - Procédé suivant l'une des revendications 1 et 2, caractérisé en ce qu'on oblige le gaz résultant de la vaporisacion du liquide ainsi que le liquide en excès à sortir de l'échangeur (2) par le bas.3. - Method according to one of claims 1 and 2, characterized in that the gas resulting from the vaporization of the liquid is forced as well as the excess liquid to exit the exchanger (2) from below. 4. - Procédé suivant l'une quelconque des revendications 1 à 3, caractérisé en ce qu'on prélève le liquide dans un bain (5) de liquide prévu au sommet de l'échangeur.4. - Method according to any one of claims 1 to 3, characterized in that the liquid is taken from a bath (5) of liquid provided at the top of the exchanger. 5. - Procédé suivant la revendication 4, caractérisé en ce que ledit bain de liquide est à niveau régulé.5. - Method according to claim 4, characterized in that said liquid bath is at regulated level. 6. - Procédé suivant l'une des revendications '4 et 5, caractérisé en ce qu'on met les passages (17) dudit premier ensemble en communication avec un espace libre situé au-dessus du bain (5) de liquide.6. - Method according to one of claims' 4 and 5, characterized in that the passages (17) of said first assembly are placed in communication with a free space located above the bath (5) of liquid. 7. - Procédé suivant l'une quelconque des revendications 1 à 6, caractérisé en ce qu'on envoie dans ledit premier ensemble de passages (17) un excès de liquide du même ordre que le débit de liquide vaporisé.7. - Method according to any one of claims 1 to 6, characterized in that sends in said first set of passages (17) an excess of liquid of the same order as the flow of vaporized liquid. 8. - Procédé suivant l'une quelconque des revendications 1 à 7, caractérisé en ce que le liquide est de l'oxygène liquide et le deuxième fluide de l'azote gazeux en cours de condensation.8. - Process according to any one of claims 1 to 7, characterized in that the liquid is liquid oxygen and the second fluid is nitrogen gas during condensation. 9. - Echangeur de chaleur pour la mise en oeuvre d'un procédé suivant l'une quelconque des revendications 1 à 8, caractérisa en ce qu'il comprend des moyens (21,27;23,29,29A) de prédistribution du liquide débouchant sur des moyens (24 ; 4 ; 40, 41) de distribution fine du liquide disposés à l'extrémité supérieure de chacun des passages (17) dudit premier ensemble.9. - Heat exchanger for implementing a method according to any one of claims 1 to 8, characterized in that it comprises means (21,27; 23,29,29A) for predistribution of the liquid leading to means (24; 4; 40, 41) for fine distribution of the liquid arranged at the upper end of each of the passages (17) of said first assembly. 10. - Echangeur de chaleur suivant la revendication 9, caractérisé en ce que les moyens de prédistribution comprennent des ouvertures (27 ; 29, 29A), notamment une rangée horizontale de trous, et des moyens de retenue (21, 28) pour former un bain de liquide (5) au-dessus de ces ouvertures.10. - Heat exchanger according to claim 9, characterized in that the predistribution means comprise openings (27; 29, 29A), in particular a horizontal row of holes, and retaining means (21, 28) to form a liquid bath (5) above these openings. 11. - Echangeur de chaleur suivant la revendication 10, caractérisé en ce que lesdits moyens de retenue comprennent des barres (21) limitant les passages (18) dudit deuxième ensemble à leur extrémité supérieure, à une certaine distance de l'extrémité supérieure des plaques verticales (4), lesdites ouvertures (27) étant percées dans les plaques au-dessus de ces barres.11. - Heat exchanger according to claim 10, characterized in that said retaining means comprise bars (21) limiting the passages (18) of said second set at their upper end, at a certain distance from the upper end of the plates vertical (4), said openings (27) being drilled in the plates above these bars. 12. - Echangeur de chaleur suivant la revendication 10, caractérisé en ce que lesdits moyens de retenue comprennent des barres (28) limitant les passages (17) dudit premier ensemble à leur extrémité supérieure, lesdites ouvertures (29, 29A) étant ménagées verticalement dans ces barres.12. - Heat exchanger according to claim 10, characterized in that said retaining means comprise bars (28) limiting the passages (17) of said first assembly at their upper end, said openings (29, 29A) being formed vertically in these bars. 13. - Echangeur de chaleur suivant la revendication 12, caractérisé en ce que chaque ouverture (29,29A) est constituée par un trou contre-alésé.13. - Heat exchanger according to claim 12, characterized in that each opening (29.29A) is constituted by a counter-bored hole. 14. - Echangeur de chaleur suivant la revendication 12, caractérisé en ce que chaque barre (28) est un profilé en U ouvert vers le bas et comportant dans son âme (30) une série de trous (29).14. - Heat exchanger according to claim 12, characterized in that each bar (28) is a U-shaped profile open downwards and comprising in its core (30) a series of holes (29). 15. - Echangeur de chaleur suivant l'une quelconque des revendications 10 à 14, pour la mise en oeuvre d'un procédé suivant la revendication 6, caractérisé en ce qu'il comprend des moyens (31) pour faire communiquer une région des passages (17) dudit premier ensemble située au-dessous des moyens de distribution fine (24) avec un espace libre situé au-dessus du bain (5).15. - Heat exchanger according to any one of claims 10 to 14, for the implementation of a method according to claim 6, characterized in that it comprises means (31) for communicating a region of the passages (17) of said first assembly located below the fine distribution means (24) with a free space located above the bath (5). 16. - Echangeur de chaleur suivant les revendications 12 et 15 prises ensemble, caractérisé en ce que les plaques (4) s'étendent jusqu'au- dessus du niveau du bain (5), en ce que des barres supplémentaires (21) limitent vers le haut les passages (18) dudit deuxième ensemble, et en ce que lesdits moyens de communication comprennent des ouvertures (31) ménagées dans les plaques (4) au-dessus de ces barres supplémentaires et au-dessous desdits moyens de distribution fine (24).16. - Heat exchanger according to claims 12 and 15 taken together, characterized in that the plates (4) extend up above the level of the bath (5), in that bars additional (21) limit upward the passages (18) of said second set, and in that said communication means comprise openings (31) formed in the plates (4) above these additional bars and below said fine distribution means (24). 17. - Echangeur de chaleur suivant l'une quelconque des revendications 9 à 16, caractérisé en ce que lesdits moyens de distribution fine (24) comprennent un garnissage.17. - Heat exchanger according to any one of claims 9 to 16, characterized in that said fine distribution means (24) comprise a lining. 18. - Echangeur de chaleur suivant la revendication 12, caractérisé en ce que le garnissage (24) est constitué par une onde à génératrices horizontales et à décalage vertical partiel.18. - Heat exchanger according to claim 12, characterized in that the lining (24) consists of a wave with horizontal generators and partial vertical offset. 19. - Echangeur de chaleur suivant la revendication 11, caractérisé en ce que lesdits moyens de distribution fine (4 ; 40, 41) comprennent une surface d'étalement des jets de liquide sortant desdites ouvertures (27).19. - Heat exchanger according to claim 11, characterized in that said fine distribution means (4; 40, 41) comprise a surface for spreading the jets of liquid leaving said openings (27). 20. - Echangeur de chaleur suivant la revendication 19, caractérisé en ce que ladite surface (40, 41) est striée, de préférence horizontalement.20. - Heat exchanger according to claim 19, characterized in that said surface (40, 41) is ridged, preferably horizontally. 21. - Echangeur de chaleur suivant la revendication 19, caractérisé en ce que ladite surface (4) porte un relief (38) situé au-dessus des jets.21. - Heat exchanger according to claim 19, characterized in that said surface (4) carries a relief (38) located above the jets. '22. - Echangeur de chaleur suivant l'une quelconque des revendications 9 à 21, caractérisé en ce que lesdits moyens de distribution fine (24) sont disposés au même niveau qu'un dispositif (20) de répartition du deuxième fluide dans les passages (18) dudit deuxième ensemble.'22. - Heat exchanger according to any one of claims 9 to 21, characterized in that said fine distribution means (24) are arranged at the same level as a device (20) for distributing the second fluid in the passages (18) of said second set. 23. - Echangeur de chaleur suivant l'une quelconque des revendications 9 à 21, caractérisé en ce que lesdits moyens de distribution fine (24 ; 4 ; 40, 41) sont disposés entièrement au-dessus d'un dispositif (20) de répartition du deuxième fluide dans les passages (18) dudit deuxième ensemble.23. - Heat exchanger according to any one of claims 9 to 21, characterized in that said fine distribution means (24; 4; 40, 41) are arranged entirely above a distribution device (20) of the second fluid in the passages (18) of said second assembly. 24. - Installation de séparation d'air par distillation, du type comprenant une première colonne de distillation (1) fonctionnant sous une pression relativement élevée, une deuxième colonne de distillation fonctionnant sous une pression relativement faible, et un échangeur de chaleur (2) permettant de mettre le liquide de cuve de la deuxième colonne en relation d'échange thermique avec le gaz de tête de la première colonne, caractérisée en ce que l'échangeur de chaleur est tel que défini dans l'une quelconque des revendications 9 à 23, et en ce que l'installation comprend des moyens d'alimentation (6, 6A ; 35) pour fournir le liquide auxdits moyens de prédistribution (21,27 ; 28,29,29A), et des moyens (8) d'alimentation en gaz des passages (18) dudit deuxième ensemble.24. - Installation for the separation of air by distillation, of the type comprising a first distillation column (1) operating under a relatively high pressure, a second distillation column operating under a relatively low pressure, and a heat exchanger (2) allowing the tank liquid of the second column to be in heat exchange relation with the top gas of the first column, characterized in that the heat exchanger is as defined in any one of claims 9 to 23, and in that the installation comprises supply means (6, 6A; 35) for supplying the liquid to said predistribution means (21,27; 28,29,29A), and means (8) for supplying gas to the passages (18) of said second set. 25. - Installation suivant la revendication 24, caractérisée en ce que lesdits moyens d'alimentation (6,6A;35) comprennent des moyens pour créer un bain (5) de liquide au sommet de l'échangeur (2).25. - Installation according to claim 24, characterized in that said supply means (6.6A; 35) comprise means for creating a bath (5) of liquid at the top of the exchanger (2). 26. - Installation suivant la revendication 25, caractérisée en ce que lesdits moyens d'alimentation (6,6A;35) comprennent des moyens (6A) de régulation du niveau dudit bain.26. - Installation according to claim 25, characterized in that said supply means (6,6A; 35) comprise means (6A) for regulating the level of said bath.
EP84401284A 1983-06-24 1984-06-21 Device for evaporating a liquid by heat exchange with a second fluid and air distillation unit comprising such a device Expired - Lifetime EP0130122B2 (en)

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FR8310472A FR2547898B1 (en) 1983-06-24 1983-06-24 METHOD AND DEVICE FOR VAPORIZING A LIQUID BY HEAT EXCHANGE WITH A SECOND FLUID, AND THEIR APPLICATION TO AN AIR DISTILLATION INSTALLATION

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FR2807826B1 (en) 2000-04-13 2002-06-14 Air Liquide BATH TYPE CONDENSER VAPORIZER
FR2793548A1 (en) 2000-07-21 2000-11-17 Air Liquide Plate vaporizer-condenser operating as a thermosiphon in which the exchange corrugations of the second passage are vertical and the exchange body has two inlet boxes spaced over its length
US6349566B1 (en) 2000-09-15 2002-02-26 Air Products And Chemicals, Inc. Dephlegmator system and process
FR2891901B1 (en) * 2005-10-06 2014-03-14 Air Liquide METHOD FOR VAPORIZATION AND / OR CONDENSATION IN A HEAT EXCHANGER
JP4704928B2 (en) * 2006-02-15 2011-06-22 大陽日酸株式会社 Heat exchange type distillation equipment
JP4818044B2 (en) * 2006-09-28 2011-11-16 三洋電機株式会社 Manufacturing method of heat exchanger
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FR2938904B1 (en) * 2008-11-24 2012-05-04 Air Liquide HEAT EXCHANGER
CN102650491B (en) * 2012-05-10 2013-10-16 西安交通大学 Plate-fin film type main cold liquid distributor for air separation
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CN105546935A (en) * 2016-02-05 2016-05-04 江苏建筑职业技术学院 Air separating membrane type main condensate liquid distributor
FR3065795B1 (en) 2017-04-27 2019-06-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude IMPROVED WAVE JUNCTION HEAT EXCHANGER, AIR SEPARATION INSTALLATION THEREFOR, AND METHOD FOR MANUFACTURING SUCH EXCHANGER
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EP0303492A3 (en) * 1987-08-14 1989-08-09 The BOC Group plc Liquefied gas boilers
US5014773A (en) * 1987-08-14 1991-05-14 The Boc Group Plc Liquefied gas boilers
EP0303492A2 (en) * 1987-08-14 1989-02-15 The BOC Group plc Liquefied gas boilers
FR2665755A1 (en) * 1990-08-07 1992-02-14 Air Liquide Apparatus for producing nitrogen
EP0501471A2 (en) * 1991-03-01 1992-09-02 Air Products And Chemicals, Inc. Boiling process and a heat exchanger for use in the process
EP0501471A3 (en) * 1991-03-01 1992-12-09 Air Products And Chemicals, Inc. Boiling process and a heat exchanger for use in the process
US5333683A (en) * 1991-12-11 1994-08-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Indirect heat exchanger
EP0546947A1 (en) * 1991-12-11 1993-06-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Indirect plate-type heat exchanger
FR2685071A1 (en) * 1991-12-11 1993-06-18 Air Liquide INDIRECT HEAT EXCHANGER OF PLATE TYPE.
EP0566435A1 (en) * 1992-04-17 1993-10-20 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Trickle heat-exchanger and an air destillation comprising such a heat-exchanger
US5321954A (en) * 1992-04-17 1994-06-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Streaming heat exchanger and apparatus for air distillation comprising such an exchanger
FR2690231A1 (en) * 1992-04-17 1993-10-22 Air Liquide Flow heat exchanger and air distillation installation comprising such an exchanger.
EP0695921A1 (en) * 1994-08-05 1996-02-07 Praxair Technology, Inc. Downflow plate and thin heat exchanger for cryogenic rectification
EP0699884A1 (en) 1994-08-29 1996-03-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen by cryogenic destillation
FR2774755A1 (en) * 1998-02-09 1999-08-13 Air Liquide PERFECTED BRAZED PLATE CONDENSER AND ITS APPLICATION TO DOUBLE AIR DISTILLATION COLUMNS
US6189338B1 (en) 1998-02-09 2001-02-20 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Brazed-plates condenser and its application to double air-distillation columns
EP1008826A1 (en) * 1998-12-07 2000-06-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Falling film vaporizer and air distillation plant
FR2786858A1 (en) 1998-12-07 2000-06-09 Air Liquide HEAT EXCHANGER
EP2508830A1 (en) * 2004-10-25 2012-10-10 ConocoPhillips Company Vertical heat exchanger configuration for lng facility
CN102792116B (en) * 2010-03-08 2015-04-08 乔治洛德方法研究和开发液化空气有限公司 Heat exchanger
WO2011110772A3 (en) * 2010-03-08 2011-11-10 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Heat exchanger
WO2011110772A2 (en) * 2010-03-08 2011-09-15 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Heat exchanger
CN102792116A (en) * 2010-03-08 2012-11-21 乔治洛德方法研究和开发液化空气有限公司 Heat exchanger
FR2957142A1 (en) * 2010-03-08 2011-09-09 Air Liquide HEAT EXCHANGER
EP3462119B1 (en) 2013-04-30 2021-03-31 Hamilton Sundstrand Corporation Integral heat exchanger distributor
WO2016124748A1 (en) 2015-02-06 2016-08-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Heat exchanger comprising a liquid-refrigerant distribution device
FR3032521A1 (en) * 2015-02-06 2016-08-12 Air Liquide HEAT EXCHANGER COMPRISING A REFRIGERANT LIQUID DISPENSING DEVICE
WO2016166473A1 (en) 2015-04-16 2016-10-20 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Heat exchanger comprising microstructure elements and separation unit comprising such a heat exchanger
FR3035202A1 (en) * 2015-04-16 2016-10-21 Air Liquide HEAT EXCHANGER HAVING MICROSTRUCTURE ELEMENTS AND A SEPARATION UNIT COMPRISING SUCH A HEAT EXCHANGER
CN107660265A (en) * 2015-04-16 2018-02-02 乔治洛德方法研究和开发液化空气有限公司 Heat exchanger including micro-structured component and the separative element for including this heat exchanger
CN105066745A (en) * 2015-08-03 2015-11-18 中冶焦耐工程技术有限公司 Condenser for acid steam
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Also Published As

Publication number Publication date
JPH0531042B2 (en) 1993-05-11
KR850000658A (en) 1985-02-28
CA1245627A (en) 1988-11-29
EP0130122B2 (en) 1994-04-06
ZA844598B (en) 1985-02-27
AU2956384A (en) 1985-01-31
FR2547898A1 (en) 1984-12-28
ES8600489A1 (en) 1985-09-16
BR8403038A (en) 1985-05-28
AU566656B2 (en) 1987-10-29
PT78780A (en) 1984-07-01
JPS6017601A (en) 1985-01-29
ES533634A0 (en) 1985-09-16
DE3474059D1 (en) 1988-10-20
IN160739B (en) 1987-08-01
EP0130122B1 (en) 1988-09-14
ATE37229T1 (en) 1988-09-15
US4599097A (en) 1986-07-08
FR2547898B1 (en) 1985-11-29

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