EP1306636B1 - Procédé et appareil pour un chauffage uniforme d'un mélange de particules de poussière dans un flux gazeux chaud - Google Patents

Procédé et appareil pour un chauffage uniforme d'un mélange de particules de poussière dans un flux gazeux chaud Download PDF

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Publication number
EP1306636B1
EP1306636B1 EP20010123693 EP01123693A EP1306636B1 EP 1306636 B1 EP1306636 B1 EP 1306636B1 EP 20010123693 EP20010123693 EP 20010123693 EP 01123693 A EP01123693 A EP 01123693A EP 1306636 B1 EP1306636 B1 EP 1306636B1
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European Patent Office
Prior art keywords
hot gas
gas flow
grains
grain
flow
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EP20010123693
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German (de)
English (en)
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EP1306636A1 (fr
Inventor
Fritz Dr.-Ing. Schoppe
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F26B17/10—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers
    • F26B17/101—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers the drying enclosure having the shape of one or a plurality of shafts or ducts, e.g. with substantially straight and vertical axis
    • F26B17/102—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers the drying enclosure having the shape of one or a plurality of shafts or ducts, e.g. with substantially straight and vertical axis with material recirculation, classifying or disintegrating means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F26B17/10—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers
    • F26B17/107—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers pneumatically inducing within the drying enclosure a curved flow path, e.g. circular, spiral, helical; Cyclone or Vortex dryers
    • 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

Definitions

  • the invention relates to the heating of a mixture of fine-grained Good different grain size using a hot gas flow and in particular relates to a method and an apparatus according to the preamble of claim 1 and 7, respectively.
  • a method according to the preamble of claim 1 is known from US-A-4 380 125.
  • This document describes a process for drying and preheating coking coal in a single flow tube, in which a hot gas stream entraining the bottom fed, ground, wet coal rises, and at the top of the air flow tube, all of the dried and preheated coal the gas stream is separated out.
  • the gas stream is divided into two streams by the larger gas volume is deflected as the first partial flow entraining the finer grain fractions from the original direction and leave the smaller amount of gas as the second partial flow entraining the coarser grain fraction initially in its direction, then deflected and with the first partial flow is reunited in approximately opposite direction to this.
  • this procedure divides the grain size mixture carried by the gas stream into only two fractions, within the fractions different treatment of the grains depending on their individual grain size is not possible.
  • Fine-grained material in particular that which has been produced by grinding, has a particle size distribution which can have a broad spectrum, ranging for example from 1 ⁇ m to 1000 ⁇ m. Also oversize from 2000 microns to 3000 microns is possible.
  • the invention is therefore based on the object to provide a method and an apparatus with which in a short time a heating of a grain mixture can be achieved at the same temperature.
  • the grain mixture is introduced into a flow of hot gases and undergoes a change in temperature during transport along the flow path of the hot gases due to the contact with the hot gases, according to the invention provided that the flow path which the single grain together with the hot Traps gases, is short for small grains and long for large grains, so that a longer heat-up time is available for the large grains.
  • the invention avoids these disadvantages in an elegant manner in that the grain mixture is introduced into an upward hot gas flow from above so that the large grains reach the hot gas flow at a lower altitude than the smaller grains, so that the larger grains are given a longer flow path becomes, as the small grains. As a result, despite a compact size of the required device uniform heating of the grains of all sizes is achieved.
  • the grain mixture is preferably introduced by means of a downward carrier gas flow in the upward hot gas flow, said two gas flows preferably in a contact surface, the length seen in the flow direction of the gases at least four times, preferably six times the thickness of the carrier gas flow, measured transversely to the contact surface of the two gas flows is.
  • Grains that do not enter the hot gas due to oversize are conveniently deposited so as not to disturb the process.
  • the hot gas flow is helical from bottom to top and the carrier gas is directed down the axis of this helix.
  • the helical flow can be guided from bottom to top widening in a conical jacket.
  • pressure conditions set along the axis of the helical flow which favor the downward flow of the carrier gas flow.
  • the apparatus of Fig. 1 consists of two substantially mutually parallel flow channels 1 and 2, of which the left channel 1 has a width B1 which is smaller than the width B2 of the channel 2.
  • the channels 1 and 2 are open to each other over a distance O, and close to the end of this open area, the flow channel 1 is closed, preferably by a cellular Z.
  • a hot air flow H is introduced from below into the flow channel 2 of greater width B2.
  • a conveying air flow F is introduced from above, which carries a grain mixture with it, consisting of small grains K1, medium grains K2 and oversize K3.
  • This flow of carrier gas and grain mixture is hereinafter referred to as F + K1 + K2 + K3.
  • all intermediate grain sizes may be included in the grain mixture.
  • the turbulence of the two flows F + K1 + K2 + K3 and H is characterized by components transverse to the main flow direction. These transverse components act on the grains, with the small grains K1 following the transverse components most easily.
  • the medium-sized grains K2 react later on the transverse components, while the oversize K3 completely falls down due to its larger mass, does not get into the hot air flow and can be deducted for example by the feeder Z.
  • the small grains K1 arrive earlier, i. above, in the upwardly directed hot air flow H, and the medium sized granules K2 reach further down in the upward flow H.
  • the medium granules K2 have thus, when they have reached the top, covered the longer flow path and therefore for that reason a longer one Residence time in the hot air flow H as the smaller grains.
  • larger grains K2 are carried in a known manner more slowly in a gas flow upward than smaller grains K1, resulting in an additional extension of the residence time for the medium-sized grains K2 in the hot air flow H.
  • a hot air flow is given here only as an example.
  • a hot gas another gas can also be used, for example an inert gas, if a chemical reaction of the grain mixture with the hot gas is to be avoided.
  • the device consists of a vertically standing, upwardly flared truncated cone 3 with a lower diameter D1, an upper diameter D2 and an axial length E.
  • a logarithmic spiral S of width B1 is concentrically attached , The spiral S is completely described by its angle ⁇ against the circumferential direction.
  • the desired separation effect has a clear optimum at angles ⁇ , which are approximately between 5 ° and about 12 °, with best values between 6 ° and 9 °. Below and above these angle values, the separation effect diminishes rapidly.
  • a discharge head C At the upper end of the truncated cone 3 is followed by a discharge head C, which has a diameter D3, to which the upper diameter D2 of the truncated cone 3 widens conically over a width B2.
  • the cylindrical portion of the discharge head C has a width B3 is arched by a dome.
  • the discharge head C is followed by a discharge line A outside.
  • the discharge head C is penetrated by a dip tube T of a diameter D T , which extends into the region of the transition between the discharge head C and the truncated cone 3 at the diameter D2.
  • the dip tube T ends at the level of the upper end of the truncated cone. 3
  • a cellular wheel Z Centrally connected to the lower end of the logarithmic spiral S is a cellular wheel Z which, on the one hand, constitutes a closure, but on the other hand permits the withdrawal of oversize particles.
  • a hot gas H of the logarithmic spiral S is fed, which initiates the hot gas H in the space enclosed by the truncated cone 3 chamber, where due to the helix angle ⁇ of the logarithmic S forms a wall-near upward flow W, which superimposes a circumferentially extending component is, which is not shown in the drawing and causes the hot gas flow to develop like a spiraling upwards from the bottom.
  • a feed gas stream F is introduced through the dip tube T, which carries with it a grain mixture containing grains K1, K2 and K3 different size, as described in the first example.
  • a grain mixture containing grains K1, K2 and K3 different size as described in the first example.
  • the carrier gas flow F emerging from the dip tube T with the entrained grains is set in rotation in the chamber enclosed by the truncated cone 3 by the peripheral component of the hot gas flow.
  • the small grains K1 follow this rotation rapidly, the larger K2s slower according to their larger mass and inertia, and the over grain K3 hardly ever.
  • the oversize K3 falls down and can be removed by the feeder Z.
  • the small grains K1 thus reach the wall-near flow W very quickly and are therefore fed quickly to the upper cone diameter D2.
  • the larger grains K2 fall deeper below and only further down in the chamber into the near-wall current W. They have a longer residence time in the chamber compared to the grains K1 for two reasons: their way in the wall-oriented, upward flow W is longer than that of the small grains K1 , and they are carried up more slowly than the small grains K1 because of their higher sink rate.
  • the spiral angle ⁇ of the logarithmic spiral S is of importance. It should be between 5 ° and 12 °, with best values between 6 ° and 9 °. Below and above these angle values, the separation effect in the chamber enclosed by the truncated cone 3 decreases rapidly.
  • the iron oxide (predominantly Fe 2 O 3 ) has ambient temperature and contains 10% moisture. It is designed with 2546 m 3 n / h hot gas (kiln exhaust) of 800 ° C heated to a temperature of 400 ° C and dried at the same time. The hot gas with the entrained iron oxide is blown through the dip tube T in the return flow R, which is established due to the forming in the chamber in a known manner pressure conditions. Of the 2546 m 3 n / h hot gas about 127 m 3 n / h are diverted before the logarithmic spiral S and used as 800 ° C hot medium F.
  • the dip tube T is intended to reach approximately to the diameter D2.
  • the pressure loss of the hot gas H as it flows through the chamber enclosed by the truncated cone is about 2200 Pa.
  • water or another suitable liquid may also be used as the carrier medium.
  • suitable liquid for grains heavier than water, water or another suitable liquid may also be used as the carrier medium.
  • the above considerations also apply to liquids as a medium instead of the aforementioned gases.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Drying Of Solid Materials (AREA)

Claims (13)

  1. Procédé pour le chauffage homogène d'un mélange de grains grossiers et fins au moyen d'un courant de gaz chaud auquel des grains de grosseurs différentes sont exposés pendant des durées différenciées, caractérisé en ce que les grains sont, en fonction de leur grosseur, introduits à différents endroits dans le courant de gaz chaud, de manière à parcourir avec le gaz chaud une distance d'entraînement dont la longueur s'accroît à mesure que la grosseur de grain augmente.
  2. Procédé selon la revendication 1, caractérisé en ce que le mélange de grains est amené dans un courant de gaz chaud s'écoulant vers le haut au moyen d'un courant de gaz porteur s'écoulant vers le bas, de telle manière qu'une séparation du mélange de grains en fonction de la grosseur de grain soit effectuée avant le passage des grains dans le courant de gaz chaud et que les grains plus fins s'élèvent plus haut dans le courant de gaz chaud que les grains plus gros.
  3. Procédé selon la revendication 2, caractérisé en ce que le courant de gaz porteur s'écoulant vers le bas avec le mélange de grains qu'il contient et le courant de gaz chaud s'écoulant vers le haut entrent en contact sur une surface de contact dont la longueur dans le sens d'écoulement des gaz représente au moins le quadruple, de préférence le sextuple, de l'épaisseur du courant de gaz porteur mesurée transversalement à la surface de contact des courants de gaz.
  4. Procédé selon la revendication 2 ou 3, caractérisé en ce que les grains qui ne parviennent pas dans le gaz chaud en raison de leur grosseur trop élevée sont séparés.
  5. Procédé selon l'une des revendications 2 à 4, caractérisé en ce que le courant de gaz chaud s'écoule suivant une ligne hélicoïdale, et en ce que le gaz porteur s'écoule avec le mélange de grains vers le bas selon l'axe de cette ligne hélicoïdale.
  6. Procédé selon la revendication 5, caractérisé en ce que le courant de gaz chaud en ligne hélicoïdale est guidé de bas en haut dans une enveloppe conique.
  7. Dispositif pour la mise en oeuvre du procédé selon l'une des revendications précédentes, caractérisé par une chambre de réaction qui s'étend du bas vers le haut à la façon d'un cône tronqué et présente à son extrémité inférieure une spirale de conduction d'entrée (S) pour le gaz chaud (H) et à son extrémité supérieure une tête de déversement (C) et un tuyau d'amenée (T) traversant celle-ci selon une ouverture centrale, orientée axialement pour l'amenée du gaz porteur (F) et du mélange de grains (K1+K2+K3) entraîné par celui-ci, avec les paramètres suivants pour un débit de gaz chaud de 2546 mn 3/h sous une température de 800°C et une pression atmosphérique approximative : Angle d'hélice de la spirale de conduction d'entrée S : ∝ = 6 -9° Hauteur de la spirale de conduction d'entrée S : B1 = 225 mm Diamètre inférieur de la chambre de réaction : D1 = 385 mm Longueur axiale de la chambre de réaction : E = 1668 mm Diamètre supérieur de la chambre de réaction : D2 = 770 mm Hauteur de la tête de déversement : B3 = 500 mm
  8. Dispositif selon la revendication 7, caractérisé en ce que l'angle d'hélice α de la spirale de conduction d'entrée S est de 6,85°.
  9. Dispositif selon la revendication 7 ou 8, caractérisé en ce qu'une pièce de passage tronconique est disposée entre l'extrémité supérieure de la chambre de réaction et la tête de déversement (C), laquelle s'étend sur une longueur B2 de 135 mm environ sur le diamètre D3=1300 mm de la tête de déversement (C).
  10. Dispositif selon la revendication 7 ou 9, caractérisé en ce que, pour un débit de gaz chaud modifié par un facteur par rapport à un débit de 2546 mn 3/h, les dimensions linéaires du dispositif sont modifiées de la racine carrée du facteur susmentionné par rapport aux dimensions indiquées dans les revendications 7 à 9.
  11. Dispositif selon l'une des revendications 7 à 10, caractérisé par un dispositif de ramification à l'aide duquel une partie du courant de gaz chaud H est dérivée comme courant de gaz porteur pour le mélange de grains (K1+K2+K3) avant de pénétrer dans la spirale de conduction d'entrée (S).
  12. Dispositif selon l'une des revendications 7 à 10, caractérisé en ce qu'une évacuation (Z) pour les grains de grosseur trop élevée (K3) est prévue au centre de la spirale de conduction d'entrée (S).
  13. Dispositif selon l'une des revendications 7 à 12, caractérisé en ce que les dimensions D1 et B1 sont modifiées dans une plage de ± 20% par rapport aux cotes indiquées dans la revendication 7, le produit de B1 x D1 étant constant.
EP20010123693 2001-10-02 2001-10-02 Procédé et appareil pour un chauffage uniforme d'un mélange de particules de poussière dans un flux gazeux chaud Expired - Lifetime EP1306636B1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
DE50111696T DE50111696D1 (de) 2001-10-02 2001-10-02 Verfahren und Vorrichtung zur gleichmässigen Erhitzung eines Staubkörnergemisches in einer Strömung heisser Gase
EP20010123693 EP1306636B1 (fr) 2001-10-02 2001-10-02 Procédé et appareil pour un chauffage uniforme d'un mélange de particules de poussière dans un flux gazeux chaud

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Application Number Priority Date Filing Date Title
EP20010123693 EP1306636B1 (fr) 2001-10-02 2001-10-02 Procédé et appareil pour un chauffage uniforme d'un mélange de particules de poussière dans un flux gazeux chaud

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EP1306636A1 EP1306636A1 (fr) 2003-05-02
EP1306636B1 true EP1306636B1 (fr) 2006-12-20

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EP20010123693 Expired - Lifetime EP1306636B1 (fr) 2001-10-02 2001-10-02 Procédé et appareil pour un chauffage uniforme d'un mélange de particules de poussière dans un flux gazeux chaud

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Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8536258B2 (en) 2007-07-20 2013-09-17 Sumitomo Chemical Company, Limited Stabilizer and method of manufacturing the same, thermoplastic polymer composition using the same, and method of stabilizing thermoplastic polymer

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE479355A (fr) *
FR1363939A (fr) * 1962-03-22 1964-06-19 Smidth & Co As F L Procédé et appareil pour l'échange de chaleur entre des particules solides et des gaz
FR1362788A (fr) * 1963-06-14 1964-06-05 Smidth & Co As F L échangeur de chaleur
AT284795B (de) * 1968-07-10 1970-09-25 Ludwig Binder & Co Sprühtrocknungsverfahren und -einrichtung zur Herstellung von Trockenpulvern
DE2256385B2 (de) * 1972-11-17 1981-04-16 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zum kontinuierlichen Erhitzen feinkörniger Feststoffe
DE2942878C2 (de) * 1979-10-24 1983-10-06 Bergwerksverband Gmbh Verfahren und Vorrichtung zur Trocknung und Vorerhitzung von Kokskohle in einem einzigen Flugstromrohr

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DE50111696D1 (de) 2007-02-01

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