EP2159526A2 - Installation de traitement pour produits en vrac - Google Patents

Installation de traitement pour produits en vrac Download PDF

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Publication number
EP2159526A2
EP2159526A2 EP09008717A EP09008717A EP2159526A2 EP 2159526 A2 EP2159526 A2 EP 2159526A2 EP 09008717 A EP09008717 A EP 09008717A EP 09008717 A EP09008717 A EP 09008717A EP 2159526 A2 EP2159526 A2 EP 2159526A2
Authority
EP
European Patent Office
Prior art keywords
heat exchanger
bulk material
section
exchanger tubes
plant according
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.)
Withdrawn
Application number
EP09008717A
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German (de)
English (en)
Other versions
EP2159526A3 (fr
Inventor
Berhard Stark
Olaf Hustert
Christoph Schumacher
Michael Dipl.-Ing. Dürr
Gero Weber
Günther Dehm
Jörg SCHULTE
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
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 Coperion GmbH filed Critical Coperion GmbH
Publication of EP2159526A2 publication Critical patent/EP2159526A2/fr
Publication of EP2159526A3 publication Critical patent/EP2159526A3/fr
Withdrawn legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • 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
    • 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
    • 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
    • F28D2021/0045—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for granular materials

Definitions

  • the invention relates to a processing plant for bulk material with a bulk material conveying device and a bulk material heat exchanger device.
  • Fluidized bed or fluidized bed heat exchangers are known from the DE 198 51 997 A1 , of the EP 0 973 716 B1 , of the DE 601 19 659 T2 , of the DE 39 39 029 C2 , of the DE 38 31 385 C2 and the DE 600 113 05 T2 ,
  • the solid which forms the fluidized bed together with a gaseous medium is either kept in a fluidized state in the heat exchanger or is an auxiliary medium for heat transfer or removal of deposits on heat transfer surfaces, but not the process medium to be processed.
  • heat transfer medium is used. Fluid guided in heat exchanger tubes.
  • the concept of a plurality of heat exchanger tubes, through which the bulk material to be cooled or to be heated flows, has a bulk material heat exchanger connect with the concept of a pneumatic conveying of the bulk material through the heat exchanger tubes.
  • the pneumatic conveying is designed depending on the application as a plug conveying, as strands promotion or as flight promotion.
  • pneumatic conveying can also be realized in the majority of the heat exchanger tubes, without the delivery collapsing in the case of individual heat exchanger tubes.
  • the processing plant according to the invention therefore represents a departure from the known in the art fluidized bed or fluidized bed heat exchanger concepts.
  • the Leerrohrgas beau is in the pneumatic conveying of the invention usually greater than ten times the fluidization, which usually in the fluidized bed or fluidized bed heat exchangers Use comes.
  • the temperature difference between the bulk material inlet temperature in the heat exchanger tubes and the Schüttgutaustrittstemperatur from the heat exchanger tubes may be greater than 5 K, greater than 10 K and greater than 20 K.
  • the pneumatic pumping can be operated as a pressure or suction through the heat exchanger device.
  • a plurality of heat exchanger devices be connected in series one behind the other.
  • the heat exchanger tubes may have an inner diameter ranging from 5 mm to 100 mm, preferably from 8 mm to 60 mm, and more preferably from 10 mm to 30 mm.
  • the inner diameter of the heat exchanger tubes may for example be 26 mm.
  • the conveying gas velocities can be in the range between 10 m / s and 100 m / s, preferably between 20 m / s and 70 m / s and even more preferably between 30 m / s and 40 m / s. The higher the delivery gas velocity, the greater the pressure loss along a given heat exchanger tube length.
  • With a smaller inner diameter of the heat exchanger tubes results in a smaller distance between the tube wall and the central tube axis, which in turn leads to a better heat exchange between the bulk material and the wall of the respective heat exchanger tube and thus to an improved heat transfer performance of the heat exchanger device.
  • Smaller heat exchanger tube diameter create the possibility of designing a total slimmer and possibly longer heat exchanger section, which manufacturing technology leads to cost advantages compared to a heat exchanger section with the same number of heat exchanger tubes larger inside diameter.
  • a vertical arrangement of the heat exchanger tubes according to claim 2 has been found to be particularly suitable.
  • the heat exchanger tubes can also be oriented differently and in particular horizontally, ie lying, arranged.
  • the pneumatic conveying can be done from bottom to top, optionally from top to bottom.
  • Structures of the heat exchanger tubes according to claim 3 may be formed, for example, as externally mounted indentations and / or elevations having typical dimensions on the one hand of their diameter and on the other hand their deviation from a surrounding shell wall of the heat exchanger tube in the range of 1 mm to one or more cm. Such structures may also be formed as additional cross-sectional profile elements, such as ribs, for enlarging the inner surface of the heat exchanger tubes.
  • An arrangement according to claim 4 leads to a pneumatic conveying of the bulk material from bottom to top.
  • a pneumatic vertical conveying can be used, for example, from the DE 39 01 110 A1 and the DE 33 32 764 A1 are known.
  • the pneumatic conveying can also be done from top to bottom or in the horizontal direction.
  • a pipe bend according to claim 5 leads to a deflection of the bulk material flow path with a low in particular with wear bulk material mechanical stress of components of the processing plant.
  • a pipe bend reduces the risk of grain breakage during the deflection.
  • the aspect ratio LF / DF can also be greater than 10 and can preferably be greater than 20.
  • An aspect ratio R / DF according to claim 7 has also proved to be particularly suitable for ensuring a uniform loading of all heat exchanger tubes.
  • the aspect ratio R / DF is in particular in the range between 3 and 10.
  • a baffle plate according to claim 8 in addition to the deflection function and a good dispersion of the bulk material in the conveyor line cross-section and the function of a resolution of possibly before the baffle plate still present bulk agglomerates.
  • a tapering section according to claim 9 ensures a good merging of the bulk material after its exit from the heat exchanger tubes.
  • the tapering portion and also the extension portion of the heat exchanger housing may be conical and have an opening angle, in particular in the range of 60 °.
  • At least one sieve according to claim 10 can ensure retention or dissolution of bulk agglomerates in front of the heat exchanger device. It may be a single sieve or it may also be provided two sieves with in particular different mesh size between the task point and the inlet openings.
  • a displacement element according to claim 11 can also lead to a homogenization of the loading of the heat exchanger tubes with bulk material.
  • a subdivision of the extension section into an extension zone and a calming zone according to claim 12 also ensures a Homogenization of the loading of the heat exchanger tubes with bulk material.
  • the internal cross section of the heat exchanger section is the entire inside width of the heat exchanger section, which of course always is greater than the sum of the cross sections of the heat exchanger tubes extending in the heat exchanger section.
  • An aspect ratio LBZ / DBZ greater than 0.1 has been found to be particularly suitable. This aspect ratio LBZ / DBZ is preferably greater than 0.5 and more preferably greater than 1.
  • Cross-sectional dimensional ratios QF / QWTR have been found to be particularly suitable for achieving a high heat exchanger efficiency.
  • the aspect ratio QF / QWTR is between 0.5 and 50, and more preferably between 1 and 30.
  • the advantages in connection with the downstream heat exchanger device are particularly well to fruition.
  • the processing plant can be operated with various bulk materials in the field of powder coatings, in the field of the chemical industry, in the food industry, the pharmaceutical industry, the cosmetic industry, in the field of fibrous natural products and animal feed and with minerals as bulk materials.
  • the processing plant for the production of powder coatings can be dispensed with an expensive nitrogen cooling after the milling device.
  • a processing plant 1 for bulk material has a conveying device 2 for the bulk material and a heat exchanger device 3 for cooling and / or heating of the bulk material.
  • the feed device 2 has a bulk material feed device 4 with a feed container 5. From the feed container 5 is fed via a feed element 6, in the illustrated embodiment with a rotary valve, the bulk material 7 in a pneumatic pressure-conveying line 8.
  • the rotary valve 6 can be a blow-through or a discharge lock.
  • a feed device 6 a pressure-transmitting vessel, a screw lock or a double-flap lock can be used.
  • the conveyor device 2 further has a feed device 9 for a conveying gas.
  • the feed device 9 has a compressed gas network 10, from which the delivery gas is removed.
  • the delivery gas can also be generated by a compressed gas generator such as a positive displacement blower, a fan or a screw compressor.
  • the conveying gas is air.
  • nitrogen which may be contaminated with hydrocarbons, are used.
  • the delivery gas may also consist entirely of one or more hydrocarbons.
  • short-chain gaseous hydrocarbons such as ethane, ethene, ethylene, propane, propene, butane or butene can be used.
  • the gas flow control 12 which includes an air or gas flow sensor or a pressure sensor and a controllable throttle valve, a quantity of conveying gas flows to the pneumatic Promotion of bulk material 7 regulated specified.
  • the conveying gas flows in the clean gas line 11 to a feed point 13. At this the feed gas mixes with the added via the feed member 6 bulk material.
  • the delivery line section 15 can be designed to extend in cross-section between the pipe bend 14 and the extension section 16 in comparison to the other delivery line 8. This can improve a dispersion of the bulk material 7 in front of the extension section 16.
  • An aspect ratio R / DF between a bending radius R of the pipe bend 14 and an outer diameter DF of the delivery line 8 between the pipe bend 14 and the extension section 16 is in the illustrated embodiment (see. FIG. 2 Also other dimensional ratios R / DF in a range between 1.5 and 20, in particular in a range between 3 and 10, are possible.
  • An aspect ratio LF / DF between a length LF of the delivery line section 15 between the pipe bend 14 and the extension section 16 and an outer diameter DF of this delivery line section 15 is in the illustrated embodiment (see FIG. FIG. 2 ). Also other dimensional ratios LF / DF greater than or equal to 5, 10 or 20 are possible.
  • the expansion section 16 initially has a conical expansion zone 18 in the bulk material flow path, corresponding to a cone opening angle ⁇ E (cf. FIG. 3 ) steadily increasing conveyor cross section and then a calming zone 19 with a constant delivery cross section DBZ.
  • the conveyor cross section DBZ the calming zone 19 corresponds in the example of Fig. 2
  • the delivery cross section DBZ of the settling zone 19 can also be greater than the internal cross section of the subsequent heat exchanger section 20.
  • the settling zone 19 can be a zone conically tapering in the conveying direction between the extension zone 18 and the heat exchanger section 20.
  • the cone angle ⁇ E is 60 ° in the illustrated embodiment.
  • the cone angle ⁇ E can be between 30 ° and 90 °.
  • An aspect ratio LBZ / DBZ between a length LBZ (cf. FIG. 2 ) of the calming zone 19 and the conveying cross section, ie the diameter DBZ, of the calming zone 19 is approximately 0.7 in the illustrated embodiment. Also other dimension ratios are LBZ / DBZ possible, in particular a ratio LBZ / DBZ which is greater than 0.1, greater than 0.5 or greater than 1.
  • each of the heat exchanger tubes 21 has an inlet opening 22 for the bulk material 7 and an outlet opening 23 for the bulk material 7.
  • the extension section 16 is arranged below the inlet openings 22.
  • the extension section 16 defines a collecting space into which all inlet openings 22 of the heat exchanger tubes 21 open.
  • the heat exchanger section 20 opens a feed nozzle of a feed 24 for a heat transfer fluid. From the heat exchanger section 20 opens a discharge nozzle of a discharge 25 for the heat transfer fluid.
  • the heat transfer fluid can be water, steam, a heat transfer oil or even a gas, for example air.
  • the heat transfer fluid is guided in the interior of the heat exchanger section 20 of the heat exchanger housing 17 in the flow path from the feed line 24 to the outlet 25 between the heat exchanger tubes 21.
  • baffles can be mounted transversely to the longitudinal direction of the heat exchanger tubes 21 at a distance from each other so that the heat transfer fluid between the supply 24 and the discharge 25 meandering through the interior of the heat exchanger section 20 each transverse to the longitudinal direction the heat exchanger tubes 21 gradually flows from top to bottom.
  • the heat exchanger section 20 is thus designed for a cross counterflow of the heat transfer fluid relative to the transported through the heat exchanger tubes 21 bulk material 7.
  • the interior of the heat exchanger section 20 between the heat exchanger tubes 21 may be filled with a heat transfer tubes 21 enveloping bed of glass beads, steel balls or plastic granules, which contributes to the improvement of heat transfer between the heat transfer fluid and the heat exchanger tubes 21.
  • a plurality of feeds open into and out of this several feeds for the heat transfer fluid. Between these inlets and outlets can then be provided separate paths for the heat transfer fluid.
  • the heat exchanger section can be subdivided into subsections along the conveying path, with each subsection being assigned a feed and an outlet for the heat carrier fluid.
  • a pitch of the heat exchanger tubes 21 is 1.05 D ⁇ b ⁇ 3 D, and preferably 1.10 D ⁇ b ⁇ 1.25 D.
  • D is the outer diameter of one of the heat exchanger tubes 21 and b is the distance of the center axes of two adjacent heat exchanger tubes 21 (see FIG , FIG. 5 ).
  • the inner diameter d of one of the heat exchanger tubes 21 is also shown.
  • the heat exchanger tubes 21 have an inner diameter d of 26 mm.
  • the heat exchanger tubes 21 may have an inner diameter d which is in the range of 5 mm to 100 mm.
  • Typical inner diameter d of the Heat exchanger tubes 21 are depending on the configuration of the heat exchanger section 17 in the range between 8 mm and 60 mm and are usually between 10 mm and 30 mm.
  • the heat exchanger tubes 21 are connected on the one hand in the region of the inlet openings 22 and on the other hand in the region of the outlet openings 23 via tube sheets, not shown, to the heat exchanger housing 17.
  • the inlet openings 22 and the outlet openings 23 may be funnel-shaped.
  • the inlet openings 22 and the outlet openings 23 may be formed recessed in the respective tube sheet. End portions of the heat exchanger tubes 21 with the inlet openings 22 on the one hand and the outlet openings 23 on the other hand then do not over the associated tube sheets over.
  • At least one vibrator may be arranged on the heat exchanger housing 17.
  • the vibration generated by the vibrator of the heat exchanger section 20 can further improve a heat transfer between the heat transfer fluid and the bulk material 7.
  • the heat exchanger tubes 21 have a length of 4 m in the illustrated embodiment. Other lengths between 0.5 m and 50 m, preferably between 0.5 m and 24 m, more preferably between 1 m and 12 m and even more preferably between 2 m and 6 m are possible.
  • the heat exchanger tubes 21 are arranged vertically. To increase an outer and / or an inner surface, the heat exchanger tubes 21 may be structured. This is in the FIG. 5 shown schematically in one of the heat exchanger tubes 21.
  • the surface enlarging Structures may be designed as indentations 26 or elevations 27 in the tube jacket of the heat exchanger tubes 21.
  • a typical dimension E of the indentations 26 or the elevations 27 and a typical deviation A of the indentations 26 or the elevations 27 from the surrounding shell wall of the heat exchanger tubes 21 may be in the range between 1 mm and 1 cm.
  • the heat exchanger tubes 21 may have additional cross-sectional profile elements 28 for enlarging an inner surface of the heat exchanger tubes 21.
  • These cross-sectional profile elements 28 are in the FIG. 5 shown as radially in one of the heat exchanger tubes 21 extending ribs.
  • the cross-sectional profile elements 28 may be extruded profile sections together with the heat exchanger tubes 21.
  • a displacement element 29 may be arranged in the bulk material flow path within the extension section 16, as in the FIG. 2 schematically indicated.
  • the displacement element may also have two cones connected to each other at the base, wherein the two cones have the same base surfaces and in addition to the cone corresponding to that in the Fig. 2 shown displacement element 29 is still a remote therefrom, so oriented toward the heat exchanger section 20 further cone, is present.
  • the two cones may have different cone angles.
  • the cone which is aligned with the heat exchanger section 20 can in this case have the larger cone angle exhibit.
  • the displacement element 29 is fixed in the extension zone 18 of the expansion section 16. Due to the deflecting effect of the cone wall, the displacement element 29 serves to improve distribution of the bulk material 7 flowing from the delivery line section 15 into the heat exchanger device 3 onto the individual heat exchanger tubes 21.
  • one or more centrically arranged instead of a single displacement element in the extension section 16, one or more centrically arranged be arranged funnel-shaped baffles. These can likewise bring about a homogenization of the admission of the heat exchanger tubes 21 to the bulk material 7.
  • An aspect ratio QF / QWTR between a cross-sectional area QF of the delivery pipe 8 between the delivery point 13 and the extension portion 16 and a cross-sectional area QWTR representing the sum of all cross-sectional areas QW of all the heat exchanger tubes 21 is 0.25 ⁇ QF / QWTR ⁇ 100.
  • the aspect ratio QF / QWTR can also be between 0.5 and 50, in particular between 1 and 30.
  • At least one sieve 31 may be arranged.
  • a mesh size of the sieve can be greater than a grain size of the bulk material 7.
  • two sieves with in particular different mesh sizes can be provided. Close to the execution FIG. 1 the screen 31 is arranged in the extension zone 18 of the extension section 16.
  • the heat exchanger section 20 is followed by a tapered section 32 in the heat exchanger housing 17.
  • the taper portion 32 is than with a cone angle ⁇ V (cf. Fig. 4 ) tapered cone section executed.
  • the cone opening angle ⁇ V of the taper portion 32 is 60 ° in the illustrated embodiment.
  • the cone opening angle ⁇ V can have values between 50 ° and 120 °.
  • Cross-sectional areas of the extension portion 16, the heat exchanger portion 20 and the taper portion 32 are made round in the illustrated embodiment. Alternatively, these cross-sectional areas can also be trimmed triangular, square or polygonal.
  • the tapering section 32 provides a collecting space into which all outlet openings 23 of the heat exchanger tubes 21 open.
  • the mixture of conveying gas and bulk material 7 is fed to a discharge conveyor line 33. Downstream of the outlet conveyor line 33 is a separator 34. This is in the FIG. 1 shown as a cyclone separator. Alternatively, the separator 34 may also be a filter.
  • the purified conveying gas is discharged via an exhaust pipe 35.
  • the deposited in the separator 34 bulk material 7 is discharged via a discharge member 36, which in turn may be a rotary valve.
  • the conveying device 2 is designed as pressure conveying. Alternatively, it is possible to design the conveying device 2 as a suction conveyor. Instead of the compressed gas network 10, a suction filter for the delivery gas is then arranged in the delivery line 8. To the exhaust pipe 35, a suction fan is then connected.
  • a switch 37, 38 is provided in each case, which are connected to one another via a bypass line 39.
  • the extension section 16, the heat exchanger section 20 and the taper section 32 that is to say the entire heat exchanger device 3 can be bypassed during operation of the processing installation 1, for example for cleaning purposes.
  • a bulk material outlet opening 40 is provided above the switch 37 in the conveyor line section 15. For cleaning purposes, inspection openings can still be provided in sections 16, 20, 32, which are not shown in the drawing.
  • a pneumatic conveying of the bulk material 7 takes place.
  • the feed devices 4, 9 for the bulk material 7 on the one hand and the conveying gas on the other hand are matched to one another and to the bulk material 7 to be processed, that at least in the heat exchanger tubes 21, the pneumatic conveying of the debris 7 is present.
  • An empty tube gas velocity in the heat exchange tubes 21 is at least 10 times as large as a minimum fluidization velocity in the corresponding inner tube diameter of the heat exchanger tube 21.
  • the feed gas feeding device 9 may also be designed such that the empty tube gas velocity in the heat exchange tubes 21 is 50 times or 100 times as large this minimum fluidizing speed. This design is such that the fluidization speed is optimized for high heat transfer with low delivery gas pressure loss.
  • a residence time of the bulk material 7 lies in the operation of the processing plant 1 between the inlet opening 22 and the outlet opening 23 of an individual Heat exchanger tube 21 at less than 30 s, preferably less than 20 s or less than 5 s.
  • ⁇ which is defined as the ratio of the bulk material mass flow to the mass flow of conveying gas (unit: [kg / kg]), which is greater than 1, and which can be greater than 5, greater than 10, greater than 15 , greater than 20 and also greater than 35.
  • a temperature difference of the bulk material 7 between the temperature of the bulk material 7 in the region of the inlet opening 22 and the temperature of the bulk material 7 in the region of the outlet opening 23 of an individual heat exchanger tube 21 is greater than 10 K.
  • pipe bend 14 may be provided in the flow path of the bulk material 7 between the delivery point 13 and the extension portion 16, a deflection in the form of a baffle plate.
  • the processing of the bulk material 7 in the processing plant 1 is done as follows: About the gas flow control 12, the feeders 4, 9 so matched to each other and on the bulk material to be processed that in the delivery line 8, in the heat exchanger tubes 21 and in the outlet conveyor line 33 a pneumatic conveying of the bulk material 7 is present.
  • the bulk material / conveying air mixture can also be present in the fluidized state.
  • the delivery cross section of the extension section 16 may be larger than the following cross section of the heat exchanger section 20, which may coincide with the cross section of the tubesheet supporting the heat exchanger tubes 21. This larger conveying cross section in the extension section 16 can be selected before the entry into the heat exchanger tubes 21 in order to reduce the conveying gas velocity and thereby facilitate equalization of the bulk material / conveying gas mixture.
  • a heat exchange takes place between the bulk material 7 and the heat transfer fluid surrounding the heat exchanger tubes 21.
  • the temperature of the bulk material 7 approaches on passing through the heat exchanger tubes 21 to the temperature of the heat transfer fluid.
  • a temperature difference of the bulk material 7 between the temperature at the inlet openings 22 and the temperature at the outlet openings 23 of the heat exchanger tubes 21 depends on the temperature difference between the inlet-side bulk material 7 and the heat transfer fluid and on the pneumatic conveying conditions and the heat transfer efficiency. This temperature difference is usually at least one Kelvin and is measurable in any case.
  • the conveying gas velocity in the heat exchanger tubes 21 is greater than the rate of descent of a bulk particle collective or greater than the rate of descent of a bulk individual grain having a mean grain diameter d 50 .
  • the processing plant has a throughput of 5840 kg / h of the bulk material 7.
  • the inlet temperature of the bulk material 7 in the inlet openings 22 of the heat exchanger tubes 21 is 66.8 ° C.
  • the outlet temperature of the bulk material 7 in the region of the outlet openings 23 of the heat exchanger tubes 21 is 53.7 Cooling water with an amount of 3700 kg / h conducted through the feed 24 and the discharge 25 is used as the heat transfer fluid, with an average cooling water temperature between the feed 24 and the discharge 25 of approximately 34 ° C.
  • Delivery gas in the delivery line 8 is 12.4 m / s in the region of the feed point 13 and 19.0 m / s in the region of the discharge delivery line 33.
  • a loading ⁇ in the conveying line 8 is 42 kg of bulk material 7 per kg of the conveying gas.
  • the delivery line 8 may be provided with an internal or external bypass for pneumatic conveying. This ensures a stable delivery at high loading and reduces the risk of clogging of the delivery line 8 by the bulk material. 7
  • FIG. 6 Based on FIG. 6 a further embodiment of a processing plant 41 for the bulk material 7 will be described. Components which correspond to those described above with reference to FIGS. 1 to 5 already described, bear the same reference numbers and will not be discussed again in detail.
  • a rotary valve 43 as a feed with a subsequent sloping down to the delivery point 13 downpipe 44.
  • Delivery gas is in the task point 13 in the FIG. 6 fed from below, so that in turn forms in the conveyor line section 15, the bulk / conveying gas mixture for pneumatic conveying.
  • the following heat exchanger device 3 corresponds to the one mentioned above in connection with FIGS. 1 to 5 was explained.
  • a pulverulent bulk material in particular a good fluidisable bulk material, can be used within the processing plant 1.
  • Average grain diameters d 50 of the bulk material 7 are in the range between 1 ⁇ m to 6,000 ⁇ m, in particular between 5 ⁇ m to 1,000, preferably between 10 ⁇ m and 500 ⁇ m and more preferably between 10 ⁇ m and 200 ⁇ m.
  • PTA terephthalic acid
  • plastic powder for example in the form of powder or granulated sugar, alumina powder, cement flour, melamine powder or a catalyst powder
  • sugar for example in the form of powder or granulated sugar
  • alumina powder alumina powder
  • cement flour melamine powder
  • melamine powder melamine powder
  • a catalyst powder a food powder such.
  • Milk powder can come as a bulk material 7 are used.
  • the bulk material 7 is cooled in the heat exchanger device 3, in particular after a fluidized bed or after a spray agglomeration, for example in a spray tower.
  • FIG. 7 a further embodiment of a processing plant 45 for the bulk material 7 will be described below.
  • Components corresponding to those described above with reference to the Fig. 1 to 6 have already been explained, bear the same reference numbers and will not be discussed again in detail.
  • a grinding device 46 is arranged between the delivery point 13 and the heat exchanger device 3, which in the Fig. 7 is indicated only schematically.
  • the grinding device 46 grinds the incoming bulk material 7, which has a first average particle size has, in outgoing bulk material with a second, smaller average particle size.
  • the grinding device may be a mill, such as in the DE 42 00 517 A1 and the DE 41 24 855 A described.
  • a type of grinding device can be used, which in the DE 694 08 267 T2 is described. At least one of the following types of grinders may be used: shredder, jet mill, hammer mill, wind sifter mill.
  • An inlet of the grinding device 46 is connected via the conveying line 8 with the delivery point 13 in pneumatic conveying connection for the incoming bulk material.
  • An outlet of the grinding device 46 communicates with the heat exchanger device 3 in pneumatic conveying connection for the outgoing, ground bulk material.
  • Fig. 7 To drive the grinding device 46 is used in the Fig. 7 also schematically illustrated drive motor 47, for example in the form of an electric motor.
  • grinding of the ground bulk material can take place in the grinding device 46, as is known from classifier mills.
  • Nitrogen can be used in particular as conveying gas in the processing plant 45.
  • the separator 34 which is designed as a cyclone in the case of the processing plant 45, may be arranged downstream of the exhaust pipe 35, a further fine dust filter 48.
  • the incoming bulk material into the grinding device 46 may be powder coating platelets, which constitute an intermediate in powder coating production.
  • a powder coating extrudate with an extruder, not shown.
  • This extrudate is then cooled in a cooling and forming device, also not shown, and formed into a sheet in the form of a wide thin strip.
  • the thus formed extrudate is then comminuted to the powder coating platelets. These platelets then represent the bulk material 7 entering the grinding device 46.
  • the pneumatic conveying of the bulk material in the processing plant 45 can also be done via a suction conveyor.
  • a typical fineness of the milled powder is d 97 ⁇ 10 ⁇ m.
  • the index "97" here means that 97% of the powder has a particle size smaller than 10 microns.
  • the expelled crushed bulk material heated in the grinding device 46 during grinding is cooled in the heat exchanger device 3.
  • the heat exchanger device 3 of the processing plant 45 are a total of 40 heat exchanger tubes with an inner diameter d of 26 mm before. Other inner diameters d in the range, for example, between 10 mm and 30 mm are possible.
  • the empty-tube gas velocity in the heat exchanger tubes of the heat exchanger 3 of the processing plant 45 is 10 m / s to 100 m / s, preferably 20 m / s to 70 m / s and even more preferably 30 m / s to 40 m / s.
  • the nominal diameter of the delivery line 8 in the case of the processing plant 45 is exactly as large as the nominal diameter of the heat exchanger housing 17. This is not to scale Fig.
  • the lines are only indicated as lines, not to be seen.
  • the processing plant 45 therefore, there is no extension section in front of the heat exchanger section 20 and also no taper section after the heat exchanger section 20.
  • a collecting space of the heat exchanger housing is arranged between the delivery point 13 and the inlet openings of the heat exchanger tubes, into which all inlet openings of the heat exchanger tubes open and in the Fig. 7 is also provided with the reference numeral 16.
  • the heat exchanger device 3 may alternatively be arranged horizontally with horizontally extending heat exchanger tubes.
  • the heat exchanger device 3 is designed with respect to the design of the heat exchanger housing 17 with a pressure shock resistance of 10 bar.
  • the processing plant 45 is operated with a powder coating throughput of 500 to 1500 kg / h. During operation of the processing system 45, a gas quantity of about 45 to 60 m 3 / min is passed through the grinding device 46.
  • the bulk material to be ground may be powder coating, for example acrylate clearcoat, epoxy / polyester, polyamide or UV-curing powder coatings.
  • the processing plant 45 can also be operated for a chemical application become.
  • bisphenol A, E-PVC, a fungicide, a herbicide, melamine, a pesticide, a polyester resin, carbon black or a stearate are used as the bulk material to be ground.
  • the processing plant 45 can be used.
  • algae, ascorbic acid, dried peas, face powder, cocoa, cacao cake, lactose, paracetamol, powdered sugar, rice starch, thickener, tartaric acid or sugar can be used.
  • fibrous natural products and animal feed, in particular grain and wood, corn, reed and wood plastic composites (WPC, wood / plastic composites) can be processed with the processing plant 45.
  • minerals such as bauxite, limestone, kaolin, calcium sulfate, sodium bicarbonate, talc and uranium oxide can be processed as bulk material in the processing plant 45.

Landscapes

  • 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)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
EP09008717.2A 2008-08-18 2009-07-03 Installation de traitement pour produits en vrac Withdrawn EP2159526A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102008038182 2008-08-18
DE102009014786A DE102009014786A1 (de) 2008-08-18 2009-03-25 Bearbeitungsanlage für Schüttgut

Publications (2)

Publication Number Publication Date
EP2159526A2 true EP2159526A2 (fr) 2010-03-03
EP2159526A3 EP2159526A3 (fr) 2013-11-13

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Country Link
EP (1) EP2159526A3 (fr)
DE (1) DE102009014786A1 (fr)

Cited By (6)

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EP2378230A2 (fr) 2010-04-15 2011-10-19 Coperion GmbH Dispositif destiné à refroidir ou à chauffer des materiaux en vrac
EP2489489A1 (fr) * 2011-02-18 2012-08-22 Coperion GmbH Dispositif de fabrication de granulés en matières premières polymères
DE102011078954A1 (de) * 2011-07-11 2013-01-17 Coperion Gmbh Schüttgut-Wärmetauschervorrichtung
DE102011078948A1 (de) * 2011-07-11 2013-01-17 Coperion Gmbh Wärmetauschersystem für Schüttgut sowie Verfahren zum Betrieb eines derartigen Wärmetauschersystems
DE102012221973A1 (de) 2012-11-30 2014-06-18 Coperion Gmbh Schüttgut-Wärmetauschervorrichtung
KR20180119118A (ko) * 2017-04-24 2018-11-01 코페리온 게엠베하 플라스틱 펠릿을 공압 수송하는 방법

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DE102012208386A1 (de) 2012-05-18 2013-11-21 Coperion Gmbh Anlage zum Bearbeiten von Schüttgut
DE102012208502A1 (de) 2012-05-22 2013-11-28 Coperion Gmbh Vorrichtung zum Behandeln von Schüttgut
CN113932632B (zh) * 2020-07-13 2024-05-14 江苏集萃冶金技术研究院有限公司 富含熔融气化组分的含尘气体余热及组分回收利用工艺

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US3524498A (en) * 1968-04-10 1970-08-18 Nat Gypsum Co Cooling apparatus
DE2504782A1 (de) * 1975-02-05 1976-08-19 Polysius Ag Schachtkuehler
DE3543664A1 (de) * 1984-12-17 1986-06-19 Veb Kombinat Textima, Ddr 9010 Karl-Marx-Stadt Kuehl- und trockensystem, insbesondere fuer kunststoffgranulat
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EP2378230A2 (fr) 2010-04-15 2011-10-19 Coperion GmbH Dispositif destiné à refroidir ou à chauffer des materiaux en vrac
DE102010027801A1 (de) * 2010-04-15 2011-10-20 Coperion Gmbh Vorrichtung zum Kühlen oder Heizen von Schüttgut
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CN102269531A (zh) * 2010-04-15 2011-12-07 科倍隆有限公司 用于冷却或加热松散材料的设备
EP2489489A1 (fr) * 2011-02-18 2012-08-22 Coperion GmbH Dispositif de fabrication de granulés en matières premières polymères
DE102011078948A1 (de) * 2011-07-11 2013-01-17 Coperion Gmbh Wärmetauschersystem für Schüttgut sowie Verfahren zum Betrieb eines derartigen Wärmetauschersystems
DE102011078954A1 (de) * 2011-07-11 2013-01-17 Coperion Gmbh Schüttgut-Wärmetauschervorrichtung
DE102011078954B4 (de) * 2011-07-11 2014-05-08 Coperion Gmbh Schüttgut-Wärmetauschervorrichtung
DE102011078948B4 (de) * 2011-07-11 2014-09-25 Coperion Gmbh Wärmetauschersystem für Schüttgut sowie Verfahren zum Betrieb eines derartigen Wärmetauschersystems
DE102012221973A1 (de) 2012-11-30 2014-06-18 Coperion Gmbh Schüttgut-Wärmetauschervorrichtung
KR20180119118A (ko) * 2017-04-24 2018-11-01 코페리온 게엠베하 플라스틱 펠릿을 공압 수송하는 방법
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US10647527B2 (en) 2017-04-24 2020-05-12 Coperion Gmbh Method for pneumatically conveying plastic pellets

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DE102009014786A1 (de) 2010-02-25
EP2159526A3 (fr) 2013-11-13

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