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US20190011191A1 - Withdrawal/ infeed of gas for influencing radial liquid migration - Google Patents

Withdrawal/ infeed of gas for influencing radial liquid migration Download PDF

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Publication number
US20190011191A1
US20190011191A1 US16/031,425 US201816031425A US2019011191A1 US 20190011191 A1 US20190011191 A1 US 20190011191A1 US 201816031425 A US201816031425 A US 201816031425A US 2019011191 A1 US2019011191 A1 US 2019011191A1
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US
United States
Prior art keywords
tube
heat exchanger
gaseous phase
shell space
medium
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.)
Abandoned
Application number
US16/031,425
Other languages
English (en)
Inventor
Manfred Steinbauer
Christiane Kerber
Manfred Schonberger
Jurgen SPREEMANN
Eva MULLER
Luis MATAMOROS
Florian Deichsel
Konrad Braun
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.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: STEINBAUER, MANFRED, KERBER, CHRISTIANE, BRAUN, KONRAD, Deichsel, Florian, MATAMOROS, LUIS, SCHONBERGER, MANFRED, SPREEMANN, JURGEN, MULLER, EVA
Publication of US20190011191A1 publication Critical patent/US20190011191A1/en
Abandoned legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/02—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/02—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled
    • F28D7/024—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled the conduits of only one medium being helically coiled tubes, the coils having a cylindrical configuration
    • 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
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
    • F28D7/1615—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation the conduits being inside a casing and extending at an angle to the longitudinal axis of the casing; the conduits crossing the conduit for the other heat exchange medium
    • F28D7/1623—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation the conduits being inside a casing and extending at an angle to the longitudinal axis of the casing; the conduits crossing the conduit for the other heat exchange medium with particular pattern of flow of the heat exchange media, e.g. change of flow direction
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/06—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
    • 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
    • F28F9/007—Auxiliary supports for elements
    • F28F9/013—Auxiliary supports for elements for tubes or tube-assemblies
    • 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
    • F28F9/0234—Header boxes; End plates having a second heat exchanger disposed there within, e.g. oil cooler
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0033—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for cryogenic applications
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0061—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for phase-change applications
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • 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
    • F28F2009/222—Particular guide plates, baffles or deflectors, e.g. having particular orientation relative to an elongated casing or conduit
    • F28F2009/224—Longitudinal partitions
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F2250/00—Arrangements for modifying the flow of the heat exchange media, e.g. flow guiding means; Particular flow patterns
    • F28F2250/06—Derivation channels, e.g. bypass
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
    • F28F27/02—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus for controlling the distribution of heat-exchange media between different channels

Definitions

  • the invention relates to a coiled heat exchanger according to Claim 1 .
  • Such coiled heat exchangers are used for example in the case of physical quenches for acid gas removal (e.g. Rectisol processes), in ethylene plants or in plants for producing liquefied natural gas (LNG).
  • acid gas removal e.g. Rectisol processes
  • LNG liquefied natural gas
  • Liquid on the shell side of such heat exchangers with falling film evaporation is, in most cases, diverted in the direction of the outer tube layers of the tube bundle. This incorrect distribution of the liquid leads to a local deficit in the supply of coolant to the tube bundle in the region of the inner tube layers of the tube bundle, and therefore to losses in performance of the heat exchanger.
  • a heat exchanger for the indirect exchange of heat between a first medium, which has a liquid phase and a gaseous phase, and a second medium is disclosed, having
  • the heat exchanger has a gas discharge device by means of which a part of the gaseous phase can be discharged out of the shell space from the region of the inner tube layers, wherein the gas discharge device of the heat exchanger has at least one discharging flow path for the gaseous phase with an inlet opening arranged in the shell space in the region of the inner tube layers, and wherein the at least one discharging flow path is formed by a tube of an inner tube layer of the tube bundle, in particular by a tube of an innermost tube layer of the tube bundle (or has such an inner or innermost tube).
  • the heat exchanger prefferably has a gas supply device via which a gaseous phase of the first medium can be supplied into the shell space in the region of the outer tube layers.
  • the tube bundle coiled onto the core tube has, as viewed in a radial direction, a multiplicity n of tube layers situated one on top of the other, wherein, in the case of an even number n of tube layers, proceeding from the core tube, all tube layers up to the n/2-th tube layer are understood in the context of the invention to be inner tube layers, whereas the tube layers that follow these toward the outside (that is to say from the (n/2+1)-th tube layer to the n-th tube layer) are regarded as outer tube layers.
  • the inner (n ⁇ 1)/2 two players are understood to be inner tube layers, and the remaining tube layers are understood to be outer tube layers.
  • the discharge of the gaseous phase takes place in the region of the innermost tube layer, and the supply of the gaseous phase takes place in the region of the outermost tube layer.
  • the radial direction of the tube bundle refers to a direction which is perpendicular to the longitudinal axis of the shell and which points outward toward the shell, whereas the axial direction coincides with the longitudinal axis.
  • the core tube is preferably arranged in the shell space coaxially with respect to the longitudinal axis, and correspondingly extends in the axial direction.
  • the liquid phase can in a known manner be applied to the tube bundle from the top.
  • a liquid distributor used for distributing the liquid phase can also at the same time perform a separation of the liquid phase from the gaseous phase of the first medium.
  • the separation of the liquid phase from the gaseous phase may however also be performed in separate units.
  • the liquid distributor can conduct the liquid phase for example via an encircling gap on the shell, or via tubes, into a ring-shaped channel which is situated therebelow and which has distributor arms.
  • the liquid phase can be introduced via a central opening into the core tube and then conducted to a distributor in the form of a pressure distributor.
  • Such liquid distributors are described in detail for example in DE 10 2004 040 974 A1. Other liquid distributors are likewise conceivable.
  • the at least one discharging flow path to run, at least in sections, in the core tube, for example instead of a discharging flow path, which is formed by a tube of an inner tube layer of the tube bundle, in particular by a tube of an innermost tube layer of the tube bundle (see also above).
  • the inlet opening may be formed in the wall of the core tube.
  • the discharging flow path may be led through a wall of the core tube, wherein the inlet opening is arranged outside the core tube in the region of the inner tube layers, or terminates flush with a surface of the wall of the core tube.
  • the inlet opening may be arranged, in a radial direction of the tube bundle, between the surface of the wall of the core tube and an innermost tube layer.
  • the at least one discharging flow path is formed by a tube line.
  • the inlet opening may be formed in particular in a wall of the respective tube.
  • the heat exchanger in one embodiment, provision is made for the heat exchanger to have a skirt surrounding the tube bundle, which skirt surrounds the outer tube layers.
  • a skirt may have a hollow cylindrical form and serve to prevent a bypass flow of the first medium past the tube bundle in the shell space.
  • the skirt preferably engages tightly around the tube bundle.
  • the heat exchanger or the gas supply device to have, for supplying a gaseous phase of the first medium, at least one supplying flow path which has an outlet opening which is arranged in the shell space, or opens into the shell space, in the region of the outer tube layers.
  • the at least one supplying flow path to be led at least in sections on an outwardly pointing outer side of the skirt (that is to say runs further to the outside, in a radial direction, than the skirt, such that there, the skirt runs between the tube bundle and the supplying flow path) or is formed by a tube of an outer tube layer of the tube bundle, in particular by a tube of an outermost tube layer of the tube bundle (or has such an outer or outermost tube).
  • the outlet opening may be formed in the skirt.
  • the supplying flow path may be led through the skirt, wherein the outlet opening may be arranged, within a shell space section surrounded by the skirt, in the region of the outer tube layers, or may terminate flush with an inner side of the skirt.
  • the outlet opening may be arranged, in a radial direction of the tube bundle, between the inner side of the skirt and an outermost tube layer.
  • the at least one supplying flow path is formed for example by a tube line.
  • the heat exchanger or the gas discharge device to have multiple discharging flow paths for the gaseous phase of the first medium within each case one inlet opening, wherein the inlet openings are each arranged in the shell space in the region of the inner tube layers. It is furthermore preferable for the inlet openings to be arranged at different heights along the longitudinal axis.
  • the individual inlet openings may in this case be formed in accordance with one of the variants mentioned above.
  • a tube or a tube line which constitutes a discharging or a supplying flow path may have multiple inlet or outlet openings, which are for example arranged one behind the other along the respective tube or the respective tube line.
  • a multiplicity of flow paths to the respective inlet or outlet opening may be provided by means of a single tube or a single tube line. It is self-evidently also possible for a separate tube or a separate tube line to be provided for each inlet or outlet opening.
  • the temperature distribution in the shell space changes in accordance with the pressure distribution, such that the temperature distribution is also suitable for the closed-loop control of the gas discharge or supply.
  • a defined height of the shell space e.g. at the level of the discharge and/or supply of the gaseous phase
  • the heat exchanger is preferably configured such that, over the entire length of the tube bundle along the longitudinal axis, a part of the gaseous phase can be discharged from the region of the inner tube layers via a multiplicity of inlet openings, and/or the gaseous phase of the first medium can, in the region of the outer tube layers, be supplied via a multiplicity of outlet openings, such that, in particular over the entire length of the tube bundle, the actual pressure distribution or the actual temperature distribution is approximated to a setpoint pressure distribution or setpoint temperature distribution respectively, in the case of which the pressure or the temperature respectively is in each case preferably constant in a radial direction and follows a predefined or desired profile in an axial direction (that is to say along the longitudinal axis).
  • the heat exchanger according to the invention may have the sensors described further below for the purposes of measuring an actual pressure distribution or an actual temperature distribution.
  • the at least one supplying flow path or the gas supply device may have a valve for the open-loop or closed-loop control of the supply of the gaseous phase.
  • the at least one discharging flow path is connected or connectable in terms of flow via a compressor, in particular a compressor which is controllable in open-loop or closed-loop fashion, to the at least one supplying flow path.
  • a compressor in particular a compressor which is controllable in open-loop or closed-loop fashion
  • a gaseous phase discharged out of the shell space from the inner layers of the tube bundle can, after corresponding compression, be supplied to the shell space again in the region of the outer tube layers in a variable manner or in a manner controllable in open-loop or closed-loop fashion.
  • the individual tube layers are provided to bear against one another via spacers.
  • the core tube preferably accommodates the load of the tubes of the tube bundle, wherein, in particular, the load of the tube layers is dissipated inward via the respective spacers.
  • the heat exchanger in a further embodiment, provision is made for the heat exchanger to have a first line, via which the first medium is introducible (in particular in two-phase form) into the heat exchanger or the shell space, and/or for the heat exchanger to have a second line, via which the first medium is withdrawable from the heat exchanger or from the shell space of the heat exchanger.
  • the first line may for example be connected to a connector of the heat exchanger (for example at an upper section of the heat exchanger).
  • the second line may likewise be connected to a connector of the heat exchanger (for example at a lower section of the heat exchanger).
  • the heat exchanger has a first flow connection between the gas discharge device and the first line, such that a gaseous phase of the first medium or a process flow is withdrawable from the gas discharge device, and introducible into the first line, via the first flow connection.
  • the heat exchanger may also have a first flow connection between the gas discharge device and the second line, such that the a gaseous phase of the first medium or a process flow is withdrawable from the gas discharge device, and introducible into the second line, via the first flow connection.
  • the heat exchanger may also have a second flow connection between the gas supply device and the second line, such that a gaseous phase of the first medium or a process flow can be introduced from the second line into the gas supply device via the second flow connection.
  • the first flow connection may also connect the gas discharge device to the shell space remotely from the first or second line (in particular at an arbitrary point of the shell of the heat exchanger).
  • the second flow connection to connect the gas discharge device to the shell space remotely from the first or second line (in particular at an arbitrary point of the shell of the heat exchanger).
  • the first and/or the second flow connection it is basically possible for the first and/or the second flow connection to also have a buffer accumulator for a gaseous phase of the first medium, and in particular also a compressor and/or a valve (see also below).
  • a buffer accumulator for a gaseous phase of the first medium and in particular also a compressor and/or a valve (see also below).
  • the compressor By means of the compressor, the first medium can be transported through the respective flow connection.
  • the valve serves for the adjustment or interruption of the flow of the gaseous phase of the first medium.
  • an industrial plant which has a heat exchanger according to the invention and a first component and a first flow connection between the gas discharge device and the first component of the plant, such that a process stream of the plant (e.g. a gaseous phase of the first medium) is introducible from the gas discharge device via the flow connection into the first component.
  • the plant may have a second component and a second flow connection between the gas supply device and the second component, such that a process stream (e.g. a gaseous phase of the first medium) is withdrawable from the second component, and introducible into the gas supply device, via the second flow connection.
  • the first or the second components may each be an apparatus or a planned part of the plant in which the first medium is conducted (e.g. a gas buffer accumulator and/or a compressor) and/or treated in some other way.
  • the first and the second component may furthermore each be a plant part or apparatus from which a gaseous phase of the first medium or a process stream is transported to the gas supply device (e.g. via a line) and/or to which a gaseous phase of the first medium is transported from the gas discharge device (e.g. via a line).
  • the first component may be identical to the second component.
  • a method for operating heat a exchanger uses in particular a heat exchanger according to the invention, wherein a first medium, which has a liquid phase and a gaseous phase, is conducted in a shell space, surrounded by a shell, of the heat exchanger and indirectly exchanges heat with a second medium which is conducted in a tube bundle arranged in the shell space, which tube bundle has multiple tubes for accommodating the second medium, which tubes are helically coiled in multiple tube layers onto a core tube of the heat exchanger, which tube bundle extends along a longitudinal axis of the shell in the shell space, wherein the tube bundle has a multiplicity of inner tube layers, which surround the core tube, and a multiplicity of outer tube layers, which surround the inner tube layers and the core tube, and wherein a part of the gaseous phase is discharged out of the shell space from the region of the inner tube layers (in particular in order to lower a pressure in the shell space there), specifically in particular via the gas discharge
  • the actual pressure distribution may be measured by means of a multiplicity of pressure sensors provided in the shell space, or by means of a fiber-optic sensor laid through the shell space.
  • effects of the pressure on a light-conducting fiber e.g. glass fiber
  • an actual temperature distribution may be measured in the shell space by means of a fiber-optic sensor or by means of at least one light-conducting fiber (e.g. glass fiber) of a sensor of said type. It is conceivable to measure both an actual temperature distribution and an actual pressure distribution by means of a fiber-optic sensor.
  • the fiber-optic sensor or a light-conducting fiber, in particular glass fiber, of the sensor may be laid along the tubes of the tube bundle, such that a 3 D actual temperature distribution can be measured.
  • the temperature of the setpoint temperature distribution is constant in a radial direction, specifically in particular at least at a defined height of the shell space (e.g. at the height of the discharge and/or supply of the gaseous phase) or in a defined shell space section along the longitudinal axis of the shell.
  • a part of the gaseous phase is discharged from the region of the inner tube layers via a multiplicity of inlet openings, and/or the gaseous phase of the first medium is, in the region of the outer layers, supplied via a multiplicity of outlet openings, such that, in particular over the entire length of the tube bundle, the actual pressure distribution or the actual temperature distribution is approximated to a setpoint pressure distribution or setpoint temperature distribution respectively, in the case of which the pressure or the temperature respectively is in each case constant in a radial direction and follows a predefined profile in an axial direction (that is to say along the longitudinal axis).
  • a heat exchanger for the indirect exchange of heat between a first medium, which has a liquid phase and a gaseous phase, and a second medium is disclosed, having
  • a heat exchanger of said type may likewise be refined by means of the features or embodiments described herein.
  • FIG. 1 shows embodiments of the heat exchanger according to the invention in which a gaseous phase is withdrawable from the shell space in the region of the innermost tube layer via the core tube;
  • FIG. 2 shows further embodiments of the heat exchanger according to the invention in which a gaseous phase is introducible into the shell space in the region of the outermost tube layer via the skirt;
  • FIG. 3 shows a further embodiment, in which both the supply and the discharge of the gaseous phase as per FIGS. 1 and 2 is possible;
  • FIG. 4 shows a modification of the embodiment shown in FIG. 3 ;
  • FIG. 5 shows a perspective view of the tube bundle of the heat exchanger shown in FIGS. 1 to 4 ;
  • FIG. 6 shows a multiplicity of different embodiments with regard to flow connections of the gas supply or gas discharge device to components of the heat exchanger or of a plant in which the heat exchanger may be incorporated;
  • FIG. 7 further embodiments with regard to flow connections of the gas supply or gas discharge device to components of the heat exchanger or of a plant in which the heat exchanger may be incorporated.
  • FIGS. 1 to 4 each show an embodiment of a coiled heat exchanger 1 according to the invention.
  • the coiled heat exchanger 1 has in each case a shell 5 , which is preferably cylindrical at least in sections and which surrounds a shell space 6 of the heat exchanger 1 , and a tube bundle 3 , which is arranged in the shell space 6 and which may have multiple tubes 30 which may be helically coiled on a core tube 300 , wherein the core tube 300 is arranged in particular coaxially with respect to a longitudinal axis z of the heat exchanger 1 or of the shell 5 , along which longitudinal axis the shell 5 extends.
  • the tube 30 of the tube bundles 3 are in particular coiled helically onto the core tube 300 in multiple tube layers, wherein the individual tube layers are supported against one another by means of spacer elements 10 , such that the entire weight of the tube layers can ultimately be dissipated through the core tube 300 .
  • the tube bundle 3 therefore correspondingly has, in a radial direction R, an innermost tube layer 4 aa , which is arranged adjacent to the core tube 300 , and an outermost tube layer 4 bb in the radial direction R.
  • the tube layers of the tube bundle 3 may in this case be divided into inner tube layers 4 a and outer tube layers 4 b in accordance with the definition given above.
  • the tube bundle 3 of FIGS. 1 to 4 may for example be formed as per FIG. 5 , wherein here, for the sake of clarity, the gas discharge device 43 and the gas supply device 53 (see below) are not shown.
  • the coiled heat exchanger 1 has an in particular cylindrical skirt 7 , which surrounds the tube bundle 3 .
  • the skirt 7 has an inner side 7 a , which faces toward the tube bundle 3 , in particular the outermost tube layer 4 bb , and an outer side 7 b , which is averted from the inner side 7 a and which faces toward the shell 5 .
  • the skirt 7 serves for preventing a bypass flow in the shell space 6 past the tube bundle 3 .
  • a liquid phase F of a first medium M is applied to the tube bundle 3 from the top by means of a liquid distributor V, which first medium then comes into indirect heat-exchanging contact with a second medium M′ conducted in the tubes 30 of the tube bundle 3 .
  • the liquid distributor V may have multiple arms A, which are fed with liquid F for example via the core tube 300 .
  • liquid distributor V is shown only in FIG. 1 , but is also provided in the embodiments as per FIGS. 2 to 5 and configured in the manner of FIG. 1 .
  • the respective radial direction R is perpendicular to the longitudinal axis z or to the core tube 300 , wherein the longitudinal axis z coincides with the axial direction of the tube bundle 3 .
  • FIG. 1 illustrates two alternative variants, which will be described in more detail below.
  • the gas discharge device 43 of the heat exchanger 1 has at least one discharging flow path 40 for the gaseous phase G with an inlet opening 41 arranged in the shell space 6 in the region of the inner tube layers 4 a , wherein, for example, the at least one discharging flow path 40 is formed by a tube 30 of an inner tube layer 4 a , in particular of an innermost tube layer 4 aa of the tube bundle 3 .
  • the heat exchanger 1 or the gas discharge device 43 may, in a second variant (cf. FIG. 1 ), have a discharging flow path 40 for the gaseous phase G, which discharging flow path runs at least in sections in an interior space of the core tube 300 and has an inlet opening 41 arranged in the shell space 6 in the region of the inner tube layers 4 a , which inlet opening is in the present case formed for example in a wall of the core tube 300 .
  • the discharging flow path 40 by means of the discharging flow path 40 , at least a part of the gaseous phase G of the first medium M can be withdrawn from the shell space, specifically in the present case in the region of the innermost tube layer 4 aa .
  • the actual pressure distribution P generated in FIG. 1 can be generated, which has an as far as possible constant pressure in a radial direction R.
  • Such withdrawal points or inlet openings 41 may, in FIG.
  • valve 8 This applies in particular both to the discharging flow path 40 which has said tube 30 of the inner or innermost tube layer 4 a , 4 aa (first variant), and to the discharging flow path 40 which runs at least in sections in the interior space of the core tube 300 (second variant).
  • the valve 8 is shown in FIG. 1 only for the flow path 40 running in the interior space of the core tube 300 .
  • the valve 8 is preferably adjusted such that an actual temperature distribution measured in the shell space 6 is approximated to a desired setpoint temperature distribution.
  • the closed-loop control may also be performed such that a measured actual pressure distribution is approximated to a desired setpoint pressure distribution.
  • the temperature or the pressure may be measured in the shell space for example in a known manner by means of a light-conducting fiber L or other suitable sensors (see also above).
  • a light-conducting fiber L may for example be laid along the tubes 30 , and is schematically indicated in FIG. 1 .
  • FIG. 2 shows a modification of the embodiment shown in FIG. 1 , wherein, by contrast to FIG. 1 , provision is made for the gaseous phase G not to be withdrawn from the shell space 6 in the region of the inner tube layers 4 a , 4 aa but introduced into the shell space 6 in the region of the outer tube layers 4 b , in particular in the region of the outermost tube layer 4 b.
  • the heat exchanger 1 as per FIG. 2 has a gas supply device 53 with at least one supplying flow path 50 for the gaseous phase G, which in a first variant runs on the outer side 7 b of the skirt 7 , and within the shell space 6 . It is self-evidently also conceivable for a flow path 50 of said type to be laid outside the shell 5 and to then lead through the shell 5 and the skirt 7 . Furthermore, it is alternatively possible, in a second variant which is likewise shown in FIG. 2 , for a flow path 50 of said type to be formed by a tube 30 of an outer tube layer 4 b of the tube bundle 3 , in particular by a tube 30 of an outermost tube layer 4 bb of the tube bundle 3 .
  • the at least one supplying flow path 50 has an outlet opening 51 which, in the present case, is formed in the skirt 7 (or alternatively in said tube 30 of the outer or outermost tube layer 4 b , 4 bb ), such that the introduced gaseous phase G in the present case impinges on the outermost tube layer 4 bb .
  • the pressure in the shell space 6 can be increased, such that, overall, a pressure P which is as far as possible constant in a radial direction R is realized as a result. Also, in FIG.
  • valve 8 specifically in particular both for the supplying flow path 50 which has said tube 30 of the outer or outermost tube layer 4 b , 4 bb and alternatively for the supplying flow path 50 which runs on the outer side 7 b of the skirt 7 .
  • the valve 8 is shown in FIG. 2 only for the flow path 50 running on the outer side 7 b of the skirt 7 .
  • the valve 8 is preferably adjusted such that an actual pressure distribution P measured in the shell space 6 , or alternatively a measured actual temperature distribution, is approximated to a corresponding setpoint pressure distribution or setpoint temperature distribution.
  • FIG. 4 shows a modification of the embodiment shown in FIG. 3 , wherein here, for the closed-loop control of the discharge of the gaseous phase G via the at least one discharging flow path 40 and for the closed-loop control of the supply of the gaseous phase G via the at least one supplying flow path 50 , provision is made for the two flow paths 40 , 50 to be connected in terms of flow by means of a compressor 9 which is controllable in closed-loop fashion, such that a gaseous phase G which is withdrawn from the shell space 6 in the region of the inner tube layers 4 a is variably compressible by means of the compressor 9 and introducible into the shell space 6 again in the region of the outer tube layers 4 b .
  • the gaseous medium G is thus conducted in a circuit.
  • the compressor 9 is shown in FIG. 4 only for the flow path 40 running in the interior space of the core tube 300 and the flow path 50 running on the outer side 7 b of the skirt 7 , though said compressor may self-evidently also be used if the two flow paths 40 , 50 are formed by a tube 30 of an inner or innermost tube layer 4 a , 4 aa and by a tube 30 of an outer or outermost tube layer 4 b , 4 bb.
  • FIGS. 1 to 4 instead of closed-loop control of the supply and discharge of the gaseous phase G, it is self-evidently also possible in FIGS. 1 to 4 for open-loop control of said supply or discharge of the gaseous phase G to be provided.
  • additional flow paths 40 , 50 which, in some embodiments as per FIGS. 1 to 4 , are used in addition to the tube bundle 3 to withdraw a gaseous phase G from the shell space 6 in spatially targeted fashion or introduce a gaseous phase G into the shell space 6 in spatially targeted fashion in order to influence pressure or temperature profiles in targeted fashion
  • FIGS. 6 and 7 show further embodiments of a heat exchanger 1 according to the invention or of a plant 2 which has the heat exchanger 1 , which embodiments relate to the interconnection of the gas discharge and gas supply device 43 , 53 .
  • the heat exchanger 1 may have a first line 411 , via which the first medium M on the shell side is fed (in particular in two-phase form) for example into an upper section of the heat exchanger 1 or into the shell space 6 .
  • the heat exchanger 1 may have a second line 511 , via which the first medium M on the shell side can be withdrawn from the shell space 6 or heat exchanger.
  • the second line 511 may for example be provided at a lower section of the heat exchanger 1 .
  • the gas discharge device 43 may be connected via a first flow connection 410 to the first line 411 , such that a part of a gaseous phase G of the first medium M can be withdrawn from the shell space 6 of the heat exchanger 1 , and fed into the first line 411 , via the gas discharge device 43 and the first flow connection 410 .
  • the gas discharge device 43 may be connected via a first flow connection 410 to the second line 511 , such that a part of the gaseous phase G of the first medium M can be withdrawn from the shell space 6 of the heat exchanger 1 , and fed into the second line 511 , via the gas discharge device 43 and the first flow connection 410 .
  • the gas supply device 53 may be connected via a second flow connection 510 to the first line 411 , such that a part of the gaseous phase G of the first medium M can be fed from the first line 411 into the gas supply device 53 via the second flow connection 510 .
  • the gas supply device 53 is connected via a second flow connection 510 to the second line 511 , such that a part of the gaseous phase G of the first medium M can be fed from the second line 511 into the gas supply device 53 via the second flow connection 510 .
  • the first and the second flow connection 410 , 510 may have a gas buffer accumulator 90 , a compressor 9 and in particular a valve 8 , by means of which the flow of the gaseous phase G of the first medium M can be adjusted or interrupted.
  • the heat exchanger 1 together with the respective gas buffer accumulator 90 , compressor 9 and valve 8 , thus forms an industrial plant 2 or a part of such a plant 2 , in which the first medium M constitutes a process stream.
  • the first medium M on the shell side is a mixture of refrigerants.
  • the first medium M may basically also be a process stream from another plant part of the plant 2 .
  • FIG. 6 combines different embodiments in one figure, that is to say shows all possible flow connections 410 and 510 between the gas supply and the gas discharge device 53 , 43 and the first and the second line 411 , 511 , wherein, however, the gas discharge device 43 is in particular connected only via one of the two stated flow connections 410 to the first line 411 and to the second line 511 .
  • the gas supply device 53 with regard to the two flow connections 510 that are shown.
  • the gas discharge device 43 may be connected to the shell space 6 of the heat exchanger 1 at an arbitrary point (in particular remotely from the two lines 411 , 511 ) via the first flow connection 410 , such that the first medium M is withdrawable from the shell space 6 , and introducible into the shell space 6 again, via the gas discharge device 43 (and in particular via the valve 8 , the gas buffer accumulator 90 and the compressor 9 ).
  • the gas supply device 53 may likewise be connected to the shell space 6 of the heat exchanger 1 at an arbitrary point (in particular remotely from the two lines 411 , 511 ) via the second flow connection 510 , such that the first medium M is withdrawable from the shell space 6 via the second flow connection 510 (in particular via the gas buffer accumulator 90 , the compressor 9 and the valve 8 ), and introducible into the shell space 6 again, via the gas supply device 53 .
  • the flow connections 410 , 510 shown in FIGS. 6 and 7 may self-evidently also be combined with one another in any desired manner.
  • the present invention has the further advantage that existing coiled heat exchangers can be particularly easily retrofitted with said flow paths 40 , 50 , such that, in this case, too, a performance improvement can be achieved.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
US16/031,425 2017-07-10 2018-07-10 Withdrawal/ infeed of gas for influencing radial liquid migration Abandoned US20190011191A1 (en)

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US11236945B2 (en) * 2019-04-02 2022-02-01 Linde Aktiengesellschaft Controllable liquid distributor of a coiled-tube heat exchanger for realizing different liquid loadings
US11634961B2 (en) 2020-03-03 2023-04-25 Petrochina Company Limited Metal-based dissolvable ball seat, setting system and setting method
EP4177556A1 (en) 2021-11-05 2023-05-10 Air Products and Chemicals, Inc. Mitigation of shell-side liquid maldistribution in coil wound heat exchanger bundles
EP4359718A1 (de) * 2021-06-23 2024-05-01 Linde GmbH Regelbare eindüsung zur realisierung unterschiedlicher lokaler kältemittelverteilung

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DE102018000468A1 (de) * 2018-01-22 2019-07-25 Linde Aktiengesellschaft Gewickelter Wärmeübertrager mit Abscheider im Kernrohr

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US11634961B2 (en) 2020-03-03 2023-04-25 Petrochina Company Limited Metal-based dissolvable ball seat, setting system and setting method
EP4359718A1 (de) * 2021-06-23 2024-05-01 Linde GmbH Regelbare eindüsung zur realisierung unterschiedlicher lokaler kältemittelverteilung
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EP4177556A1 (en) 2021-11-05 2023-05-10 Air Products and Chemicals, Inc. Mitigation of shell-side liquid maldistribution in coil wound heat exchanger bundles

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