EP4062118B1 - Echangeur de chaleur avec agencement de dispositifs mélangeurs améliorant la distribution d'un mélange diphasique - Google Patents

Echangeur de chaleur avec agencement de dispositifs mélangeurs améliorant la distribution d'un mélange diphasique Download PDF

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Publication number
EP4062118B1
EP4062118B1 EP20804293.7A EP20804293A EP4062118B1 EP 4062118 B1 EP4062118 B1 EP 4062118B1 EP 20804293 A EP20804293 A EP 20804293A EP 4062118 B1 EP4062118 B1 EP 4062118B1
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EP
European Patent Office
Prior art keywords
longitudinal
passages
mixing device
exchanger
phase
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EP20804293.7A
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German (de)
English (en)
French (fr)
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EP4062118A1 (fr
Inventor
Marine ANDRICH
Paul Berhaut
Marc Wagner
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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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Publication of EP4062118A1 publication Critical patent/EP4062118A1/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
    • F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0214—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—Details of the cold heat exchange system
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F3/00—Plate-like or laminated elements; Assemblies of plate-like or laminated elements
    • F28F3/02—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations
    • F28F3/04—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being integral with the element
    • F28F3/048—Elements or assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with recesses, with corrugations the means being integral with the element in the form of ribs integral with the element or local variations in thickness of the element, e.g. grooves, microchannels
    • 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
    • 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

Definitions

  • the present invention relates to a heat exchanger comprising sets of passages for each of the fluids to be placed in a heat exchange relationship, the exchanger comprising an arrangement of mixing devices configured to distribute more homogeneously at least a mixture of two liquid phases -gas in at least one of the sets of passages.
  • the present invention can be applied to a heat exchanger which vaporizes at least a flow of liquid-gas mixture, in particular a flow of liquid-gas mixture with several constituents, for example a mixture comprising hydrocarbons, by exchange heat with at least one other fluid, for example natural gas, which cools, or even liquefies at least in part, or even liquefied natural gas which subcools.
  • a heat exchanger which vaporizes at least a flow of liquid-gas mixture, in particular a flow of liquid-gas mixture with several constituents, for example a mixture comprising hydrocarbons, by exchange heat with at least one other fluid, for example natural gas, which cools, or even liquefies at least in part, or even liquefied natural gas which subcools.
  • liquefying a stream of natural gas to obtain liquefied natural gas LNG
  • a refrigerant stream generally a mixture with several constituents, such as a mixture containing hydrocarbons, is compressed by a compressor then introduced into an exchanger or a succession of exchangers where it is completely liquefied and subcooled until the coldest temperature in the process, typically that of the liquefied natural gas stream.
  • the refrigerant stream is expanded, forming a liquid phase and a gaseous phase.
  • phase separator then reintroduced into the exchanger and remixed before being reintroduced in the liquid-gas mixture state, ie in the two-phase state, in the exchanger.
  • the refrigerant stream introduced in the two-phase state into the exchanger is vaporized there against the stream of hydrocarbons which liquefies and against the natural gas.
  • WO-A-2017081374 describes one of these known methods.
  • exchangers comprise a stack of plates which extend along two dimensions, length and width, thus constituting a stack of several sets of passages positioned on top of each other, some being intended for the circulation of a circulating fluid, for example the stream of hydrocarbons to be liquefied, others being intended for the circulation of a refrigerant fluid, for example the two-phase refrigerant stream to be vaporized.
  • Heat exchange structures such as heat exchange waves, are generally arranged in the passages of the exchanger. These structures comprise fins which extend between the plates of the exchanger and make it possible to increase the heat exchange surface of the exchanger. They also play the role of spacers and contribute to the mechanical strength of the passages.
  • the proportion of liquid phase and gas phase must be the same in all the passages and must be uniform within the same passage.
  • the sizing of the exchanger is calculated assuming a uniform distribution of the phases, and therefore a single temperature at the end of vaporization of the liquid phase, equal to the dew point temperature of the mixture.
  • the end of vaporization temperature will depend on the proportion of liquid phase and gaseous phase in the passages since the two phases do not have the same compositions.
  • the temperature profile of the first fluid will therefore vary according to the passages and/or within the same passage. Due to this non-uniform distribution, it may then happen that the fluid or fluids in exchange relationship with the two-phase mixture have a temperature at the outlet of the exchanger higher than that expected, which consequently degrades the performance of the the heat exchanger.
  • a problem which arises with this type of mixing device relates to the uneven distribution of the liquid-gas mixture in the width of the passages of the exchanger.
  • the two-phase mixture is distributed at the outlet of the channels opening into the passage.
  • the introduction of the liquid-gas mixture into the exchange zone takes place discreetly over the width of the passage.
  • a distribution can take place in the direction orthogonal to the overall direction of flow, in particular thanks to the waves of exchanges generally employed in this type of exchanger such as perforated waves or of the "serrated" type which tend to deviate part of the fluid from its direction of flow.
  • the homogenization of the distribution of fluid in the width of the exchanger is only achieved after a certain distance traveled by the mixture after the outlet of the mixing device. Over this distance, the fluid supplies the exchange zone with unequal mass flow rates depending on the position considered in the width of the exchanger. Certain channels of the exchange waves may be poorly supplied, or even not supplied. The performance of the exchanger is degraded. In some configurations, acceptable homogenization may not even be achieved. This is particularly the case when the exchange zone is provided with straight waves, with which a distribution by lateral deflection of the fluid is not possible.
  • the object of the present invention is to solve all or part of the problems mentioned above, in particular by proposing a heat exchanger ensuring a more homogeneous distribution of a two-phase mixture in the width of the exchanger.
  • natural gas relates to any composition containing hydrocarbons including at least methane.
  • Fig. 1 is a sectional view of a heat exchanger 1 comprising a stack of plates 2 (not visible) which extend along two dimensions, parallel to a plane defined by a longitudinal direction z and a lateral direction y.
  • the plates 2 are arranged parallel one above the other with spacing and thus form a superposition of passages for fluids in relation to indirect heat exchange via said plates.
  • each passage has a parallelepiped and flat shape.
  • the gap between two successive plates is small compared to the length, measured along the longitudinal direction z, and the width, measured along the lateral direction y, of each passage.
  • the exchanger 1 can comprise a number of plates greater than 20, or even greater than 100, defining between them a first set of first and second passages 10A, 10B (the passages 10B are not visible on Fig. 1 ) to channel at least a first fluid F1, and a second set of passages 20 (not visible on Fig. 1 ) to channel at least a second fluid F2, the flow of said fluids taking place generally in the direction z.
  • the passages 10A, 10B can be arranged, in whole or in part, alternately and/or adjacent to all or part of the passages 20.
  • the exchanger 1 can comprise a third set of passages, or even more, for the flow of one or more additional fluids. These sets of passages are superimposed on each other forming a stack of passages.
  • the sealing of the passages 10A, 10B, 20 along the edges of the plates 2 is generally ensured by lateral and longitudinal sealing strips 4 fixed to the plates 2.
  • the lateral sealing strips 4 do not completely block the passages 10A, 10B, 20 but advantageously leave fluid inlet and outlet openings located in the diagonally opposite corners of the passages.
  • the openings of the passages 10A, 10B of the first set are arranged in coincidence one above the other, while the openings of the passages 20 of the second set are arranged in the opposite corners.
  • the openings placed one above the other are united respectively in collectors of semi-tubular form 40, 45, 52, 55, by which the distribution and the evacuation of the fluids in and from the passages are carried out. 10A, 10B, 20.
  • fluid inlet and outlet configurations other than that according to Fig. 1 can be used.
  • the openings of the passages can thus be arranged at other positions in the width of the exchanger, in particular in the center of the width of the exchanger, and/or at other positions in the length of the exchanger.
  • the semi-tubular collectors 52 and 45 are used to introduce fluids into the exchanger 1 and the semi-tubular collectors 40, 55 are used to evacuate these fluids from the exchanger 1.
  • the supply manifold for one of the fluids and the discharge manifold for the other fluid are located at the same end of the exchanger, the fluids F1, F2 thus circulating in counter-current in exchanger 1.
  • the first and second fluids can also circulate in co-current, the means for supplying one of the fluids and the means for discharging the other fluid then being located at opposite ends of the exchanger 1.
  • the z direction is oriented vertically when the exchanger 1 is in operation.
  • the first fluid F1 generally flows vertically and in the upward direction.
  • Other directions and directions of flow of the fluids F1, F2 can of course be envisaged, without departing from the scope of the present invention.
  • one or more second fluids F2 of different natures can flow within the passages 20 of the second set.
  • the first fluid F1 is a refrigerant and the second fluid F2 is a circulating fluid.
  • the exchanger advantageously comprises distribution waves 51, 54, arranged between two successive plates 2 in the form of corrugated sheets, which extend from the inlet and outlet openings.
  • the distribution waves 51, 54 ensure the uniform distribution and recovery of fluids over the entire width of the passages 10A, 10B, 20.
  • the passages 10A, 10B, 20 advantageously comprise heat exchange structures arranged between the plates 2.
  • the function of these structures is to increase the heat exchange surface of the exchanger and to increase the coefficients of exchange between fluids by making the flows more turbulent.
  • the heat exchange structures are in contact with the fluids circulating in the passages and transfer heat flows by conduction to the adjacent plates 2, to which they can be fixed by brazing, which increases the mechanical resistance of the exchanger.
  • the heat exchange structures also have a function of spacers between the plates 2, in particular during the assembly by brazing of the exchanger and to avoid any deformation of the plates during the implementation of pressurized fluids. They also ensure the guiding of fluid flows in the passages of the exchanger.
  • these structures comprise heat exchange waves 11 which advantageously extend along the width and length of the passages 10A, 10B, 20, parallel to the plates 2, in the extension of the distribution waves along the length of the passages.
  • the passages 10A, 10B, 20 of the exchanger thus have a main part of their length constituting the heat exchange part itself, which is lined with a heat exchange structure, said main part being bordered by distribution parts lined with distribution waves 51, 54.
  • Fig. 1 shows a first passage 10A of the first assembly configured for the flow of a first fluid F1 in the form of a two-phase mixture, also called two-phase mixture.
  • the first set comprises several first passages 10A of this type as well as several second passages 10B superimposed on the first passages and of a structure similar to that of the first passages 10A.
  • the first fluid F1 is separated in a separator device 6 into a first phase 61 and a second phase 62 introduced separately into the exchanger 1 via a first manifold 30 and a second manifold 52 which are distinct.
  • the first phase 61 is liquid and the second phase 62 is gaseous.
  • the first and second phases 61, 62 are then mixed with each other by means of a first mixing device 3A arranged in at least one first passage 10A.
  • a first mixing device 3A arranged in at least one first passage 10A.
  • several first passages 10A, or even all of the passages 10A of the first set comprise a first mixing device 3A.
  • the first and second phases 61, 62 are mixed with each other by means of a second mixing device 3B arranged in at least one second passage 10B.
  • several second passages 10B, or even all of the passages 10B of the first set comprise a second mixing device 3B.
  • Semi-tubular collectors 52 and 55 are fluidically connected to the inlets and outlets of passages 10A and 10B.
  • the first collector 30 is fluidically connected to at least one first input 311A, 311B of each of the first and second mixing devices 3A, 3B.
  • the second collector 52 is fluidically connected to at least one second input 321A, 321B of each of the first and second mixing devices 3A, 3B.
  • Fig. 1 illustrates a mixing device 3A positioned at a certain distance from the distribution zone 51 of the exchanger 1.
  • the first mixing device 3A can be positioned directly after the distribution zone, either juxtaposed with said zone, or by being formed in one piece with the dispensing area.
  • the mixing device forms a monolithic part, which can be manufactured by conventional machining or by additive manufacturing, ie by 3D printing, for example by laser sintering.
  • Fig. 2 is a three-dimensional view of a first mixer device 3A advantageously consisting of a bar, or rod, housed in a first passage 10A.
  • the second mixer device 3B can have all or some of the characteristics described for the first device 3A.
  • the first mixing device 3A preferably extends in the section of the passage 10 over almost all, or even all, of the height of the first passage 10A, so that the mixing device is in contact with each plate 2 forming the first pass 10A.
  • the first mixing device 3A is advantageously fixed to the plates 2 by brazing.
  • the first mixing device 3A is advantageously of generally parallelepipedal shape.
  • the first mixing device 3A is a monolithic part, i. e. formed in one piece or in one piece.
  • the first mixing device 3A can be manufactured by conventional machining or by additive manufacturing.
  • the first mixer device 3A may have, parallel to the longitudinal direction z, a first dimension comprised between 20 and 200 mm and, parallel to the lateral direction y, a second dimension comprised between 100 and 1400 mm.
  • the first mixing device 3A comprises at least one side channel 31A configured for the flow of the first phase 61 of the first fluid F1 from at least one first inlet 311A.
  • the lateral channel 31A extends parallel to the lateral direction y.
  • It further comprises a series of longitudinal channels 32A extending parallel to the longitudinal direction z and configured for the flow of the second phase 62 of the first fluid F1 from a second inlet 321A to a second outlet 322A, said longitudinal channels being arranged at successive positions y i , y i+1 ,... in a lateral direction y.
  • the lateral channel 31A extends over the entire second dimension and/or the longitudinal channel 32A extends over the entire first dimension.
  • the mixer device 3A comprises at least a first inlet 311A in fluid communication with the first manifold 30 and a second inlet 321A, separate, ie distinct, from the first inlet 311A, in fluid communication with the second manifold 52.
  • the first collector 30 is fluidically connected to a first phase source 61 and the second collector 52 is fluidically connected to another second phase source 62.
  • Said at least one first inlet 311A and said at least one second inlet 321A are placed in fluid communication via at least one orifice 34.
  • the first and second inlets are advantageously formed by opening the side channels and longitudinal at the lateral and longitudinal peripheral edges of the devices 3A, 3B.
  • Fig. 2 shows an introduction of the first phase 61 by one end of the device 3A comprising several first inputs 311A.
  • the first mixer device 3A comprises at least one other first input for the first phase 61 located at an opposite end of the device 3A.
  • these other inlets are obtained by extending the side channels 31A, 31B until they emerge at an opposite side edge of the exchanger 1.
  • another first manifold 30 is arranged on a opposite side of the exchanger 1.
  • the introduction of the first phase 61 on either side of the mixing device makes it possible to reduce the effect of pressure drops during the flow of the first phase in the side channels, this which favors a more homogeneous distribution of the two-phase mixture over the width of the exchanger.
  • the first mixing device 3A comprises a mixing volume located in the longitudinal channel 32A, downstream of the orifice 34 following the flow direction of the first phase 61 in the orifice 34
  • the lateral channel 31A is fluidically connected to at least one longitudinal channel 32A so that, when the first phase 61 flows in the lateral channel 31A and the second phase 62 flows in the longitudinal channel 32A, the first mixing device 3A distributes through a second outlet 322A of channel 32A a mixture of the first phase 61 and of the second phase 62, preferably a two-phase liquid-gas mixture F1.
  • the longitudinal channel and/or the lateral channel have generally rectilinear shapes.
  • the channels 31A, 32A are advantageously in the form of longitudinal recesses formed in the mixer device 3. They are preferably open at the level of the upper 3a and lower 3b surfaces of the mixer device 3A.
  • the channels 31A, 32A have a cross-section of square or rectangular shape but may optionally have other shapes (round, round portion, etc.).
  • the orifices 34 are advantageously holes 34 made in the material of the device 3A and extending between the lateral channel 31A and the longitudinal channel 32A, preferably in the plane formed by the x and y directions, the orifices 34 being able to be inclined by relative to the x direction or, preferably, be aligned with the vertical x direction.
  • the orifices 34 are cylindrically symmetrical, more preferably cylindrical in shape.
  • said at least one lateral channel 31A comprises a bottom wall 3c and said at least one longitudinal channel 32A comprises a top wall 3d which extends opposite the bottom wall 3c, the orifices 34 being drilled in the bottom wall of the lateral channel 31 and opening into the top wall of the longitudinal channel 32A.
  • Fig. 3 is a view of the mixer device 3A of Fig. 2 in a section plane orthogonal to the lateral direction y and passing through the orifice 34.
  • the flow of the two-phase mixture of the first fluid F1 preferentially takes place along the longitudinal direction z, with a progressive expansion in the width of the passage.
  • the homogenization of the flows in each passage is only obtained beyond a certain distance traveled by the mixture. This lack of homogenization of the mixture F1 takes place throughout the stack of passages 10A, 10B of the first set.
  • the present invention proposes arranging respectively in a first passage 10A and in a second passage 10B of the first set, a first mixing device 3A and a second device 3B of different configuration with at least one part, preferably all of the longitudinal channels 32A of the first mixer device 3A positioned, along the lateral direction y, at positions different from those of the longitudinal channels 32B of the first mixer device 32B.
  • at least a part is meant one or more or all of the longitudinal channels 32A of the series.
  • the disparities in the flow rate of the mixture in the width of the exchanger are reduced, or even eliminated, after a shorter propagation distance of the mixture downstream of the mixing devices.
  • the heat exchanges between the two-phase mixture and the second fluid F2, and hence the operation of the exchanger, are improved.
  • the mechanical strength of the exchanger, during its brazing or in operation is improved.
  • the channels 32A and 32B are no longer positioned superimposed in the stack of the exchanger and the lack of material resulting from the channels 32A and 32B is better distributed, which stiffens the stack.
  • the thermal stresses are reduced due to a better distribution of the diphasic mixture seen by the second fluid.
  • the first set of passages for the flow of the two-phase mixture comprises several first passages 10A and several second passages 10B comprising first and second mixing devices configured according to the invention.
  • the first passages 10A and second passages 10B are advantageously positioned alternately within the stack of passages forming the exchanger.
  • At least one passage 20 of the second set is arranged between at least one first passage 10A and at least one second passage 10B consecutive to said at least one first passage 10A.
  • the stack of passages may have the following alternation pattern: first passage 10A, passage 20, second passage 10B, passage 20, first passage 10A, passage 20, etc. The number of refrigerant passages is thus minimized.
  • the stack of passages could have the following alternation pattern: first passage 10A, second passage 10B, passage 20, first passage 10A, second passage 10B, passage 20, ...
  • the present invention allows better homogenization of the overall cooling supply of the two-phase mixture to the second circulating fluid and therefore an improvement in the performance of the exchanger.
  • Fig. 4 And Fig. 5 represent embodiments of first and second device 3A, 3B according to the invention.
  • the devices 3A, 3B are shown side by side in the same plane but, in operation, they are arranged in separate passages 10A, 10B superimposed in the direction x, preferably they are located at the same position along the longitudinal direction z.
  • the positioning of the longitudinal channels 32A, 32B within the devices 3A, 3B is shown schematically by vertical lines.
  • the axis AA represents the longitudinal axis of symmetry of each passage 10A, 10B in the plane formed by the directions y and z.
  • Fig. 4 And Fig. 5 schematically represent the longitudinal channels in the form of lines.
  • the positions y i , y i+1 , y i+2 ... of each channel in the lateral direction y can be determined by considering the position of the center of each channel in the lateral direction y.
  • the position of a channel along the y direction corresponds to the position of the axis of symmetry of the channel located at an equal distance from the side walls of the channel, as seen in Fig. 2 .
  • the longitudinal channels 32A of the first mixer device 3A are separated from each other by a first constant distance D A and the longitudinal channels 32B of the second mixer device 3B are separated from each other by a second constant distance D B .
  • the distances D A , D B are measured parallel to the longitudinal direction y.
  • the first distance D A and the second distance D B are equal.
  • the first distance D A and/or the second distance D B can be between 10 and 40 mm, preferably greater than or equal to 20 mm and less than or equal to 30 mm.
  • the mixing devices 3A, 3B are each delimited by two longitudinal edges 3e.
  • the mixing devices 3A, 3B are dimensioned so as to cover at least partly, preferably completely, the longitudinal sealing strips 4 which ensure the sealing of the passages along the longitudinal direction z.
  • the mixing devices 3A, 3B thus have a useful width L y which is less than the distance between the two longitudinal edges 3e and which corresponds to the width of the mixing devices exposed to the fluid, that is to say the width of the passage 10A or 10B.
  • the mixing devices 3A, 3B have a useful zone of width L y which extends between two ends 81 and overlapping zones 80 which extend beyond the passages 10A, 10B and whose width advantageously corresponds to that of the strips side seals 4, as shown on Fig. 1 .
  • Such an arrangement ensures the rigidity of the stack and better mechanical strength of the brazed assembly.
  • each longitudinal channel 32A of the first mixing device 3A is inserted, in the lateral direction y, between two successive longitudinal channels 32B of the second mixing device 3B or between a longitudinal channel 32B and a third longitudinal edge of the second mixing device 3B.
  • a single longitudinal channel 32A of the first mixer device 3A is inserted, in the lateral direction y, between two successive longitudinal channels 32B of the second mixer device 3B or between a longitudinal channel 32B and a lateral edge 3e of the second mixer device 3B.
  • each pair of successive longitudinal channels 32B of the second mixer device 3B corresponds to a longitudinal channel 32A of the first mixer device 3A interposed between the channels of said pair, possibly with a longitudinal channel 32A of the first mixer device 3A interposed between a longitudinal channel 32B and a third side edge of the second mixing device 3B.
  • the series of longitudinal channels 32B of the second mixing device 3B is offset by a predetermined offset distance D y , measured in the lateral direction y, with respect to the series of longitudinal channels 32A of the first device 3A.
  • the offset distance D y represents between 25 and 75% of the first distance D A , preferably the offset distance D y is of the order of 50% of the first distance D A .
  • the expression “in order” means 50% or approximately 50%, with a variation of plus or minus 10% around this value.
  • the first and second mixing devices are of identical structure, one of the mixing devices being rotated through 180° relative to the other in the plane formed by the y and z directions before being mounted in its passage.
  • the advantage of this configuration is to only have to manufacture one type of mixing device, the different distribution of the longitudinal channels 32A, 32B being obtained by a simple reversal of the device in the plane formed by the directions y and z.
  • the distances D A and D B are equal and the offset D y is equal to half of D A .
  • the number of longitudinal channels 32A, 32B of the first and second mixer devices is identical.
  • the longitudinal channels 32A, 32B are arranged so that, for one of the mixing devices, the first longitudinal channel of the series is located at a distance D A from one end 81 of the useful zone and the last longitudinal channel 32A from the series is located at a distance D A /2 from the opposite end 81 of the useful zone, and vice versa for the other mixer device.
  • Fig. 5 represents a variant embodiment in which the longitudinal channels of the first and second passages 10A, 10B are arranged symmetrically with respect to the axis of symmetry AA of the exchanger.
  • the advantage of this configuration is to keep distribution points of the diphasic mixture distributed symmetrically across the width of the exchanger.
  • the distances D A and D B are equal and the offset D y is equal to half of D A .
  • One of the first and second mixing devices has an additional longitudinal channel relative to the other mixing device.
  • the longitudinal channels 32A, 32B are arranged so that, for one of the mixing devices, the first longitudinal channel and the last longitudinal channel 32A of the series are located at a distance D A from each opposite end 81 of the useful zone.
  • the first longitudinal channel and the last longitudinal channel of the series are located at a distance D A /2 from the opposite ends 81 of the useful zone.
  • the useful width L y of the mixing devices is a multiple of the distance D A .
  • the first and second mixer devices 3A, 3B are arranged in their respective passages 10A, 10B so that their lower surfaces 3b at which their longitudinal channels 32A, 32B open out are all oriented in the vertical direction x or, as illustrated in particular on Fig. 3 , are all oriented in a direction opposite to the vertical direction x.
  • At least one of the first mixing devices 3A has a lower surface 3b oriented in an opposite direction with respect to the orientation direction of the lower surface 3b of at least one second mixing device 3B and/or d at least one other first mixing device 3A, that is to say that at least one first mixing device is turned over, before being arranged in its passage, 180° around an axis parallel to the y direction.
  • This makes it possible to direct the flow of the two-phase mixture towards certain adjacent passages 20 of the second set in order to favor a heat exchange with certain calorigenic fluids rather than others. It is for example possible to envisage an alternation of orientation of the lower surfaces 3b of the first and second mixing devices succeeding each other in the stack of passages.
  • the longitudinal channels of the additional mixing devices are arranged, in the lateral direction y, at positions different from those of the first and second mixing devices.
  • the exchanger would comprise a third mixing device 3C with longitudinal channels 32C, longitudinal channels of the first mixing device 3A and of the second mixing device 3B being intercalated, in the lateral direction y, between two successive longitudinal channels 32C of the third device or between a longitudinal channel 32C and a longitudinal edge of the third device 3C.
  • FIG. 6 shows the results of simulations of the propagation of a two-phase mixture in an exchanger comprising a conventional arrangement of passages with the same type of mixing devices (configuration A), and an arrangement of passages with first and second mixing devices configured according to the invention (configuration B).
  • each pass of the first set comprised a mixing device in the form of a grooved bar comprising, as longitudinal channels, a series of parallelepiped-shaped grooves succeeding each other at regular intervals of 30 mm and, as lateral channels, a series of parallelepiped-shaped grooves fluidly connected to the longitudinal channels by a single orifice per longitudinal channel.
  • the geometry of the orifices was identical for all the longitudinal channels.
  • the longitudinal channels of each mixer device were arranged in the same number and at identical positions y i , y i+1 ,... in the lateral direction y.
  • first and second mixing devices were arranged alternately in the passages of the first set of passages of the exchanger.
  • “serrated” type waves i. e. partially offset, were arranged at the output of the mixing devices in each passage.
  • An assumption of the simulation being that the mixing flow was divided into two equal parts at each change in the serration of the waves.
  • Fig. 6 shows the scaled mass flow rates obtained along the lateral direction y and this at a propagation distance of 200 mm, along the longitudinal direction z, after the exit from the longitudinal channels and by averaging the flow rates over all the passages of the first set of the exchanger. It can be seen that the amplitude of the flow variation across the width of the exchanger is reduced in configuration B according to the invention.
  • Fig. 7 And Fig. 8 show examples of processes using one or more exchangers according to the invention.
  • Fig. 7 diagrams a process for liquefying a stream of hydrocarbons 102 as second fluid F2, which may be natural gas, optionally pre-treated, for example having undergone separation of at least one of the following constituents: water, carbon dioxide carbon, sulfur compounds, methanol, mercury, before its introduction into heat exchanger 1.
  • the hydrocarbon stream comprises, in molar fraction, at least 60% methane, preferably at least 80%.
  • the hydrocarbon stream 102 and the coolant stream 202 enter the exchanger 1 respectively via a third inlet 25 and a fourth inlet 21 to circulate therein in dedicated passages of the exchanger according to directions parallel to the longitudinal direction z, which is substantially vertical in operation.
  • the flow of hydrocarbons 102 circulates in the passages 20 of the second set supplied by the third inlet 25.
  • the refrigerant stream 202 circulates in a third set of passages arranged within the stack forming the exchanger 1. These streams come out via a third outlet 22 and a first outlet 23.
  • the passages of the second and third sets are arranged, in whole or in part, alternately and/or adjacent to all or part of the passages 10A, 10B of the first set.
  • the fourth inlet 21 for the coolant stream 202 and the third inlet 25 for the hydrocarbon stream 102 are arranged so that the coolant stream 202, and optionally the hydrocarbon stream 102, flow co-currently in the downward direction, towards a second end 1b of the exchanger which is located at a level lower than that of a first end 1a of said exchanger.
  • the first end 1a corresponds to the hot end of the exchanger 1, i. e. the entry point of the exchanger where a fluid is introduced at the highest temperature of the temperatures of the exchanger, this entry point possibly being the fourth entry 21 or the third entry 25 according to the method.
  • the hydrocarbon stream 102 can be introduced into the exchanger 1 at a temperature between -130 and 40°C.
  • the stream of hydrocarbons 102 is introduced in the completely gaseous or partially liquefied state into the exchanger 1 at a temperature between -80 and -35°C.
  • the stream of hydrocarbons 102 is introduced completely liquefied into the exchanger 1 at a temperature between -130 and -100°C.
  • the refrigerant stream 201 leaving the exchanger 1 is expanded by an expansion device T3, such as a turbine, a valve or a combination of a turbine and a valve, so as to form a two-phase refrigerant stream 203 comprising a phase liquid and a gas phase.
  • the two-phase refrigerant stream 203 forms the first fluid F1 considered above.
  • At least part of the two-phase refrigerant stream 203 resulting from the expansion is introduced into a separator member 27.
  • the separator member can be any device suitable for separating a two-phase fluid into a gas stream on the one hand and a liquid stream on the other. go.
  • the gaseous phase 62 is introduced through the manifold 52 which supplies the second inlets 321A, 321B of the first and second mixing devices 3A, 3B arranged in the first and second passages 10A, 10B of the first set.
  • the liquid phase 61 is introduced by the first collector 30 which supplies the first inlets 311A, 311B of the first and second mixer devices 3A, 3B (not illustrated on Fig. 7 ).
  • the gaseous phase is introduced through an inlet located in the region of the second end 1b corresponding to the cold end of the exchanger 1, i. e. the point of entry into the exchanger where a fluid is introduced at the lowest temperature of the temperatures of the fluids in the exchanger.
  • the two phases 61, 62 of the two-phase current 203 are recombined within the exchanger 1 and distributed in the state of liquid-gas mixture in the first 10A and second 10B passages of the exchanger 1 provided respectively with first 3A and second 3B mixing devices according to the invention.
  • the two-phase refrigerant stream 203 is introduced into the heat exchanger 1 at a first temperature T1 between -120 and -160 ° C and leaves the heat exchanger 1 at a second temperature T2 higher than the first temperature T1, preferably with T2 between -35 and -130°C.
  • the two-phase refrigerant stream 203 is introduced into the heat exchanger 1 at a first temperature T1 comprised between -130 and -80° C. and leaves the heat exchanger 1 at a second temperature T2 higher than the first temperature T1, preferably with T2 between -10 and 50°C.
  • Said at least part of the two-phase refrigerant stream 203 flows in the passages 10A, 10B in the upward direction and is vaporized by counter-current cooling the natural gas 102 and the refrigerant stream 202. A cooled hydrocarbon stream is thus obtained. and/or at least partially liquefied 101 at the outlet of exchanger 1.
  • the vaporized refrigerant stream leaves the exchanger 1 through a second outlet 42 connected to the manifold 55 to be compressed by a compressor and then cooled in an indirect heat exchanger by heat exchange with an external cooling fluid, for example water. or air (in 26 on Fig. 1 ).
  • the pressure of the refrigerant stream at the outlet of the compressor can be between 2 MPa and 9 MPa.
  • the temperature of the refrigerant stream leaving the indirect heat exchanger can be between 10°C and 45°C.
  • the refrigerant stream is not split into separate fractions, but, to optimize the approach in the exchanger 1, the refrigerant stream can also be split into two or three fractions, each fraction being expanded to a different pressure level and then sent to different compressor stages.
  • the coolant stream 202 contains hydrocarbons having a number of carbon atoms of at most 5, preferably at most three, more preferably at most two.
  • the coolant stream 202 is formed for example by a mixture of hydrocarbons and nitrogen such as a mixture of methane, ethane and nitrogen but can also contain propane, butane, isobutane , n-butane, pentane, isopentane, n-pentane and/or ethylene.
  • nitrogen such as a mixture of methane, ethane and nitrogen but can also contain propane, butane, isobutane , n-butane, pentane, isopentane, n-pentane and/or ethylene.
  • the refrigerant stream may comprise, replacing ethane, ethylene and, replacing all or part of the propane, compounds of the C4, C5 type.
  • the natural gas leaves at least partially liquefied 101 from the exchanger 1 at a temperature preferably higher by at least 10° C. with respect to the bubble temperature of the liquefied natural gas produced at atmospheric pressure (the bubble temperature refers to the temperature at which the first vapor bubbles form in a liquid natural gas at a given pressure) and at a pressure identical to the natural gas inlet pressure, except for pressure drops.
  • the natural gas leaves the exchanger 1 at a temperature between -100° C. and -162° C. and at a pressure between 2 MPa and 7 MPa. Under these temperature and pressure conditions, and depending on its composition, natural gas generally does not remain liquid after expansion to atmospheric pressure.
  • the process for liquefying a hydrocarbon stream according to the invention can implement one or more additional refrigeration cycles carried out upstream of the main refrigeration cycle described above, so as to pre-cool the hydrocarbon stream.
  • Fig. 8 diagrams a process for the liquefaction of a hydrocarbon stream such as natural gas comprising an additional refrigeration cycle in which the natural gas is cooled to a temperature close to its dew point using at least two different levels of relaxation to increase cycle efficiency.
  • This additional refrigeration cycle is operated by means of an additional refrigerant stream 300 in an additional heat exchanger 2, called pre-cooling exchanger, arranged upstream of the heat exchanger 1 in the direction of the current flow. of hydrocarbons 110, which then forms the liquefaction exchanger.
  • a feed stream 110 arrives for example at a pressure comprised between 2.5 MPa and 7 MPa and at a temperature comprised between 20°C and 60°C.
  • the feed stream 110 comprising a mixture of hydrocarbons such as natural gas, the refrigerant stream 202, an additional refrigerant stream 300 enter the additional exchanger 2 to circulate therein in parallel directions and in co-current in the direction descending.
  • the hydrocarbon stream 102 leaves in the gaseous or partially liquefied state, for example at a temperature between between -35°C and -70°C.
  • the refrigerant stream 202 can also leave the exchanger 2 completely condensed, for example at a temperature between -35°C and -70°C.
  • Stream 102 is then introduced into exchanger 1.
  • stream 203 is vaporized in exchanger 1 and leaves it to be compressed by compressor K2 and then cooled in indirect heat exchanger C2 by heat exchange with an external cooling fluid, for example water or the air.
  • the refrigerant stream from exchanger C2 is then returned to additional exchanger 2.
  • the additional exchanger 2 which is also of the brazed plate and fin type, at least two partial streams from the additional refrigerant stream 300 are withdrawn from the exchanger at at least two separate outlet points and then expanded to pressure levels different, giving rise to two-phase relaxed partial currents each comprising a liquid phase and a gaseous phase. At least a part of these diphasic partial currents is introduced into respective separator members 24, 25, 26.
  • the gaseous and liquid phases separated by each separator member are introduced through separate inlets of the additional exchanger 2 and recombined within mixing devices (not shown) so as to form at least two refrigerants introduced in the liquid mixture state -gas in dedicated refrigerant passages.
  • mixing devices not shown
  • only the liquid phase is injected into the exchanger 2 and the gas phase is directed towards the inlet of the compression stages of the compressor K1.
  • These refrigerants are vaporized in the additional exchanger 2 by heat exchange with the feed stream 110 and the refrigerant stream 200 and the additional refrigerant stream 300.
  • the additional exchanger 2 comprises at least two refrigerant passages each comprising a mixing device, these devices comprising one or more of the characteristics previously described for the first and second mixing devices 3A, 3B.
  • the refrigerants vaporized in their respective refrigerant passages are sent to different stages of the compressor K1, compressed and then condensed in a condenser by heat exchange with an external cooling fluid, for example water or air.
  • the stream from the condenser is returned to the additional exchanger 2.
  • the pressure of the first refrigerant stream at the outlet of the compressor K1 can be between 2 MPa and 6 MPa.
  • the temperature of the additional refrigerant stream at the outlet of condenser C1 can be between 10°C and 45°C.
  • the refrigerants flow from one end 2b of the additional exchanger 2 to another end 2a in the longitudinal direction z, in the upward direction.
  • End 2b corresponds to the cold end of additional exchanger 2 where the refrigerant is introduced at the lowest temperature of the temperatures of additional exchanger 2.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP20804293.7A 2019-11-21 2020-11-16 Echangeur de chaleur avec agencement de dispositifs mélangeurs améliorant la distribution d'un mélange diphasique Active EP4062118B1 (fr)

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FR1913017A FR3103543B1 (fr) 2019-11-21 2019-11-21 Echangeur de chaleur avec agencement de dispositifs mélangeurs améliorant la distribution d’un mélange diphasique
PCT/EP2020/082300 WO2021099275A1 (fr) 2019-11-21 2020-11-16 Echangeur de chaleur avec agencement de dispositifs mélangeurs améliorant la distribution d'un mélange diphasique

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DE3415807A1 (de) 1984-04-27 1985-10-31 Linde Ag, 6200 Wiesbaden Waermetauscher
FR2751059B1 (fr) * 1996-07-12 1998-09-25 Gaz De France Procede et installation perfectionnes de refroidissement, en particulier pour la liquefaction de gaz naturel
US7163051B2 (en) * 2003-08-28 2007-01-16 Praxair Technology, Inc. Heat exchanger distributor for multicomponent heat exchange fluid
DE102008052875A1 (de) * 2008-10-23 2010-04-29 Linde Ag Plattenwärmetauscher
FR3043451B1 (fr) 2015-11-10 2019-12-20 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Methode pour optimiser la liquefaction de gaz naturel
FR3053452B1 (fr) * 2016-07-01 2018-07-13 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Echangeur de chaleur comprenant un dispositif de distribution d'un melange liquide/gaz
JP6718806B2 (ja) * 2016-12-14 2020-07-08 株式会社神戸製鋼所 流体流通装置
FR3060721B1 (fr) * 2016-12-16 2019-08-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Echangeur de chaleur avec dispositif melangeur liquide/gaz a geometrie de canal amelioree
FR3060729A1 (fr) * 2016-12-16 2018-06-22 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Echangeur de chaleur avec dispositif melangeur liquide/gaz a canal isolant thermique
FR3064346B1 (fr) 2017-03-24 2019-03-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Echangeur de chaleur avec dispositif melangeur liquide/gaz a portion de canal regulatrice
FR3064345B1 (fr) * 2017-03-24 2019-03-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Echangeur de chaleur avec dispositif melangeur liquide/gaz a orifices de forme amelioree
JP6623244B2 (ja) * 2018-03-13 2019-12-18 株式会社神戸製鋼所 再液化装置
US11098829B2 (en) 2018-10-03 2021-08-24 Cantex International, Inc. Swivel joint
CN111989556B (zh) 2018-10-26 2022-05-10 富士电机株式会社 压力传感器

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US20230003447A1 (en) 2023-01-05
EP4062118A1 (fr) 2022-09-28
CN114829864A (zh) 2022-07-29
US12018887B2 (en) 2024-06-25
FR3103543B1 (fr) 2021-10-22
JP2023503815A (ja) 2023-02-01
FR3103543A1 (fr) 2021-05-28

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