EP1363097A1 - Séchoir centrifuge pneumatique - Google Patents

Séchoir centrifuge pneumatique Download PDF

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Publication number
EP1363097A1
EP1363097A1 EP03010678A EP03010678A EP1363097A1 EP 1363097 A1 EP1363097 A1 EP 1363097A1 EP 03010678 A EP03010678 A EP 03010678A EP 03010678 A EP03010678 A EP 03010678A EP 1363097 A1 EP1363097 A1 EP 1363097A1
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EP
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Prior art keywords
dryer
vapor
transport
loop reactor
furnace
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EP03010678A
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German (de)
English (en)
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EP1363097B1 (fr
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Robert Dr. Bankwitz
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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
    • F26B17/24—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by shooting or throwing the materials, e.g. after which the materials are subject to impact

Definitions

  • the invention relates to a method and a device for drying pneumatically conveyable Goods, especially of wood fiber and similar vegetable substances, in one indirect heated spin dryer.
  • Wood fibers are dried industrially in a very energy-intensive way in electric dryers.
  • tube bundle rotary dryers were considered to be the dryers with the least amount of pollutants when drying wood pulp. This is because these dryers are gently indirect be heated with steam (or heat transfer oil). However, the one for it is of great disadvantage Steam boilers required, unless steam is available anyway. In normal tube bundles however, wood fibers get caught. A special, complex one is suitable for this Heating register dryer from VETTER MASCHINENBAU GMBH KASSEL.
  • EP 0 457 203 B1 (KUNZ, priority 18.05.90) claims a drum dryer with a closed Steam-air cycle, especially for drying substances with strong Odor nuisance is suitable, the vapors being condensed and the non-condensable Vapors are burned. The use of condensation heat is also used for this dryer the brothers claimed. In the patent, the heating is not condensable vapor components described by means of a flue gas cooler before they enter the combustion chamber.
  • EP 0 459 603 B1 (K ⁇ RTING, priority 01.06.90) claims methods and system for Drying wood shavings, wood fibers or similar bulk materials in a vapor cycle, at the smoke-free vapors leaving a drum dryer in a heat exchanger from the hot fuel gases are indirectly heated and fed back to the dryer, whereby a Branch stream branched off from this circuit and for thermal decomposition of the pollutants Combustion chamber is guided. There is no vapor condensation. Describes the same procedure with later priority the application EP 0 508 546 A1 (VAN DEN BROEK).
  • EP 0 714 006 B1 (KUNZ, PRIORITY 24.11.94) claims an improvement of the method EP 0 459 063 B1 by heating the partial vapor stream which is incinerated that is, the flue gas leaving the combustion chamber directly, so that the following counterflow heat exchanger for decoupling the dryer heat at the hottest point not thermally is more heavily burdened. The residual heat of the flue gases is then used to heat the Combustion air and possibly used for predrying.
  • EP 0 851 194 A3 (KNABE, Priority DE 196 54 043 C2) claims that the hot flue gas of a combustion chamber first Heat is removed by a steam generator before the in a second heat exchanger Vapor circuit is heated. The excess of vapor is burned.
  • a steam generator Preferably used as a dryer obviously uses a shell and tube rotary drum dryer with a rotating drum, a current dryer can be connected upstream. This arrangement is said to be lower Exhaust gas temperatures can be reached than with the dryers from W. KUNZ DRYTEC AG. From the The illustration does not show whether this arrangement has economic advantages over the classic one Has tube bundle rotary dryer with only one heat transfer circuit.
  • fibrous materials with low Bulk density and high internal friction e.g. Basically, wood fibers are not in one Dryer according to EP 0 714 006 B1 or DE 196 54 043 C2 can be dried.
  • the GERMAN BUNDESSTIFTUNG UMWELT developed the hot steam fiber dryer in 1999/2000 funded by SCHENKMANN & PIEL, LEVERKUSEN. This is a 100 m long current dryer operated with 0.5 to 1.5 bar overpressure with only a small amount Overheating of the vapors circulated ( ⁇ 180 ° C) to avoid gaseous emissions. For 1 kg of water evaporation, about 50 kg (!) Vapors have to be circulated in this dryer become.
  • DE 196 06 472 C1 (B ⁇ HLER) describes, like a continuous dryer, the target residual moisture right from the start can be achieved quickly by a complex regulation.
  • DE 196 09 530 A1 (B ⁇ HLER) describes a two-stage drying of biomass, with the hot biomass of the first stage in a downstream power dryer by controlled evaporative cooling with conditioned Supply air is set to the exact processing humidity.
  • EP 1 128 145 A2 (LEB FIRE TECHNOLOGY) describes the control of a power dryer by recording the climate data within the dryer with pressure, temperature and humidity sensors, the signals from a controller are evaluated, which regulates the temperature of the hot gas flow.
  • a problem with multi-stage drying e.g. the widespread combination electric dryer for pre-drying and drum dryer for main drying is the amount of the total Plant led vapor steam, its separation after predrying DE 44 27 709 A1 (KNABE) describes.
  • centrifugal wave dryers When drying mechanically insensitive goods, or if in a process anyway with comminution, centrifugal wave dryers are very Heat transfers reached. Due to the very good separation of the dry goods, almost the entire specific outer surface of the dry material with high turbulence available for mass and heat exchange.
  • This pneumatic heated indirectly with gas Centrifugal tumble dryers combine an axially standing centrifugal shaft in one container with a classifying current dryer. Here granules are defined from a suspension Grain produced. For drying wood fibers and similar vegetable substances this pneumatic tumble dryer with gas operation seems to be less suitable.
  • the object of the present invention is a method and a device for indirect Drying of pneumatically conveyable goods, in particular for wood fibers and similar vegetable Fabrics with very good separation of the dry goods and use of the wall of the drying room as a heat exchanger.
  • FIG 1 the essential elements of the invention are shown:
  • the suction 3 The suction tube 4 and the downpipe 5 of the existing loop reactor are in an oven 6.
  • the material 1 gets wet abandoned and the spin dryer leaves vapor and dried goods 2.
  • the pneumatic centrifugal dryer according to the invention combines the very good heat transfer the centrifugal dryer with the very simple control behavior of the loop reactor, which corresponds approximately to that of the ideal stirred tank.
  • a current dryer it is special for drying goods that are difficult to handle, such as wood fiber and similar vegetable Suitable for fabrics.
  • indirectly heated electricity dryers there is no need to enter the heat of vaporization via a vapor circuit with various devices and the extreme required for low overheating of the vapors high gas circulation or the high vapor superheating required for lower circulation Product decomposition.
  • the centrifugal dryer is located directly in an oven. The Burned-out flue gas is suddenly brought up to furnace temperature of e.g.
  • the dry material-vapor mixture is circulated in the loop reactor with a transport impeller, as is known from the suction of pneumatic chip conveyance. That is a very robust open radial fan with closed back, on which nothing gets stuck. At the Passage through the transport impeller and when skidding against the reactor wall becomes that Dried goods very well isolated, as in every spin dryer.
  • the in the downpipe due to centrifugal force Dry material particles rubbing the reactor wall create a thin PRANDTL boundary layer and thus an excellent heat transfer from the wall to the circulating vapors.
  • the centrifugal dryer according to the invention can also be operated at the bottom by means of suction be operated, the transport impeller can also be a floor agitator. In this case there is an external circulation of the dry material / vapor mixture.
  • This version at that the entire machine technology is at ground level can be very advantageous for smaller dryers his.
  • the heat transported from the dryer wall to the dry goods without much overheating of the vapors.
  • the thermal inertia of the dryer wall can be very high if the loading of dry goods is disrupted Emergency cooling with injected water quickly reaching the entire drying room. This can make the special fire risk of drying vegetable substances practical be excluded. If there is a fire, it will simply suffocated by pushing off all openings. Should inadmissible excess pressure build up are removed via pressure relief flaps.
  • the pneumatic centrifugal dryer can be very well adjusted to the inside temperature of the Regulate loop reactor.
  • the residual moisture correlates very well with a given product Temperature.
  • the dryer is preheated to the operating temperature and then Slowly wet dry material is added in such an amount that the internal temperature is constant in the The target value range remains.
  • the feed is continuously increased until the furnace wall is fully heated and the full firing capacity is available for drying.
  • the furnace is used to shut down set and continue to dry with decreasing loading until it is safely switched off can be.
  • the dryer can also quickly evaporate through injected water be emptied and cooled.
  • the pneumatic centrifugal dryer can use an exhaust gas Gas turbine are heated or with steam from a steam engine, a back pressure turbine or an extraction condensation turbine.
  • the downpipes can also be used as double jacket pipes for steam heating be carried out.
  • the pneumatic Spin dryer can be used as a condenser of an ORC power plant.
  • the centrifugal dryer according to the invention is particularly suitable for decentralized processing renewable raw materials.
  • the systems preferably have a firing capacity from 0.3 to 3 MW.
  • a high level of profitability is achieved by burning biomass reached.
  • the company LEHMANN MASCHINENBAU GMBH JOCKETA from wet wood chips from whole construction the fine fraction, which contains a high proportion of bark and needles or leaves, separated by air sifting and burned directly in a front furnace.
  • the wind sifter can be adjusted to the current fuel requirement. In this case there is only one common line for raw material and fuel.
  • the dry material is as in each spin dryer very well isolated, so that usually almost the entire specific Surface of the dry material is available for mass and heat exchange with the vapors stands and very good mass and heat transfers can be achieved due to the high turbulence.
  • To to the kink moisture is the speed-determining step the heat input in the Dryer.
  • the retention time behavior is therefore the simple one Mixing kettle sufficient.
  • two or more dryers can be cascaded in series to be higher only for the diffusion-controlled final drying below the kink point moisture Driving temperatures in the dryer.
  • two or more can be used in the main drying Spin dryer work in parallel and with a common spin dryer for final drying be connected in series.
  • the dry material discharged from the centrifugal dryer can be pneumatic with air be transported away.
  • the sensible warmth of the dry material is then used for subsequent drying used by evaporative cooling.
  • the efficiency is even better if the Transport air is previously heated with waste heat.
  • the used transport air is advantageous as Combustion air used in the dryer furnace.
  • flammable dry matter such as vegetable No further dedusting is then required after the product separator.
  • the water vapor from the after-drying must be at the exhaust gas temperature with the flue gases be heated, but this only requires a fraction of the evaporation heat saved.
  • the pneumatic centrifugal dryer is preferably also fed pneumatically. If transport air is used for this, the water vapor partial pressure in the dryer drops, which is beneficial for drying, but also reduces the dew point temperature of the vapors, which is disadvantageous for the use of waste heat. Vapor vapor should be overheated as a transport gas, to avoid falling below the dew point. Through such vapor overheating with one Exhaust gas cooler improves efficiency.
  • the pneumatic centrifugal dryer can, however e.g. can also be fed with a screw conveyor.
  • Vapor vapor with a high dew point temperature is known to be very good for waste heat recovery suitable. Often, however, there is no heat requirement at the place of occurrence. Renewable intended for drying Raw materials are often wet. In this case it can be advantageous to use the raw materials Steam vapor to save heating in the dryer. The thing that happens when steaming Water is usually very easy to clean biologically. Such a damper causes at the same time dust removal from the vapors.
  • the vapor vapor can e.g. can also be condensed in an air cooler that doesn't condensed portion can be fed directly or indirectly to the furnace and the heated air can can be used for pre- or post-drying.
  • the Green fodder is aerated much better after predrying and the heating energy is here used twice.
  • wood chips are used for the production of fuel pellets in silos with floor ventilation pre-dried by this warm air, crushed in a hammer mill, in pneumatic tumble dryer dried and then pelletized.
  • Example 1 Plant and method for processing wood chips into wood fibers with drying in one embodiment of the dryer according to the invention.
  • the most important dimensions are: Eight downpipes 508 x 8 mm with 12,750 mm drop height.
  • the suction pipe 406.4 x 12 mm, the distributor head made of square hollow profile 150 x 10 mm and hemispherical collecting device 2,600 mm diameter, 1,300 mm height and 10 mm wall thickness.
  • This loop reactor is made of material St 37-2.
  • the furnace wall has an inner diameter of 2,400 mm and an outer diameter of 3,000 mm and is stuffed with mineral insulating wool to about 100 kg / m 3 .
  • the inside of the furnace wall consists of a 1 mm thick sheet metal jacket made of material 1.4713, which is provided with cross beads for reinforcement and length compensation.
  • the combustion chamber for a wood blowing furnace and all thermally highly stressed furnace internals are made of material 1.4762.
  • the total heat exchanger area is approximately 180 m 2 .
  • the maximum evaporation capacity for water is approx. 1,200 to 2,400 kg / h depending on the material and wall temperature.
  • the firing capacity is designed for 0.99 to 2.7 MW, depending on the specific circumstances, whereby basically any fuel is possible.
  • the specific power consumption of the induced draft is 0.01 to 0.06 kWh / kg water evaporation.
  • the loop reactor with furnace wall is the largest single part for assembly and, with dimensions of 3,000 x 3,000 x 16,000 mm, does not pose any problems for road transport.
  • the wet wood chips are discharged from the bunker to the moving floor Air classifier, where the fine fraction is based on the heat demand of the dryer using transport air is discharged and blown into a front furnace.
  • the wood chips separated from the fines reach the Damper, where the coarse-grained heap is well flowed through by vapor.
  • the condensed Vapors and the water drained from the wood chips are subjected to biological purification fed.
  • the vapors dedusted in the damper become, depending on the other heat requirements a condenser recovered waste heat with a flow temperature of 80 ° C.
  • the steamed hot wood chips become a twin-screw extruder from the company LEHMANN MASCHINENBAU GMBH JOCKETA fed to the defibration and get from there with a Screw conveyor in the suction pipe of the dryer.
  • the wood fiber / vapor mixture is at the lowest point of the collecting device sucked in by the intake manifold, being above the collecting device in the intake manifold also the fresh material is fed.
  • a transport wheel like this is known from the chip production, hanging with a vertical axis in the distributor head appropriate.
  • the distributor head corresponds to the housing of a radial fan with the difference that that it has several outlets arranged around an axis of symmetry, here eight.
  • the Transport impeller throws the aspirated wood fiber / vapor mixture through the outlets of the Distribution head with tangential entry into the downpipes, where the wood fibers are thrown against the wall fall down on a spiral path and together with the circulated vapors into the Arrive collection device where they are sucked again.
  • a floor agitator at the bottom of the collecting device ensures that there is no wood pulp and for the fact that wood fibers are constantly transported into the outlet from where they are reach the cyclone separator with the vapors.
  • the blow-in firing is designed as a pre-furnace, so that the fine fraction is wet Wood chips reach the combustion chamber temperature necessary for clean combustion becomes.
  • the actual oven space of the centrifugal dryer stands on the hemispherical collecting device of the loop reactor and envelops the entire remaining part of the loop reactor, except for the drive of the transport wheel.
  • the hot exhaust gases from the furnace are heated to around 400 ° C Air preheater cooled to about 200 ° C chimney temperature.
  • Example 2 Process for the production of fuel pellets from wet sawdust.
  • the pneumatic centrifugal dryer is moved by an adjustable loading belt a rotary valve in a pneumatic bay pass loaded with sawdust.
  • Cyclone separators separate the dried sawdust from the vapors and through a Cell rotary valve fed directly to a pellet press from M ⁇ NCH, RATINGEN.
  • the optimal one The degree of dryness of the sawdust is assessed according to the appearance of the pellets and! the speed the feed belt increased or decreased accordingly. Due to the hot steam short-time drying the otherwise necessary conditioning and the intermediate buffer are omitted.
  • Example 3 Process for energy self-sufficient sewage sludge drying with direct combustion and optional phosphate recovery.
  • the organic dry matter (oTS) of municipal sewage sludge has about that Heating value like dry wood. Sewage sludge mechanically dewatered with filter presses or centrifuges with at least 20% oTS can therefore be burned autothermally. According to the state of the Technology, the sewage sludge is dried and the dry material can be used to heat the Dryer can be burned. As the sewage sludge dries a so-called glue phase passes through, it has to be dried in convection dryers by backmixing with dry goods can be set to over 60% TS. Due to the internal product return is the invention pneumatic centrifugal dryers are ideally suited for this. In the collecting device a kneader is installed, which causes the mixture to have a crumbly consistency.
  • the dust-like dry sewage sludge is roughly separated from the vapor in a cyclone and with preheated air in an eddy current burner from GIV MBH, HALLE very clean burned.
  • the dusty vapors are fed directly to the secondary combustion chamber and thus thermally cleaned.
  • the steam generator is heated with the completely burned-out smoke gases.
  • the steam engine of the generator is operated at 16 bar back pressure and the dryer acts as a capacitor.
  • the ashes of sewage sludge can be removed without heavy metal pollution by mono-combustion can be used directly as a biocide-free phosphate fertilizer, otherwise there is a more extensive one Treatment for phosphate recovery required.
EP03010678A 2002-05-13 2003-05-13 Séchoir centrifuge pneumatique Expired - Lifetime EP1363097B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10221367 2002-05-13
DE10221367A DE10221367B4 (de) 2002-05-13 2002-05-13 Pneumatischer Schleudertrockner

Publications (2)

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EP1363097A1 true EP1363097A1 (fr) 2003-11-19
EP1363097B1 EP1363097B1 (fr) 2010-12-15

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EP (1) EP1363097B1 (fr)
AT (1) ATE491922T1 (fr)
DE (2) DE10221367B4 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105918454A (zh) * 2016-07-07 2016-09-07 河北皓凯农业机械有限公司 气吸循环式粮食干燥机

Citations (23)

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Publication number Priority date Publication date Assignee Title
DE148620C (fr) * 1902-03-27
US1571518A (en) * 1922-12-12 1926-02-02 Vermont Casein Pty Ltd Apparatus for reducing and drying casein curd
US2118078A (en) * 1933-09-07 1938-05-24 Flugel Heinrich Drying method and apparatus
FR998617A (fr) 1949-09-06 1952-01-21 Procédé et dispositif pour la dessication et la vitaminisation de matières par atomisation
DE1629070A1 (de) * 1966-11-30 1971-01-28 Seidner Maschf E Grastrocknungsvorrichtung
DE2006366A1 (en) * 1970-02-12 1971-08-12 Gebr Giulini GmbH, 6700 Ludwigs hafen Drying of sticky temperature sensitive part-icles
GB1322018A (en) * 1970-06-30 1973-07-04 Do Nii Chernoj Metallurgii Method and apparatus for the thermal and or chemical treatment of particulate material
US3861059A (en) * 1972-07-03 1975-01-21 Hazemag Andreas Kg Drying apparatus
DE3919828A1 (de) * 1989-06-16 1990-12-20 Burgert Burdosa Schlaufenreaktor
EP0459603A1 (fr) * 1990-06-01 1991-12-04 Körting Hannover Ag Procédé et dispositif pour le séchage continu de copeaux de bois, de fibres de bois ou d'autres matières en vrac
EP0365851B1 (fr) 1988-09-27 1991-12-11 Bison-Werke Bähre & Greten GmbH & Co. KG Séchoir à tambour à position horizontale pour matériau granulé
EP0508546A1 (fr) 1991-04-08 1992-10-14 VandenBroek International B.V. Dispositif de séchage
EP0536650A1 (fr) 1991-10-11 1993-04-14 Alb. Klein GmbH & Co. KG Procédé et dispositif pour sècher des substances humides
EP0457203B1 (fr) 1990-05-18 1993-09-29 SC Technology AG Procédé de séchage sans émissions d'une substance dans un tambour de séchage
DE4427709A1 (de) 1994-06-08 1996-01-11 Martin Knabe Verfahren und Vorrichtung zur Trocknung von Schüttgütern
EP0714006A1 (fr) 1994-11-24 1996-05-29 W. Kunz AG Procédé de séchage d'une substance, en particulier de copeaux de bois
DE19606472C1 (de) 1996-02-21 1997-07-03 Fritz Egger Ges M B H & Co Verfahren und Vorrichtung zum schnellen Erreichen der Soll-Restfeuchte von Fasergut beim Start einer Durchlauftrocknung
DE19609530A1 (de) 1996-03-11 1997-10-02 Fritz Egger Ges M B H & Co Verfahren und Vorrichtung zur zweistufigen Trocknung von Fasern aus Biomasse
DE19654043C2 (de) 1996-12-23 1998-05-28 Martin Dipl Ing Knabe Trockner mit Abgasreinigung mittels thermischer Nachverbrennung
EP0862718A1 (fr) 1995-11-21 1998-09-09 APV Anhydro A/S Procede et dispositif pour l'elaboration d'un produit pulverulent dans un four rotatif a sechage instantane
EP1128145A2 (fr) 2000-02-24 2001-08-29 LBE Feuerungstechnik GmbH Procédé et dispositif pour le séchage de fibres de bois
WO2001067016A1 (fr) 2000-03-08 2001-09-13 Valmet Panelboard Gmbh Procede et dispositif pour le sechage direct de particules
DE10056459C1 (de) 2000-11-14 2002-04-04 Fraunhofer Ges Forschung Verfahren zum Aufbereiten faseriger Substanzen

Patent Citations (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE148620C (fr) * 1902-03-27
US1571518A (en) * 1922-12-12 1926-02-02 Vermont Casein Pty Ltd Apparatus for reducing and drying casein curd
US2118078A (en) * 1933-09-07 1938-05-24 Flugel Heinrich Drying method and apparatus
FR998617A (fr) 1949-09-06 1952-01-21 Procédé et dispositif pour la dessication et la vitaminisation de matières par atomisation
DE1629070A1 (de) * 1966-11-30 1971-01-28 Seidner Maschf E Grastrocknungsvorrichtung
DE2006366A1 (en) * 1970-02-12 1971-08-12 Gebr Giulini GmbH, 6700 Ludwigs hafen Drying of sticky temperature sensitive part-icles
GB1322018A (en) * 1970-06-30 1973-07-04 Do Nii Chernoj Metallurgii Method and apparatus for the thermal and or chemical treatment of particulate material
US3861059A (en) * 1972-07-03 1975-01-21 Hazemag Andreas Kg Drying apparatus
EP0365851B1 (fr) 1988-09-27 1991-12-11 Bison-Werke Bähre & Greten GmbH & Co. KG Séchoir à tambour à position horizontale pour matériau granulé
DE3919828A1 (de) * 1989-06-16 1990-12-20 Burgert Burdosa Schlaufenreaktor
EP0457203B1 (fr) 1990-05-18 1993-09-29 SC Technology AG Procédé de séchage sans émissions d'une substance dans un tambour de séchage
EP0459603A1 (fr) * 1990-06-01 1991-12-04 Körting Hannover Ag Procédé et dispositif pour le séchage continu de copeaux de bois, de fibres de bois ou d'autres matières en vrac
EP0459603B1 (fr) 1990-06-01 1993-11-10 Körting Hannover Ag Procédé et dispositif pour le séchage continu de copeaux de bois, de fibres de bois ou d'autres matières en vrac
EP0508546A1 (fr) 1991-04-08 1992-10-14 VandenBroek International B.V. Dispositif de séchage
EP0536650A1 (fr) 1991-10-11 1993-04-14 Alb. Klein GmbH & Co. KG Procédé et dispositif pour sècher des substances humides
DE4427709A1 (de) 1994-06-08 1996-01-11 Martin Knabe Verfahren und Vorrichtung zur Trocknung von Schüttgütern
EP0714006A1 (fr) 1994-11-24 1996-05-29 W. Kunz AG Procédé de séchage d'une substance, en particulier de copeaux de bois
EP0862718A1 (fr) 1995-11-21 1998-09-09 APV Anhydro A/S Procede et dispositif pour l'elaboration d'un produit pulverulent dans un four rotatif a sechage instantane
DE19606472C1 (de) 1996-02-21 1997-07-03 Fritz Egger Ges M B H & Co Verfahren und Vorrichtung zum schnellen Erreichen der Soll-Restfeuchte von Fasergut beim Start einer Durchlauftrocknung
DE19609530A1 (de) 1996-03-11 1997-10-02 Fritz Egger Ges M B H & Co Verfahren und Vorrichtung zur zweistufigen Trocknung von Fasern aus Biomasse
DE19654043C2 (de) 1996-12-23 1998-05-28 Martin Dipl Ing Knabe Trockner mit Abgasreinigung mittels thermischer Nachverbrennung
EP0851194A2 (fr) 1996-12-23 1998-07-01 Martin Dipl.-Ing. Knabe Sécheur avec purification de gaz d'échappement par post-combustion thermique
EP1128145A2 (fr) 2000-02-24 2001-08-29 LBE Feuerungstechnik GmbH Procédé et dispositif pour le séchage de fibres de bois
WO2001067016A1 (fr) 2000-03-08 2001-09-13 Valmet Panelboard Gmbh Procede et dispositif pour le sechage direct de particules
DE10056459C1 (de) 2000-11-14 2002-04-04 Fraunhofer Ges Forschung Verfahren zum Aufbereiten faseriger Substanzen

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105918454A (zh) * 2016-07-07 2016-09-07 河北皓凯农业机械有限公司 气吸循环式粮食干燥机

Also Published As

Publication number Publication date
DE10221367B4 (de) 2006-05-11
ATE491922T1 (de) 2011-01-15
DE10221367A1 (de) 2003-12-11
DE50313317D1 (de) 2011-01-27
EP1363097B1 (fr) 2010-12-15

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