EP2006628A2 - Dispositif de refroidissement ou de chauffage de produits en vrac ainsi que procédé de fonctionnement d'un tel dispositif - Google Patents

Dispositif de refroidissement ou de chauffage de produits en vrac ainsi que procédé de fonctionnement d'un tel dispositif Download PDF

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Publication number
EP2006628A2
EP2006628A2 EP08008794A EP08008794A EP2006628A2 EP 2006628 A2 EP2006628 A2 EP 2006628A2 EP 08008794 A EP08008794 A EP 08008794A EP 08008794 A EP08008794 A EP 08008794A EP 2006628 A2 EP2006628 A2 EP 2006628A2
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EP
European Patent Office
Prior art keywords
bulk material
gas
heat transfer
section
heat exchanger
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
EP08008794A
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German (de)
English (en)
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EP2006628A3 (fr
EP2006628B1 (fr
Inventor
Bernhard Dr. Stark
Egon Zechner
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.)
Coperion GmbH
Original Assignee
Coperion GmbH
Coperion Waeschle GmbH and Co KG
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Publication of EP2006628A2 publication Critical patent/EP2006628A2/fr
Publication of EP2006628A3 publication Critical patent/EP2006628A3/fr
Application granted granted Critical
Publication of EP2006628B1 publication Critical patent/EP2006628B1/fr
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
    • F28C3/00—Other direct-contact heat-exchange apparatus
    • F28C3/10—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material
    • F28C3/12—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material the heat-exchange medium being a particulate material and a gas, vapour, or liquid
    • F28C3/14—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material the heat-exchange medium being a particulate material and a gas, vapour, or liquid the particulate material moving by gravity, e.g. down a 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
    • F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus

Definitions

  • the invention relates to a device for cooling or heating of bulk material according to the preamble of claim 1 and 2. Furthermore, the invention relates to a method for operating such a device.
  • a device of the type mentioned is known from the DE 10 2004 041 375 A1 , There, in order to improve the heat transfer gas is passed in countercurrent through the heat exchanger tubes.
  • the heat transfer from the bulk material to the heat transfer fluid depends significantly on the gas flow of the heat transfer gas passed countercurrently through the heat exchanger tubes.
  • a maximum of the heat transfer for a very specific amount of the heat transfer gas, which is passed through the heat exchanger tubes is assigned an empty-tube gas velocity, which is referred to below as the critical empty- tube gas velocity V Lg, kr , lies at a differential pressure that can be unambiguously determined for the respective bulk material at the heat exchanger section of the device.
  • the critical empty tube gas velocity is calculated from the optimum gas amount and the free cross section of all heat exchanger tubes in the heat exchanger section of the device.
  • the critical empty-tube gas velocity is a function of the product temperature, that is a function of the bulk material passed through the tubes, and of the static pressure in the heat exchanger tubes.
  • the critical empty- tube gas velocities V Lg, kr referred to here relate to an average bulk material temperature and an average static pressure in the heat exchanger section.
  • the heat exchanger tubes can also have any cross-sectional shape.
  • the heat exchanger tubes for example, a square or rectangular cross section, wherein a long side of the cross section may have an extent up to the diameter of the housing.
  • those housing sections in which the heat transfer fluid is guided plate-shaped. Therefore, a plate-shaped configuration of heat exchanger elements, such as in the EP 0 444 338 B1 described, a configuration with heat exchanger tubes in the context of this application.
  • a gas source of the gas supply device can simultaneously also be the gas supply of a pneumatic conveying device used in connection with the device. This can be realized by withdrawing a gas partial flow in a clean gas line upstream of a cooling or heating device, for example a downstream rotary valve, and connecting it to the supply line for the heat transfer gas.
  • a heat transfer gas quantity has to create an optimal heat transfer between the bulk material and the heat transfer fluid suitable, which is at absolute Leerrohrgas niethen between 0.2 m / s and 2.0 m / s.
  • a heat transfer gas amount which corresponds to a Leerrohrgas nieth of 0.5 m / s to 1.2 m / s in the heat exchanger tubes, has been found to be suitable for many typically used bulk materials.
  • a filter according to claim 3 provides for a purification of the heat transfer gas before the introduction into or after the discharge from the bulk material heat exchanger.
  • a gas heater and / or a gas-cooling device may be arranged in the path of the heat transfer gas before the confluence of the supply line. This allows an additional improvement of the effect of the bulk material heat exchanger in that the heat transfer gas gets a heat exchanger effect.
  • the heat transfer gas gets a heat exchanger effect.
  • the heat transfer gas is heated by the gas heater.
  • the heat transfer gas is cooled by means of the gas cooling device.
  • a condensate separator may be arranged between the gas-cooling device and the mouth of the supply line. Such a condensate separator prevents unwanted moisture from being fed via the heat transfer gas to the bulk material.
  • the discharge line can communicate with the environment of the bulk material heat exchanger. Such an embodiment of the discharge line allows a non-pressurized bulk material entry section.
  • the discharge line can be pressure-tight connected to the then also pressure-tight executed bulk material entry section.
  • Such a design of the discharge line allows the heat transfer gas supply with a pressure gas generator, in particular with exactly one pressure gas generator, or with a suction gas generator, in particular with exactly one suction gas generator.
  • a rotary feeder according to claim 4 enables a substantially pressure-tight discharge-side termination of the entry section. This is particularly advantageous if a pressure-tight discharge side Design of the discharge line and / or the bulk material entry section to be realized.
  • a sieve according to claim 5 prevents undesirable large or small particles from entering the entry section.
  • the sieve can also be accommodated within the entry section.
  • a distributor or a classifier can be used to specify bulk particle sizes.
  • a bulk material supply line according to claim 6 ensures a defined and symmetrical bulk material supply. Also, an eccentric bulk material supply is possible, which may be particularly advantageous for small diameters of the device for reasons of space.
  • This bulk material distribution unit can be formed in particular as the bulk material feed line downstream cone, the top of the bulk material Zufiihr ein faces and is arranged centrally to this.
  • a discharge line according to claim 8 leads to a defined symmetrical flow of the heat transfer gas.
  • the discharge line can be designed in particular as a concentric gap or as a ring line around the bulk material supply line.
  • a sighting gas supply line according to claim 9 allows a sighting of the bulk material feed section supplied bulk material.
  • An embodiment according to claim 11 allows an adaptation of the heat transfer gas quantity to the temperature of the discharged bulk material.
  • An embodiment according to claim 12 allows optimization of the heat transfer gas amount in dependence on the measured differential pressure.
  • Another object of the invention is to specify an operating method for a device according to the invention, which leads to the most efficient possible operation of the bulk material heat exchanger, in particular to an acceleration of the commissioning of the bulk material heat exchanger.
  • a determination of the critical Leerrohrgas für a via a temperature measurement according to claim 14 and / or via a differential pressure measurement according to claim 15 enables a safe and reproducible determination of the optimal heat transfer gas quantity.
  • One in the Fig. 1 illustrated apparatus for cooling or heating of bulk material has an upper entry or buffer section 1, a central heat exchanger section 2 and a lower discharge section 3.
  • the sections 1, 2, 3 each have a circular cross-section.
  • the housing-like, substantially enclosed buffer section 1 is provided with an upper inlet nozzle 4 for supplying a bulk material to be cooled or heated.
  • the bulk material to be cooled or heated is, in particular, a granulate or a pellet-shaped bulk material.
  • a particle or grain size distribution of the bulk material can essentially be centered around a pronounced maximum, that is to say lead to a homogeneous bulk material with practically identical particle sizes, as is generally the case for a granulate.
  • the particle or particle size distribution can also be more heterogeneous, ie particles of significantly different sizes can be present either in the form of a continuous particle size distribution or in the form of a particle size distribution with several maxima.
  • a heterogeneous distribution is usually the case with granular bulk material. These may be plastic granules, urea pellets, fertilizer prills or wood or feed pellets.
  • the volume of the upper buffer section 1 is so large that bulk material has a residence time there which is less than 2 minutes. In principle, longer residence times up to 30 minutes are possible.
  • the inlet nozzle 4 which represents a Schüttgutzufiihr-line in the buffer section 1, opens centrally into the buffer section 1 a. Upstream of the inlet nozzle 4 may be in the conveying path of the bulk material still a screening device 4a, with the coarse and / or fines of the bulk material whose particle sizes are above a first predetermined limit or below a second predetermined limit, retained or separated.
  • a distributor or a sifter can also be arranged in the feed path of the bulk material in front of the inlet connection 4.
  • a static sieve 4b may be incorporated in the entry or buffer section 1. The static sieve 4b serves in particular to retain bulk agglomerates.
  • the heat exchanger section 2 has a housing 5, in whose interior space 6 heat exchanger tubes 7 are arranged parallel to each other at a distance from each other.
  • the interior 6 is therefore a heat exchange space.
  • the heat exchanger tubes 7 have a length to diameter ratio which is in the range between 15 and 300 and in particular between 30 and 250.
  • baffles 10 are each mounted transversely to the longitudinal direction of the tubes 7 at a distance from each other such that the supplied via the supply port 8 heat transfer fluid corresponding to a flow direction arrow 11 meandering through the interior 6 respectively transversely to the longitudinal direction of the tubes 7 gradually upward to the discharge nozzle 9 flows.
  • the baffles 10 will pass from the tubes 7.
  • the heat exchanger section 2 is thus designed for a cross counterflow of the heat transfer fluid.
  • the interior 6 can be filled with a tube 7 enveloping bed 12 of glass beads, steel balls and / or plastic granules, which contributes to the improvement of the heat transfer between the heat transfer fluid and the tubes 7.
  • a tube 7 enveloping bed 12 of glass beads, steel balls and / or plastic granules which contributes to the improvement of the heat transfer between the heat transfer fluid and the tubes 7.
  • the nozzle 8, 9 removable retention screens 13 The size of the particles of the Bulk 12 should be such that they can be introduced after the production of the heat exchanger section 2 in this.
  • the particles of the bed 12 are so in any case smaller than the pitch of the tubes 7.
  • the particles of the bed 12 are preferably spherical, lens or cylindrical shape.
  • the tubes 7 are connected at their upper ends with an inlet tube plate 14 fixedly connected to the housing 5 and with a discharge tube bottom 15 at their lower ends such that they are open towards the buffer section 1 and the discharge section 3. Between the buffer portion 1 and the heat exchanger section 2 on the one hand and the heat exchanger section 2 and the discharge section 3 on the other hand, there are flange 16 and 17.
  • the inlet tube plate 14 is designed so that each tube 7 a widening towards the buffer section 1, to the respective pipe. 7 thus narrowing feed hopper 18 has.
  • Adjacent funnels 18 are dimensioned to meet at the top in a relatively sharp edge.
  • the inlet funnels 18 have an opening angle ⁇ , which may be between 30 ° and 180 ° and is preferably in the range of 40 ° to 120 °.
  • inlet tube plate 14 between adjacent tubes 7 dead spaces, dead surfaces or bulk material bridges arise on which bulk 20 remains undesirable.
  • Preferred arrangements for the tubes 7 are triangular, ie in particular a hexagonal arrangement in which each tube has six nearest neighbors, square, that is to say an arrangement in which each tube has four nearest neighbors, or an arrangement on pitch circles.
  • the discharge section 3 has the shape of a downwardly tapered cone-shaped funnel. Such a shape causes the bulk material 20 flows in the discharge section 3 at all points of an arbitrarily selected cross section with almost the same speed, in this consideration, the immediate edge area is not taken into account, since there is always a certain delay due to wall friction.
  • a rotary valve 22 As a discharge a rotary valve 22 is provided, the housing 23 is connected via a downpipe 24 with the discharge section 3.
  • a cellular wheel 25 is arranged that is rotatably driven by a motor 26.
  • the motor 26 is driven by a level detector 27, which detects the level of the bulk material 20 in the buffer section 1.
  • the rotary valve 22 can be used at the same time as Austragsorgan in a pneumatic conveyor, which in the drawing not shown. Instead of the rotary valve 22, other, sufficiently fluid-tight discharge organs can be used. Such alternative dispensing devices include double flap locks or screw conveyors in which the product is compacted for fluid sealing. As a discharge can also be used a long downpipe with an associated metering, as far as the bulk material in the down pipe assumes a sufficient fluid-sealing effect.
  • a supply line 28 for a heat transfer gas Connected to the supply line 28 is a compressed gas generator 29, which may be, for example, a fan, a rotary blower, a screw compressor or a side channel blower.
  • the compressed gas generator 29 sucks in heat transfer gas, for example air, via a suction line 30 and an intake filter 31.
  • a gas heat exchanger 32 Downstream of the compressed gas generator 29 in the gas supply line 28 is a gas heat exchanger 32, with which the heat transfer gas can optionally be heated or cooled. If the heat transfer gas is to be cooled or only heated depending on the use of the bulk material heat exchanger, instead of the gas heat exchanger 32, a pure gas cooler or a pure gas heater can be provided.
  • a Kondensatabscheider 33 Downstream of the gas heat exchanger 32 in the gas supply line 28 is a Kondensatabscheider 33. Between this and the confluence of the feed line 28 in the discharge section 3, a safety filter 33a for filtering out remaining residues in the heat exchanger gas is arranged.
  • a differential pressure sensor 34a communicates via a first measuring line 34b with the upper buffer section 1 and via a second measuring line 34c the discharge section 3 in conjunction. Via a signal connection, not shown, the differential pressure sensor 34a communicates with the control device 45 and a control unit 34d. The latter is in turn connected to the compressed gas generator 29 in signal connection.
  • the heat transfer gas flows through the bulk material heat exchanger counter to the flow direction of the bulk material 20.
  • the bulk material heat exchanger is thus designed for a countercurrent of the heat transfer gas to the bulk material 20.
  • the heat transfer gas flows through the upper buffer section 1 and leaves it via an exhaust port 34.
  • the outlet side of the exhaust port 34 is an open point 35. In this area, the path of the heat transfer gas is therefore not pressure-tight to the environment completed.
  • an intake funnel 36 of a further suction line 37 is arranged above the open point 35.
  • the suction line 37 opens into a suction gas generator 38, which may also be a fan, a rotary blower, a screw compressor or a side channel blower.
  • a cyclone or a filter 39 for cleaning the heat transfer gas is arranged between the suction hopper 36 and the suction gas generator 38.
  • a cooling device not shown, may be arranged for the heat transfer gas, in order to avoid that the gas enters the suction gas generator 38, in particular for cooling tasks at too high a temperature.
  • the delivery rate of the suction gas generator 38 is matched to that of the compressed gas generator 29.
  • the heat transfer gas can in turn via a connecting line, not shown in the drawing, via the suction filter 31 and the suction line 30th supplied to the compressed gas generator 39, so that a closed guide of the heat transfer gas results.
  • the power of gas generator 29 is tuned to the flow conditions in the heat exchanger tubes 7 such that the heat transfer gas in the tubes 7 has a Leerrohrgas nietha ranging between 20% and 200% of a critical Leerrohrgas nietha ranging between 20% and 200% of a critical Leerrohrgas nietha ranging between 20% and 200% of a critical Leerrohrgas nietha ranging between 20% and 200% of a critical Leerrohrgas nietha ⁇ . Typical dimensions of the bulk material 20, namely in particular a typical bulk density, a typical diameter of the bulk material particles, a typical volume of cavities (see for example 40 in the Fig.
  • the power of the compressed gas generator 29 is adjusted so that the gas in the heat exchanger tubes 7 a Leerrohrgas founded between 0.2 m / s and 2.0 m / s, preferably between 0.4 m / s and 1.6 m / s, more preferably between 0.6 m / s and 1.4 m / s, even more preferably between 0.6 m / s and 1.2 m / s.
  • guide surfaces 41 are formed for the gas supply.
  • the heat transfer gas can also be introduced into the discharge section 3 in a constructive manner.
  • Corresponding apparatus for introducing gas for example when blowing gas over a cone which is inverted compared to the discharge section 3, are known to the person skilled in the art, for example, from US Pat DE 100 54 240 A1 known.
  • a further guide surface 42 is formed, which directs the bulk material 20 from the discharge section 3 to the revolving side of the driven in a rotational direction 43 cell wheel 25. This ensures a uniform withdrawal of the bulk material 20 over the entire inlet cross section of the rotary valve 22nd
  • a temperature sensor 44 for determining the temperature of the bulk material 20 in the downpipe 24 is arranged on the inner wall of the downpipe 24.
  • the temperature sensor 44 is in signal communication with a central control device 45 of the bulk material heat exchanger.
  • This signal connection can be wired or wireless.
  • the control device 45 is again in a manner not shown, which may also be wired or wireless, with the compressed gas generator 29 and the suction gas generator 38 in signal communication. Also, a connection of the control device 45 with a throttle valve, not shown for adjusting a gas flow rate is possible.
  • a critical empty- tube gas velocity V Lg, kr is first determined.
  • the bulk material heat exchanger 20 is operated with bulk material and with a first low power of the compressed gas generator 29, which corresponds to a first, low countercurrent gas quantity.
  • This amount of gas is then gradually increased by gradually increasing the power of the compressed gas generator 29 or by opening a throttle valve, not shown, on the suction side or on the pressure side of the compressed gas generator 29.
  • the influence of the heat transfer gas on the bulk material within the heat exchanger tubes 7 is monitored. This monitoring can be done for example by measuring the differential pressure at the heat exchanger section 2 via the differential pressure sensor 34a. Alternatively, the monitoring can be carried out by measuring the temperature of the bulk material 20 via the temperature sensor 44 in the discharge section 3.
  • a critical amount of heat transfer gas is achieved in the case of differential pressure monitoring, if, after a gradual increase in the Heat transfer gas amount has a maximum pressure loss between the buffer section 1 and the discharge section 3, measured by the differential pressure sensor 34 a, has set. In a temperature monitoring, the critical amount of heat transfer gas is reached when the temperature of the bulk material in the discharge section 3 during cooling of the bulk material 20 is minimal or becomes maximum during heating of the bulk material 20.
  • the transport of bulk material through the heat exchanger tubes 7 can be monitored to determine a critical amount of heat transfer gas.
  • This monitoring can be done for example by a visual inspection of a gas bubble formation in the heat exchanger tubes 7.
  • the monitoring can be carried out by measuring the bulk transport of the bulk material through all heat exchanger tubes 7 or through certain heat exchanger tubes 7.
  • the monitoring can also take place by measuring the speed of the bulk material transport through all or through specific heat exchanger tubes 7.
  • a critical amount of heat transfer gas is achieved when, for the first time, gas bubbles form in the bulk material 20 transported in the tubes 7 or when an initial fluidization of the bulk material 20 is detected.
  • a critical amount of heat transfer gas is reached when the measured bulk quantity transport is less than 90% of a heat transfer gas countercurrent-free bulk material transport.
  • a critical amount of heat transfer gas is achieved if the measured bulk material velocity is less than 90 ° of a heat transfer gas countercurrent-free bulk material velocity.
  • the bulk material heat exchanger is operated with a power of the compressed gas generator 29, which at a Leerrohrgas founded between 0.2 m / s and 2.0 m / s, preferably between 0.4 m / s and 1.6 m / s even more preferably between 0.6 m / s and 1.4 m / s, even more preferably between 0.6 m / s and 1.2 m / s.
  • the heat transfer gas flowing countercurrently through the heat exchanger tubes 7 improves the heat transfer between the bulk material 20 and the heat transfer fluid flowing through the interior 6.
  • the heat transfer gas serves on the one hand as a direct heat transfer medium; On the other hand, the heat transfer gas provides for a mechanical rearrangement of the bulk material particles to each other and to the inner walls of the tubes. 7
  • the heat transfer gas itself absorbs heat from the bulk material 20 or releases heat to the bulk material 20.
  • the heat transfer gas is pre-cooled in the heat exchanger 32. If the bulk material 20 to be heated in the bulk material heat exchanger, the heat transfer gas is preheated in the heat exchanger 32. When the heat transfer gas is cooled, condensate occurring thereby can be deposited in the condensate separator 33.
  • the amount of heat transfer gas to be set to achieve optimal heat transfer to the bulk material 20 may depend on the outlet temperature of the bulk material 20. This can after the bulk material heat exchanger Fig. 1 be taken into account. In this case, the temperature of the bulk material 20 in the discharge section 3 or in the downpipe 24 is determined by the temperature sensor 44. By appropriate control of the compressed gas generator 29 via the control device 45, the heat transfer gas quantity is then changed as a function of the measured temperature and of the actual output of the compressed gas generator 29, that is to say of the current gas quantity.
  • the schematic diagrams of Fig. 5 to 8 show typical relationships between parameters of the bulk material 20 and the critical Leerrohrgas familia.
  • the critical Leerrohrgas Anthony V Lg, kr increases with increasing bulk density ⁇ Sch (see Fig. 5 ).
  • the critical empty- tube gas velocity V Lg, kr increases with the mean particle diameter d P (cf. Fig. 6 ).
  • the critical empty- tube gas velocity V Lg, kr increases with the volume V H of the cavities 40 between the bulk material particles (see Fig. 7 ).
  • the critical empty- tube gas velocity V Lg, kr increases with the particle density ⁇ P (cf. Fig. 8 ).
  • the void volumes may result in a void fraction between the bulk particles which is typically between 30% and 70% and often between 35% and 60%.
  • the bulk material 20 may have a typical mean particle diameter (diameter of a sphere of equal volume content) in the range between 0.5 mm and 15 mm, for example between 1 and 10 mm. Fines, rod or fine grain breakage are not taken into consideration here.
  • the average particle diameter is in particular in the range of 2 mm to 6 mm.
  • FIG. 2 Another embodiment of a bulk material heat exchanger is described below with reference to Fig. 2 described. Components which correspond to those described above with reference to the Fig. 1 have the same reference numbers and will not be discussed again in detail.
  • a feeder rotary valve 46 directly upstream.
  • the feed rotary valve 46 substantially seals the inlet connection 4 on the supply side.
  • the delivery line 47 may be connected to the intake filter 31 and the suction line 30, so that overall a closed line system for guiding the heat carrier gas results.
  • exhaust port 34 in the Fig. 1 and 2 has the buffer section 1 of the bulk material heat exchanger after Fig. 3 a concentric to the inlet nozzle 4 arranged exhaust gas ring line 49, which will pass from the coaxially arranged inlet nozzle 4.
  • the ring line 49 or a correspondingly arranged concentric gap is in turn in fluid communication with a connecting line 50, which in turn ends below the suction funnel 36.
  • a cone is arranged as a bulk material distribution unit 51.
  • the tip 52 of the cone 51 faces the inlet nozzle 4.
  • the tip 52 is centered below the mouth of the inlet nozzle 4 in the buffer section 1 arranged.
  • the bulk material distribution unit 51 is rotationally symmetrical about a central longitudinal axis of the buffer section 1.
  • a sighting gas supply line 53 opens.
  • the latter is connected to a sighting gas feed device 54 in the form of another compressed gas generator.
  • Viewing gas can be blown into the buffer section 1 via the sighting gas supply line 53, whereby the supplied bulk material 20 can be viewed.
  • the heat transfer gas routing differs according to the bulk material heat exchanger Fig. 4 from the one after Fig. 1 in the following:
  • the bulk material heat exchanger after Fig. 4 has no pressure gas generator (compare 29 gas pressure generator in the Fig. 1 ).
  • the bulk material is after the heat exchangers Fig. 4 supplied via a sufficiently gastight rotary valve 46.
  • the bulk material heat exchanger is missing Fig. 4 the open location 35.
  • the exhaust port 34 is pressure-tight connected to the suction line 37.
  • the suction gas generator 38 is the gas supply device.
  • the heat transfer gas flowing through the bulk material 20 can in particular also bring about drying of the bulk material.
  • the heat transfer gas can be pre-dried in the gas supply line 28.
  • An example of the bulk 20 is pelleted animal feed having a bulk density of 650 kg / m 3 and a particle density of 1461 kg / m 3 .
  • the resulting void volume fraction is 56%.
  • the animal feed pellets are rod-shaped with a diameter of the rods of about 5 mm and a length of about 10 to 25 mm.
  • the optimum empty-tube gas velocity for achieving efficient heat transfer from the bulk material 20 to the heat-transfer fluid is in the range from about 0.8 m / s to 1.4 m / s.
  • the bulk material 20 is a granulated plastic granulate with a bulk density of 530 kg / m 3 and a solids density of 950 kg / m 3 . This results in a void volume fraction of 42%. The equivalent volume equal ball diameter of this granule is 3.8 mm.
  • the bulk material 20 was cooled from a temperature of 90 ° to 95 ° C with the aid of cooling water at a temperature of about 20 ° to 30 ° C and it was injected various amounts of heat transfer gas.
  • Typical heat conductivity values for the bulk material 20 are in the range between 0.05 and 0.25 W / mK, as long as the beds are not gas-flowed.
  • heat exchanger gas In addition to air, other gases, in particular nitrogen, carbon dioxide, offgas, ie nitrogen contaminated with various hydrocarbons, and optionally also steam, can be used as the heat exchanger gas.
  • gases in particular nitrogen, carbon dioxide, offgas, ie nitrogen contaminated with various hydrocarbons, and optionally also steam, can be used as the heat exchanger gas.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
EP20080008794 2007-06-19 2008-05-10 Dispositif de refroidissement ou de chauffage de produits en vrac ainsi que procédé de fonctionnement d'un tel dispositif Not-in-force EP2006628B1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE102007027967A DE102007027967A1 (de) 2007-06-19 2007-06-19 Vorrichtung zum Kühlen oder Heizen von Schüttgut sowie Verfahren zum Betrieb einer derartigen Vorrichtung

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EP2006628A2 true EP2006628A2 (fr) 2008-12-24
EP2006628A3 EP2006628A3 (fr) 2011-10-19
EP2006628B1 EP2006628B1 (fr) 2013-03-06

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Cited By (1)

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CN102645111A (zh) * 2012-04-18 2012-08-22 常州市姚氏铸造材料有限公司 对松散固体颗粒物进行调温的换热装置

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Publication number Priority date Publication date Assignee Title
DE102009032390A1 (de) 2009-07-08 2011-01-13 Coperion Gmbh Vorrichtung zum Kühlen von Schüttgut sowie Verfahren zum Behandeln von Schüttgut
DE102010005578A1 (de) * 2010-01-22 2011-07-28 Technische Universität Darmstadt, 64289 Regenerativer Wärmetauscher und Verfahren zur Übertragung von Wärme zwischen zwei Feststoffen
DE102010027801A1 (de) * 2010-04-15 2011-10-20 Coperion Gmbh Vorrichtung zum Kühlen oder Heizen von Schüttgut

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DE102004041375A1 (de) 2004-03-24 2005-10-13 Coperion Waeschle Gmbh & Co. Kg Vorrichtung zum Temperieren von Schüttgut

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DE102007027967A1 (de) 2008-12-24
EP2006628B1 (fr) 2013-03-06

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