EP3009776A1 - Appareil et procédé de séchage de matière particulaire en vrac - Google Patents

Appareil et procédé de séchage de matière particulaire en vrac Download PDF

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Publication number
EP3009776A1
EP3009776A1 EP14189037.6A EP14189037A EP3009776A1 EP 3009776 A1 EP3009776 A1 EP 3009776A1 EP 14189037 A EP14189037 A EP 14189037A EP 3009776 A1 EP3009776 A1 EP 3009776A1
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EP
European Patent Office
Prior art keywords
cylindrical part
superheated steam
steam
inlet chamber
inner cylindrical
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.)
Withdrawn
Application number
EP14189037.6A
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German (de)
English (en)
Inventor
Jensen Arne Sloth
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.)
ASJ-IPR ApS
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ASJ-IPR ApS
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Publication date
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Application filed by ASJ-IPR ApS filed Critical ASJ-IPR ApS
Priority to EP14189037.6A priority Critical patent/EP3009776A1/fr
Priority to DE202015009570.4U priority patent/DE202015009570U1/de
Priority to EP18154880.1A priority patent/EP3351884A1/fr
Priority to EP19171293.4A priority patent/EP3550242B1/fr
Priority to PL19171293.4T priority patent/PL3550242T3/pl
Priority to TR2018/08829T priority patent/TR201808829T4/tr
Priority to PL15189711T priority patent/PL3009777T3/pl
Priority to DE202015009713.8U priority patent/DE202015009713U1/de
Priority to RS20231211A priority patent/RS64984B1/sr
Priority to EP15189711.3A priority patent/EP3009777B1/fr
Publication of EP3009776A1 publication Critical patent/EP3009776A1/fr
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
    • F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
    • 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

Definitions

  • the present invention relates to an apparatus for drying bulk particulate material and a method of drying bulk particulate material, the bulk particulate material in particular being sugar beet pulp.
  • EP 0 058 651 A1 which relates to a method of preparing cattle feed from various agricultural products, such as sugar beet pulp, molasses, citrus fruit pulp and peel and various fermentation products.
  • EP 0 153 704 A2 teaches a process of removing liquid from a particulate solid material in which the material is passed through a row of interconnected cells and superheated steam is introduced into said cells at their lower ends so as to impart a whirling movement during which dried panicles are lifted out of the cells and into a common transfer zone and into a discharge cell with no steam supply.
  • the prior art document WO 92/01200 discloses an apparatus for drying a moist particulate material having a non-uniform particle size with superheated steam.
  • the apparatus comprises a cylindrical vessel comprising a number of parallel, substantially vertical drying chambers located in ring form.
  • the preferred embodiment includes 15 drying chambers connected in series, and a discharge chamber located between the first and the last drying chamber.
  • the particulate material At the first drying chamber after the inlet, the particulate material will have a high liquid content whereas the particulate material at the last drying chamber will have a low liquid content.
  • the drying chambers are adapted to induce a whirling movement of the flow of superheated steam in order to improve the contact between the steam and the particulate material and to cause the particulate material to remain a short and uniform time period within each of the drying chambers.
  • the drying chambers all have a substantially uniform size and shape and receive about the same amount of superheated steam although it is evident that the particulate material will behave differently when it is moist and when it is dry. In particular, the moist particles tend to be heavier than the dry particles and thus cause a larger flow resistance.
  • the moist particulate material tend to accumulate in first drying chamber. Particulate material remaining an extended time period in the first drying chamber may potentially clog the first drying chamber and reduce the intensity of the whirling movement of the flow of superheated steam.
  • Previous technologies suggest the inclusion of means for increasing the retention time of the particulate material in some of the drying chambers and means for reducing the retention time of the particulate material in some of the other drying chambers. However, such means may add to the flow resistance and risk reducing the whirling movement of the flow of superheated steam which is necessary for achieving an effective drying of the particulate material.
  • the whirling movement allows the particulate material to distribute more evenly within the chamber which will result in a more effective drying than particulate material which clogs up and forms large chunks of material.
  • an apparatus for drying bulk particulate materials comprising:
  • the vessel is typically made of metal capable of withstanding temperatures of superheated steam exceeding 100°C and pressures exceeding the ambient atmospheric pressure. Typical pressures range from ambient atmospheric pressures to a pressure of up to 3 barg.
  • the vessel comprises a lower cylindrical part and an upper cylindrical part which form part of the outer enclosure of the vessel.
  • the vessel further comprises a top part and a bottom part in order to form an essentially enclosed vessel.
  • the first flow path inside the inner cylindrical part and the second flow path between the outer enclosure of the vessel and the inner cylindrical part define the recirculation of the superheated steam.
  • the flow of superheated steam is established by the impeller which is located in the lower cylindrical part below the steam permeable bottom and/or between the inner cylindrical part and the steam permeable bottom of the lower cylindrical part in order to establish a high pressure below the steam permeable bottom, which in turn establishes a fluid bed and the re-circulating flow of superheated steam.
  • the inner cylindrical part includes the heat exchanger which maintains the re-circulating steam in a superheated state for avoiding any condensation to occur within the vessel.
  • the drying is taking place by superheated steam contacting the moist particulate material and transferring some of its heat to the moist particles.
  • the liquid content of the moist particulate material will vaporize and the vapor becomes part of the superheated steam.
  • the heat energy required for the vaporization and thereby removed from the superheated steam is replenished at the heat exchanger in order to avoid condensation of the superheated steam into liquid within the vessel. Any surplus steam may be released via an overpressure valve at the top part of the vessel.
  • the vessel also includes means for inducing a circumferential flow component in order to cause the particulate material to move slowly in a circumferential direction from the inlet to the outlet.
  • the partitioning walls serve to delimit the lower cylindrical part into several chambers.
  • the first chamber is the inlet chamber which is connected to a closed off screw conveyor or the like for injecting the moist particulate material into the inlet chamber.
  • the outlet chamber also comprises a closed off screw conveyor or the like for discharging the dry particulate material.
  • the intermediate chambers are located between inlet chamber and the outlet chamber.
  • the partitioning walls include openings for allowing particulate material to be transported from the inlet chamber to the outlet chamber via the intermediate chambers.
  • the inlet chamber and the intermediate chambers receive superheated steam from a steam permeable bottom and thus constitute drying chambers.
  • a whirling fluid bed and a whirling flow is established which maintains most of the particulate material in the lower cylindrical part and increases the contact between the superheated steam and the particulate material.
  • the outlet chamber does not have a steam permeable bottom to allow the particulate material to settle before being discharged.
  • the number of chambers determines the retention time of the particulate material within the vessel and the mixing behaviour of the particulate material within each of the chambers. A small number of chambers reduces the retention time of the particulate material while allowing the particulate material to distribute more uniformly within the chamber, and vice versa.
  • the particulate material arriving at the first drying chamber i.e. the inlet chamber
  • the particulate material arriving at the first drying chamber is moist and contains a large portion of liquid and thus tends to be heavy and clogging up the chamber. These particles generate a large drag and the flow velocity of the superheated steam is reduced due to the increased flow resistance. This leads to less lift in the fluid bed, less whirling motion of the flow and less distribution of the particulate material which results in the accumulation of moist particulate material in some parts of the inlet chamber.
  • the particulate material arriving at the last drying chamber before the outlet chamber in which the now dried particulate material is ejected is substantially dry and light and well distributed within the chamber since nothing is preventing the formation of an effective whirling flow of superheated steam. This may lead to increased lift in the fluid bed and a large amount of particulate material flowing into the upper cylindrical part of the vessel
  • the heavy and liquid particulate material contained in the first chamber should receive a larger portion of the superheated steam received from the inner cylindrical part via the impeller.
  • a sufficient flow of superheated steam may form which will generate sufficient lift to be capable of overcoming the drag of the moist particulate material.
  • a uniform distribution of the particulate material may be achieved in all of the drying chambers.
  • the inlet chamber is adapted to receive between 22% and 45% of the superheated steam received from the inner cylindrical part, preferably between 25% and 40% of the superheated steam received from the inner cylindrical part, more preferably between 30% and 35% of the superheated steam received from the inner cylindrical part, such as 33% of the superheated steam received from the inner cylindrical part, alternatively, the inlet chamber being adapted to receive between 20% and 22% of the superheated steam received from the inner cylindrical part, and/or between 22% and 25% of the superheated steam received from the inner cylindrical part, and/or between 25% and 30% of the superheated steam received from the inner cylindrical part, and/or between 30% and 35% of the superheated steam received from the inner cylindrical part, and/or between 35% and 40% of the superheated steam received from the inner cylindrical part, and/or between 40% and 45% of the superheated steam received from the inner cylindrical part, and/or between 45% and 50% of the superheated steam received from the inner cylindrical part.
  • the inlet chamber and the intermediate chambers each define a flow area being parallel with the first cross-sectional area, the flow area of the inlet chamber being greater than the flow area of any of the intermediate chambers.
  • the cross-sectional area of the inlet chamber may thus constitute at least 20% of the cross-sectional area of all of the chambers, preferably any of the previously mentioned percentages.
  • the partitioning walls define a first partitioning wall and a second partitioning wall both delimiting the inlet chamber in the circumferential direction, the first partitioning wall and a second partitioning wall defining an angle them between of between 50° and 180°, preferably between 70° and 160, more preferably between 90° and 140°, such as 120°.
  • the inlet chamber By allowing the inlet chamber to occupy a larger circular sector of the ring-shaped space between the lower cylindrical part and the inner cylindrical part, the inlet chamber will receive a larger portion of the superheated steam from the impeller, provided the superheated steam is uniformly distributed over the ring-shaped space.
  • the steam permeable bottom of the inlet chamber defines a steam permeability of between 20% and 45% of the steam permeability of the total steam permeability of all of the steam permeable bottoms, preferably between 25% and 40%, more preferably between 30% and 35%, such as 33%.
  • all chambers may have the same size and the permeability of the steam permeable bottom may be higher for the inlet chamber compared to the intermediate chambers. In this way, a larger portion of the superheated steam will enter the inlet chamber.
  • the steam permeable bottoms of the inlet chamber and the intermediate chambers define perforations.
  • the perforations will be located between the impeller and the fluid bed.
  • the size of each individual perforation should be made such that no particulate material may slip through into the impeller.
  • the perforations of the steam permeable bottoms of the inlet chamber define an area being 20% to 45% of the total area of all of the perforations of all of the steam permeable bottoms, preferably between 25% and 40%, more preferably between 30% and 35%, such as 33%.
  • the vessel comprises an intermediate conical part interconnecting the lower cylindrical part and the upper cylindrical part so that the second cross-sectional area is larger than the first cross-sectional area.
  • the lower cylindrical part and the upper cylindrical part may be interconnected by the conical part in which the flow velocity will decrease due to the increasing flow area, as described by the Bernoulli principle. In this way, the lift will decrease in the upper cylindrical part and most of the particulate material in the conical part will not reach the upper cylindrical part and any particulate material appearing in the upper cylindrical part will fall back into the lower cylindrical part.
  • the second cross-sectional is substantially equal to the first cross-sectional area.
  • all of the steam originates from the moist bulk particulate material.
  • no superheated steam must be separately added to the vessel as the superheated steam may be generated from the liquid which is vaporized from the moist particulate material.
  • the surplus superheated steam may, as described above, be let out via an overpressure valve or outlet, preferably into a heat exchanger in order to re-use some of the heat energy of the steam.
  • the second number of intermediate chambers is between 6 and 40, preferably 10 to 25, more preferably 12 to 20, such as 14.
  • the number of intermediate chambers may thus vary between any of the above numbers.
  • the total number of chambers adds the inlet chamber and the outlet chamber to the above number.
  • the upper cylindrical part comprises a cyclone for transporting particulate material from the upper cylindrical part to the lower cylindrical part.
  • FIG. 1 shows a side sectional view of an apparatus 10 for drying bulk particulate materials, in particular drying of beet pulp.
  • the apparatus 10 comprises a vessel 12 comprising a lower cylindrical part 14, an intermediate conical part 16 and an upper cylindrical part 18.
  • the vessel 12 is closed off by a top 20 and a bottom 22.
  • the vessel 12 further comprises an inner cylindrical part 24 extending within the vessel between the upper cylindrical part 18 and the lower cylindrical part 14.
  • the inner cylindrical part 24 includes a heat exchanger (not visible) and defines a first fluid path from said upper cylindrical part 18 to said lower cylindrical part 14 within said inner cylindrical part 24 and a second fluid path from said lower cylindrical part 14 to said upper cylindrical part 18 outside said inner cylindrical part, as shown by the arrows.
  • the vessel 12 further comprises an inlet 26 constituting a screw conveyor for introducing moist particulate material into the lower cylindrical part 14 of the vessel 12 as shown by the arrow, and an outlet 28 constituting a screw conveyor for ejecting dry particulate material from the lower cylindrical part 14 of the vessel 12 as shown by the arrow.
  • the inlet 26 is located above and circumferentially shifted relative to the outlet 28.
  • a motor 30 is located below the vessel 12 for driving an impeller 32 located in the lower cylindrical part 14 below the inner cylindrical part 24.
  • the impeller 32 generates a flow of superheated steam along the above mentioned fluid paths.
  • a steam permeable bottom 34 is located above the impeller 32.
  • a number of partitioning walls 36 are radially extending between the lower cylindrical part 14 and the inner cylindrical part 24 and dividing the space between the lower cylindrical part 14 and the inner cylindrical part 24 into a number of chambers 38.
  • the chamber located at the inlet 26 is designated inlet chamber 38' and the chamber located at the outlet 28 is designated outlet chamber 38".
  • the inlet chamber 38' and the outlet chamber 38" are located adjacent each other, however, the particulate material should not be able to move directly from the inlet chamber 38' to the outlet chamber 38" without passing the intermediate chambers 38.
  • the moist particulate material is received in the inlet chamber 38' on a fluid bed established by the flow of superheated steam above the steam permeable bottom 34.
  • the partitioning walls 36 include whirling blades 40 for inducing a circumferential whirl for transporting the particulate material from the inlet chamber 38' to the outlet chamber 38" via the intermediate chambers 38 as shown by the arrows.
  • the outlet chamber 38" has a non-permeable bottom which allows the dried particulate material to be ejected via the outlet 28 as shown by the arrow.
  • the upper cylindrical part 18 of the vessel 12 comprises guide blades 42 for generating a cyclone field in upper cylindrical part 18.
  • the guide blades 42 will establish a whirling movement of the flow of superheated steam corresponding to the above mentioned circumferential whirl and force any particles outwardly which have been lifted from the lower cylindrical part 14 through the intermediate conical part 16 into the upper cylindrical part 18.
  • the outwardly forced particles will be collected in a cyclone 44 and returned to the lower cylindrical part 14 as shown by the arrows.
  • the superheated steam will be introduced into the inner cylindrical part 24 and be reheated by the heat exchanger before returning to the impeller 32. A small portion of the superheated steam will escape the vessel 12 via a centrally located steam exit 46.
  • the superheated steam exiting the vessel 12 is subsequently cooled off via a heat exchanger.
  • Each chamber 38 may include further blades or similar means for establishing a whirling flow in the radial direction of the chamber 38.
  • the whirling flow will increase the distribution of the particulate material within the chambers 38 and thereby increase the contact between the superheated steam and the particulate material, thereby increasing the vaporization of fluid from the particulate material and improving the drying.
  • FIG. 2 shows a perspective view of the lower cylindrical part 14 of the apparatus 10.
  • the inlet chamber 38' is larger than the intermediate chambers 38 for allowing a larger portion of the superheated steam to enter the inlet chamber 38' compared to the intermediate chambers 38.
  • the heavy liquid containing particulate material entering the inlet chamber 38' may be distributed over a larger area, reducing the flow resistance and thereby both preventing clogging and improving the drying.
  • FIG. 3 shows a top sectional view of the lower cylindrical part 14 of the apparatus 10.
  • the radial partitioning walls 36 define the circular sector shape of the chambers 38.
  • the particulate material may move in a clockwise direction from the inlet chamber 38' to the outlet chamber 38" via all of the chambers by flowing above the partition wall 36 or through apertures 48 which may optionally exist in the partition wall 36.
  • the steam permeable bottom 34 is shown having perforations 50 for allowing superheated steam to flow into the drying chambers.
  • FIG. 4 a perspective view of a lower cylindrical part 14 of an alternative embodiment of the apparatus designated 10'.
  • the inlet chamber 38' may be made as large as the intermediate chambers 38 and have a steam permeable bottom 34' allowing a larger portion of the superheated steam from the impeller (not shown) to pass compared to the intermediate chambers 38.
  • FIG. 5 shows a top sectional view of the lower cylindrical part 14 of the alternative embodiment of the apparatus 10'.
  • the perforations 50 may be larger as shown in the present figure.
  • the additional superheated steam allows the inlet chamber 38' to produce additional lift overcoming the drag by the heavy liquid containing particulate material.
  • the intermediate chambers 38 have less or smaller perforations 50 since the particulate material will be lighter and thereby less prone to clog.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Drying Of Solid Materials (AREA)
EP14189037.6A 2014-10-15 2014-10-15 Appareil et procédé de séchage de matière particulaire en vrac Withdrawn EP3009776A1 (fr)

Priority Applications (10)

Application Number Priority Date Filing Date Title
EP14189037.6A EP3009776A1 (fr) 2014-10-15 2014-10-15 Appareil et procédé de séchage de matière particulaire en vrac
EP15189711.3A EP3009777B1 (fr) 2014-10-15 2015-10-14 Appareil et procédé de séchage de matière particulaire en vrac
PL19171293.4T PL3550242T3 (pl) 2014-10-15 2015-10-14 Urządzenie do suszenia materiału sypkiego luzem i metoda suszenia materiału sypkiego luzem
EP18154880.1A EP3351884A1 (fr) 2014-10-15 2015-10-14 Appareil et procédé de séchage de matière particulaire en vrac
EP19171293.4A EP3550242B1 (fr) 2014-10-15 2015-10-14 Appareil et procédé de séchage de matière particulaire en vrac
DE202015009570.4U DE202015009570U1 (de) 2014-10-15 2015-10-14 Vorrichtung zum Trocknen von teilchenförmigem Schüttgut
TR2018/08829T TR201808829T4 (tr) 2014-10-15 2015-10-14 Dökme tanecikli malzemenin kurutulması için bir aparat ve dökme tanecikli malzemenin kurutulması için bir usul.
PL15189711T PL3009777T3 (pl) 2014-10-15 2015-10-14 Urządzenie do suszenia dużej ilości drobnocząsteczkowego materiału oraz sposób suszenia dużej ilości drobnocząsteczkowego materiału
DE202015009713.8U DE202015009713U1 (de) 2014-10-15 2015-10-14 Vorrichtung zur Trocknung von partikelförmigem Schüttgut
RS20231211A RS64984B1 (sr) 2014-10-15 2015-10-14 Aparat za sušenje čestičnog materijala u masi i postupak sušenja čestičnog materijala u masi

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP14189037.6A EP3009776A1 (fr) 2014-10-15 2014-10-15 Appareil et procédé de séchage de matière particulaire en vrac

Publications (1)

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EP3009776A1 true EP3009776A1 (fr) 2016-04-20

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ID=51690974

Family Applications (4)

Application Number Title Priority Date Filing Date
EP14189037.6A Withdrawn EP3009776A1 (fr) 2014-10-15 2014-10-15 Appareil et procédé de séchage de matière particulaire en vrac
EP15189711.3A Active EP3009777B1 (fr) 2014-10-15 2015-10-14 Appareil et procédé de séchage de matière particulaire en vrac
EP18154880.1A Withdrawn EP3351884A1 (fr) 2014-10-15 2015-10-14 Appareil et procédé de séchage de matière particulaire en vrac
EP19171293.4A Active EP3550242B1 (fr) 2014-10-15 2015-10-14 Appareil et procédé de séchage de matière particulaire en vrac

Family Applications After (3)

Application Number Title Priority Date Filing Date
EP15189711.3A Active EP3009777B1 (fr) 2014-10-15 2015-10-14 Appareil et procédé de séchage de matière particulaire en vrac
EP18154880.1A Withdrawn EP3351884A1 (fr) 2014-10-15 2015-10-14 Appareil et procédé de séchage de matière particulaire en vrac
EP19171293.4A Active EP3550242B1 (fr) 2014-10-15 2015-10-14 Appareil et procédé de séchage de matière particulaire en vrac

Country Status (5)

Country Link
EP (4) EP3009776A1 (fr)
DE (2) DE202015009570U1 (fr)
PL (2) PL3009777T3 (fr)
RS (1) RS64984B1 (fr)
TR (1) TR201808829T4 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3486591B1 (fr) 2014-04-30 2020-06-17 BMA Braunschweigische Maschinenbauanstalt AG Dispositif de séchage par vaporisation du lit fluidisé

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3663687B1 (fr) * 2018-12-05 2024-01-24 ED-IPR ApS Appareil, composant de plaque inférieure et procédé de séchage de matière particulaire en vrac

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EP2457649A1 (fr) 2010-11-25 2012-05-30 BMA Braunschweigische Maschinenbauanstalt AG Installation à lit fluidisé et procédé de fonctionnement d'une installation à lit fluidisé

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Publication number Priority date Publication date Assignee Title
AT345769B (de) 1976-08-18 1978-10-10 Waagner Biro Ag Verfahren zur trocknung und vorerhitzung der kohle und einrichtung zur durchfuehrung des verfahrens
EP0058651A1 (fr) 1981-02-11 1982-08-25 Svensk Exergiteknik AB Méthode pour fabriquer le fourrage de boeuf et usine pour exécuter la méthode
EP0153704A2 (fr) 1984-02-24 1985-09-04 Aktieselskabet De Danske Sukkerfabrikker Procédé et dispositif pour l'enlèvement d'un liquide d'une matière solide en particules
US4813155A (en) 1984-02-24 1989-03-21 Aktieselskabet De Danske Sukkerfabrikker Process and apparatus for removal of liquid from a solid particulate material
US4602438A (en) 1985-04-26 1986-07-29 Westinghouse Electric Corp. Method and apparatus for fluidized steam drying of low rank coals with wet scrubbing
EP0268819A2 (fr) 1986-11-27 1988-06-01 Uhde GmbH Procédé et dispositif pour le conditionnement de matériel en vrac
US5199184A (en) * 1988-05-09 1993-04-06 Buhler Ag Fluidized-bed or effervescent bed chamber, treatment tower and process in two stages
WO1992001200A1 (fr) 1990-07-09 1992-01-23 Niro A/S Appareil de sechage par vapeur surchauffee d'un materiau particulaire humide
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EP0819904A1 (fr) * 1996-07-17 1998-01-21 GEA Wärme- und Umwelttechnik GmbH Installation de séchage à vapeur à lit fluidisé
US6154979A (en) 1998-01-09 2000-12-05 Asj Holding Aps Method and apparatus for the removal of liquid from particulate material
EP1044044A1 (fr) 1998-01-09 2000-10-18 ASJ Holding ApS Procede et appareil servant a extraire un liquide d'une matiere particulaire
US6438863B1 (en) 1998-04-06 2002-08-27 Asj Holding Aps Apparatus for the drying of moist particulate material in superheated steam
EP1070223A1 (fr) 1998-04-06 2001-01-24 ASJ Holding ApS Appareil de sechage de la matiere particulaire humide contenue dans une vapeur surchauffee
US6266895B1 (en) 1998-05-07 2001-07-31 Asj Holding Aps Apparatus for the drying of moist particulate material in superheated steam
EP0955511A2 (fr) 1998-05-07 1999-11-10 ASJ Holding ApS Appareil pour le séchage d'un matériau particulaire humide par vapeur surchauffée
US6966466B2 (en) 2003-11-07 2005-11-22 Asj Holding Aps Rotary airlock valve
US7578073B2 (en) 2007-02-09 2009-08-25 Braunschweigische Maschinenbauanstalt Ag Appliance for removing fluids and/or solids
EP1956326B1 (fr) 2007-02-09 2010-04-14 Braunschweigische Maschinenbauanstalt AG Dispositif de suppression de fluides et/ou de substances solides
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WO2010139331A2 (fr) 2009-06-03 2010-12-09 Asj Holding Aps Système et procédé pour l'élimination d'une matière solide particulaire à partir d'un contenant sous pression contenant un gaz, et leur utilisation
EP2457649A1 (fr) 2010-11-25 2012-05-30 BMA Braunschweigische Maschinenbauanstalt AG Installation à lit fluidisé et procédé de fonctionnement d'une installation à lit fluidisé

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3486591B1 (fr) 2014-04-30 2020-06-17 BMA Braunschweigische Maschinenbauanstalt AG Dispositif de séchage par vaporisation du lit fluidisé

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EP3351884A1 (fr) 2018-07-25
EP3009777A1 (fr) 2016-04-20
EP3550242C0 (fr) 2023-09-27
DE202015009713U1 (de) 2019-06-07
DE202015009570U1 (de) 2018-05-04
EP3550242B1 (fr) 2023-09-27
PL3550242T3 (pl) 2024-03-18
PL3009777T3 (pl) 2018-08-31
RS64984B1 (sr) 2024-01-31
EP3550242A1 (fr) 2019-10-09
EP3009777B1 (fr) 2018-04-04
TR201808829T4 (tr) 2018-07-23

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