EP2202474B1 - Installation de séchage de produit de concassage du bois - Google Patents

Installation de séchage de produit de concassage du bois Download PDF

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Publication number
EP2202474B1
EP2202474B1 EP08022360A EP08022360A EP2202474B1 EP 2202474 B1 EP2202474 B1 EP 2202474B1 EP 08022360 A EP08022360 A EP 08022360A EP 08022360 A EP08022360 A EP 08022360A EP 2202474 B1 EP2202474 B1 EP 2202474B1
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Prior art keywords
wood
exhaust gas
convection part
radiation
combined radiation
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EP08022360A
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German (de)
English (en)
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EP2202474A1 (fr
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Kronotec AG
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Kronotec AG
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Priority to EP08022360A priority Critical patent/EP2202474B1/fr
Priority to ES08022360T priority patent/ES2368960T3/es
Priority to PL08022360T priority patent/PL2202474T3/pl
Priority to AT08022360T priority patent/ATE514909T1/de
Priority to RU2009147837/06A priority patent/RU2529985C2/ru
Priority to UAA200913367A priority patent/UA104278C2/ru
Publication of EP2202474A1 publication Critical patent/EP2202474A1/fr
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Publication of EP2202474B1 publication Critical patent/EP2202474B1/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
    • F26B23/028—Heating arrangements using combustion heating using solid fuel; burning the dried product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/10—Heating arrangements using tubes or passages containing heated fluids, e.g. acting as radiative elements; Closed-loop systems
    • 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 invention relates to a wood shredder drying plant according to the preamble of claim 1 and a method for drying wood shredded products.
  • Wood shredder drying equipment is used to dry wood shredded products prior to further processing.
  • material is burned in the combustion vessel, which is obtained in the production of wood-based panels as waste, such as bark, wood fibers or residual waste.
  • the flue gas temperature is further increased via the additional firing, which is, for example, a gas firing.
  • thermal oil can be used as an energy source in production processes, for example when pressing wood-based panels.
  • a disadvantage of the drying system described is that ash components of the flue gas can be deposited in the heat exchangers, which requires a high maintenance.
  • a method of firing a boiler designed for oil or gas firing with a dusty fuel is known.
  • the document refers to the prior art, in which rising flame gases have a low speed of 6 to 10 m / s, which is considered a disadvantage.
  • a disadvantage of this embodiment is that ash particles can settle in the furnace, which leads to an increased standstill risk of the system.
  • a tobacco dryer which has a water evaporator.
  • the gentle drying of the tobacco is in the foreground, but not as in wood crushing product drying equipment efficiency.
  • a device for producing superheated steam is known in which downstream of a heat exchanger, an ash separator is provided in the form of a cyclone separator.
  • a disadvantage of known wood shredder drying systems is that ash constituents of the flue gas can be deposited in the heat exchangers. This results in a high maintenance, the downtime of the plant after pulls that reduce the effectiveness of the plant. In the worst case, the deposits are so strong that an accident can occur as a result of which thermal oil can escape and ignite. This can even lead to the destruction of the solid fuel firing.
  • the invention has for its object to provide a wood shredder-drying plant, with a continuous operation in combustion, inter alia, wood fibers with high moisture content with reduced maintenance is safe and high efficiency possible.
  • the invention solves the problem by a Holzzerkleinticiansprodükt-drying plant according to claim 1.
  • the invention solves the problem by a method according to claim 10.
  • An advantage of the invention is that existing equipment can be easily retrofitted. Existing wood shredder drying systems often have a combustion boiler that is poorly modifiable. By the downstream, combined radiation and convection part of the old combustion boiler can continue to be used and it also achieves a high level of operational safety. It is also advantageous that the combined radiation and convection part makes it possible to lower the flow velocity of the flue gas so far that a large proportion of the ash constituents fails. The combined radiation and convection part thus also acts as an ash separator, so that virtually no further formation of deposits can occur in a possibly downstream pure convection part. As a result, the reliability of the system is significantly increased.
  • a combustion vessel is understood to mean, in particular, any technical device which is set up for burning wood and / or wood-based materials, as well as wood chips, wood chips, barks and / or residual waste.
  • the apparatus for burning wood and / or wood materials may be for example a traveling grate, which is also referred to as a feed grate.
  • the combustion boiler is a fluidized bed boiler in which the wood waste is burned in a fluidized bed.
  • the additional firing may be, for example, a gas firing.
  • a combined radiation and convection part is understood in particular to mean a component of the drying plant in which the heat transfer between the smoke and the radiation and convection part is neither dominantly due to heat radiation nor dominant to heat conduction.
  • Pure radiation parts and pure convection parts are optimized for their respective task. For example, in radiation parts trying to avoid turbulence of the flue gas in order not to slow down the flue gas unnecessarily.
  • the radiation part is essentially advantageous only in the case of very hot flue gases, since the power transmitted by heat radiation increases in the fourth power with the absolute temperature.
  • the most turbulent flow possible is sought, since then the heat transfer coefficient is particularly high. But that leads to losses in the flow velocity.
  • the at least one combined radiation and convection part is designed so that the flue gas initially flows vertically upwards and subsequently vertically downwards.
  • the advantage of this is that the hot flue gas in the section in which it flows vertically upward, can have a high flow velocity, since the heat is released to a large extent via heat radiation to heat exchanger tubes.
  • the flow velocity may be reduced and optionally more turbulent, which may cause ash particles to precipitate.
  • the flue gas is already moving downwards, so that the deposition of the ash particles is promoted.
  • the combined radiation and convection part has a radially inner riser channel and a fall channel radially surrounding the riser channel. This ensures that the flow rate drops sharply when the flue gases pass from the riser channel into the drop channel. If baffles are arranged in the fall channel to swirl the flue gas stream for a better convective heat transfer, the energy losses are therefore lower. Namely, a reduction in the flow velocity means the less energy loss, the lower the overall flow velocity is, because the flow energy depends quadratically on the flow velocity.
  • the combined radiation and convection part is particularly compact if the riser channel and the drop channel have a common wall.
  • the common wall is at least partially formed by heat exchanger tubes. This is achieved, for example, in that the combined radiation and convection part has a pipe-web-pipe structure at this point. But it is also possible that the heat exchanger tubes are mounted on the common wall.
  • the combined radiation and convection part is designed such that a flow velocity of the flue gas, at least in a possibly existing drop channel, is less than 19 m / sec, for example about 18 m / sec. It has been shown that such a particularly efficient ash separation with simultaneous high heat transfer between the flue gas and the thermal oil is possible.
  • the flow rate of the flue gas before entering the combined radiation and convection part is greater than 22 m / sec and is for example 24 m / sec. If the combined radiation and convection part has a riser channel, the flow velocity there may also be above 22 m / sec. The advantage of this is that heat losses between the combustion boiler and the combined radiation and convection are avoided and an ash separation is suppressed before the fall channel by the high flow rate.
  • a pure radiation part is arranged between the combustion boiler and the combined radiation and convection part.
  • the flue gas flows in the radiation part from top to bottom.
  • particularly hot thermal oil can be generated
  • the heat content of the flue gas is utilized particularly efficiently.
  • the combined radiation and convection part acts as ash separator and has an automatic ash removal. This is to be understood that in particular more than 85% of the ash leaving the combustion boiler is deposited in the combined radiation and convection part.
  • the wood shred product drying plant preferably comprises at least two combined radiation and convection parts, which are connected in such a way that their flue gases are brought together before they enter the at least one convection part. In this way, the system can be operated continuously, even if one of the combined radiation and convection parts is serviced.
  • the combustion boiler ie the immediate vicinity of the firing point, to be burned in the wood particles to comprise heat exchanger pipes through which thermal oil flows.
  • the combustion boiler does not have to have such heat exchanger tubes. It is thus possible to clean the combustion boiler particularly easy, since it does not have to be taken into account on sensitive heat exchanger tubes.
  • Known wood crushing product drying plants generally have a mixing chamber in which a portion of the flue gas is removed immediately behind the combustion boiler. This hot gas is passed through multicyclones and sent directly to the dryer to raise the temperature. Disadvantages are the high costs for the mixing chamber, which according to a preferred embodiment of the invention are avoided in that the wood shredder drying plant comprises a controllable branching device which is arranged to remove flue gas from the combined radiation and convection section.
  • This branching device is easy to implement and therefore inexpensive.
  • the branching device is designed to direct the flue gas in a path to the dryer, in which no cooling heat exchanger is arranged.
  • a flue gas cleaning device is arranged, for example a multi-cyclone.
  • the branching device is arranged so that it takes the flue gas in the flow direction behind the riser channel and in particular before the drop channel.
  • the branching device is arranged to remove the flue gas behind the combined radiation and convection part.
  • a method according to the invention it is preferably provided that air is added to the flue gas behind the combined radiation and convection part and that the resulting dry gas mixture is subsequently passed into the dryer. But it is not necessary that the air is mixed directly behind the combined radiation and convection part. If a pure convection section is still connected downstream, air is preferably mixed in behind it. This makes it possible to control the total amount of dry gas required, simply and independently of the combustion vessel.
  • the flue gas temperature of the flue gas when entering the combined radiation and convection part is above 850 ° C.
  • the exhaust gas temperature is below about 600 ° C in particular. In this way it is achieved that a particularly large amount of energy is taken from the flue gas.
  • the flue gases remain for a certain time in the combined radiation and convection part, whereby the ash deposition is promoted.
  • FIG. 1 shows a Holzzerkleineruhgs slaughter-drying plant 10 according to the invention, which is hereinafter referred to briefly as a drying plant.
  • the drying plant 10 comprises a combustion boiler 12 with a device for burning wood waste in the form of a traveling grate 14, a supplementary firing 16, which is operated with gas, and a supply line 18 to a only in FIG. 4 marked dryer for wood shredded products.
  • the drying plant 10 is for example part of a production plant for wood-based panels.
  • the combustion boiler 12 is designed for a thermal output of 42 megawatts and a combustion temperature of more than 850 ° C, in the present case 950 ° C.
  • Emerging flue gas 20 is, as indicated by the arrow P1, passed through a flue gas duct 22 in a combined radiation and convection 24.
  • the flue gas 20 enters the bottom of the radiation and convection part 24 and flows in a radially inner riser channel 26 upwards.
  • the riser 26 is bounded by heat exchanger tubes 28 radially outward.
  • a header 30 changes the flue gas 20 its flow direction and flows in a fall channel 32 vertically downward, as indicated by the arrows P2.
  • the drop channel 32 surrounds the riser channel 26 radially.
  • the riser 26 has a riser channel cross-sectional area A 26 which is smaller than a drop channel cross-sectional area A 32 . This reduces a flow velocity v 26 in the riser channel 26, which is about 24 m / sec, to a flow velocity v 32 of about 18 m / sec. Due to the different flow velocities v 26 and v 32 prevails in the riser 26, the heat transfer by heat radiation, in the case channel 32, however, outweighs the heat transfer by convection.
  • the flow velocity v of the flue gas is always greater than 22 m / sec, which ensures that the ash particles 34 hardly deposit on the insides of the flue gas duct 22.
  • the flow velocity v 32 is so low that the ash particles settle to the bottom, as indicated by the ash particles 34.4 and 34.5, where they are drawn off via an automatic ash removal not shown.
  • the now ash-poor flue gas 20 passes through a second supply line 36 in downstream pure convection parts 38.1, 38.2, in which further heat exchanger tubes 40 are provided and the flue gas 20 to cool further.
  • the flue gas 20 leaves the convection part through a discharge line 42, as the arrows P3 show.
  • FIG. 2 shows a section through the drying plant 10 according to FIG. 1 in the plane BB.
  • FIG. 1 a section along the line AA according to FIG. 2 , It can be seen that the flue gas 20, as indicated by the arrows P1, in Brennkessel 12 flows upwards.
  • FIG. 2 can also be seen that the flue gas 20 initially enters a pure radiation part 44 and flows there from top to bottom.
  • the radiation part 44 is likewise lined with heat exchanger tubes, in which, as with all other heat exchangers, a thermal oil flows and absorbs heat of the flue gas.
  • the flue gas flows out of the radiation part 44 into a first radiation and convection part 24 FIG. 1 is shown, and a second radiation and convection 24.2. Subsequently, the flue gas flows through four pure convection parts 38.1, 38.2, 38.3 and 38.4. In this case, it can be provided that the two pure convection parts 38.1, 38.2 are exposed to flue gas from the radiation and convection part 24.1, whereas the convection parts 38.3 and 38.4 are exposed to flue gas from the radiation and convection part 24.2.
  • the reference numeral 38 designates the convection parts as such.
  • FIG. 3 shows the drying plant 10 with the combustion boiler 12, the supply line 18 and the radiation and convection part 24.1, which has an ash discharge 46. There is provided a branching device 47, which is arranged so that the flue gas 20 can get into a branch line 50. The closer function will be described below.
  • FIG. 4 shows a view from above of a detail of the drying plant 10 according to FIG. 3 with the radiation part 44, the combined radiation and convection parts 24.1. and 24. 2 and the convection parts 38. Also visible are the riser channel 26.1 of the radiation and convection part 24.1 and the riser channel 26.2 of the radiation and convection part 24.2. These components form a flue gas cooling 48 of the drying plant.
  • the branching device 47 comprises a first flap 52.1 and a second flap 52.2.
  • the first flap 52.1 is connected to the radiation and convection part 24.1 such that the flue gas 20 is partially withdrawn from the riser channel 26.1 before it enters the fall channel 32.1.
  • the second flap 52.2 is correspondingly connected to the radiation and convection part 24.2.
  • the flaps 52 are designed so that the amount of extracted flue gas is adjustable.
  • the flue gas 20 is passed by means of the branch line 50 directly to a not shown mixing device, where it is mixed with flue gas, which has previously flowed through at least one of the convection parts 38. Based on the mixing ratio, a temperature of the mixed gas is controlled, which then enters the dryer 49.

Claims (10)

  1. Installation de séchage de produit de fragmentation du bois, en particulier pour des éclats de bois, des copeaux de bois, ou des fibres de bois, comprenant
    (a) une chaudière de combustion (12) qui comprend
    (i) un dispositif (14) pour la combustion de déchets de bois, et
    (ii) un foyer additionnel (16),
    (b) une conduite de gaz de fumée (22) pour diriger les gaz de fumée (20) provenant de la combustion, et
    (c) un sécheur (49) pour les produits de fragmentation du bois qui est alimenté par la conduite de gaz de fumée (22),
    (d) un élément de convection et de rayonnement combiné (24) traversé par de l'huile thermique étant agencé entre la chaudière de combustion (12) et le sécheur (49), pour réchauffer l'huile thermique,
    (e) l'élément de convection et de rayonnement combiné (24) présentant :
    - un canal ascendant (26) radialement interne, et
    - un canal descendant (32) entourant radialement le canal ascendant (26),
    caractérisée en ce que
    (f) entre la chaudière de combustion (12) et l'élément de convection et de rayonnement combiné (24) est agencé un élément de rayonnement (44) dans lequel le gaz de fumée circule de haut en bas, et
    (g) l'élément de convection et de rayonnement combiné est formé de façon qu'une vitesse d'écoulement du gaz de fumée avant entrée dans l'élément de convection et de rayonnement combiné (24) soit supérieure à 22 m/s,
    (h) l'élément de convection et de rayonnement combiné est formé de façon qu'une vitesse d'écoulement du gaz de fumée dans le canal descendant soit inférieure à 19 m/sec, de sorte qu'une séparation efficace des cendres soit possible, et
    (i) l'élément de convection et de rayonnement combiné (24) agissant comme un séparateur de cendres et présentant une extraction automatique de cendres et
    (ii) l'au moins un élément de convection et de rayonnement combiné (24) étant formé de façon que le gaz de fumée (20) s'écoule tout d'abord verticalement vers le haut puis verticalement vers le bas.
  2. Installation de séchage de produit de fragmentation du bois selon la revendication 1, caractérisée en ce que le canal ascendant (26) et le canal descendant (32) possèdent une paroi commune.
  3. Installation de séchage de produit de fragmentation du bois selon la revendication 2, caractérisée en ce que la paroi commune est formée au moins partiellement par des tubes d'échange thermique (28, 40).
  4. Installation de séchage de produit de fragmentation du bois selon l'une quelconque des revendications précédentes, caractérisée en ce qu'un élément de convection (38) est agencé derrière l'élément de convection et de rayonnement combiné (24).
  5. Installation de séchage de produit de fragmentation du bois selon la revendication 4, caractérisée par au moins deux éléments de convection et de rayonnement combiné (24) qui sont reliés de façon que leurs gaz de fumée (20) soient réunis avant l'entrée dans l'au moins un élément de convection (38).
  6. Installation de séchage de produit de fragmentation du bois selon l'une quelconque des revendications 1 à 5, caractérisée par un dispositif de bifurcation (47) pilotable qui est agencé pour prélever une partie du gaz de fumée (20) hors de l'élément de convection et de rayonnement combiné (24).
  7. Installation de séchage de produit de fragmentation du bois selon la revendication 6, caractérisée en ce que le dispositif de bifurcation (47) est formé pour diriger le gaz de fumée (20) sur un chemin jusqu'au sécheur (49), aucun échangeur thermique n'étant agencé dans le chemin.
  8. Installation de séchage de produit de fragmentation du bois selon la revendication 6 ou 7, caractérisée en ce que le dispositif de bifurcation est agencé pour prélever du gaz de fumée dans la direction de circulation derrière le canal ascendant (26) et en particulier devant le canal descendant (32).
  9. Installation de séchage de produit de fragmentation du bois selon l'une quelconque des revendications 6 à 8, caractérisée par une régulation qui est établie pour réguler une température dans le sécheur (49) au moins aussi au moyen d'un courant de gaz de fumée (20) à travers le dispositif de bifurcation (47).
  10. Procédé de séchage de produits de fragmentation du bois, en particulier d'éclats de bois, de copeaux de bois, ou de fibres de bois, comprenant les étapes suivantes :
    (a) brûler des déchets de bois, le cas échéant avec un foyer additionnel (16), dans une chaudière de combustion (12), de sorte qu'il y ait du gaz de fumée (20),
    (b) conduire le gaz de fumée
    (i) dans un élément de rayonnement (44) agencé entre la chaudière de combustion (12) et l'élément de convection et de rayonnement combiné (24), et dans lequel le gaz de fumée est dirigé de haut en bas, et
    (ii) dans un élément de convection et de rayonnement combiné (24) qui présente
    - un canal ascendant (26) radialement interne, et
    - un canal descendant (32) entourant radialement le canal ascendant (26),
    d'abord vers le haut, puis vers le bas, et dans lequel le gaz de fumée (20) se refroidit et une huile thermique est réchauffée, et
    (iii) finalement à travers un élément de convection, de façon que le gaz de fumée (20) continue à refroidir et l'huile thermique à être réchauffée, et
    (c) la vitesse d'écoulement (v) du gaz de fumée avant entrée dans l'élément de convection et de rayonnement combiné (24) étant supérieure à 22 m/s,
    (d) la vitesse d'écoulement (v) du gaz de fumée dans le canal descendant étant inférieure à 19 m/sec, de sorte qu'une séparation des cendres s'effectue,
    (e) l'élément de convection et de rayonnement combiné (24) agissant comme un séparateur de cendres et présentant une extraction automatique de cendres et
    (f) puis conduire le gaz de fumée (20) dans un sécheur (49) pour les produits de fragmentation du bois.
EP08022360A 2008-12-23 2008-12-23 Installation de séchage de produit de concassage du bois Active EP2202474B1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
EP08022360A EP2202474B1 (fr) 2008-12-23 2008-12-23 Installation de séchage de produit de concassage du bois
ES08022360T ES2368960T3 (es) 2008-12-23 2008-12-23 Instalación de secado de productos de la trituración de la madera.
PL08022360T PL2202474T3 (pl) 2008-12-23 2008-12-23 Urządzenie do suszenia produktu z rozdrabniania drewna
AT08022360T ATE514909T1 (de) 2008-12-23 2008-12-23 Holzzerkleinerungsprodukt-trocknungsanlage
RU2009147837/06A RU2529985C2 (ru) 2008-12-23 2009-12-22 Сушильная установка для продуктов измельчения древесины
UAA200913367A UA104278C2 (ru) 2008-12-23 2009-12-22 Сушильная установка для продуктов измельчения дерева

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP08022360A EP2202474B1 (fr) 2008-12-23 2008-12-23 Installation de séchage de produit de concassage du bois

Publications (2)

Publication Number Publication Date
EP2202474A1 EP2202474A1 (fr) 2010-06-30
EP2202474B1 true EP2202474B1 (fr) 2011-06-29

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EP (1) EP2202474B1 (fr)
AT (1) ATE514909T1 (fr)
ES (1) ES2368960T3 (fr)
PL (1) PL2202474T3 (fr)
RU (1) RU2529985C2 (fr)
UA (1) UA104278C2 (fr)

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CN107166946B (zh) * 2017-07-09 2019-06-07 杭州浙贵机械设备有限公司 一种羽绒干燥系统的加热方法
CN107816801A (zh) * 2017-11-20 2018-03-20 江苏太湖锅炉股份有限公司 π型燃油气有机热载体炉

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Publication number Priority date Publication date Assignee Title
CA2441692A1 (fr) * 2003-09-19 2005-03-19 Hipp Engineering Ltd. Methode et dispositif de production de vapeur surchauffee
WO2007077293A1 (fr) * 2005-12-30 2007-07-12 Wärtsilä Biopower Oy Procede de chauffage et / ou d'evaporation d'un milieu organique et unite d'echangeur de chaleur destinee a recuperer de la chaleur a partir d'un ecoulement de gaz chaud

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EP2202474A1 (fr) 2010-06-30
PL2202474T3 (pl) 2012-01-31
ATE514909T1 (de) 2011-07-15
RU2529985C2 (ru) 2014-10-10
RU2009147837A (ru) 2011-06-27
ES2368960T3 (es) 2011-11-24

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