EP1249181B1 - Préparation d'un gaz de traitement pour un sèchoir de tabac - Google Patents

Préparation d'un gaz de traitement pour un sèchoir de tabac Download PDF

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Publication number
EP1249181B1
EP1249181B1 EP02006529A EP02006529A EP1249181B1 EP 1249181 B1 EP1249181 B1 EP 1249181B1 EP 02006529 A EP02006529 A EP 02006529A EP 02006529 A EP02006529 A EP 02006529A EP 1249181 B1 EP1249181 B1 EP 1249181B1
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EP
European Patent Office
Prior art keywords
process gas
jets
set forth
tobacco
water
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
Application number
EP02006529A
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German (de)
English (en)
Other versions
EP1249181A2 (fr
EP1249181A3 (fr
Inventor
Dietmar Franke
Franck Plückhahn
Gerald Schmekel
Arno Dr. Weiss
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.)
British American Tobacco Germany GmbH
Original Assignee
British American Tobacco Germany GmbH
BAT Cigarettenfabriken GmbH
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 British American Tobacco Germany GmbH, BAT Cigarettenfabriken GmbH filed Critical British American Tobacco Germany GmbH
Publication of EP1249181A2 publication Critical patent/EP1249181A2/fr
Publication of EP1249181A3 publication Critical patent/EP1249181A3/fr
Application granted granted Critical
Publication of EP1249181B1 publication Critical patent/EP1249181B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B21/00—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects
    • F26B21/06—Controlling, e.g. regulating, parameters of gas supply
    • F26B21/08—Humidity
    • A—HUMAN NECESSITIES
    • A24—TOBACCO; CIGARS; CIGARETTES; SIMULATED SMOKING DEVICES; SMOKERS' REQUISITES
    • A24B—MANUFACTURE OR PREPARATION OF TOBACCO FOR SMOKING OR CHEWING; TOBACCO; SNUFF
    • A24B3/00—Preparing tobacco in the factory
    • A24B3/04—Humidifying or drying tobacco bunches or cut tobacco
    • 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
    • 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
    • F26B2200/22—Tobacco leaves
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S261/00—Gas and liquid contact apparatus
    • Y10S261/15—Duct humidifiers

Definitions

  • the invention relates to process gas processing for tobacco dryers.
  • the invention relates to a device for processing the process gas for a tobacco dryer and a method for processing the process gas for a tobacco dryer, in particular a stream or flight dryer.
  • Successful tobacco drying is generally characterized by the fact that the final tobacco moisture level after leaving the dryer has to be within a very narrow range around the so-called setpoint moisture level (for example 13.5% ⁇ 0.5%).
  • setpoint moisture level for example 13.5% ⁇ 0.5%).
  • complex control strategies with high control quality have been developed, which, however, can only prove their performance in connection with suitable control variables / actuators.
  • the degree of drying of the tobacco depends on the energy content, for example on the temperature of the water vapor / air mixture being transported, since the dwell time in the drying section is determined by the length of the dryer or the size of the tobacco separator. That is why influencing the drying gas temperature is a suitable parameter for setting the final tobacco moisture.
  • DE-A-31 14 712 relates to a device for drying tobacco, it relates in particular to a device for drying tobacco under drying conditions with a relatively high humidity.
  • US-A-5,955,011 relates to a device for producing and collecting fine fibers, e.g. Microfibers made of glass, high temperature resistant ceramic materials, organic materials based on carbon, polymers and other materials that can be defibrated.
  • Microfibers made of glass, high temperature resistant ceramic materials, organic materials based on carbon, polymers and other materials that can be defibrated.
  • an inertia in the adjustment to fluctuating process parameters should preferably be minimized.
  • this object is achieved by a device for processing the process gas for a tobacco dryer, in particular a stream or flight dryer, with a device, in particular a flow-through device, in the process gas stream before the tobacco dryer and before the tobacco is introduced into the process gas Boiler is provided, in which water introduced via several atomizing nozzles can be completely evaporated in contact with the process gas, the water supply being adjustable with regard to changes in tobacco inlet moisture and / or tobacco inlet quantity.
  • the process gas is loaded with moisture by the device according to the invention at a point in time when it does not come into contact with the tobacco, ie the evaporation unit ensures that when the tobacco is introduced a process gas is available which has the necessary process gas humidity and thus also the process gas temperature.
  • the evaporation unit can be arranged downstream of an indirect process gas heating system, in particular a heat exchanger system, the disadvantage of the inertia of such heat exchanger systems already mentioned being overcome.
  • the evaporation unit has a boiler or container through which flow flows, in which water introduced via a plurality of atomization nozzles is completely evaporated in contact with the process gas.
  • the evaporation unit can be constructed and installed in a process gas piping system if it is designed in such a way that it has a gas inlet, an adjoining, expanded steam generation chamber and a gas outlet, the water being introduced into the steam generation chamber via a plurality of two-substance nozzles, which are arranged in a ring on an expansion section or diffuser between the gas inlet and the steam generation chamber.
  • nozzles are used which introduce water droplets at a speed and droplet size which ensure complete evaporation over a short path length.
  • the process gas stream has a speed of 15 to 45 m / s at the gas inlet, for example, a diffuser angle of 10 ° to 40 °, in particular 25 ° to 35 °, preferably 30 °, is preferably selected.
  • a process gas speed of 2-10 m / s should be present in the boiler to minimize the length of the equipment.
  • the water spray emerging from the nozzles should have a droplet size of ⁇ 250 ⁇ m, in particular ⁇ 100 ⁇ m.
  • the atomizing nozzles or two-substance nozzles are preferably arranged in such a way that their spray areas do not essentially overlap in order to prevent the formation of larger droplets, and the cross-section of the apparatus is used optimally without droplets touching the apparatus wall.
  • the device for processing the process gas can be used for tobacco dryers with different cross sections.
  • the cross section of the device can be identical to or different from the cross section of the tobacco dryer.
  • Possible cross sections of the device or of the tobacco dryer with which the device is used are rectangular, in particular square, circular, or all shapes in between, such as oval, elliptical or also in the form of an elongated hole.
  • the device has four to twelve, in particular six to ten and preferably eight, nozzles, which are arranged in a ring essentially between the central section and the end section of the diffuser at the same angular distance from one another, the nozzles preferably having a spray jacket angle of 15 ° to 30 °, in particular 20 ° to 25 ° and preferably 22 °.
  • the water throughput of the nozzles can be 150 to 500 kg / h, preferably 200 to 300 kg / h.
  • the invention further relates to an evaporation unit for introducing water into the process gas stream of a tobacco dryer, with a flow-through boiler, in which water introduced via several atomizing nozzles is completely evaporated in contact with the process gas.
  • a flow-through boiler in which water introduced via several atomizing nozzles is completely evaporated in contact with the process gas.
  • the parameters already described above for the device according to the invention can also be implemented specifically in the case of the evaporation unit according to the invention. This applies in particular to the shape of the boiler or the evaporation unit through which the flow passes and the arrangement and flow through the nozzles.
  • this evaporation unit or, more generally, the boiler through which it flows and in particular the steam generation chamber can be constructed in modular longitudinal sections, which can preferably be connected to one another via flanges.
  • this can also be achieved by a basic setting of the overall length for the evaporation unit, but preferably by means of corresponding intermediate pieces to be installed with flanges, so that an adaptation to a possibly desired nozzle change is also possible.
  • the method according to the invention for processing the process gas for a tobacco dryer in particular a stream or flight dryer
  • more than one is used in one device, in particular a boiler through which the process gas flow is provided before the tobacco dryer and before the tobacco is introduced into the process gas
  • Water introduced into the atomizing nozzles completely evaporates in contact with the process gas, the water supply being adjustable with regard to changes in a tobacco inlet moisture and / or tobacco inlet quantity.
  • FIGS. 1 and 2 An evaporation unit according to the invention is shown in FIGS. 1 and 2 in a schematic cross section and in a longitudinal section.
  • hot process gas flows into the evaporation unit 1, which comes, for example, from a heat exchanger system.
  • the process gas is indirectly heated via a flue gas heat exchanger that is supplied with hot gas from a burner.
  • a process gas stream 24 enters the gas inlet 2 of the evaporation unit according to the invention after heating in the heat exchanger system.
  • a diffuser 4 adjoins the gas inlet 2, on the circumference of which there are arranged two-substance nozzles 6 with which water can be injected into the evaporation unit 1.
  • the distribution of the nozzles 6 can be seen in FIG. 1, there are eight nozzles each with an angular distance of 45 °.
  • the spray projection surface of each nozzle is also drawn in with reference numeral 7, and it can be seen here that these projection surfaces do not overlap.
  • the steam generating chamber 8 which is referred to here because the water injected from the nozzles 6 converts to steam in this area, which then forms part of the process gas, adjoins the diffuser 4 with the nozzles 6.
  • the chamber 8 is of modular construction, and the longitudinal sections 8a and 8b are shown in Figure 2, which are integrated via the flanges 12 and 14. This modular design allows the chamber 8 to be lengthened or shortened as required, if this should be necessary, possibly when using other nozzles.
  • the chamber 8 is followed by the confuser 16, to which the gas outlet 18 then connects.
  • the process gas heated in the heat exchanger system therefore flows through the evaporation unit 1 and is enriched with evaporating water via the nozzles 6, so that it is present at the outlet 18 as a homogeneous flow without droplets into which the cut tobacco can be introduced without the risk of clumping due to water accumulation consists.
  • the process gas temperature can be regulated and thus the final tobacco moisture can be adjusted very quickly and directly by increasing or decreasing water or steam supply via the nozzles 6.
  • a so-called “dummy load” that is to say a load for the dryer by supplying water or steam to the process gas, which prevents dryer overheating even when there is occasionally no tobacco entry during production interruptions.
  • the surface created is of crucial importance for a fast evaporation process until the thermodynamic equilibrium is reached. That is why the generation of a fine spray is an important prerequisite for successful evaporation.
  • the so-called two-component nozzle is particularly suitable for solving this task because, in contrast to the simpler single-component nozzles, this achieves atomization with average diameters of less than 100 ⁇ m.
  • Two-component nozzles generally have a limited throughput of approximately 500 kg / h with the required droplet sizes of ⁇ 100 ⁇ m. Therefore, several nozzles are advantageous for larger water flow rates.
  • the evaporation time is a quadratic function of the droplet diameter.
  • Another variable that affects the necessary evaporation time is the so-called relative speed of drying gas / droplets. In the case of small particle diameters, the relative speed after a short particle flight becomes negligible; so that no influence of this size can be observed.
  • the particle trajectories (trajectories) of the droplets are determined by the size, the spray angle and the initial speed.
  • the orbits for particles with 50 ⁇ m and 100 ⁇ m have been approximated.
  • the end of the particle track means complete evaporation. It is easy to see that smaller particles completely change to the gaseous state after short flight times (container lengths).
  • the drying gas flow acts as a kind of burning glass.
  • the complete evaporation of the sprayed-in water is of great advantage in a current dryer for optimal regulation of the tobacco moisture / drying gas temperature by means of a water nozzle.
  • this complete evaporation is carried out in a compact apparatus which is of the smallest possible size in which even large amounts of water to be evaporated are completely evaporated.
  • the size of the evaporation unit (evaporator) 1 is an important criterion for use not only in the tobacco industry for reasons of cost and space.
  • the optimal evaporation of water depends on many factors.
  • these are the water droplet size, the gas temperature and, depending on this, the residence time of the droplets in the hot gas stream.
  • the gas temperature in the present case "current dryer” is fixed, since it depends on the tobacco drying process. Under the boundary condition of the fixed gas temperature, the task is to generate droplets that are as small as possible by means of suitable nozzles and then to give these droplets sufficient time to evaporate.
  • the minimum residence time of the drops in the hot gas stream leads to the task of designing a suitable evaporator 1 (length, diameter, etc.) which ensures that the drops are still in the evaporator 1 and not within the necessary evaporation time fly unevaporated through the following pipe system.
  • the most important criterion for the residence time in the evaporator 1 is the flight speed of the drops. In order to be able to make the evaporator 1 as short as possible, the droplet speed and, accordingly, the gas speed (in the case of very small droplets, approximately the same speed as the gas ⁇ low slip) must be low.
  • the gas velocities in hot gas pipes are usually between 20 and 40 m / s (in the present case between 20 and 30 m / s), this means that the evaporator 1 must be enlarged in diameter (diffuser 4) in order to reduce the gas velocity to reach. Based on the tests carried out, it was found that the gas velocity should be in the range between approx. 2 to 10 m / s in order to achieve an optimal design in terms of evaporation and size of the container.
  • the cylindrical length of the chamber 8 could be varied between 0.8 and 2 m in the experimental setup in order to investigate the influence of the residence time of the droplets in the hot gas stream.
  • the assessment of the complete evaporation of the drops was carried out using a relatively simple structure in terms of apparatus and measurement technology.
  • a baffle plate pack (not shown) was installed in the gas outlet 18 (diameter 700 mm) in the flow direction directly after the chamber 8, in which the non-evaporated water drops are separated by the centrifugal forces that occur at the sharp deflections.
  • the baffle plate packs were designed so that the separated water runs in the direction of a sump and is enriched there.
  • Small temperature sensors (PT 100) were installed at several points in this tub.
  • the measured temperature due to the cooling effect of the water corresponds approximately to the so-called cooling surface limit temperature of the phase mixture water / hot air.
  • this temperature is always below 100 ° C and accordingly differs significantly from the hot gas temperatures, which are between approx. 120 ° C to 200 ° C in the area of the baffle plate package.
  • the temperature measured there corresponds to the hot gas temperature.
  • the trough is designed so that it can be easily emptied using a swivel device at the start of an experiment.
  • Each of the eight nozzles 6 has a water throughput of 250 kg / h.
  • the propellant for the nozzles 6 is saturated steam: in principle, the use of compressed air is also possible.
  • the mass flow is applied uniformly to the nozzles.
  • the drop spectrum consists of particles with a diameter of less than 100 ⁇ m.
  • the measured gas and separator sump temperature is in the range of complete evaporation.
  • the chamber length and the angle of the nozzle positioning can have an important influence on the complete evaporation.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Manufacture Of Tobacco Products (AREA)
  • Drying Of Solid Materials (AREA)

Claims (21)

  1. Dispositif pour la préparation du gaz de traitement d'un séchoir à tabac, en particulier un séchoir pneumatique ou à ailettes, caractérisé en ce que, dans le courant de gaz de traitement (24) avant le séchoir à tabac et avant l'introduction du tabac dans le gaz de traitement, on prévoit une installation (1), en particulier une bouilloire à passage, dans laquelle de l'eau introduite au moyen de plusieurs buses d'atomisation (6) en contact avec le gaz de traitement est complètement vaporisable, l'introduction d'eau étant ajustable en fonction des changements de l'humidité du tabac d'entrée et/ou de la quantité de tabac introduite.
  2. Dispositif selon la revendication 1, caractérisé en ce que l'installation (1) présente une unité d'évaporation qui est disposée dans le courant de gaz de traitement (24) après un système de réchauffement indirect du gaz de traitement, en particulier un système échangeur de chaleur.
  3. Dispositif selon l'une des revendications 1 ou 2, caractérisé en ce que l'installation (1) présente une introduction de gaz (2), une chambre de production de vapeur élargie qui y est raccordée (8) et une sortie de gaz (18), l'eau étant introduite dans la chambre de production de vapeur (8) au moyen de plusieurs buses doubles (6), qui sont disposées en forme d'anneau sur une section d'expansion ou diffuseur (4) entre l'entrée de gaz (2) et la chambre de production de vapeur (8).
  4. Dispositif selon la revendication 1 ou 3, caractérisé en ce que l'on utilise des buses (6) qui introduisent des gouttelettes d'eau avec une vitesse et une taille de gouttelettes, qui assurent une évaporation complète en un parcours court.
  5. Dispositif selon la revendication 4, caractérisé en ce que la position des buses (6) est ajustée de telle sorte que les gouttelettes d'eau sortant des buses (6) après un court chemin présentent essentiellement la même vitesse que le courant de gaz de traitement (24).
  6. Dispositif selon la revendication 4 ou 5, caractérisé en ce que lorsque le courant de gaz de traitement (24) présente dans l'installation (1) une vitesse de 2 à 10 m/s, on choisit un angle de diffuseur de 10° à 40°, en particulier de 25° à 35°, de préférence de 30°.
  7. Dispositif selon l'une des revendications 4 à 6, caractérisé en ce que le nuage d'eau sortant des buses (6) présente une taille de gouttelettes < 250 µm, en particulier < 100 µm.
  8. Dispositif selon l'une des revendications 1 à 7, caractérisé en ce que les buses d'atomisation ou les buses doubles (6) sont disposées de telle sorte que leurs domaines de pulvérisation ne se recoupent essentiellement pas.
  9. Dispositif selon l'une des revendications 3 à 8, caractérisé en ce que quatre à douze, en particulier six à dix, de préférence huit buses (6) sont disposées en forme d'anneaux essentiellement entre la partie médiane et la partie d'extrémité du diffuseur (4) l'un par rapport à l'autre dans le même écart angulaire, les buses (6) présentant un angle de manteau de pulvérisation de 15° à 30°, en particulier de 20° à 25°, de préférence de 22°.
  10. Dispositif selon l'une des revendications 1 à 9, caractérisé en ce que les buses (6) présentent un débit d'eau de 150 à 500 kg/h, de préférence d'environ 200 à 350 kg/h.
  11. Dispositif selon la revendication 3, caractérisé en ce que la bouilloire à passage, en particulier la chambre de production de vapeur (8) est construite en partie de sections de longueurs modulaires (8a, 8b), qui peuvent être reliées entre elles de préférence au moyen de flasques (12, 14).
  12. Procédé pour la préparation du gaz de traitement pour un séchoir à tabac, en particulier un séchoir pneumatique ou un séchoir à ailettes, caractérisé en ce que, dans une installation (1), en particulier une bouilloire à passage, qui est prévue dans le courant de gaz de traitement (24) avant le séchoir à tabac et avant l'introduction du tabac dans le gaz de traitement, on évapore complètement l'eau introduite au moyen de plusieurs buses d'atomisation (6) en contact avec le gaz de traitement, l'introduction d'eau étant ajustable en fonction des modifications de l'humidité du tabac d'entrée et/ou de la quantité de tabac introduite.
  13. Procédé selon la revendication 12, dans lequel l'installation (1) qui présente une unité d'évaporation, est disposée dans le courant de gaz de traitement (24) après un système de réchauffement du gaz de traitement indirect, en particulier un système d'échangeur de chaleur.
  14. Procédé selon l'une des revendications 12 ou 13, dans lequel l'eau est introduite dans une chambre de production de vapeur (8) de l'installation (1) via plusieurs buses doubles (6), qui sont disposées en forme d'anneaux dans une section d'expansion ou diffuseur (4) entre l'entrée de gaz (2) et la chambre de production de vapeur (8).
  15. Procédé selon la revendication 12 ou 14, dans lequel on introduit des gouttelettes d'eau avec une vitesse et une taille de gouttelettes, qui assurent une évaporation complète en un parcours court.
  16. Procédé selon la revendication 15, dans lequel les gouttelettes qui sortent de la buse (6) après un court parcours présentent essentiellement la même vitesse que le courant de gaz de traitement (24).
  17. Procédé selon la revendication 15 ou 16, dans lequel le courant de gaz de traitement dans le récipient présente une vitesse de 2 à 10 m/s, en choisissant un angle de diffuseur de 20° à 40°, en particulier de 25° à 35°, de préférence 30°.
  18. Procédé selon l'une des revendications 12 à 17, dans lequel le nuage d'eau sortant des buses présente une taille de gouttelettes < 250 µm, en particulier < 100 µm.
  19. Procédé selon l'une des revendications 12 à 18, dans lequel les zones de pulvérisation des buses d'atomisation ou des buses doubles (6) sont ajustées de manière à ce qu'elles ne se recoupent essentiellement pas.
  20. Procédé selon l'une des revendications 12 à 19, dans lequel sont disposées quatre à douze, en particulier six à dix, de préférence huit buses (6) en forme d'anneaux essentiellement entre la partie médiane et la partie finale du diffuseur (4) entre elles à distance angulaire identique, les buses (6) présentant un angle de manteau de pulvérisation de 15° à 30°; en particulier de 20° à 25°, de préférence 22°.
  21. Procédé selon l'une des revendications 12 à 20, dans lequel les buses (6) présentent un débit d'eau de 150 à 500 kg/h, de préférence d'environ 200 à 300 kg/h.
EP02006529A 2001-04-10 2002-03-19 Préparation d'un gaz de traitement pour un sèchoir de tabac Expired - Lifetime EP1249181B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10117783A DE10117783A1 (de) 2001-04-10 2001-04-10 Prozessgasaufbereitung für Tabaktrockner
DE10117783 2001-04-10

Publications (3)

Publication Number Publication Date
EP1249181A2 EP1249181A2 (fr) 2002-10-16
EP1249181A3 EP1249181A3 (fr) 2003-10-29
EP1249181B1 true EP1249181B1 (fr) 2004-12-29

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EP02006529A Expired - Lifetime EP1249181B1 (fr) 2001-04-10 2002-03-19 Préparation d'un gaz de traitement pour un sèchoir de tabac

Country Status (7)

Country Link
US (1) US6880814B2 (fr)
EP (1) EP1249181B1 (fr)
AT (1) ATE285686T1 (fr)
BR (1) BR0201174B1 (fr)
DE (2) DE10117783A1 (fr)
ES (1) ES2233731T3 (fr)
RU (1) RU2229252C2 (fr)

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ATE514909T1 (de) 2008-12-23 2011-07-15 Kronotec Ag Holzzerkleinerungsprodukt-trocknungsanlage
CN101982387A (zh) * 2010-10-29 2011-03-02 秦皇岛烟草机械有限责任公司 一种气流设备的进料装置
EP2702880A4 (fr) * 2011-04-28 2015-06-10 Japan Tobacco Inc Dispositif de traitement de matière première sous forme de tabac
CN106974317B (zh) * 2016-01-15 2019-01-11 红塔烟草（集团）有限责任公司楚雄卷烟厂 一种热风润叶设备的控制方法
CN108323790A (zh) * 2018-03-12 2018-07-27 周亚男 一种烟草汁液提取用的烘干装置
CN114226226A (zh) * 2021-12-15 2022-03-25 河南中烟工业有限责任公司 一种烟丝湿团筛分检测装置
CN114279202A (zh) * 2021-12-15 2022-04-05 河北白沙烟草有限责任公司保定卷烟厂 一种提高蒸汽干度的装置

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103948157A (zh) * 2014-04-04 2014-07-30 广东中烟工业有限责任公司 一种烟草烘丝装置
CN103948157B (zh) * 2014-04-04 2016-03-30 广东中烟工业有限责任公司 一种烟草烘丝装置

Also Published As

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BR0201174B1 (pt) 2012-10-02
US6880814B2 (en) 2005-04-19
BR0201174A (pt) 2003-06-10
EP1249181A2 (fr) 2002-10-16
EP1249181A3 (fr) 2003-10-29
US20020185755A1 (en) 2002-12-12
DE10117783A1 (de) 2002-10-24
ATE285686T1 (de) 2005-01-15
DE50201868D1 (de) 2005-02-03
RU2229252C2 (ru) 2004-05-27
ES2233731T3 (es) 2005-06-16

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