EP3137832A1 - Sécheuse à vapeur à lit fluidisé - Google Patents

Sécheuse à vapeur à lit fluidisé

Info

Publication number
EP3137832A1
EP3137832A1 EP15710008.2A EP15710008A EP3137832A1 EP 3137832 A1 EP3137832 A1 EP 3137832A1 EP 15710008 A EP15710008 A EP 15710008A EP 3137832 A1 EP3137832 A1 EP 3137832A1
Authority
EP
European Patent Office
Prior art keywords
cell
flow
mixture
inlet
outlet
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
EP15710008.2A
Other languages
German (de)
English (en)
Other versions
EP3137832B1 (fr
Inventor
Gerald Caspers
Hartmut Hafemann
Carsten BONATH
Holger Fersterra
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.)
BMA Braunschweigische Maschinenbauanstalt AG
Original Assignee
BMA Braunschweigische Maschinenbauanstalt 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
Family has litigation
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Application filed by BMA Braunschweigische Maschinenbauanstalt AG filed Critical BMA Braunschweigische Maschinenbauanstalt AG
Priority to EP18214410.5A priority Critical patent/EP3486591B1/fr
Priority to PL15710008T priority patent/PL3137832T3/pl
Priority to DK18214410.5T priority patent/DK3486591T3/da
Publication of EP3137832A1 publication Critical patent/EP3137832A1/fr
Application granted granted Critical
Publication of EP3137832B1 publication Critical patent/EP3137832B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • F26B17/107—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 pneumatically inducing within the drying enclosure a curved flow path, e.g. circular, spiral, helical; Cyclone or Vortex dryers
    • 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
    • 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
    • F26B17/103—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 specific material feeding arrangements, e.g. combined with disintegrating means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/005—Treatment of dryer exhaust gases
    • F26B25/007—Dust filtering; Exhaust dust filters
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/02—Applications of driving mechanisms, not covered by another subclass

Definitions

  • the invention relates to a device for removing fluids and / or solids from a mixture of particulate materials with a container forming an annular process space with a plurality of cells separated by walls, comprising an inlet cell, intermediate cells and an outlet cell Introducing the mixture to be treated into the inlet chamber of the process chamber, a discharge device for discharging the treated mixture from the outlet cell of the process chamber, a fan device for supplying a first fluidizing agent, in particular in the form of superheated steam, from below into the process chamber through a distributor plate for producing a Fluidized bed in the process chamber, a heating device for processing the first fluidizing agent in the flow direction in front of the fan device, swirl blades for conditioning the flow in the container from the process chamber to the heating and a part also leads to a steam outlet, and a dedusting device in the flow path between the process chamber and the heating device, wherein dust can be guided to the outlet cell via the dedusting device.
  • a device is particularly suitable for drying bulk materials and materials from the food and
  • Particles entrained by the steam are separated on the way from the process space to a (vapor) discharge using swirl-producing blades and a de-dusting device to then supply the dust-free steam to the process space after re-heating in a heating device via a distributor plate.
  • Such devices are known, for example, from EP 1 956 326 B1, EP 2 146 167 B1, EP 1 070 223 B1, US Pat. No. 5,357,686 and EP 2 457 649 A1.
  • Object of the present invention is therefore to further develop the generic device such that it has a higher reliability.
  • a clumping of material to be dried, ie the mixture of particulate materials, should be substantially avoided. So it should be improved overall flow of the device.
  • This object is achieved according to the invention in that in order to support a transport of the mixture from the inlet cell to the outlet cell and / or a Turbulence of the mixture in the process space of the distributor plate has first unevenness, and / or at least temporarily a second fluidizing agent, in particular in the form of superheated steam, substantially parallel to the distributor plate by means of first nozzles at least in the inlet cell can be fed, and / or first Strömungsleitglieder above the inflow and / or second, Strömungsleitglieder are provided below the inflow floor.
  • a flow guide is realized in the manner of a flow tube, and in the outlet no fluidizing agent passes through the distributor plate.
  • the feed device for the mixture is connected to the container in the region of the inlet cell, preferably in the middle of the height of the inlet cell and / or at the level of the upper extensions of the fluidized bed.
  • the entry device loosened the mixture by a mechanical transport, preferably by means of mechanically acting paddle, in particular a screw conveyor, and / or preheated and / or over
  • Air transport preferably by applying a third fluidizing agent, in particular in the form of superheated steam by steam injection into the
  • Screw conveyor feeding inlet cell
  • the area of the inflow floor in the inlet cell is greater than, preferably twice as large as, the respective area of the inflow base of
  • the inflow base has first openings in the inlet cell and the intermediate cells, the opening ratio of which preferably decreases from the inlet cell in the direction of the outlet cell.
  • Devices according to the invention may be characterized in that the distributor plate has the first unevennesses in the form of recessed recesses and / or at least over the first quarter of the process chamber.
  • the inflow base is inclined at its edge facing the container upwards and otherwise substantially horizontally extending, wherein the edge is preferably provided with first openings and / or first unevenness at least over the first quarter of the process space.
  • the second fluidizing agent can be fed with a pressure of at least 2 bar above the mean pressure in the container and / or in the first quarter of the process space.
  • Shielding of the heating device may be provided, preferably with the shield conically widening from top to bottom in the process space, the first nozzles extending between the shield and the inflow base, and / or the shield having second openings and / or second unevenness, preferably in shape of recessed recesses, has.
  • Inlet cell extends down to the height of the inflow floor, and / or the walls between the inlet cell and a first intermediate cell, between the
  • first flow guide members are provided and / or adjustable between the first nozzles.
  • first second flow guide members are provided in a dished bottom as part of a Nachleitapparats the fan device, wherein preferably the fan device, a fan within the
  • Preferred devices according to the invention are characterized in that second second flow directing members are provided in a dished bottom and / or mounted on the Nachleitapparat and / or adjustable, preferably each about a substantially perpendicular to the distributor plate or vertically extending axis of rotation, are.
  • Verwirbelungsimpulsen is determined or changeable is or are.
  • FIG. 1a shows a perspective side view of a first exemplary embodiment of a device according to the invention
  • Figure lb a schematic representation of the device of Figure la;
  • FIG. 2 shows a longitudinal sectional view of an insertion device of the device according to FIG.
  • FIGS. 3a-3c show perspective partial views of the bottom region of the device according to FIG.
  • Figures 4a and 4b partial perspective views of the underside and top of a
  • FIG. 5a a plan view of a ground area of a second
  • Figure 5b is a partial sectional view of the bottom portion of Figure 5a;
  • FIG. 5c a view like FIG. 5a with additional, adjustable
  • FIG. 5d shows a perspective partial view of the bottom region of FIG. 5c
  • Figure 6 a perspective view of the bottom portion of a third
  • FIGS. 1 a and 1 b show a device according to the invention in the form of a fluidized-bed evaporator dryer 1000 with an introduction device 1 for introducing material to be dried in the form of pressed pulp into a container 21 which has a process space 23 in the region of its bottom 22. More specifically, the pulp is introduced into the process space 23 in which a fluidized bed 2 can be generated by flowing a superheated steam inflow floor 24 to dry the pulp.
  • Dried pulp can then be discharged from the container 21 by means of a discharge device 3, while particles entrained by the vapor from the process space 23 are separated within the container 21, inter alia by means of a dust collector 4 above the fluidized bed 2.
  • the vapor freed of particles finally passes in part to a steam outlet 5 and partly to a heating device to be reheated by means of a heater 6, so that it again with the interposition of a fan device or a blower 7 the process chamber 23 through the distributor plate 24 can be fed therethrough.
  • a discharge device 3 to discharge a discharge device 3
  • the vapor freed of particles finally passes in part to a steam outlet 5 and partly to a heating device to be reheated by means of a heater 6, so that it again with the interposition of a fan device or a blower 7 the process chamber 23 through the distributor plate 24 can be fed therethrough.
  • walls 25 are arranged vertically aligned and extend substantially from an outer wall of the heater 6 to a wall of the container 21 to form cells between them in the process space 23.
  • the walls 25 may extend down to the inflow base 24, but then have to have openings or form a space between them and the inflow base 24.
  • the cells formed by the walls 25 are open at the top, so that the steam serving as the fluidizing agent flows through the cells from bottom to top and entrains the material or particles to be treated and optionally transports them to a downstream cell.
  • the expansion cone 26 there is a reduction in the flow rate, which leads to a broadening of the flow of steam from the cells.
  • the expansion cone 26 and an upper region 27 adjoining the same have no internals, ie they provide a free space in which, with the separation of particles, the flows spread out of the cells and at least partially intermix.
  • superheated steam is blown into the upper region 27 via nozzles 34 and 35.
  • Separated particles are discharged vertically along the wall in the expansion cone 26 via ribs 36, while the rest of the particles enter together with the steam in a central separator in the form of the dust collector 4 in the lid 28 of the container.
  • the ribs 36 thereby ensure a deceleration of the particles, which promotes the deposition.
  • the inner contour of the lid 28 is formed to deflect the flow.
  • the separation of smaller particles takes place by flowing the particle vapor mixture into the dust collector 4. Finally, the separated dust passes through a dust cyclone 33 into an outlet cell 202 in the process space 23.
  • the entry device 1 introduces the pulp to be treated into a first cell into the process space 23, which is referred to below as the inlet cell 201.
  • the last cell or outlet cell 202 provided with the discharge device 3 is not or only to a small extent flowed through by the fluidizing agent, so that material entering the cell 202 from above or at the inlet bottom 24 reaches the bottom region and via the discharge device 3 , in particular as described in EP 214667 Bl, can be removed.
  • a process control according to EP 2 457 649 AI can be used.
  • the inserter 1 is arranged to introduce the pulp into the center of the inlet cell 201, at the level of the upper extensions of the fluidized bed 2, which is a lower installation than known devices. In addition, it ensures that the pulp loosens and preheated in the inlet cell 201 passes.
  • it comprises a screw conveyor 400 with rotatable paddles 401, as shown in FIG.
  • wet material that is to say pulp to be dried, is supplied and immediately supplied with steam from a first steam feed 403, and comminution of clumped pulp takes place by mechanical energy input of the rotating paddle 401.
  • the pulp is also transported and again supplied with steam from second steam feeders 404 and 405 during the transport.
  • the screw conveyor 400 is attached to the container 21 via a docking area 406 and causes the pulp to be preheated and released into the inlet cell 201 along with an excess amount of vapor immediately escaping upwardly in the container 21.
  • the inlet cell 201 preferably covers a larger area of the inflow bottom 24 than any of the remaining cells, so that the supplied pulp is brought into contact with an increased amount of steam on an increased bottom area, which also counteracts lumping acts. Because in the inlet cell 201, the pulp is still the wettest. Doubling the size of the inlet cell 201 from the rest of the cell has been found to be particularly good.
  • the flow from the inlet cell 201 to the outlet cell 202 is conditioned via a plurality of flow directors to further counteract agglomeration, as will be described below with reference to Figs. 3a to 3c, 4a and 4b.
  • An apron 300 bounds the annular process space 23 inwards.
  • a steam supply pipe 301 opens above the inflow bottom 24 to supply steam to at least a first quarter of the cells across the inflow base 24 via nozzles 302, as shown in Figure 3a.
  • the steam supply pipe 301 is disposed in the annular portion of the inlet cell 201 to provide there increasingly with transverse steam for loosening, since there also the pulp still carries the largest amount of water.
  • guide plates 303 are disposed between the nozzles 302 to ensure the transverse flow in each cell. The nozzles 302 and the guide plates 303 thus provide flow directing members, with the addition of steam via the nozzles 302 in addition to heating and water evaporation from the pulp.
  • the inflow base 24 and the skirt 300 are formed with perforated plates 304a, 304b and 305, respectively, for guiding the flow in a targeted manner.
  • all the perforated plates 304a, 304b and 305 have holes for the passage of superheated steam, while some of these perforated plates, namely the perforated plates 304b and 305, also have unevennesses for guiding said vapor.
  • the perforated plates 305 of the skirt 300 support a flow along the skirt 300 down to the inflow base 24, see the flow lines 310, while the perforated plates 304b support a flow along the flow lines 312 as an extension of the flow line 311, so that a circular flow in the fluidized bed 2 in substantially perpendicular to the distributor plate 24, namely from the skirt 300 via the distributor plate 24 back to the skirt 300th is enforced.
  • a further circular flow of the same direction of rotation is enforced by not shown perforated plates with unevenness in a direction of the open ends of the cells upwardly inclined floor extension, which forms a wall of the container 21 contacting edge 307 of FIG 3b, namely along the inflow floor 24, Rands 307 and the wall back to the distributor plate 24th
  • the nozzles 302, guide plates 303 and perforated plates 304a, 304b and 305 may differ for each cell to account for the progressing drying of the pulp.
  • the opening ratio of the perforated plates 304a to 305 from the inlet cell 201 to the outlet cell 202 becomes smaller.
  • FIGS. 4a and 4b show by way of example a perforated plate 304b which has a multiplicity of holes 341 and flakes 342. More specifically, Figure 4a shows a bottom 343 on which the perforated plate 403b in the region of the flakes 342 each has a large opening for superheated steam, which leads to a bump on the top 344 shown in Figure 4b, and thus the superheated steam can be provided with a directional pulse.
  • Many different geometric designs are conceivable; It is also conceivable that the flow lines 312 shown in FIGS. 3b and 3c do not run exactly radially, but are inclined in the direction of the flow lines 313 so as to serve for transporting the pulp.
  • the fan 7, which is provided according to Figure la within a dished bottom 22 a of the bottom 22, serves to convey superheated steam from the heater 6, which is often referred to as the vapor stream and which allows fluidization in the fluidized bed 2.
  • the need for vapors or drying vapors in the individual cells of the process space 23 is different, since the pulp to be dried from the inlet cell 201 in the direction of the outlet cell 202 loses moisture. Since the vapor stream enters the individual cells via the distributor plate 24 substantially in parallel via the fan 7, the vapor is distributed in accordance with the pressure loss which arises when the individual cells flow. This pressure loss is primarily influenced by the pressure loss of the inflow base 24 and the overlying mass of the fluidized bed 2.
  • both the transport and the turbulence and thus drying can be influenced.
  • the holes 341 and flakes 342 in the perforated plates 304a, 304b, and 305 as well as the guide plates 303 are fixedly installed in the fluidized bed dryer 1000. In the following, an alternative construction will be described with reference to FIGS. 5a-5d.
  • FIG. 5a shows a plan view of a dished bottom 22'a of a second exemplary embodiment of a fluidized-bed evaporation dryer in which, in addition to a fan 7 ', a plurality of baffles 501 of a Nachleitapparats 500 are arranged, which serve to condition the flow in the dished bottom 22'a, namely for guiding said flow radially outwards, as represented by the flow paths A in FIG. 5a.
  • the Nachleitapparat 500 includes further baffles 502 and 503 with different orientations, as best shown in Figure 5b, which is a partial perspective of the area below a Incoming bottom 24 'within a bottom 22' with the dished bottom 22'a shows.
  • FIG. 5b is a partial perspective of the area below a Incoming bottom 24 'within a bottom 22' with the dished bottom 22'a shows.
  • FIG. 5b also shows a distributor plate support member 24'a, along which the flow conditioned by the guide device 500 ascends according to the flow path B, and either through openings in the substantially horizontally extending distributor plate 24 'or inclined to the wall of the bottom 22' Edge 240 'to get into the process space or in the region of the bottom 22' below the inflow base 24 'is circulated.
  • each adjustable guide plate 600 is rotatable about an axis of rotation 601 via an adjusting device 602.
  • the adjusting device 602 can be adjusted either manually in the case of the opening of the fluidized bed evaporator dryer according to the invention, or else from outside the fluidized bed evaporator, even in the drying operation thereof.
  • adjustable baffles 700 can be arranged directly underneath the baffle bottom. This is shown in Figure 6 in a perspective view, according to which are arranged substantially parallel to the distributor plate 24 "the adjustable baffles 700 in the area of Anströmm Camillstützgliedern 24" b, namely about an axis of rotation 701 rotatable, as indicated by the arrow F.
  • the inflow base support members 24 "b are in turn supported by the inflow base support members 24" a, which are secured to the wall of the floor.
  • FIGS. 7a and 7b show the flow path G or G 'through the individual openings in a distributor plate 24 "', which has an effect on the solids transport path H or H 'within the fluidized bed 2''.'
  • FIGS. 7a and 7b show the flow path G or G 'through the individual openings in a distributor plate 24 "', which has an effect on the solids transport path H or H 'within the fluidized bed 2''.'
  • a flow path G according to FIG '' to an increased transport within the fluidized bed 2 ''
  • a flow path G 'according to Figure 7b steeper through the inflow base 24 "' passes and thus provides for increased turbulence in the fluidized bed 2"'.
  • adjustable baffles 600 and 700 can be combined with special perforated plate designs as well as guide plates above the inflow floor. Such a combination provides a precise adjustment of the flow needed for the particular pulp to optimize drying from an inlet cell to an outlet cell.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Drying Of Solid Materials (AREA)

Abstract

L'invention concerne un dispositif (1000) permettant d'enlever des substances solides et/ou des fluides présents dans un mélange de matériaux particulaires, comprenant un réservoir (21) qui forme une chambre de traitement annulaire (23) comportant une pluralité de cellules séparées par des parois (25), dont une cellule d'entrée (201), des cellules intermédiaires et une cellule de sortie (202), un dispositif d'introduction permettant d'introduire le mélange à traiter dans la cellule d'entrée (201) de la chambre de traitement (23), un dispositif d'évacuation (3) permettant d'évacuer le mélange à traiter de la cellule de sortie (202) de la chambre de traitement (23), un dispositif de ventilation (7, 7') servant à l'amenée par le bas dans la chambre de traitement (23) en traversant un fond d'écoulement (24, 24´, 24´´, 24´´´) d'un premier agent de fluidisation, en particulier sous la forme de vapeur surchauffée, pour la production d'un lit fluidisé (2) dans la chambre de traitement (23), un dispositif de chauffage (6) servant à préparer le premier agent de fluidisation en amont du dispositif de ventilation (7, 7') dans le sens de l'écoulement, des aubes de turbulence (29) servant au conditionnement de l'écoulement (110-160) dans le réservoir à partir de la chambre de traitement (23) vers le dispositif de chauffage (6) et en partie vers une sortie de vapeur (5), et un dispositif de dépoussiérage (4) sur le trajet d'écoulement entre la chambre de traitement (23) et le dispositif de chauffage (6), la poussière pouvant être dirigée par le dispositif de dépoussiérage (4) vers la cellule de sortie (202). Pour favoriser le transport du mélange de la cellule d'entrée (201) vers la cellule de sortie (202) et/ou une mise en turbulence du mélange dans la chambre de traitement (23), le fond d'écoulement (24) présente de premières irrégularités (342) et/ou un deuxième agent de fluidisation, en particulier sous la forme de vapeur surchauffée, peut au moins par moments être introduit au moins dans la cellule d'entrée (201) sensiblement parallèlement au fond d'écoulement (24) au moyen de premières buses (302), et/ou de premiers éléments de guidage de l'écoulement (303) sont placés au-dessus du fond d'écoulement (24) et/ou de deuxièmes éléments de guidage de l'écoulement (501, 502, 503, 600, 700) sont placés au-dessous du fond d'écoulement (24´, 24´´, 24´´´´).
EP15710008.2A 2014-04-30 2015-03-09 Sécheuse à vapeur à lit fluidisé Active EP3137832B1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
EP18214410.5A EP3486591B1 (fr) 2014-04-30 2015-03-09 Dispositif de séchage par vaporisation du lit fluidisé
PL15710008T PL3137832T3 (pl) 2014-04-30 2015-03-09 Suszarka z odparowaniem w złożu fluidalnym
DK18214410.5T DK3486591T3 (da) 2014-04-30 2015-03-09 Fluid bed-fordampningstørrer

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102014106122.5A DE102014106122A1 (de) 2014-04-30 2014-04-30 Wirbelschichtverdampfungstrockner
PCT/IB2015/051707 WO2015166358A1 (fr) 2014-04-30 2015-03-09 Sécheuse à vapeur à lit fluidisé

Related Child Applications (2)

Application Number Title Priority Date Filing Date
EP18214410.5A Division-Into EP3486591B1 (fr) 2014-04-30 2015-03-09 Dispositif de séchage par vaporisation du lit fluidisé
EP18214410.5A Division EP3486591B1 (fr) 2014-04-30 2015-03-09 Dispositif de séchage par vaporisation du lit fluidisé

Publications (2)

Publication Number Publication Date
EP3137832A1 true EP3137832A1 (fr) 2017-03-08
EP3137832B1 EP3137832B1 (fr) 2019-08-14

Family

ID=52682789

Family Applications (2)

Application Number Title Priority Date Filing Date
EP18214410.5A Active EP3486591B1 (fr) 2014-04-30 2015-03-09 Dispositif de séchage par vaporisation du lit fluidisé
EP15710008.2A Active EP3137832B1 (fr) 2014-04-30 2015-03-09 Sécheuse à vapeur à lit fluidisé

Family Applications Before (1)

Application Number Title Priority Date Filing Date
EP18214410.5A Active EP3486591B1 (fr) 2014-04-30 2015-03-09 Dispositif de séchage par vaporisation du lit fluidisé

Country Status (8)

Country Link
US (1) US10330385B2 (fr)
EP (2) EP3486591B1 (fr)
DE (1) DE102014106122A1 (fr)
DK (2) DK3486591T3 (fr)
PL (1) PL3137832T3 (fr)
RU (1) RU2673041C2 (fr)
UA (1) UA120365C2 (fr)
WO (1) WO2015166358A1 (fr)

Cited By (2)

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Publication number Priority date Publication date Assignee Title
EP3351884A1 (fr) * 2014-10-15 2018-07-25 ASJ-IPR ApS Appareil et procédé de séchage de matière particulaire en vrac
CN108917368A (zh) * 2018-04-30 2018-11-30 中山市加丰机械科技有限公司 一种用作饲料的玉米颗粒除屑烘干装置

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DE102014106122A1 (de) 2014-04-30 2015-11-05 Bma Braunschweigische Maschinenbauanstalt Ag Wirbelschichtverdampfungstrockner
EP3582887B1 (fr) * 2017-02-20 2023-08-09 Nous, Llc Système à lit fluidisé
CN107702474A (zh) * 2017-10-20 2018-02-16 张家港大塚化学有限公司 低粉尘的桨叶式干燥机
CN110064528B (zh) * 2019-05-07 2020-03-17 中国矿业大学 一种用于干燥分选矿物的干法提质系统及提质方法
CN111617878B (zh) * 2020-05-12 2021-11-16 路德环境科技股份有限公司 一种适用于连续流化床烘干过程的除杂装置
CN111964364B (zh) * 2020-08-24 2022-06-10 哈尔滨昂农科技有限公司 拆分式粮食烘干设备
CN112033141A (zh) * 2020-08-31 2020-12-04 王寅 一种粉料干燥用放料装置
CN117284650B (zh) * 2023-11-24 2024-02-23 江苏扬子催化剂有限公司 一种催化剂载体加湿料仓

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EP3550242A1 (fr) * 2014-10-15 2019-10-09 ASJ-IPR ApS Appareil et procédé de séchage de matière particulaire en vrac
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DK3486591T3 (da) 2020-08-31
DK3137832T3 (da) 2019-11-18
US10330385B2 (en) 2019-06-25
EP3137832B1 (fr) 2019-08-14
UA120365C2 (uk) 2019-11-25
EP3486591A1 (fr) 2019-05-22
US20170045293A1 (en) 2017-02-16
RU2016146789A (ru) 2018-05-30
EP3486591B1 (fr) 2020-06-17
RU2016146789A3 (fr) 2018-05-30
PL3137832T3 (pl) 2020-04-30
RU2673041C2 (ru) 2018-11-21
DE102014106122A1 (de) 2015-11-05

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