EP2202474A1 - 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
EP2202474A1
EP2202474A1 EP08022360A EP08022360A EP2202474A1 EP 2202474 A1 EP2202474 A1 EP 2202474A1 EP 08022360 A EP08022360 A EP 08022360A EP 08022360 A EP08022360 A EP 08022360A EP 2202474 A1 EP2202474 A1 EP 2202474A1
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EP
European Patent Office
Prior art keywords
wood
flue gas
convection
drying plant
radiation
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP08022360A
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German (de)
English (en)
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EP2202474B1 (fr
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.)
Kronotec AG
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Kronotec AG
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 Kronotec AG filed Critical Kronotec AG
Priority to AT08022360T priority Critical patent/ATE514909T1/de
Priority to PL08022360T priority patent/PL2202474T3/pl
Priority to ES08022360T priority patent/ES2368960T3/es
Priority to EP08022360A priority patent/EP2202474B1/fr
Priority to UAA200913367A priority patent/UA104278C2/ru
Priority to RU2009147837/06A priority patent/RU2529985C2/ru
Publication of EP2202474A1 publication Critical patent/EP2202474A1/fr
Application granted granted Critical
Publication of EP2202474B1 publication Critical patent/EP2202474B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • 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 crushing product drying plant, in particular for wood chips, wood chips or wood fibers, with a combustion boiler comprising a furnace for burning Holz- andloder wood materials and an additional firing, a flue gas line for conducting the resulting during combustion flue gases and a dryer for the wood crushing products , which is fed by the flue gas line.
  • a combustion boiler comprising a furnace for burning Holz- andloder wood materials and an additional firing
  • a flue gas line for conducting the resulting during combustion flue gases
  • a dryer for the wood crushing products which is fed by the flue gas line.
  • the invention relates to a method for drying wood chipping products, in particular wood chips, wood shavings and / or wood fibers.
  • 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 known Holzzerklein mecanics 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 crushing product drying plant, with a continuous operation in combustion, among other things of wood fibers with high moisture content with reduced maintenance is certainly possible.
  • the invention solves the problem by a generic wood crushing product drying plant, in which a combined radiating and convection part, through which thermal oil flows, for heating the thermal oil is arranged between the combustion boiler and the dryer.
  • the invention solves the problem by a method for drying wood chipping products, comprising the steps of (a) burning wood and / or wood materials, optionally with additional firing, in a combustion vessel to produce flue gas, (b) passing the Flue gas in a combined radiation and convection section first upwards and then downwards, whereby the flue gas cools and a thermal oil is heated, and then from top to bottom through a convection part, so that the flue gas is further cooled and heated thermal oil, and ( c) then passing the flue gas into a dryer for the wood chipping products.
  • 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.
  • 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 acts at least partially as an ash separator, so that in a possibly downstream pure convection part as good as no longer can lead to the formation of deposits, thereby 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 combined radiation and convection part is thus neither a pure radiation part nor a pure convection part.
  • the at least one combined radiation and convection part is designed such 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 drop duct radially surrounding the riser duct. 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 so that a flow velocity of the flue gas is at least in a possibly existing drop channel below 19 m / sec, for example at 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 entry into 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 and / or a pure convection part are arranged behind the combined radiation and convection part between the combustion boiler and the combined radiation and convection part.
  • the heat content of the flue gas is utilized particularly efficiently.
  • the combined radiation and convection acts as an 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 wood crushing product drying plant 10 according to the invention, which is referred to below 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 inner sides 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, whereupon 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, can also be seen the riser 26.1 of the radiation and Konvezzysteils 24.1 and the riser 26.2 of the radiation and Konvezzysteils 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.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Drying Of Solid Materials (AREA)
  • Chemical And Physical Treatments For Wood And The Like (AREA)
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
AT08022360T ATE514909T1 (de) 2008-12-23 2008-12-23 Holzzerkleinerungsprodukt-trocknungsanlage
PL08022360T PL2202474T3 (pl) 2008-12-23 2008-12-23 Urządzenie do suszenia produktu z rozdrabniania drewna
ES08022360T ES2368960T3 (es) 2008-12-23 2008-12-23 Instalación de secado de productos de la trituración de la madera.
EP08022360A EP2202474B1 (fr) 2008-12-23 2008-12-23 Installation de séchage de produit de concassage du bois
UAA200913367A UA104278C2 (ru) 2008-12-23 2009-12-22 Сушильная установка для продуктов измельчения дерева
RU2009147837/06A RU2529985C2 (ru) 2008-12-23 2009-12-22 Сушильная установка для продуктов измельчения древесины

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

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Family Applications (1)

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

Country Status (6)

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

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Citations (11)

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Publication number Priority date Publication date Assignee Title
DE2534092A1 (de) 1975-07-30 1977-02-17 Konus Kessel Waermetech Liegender kessel fuer feste brennstoffe
DE2534093A1 (de) 1975-07-30 1977-04-21 Konus Kessel Waermetech Einrichtung zum erwaermen einer gegen ueberhitzung zu schuetzenden waermeuebertragungsfluessigkeit
DE2845630A1 (de) 1978-10-19 1980-04-30 Konus Kessel Waermetech Mehrzuegiger rohrschlangenkessel
DE3534260A1 (de) * 1985-09-26 1987-04-02 Plonka Dohren Marianne Verfahren zum thermischen trocknen temperaturempfindlicher gueter in drehtrommeln sowie vorrichtungen zur durchfuehrung dieses verfahrens
DE4442859A1 (de) * 1994-12-02 1996-06-05 Manfred Klemm Thermisch, energetisch optimiertes Verfahren zur Kraft-Wärme-Kopplung für gewerbliche Trocknungsanlagen
WO2002039018A1 (fr) 2000-11-09 2002-05-16 Fritz Schoppe Procede de mise a feu d'une chaudiere conçue pour le chauffage au mazout ou au gaz avec un combustible pulverulent
EP1249181A2 (fr) 2001-04-10 2002-10-16 British American Tobacco (Germany) GmbH Préparation d'un gaz de traitement pour un sèchoir de tabac
CA2441692A1 (fr) 2003-09-19 2005-03-19 Hipp Engineering Ltd. Methode et dispositif de production de vapeur surchauffee
DE202007005195U1 (de) 2006-10-24 2007-07-05 Fritz Egger Gmbh & Co. Heißgasbetriebene Trocknungsvorrichtung
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
US20070214676A1 (en) * 2006-03-17 2007-09-20 Efb, Inc. Apparatus and method using an electrified filter bed for removal of pollutants from a flue gas stream

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SU1460362A1 (ru) * 1987-07-06 1989-02-23 М.А.Девочкин Парогазова установка на твердом топливе
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DE4017806A1 (de) * 1990-06-01 1991-12-05 Koerting Ag Verfahren und anlage zur kontinuierlichen trocknung von holzspaenen, holzfasern oder anderen schuettguetern
RU2170897C1 (ru) * 2000-01-06 2001-07-20 Акционерное общество открытого типа "Радиатор" Жидкостно-масляный теплообменник
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Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2534092A1 (de) 1975-07-30 1977-02-17 Konus Kessel Waermetech Liegender kessel fuer feste brennstoffe
DE2534093A1 (de) 1975-07-30 1977-04-21 Konus Kessel Waermetech Einrichtung zum erwaermen einer gegen ueberhitzung zu schuetzenden waermeuebertragungsfluessigkeit
DE2845630A1 (de) 1978-10-19 1980-04-30 Konus Kessel Waermetech Mehrzuegiger rohrschlangenkessel
DE3534260A1 (de) * 1985-09-26 1987-04-02 Plonka Dohren Marianne Verfahren zum thermischen trocknen temperaturempfindlicher gueter in drehtrommeln sowie vorrichtungen zur durchfuehrung dieses verfahrens
DE4442859A1 (de) * 1994-12-02 1996-06-05 Manfred Klemm Thermisch, energetisch optimiertes Verfahren zur Kraft-Wärme-Kopplung für gewerbliche Trocknungsanlagen
WO2002039018A1 (fr) 2000-11-09 2002-05-16 Fritz Schoppe Procede de mise a feu d'une chaudiere conçue pour le chauffage au mazout ou au gaz avec un combustible pulverulent
EP1249181A2 (fr) 2001-04-10 2002-10-16 British American Tobacco (Germany) GmbH Préparation d'un gaz de traitement pour un sèchoir de tabac
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
US20070214676A1 (en) * 2006-03-17 2007-09-20 Efb, Inc. Apparatus and method using an electrified filter bed for removal of pollutants from a flue gas stream
DE202007005195U1 (de) 2006-10-24 2007-07-05 Fritz Egger Gmbh & Co. Heißgasbetriebene Trocknungsvorrichtung

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Also Published As

Publication number Publication date
EP2202474B1 (fr) 2011-06-29
UA104278C2 (ru) 2014-01-27
ATE514909T1 (de) 2011-07-15
RU2009147837A (ru) 2011-06-27
ES2368960T3 (es) 2011-11-24
PL2202474T3 (pl) 2012-01-31
RU2529985C2 (ru) 2014-10-10

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