EP0714006B1 - Procédé de séchage d'une substance, en particulier de copeaux de bois - Google Patents

Procédé de séchage d'une substance, en particulier de copeaux de bois Download PDF

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Publication number
EP0714006B1
EP0714006B1 EP95810726A EP95810726A EP0714006B1 EP 0714006 B1 EP0714006 B1 EP 0714006B1 EP 95810726 A EP95810726 A EP 95810726A EP 95810726 A EP95810726 A EP 95810726A EP 0714006 B1 EP0714006 B1 EP 0714006B1
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EP
European Patent Office
Prior art keywords
heat exchanger
gas mixture
vapour
heated
temperature
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.)
Expired - Lifetime
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EP95810726A
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German (de)
English (en)
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EP0714006A1 (fr
Inventor
Werner Kunz
Cyrill Hammer
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W Kunz Drytec AG
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W Kunz Drytec AG
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Publication of EP0714006A1 publication Critical patent/EP0714006A1/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/02—Heating arrangements using combustion heating
    • F26B23/022—Heating arrangements using combustion heating incinerating volatiles in the dryer exhaust gases, the produced hot gases being wholly, partly or not recycled into the drying enclosure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B2200/00—Drying processes and machines for solid materials characterised by the specific requirements of the drying good
    • F26B2200/24—Wood particles, e.g. shavings, cuttings, saw dust

Definitions

  • the present invention relates to a method for drying a substance, in particular wood chips, as described in the preamble of claim 1.
  • the exhaust air emerging from the drum dryer contains, in addition to water vapor, gaseous wood constituents and aerosols, which cannot be released into the atmosphere without being cleaned, since the pollutant contents are too high.
  • the flue gas must therefore be cleaned, which can be done by filtration, washing and / or regenerative thermal oxidation.
  • An optimal cleaning of the flue gas would be obtained by combining these options. Since these facilities have to be purchased in addition to the entire drying system, this is an expensive solution, and the operation and maintenance of these additional systems is also complex.
  • the exhaust gas emerging from the combustion chamber can therefore, as a rule, be released directly into the atmosphere after passing through the first heat exchanger and heating the steam-gas mixture, with no optical cloudiness and no odor nuisance when emerging from the chimney.
  • the temperature In order to achieve the above-mentioned oxidations in the combustion chamber, the temperature must be kept at around 900 ° C.
  • the fuel gas having this temperature is fed to a first heat exchanger in which the steam-gas mixture fed into the drum dryer is heated to a temperature of approximately 500.degree. It has now been shown that on the entry side of the fuel gas into the first heat exchanger, the first flow around the heat exchanger elements is subject to strong heating, since the steam-gas mixture on the inside also already has a temperature of approximately 500 ° C.
  • the material of these first heat exchanger elements is exposed to such severe stresses that their service life is limited.
  • the object of the invention is to modify the known methods so that the thermal load on the heat exchanger elements is reduced and, consequently, their service life is increased.
  • this further heat exchanger in which the fuel gas is supplied at a high temperature, is flowed through by the decoupled part of the steam-gas mixture at a relatively low temperature, the material of the heat exchanger elements of this heat exchanger is consequently relatively strongly cooled from the inside, so that the thermal load on the material can be kept correspondingly low.
  • Fig. 1 shows a schematic representation of the sequence of the inventive method in a possible embodiment.
  • FIG. 2 shows a schematic representation of the sequence of the method according to the invention according to FIG. 1, with predrying being provided.
  • a burner 1 is supplied in a known manner with a fuel which is burned in the combustion chamber 2.
  • the supply air to this burner 1 or the combustion chamber 2 is supplied through the supply line 3.
  • the heated fuel gas is, before it is through a first heat exchanger 4 is passed, pass through a further heat exchanger 21.
  • the exhaust air passes through a second heat exchanger 5, in which the supply air fed to the burner 1 is heated, and via a line 6 into a chimney 7, through which the exhaust air is released into the atmosphere.
  • a steam-gas mixture is heated by the fuel gas.
  • the heated steam-gas mixture is fed to a drum dryer 8, in which the substance to be dried is introduced in a known manner via the feed 9.
  • a drum dryer 8 By drying wood shavings, for example, further steam and wood contents are released into the vapor-gas mixture in gaseous form and in the form of aerosols, such as volatile hydrocarbons.
  • the dried wood chips and the steam-gas mixture are fed via a closed channel 10 to a cyclone separator 11, in which the dried wood chips and the steam-gas mixture are separated. The further processing of the dried wood chips takes place in a known manner.
  • the steam-gas mixture is fed back into the first heat exchanger 4 with the aid of a fan 12. This creates a closed cycle for the steam-gas mixture.
  • a partial stream of the steam-gas mixture can be coupled out via a line 22.
  • This decoupled partial flow of the steam-gas mixture is passed through the further heat exchanger 21, after which it is introduced into the combustion chamber 2.
  • a flap 23 is provided in a known manner for flow rate control.
  • the fuel gas must reach a temperature of around 900 ° C so that all combustible gases can be combusted in the combustion chamber.
  • This fuel gas is cooled in the further heat exchanger 21 to a temperature of approximately 750 ° C., whereupon it reaches the first heat exchanger 4.
  • the steam-gas mixture is heated in this first heat exchanger 4 from approximately 130 ° C. to approximately 500 ° C.
  • the outcoupled partial flow of the steam-gas mixture brings about a reduction in the temperature of the fuel gas from 900 ° C. to 750 ° C.
  • this outcoupled part of the steam-gas mixture is approximately 130 ° C warmed to approximately 370 ° C. Due to the relatively low temperature of the outcoupled partial stream of the steam-gas mixture, the heat exchanger elements in the further heat exchanger 21 are not heated as much as a whole, even if the fuel gas flows around them at a temperature of 900 ° C., so that in this further heat exchanger 21 the thermal load on the material of the heat exchanger elements remains low and, as a result, a long service life is achieved.
  • the drying process according to the invention can thus keep the thermal load on the materials from which the heat exchanger elements in the heat exchangers 4 and 21 consist so that the service life of these elements is increased.
  • FIG. 2 shows in principle the same procedure for drying wood chips as in FIG. 1, the difference being that the exhaust air from the second heat exchanger 5 flows through a predrying device 14 and from there by means of a further fan 15 to the chimney 7 is supplied for release to the atmosphere.
  • the wood chips to be dried are passed through this predrying device 14 before they are fed to the drum dryer 8 through the feed 9.
  • these wood chips are preheated to a temperature of approximately 75 ° C.
  • the systems shown schematically in the two figures can be equipped in a known manner by the necessary control devices.
  • the method according to the invention can also be used to dry other substances, such as grass, sugar beet chips or sludges of any kind.

Claims (7)

  1. Procédé de séchage d'une substance, en particulier de copeaux de bois, dans un sécheur rotatif, à travers lequel un mélange vapeur-gaz chauffé dans un premier échangeur de chaleur passe selon un trajet essentiellement fermé, qui après passage dans le sécheur rotatif est renvoyé dans le premier échangeur de chaleur, un gaz d'échappement chauffé dans une chambre de combustion d'un brûleur étant conduit dans le premier échangeur de chaleur pour le chauffage du mélange vapeur-gaz, et une portion du mélange vapeur-gaz étant extraite du trajet pour être introduite dans la chambre de combustion, dans laquelle une combustion du gaz produit lors du séchage se produit, caractérisé en ce que l'extraction de la portion du mélange vapeur-gaz se fait avant l'introduction du mélange vapeur-gaz dans le premier échangeur de chaleur (4) et cette portion de mélange vapeur-gaz extraite passant par un autre échangeur de chaleur (21), à travers lequel le gaz d'échappement réchauffé sortant de la chambre de combustion (2) passe avant d'être conduite dans le premier échangeur de chaleur (4), afin de chauffer la portion de mélange vapeur-gaz.
  2. Procédé selon la revendication 1, caractérisé en ce que l'air amené au brûleur (1) passe par un deuxième échangeur de chaleur (5) et est chauffé par le gaz d'échappement du brûleur (1) après passage dans le premier échangeur de chaleur (4).
  3. Procédé selon l'une des revendications 1 ou 2, caractérisé en ce que la portion de mélange vapeur-gaz extraite est chauffée d'une température d'environ 130°C à une température de 350 à 400°C durant le passage dans l'autre échangeur de chaleur (21).
  4. Procédé selon l'une des revendications 1 à 3, caractérisé en ce que le gaz d'échappement chauffé dans la chambre de combustion (2) est refroidi à une température d'environ 750°C durant le passage par l'autre échangeur de chaleur (21) et avant l'entrée dans le premier échangeur de chaleur (4).
  5. Procédé selon l'une des revendications 1 à 4, caractérisé en ce que le mélange vapeur-gaz est chauffé d'une température d'environ 130°C à une température d'environ 500°C durant le passage par le premier échangeur de chaleur (4), et le gaz d'échappement est refroidi à une température d'environ 180°C.
  6. Procédé selon l'une des revendications 2 à 5, caractérisé en ce que le gaz d'échappement sortant de la chambre de combustion (2) du brûleur (1) est conduit après passage dans le deuxième échangeur de chaleur (5) dans un dispositif de préséchage (14), dans lequel la substance à sécher est préséchée, après quoi le gaz d'échappement est relâché dans l'atmosphère.
  7. Procédé selon la revendication 6, caractérisé en ce que la substance à sécher est préchauffée à environ 75°C dans le dispositif de préchauffage (14).
EP95810726A 1994-11-24 1995-11-21 Procédé de séchage d'une substance, en particulier de copeaux de bois Expired - Lifetime EP0714006B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CH3549/94 1994-11-24
CH354994 1994-11-24

Publications (2)

Publication Number Publication Date
EP0714006A1 EP0714006A1 (fr) 1996-05-29
EP0714006B1 true EP0714006B1 (fr) 1997-12-29

Family

ID=4258390

Family Applications (1)

Application Number Title Priority Date Filing Date
EP95810726A Expired - Lifetime EP0714006B1 (fr) 1994-11-24 1995-11-21 Procédé de séchage d'une substance, en particulier de copeaux de bois

Country Status (5)

Country Link
US (1) US5697167A (fr)
EP (1) EP0714006B1 (fr)
AT (1) ATE161622T1 (fr)
CA (1) CA2163305A1 (fr)
DE (1) DE59501167D1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10056459C1 (de) * 2000-11-14 2002-04-04 Fraunhofer Ges Forschung Verfahren zum Aufbereiten faseriger Substanzen
DE10157596C1 (de) * 2001-11-23 2003-03-20 Fraunhofer Ges Forschung Verfahren zum Aufbereiten faseriger Substanzen
DE10221367B4 (de) * 2002-05-13 2006-05-11 Bankwitz, Robert, Dr. Pneumatischer Schleudertrockner

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DE19710711A1 (de) * 1995-09-22 1998-09-17 Dieffenbacher Gmbh Maschf Verfahren, Filterpresse sowie Steuer- und Regeleinrichtung zur Reduzierung des Wassergehaltes von Feststoffmaterialien und/oder Schlämmen
SE9601721L (sv) * 1996-05-06 1997-11-07 Flaekt Ab Trätorkningsanläggning samt förfarande för att rena en torkgas från en trätorkningsanordning
DE19654043C2 (de) * 1996-12-23 1998-05-28 Martin Dipl Ing Knabe Trockner mit Abgasreinigung mittels thermischer Nachverbrennung
US6163981A (en) * 1998-11-25 2000-12-26 Nilsson; Bengt Method and apparatus for drying wood particles
US6393727B1 (en) * 1999-10-01 2002-05-28 Louisiana-Pacific Corporation Method for reducing VOC emissions during the manufacture of wood products
DE10011177A1 (de) * 2000-03-08 2001-09-20 Valmet Panelboard Gmbh Verfahren und Vorrichtung zum direkten Trocknen von Teilchen
TW562700B (en) * 2000-11-28 2003-11-21 Takamo Ind Co Ltd Garbage processing machine
WO2003052336A1 (fr) * 2001-12-17 2003-06-26 Holm Christensen Biosystemer Aps Dispositif de sechage de produit particulaire au moyen d'un flux surchauffe
GB0214412D0 (en) 2002-06-21 2002-07-31 Svonja George Method and apparatus for drying
DE10349090A1 (de) * 2003-10-22 2005-06-16 Eisenmann Maschinenbau Gmbh & Co. Kg Anlage und Verfahren zum Trocknen von Gegenständen
US20060101663A1 (en) * 2004-11-08 2006-05-18 Perin Nolan A Lumber drying
EP1843114A1 (fr) * 2006-04-06 2007-10-10 Swedish Exergy Consulting AB Installation de séchage
US7456326B2 (en) * 2007-03-01 2008-11-25 Praxair Technology, Inc. VOC reduction in ethanol plants
ATE520939T1 (de) * 2008-01-10 2011-09-15 Douglas Technical Ltd Verfahren zur kontinuierlichen trocknung von schüttgut, insbesondere von holzfasern und/oder holzspänen
PT2230477E (pt) * 2009-03-10 2015-03-04 Kronotec Ag Instalação de secagem de aparas de madeira para secagem de aparas de madeira e processo associado de secagem de aparas de madeira
WO2010110702A1 (fr) * 2009-03-25 2010-09-30 Svensk Rökgasenergi Intressenter Ab Système et procédé de séchage
DE102010012005A1 (de) * 2010-03-15 2011-09-15 Dürr Systems GmbH Thermische Abluftreinigungsanlage
CH708975B1 (de) * 2013-12-04 2016-07-15 Kaindl Rupert Verbrennungsanlage.
US11499778B2 (en) 2017-03-03 2022-11-15 Douglas Technical Limited Apparatus and method for continuously drying bulk goods, in particular wood chips and/or wood fibers comprising a solid fired hot gas generator
CN110382961A (zh) 2017-03-03 2019-10-25 道格拉斯科技有限公司 用于连续干燥散装物品、特别是木屑和/或木纤维的包括热气旋风分离器的设备和方法
CA3053986C (fr) 2017-03-03 2023-03-07 Douglas Technical Limited Appareil et procede de sechage continu de produits en vrac, en particulier de copeaux de bois et/ou de fibres de bois comprenant un bruleur multicombustible dote d'un systeme de r efroidissement de moufle
WO2018157947A1 (fr) 2017-03-03 2018-09-07 Douglas Technical Limited Appareil et procédé de séchage continu de produits en vrac, en particulier de copeaux de bois et/ou de fibres de bois, comprenant un échangeur de chaleur
EP3635312A1 (fr) 2017-06-06 2020-04-15 Douglas Technical Limited Appareil et procédé de séchage continu de produits en vrac

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Cited By (4)

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Publication number Priority date Publication date Assignee Title
DE10056459C1 (de) * 2000-11-14 2002-04-04 Fraunhofer Ges Forschung Verfahren zum Aufbereiten faseriger Substanzen
DE10157596C1 (de) * 2001-11-23 2003-03-20 Fraunhofer Ges Forschung Verfahren zum Aufbereiten faseriger Substanzen
EP1314943A1 (fr) 2001-11-23 2003-05-28 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Procédé pour traiter des substances fibreuses
DE10221367B4 (de) * 2002-05-13 2006-05-11 Bankwitz, Robert, Dr. Pneumatischer Schleudertrockner

Also Published As

Publication number Publication date
US5697167A (en) 1997-12-16
DE59501167D1 (de) 1998-02-05
ATE161622T1 (de) 1998-01-15
EP0714006A1 (fr) 1996-05-29
CA2163305A1 (fr) 1996-05-25

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