EP3475642B1 - Verfahren zum betrieb eines rohrbündel-wärmeaustauschers zur erhitzung eines temperatursensiblen konzentrats eines lebensmittelprodukts unter hohem druck und rohrbündel-wärmeaustauscher zur durchführung des verfahrens - Google Patents

Verfahren zum betrieb eines rohrbündel-wärmeaustauschers zur erhitzung eines temperatursensiblen konzentrats eines lebensmittelprodukts unter hohem druck und rohrbündel-wärmeaustauscher zur durchführung des verfahrens Download PDF

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Publication number
EP3475642B1
EP3475642B1 EP17751998.0A EP17751998A EP3475642B1 EP 3475642 B1 EP3475642 B1 EP 3475642B1 EP 17751998 A EP17751998 A EP 17751998A EP 3475642 B1 EP3475642 B1 EP 3475642B1
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EP
European Patent Office
Prior art keywords
concentrate
heat exchanger
tube bundle
inner tubes
support plate
Prior art date
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EP17751998.0A
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German (de)
English (en)
French (fr)
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EP3475642A1 (de
Inventor
Uwe Schwenzow
Ludger LÜTKE SUNDERHAUS
Ulrich ROLLE
Hubert Assing
Ludger Tacke
Dietrich Zimmermann
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GEA TDS GmbH
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GEA TDS GmbH
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Priority to PL17751998T priority Critical patent/PL3475642T3/pl
Publication of EP3475642A1 publication Critical patent/EP3475642A1/de
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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
    • F28D7/16—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
    • F28D7/163—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 with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing
    • F28D7/1669—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 with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing the conduit assemblies having an annular shape; the conduits being assembled around a central distribution tube
    • 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
    • F28F9/0265—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits by using guiding means or impingement means inside the header box
    • 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
    • F28D2021/0042—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for foodstuffs
    • 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
    • F28D2021/0098—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for viscous or semi-liquid materials, e.g. for processing sludge

Definitions

  • the invention relates to a method for operating a tube bundle heat exchanger for heating a temperature-sensitive concentrate of a food product under high pressure according to the preamble of claim 1 and a tube bundle heat exchanger for carrying out the method according to the preamble of claim 5.
  • the invention further relates to a method for control the operation of a tube bundle heat exchanger of the type in question.
  • Temperature-sensitive concentrates are to be understood in particular to mean those substrates which have a high content of proteins and drying agents and little water, which easily denature, which undergo an increase in viscosity during heating or one Gelation subject and are processed under aseptic conditions to a sterile end product.
  • Indirect product heating for example in UHT systems (UHT: ultra-high temperature)
  • UHT ultra-high temperature
  • tube bundle heat exchangers which the heat energy is transmitted through the tube walls of a group of inner tubes.
  • the food product to be treated flows in the inner tubes, while a heat transfer medium, hereinafter referred to as heating medium in the context of the invention, usually water or steam, flows through the annular gap space of a jacket tube, which surrounds the parallel connected inner tubes.
  • a related tube bundle heat exchanger is from the DE 94 03 913 U1 known.
  • the DE 10 2005 059 463 A1 also discloses such a tube bundle heat exchanger for a low pressure level and also shows how a number of tube bundles can be arranged in parallel in this heat exchanger and connected in series through the fluid by means of a connecting bend or connecting fittings.
  • An arrangement in this regard shows Figure 1 this document (state of the art).
  • Particularly temperature-sensitive products such as concentrates, especially those with a high dry matter content, require the product to be precisely and quickly adjusted to the required temperature conditions. This results in the requirement that all partial quantities of a product to be subjected to the heat treatment of the type in question pass through the required same temperature-level curve at the same time and over the same period of time. In other words, this means that all subsets are subject to the same thermal and fluid-mechanical conditions with the same dwell time.
  • the branching problem of the flow in the inlet area of the tube support plates of a tube bundle heat exchanger (e.g. DE 94 03 913 U1 ), as he prefers to use in UHT systems, is dedicated to DE 103 11 529 B3 .
  • the targeted measures proposed under the task specified there relate exclusively to the branching of a product onto the inner tubes of the tube bundle heat exchanger which hold a number of partial quantities of this product, wherein, among other things, a displacement body is provided which is arranged axially symmetrically and concentrically with the tube carrier plate.
  • This prior art thus relates exclusively to a device for influencing the flow area of a tube support plate of a tube bundle heat exchanger in question.
  • the inner tubes are arranged over the entire circular area of the tube support plate, with the exception of a narrowly limited central area, and are generally distributed over more than one partial circle. Under these conditions, flow paths of different lengths for entering and exiting the inner pipes exist both in the entry and in the exit area of the respective tube support plate, that is to say when branching and combining the flow. This alone results in different dwell times for the partial quantities of the product flowing through the respective inner tubes.
  • the WO 2011/085784 A2 proposes to solve the above-described problem of different dwell times in the branching and the unification of the flow, to arrange all the inner tubes of the tube bundle in a circular shape, on a single circle and in an outer channel of the tube bundle heat exchanger designed as an annular space, the inner tubes flowing in parallel in the longitudinal direction of the outer channel and support each end in a tube support plate.
  • This arrangement of the inner tubes is combined with an axially symmetrical displacer which is fixedly arranged concentrically on the tube support plate at the inlet and at the outlet of the product.
  • the respective displacer body extends centrally through an exchanger flange assigned to the tube support plate, the exchanger flange having a connection opening on its side facing away from the associated tube support plate.
  • the end regions of the known tube bundle heat exchanger are, at least in each case adjacent to the outer channel, of mirror-image design and of identical dimensions, this symmetry expressly also encompassing the two displacement bodies and the two annular channels.
  • the annular space-shaped outlet-side channel has a channel passage cross-section at least everywhere in its area between a largest outer diameter of the outlet-side displacer body and the connection opening, which corresponds to a total passage cross-section of all inner tubes with parallel flow.
  • a tube bundle heat exchanger has proven suitable for heating processes of the type in question at the usual, relatively low pressure level.
  • the production of powdered food products, in particular milk products, such as, for example, easily soluble foods for small children, is carried out in many cases by atomizing or spray drying in a so-called drying tower.
  • a concentrate which has previously been concentrated to a certain dry substance content in an evaporator or an evaporator and then warmed to a defined temperature in a heater is atomized into a hot air stream, for example via nozzles, in particular single-substance nozzles.
  • the concentrate emerging from the heater is fed to these so-called pressure atomizing nozzles by means of a high-pressure piston pump, a so-called nozzle pump, with a pressure which can reach up to a maximum of 350 bar.
  • the static of the dryer towers is usually not sufficient to support the heavy high-pressure piston pump and to install it in the immediate vicinity of the pressure atomizer nozzles, which would be desirable for technological and procedural reasons.
  • a high-pressure piston pump located in the vicinity of the pressure atomizer nozzles would work in this area, the so-called hot space in the head space of the drying tower, at ambient temperatures which are between 75 and 80 ° C. and would require aseptic operation. A further thermal inactivation of microorganisms would also not be possible.
  • the high-pressure piston pump has hitherto been arranged in the lower region of the drying tower.
  • a significant difference in height between the high-pressure piston pump and the pressure atomizer nozzles is bridged via a riser, which, according to plan or inevitably, also functions as a hot holding section.
  • the end product In order to ensure that the powdered food product is stored for as long and as hygienically as possible, the end product must have good solubility and be as germ-free as possible.
  • the necessary sterility results from the killing of microorganisms as far as possible for the concentrate escaping from the heater if this is carried out with a suitable temperature and holding time profile and if the riser to the pressure atomizer nozzles, which acts as a heat retention section, is taken into consideration.
  • so-called "low heat powder” a temperature of maximum 77 ° C, of so-called “high heat powder” of approx. 85 ° C and of so-called “ultra high heat powder” of up to 125 ° C is required.
  • the inevitable mean residence time of the concentrate in the riser after high pressure treatment in connection with a hot temperature has an undesirable effect on the solubility of the end product.
  • the long heat retention in the riser can lead to an uncontrolled denaturation of the concentrate.
  • the average residence time of the concentrate is 42 seconds when it is conveyed in a 30 m long riser pipe with a diameter of DN50 with a volume flow of 5,000 liters / h. This usually means a reduction in the quality of the end product. Denaturation in this regard can, for example, influence the powder quality of baby food in such a way that its complete solubility is no longer ensured and an unacceptable lump formation occurs in the prepared baby food.
  • the temperature in the riser and thus up to the pressure atomizer nozzles must not be higher than 65 to 68 ° C.
  • the long riser therefore limits the permissible temperature there.
  • the procedural problem is also not solved, which consists in subjecting a concentrate, for example for atomizing drying, immediately before the pressure atomizer nozzles to a treatment by means of which the tendency to denaturate the concentrate, to increase the viscosity in the concentrate or to gel the Concentrate and deposits of the same reduced and a germ-free, ie microbiologically perfect end product is ensured.
  • the object of the present invention is therefore to overcome the disadvantages of the prior art and to provide a method of the generic type and a tube-bundle heat exchanger for carrying out the method which, at a high pressure level, have a tendency to denaturate the concentrate and to increase the viscosity in the concentrate or to reduce the gelation of the concentrate and its deposits and a germ-free, ie Ensure the microbiologically perfect end product.
  • the present invention is based on a tube bundle heat exchanger, as it is in its basic structure in the DE 10 2013 010 460 A1 is described.
  • This has at least one tube bundle, which consists of a number of inner tubes connected in parallel and inside each of which the concentrate flows.
  • the inner tubes are circular, arranged on a single circle, they are supported at the ends in a first and a second tube support plate and they extend in the longitudinal direction of an outer channel designed as an annular space through which a heating medium flows.
  • the inner tubes are preferably arranged in the outer edge region of the respective tube support plate.
  • the inner tubes have a common inlet, which is formed in a first exchanger flange connected to the first tube carrier plate in the form of a first connection opening arranged centrally there with respect to an axial axis of symmetry of the tube bundle, and they have a common outlet, which is in one with the second Tube carrier plate connected second exchanger flange is formed in the form of a second connection opening also arranged centrally there. Furthermore, the inner tubes end in a fluid-permeable manner at least on the outlet side in a circumferential annular space which is formed in the second tube carrier plate and / or the second exchanger flange.
  • the circumferential annulus is fluidly connected to the second connection opening via an annulus-shaped outlet-side channel, and the annulus-shaped outlet-side channel is delimited radially on the outside by the second exchanger flange and radially on the inside by an axially symmetrically arranged displacer body.
  • the annulus-shaped outlet-side channel has a defined extension length and a defined length-dependent course of its channel passage cross sections.
  • the feature with regard to the arrangement of a number of inner tubes with parallel flow is to be understood as an arrangement which, regardless of the number of inner tubes, for example 4 to 19 or more in number, does not occupy an entire circular cross section of the tube carrier plate. Rather, all inner tubes are arranged on said single circle, which leaves an inner area, not just a limited center, unoccupied by inner tubes.
  • This arrangement makes it possible for the inner channel, formed by the inner tubes arranged in the form of a ring and arranged on a single circle, in the flow direction, to be designed in the form of the circumferential annular space following the inner tubes.
  • the basic idea of the invention is to first increase the pressure of the concentrate to a maximum pressure of 350 bar, as is necessary for a treatment of the concentrate following heating.
  • the concentrate is then heated at this high pressure level.
  • This heating is combined with a defined fluidic shear stress, which is provided in the course of the heating and / or preferably immediately after the heating.
  • the defined fluidic shear stress which does not require any moving elements and / or the supply of external energy, takes place in the respective inner tube with its defined passage cross-section and its defined flow-through length and with an increased flow rate and / or preferably in an annular space-shaped outlet-side connecting to the inner tubes Channel.
  • the latter has a defined extension length and a defined length-dependent course of its channel passage cross sections and is flowed through with the increased flow velocity.
  • the increased flow speed be up to a maximum of 3 m / s.
  • the disadvantageous keeping of pressure between the increase in pressure to the high-pressure level, which is followed by the low-pressure heating, and a further treatment of the concentrate following the increase in pressure, which has hitherto been accepted in the prior art, is virtually eliminated and succeeds immediately this further treatment, for example pressure atomization, to define the heating or to set up the heat treatment in a reproducible manner.
  • this further treatment for example pressure atomization
  • the desired heat loads the mass flow and the ingredients can be defined.
  • the invention further proposes a tube-bundle heat exchanger for carrying out the method, which, in a manner known per se, has, inter alia, at least one tube bundle which consists of a number of inner tubes through which the concentrate flows in parallel, which are arranged in an annular manner and in a single circle Support each end in a first and a second tube support plate.
  • the inner tubes end in a fluid-permeable manner at least on the outlet side in a circumferential annular space which is formed in the second tube carrier plate and / or the second exchanger flange.
  • the means for the defined fluidic shear stress of the concentrate consist of an annular channel on the outlet side, which is fluidly connected to the outlet of the circumferential annular space, which is formed in the second tube support plate and / or the second exchanger flange, and fluidly connected to the second connection opening.
  • the annular space on the outlet-side channel is delimited radially on the outside by the second exchanger flange and radially on the inside by an displacer body arranged axially symmetrically on the second tube support plate.
  • the annular space has in the most general case, the outlet-side channel has a defined extension length and a defined course of its channel passage cross sections which is dependent on the extension length.
  • the first connection opening is seamless, i.e. in alignment and without changing the cross-section, into an inner passage of a connecting bend or a connecting fitting which, viewed in the direction of flow, is arranged upstream of the first connection opening.
  • the second connection opening is seamless, i.e. aligned and without changing the cross-section, into an inner passage of a connecting bend or a connecting fitting, which, viewed in the direction of flow, is arranged downstream of the second connection opening.
  • the respective connection bend / connection fitting reaches into the assigned exchanger flange to a certain extent by at least the wall thickness of the person Connection bend / connection fitting at this point, namely by a depth of penetration.
  • the connecting bend or the connecting fitting is welded to the associated exchanger flange on the outside with a high-pressure-resistant, multi-layer, orbital first weld seam, preferably a so-called fillet weld, and on the inside with an orbital second weld seam, preferably a so-called V-seam.
  • the end of each inner tube on the outlet side is welded all around to the associated tube carrier plate with a third weld seam, preferably a fillet or corner seam.
  • the channel passage cross sections of the annular-shaped outlet-side channel are constant over the entire length of the extension.
  • This desirable equal treatment is further promoted by the fact that the increased flow velocity through the entire tube bundle heat exchanger is as uniform as possible up to the end of the defined shear stress of the concentrate, a further embodiment providing in this regard that the channel cross-section of the annular-shaped outlet-side channel corresponds to the total cross-section of all inner tubes with parallel flow.
  • the invention proposes a method for controlling the operation of a tube bundle heat exchanger, the control parameters for the heating and the defined fluidic shear stress being determined by the properties of the concentrate to be heated and the physical boundary conditions.
  • the properties of the concentrate to be heated are understood to mean its volume flow, viscosity, pressure, temperature and dry substance concentration, and the physical boundary conditions are understood to mean pressure and temperature at the location of a treatment of the concentrate which follows the defined fluid mechanical shear stress.
  • the control parameters, based in each case on the concentrate are the pressure, an outlet-side heating temperature, the increased flow speed and an intensity of the defined fluidic shear stress, generated by a specific design of the annular-shaped outlet-side channel.
  • the method according to the invention and the method for controlling the operation of a tube bundle heat exchanger can advantageously be applied to the atomizing drying of concentrates in drying plants with a drying tower, the concentrate then immediately after heating and the defined fluidic shear stress, i.e. is immediately transferred to a place where it is atomized.
  • a transfer time for the direct transfer is determined by a corresponding fluidically effective distance between the means for carrying out the defined fluidic shear stress and the location of the pressure atomization.
  • directly in the ideal case means that the exit of the means for carrying out the defined fluidic shear stress immediately, i.e. without the interposition of a pipeline section into which the atomizer nozzle (s) opens or is brought up to it.
  • a tube bundle heat exchanger 100 of which a tube bundle 100.1 is shown, has between an inlet E penetrated by an entire concentrate P and an outlet A (see Figure 1 ) have congruent flow paths for all subsets of the concentrate P which branch and unite between the latter.
  • This is achieved objectively in that, in the case of the tube bundle 100.1, which consists of a group of inner tubes 300 connected in parallel and flowed through by the concentrate P on the inside in each case, all the inner tubes 300 are annular, on a single circle K ( Figure 3 ) and are arranged in an outer channel 200 * designed as an annular space and extend in the longitudinal direction thereof and are supported at the ends in a first and a second tube support plate 700, 800.
  • the inner tubes 300 are arranged in the largest possible circumferential area of the tube support plate 700, 800, preferably evenly distributed over the circumference of the circle K.
  • a number N ( Figure 4 ) the inner tubes 300, which extend axially parallel to an outer jacket 200.1 of the outer channel 200 * through the latter, together forming an inner channel 300 *, are passed through the end of the first tube support plate 700 and the second tube support plate 800 (both also referred to as tube mirror plate) and there at their respective Pipe outer diameter and welded to its respective end face by means of a third weld S3 high pressure resistant.
  • the inner tubes 300 ( Figure 1 ) have on the one hand the common inlet E, which is formed in a first exchanger flange 500 connected to the first tube support plate 700 in the form of a first connection opening 500a arranged centrally there with respect to an axial axis of symmetry a of the tube bundle 100.1, and on the other hand the inner tubes 300 have the common outlet A, which is formed in a second exchanger flange 600 connected to the second tube support plate 800 in the form of a second connection opening 600a arranged centrally there.
  • the first tube support plate 700 is screwed to the assigned first exchanger flange 500 and the second tube support plate 800 is screwed to the assigned second exchanger flange 600 in a pressure-resistant manner.
  • a number of screw connections ( Figures 2, 3 ) are provided, which preferably consist of screw bolts 1100 anchored in the tube support plates 700, 800 in connection with nuts 1200 and washers 1300.
  • 8 such screw connections 1100, 1200, 1300 are provided.
  • the first exchanger flange 500 is sealed against the first tube support plate 700 by a flange seal 900. The same applies to the second exchanger flange 600 and the second tube support plate 800.
  • the embodiment shown are the end regions of the tube bundle 100.1 of the tube bundle heat exchanger 100, with the exception of an inlet and outlet displacement body 11, 12 and its respective immediate vicinity in the region of the exchanger flange 500, 600, each following the outer channel 200 *, preferably mirror image of identical shape and dimensionally identical. Because the present invention relates to the downstream side of the tube bundle 100.1, the following description can primarily refer to the outlet-side end region ( Figure 4 ) limit and the corresponding reference numerals of the other end range are only given.
  • the structure of the entry-side area is derived from the construction of the exit-side area.
  • the connection opening 600a, 500a merges seamlessly into an inner passage of the connection bend / connection fitting 1000, which, viewed in the flow direction, is arranged downstream of the second connection opening 600a or upstream of the first connection opening 500a.
  • connection bend / connection fitting 1000 engages to a certain extent in the assigned exchanger flange 600, 500 to ensure the necessary high-pressure strength, and does so with an engagement depth t, and is on the outside with the exchanger flange 600, 500 with a high-pressure-resistant, multi-layered first weld S1, preferably a fillet weld, and welded on the inside with a second weld S2, preferably a V-seam.
  • the end of each inner tube 300 is welded all around on the outlet side into the associated tube support plate 800, 700 with the third weld seam S3, preferably a corner seam.
  • the tube bundle heat exchanger 100 is composed of more than one tube bundle 100.1.
  • the tube bundle 100.1 consists of the outer jacket 200.1 delimiting the outer channel 200 * with the first tube support plate 700 arranged on the right-hand side with respect to the illustration, and the second tube support plate 800 arranged in the same way on the left-hand side.
  • a first connection piece 400a and in the area of the right-hand end of the outer casing 200.1 a second connection piece 400b is provided on the latter for the application of a heating medium M.
  • the outer channel 200 * for the heating medium M is delimited from the inside by an inner jacket 200.2.
  • the inner tubes 300 terminate in a circumferential annular space R (at least on the outlet side) Figure 4 ), which is formed in the second tube support plate 800 and / or the second exchanger flange 600.
  • the circumferential annular space R is via an annular outlet side Channel 600b fluidly connected to the second connection opening 600a.
  • the annulus-shaped outlet-side channel 600b is delimited radially on the outside by the second exchanger flange 600 and radially on the inside by the outlet-side displacement body 12 arranged axially symmetrically on the second tube support plate 800.
  • the annulus-shaped outlet-side channel 600b has a defined extension length L and a defined length-dependent course of its channel passage cross sections A S.
  • the inlet side of the tube bundle 100.1 of the tube bundle heat exchanger 100 ( Figure 1 ), adequate to the outlet side, in the form of an annular-shaped inlet-side channel 500b, which is delimited radially on the outside by the first exchanger flange 500 and radially on the inside by the inlet-side displacement body 11 arranged symmetrically on the first tube support plate 700.
  • this is not aimed at on the inlet side; it is located in the inner tubes 300 and preferably in the annulus-shaped outlet-side channel 600b.
  • a medium increased flow velocity in the inner tube 300 and thus in the inner channel 200 * is marked with v ( Figures 1 . 4 ).
  • the annulus-shaped outlet-side channel 600b has, at least everywhere in its area between a largest outer diameter of the outlet-side displacer 12 and the second connection opening 600a, the defined extension length L and, in the most general case, the defined length-dependent course of its channel passage cross sections A S.
  • the method according to the invention for operating a tube bundle heat exchanger 100 for heating a temperature-sensitive concentrate P under a high pressure p is distinguished in that, on the one hand, the concentrate P acts on it Flow paths of the tube bundle heat exchanger 100 are designed in such a way that the concentrate P can be pressurized with the pressure p up to a maximum of 350 bar.
  • the tube bundle heat exchanger 100 is operated at this pressure p and an outlet-side heating temperature T in such a way that the increased flow velocity v of the concentrate P in the inner tubes 300 and / or in the annular-shaped outlet-side channel 600b is provided to generate a defined fluidic shear stress of the concentrate P. which is up to a maximum of 3 m / s ( Figure 4 ).
  • the tube-bundle heat exchanger 100 which is designed as a high-pressure heat exchanger, has on the output side means for defined fluid-mechanical shear stress on the concentrate P being conveyed, these means being effective without mechanical elements and / or supply of external energy purely in terms of fluid mechanics through defined passage cross-sections, defined lengths of the flow paths and defined increased flow velocities are.
  • the means for the defined shear stress of the concentrate P preferably consist in the annular space-shaped outlet-side channel 600b, which on the one hand has the exit of the circumferential annular space R, which is formed in the second tube support plate 800 and / or the second exchanger flange 600, and on the other hand has the second connection opening 600a connected is.
  • the annulus-shaped outlet-side channel 600b has the defined extension length L and the defined course of its channel passage cross sections A S which is dependent on the extension length L.
  • the channel passage cross sections A S are constant over the entire extension length L.
  • This desirable equal treatment is further promoted in that the increased flow velocity v through the entire tube bundle heat exchanger 100 or the respective tube bundle 100.1 is as uniform as possible until the end of the defined shear stress of the concentrate P, a further embodiment providing in this regard that the channel passage cross section A S of the annular outlet-side channel 600b corresponds to the total passage cross section NA i of all inner tubes 300 through which flow occurs in parallel.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Geometry (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Food Preservation Except Freezing, Refrigeration, And Drying (AREA)
  • General Preparation And Processing Of Foods (AREA)
  • Details Of Heat-Exchange And Heat-Transfer (AREA)
EP17751998.0A 2016-06-23 2017-06-16 Verfahren zum betrieb eines rohrbündel-wärmeaustauschers zur erhitzung eines temperatursensiblen konzentrats eines lebensmittelprodukts unter hohem druck und rohrbündel-wärmeaustauscher zur durchführung des verfahrens Active EP3475642B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL17751998T PL3475642T3 (pl) 2016-06-23 2017-06-16 Sposób działania wymiennika ciepła w postaci wiązki rur do nagrzewania wrażliwego na temperaturę koncentratu produktu spożywczego pod wysokim ciśnieniem i wymiennik ciepła w postaci wiązki rur do przeprowadzenia tego sposobu

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016007637.2A DE102016007637B4 (de) 2016-06-23 2016-06-23 Verfahren zum Betrieb eines Rohrbündel-Wärmeaustauschers zur Erhitzung eines temperatursensiblen Konzentrats eines Lebensmittelprodukts unter hohem Druck und Rohrbündel-Wärmeaustauscher zur Durchführung des Verfahrens
PCT/EP2017/000702 WO2017220194A1 (de) 2016-06-23 2017-06-16 Verfahren zum betrieb eines rohrbündel-wärmeaustauschers zur erhitzung eines temperatursensiblen konzentrats eines lebensmittelprodukts unter hohem druck und rohrbündel-wärmeaustauscher zur durchführung des verfahrens

Publications (2)

Publication Number Publication Date
EP3475642A1 EP3475642A1 (de) 2019-05-01
EP3475642B1 true EP3475642B1 (de) 2020-01-22

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DE (1) DE102016007637B4 (es)
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DE9403913U1 (de) * 1994-03-09 1994-05-05 Gea Finnah Gmbh Rohrbündel-Wärmetauscher
DE10256232B4 (de) * 2002-12-02 2004-10-21 Tuchenhagen Dairy Systems Gmbh Vorrichtung zur Verlängerung der Standzeit von Rohrbündel-Wärmeaustauschern in indirekt beheizten UHT-Anlagen für Nahrungsmittel
DE10311529B3 (de) * 2003-03-17 2004-09-16 Tuchenhagen Dairy Systems Gmbh Vorrichtung zur Einflussnahme auf den Anströmbereich einer Rohrträgerplatte eines Rohrbündel-Wärmeaustauschers
DE102005059463B4 (de) * 2005-12-13 2009-12-24 Gea Tds Gmbh Vorrichtung zur Einflussnahme auf die Strömung im Bereich einer Rohrträgerplatte eines Rohrbündel-Wärmeaustauschers
DE102010004418A1 (de) * 2010-01-13 2011-07-14 GEA TDS GmbH, 31157 UHT-Anlage zur Wärmebehandlung von temperatursensiblen Lebensmittelprodukten und Verfahren zur Wärmebehandlung von temperatursensiblen Lebensmittelprodukten in einer UHT-Anlage
EP2909558A1 (en) * 2012-10-17 2015-08-26 Tetra Laval Holdings & Finance SA A tube holding element
DE102013010460A1 (de) * 2013-06-22 2014-12-24 Gea Tds Gmbh Vorrichtung zur Einflussnahme auf den Abströmbereich einer Rohrträgerplatte eines Rohrbündel-Wärmeaustauschers
DE102014012279B3 (de) * 2014-08-22 2015-08-20 Gea Tds Gmbh Krümmer für einen Rohrbündel-Wärmeaustauscher für große Produktdrücke, Herstellverfahren für einen und Rohrbündel-Wärmeaustauscher mit einem solchen Krümmer und Verwendung eines Rohrbündel-Wärmeaustauschers für große Produktdrücke mit einem solchen Krümmer in einer Zerstäubungstrocknungsanlage

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WO2017220194A4 (de) 2018-02-15
DE102016007637B4 (de) 2020-02-20
JP2019529849A (ja) 2019-10-17
DE102016007637A1 (de) 2017-12-28
AU2017280491B2 (en) 2020-10-29
JP6806803B2 (ja) 2021-01-06
PL3475642T3 (pl) 2020-08-24
AU2017280491A1 (en) 2019-02-07
ZA201900437B (en) 2019-10-30
CL2018003709A1 (es) 2019-05-10
EP3475642A1 (de) 2019-05-01
WO2017220194A1 (de) 2017-12-28
NZ750017A (en) 2020-06-26
DK3475642T3 (da) 2020-04-27

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