EP4078065B1 - Mischvorrichtung zur förderung einer homogenen verteilung einer zweiphasenmischung, wärmetauscheinrichtung und zugehöriges mischverfahren - Google Patents

Mischvorrichtung zur förderung einer homogenen verteilung einer zweiphasenmischung, wärmetauscheinrichtung und zugehöriges mischverfahren

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Publication number
EP4078065B1
EP4078065B1 EP20817018.3A EP20817018A EP4078065B1 EP 4078065 B1 EP4078065 B1 EP 4078065B1 EP 20817018 A EP20817018 A EP 20817018A EP 4078065 B1 EP4078065 B1 EP 4078065B1
Authority
EP
European Patent Office
Prior art keywords
phase
longitudinal
fluid
channel
mixing device
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.)
Active
Application number
EP20817018.3A
Other languages
English (en)
French (fr)
Other versions
EP4078065A1 (de
Inventor
Marine ANDRICH
Paul Berhaut
Marc Wagner
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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Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP4078065A1 publication Critical patent/EP4078065A1/de
Application granted granted Critical
Publication of EP4078065B1 publication Critical patent/EP4078065B1/de
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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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
    • 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
    • F25J1/0214—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
    • 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
    • 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
    • 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
    • F28F9/0278—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits in the form of stacked distribution plates or perforated plates arranged over end plates
    • 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
    • F28F9/028—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits by using inserts for modifying the pattern of flow inside the header box, e.g. by using flow restrictors or permeable bodies or blocks with channels
    • 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
    • F28F9/0282—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits by varying the geometry of conduit ends, e.g. by using inserts or attachments for modifying the pattern of flow at the conduit inlet or outlet
    • 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
    • F28F9/22—Arrangements for directing heat-exchange media into successive compartments, e.g. arrangements of guide plates
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/18—External refrigeration with incorporated cascade loop
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
    • 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

Definitions

  • the present invention relates to a mixing device for distributing a mixture of two liquid/gas phases more homogeneously in at least one passage of a heat exchanger as well as a heat exchange installation comprising such a mixing device.
  • the present invention can be applied to a heat exchanger which vaporizes at least one flow of liquid-gas mixture, in particular a flow of liquid-gas mixture with several constituents, for example a mixture comprising hydrocarbons, by heat exchange 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 one flow of liquid-gas mixture, in particular a flow of liquid-gas mixture with several constituents, for example a mixture comprising hydrocarbons, by heat exchange 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 natural gas stream to obtain liquefied natural gas LNG
  • a refrigerant stream generally a mixture of several constituents, such as a mixture containing hydrocarbons, is compressed by a compressor and then introduced into an exchanger or a succession of exchangers where it is completely liquefied and sub-cooled to the coldest temperature of the process reached by the fluids which are cooled, typically that of the liquefied natural gas stream.
  • the refrigerant stream is expanded to form a first phase and a second phase.
  • brazed plate and fin aluminum exchangers makes it possible to obtain very compact devices offering a large exchange surface, which improves the energy performance of the process, and this in a limited volume.
  • the sizing of the exchanger is calculated assuming a uniform distribution of the phases, and therefore a single end of vaporization temperature of the liquid phase per passage, equal to the dew point temperature of the mixture.
  • the end of vaporization temperature will depend on the proportion of liquid phase and gas phase in the passages given that the two phases do not have the same compositions.
  • This mixing device comprises a series of separate channels or grooves for the flow of the liquid phase of the refrigerant and another series of separate channels for the flow of the gaseous phase of the refrigerant.
  • the channels of one series are fluidically connected to channels of the other series by orifices so that a liquid-gas mixture, i.e. a two-phase flow, is distributed at the outlet of the mixing device to the heat exchange zone.
  • Each refrigerant passage of the exchanger is provided with such a device.
  • a problem that arises with this type of mixing device concerns the uneven distribution of the liquid-gas mixture across the width of the exchanger passages.
  • 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 is done discretely over the width of the passage.
  • a distribution can take place in the direction orthogonal to the overall flow direction, in particular thanks to the exchange waves generally used in this type of exchanger such as perforated or serrated waves (from the term "serrated" in English).
  • perforated or serrated waves from the term "serrated” in English.
  • the document FR 3 064 346 describes a mixing device in which the channels all have downstream portions with external profiles forming an angle, measured between the tangent to said external profile at the point of intersection with the downstream face of the downstream portion and the axis of symmetry of the longitudinal channel, equal to 0°.
  • the arrangement of a free space at the outlet of the mixing device poses problems in terms of mechanical strength of the exchanger and can lead to an accumulation of the first phase in this area.
  • Increasing the number of channels following one another in the width of the exchanger leads to a reduction in the flow rate of the first phase through each orifice of each channel and is detrimental to the good distribution of the two-phase mixture at the outlet of the mixing device.
  • the arrangement of "hardway" type waves at the outlet of the mixing device or the arrangement of mixing devices with more complex geometry increases the pressure losses, which degrades the performance of the process.
  • the present invention aims to solve all or part of the problems mentioned above, in particular by proposing a mixing device allowing a more homogeneous distribution of a two-phase mixture in the width of a heat exchanger passage while limiting the pressure losses that the two-phase mixture can undergo at the outlet of the mixing device.
  • the invention relates to a heat exchanger comprising a plurality of plates arranged parallel to each other and to a longitudinal direction, said plates being stacked with spacing so as to define between them at least a first set of passages configured for the flow of the first fluid.
  • a first set of passages configured for the flow of the first fluid.
  • a second set of passages configured for the flow of a second fluid to be put into heat exchange relation with the first fluid, at least one passage of the first set comprising a mixing device according to the invention.
  • the first phase is a liquid phase.
  • the second phase is a gaseous phase.
  • natural gas refers to any composition containing hydrocarbons including at least methane. This includes a “raw” composition (prior to any processing or washing), as well as any composition that has been partially, substantially or completely processed for the reduction and/or removal of one or more compounds, including, but not limited to, sulfur, carbon dioxide, water, mercury and certain heavy and aromatic hydrocarbons.
  • Fig. 1 is a sectional view of a heat exchanger 1 comprising a mixing device 3 according to the invention.
  • the exchanger 1 is preferably of the brazed plate and fin type. It comprises a stack of plates 2 (not visible) which extend in two dimensions, parallel to a plane defined by a longitudinal direction z and a lateral direction y.
  • the plates 2 are arranged parallel to one another with a spacing between each plate and thus form a superposition of passages for the flow of fluids in indirect heat exchange relationship 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 may comprise a number of plates greater than 20, or even greater than 100, defining between them a first set of passages 10 (only one passage is 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 one second fluid F2, the flow of said fluids taking place generally in the direction z.
  • the passages 10 may be arranged, in whole or in part, alternating and/or adjacent to all or part of the passages 20.
  • the exchanger 1 may 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 10, 20 along the edges of the plates 2 is generally ensured by lateral and longitudinal sealing strips 4 fixed on the plates 2.
  • the lateral sealing strips 4 do not close completely the passages 10, 20 but advantageously leave fluid inlet and outlet openings located in the diagonally opposite corners of the passages.
  • the openings of the passages 10 of the first set are arranged coincidentally one above the other in the stacking direction x of the passages, which is perpendicular to the directions y and z, while the openings of the passages 20 of the second set are arranged in the other corners of the exchanger located on Fig. 1 by the arrows F2, with the inlet and outlet for the second fluid F2 located respectively at the top left and bottom right.
  • the openings placed one above the other are joined respectively in semi-tubular collectors 40, 45, 52, 55, through which the distribution and evacuation of the fluids in and from the passages 10, 20 are carried out.
  • passage openings can thus be arranged at other positions within the width of the exchanger, in particular in the center of the width of the exchanger, and/or at other positions within the length of the exchanger.
  • the semi-tubular collectors 52 and 45 are used for introducing fluids into the exchanger 1 and the semi-tubular collectors 40, 55 are used for evacuating 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 counter-currently in the exchanger 1.
  • the first and second fluids can also circulate co-currently, 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 direction z is oriented vertically when the exchanger 1 is in operation.
  • the first fluid F1 flows generally vertically and in an upward direction.
  • Other directions and flow directions of the fluids F1, F2 are of course conceivable, 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 assembly.
  • the first fluid F1 is a refrigerant fluid and the second fluid F2 is a heat-transfer 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 the fluids over the entire width of the passages 10, 20.
  • these structures comprise heat exchange waves 11 which advantageously extend along the width and length of the passages 10, 20, parallel to the plates 2, in the extension of the distribution waves along the length of the passages.
  • the passages 10, 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 the distribution waves 51, 54.
  • Fig. 1 shows a passage 10 of the first assembly configured for the flow of a first fluid F1 in the form of a mixture of two phases, also called a two-phase mixture.
  • the first assembly comprises several passages 10 of this type superimposed on each other.
  • 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 collector 30 and a second collector 52 which are separate.
  • the separator 6 then forms a source of first phase and second phase.
  • source of fluid is meant any means suitable for supplying the channels of the mixing device with a fluid.
  • the mixing device 3 preferably extends in the section of the passage 10 over almost all, or even all, of the height of the passage 10, so that the mixing device is in contact with each plate 2 forming the passage 10.
  • the mixing device 3 is advantageously fixed to the plates 2 by brazing.
  • the mixing device 3 is advantageously of generally parallelepiped shape.
  • It further comprises a series of longitudinal channels 32 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 321 to a second outlet 322, said longitudinal channels 32 being arranged at successive positions y i , y i+1 ,... along the lateral direction y.
  • the mixing device 3 comprises at least a first inlet 311 in fluid communication with the first collector 30 and a second inlet 321, separate, i.e. distinct, from the first inlet 311, in fluid communication with the second collector 52.
  • the first collector 30 is fluidly connected to a first phase source 61 and the second collector 52 is fluidly connected to another second phase source 62.
  • Said at least a first inlet 311 and said at least a second inlet 321 are placed in fluid communication via at least one orifice 34.
  • the mixing device is configured for separate introduction of the first phase and the second phase, the first inlet 311 being adapted for supplying the first phase 61 to the lateral channel 31 and said at least one second inlet 321 being adapted for supplying the longitudinal channels 32 with the second phase 62.
  • the first and second inlets are advantageously formed by opening the lateral and longitudinal channels at the lateral and longitudinal peripheral edges of the device 3.
  • the lateral channel 31 is fluidically connected to at least one longitudinal channel 32 such that, when the first phase 61 flows in the lateral channel 31 and the second phase 62 flows in the longitudinal channel 32, the mixing device 3 distributes through a second outlet 322 of the channel 32 a mixture of the first phase 61 and the second phase 62, preferably a two-phase liquid/gas mixture F1, also called a two-phase mixture.
  • the longitudinal channel and/or the lateral channel have generally rectilinear shapes.
  • the channels 31, 32 are advantageously in the form of longitudinal recesses provided in the mixing device 3. They preferably open out at the level of the upper 3a and lower 3b surfaces of the mixing device 3.
  • the orifices 34 are advantageously holes 34 made in the material of the device 3 and extending between the first channel 31 and the second channel 32, preferably in the plane formed by the directions x and y, the orifices 34 being able to be inclined relative to the direction x or, preferably, being aligned with the vertical direction x.
  • the orifices 34 are cylindrically symmetrical, more preferably cylindrical in shape.
  • said at least one lateral channel 31 comprises a bottom wall 3c and said at least one longitudinal channel 32 comprises a top wall 3d which extends opposite the bottom wall 3c, the orifices 34 being pierced in the bottom wall of the first channel 31 and opening into the top wall of the longitudinal channel 32.
  • Fig. 3 is a view of the mixing device 3 of Fig. 2 in a section plane orthogonal to the lateral direction y and passing through an orifice 34.
  • mixing devices 3 having longitudinal channels whose width, measured in the lateral direction y, remains constant along the longitudinal direction z are arranged in the passages 10 of the first set, in particular longitudinal channels of parallelepipedal shape such as the shape of the lateral channels 31 visible on Fig. 2 .
  • each longitudinal channel 32 At the outlet of each longitudinal channel 32, the flow of the two-phase mixture of the first fluid F1 takes place preferentially along the longitudinal direction z, with a progressive expansion of the flow in the width of the passage 10.
  • 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 10 of the first set.
  • width means the distance measured between the edges delimiting the longitudinal channel 32 in a predetermined longitudinal section plane which is parallel to the longitudinal direction z and parallel to the lateral direction y, i.e. the width of the external profile of the channel in said section plane, as shown for example in Fig. 4 to Fig. 9 .
  • the disparities in the flow rate of the mixture in the width of the passage 10 are thus reduced, or even eliminated, after a shorter propagation distance of the mixture downstream of the mixing device 3.
  • the heat exchanges between the two-phase mixture and the second fluid F2, and hence the operation of the exchanger, are improved.
  • the downstream portion 324 opens at a downstream face 326 of the mixing device 3, the second outlet 322 being arranged at the downstream face 326. At least a portion of the first phase 61 flowing in the lateral channel 31 feeds the orifice 34 to flow into the longitudinal channel where the mixture. The second phase 62 flows successively into the upstream 323 and downstream 324 portions. The mixture is distributed through the second outlet 322.
  • the downstream portion 324 has a width D y increasing along the length L 4 in the direction of the second outlet 322, preferably increasing over the entire length L 4 .
  • downstream portion along the longitudinal direction z can be induced punctually, in one or more times, or in a progressive manner, i.e. be continuously increasing, along all or part of the downstream portion 324.
  • the width D y of the downstream portion 324 increases continuously, i.e. progressively, over the entire length L 4 in the direction of the second outlet 322. This limits the disturbances that could be caused by sudden variations in channel width in the flow of the mixture.
  • the width D M can be between 6 and 25 mm, preferably between 8 and 20 mm.
  • a mixing device may be intended to be arranged in a passage 10 provided, downstream of the mixing device, with at least one exchange wave comprising exchange channels each having a width of between 0.6 and 2 mm, preferably a width of at least 0.7 mm and/or at most 1.5 mm.
  • the minimum width D m is measured at the end 324a of the downstream portion 324 and the maximum width D M is measured at the second outlet 322.
  • the longitudinal channel 32 is delimited by side walls 325 forming, in a longitudinal section plane which is parallel to the longitudinal direction z and to the lateral direction y, an external profile of said channel 32 with axis of symmetry AA' parallel to the longitudinal direction z.
  • Fig. 9 represents an embodiment in which the widening of the downstream portion along the longitudinal direction z is induced punctually, in one go, at the end 324a.
  • the upstream portion 323 is connected to the downstream portion 324 by its end 324a.
  • the upstream portion 323 has a length L 3 measured along the longitudinal direction z with the ratio L 3 / L 4 between 1 and 15, preferably between 3 and 12.
  • the length L 4 can be between 5 and 40 mm.
  • the length L 3 can be between 30 and 70 mm.
  • said at least one orifice 34 opens into the longitudinal channel 32 at its upstream portion 323, preferably at a distance L z from the end 324a of the downstream portion 324 with L z at least equal to 4%, more preferably between 7 and 90%, and even more preferably ranging from 10 to 50%, of the length L 3 of the upstream portion (323).
  • the orifice 34 may open at a distance L z between 3 and 70 mm from the end 324a of the downstream portion 324.
  • the orifice(s) 34 of a longitudinal channel 32 all open at its upstream portion 323.
  • the mixing device is advantageously free of orifice 34 opening at its upstream portion 324.
  • the higher speed of the second phase 62 in the portion 323 of the channel 32 compared to the speed of the fluid F1 in the portion 324 also makes it easier to pass the phase 61 from the channel 31 to the channel 32 via the orifice 34 due to the high inertia of the phase 61 by the phase 62 and the resulting entrainment.
  • the position of the at least one orifice 34 along the longitudinal direction z varies between the longitudinal channels. This is particularly for for this reason some ports 34 may be closer to the end 324a than others.
  • the longitudinal channels advantageously have identical dimensional characteristics, i.e. the same external profile, the same depth, the same ratio L 3 / L 4 , the same distance L z , although it is possible in certain configurations to vary at least one characteristic of at least one channel relative to the others, in particular the ratio of lengths of the downstream and upstream portions.
  • all or part of the upstream portion 323 has a rectilinear external profile with a constant width D 3 , preferably equal to the minimum width D m of the downstream portion 324.
  • the upstream portion 323 has a variable width D 3 over all or part of its length, D y being greater than the maximum value that can be reached by D 3 .
  • Fig. 6 And Fig. 7 schematize embodiments according to which the longitudinal channel 32 comprises at least one obstacle 327 arranged so as to subdivide the downstream portion 324 into several intermediate channels 328 opening at the level of the second outlet 322.
  • the installation of one or more obstacles makes it possible to modify the flow direction of the two-phase mixture by giving a component along the y direction to its speed. This increases the angular opening of the fluid jet at the outlet of the longitudinal channel, which makes it possible to supply a greater number of exchange channels positioned downstream of the mixing device.
  • Obstacles can also be used to keep the fluid passage section constant or almost constant, or possibly reduce it, in the downstream portion, despite its widening.
  • fluid passage section we mean the surface through which the fluid flows measured perpendicular to the longitudinal direction z. This is to ensure lateral expansion of the mixture, without increasing the fluid passage section.
  • the total surface area of said obstacle 327 measured in a cross-sectional plane perpendicular to the longitudinal direction z represents between 20 and 80%, preferably between 30 and 70%, of the total fluid passage section of the downstream portion (324) measured in said cross-sectional plane.
  • the total surface area is understood as the sum of the surfaces of each obstacle.
  • the surface of the obstacle measured at a distance of 1 mm along the longitudinal direction z, in the direction of the flow of the fluid, after the point of appearance in the channel 32, that is to say at a so-called impact position located 1 mm after the point of appearance of the obstacle where the fluid impacts on the obstacle, represents between 1% and 80% of the fluid passage section of the channel 32 determined in a cross-sectional plane positioned at the impact position.
  • the longitudinal channel 32 further comprises at least one balancing channel 329 placing the intermediate channels 328 in fluid communication. This makes it possible to rebalance the fluid pressures between the intermediate channels 328, in the case where there are disparities in flow rate and fluid pressure between the intermediate channels.
  • Fig. 8 represents an example of such a configuration.
  • an even number of intermediate channels is provided in order to maintain a distribution symmetry along the AA' axis of the mixture within the longitudinal channel.
  • the obstacles 327 have a height equal to those of the side walls of the longitudinal channel.
  • said at least one obstacle 327 has a width dy, measured in the lateral direction y, increasing in the direction of the second exit. 322, preferably with a curvilinear, convex and/or concave external profile. This makes it possible to conform the obstacle so as to avoid additional pressure losses of the fluid F1 in the downstream portion 324 of the channel 32 due to detachment of the fluid at the walls of the obstacle or due to fluid recirculation zones.
  • passages 10 of the first set comprise a mixing device according to the invention.
  • At least one passage 20 of the second set is arranged between at least one pair of consecutive passages 10 of the first set.
  • the positions y i , y i+1 , y i+2 ... of each channel along the lateral direction y can be determined by considering the position of the center of each channel along the lateral direction y. For example, by considering channels in the form of parallelepiped grooves as shown in Fig. 2 , 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 distance D A can be between 10 and 40 mm, preferably greater than or equal to 20 mm and less than or equal to 30 mm.
  • FIG. 11 shows the results of a simulation of the propagation of a two-phase mixture in a longitudinal channel of a conventional mixing device (configuration A) and in a longitudinal channel of a mixing device according to an embodiment of the invention (configuration B).
  • the mixing device was in the form of a grooved bar having, as longitudinal channels, a series of parallelepipedal grooves succeeding one another at regular intervals of 30 mm.
  • Each groove measured 7 mm in width, 70 mm in length and 7 mm in height.
  • the mixing devices were in the form of grooved bars with grooves succeeding each other at regular intervals of 30 mm.
  • Each groove was in the form of a longitudinal channel with an upstream portion 323 having dimensions of 7 mm width, 63 mm length and 7 mm height.
  • the downstream portion 324 was truncated in shape with a width of 7 mm at the end 324a and 14 mm at the second outlet 322.
  • the upstream portion 323 had a length of 7 mm and a height of 7 mm.
  • An obstacle in the shape of an isosceles triangle was placed in the downstream portion 324, symmetrically with respect to the axis of symmetry AA', with a height of 7 mm in the z direction and a base width of 7 mm at the second outlet 322.
  • the width D M was twice as high as D 3 .
  • the ratio L 3 / L 4 was 8 and the length L z was 5 mm.
  • the angle ⁇ was 45°. Note that configuration B corresponds to the particular case in which the fluid passage section of the downstream portion is kept constant in the longitudinal direction z due to the presence of the obstacle although the width of said portion increases in the direction of the second outlet 322.
  • the longitudinal channels of the mixing devices of configurations A and B were arranged in the same number and at identical positions y i , y i+1 ,... along the lateral direction y.
  • waves 11 of the "serrated” type i.e. with partial offset, were arranged at the outlet of the mixing devices in each passage.
  • Simulation is a three-dimensional CFD-type calculation using the finite element method, which is the English acronym for "Computational Fluid Dynamics”.
  • Fig. 11 shows the evolution of the value of the smallest dimensionless velocity of the fluid along the longitudinal direction z (denoted V z ) measured on successive sections of the waves located after the outlet 322 in planes parallel to the x and y directions, for several distance values between the outlet 322 and said planes.
  • V z longitudinal direction
  • These velocity values are representative of the quality of the distribution of the fluid in the waves: a negative value indicates the presence of a recirculation zone, with stagnant fluid in the center of the zone. A zero value indicates the presence of stagnant fluid. Since the stagnant fluid is not renewed, it does not participate in the heat exchange and reduces the overall efficiency of the exchanger.
  • a performance indicator of fluid distribution is the minimum distance required along the longitudinal z direction from which all fluid has a positive velocity along the longitudinal z direction.
  • Fig. 12 schematizes a process for liquefying a hydrocarbon stream 102 as a second fluid F2, which may be natural gas, possibly pretreated, for example having undergone separation of at least one of the following constituents: water, carbon dioxide, sulfur compounds, methanol, mercury, before its introduction into the heat exchanger 1.
  • the hydrocarbon stream comprises, in mole fraction, at least 60% methane, preferably at least 80%.
  • the hydrocarbon stream 102 and the refrigerant stream 202 enter the exchanger 1 respectively through a third inlet 25 and a fourth inlet 21 to circulate in dedicated passages of the exchanger in directions parallel to the longitudinal direction z, which is substantially vertical in operation.
  • the hydrocarbon stream 102 circulates in the passages 20 of the second assembly 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 exit through a third outlet 22 and a first outlet 23.
  • the passages of the second and third sets are arranged, in whole or in part, alternating and/or adjacent to all or part of the passages 10 of the first set.
  • the fourth inlet 21 for the refrigerant stream 202 and the third inlet 25 for the hydrocarbon stream 102 are arranged so that the refrigerant stream 202, and possibly 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 exchanger temperatures, this entry point being able to be the fourth entry 21 or the third entry 25, depending on the process considered.
  • the hydrocarbon stream 102 can be introduced into the exchanger 1 at a temperature between -130 and 40°C.
  • the hydrocarbon stream 102 is introduced fully 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 member 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 first phase and a second phase.
  • the two-phase refrigerant stream 203 forms the first fluid F1 considered previously.
  • At least a portion of the two-phase refrigerant stream 203 resulting from the expansion is introduced into a separating member 27.
  • the separating member may be any device suitable for separating a two-phase fluid into a predominantly gaseous stream on the one hand and a predominantly liquid stream on the other hand.
  • the second phase 62 is introduced by the collector 52 which feeds the second inlets 321 of mixing devices 3 arranged in the passages 10 of the first set.
  • the first phase 61 is introduced by the first collector 30 which feeds the first inlets 311 of mixing devices 3 arranged in each passage 10 (not shown in Fig. 9 ).
  • the second 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 entry point 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 liquid-gas mixture state in the passages 10 of the exchanger 1 each provided with mixing devices 3 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 of between -130 and -80°C and exits the heat exchanger 1 at a second temperature T2 higher than the first temperature T1, preferably with T2 of between -10 and 50°C.
  • Said at least a portion of the two-phase refrigerant stream 203 flows in the passages 10 in an upward direction and is vaporized by counter-cooling the natural gas 102 and the refrigerant stream 202.
  • a cooled and/or at least partially liquefied hydrocarbon stream 101 is thus obtained at the outlet of the exchanger 1.
  • the vaporized refrigerant stream leaves the exchanger 1 through a second outlet 42 connected to the collector 55 to be compressed by a compressor then cooled in an indirect heat exchanger by heat exchange with an external cooling fluid, for example water or air (at 26 on Fig. 12 ).
  • the pressure of the refrigerant stream at the compressor outlet can be between 2 MPa and 9 MPa.
  • the temperature of the refrigerant stream at the outlet of 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 exchanger 1, the refrigerant stream can also be separated into two or three fractions, each fraction being expanded to a different pressure level and then sent to different stages of the compressor.
  • the refrigerant stream 202 is formed for example by a mixture of hydrocarbons and nitrogen such as a mixture of methane, ethane and nitrogen but may 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 may also contain propane, butane, isobutane, n-butane, pentane, isopentane, n-pentane and/or ethylene.
  • the refrigerant stream may include, as a replacement for ethane, ethylene and, as a replacement for all or part of the propane, compounds of the C4, C5 type.
  • the method 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 carry out pre-cooling of the hydrocarbon stream.
  • Fig. 13 schematizes a process for liquefying 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 expansion levels to increase the efficiency of the cycle.
  • This additional refrigeration cycle is operated by means of an additional refrigerant stream 300 in an additional heat exchanger 2, called a pre-cooling exchanger, arranged upstream of the heat exchanger 1 in the direction of the flow of the hydrocarbon stream 110, which then forms the liquefaction exchanger.
  • a feed stream 110 arrives for example at a pressure of between 2.5 MPa and 7 MPa and at a temperature of 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 co-currently in the downward direction.
  • a cooled, or at least partially liquefied, hydrocarbon stream 102 leaves the pre-cooling exchanger 2.
  • the hydrocarbon stream 102 leaves in the gaseous or partially liquefied state, for example at a temperature 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.
  • the stream 102 is then introduced into the exchanger 1.
  • the stream 203 is vaporized in the exchanger 1 and leaves to be compressed by the compressor K2 then cooled in the indirect heat exchanger C2 by heat exchange with an external cooling fluid, for example water or air.
  • the refrigerant stream from the exchanger C2 is then returned to the 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 different pressure levels, giving rise to expanded two-phase partial streams each comprising a first phase and a second phase. At least a portion of these two-phase partial streams is introduced into respective separator members 24, 25, 26.
  • the gaseous and liquid phases separated by each separating 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-gas mixture state into dedicated refrigerant passages.
  • mixing devices not shown
  • only the first 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 202 and the additional refrigerant stream 300.

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Claims (14)

  1. Mischvorrichtung (3) zum Verteilen eines Gemisches aus einer ersten Phase (61) und einer zweiten Phase (62) eines ersten Fluids (F1) im Wesentlichen in einer Längsrichtung (z) in mindestens einem Durchgang (10) eines Wärmetauschers (1), wobei die Mischvorrichtung (3) umfasst:
    - mindestens einen seitlichen Kanal (31), der für die Strömung der ersten Phase (61) von mindestens einem ersten Einlass (311) ausgebildet ist,
    - eine Reihe von Längskanälen (32), die sich in der Längsrichtung (z) erstrecken und jeweils für die Strömung der zweiten Phase (62) von einem zweiten Einlass (321) bis zu einem zweiten Auslass (322) ausgebildet sind, wobei die Längskanäle in einer zur Längsrichtung (z) orthogonalen Querrichtung (y) aufeinanderfolgen, und
    - mindestens eine Öffnung (34), die den seitlichen Kanal (31) fluidisch mit mindestens einem Längskanal (32) verbindet, so dass die Mischvorrichtung (3) ausgebildet ist, um ein Gemisch aus der ersten Phase (61) und der zweiten Phase (62) durch den zweiten Auslass (322) des Längskanals (32) zu verteilen,
    - wobei der mindestens eine Längskanal (32) der Mischvorrichtung (3) in Längsrichtung (z) in einen stromaufwärtigen Abschnitt (323) und einen stromabwärtigen Abschnitt (324) unterteilt ist, die jeweils eine in Längsrichtung (z) gemessene Länge (L3, L4) und eine in Querrichtung (y) gemessene Breite (D3, Dy) aufweisen , wobei der stromabwärtige Abschnitt (324) zwischen dem stromaufwärtigen Abschnitt (323) und dem zweiten Auslass (322) angeordnet ist, wobei der stromabwärtige Abschnitt (324) an jedem Punkt seiner Länge (L4) eine Breite (Dy) aufweist, die größer ist als die Breite (D3) des stromaufwärtigen Abschnitts (323) , wobei der stromabwärtige Abschnitt (324) auf Höhe einer stromabwärtigen Fläche (326) der Mischvorrichtung (3) mündet , wobei der zweite Auslass (322) auf Höhe der stromabwärtigen Fläche (326) eingerichtet ist,
    - dadurch gekennzeichnet, dass der stromabwärtige Abschnitt (324) im Längsschnitt in einer zur Längsrichtung (z) und zur Querrichtung (y) parallelen Ebene (P) ein Außenprofil aufweist, das einen Winkel () bildet, der zwischen der Tangente (T) an das Außenprofil am Schnittpunkt mit der stromabwärtigen Fläche (326) und der Symmetrieachse (AA') des Längskanals (32) gemessen wird und zwischen 5 und 85° liegt.
  2. Vorrichtung nach Anspruch 1, dadurch gekennzeichnet, dass der stromabwärtige Abschnitt (324) über seine gesamte Länge (L4) in Richtung des zweiten Auslasses (322) eine kontinuierlich zunehmende Breite (Dy) aufweist.
  3. Vorrichtung nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass der stromabwärtige Abschnitt (324) ganz oder teilweise im Längsschnitt in einer zur Längsrichtung (z) und zur Querrichtung (y) parallelen Ebene (P) ein Außenprofil in Form eines gleichschenkligen Trapezes aufweist.
  4. Vorrichtung nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass der stromaufwärtige Abschnitt (323) des Längskanals (32) durch ein Ende (324a) mit dem stromabwärtigen Abschnitt verbunden ist, wobei die mindestens eine Öffnung (34) in den Längskanal (32) auf Höhe des stromaufwärtigen Abschnitts (323) in einem Abstand (Lz) vom Ende (324a) mündet , vorzugsweise ist (Lz) größer oder gleich 4 % und vorzugsweise zwischen 7 und 90 % der Länge (L3) des stromaufwärtigen Abschnitts (323).
  5. Vorrichtung nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass die mindestens eine Öffnung (34) so angeordnet ist, dass, wenn die erste Phase (61) vom ersten Einlass des seitlichen Kanals (31) und die zweite Phase (62) vom zweiten Einlass (321) des Längskanals (32) strömt, das Mischen der ersten Phase (61) und der zweiten Phase (62) stromaufwärts des stromabwärtigen Abschnitts (324) stattfindet.
  6. Vorrichtung nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass die Öffnung oder die Öffnungen (34) der Mischvorrichtung (3) alle auf Höhe des stromaufwärtigen Abschnitts (324) eines Längskanals (32) münden.
  7. Vorrichtung nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass jeder Längskanal der Reihe von Längskanälen (32) mindestens eine Öffnung (34) umfasst, die auf Höhe seines stromaufwärtigen Abschnitts (323) mündet , wobei die Position der mindestens einen Öffnung (34) in Längsrichtung (z) zwischen den Längskanälen (32) variiert.
  8. Vorrichtung nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass die Länge (L3) des stromaufwärtigen Abschnitts (323) und die Länge (L4) des stromabwärtigen Abschnitts (324) so sind, dass das Verhältnis L3 / L4 zwischen 1 und 15, vorzugsweise zwischen 3 und 12, liegt.
  9. Vorrichtung nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass der stromabwärtige Abschnitt (324) eine in einer sogenannten Stapelrichtung (x), die senkrecht zur Längsrichtung (z) und senkrecht zur Querrichtung (y) ist, gemessene Tiefe aufweist, die in Richtung des zweiten Auslasses (322) zunimmt.
  10. Vorrichtung nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass der Längskanal (32) mindestens ein Hindernis (327) umfasst, das so angeordnet ist, dass es den stromabwärtigen Abschnitt (324) in mehrere Zwischenkanäle (328) unterteilt, die auf Höhe des zweiten Auslasses (322) münden , wobei vorzugsweise die Zwischenkanäle (328) symmetrisch zur Symmetrieachse (AA') des Längskanals (32) angeordnet sind.
  11. Wärmetauscheranlage, umfassend:
    - einen Wärmetauscher (1), der mehrere Platten (2) umfasst, die parallel zueinander und zu einer Längsrichtung (z) angeordnet sind, wobei die Platten (2) mit Abstand gestapelt sind, um zwischen sich mindestens einen ersten Satz von Durchgängen (10), die für die Strömung eines ersten Fluids (F1) im Wesentlichen in Längsrichtung (z) ausgebildet sind, und mindestens einen zweiten Satz von Durchgängen (20) zu definieren, die für die Strömung eines zweiten Fluids (F2) ausgebildet sind, das mit dem ersten Fluid (F1) in Wärmetauschbeziehung zu bringen ist,
    - eine Quelle einer ersten Phase (61) des ersten Fluids (F1), die fluidisch mit mindestens einem ersten Sammler (30) des Wärmetauschers (1) verbunden ist,
    - eine Quelle einer zweiten Phase (62) des ersten Fluids (F1), die fluidisch mit mindestens einem zweiten Sammler (52) des Wärmetauschers (1) verbunden ist,
    - eine Mischvorrichtung (3) nach einem der Ansprüche 1 bis 10 , wobei die Mischvorrichtung (3) in mindestens einem Durchgang (10) der ersten Reihe angeordnet und ausgebildet ist, um das erste Fluid (F1), das aus einem Gemisch der ersten Phase (61) und der zweiten Phase (62) gebildet ist, in dem Durchgang (10) der ersten Reihe zu verteilen , wobei der erste Einlass (311) des seitlichen Kanals (31) in fluider Verbindung mit dem ersten Sammler (30) steht und der zweite Einlass (321) in fluider Verbindung mit dem zweiten Sammler (52) steht , wobei die erste Phase (61) eine flüssige Phase und die zweite Phase (62) eine gasförmige Phase ist.
  12. Verfahren zum Mischen einer ersten Phase (61) und einer zweiten Phase (62) eines ersten Fluids (F1) in einer Mischvorrichtung (3) nach einem der Ansprüche 1 bis 10, wobei das Verfahren die folgenden Schritte umfasst:
    i) Einleiten der ersten Phase (61) des ersten Fluids (F1) durch mindestens einen ersten Einlass (311) des seitlichen Kanals (31),
    ii) Einleiten der zweiten Phase (62) des ersten Fluids (F1) durch einen zweiten Einlass (321) jedes Längskanals (32) , wobei die zweite Phase (62) in jedem Längskanal (32) in Längsrichtung (z) bis zu einem zweiten Auslass (322) des Längskanals (32) strömt,
    iii) Strömen mindestens eines Teils der ersten Phase (61) vom seitlichen Kanal (31) zum Längskanal (32) durch die Öffnung (34), um die erste Phase (61) mit der zweiten Phase (62) im Längskanal (32) zu mischen,
    iv) Verteilen des Gemisches aus der ersten Phase (61) und der zweiten Phase (62) durch den zweiten Auslass (322) jedes Längskanals (32).
  13. Mischverfahren nach Anspruch 12, dadurch gekennzeichnet, dass das Mischen der ersten Phase (61) mit der zweiten Phase (62) stromaufwärts des stromabwärtigen Abschnitts (324) durchgeführt wird.
  14. Verfahren zur Verflüssigung eines Kohlenwasserstoffstroms (102) wie Erdgas als zweites Fluid (F2) durch Wärmetausch mit mindestens einem zweiphasigen Kältemittelstrom (203) als erstes Fluid (F1) , wobei das Verfahren ein Mischverfahren nach einem der Ansprüche 12 oder 13 in einer Mischvorrichtung (3) nach einem der Ansprüche 1 bis 10 anwendet und die folgenden Schritte umfasst:
    a) Einleiten des Kohlenwasserstoffstroms (102) in einen zweiten Satz von Durchgängen (20) eines Wärmetauschers (1),
    b) Einleiten eines Kältemittelstroms (202) in einen dritten Satz von Durchgängen des Wärmetauschers (1),
    c) Austritt des Kältemittelstroms (201) aus dem Wärmetauscher (1) und Entspannung des Kältemittelstroms (201) auf mindestens einer Druckstufe, um mindestens einen zweiphasigen Kältemittelstrom (203) zu erzeugen,
    d) Trennung mindestens eines Teils des aus Schritt c) stammenden zweiphasigen Kältemittelstroms (203) in eine zweite Phase (62) und eine erste Phase (61),
    e) Anordnung der Mischvorrichtung (3) in mindestens einem Durchgang (10) eines ersten Satzes von Durchgängen des Wärmetauschers (1),
    f) Einleiten mindestens eines Teils der zweiten Phase (62) und mindestens eines Teils der ersten Phase (61) in die Mischvorrichtung (3), um ein erstes Fluid (F1) zu erhalten, das aus einem Gemisch der ersten Phase (61) und der zweiten Phase (62) am Auslass der Mischvorrichtung (3) gebildet ist,
    g) Verdampfung mindestens eines Teils des aus Schritt f) stammenden ersten Fluids (F1) in dem Durchgang (10) durch Wärmetausch mit mindestens dem Kohlenwasserstoffstrom (102), um einen gekühlten und/oder zumindest teilweise verflüssigten Kohlenwasserstoffstrom (101) am Auslass des Tauschers (1) zu erhalten.
EP20817018.3A 2019-12-19 2020-12-07 Mischvorrichtung zur förderung einer homogenen verteilung einer zweiphasenmischung, wärmetauscheinrichtung und zugehöriges mischverfahren Active EP4078065B1 (de)

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PCT/EP2020/084935 WO2021122115A1 (fr) 2019-12-19 2020-12-07 Dispositif mélangeur favorisant une distribution homogène d'un mélange diphasique, installation d'échange de chaleur et procédé de mélange associé

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DE3415807A1 (de) * 1984-04-27 1985-10-31 Linde Ag, 6200 Wiesbaden Waermetauscher
US6783662B2 (en) * 1999-03-18 2004-08-31 Exxonmobil Research And Engineering Company Cavitation enhanced liquid atomization
KR100781820B1 (ko) * 2001-02-21 2007-12-03 시부야 코교 가부시키가이샤 기체액체 혼합류의 분사장치
FR2944460B1 (fr) * 2009-04-21 2012-04-27 Ass Pour La Rech Et Le Dev De Methodes Et Processus Indutriels Armines Buse apte a maximaliser la quantite de mouvement produite par un ecoulement diphasique provenant de la detente d'un debit saturant
CN103983138A (zh) * 2014-05-16 2014-08-13 杭州杭氧股份有限公司 一种铝制板翅式换热器大气量两相流均布装置
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
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

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US20230125515A1 (en) 2023-04-27
CN114846291A (zh) 2022-08-02
WO2021122115A1 (fr) 2021-06-24
FR3105388A1 (fr) 2021-06-25
FR3105388B1 (fr) 2022-10-07
EP4078065A1 (de) 2022-10-26
JP2023506902A (ja) 2023-02-20
JP7654663B2 (ja) 2025-04-01

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