EP1742006A1 - Procédé et dispositif de guidage du fluide dans les conduits d'un échangeur de chaleur à tubes pour le traitement térmique des suspensions - Google Patents

Procédé et dispositif de guidage du fluide dans les conduits d'un échangeur de chaleur à tubes pour le traitement térmique des suspensions Download PDF

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Publication number
EP1742006A1
EP1742006A1 EP06011990A EP06011990A EP1742006A1 EP 1742006 A1 EP1742006 A1 EP 1742006A1 EP 06011990 A EP06011990 A EP 06011990A EP 06011990 A EP06011990 A EP 06011990A EP 1742006 A1 EP1742006 A1 EP 1742006A1
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EP
European Patent Office
Prior art keywords
tube
tube bundle
flow
arrangement according
distributor
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP06011990A
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German (de)
English (en)
Other versions
EP1742006B1 (fr
Inventor
Ludger Tacke
Norbert Hidding
Josef Tenspolde
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.)
GEA TDS GmbH
Original Assignee
Tuchenhagen Dairy Systems 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 Tuchenhagen Dairy Systems GmbH filed Critical Tuchenhagen Dairy Systems GmbH
Priority to PL06011990T priority Critical patent/PL1742006T3/pl
Publication of EP1742006A1 publication Critical patent/EP1742006A1/fr
Application granted granted Critical
Publication of EP1742006B1 publication Critical patent/EP1742006B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • 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
    • F28F9/027—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 distribution pipes
    • F28F9/0275—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 distribution pipes with multiple branch pipes
    • 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
    • F28D7/1607—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 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
    • F28F19/00—Preventing the formation of deposits or corrosion, e.g. by using filters or scrapers
    • 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
    • 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
    • F28F9/26—Arrangements for connecting different sections of heat-exchange elements, e.g. of radiators

Definitions

  • the invention relates to a method for flow guidance in tube bundle heat exchangers for the thermal treatment of suspensions, which include lumpy and / or long-fiber components, according to the preamble of claim 1 and an arrangement for carrying out the method according to the preamble of the independent claim.
  • the known tube bundle heat exchangers have in common that the isolated in the inner tubes of the respective tube bundles partial flows of the inner channel are combined at the outlet of the tube support plate and this combined total flow is supplied together via the connected connection sheet the adjacent tube bundle. There, in the entry region of the tube bundle, this total flow is again separated into partial flows in the inner tubes that are streamed there.
  • the product to be thermally treated in the shell-and-tube heat exchanger is such with fibrous admixtures, for example juices with pulp
  • deposits may occur at the inlet openings of the inner tubes of the tube carrier plate.
  • the treatment at relatively high temperatures favor the agglomeration of fibers and the formation of pulp.
  • These store preferably at the webs between the multiple parallel arranged inner tubes and at the transverse to the flow direction oriented surfaces of the tube support plate and can lead to blockages there. Remedy here measures, as in the aforementioned WO 20041083 761 A1 are provided in the critical inflow of the respective pipe support plate.
  • suspensions containing particulate and / or long-fiber constituents, wherein the fiber lengths can reach up to 100 mm.
  • suspensions are for example in the context of methods for energy production by biofermentation.
  • a fermentation tank in which the biofermentation takes place, fed a suspension continuously, for example, this suspension consists essentially of corn and manure or whole plant silage (GPS) and manure or grass silage and manure. The fermentation reaction provides so-called.
  • Biogas which consists for the most part of methane and a (one) coupled to a generator for generating electricity gas piston engine (gas turbine) is supplied.
  • gas piston engine gas turbine
  • the liquid manure essentially forms the continuous phase, while the disperse phase through the maize or the other vorg. lumpy constituents and possibly other particulate constituents, such as lumpy foods and their waste products and other long-fiber constituents is formed.
  • the above-mentioned biofermentation in the fermenter requires a certain optimum reaction temperature (fermentation temperature).
  • the continuous supply of suspension consisting essentially of the above enumerated products to be fermented means a disturbance of the reaction in Fermenter, which inevitably results from feed-related temperature and concentration changes and then particularly significant, for example, if in the cold season, the supplied suspension is not sufficiently preheated to the fermentation temperature in the fermenter or can be.
  • a heating device is arranged in the interior of the fermenter. This can be formed in a cylindrical configuration of the fermentation as a heating wall, which is then preferably elevated stands on the bottom of the fermenter ( DE 202 18 022U1 ). Another embodiment provides in this regard, to arrange heating pockets on the inner wall of the fermenter.
  • a first approach provides that the total flow of a lumpy and / or fibrous suspension is separated before entering the tube bundle heat exchanger in a number of sub-streams.
  • the partial streams are generated in each case with a distance which is at least as great as the greatest length of the fibrous constituents of the suspension.
  • a third approach is that the individual streams separated, each separated, are passed through the entire shell and tube heat exchanger. It is in the proposal according to the invention in this regard, therefore, in each case to a single deflection of the partial flow, seen in the flow direction, in front of and behind the respective inner tube.
  • the partial flows of all parallel-connected inner tubes of a tube bundle are first combined, and the resulting total flow is then deflected and fed to the next tube bundle as the total flow.
  • the separation of the total current in one of the number of inner tubes corresponding number of partial flows is then carried out, as is known, by acting as a distributor tube support plate.
  • the proposed arrangement is also characterized by three basic approaches.
  • the first approach is that, viewed in the flow direction, the first tube bundle upstream of an inlet and distribution device with a distributor body, which forms a distributor space on the inside.
  • the second solution concept includes that the distributor space is separately connected to each inner tube of the first tube bundle via a respective distributor tube from a group of distributor tubes, wherein the distance of adjacent distributor tubes is at least as long as the largest length of the fibrous components.
  • each inner tube of a tube bundle is separately connected to an associated inner tube of the following tube bundle via a connecting bend from a group of connecting bend of the connecting fitting.
  • the separation is made in the respective partial flows of the inner tubes, which is provided in tube bundle heat exchangers according to the prior art only in the region of the raw plate of the first tube bundle.
  • By dimensioning the distances of adjacent, emanating from the distribution space distribution pipes so-called. "Bridging" is largely avoided by langturige components and by the separate connection of each inner tube of the first tube bundle with the distributor space via a respective manifold from a group of distribution pipes is a clear feed ensures each of these inner tubes, which is eliminated in the tube bundle heat exchangers of the prior art critical inflow region of the tube support plate of the first tube bundle.
  • An advantageous embodiment of the arrangement according to the invention further provides that the respective partial flow has to overcome through the inner tubes from the distributor space to the entry into an outflow and collection device fed by all inner tubes of the last tube bundle equivalent or approximately equivalent flow resistance.
  • the relevant design of all partial flow paths ensures a uniform flow through all parallel connected areas of the tube bundle heat exchanger and uniform thermal treatment of these parallel partial flows. It is achieved that on the way through the entire shell-and-tube heat exchanger separately guided partial flows of the interconnected inner tubes experience the same residence time in the tube bundle heat exchanger and thus treated uniformly thermally. Leading or lagging streams with different Exit temperatures and solids concentrations are thus avoided.
  • a first shell-and-tube heat exchanger and a second shell-and-tube heat exchanger are connected in parallel to the inlet and distribution device.
  • the inner tubes of the respective last tube bundle open into an outlet and collection device with a collecting body, which forms a collecting space on the inside.
  • This embodiment relates both to a single shell-and-tube heat exchanger arrangement and to one in which two shell-and-tube heat exchangers are connected in parallel.
  • the design of the outlet and collection device designed according to a further proposal is particularly simple when the collecting body is designed as an elongated hollow cylinder.
  • the collecting body in the region of the connection fittings on one side of the tube bundle heat exchanger initially substantially vertically ascending and then laid down substantially vertically descending provides the inner surface of the inner tubes.
  • the outlet and collection device acts in this case as a so-called. Flow tube, the necessary length is to install space-saving by the proposed installation, and on the other hand as a siphon to prevent unwanted idling of the tube bundle heat exchanger.
  • the distributor body is designed as an elongate hollow cylinder with an inner diameter D, if the group of distribution pipes emanating from the distributor body is furthermore arranged in the longitudinal direction of its branch pipe stubs and if the distributor pipes are arranged inside their group each have an axial distance a from each other, which is equal to or greater than the inner diameter D.
  • the latter is expediently carried out about as large as the largest length of the fibrous constituents of the suspension.
  • the aforementioned dimensioning of the distributor body creates favorable conditions for long fibers not being able to lay over the intermediate region between two distributor tubes in the sense of a so-called "bridge formation".
  • Run as a further embodiment of the arrangement according to the invention provides, the longitudinal axis of the manifold body parallel to the tube bundle heat exchanger and the group of manifolds in the region of their branch pipe stubs in a meridian plane of the manifold body, the latter perpendicular to an assembly plane of the tube bundle heat exchanger stands, then the distributor body provides space for a second group of distribution pipes, which can supply a second shell-and-tube heat exchanger if required.
  • each distributor pipe has a shut-off device in the region of its branch pipe socket opening out at the distributor body, as is also provided, then each inner pipe can be used individually and independently of the others Shut off.
  • This shut-off option allows the flushing or flushing of each inner tube, if necessary.
  • This shut-off device can be operated independently of the others either manually or remotely controlled optional. The actuation is expediently controlled as a function of a pressure of the suspension which is significant for the flow through the inner tube. To measure this pressure, a connection for a pressure measuring device is provided on each distributor pipe, viewed in the flow direction, behind the respective shut-off device. Due to the above configuration, each individual inner tube can be purposely flushed or flushed separately, if required, while all other inner tubes are shut off.
  • a clogged inner tube leads to a suitable measuring point to a pressure increase, which either generates an alarm message or causes an automatic flushing of the clogged inner tube, while all other inner tubes or partial streams are shut off or interrupted in the course of this Freiêtens.
  • the distributor body has, as another embodiment provides, at its end facing away from its inflow end on a closable by means of a shut-off flushing port.
  • the distributor body can be flushed through in its longitudinal direction and the transverse flow generated thereby allows flushing of the branch pipe outlets leading from the distributor body to the respective inner pipes, whereby the fibers possibly deposited there are effectively removed and discharged via the flushing connection.
  • the shut-off device is expedient to operate manually or remotely, so that the latter variant in conjunction with the vorg. Pressure measurement allows the greatest possible automation of the through- or Freei Crowvorganges.
  • connection fitting maps an arrangement pattern of the inner tubes complementary in their connecting flange in the two tube carrier plates of adjacent tube bundles to be respectively tightly connected, the connection fittings produce the flow connection between the respective inner tubes at the ends of two adjacent tube bundles on the one hand and at the subsequent ends of the adjacent tube bundles on the other hand, and that the respective flow path through the respective two connection fittings between the adjacent tube bundles always has the same flow resistance in the sum ,
  • This measure ensures that regardless of the number of series-connected, parallel tube bundles alone, the deflection is configured from one to the other tube bundle that present in each relevant portion of the tube bundle heat exchanger equivalent flow resistance and thus on the inner tubes to each contemplated tube bundle same flow conditions and thus the same residence times are present.
  • a particularly useful arrangement in this respect is further achieved in that a number of four to seven, preferably four, inner tubes are provided in a tube bundle.
  • connection fitting In a preferred number of four inner tubes in the tube bundle results in a particularly simple embodiment of the connection fitting, if these inner tubes, as another proposal provides, are distributed evenly distributed on a common pitch diameter such that two adjacent tube bundles are connected to only two different connection arc , wherein two long, same connecting arc the four outer inner tubes and two short, equal connecting arc associated with the four inner inner tubes.
  • the arrangement according to the invention for guiding the flow in tube bundle heat exchangers is not only suitable for particularly effectively heating the products to be fermented outside the fermenter in order to ensure a sufficient fermentation temperature, but also in contrast to "internal" and “external” heating devices according to the prior art
  • the technology is particularly well suited, for example, to protect the fermented products in the fermenter from overheating.
  • the products to be fermented are taken from the fermenter in the partial stream and circulated through the tube bundle heat exchanger according to the invention, with well water preferably being used as the heat transfer medium (cooling medium).
  • the heat transfer medium cooling medium
  • a tube bundle heat exchanger 100 which is generally composed of a multiplicity of tube bundles 100.1 to 100.n, wherein 100.i denotes an arbitrary tube bundle (see FIG DE-U-94 03 913 ), consists in its middle part of an outer channel 200 * limiting outer shell 200 with respect to the display position, left side disposed fixed bearing side technicallymantelflansch 200a and a right side arranged loslager facultyenareamantelflansch 200b.
  • a first transverse channel 400a * bounded by a first housing 400.1 with a first connecting piece 400a closes and the outer jacket flange 200a adjoins a second transverse channel 400b * bounded by a second housing 400.2 with a second connecting branch 400b.
  • a number of axially parallel to the outer shell 200 through the outer channel 200 * extending, together an inner channel 300 * forming inner tubes 300, starting with four and then rising to nineteen and possibly more in number, are each end in a fixed bearing side tube support plate 700th or a loslager chandelieren pipe support plate 800 (both also referred to as tube mirror plate) supported and welded at its pipe outside diameter in this, this overall arrangement introduced via an unspecified opening on the second housing 400.2 in the outer shell 200 and a festlager facultyen Ausauscherflansch 500 with the second housing 400.2 is clamped together with the interposition of one flat gasket 900 (fixed bearing 500, 700, 400.2).
  • the two housings 400.1, 400.2 are likewise sealed off from the respectively adjacent outer jacket flange 200b, 200a by a flat gasket 900, the first housing 400.1 arranged on the right side being connected to the outer jacket 200 via a replacement bearing 600 with the interposition of an O-ring 910 against the left arranged fixed bearing 500, 700, 400.2 is pressed.
  • the loose bearing tube carrier plate 800 engages through an unspecified bore in the loose bearing side Ausauscherflansch 600 and is compared to the latter their seal by means of the dynamically stressed O-ring 910, which also seals the first housing 400.1 statically against the loslager facilityen Ausauscherflansch 600.
  • the latter and the loose bearing tube support plate 800 form a so-called.
  • Floating bearing 600, 800 which allows the changes in length of welded in the loslager chandelieren tube support plate 800 inner tubes 300 due to temperature change in both axial directions.
  • the inner tubes 300 based on the display position, either from left to right or vice versa of a product P are flowed through, wherein the average flow velocity in Inner tube 300 and thus in the inner channel 200 * is marked with v.
  • the cross-sectional interpretation is usually such that this mean flow velocity v is also present in a connecting sheet 1000, which is connected on the one hand to the fixed bearing side Ausauscherflansch 500 and on the other hand indirectly with a firmly connected to the loslager chandelieren pipe support plate 800 loslager stoolen connecting piece 800d.
  • the bundle of tubes 100.i in question is connected in series with the respectively adjacent bundle of tubes 1 00.i-1 and 100.i + 1 connected. Therefore, once the fixed bearing side exchanger flange 500 forms an inlet E for the product P and the loose bearing side fitting 800d accommodates an associated outlet A; in the respectively adjacent tube bundle 100.i-1 or 100.i + 1, these inlet and outlet conditions are reversed accordingly.
  • the fixed bearing side exchanger flange 500 has a first connection opening 500a, which corresponds to a nominal diameter DN and thus to a nominal passage cross section A 0 of the connection bend 1000 connected there and which is generally dimensioned such that there the mean flow velocity v in the inner tube 300 and mecanickanal 300 * corresponding flow velocity is present.
  • a second connection opening 800a in the loslager lakeen connection piece 800d dimensioned, wherein the respective connection opening 500a or 800a on a respective enlarged passage cross section 500c and 800c in the region to the adjacent pipe support plate 700 or 800 through a conical transition 500b or 800b extended.
  • the extended passage cross section 500c or 800c is substantially cylindrical and designed with a diameter which is usually one to two nominal diameters greater than the nominal diameter DN of the connecting bend 1000 (nominal passage cross section A o of the connecting bend) and accordingly correspondingly larger than the total passage cross section of all the fixed bearing side exchanger flange 500 entering inner tubes 300 is dimensioned with a respective pipe inner diameter D i .
  • the product P to be treated either flows via the first connection opening 500a or the second connection opening 800a to the tube bundle 100.1 to 100.n, so that either the fixed-bearing-side tube support plate 700 or the loslager furnishede pipe support plate 800 is flown. Since in each case a heat exchange between product P in the inner tubes 300 and the inner channels 300 * and a heat transfer medium M in the outer jacket 200 and in the outer channels 200 * has to be made in countercurrent, this heat transfer medium M flows either the first port 400a or the second connecting piece 400b with a mean flow velocity in the outer jacket c too.
  • Both Tube bundle heat exchangers 101 and 102 are connected according to the invention together to an inlet and distribution device 10, which consists of a distributor body 10.3, the input side continues in a first conical transition body 10.4 with a first flange 10.5 ( Figures 4, 4a ).
  • the distributor body 10.3 is preferably designed as an elongate hollow cylinder with an inner diameter D, which forms a distributor space V on the inside.
  • each inner tube 300, 300 * (see Figure 1) of the respective first tube bundle 101.1, 102.1 ( Figure 2) via a respective manifold 10.1.1 to 10.1.4 (10.1.i) from a first group of manifolds 10.1 and above each a distribution pipe 10.2.1 to 10.2.4 (10.2.i) from a second group of distribution pipes 10.2 separately connected, wherein an axial distance a adjacent distribution pipes is at least as large as the largest length of the fibrous components ( Figure 4 ). It has proven to be advantageous to execute the axial distance a equal to or greater than the inner diameter D, wherein the design of the inner diameter D, taking into account the volume flow of the suspension P soumony the desired average flow rate c of a respective partial flow P (T) allow in the respective inner tube got to.
  • a suspension P to be treated thermally enters the inlet and distribution device 10 via the first connection flange 10.5 in conjunction with the first conical transition body 10.4 (total flow of the suspension at the inlet P (E)), where it is located at the beginning of the flow Distributor body 10.3 on a sight glass 10.7 is visually observed ( Figures 2, 4 ).
  • the total flow of the suspension P (E) branches into the respective distribution pipes 10.1.1 to 10.1.4 on the one hand and into the distribution pipes 10.2.1 to 10.2.4 on the other.
  • Such isolated partial flows P (T) of the suspension P (E) pass via a second connecting flange 10.6 arranged at the ends of the respective distributor pipes 10.1.1 to 10.1.4 and 10.2.1 to 10.2.4 to the respective first tube bundles 101.1 and 102.1 ( FIG 2 and Figures 3a, 3b, 3c, 4 ).
  • the connection in the region of the second connecting flange 10.6 is designed such that here a tight connection with the respective corresponding inner tube of the first tube bundle 101.1, 102.1 is given.
  • the distribution chamber V is located, in the flow direction seen at the end of the manifold body 10.3 a controllable via a drive 11 a shut-off device 11, for example a ball valve, wherein the shut-off device 11 on its side facing away from the manifold body 10.3 a flushing port 11 b has ( Figures 4, 4a ).
  • the longitudinal axis of the distributor body 10.3 ( FIGS. 2, 4 ) runs parallel to the tube bundle heat exchanger 101 and thus also to the tube bundle heat exchanger 102 arranged parallel to it.
  • the first group of distributor tubes 10.1 is arranged in a meridian plane of the distributor body 10.3, the latter being vertical is on an assembly plane AE of the first shell-and-tube heat exchanger 101 ( FIG. 3c ).
  • the second group of distribution pipes 10.2 is arranged diametrically opposite the first group 10.1.
  • each distributor tube 10.1.i, 10.2.i has a shut-off device 10.8.i or 10.9.i (10.8.1, 10.8.2, 10.8.3, 10.8.4, 10.9.1) in the region of its branch pipe connection opening at the distributor body 10.3. 10.9.2, 10.9.3, 10.9.4), wherein the first mentioned a first group shut-off 10.8 and the second mentioned form a second group shut-off 10.9.
  • shut-off 10.8.i, 10.9.i is independent of the other either manually or remotely controlled selectively operable.
  • a connection for a pressure measuring device 10.10 is provided.
  • Each inner tube 300, 300 * (see FIG. 1 ) of a tube bundle (for example, the tube bundle 101 .i is selected here, see FIG. 2 and FIGS. 3 a, 3 b, 3 c) with an associated inner tube 300, 300 * of the following tube bundle 101. i + 1 via a connection sheet 20.1.i from a group connection sheet 20.1 a connection fitting 20 separately connected (see also Figures 5a and 5b ).
  • the connection is made via a connection flange 20.5 bridging the two pipe support plates 700 and 800, respectively.
  • a number N 4 inner tubes is, as shown in Figure 5a , evenly distributed on a common pitch circle diameter, wherein the arrangement is chosen so that two adjacent tube bundles 101.i, 101.i + 1 with only two different length connecting arc are connected.
  • Two long, identical connecting bows 20.1.1 and 20.1.2 are assigned to the four outer inner tubes (see also connecting bows 20.1.1 at the right-hand end of the tube bundles 101.i, 101.i + 1).
  • Two short, identical connecting elbows 20.1.3 and 20.1.4 are assigned to the four inner inner tubes.
  • the partial flows P (T) of the two inner tubes of the adjacent tube bundle outer 101.i and 101.i + 1 take in the diverting armature 20, as shown above, the long flow path L l (s. Also figure 5b ).
  • the partial flows P (T) of the two inner inner tubes of the adjacent tube bundles 101.i + 1 and 101.i + 2 ( FIGS. 2 and 3a ) now take the short flow path in the deflection fitting 20 L k (see also Figure 5b ).
  • the inventive approach is realized that the partial flow P (T) in the deflection of the inner tube 300, 300 * of the tube bundle 101.i to the associated inner tube 300, 300 * of the subsequent tube bundle 100.i + 1 on the one hand and from there to the associated inner tube 300, 300 * of the subsequent tube bundle 100.i + 2 on the other hand always has to overcome in the sum always equivalent or approximately equivalent flow resistance.
  • the collecting body 30.1 is preferably designed as an elongate hollow body and defines on the inside a collecting space S.
  • the collecting body 30.1 is adjoined by a second conical transition body 30.5 and a fourth connecting flange 30.6.
  • the outlet and collecting device 30 is space-saving in the area of the connection fittings 20 on one side of the tube bundle heat exchangers 101, 102 first substantially vertically ascending and then laid down substantially vertically, thereby emptying the tube bundle heat exchanger 101, 102 and thus a burning is prevented by residual suspension. In addition to this siphon effect, it homogenizes a suspension P (A) emerging from the last tube bundles 101.n and 102.n with regard to temperature and solids concentration, if this is still necessary in view of the arrangement according to the invention.
  • the heat exchange between the suspension P (partial flows P (T)) flowing at the mean flow velocity v in the inner tubes 300 and the inner channels 300 * and a heat transfer medium M flowing in the outer jacket 200 or in the outer channels 200 * takes place in countercurrent.
  • the heat transfer medium M (E) for example, hot water or, in the case of cooling the products to be fermented, cooling water flows to the nth tube bundle 101.n on the one hand via the first connection piece 400a with the average flow velocity c in the outer shell ( Figure 2). It leaves the tube bundle 101.n on the other hand via the second connecting piece 400b, which is connected to the first connecting piece 400a of the adjacent tube bundle 101.n-1 on a short path.
  • the heat transfer medium M (A) leaves the first tube bundle 101.1 via the second connecting piece 400b with the mean flow velocity c in the outer jacket.

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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)
  • Heat Treatment Of Articles (AREA)
EP06011990A 2005-07-02 2006-06-10 Procédé et agencement de guidance d'écoulement dans des échangeurs de chaleur à faisceau tubulaire pour le traitement thermique de suspensions Active EP1742006B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL06011990T PL1742006T3 (pl) 2005-07-02 2006-06-10 Sposób i urządzenie do prowadzenia płynu w wymiennikach ciepła płaszczowo-rurowych do obróbki termicznej zawiesin

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE102005030999A DE102005030999B4 (de) 2005-07-02 2005-07-02 Anordnung zur Strömungsführung in Rohrbündel-Wärmeaustauschern zur thermischen Behandlung von Suspensionen

Publications (2)

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EP1742006A1 true EP1742006A1 (fr) 2007-01-10
EP1742006B1 EP1742006B1 (fr) 2012-02-01

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EP (1) EP1742006B1 (fr)
AT (1) ATE544046T1 (fr)
DE (1) DE102005030999B4 (fr)
PL (1) PL1742006T3 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014006151A1 (fr) * 2012-07-05 2014-01-09 Tetra Laval Holdings & Finance S.A. Echangeur de chaleur tubulaire amélioré
WO2014118048A1 (fr) * 2013-01-30 2014-08-07 Tetra Laval Holdings & Finance S.A. Appareil de traitement thermique tubulaire avec rendement en énergie amélioré
WO2015075633A1 (fr) * 2013-11-19 2015-05-28 Nestec Sa Système d'échangeur de chaleur ramifié, symétrique et concentrique

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102011114326A1 (de) 2011-09-24 2013-03-28 Peter Wolf Molchbarer, zerlegbarer Endloswärmetauscher
EP2762822B1 (fr) 2013-02-01 2016-05-18 Molkerei Ammerland eG Élément d'échangeur de chaleur et agencement d'échangeur thermique

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0246111A1 (fr) * 1986-05-16 1987-11-19 Santa Fe Braun Inc. Dispositif de guidage de l'écoulement pour des échangeurs de chaleur dans des canalisations de transfert
DE9403913U1 (de) * 1994-03-09 1994-05-05 Gea Finnah Gmbh Rohrbündel-Wärmetauscher
US20030111216A1 (en) * 1999-08-23 2003-06-19 Harunori Hirao Method for preventing plate type heat exchanger from blockage
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US20030111216A1 (en) * 1999-08-23 2003-06-19 Harunori Hirao Method for preventing plate type heat exchanger from blockage
WO2004051174A1 (fr) * 2002-12-02 2004-06-17 Tuchenhagen Dairy Systems Gmbh Dispositif pour prolonger la duree d'utilisation d'un echangeur thermique a faisceau tubulaire dans des installations a ultra-haute temperature (uht) pour produits alimentaires, a chauffage indirect
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US20150159964A1 (en) * 2012-05-07 2015-06-11 Tetra Laval Holdings & Finance S.A. Tubular heat exchanger
WO2014006151A1 (fr) * 2012-07-05 2014-01-09 Tetra Laval Holdings & Finance S.A. Echangeur de chaleur tubulaire amélioré
WO2014118048A1 (fr) * 2013-01-30 2014-08-07 Tetra Laval Holdings & Finance S.A. Appareil de traitement thermique tubulaire avec rendement en énergie amélioré
CN104937361A (zh) * 2013-01-30 2015-09-23 利乐拉瓦尔集团及财务有限公司 具有改进的能量效率的管式热处理装置
JP2016509192A (ja) * 2013-01-30 2016-03-24 テトラ・ラヴァル・ホールディングス・アンド・ファイナンス・ソシエテ・アノニムＴｅｔｒａ Ｌａｖａｌ Ｈｏｌｄｉｎｇｓ ＆ Ｆｉｎａｎｃｅ Ｓ．Ａ． 改善されたエネルギー効率を有するチューブ式熱処理装置
RU2643283C2 (ru) * 2013-01-30 2018-01-31 Тетра Лаваль Холдингз Энд Файнэнс С.А. Трубчатое устройство для термообработки с повышенной эффективностью использования энергии
CN104937361B (zh) * 2013-01-30 2018-09-21 利乐拉瓦尔集团及财务有限公司 具有改进的能量效率的管式热处理装置
US10234208B2 (en) 2013-01-30 2019-03-19 Tetra Laval Holdings & Finance S.A. Tubular heat treatment apparatus with improved energy efficiency
WO2015075633A1 (fr) * 2013-11-19 2015-05-28 Nestec Sa Système d'échangeur de chaleur ramifié, symétrique et concentrique
RU2663676C1 (ru) * 2013-11-19 2018-08-08 Нестек Са Концентрическая симметричная система теплообменников с разветвленной поверхностью

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DE102005030999A1 (de) 2007-01-11
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EP1742006B1 (fr) 2012-02-01
ATE544046T1 (de) 2012-02-15

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