EP3486591B1 - Wirbelschichtverdampfungstrockner - Google Patents

Wirbelschichtverdampfungstrockner Download PDF

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Publication number
EP3486591B1
EP3486591B1 EP18214410.5A EP18214410A EP3486591B1 EP 3486591 B1 EP3486591 B1 EP 3486591B1 EP 18214410 A EP18214410 A EP 18214410A EP 3486591 B1 EP3486591 B1 EP 3486591B1
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EP
European Patent Office
Prior art keywords
cell
flow
inflow bottom
process chamber
inflow
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EP18214410.5A
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German (de)
English (en)
French (fr)
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EP3486591A1 (de
Inventor
Gerald Caspers
Hartmut Hafemann
Carsten BONATH
Holger Fersterra
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BMA Braunschweigische Maschinenbauanstalt AG
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BMA Braunschweigische Maschinenbauanstalt AG
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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 which forms an annular process space with a plurality of cells separated by walls, comprising an inlet cell, intermediate cells and an outlet cell, an entry device for Introducing the batch to be treated into the inlet cell of the process space, a discharge device for discharging the treated batch from the outlet cell of the process space, a fan device for supplying a first fluidizing agent, in particular in the form of superheated steam, from below into the process space through an inflow floor to generate a Fluidized bed in the process space, a heating device for processing the first fluidizing agent in the flow direction upstream of the fan device, swirl vanes for conditioning the flow in the container from the process room to the heating device g and in part also leads to a steam outlet, and a dedusting device in the flow path between the process space 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
  • a large number of devices of the type mentioned are known from the prior art, which generally use superheated steam as a fluidizing agent. These so-called fluidized bed evaporation dryers are used to flow through and fluidize bulk material or particulate materials from below with superheated steam, so that a fluidized bed is created.
  • the material to be treated is conveyed from an entry cell, in which the material to be treated is introduced into the container and the process space, via subsequent process cells to a discharge cell. Takes place in the discharge cell no inflow from below, so that the finished material can be discharged at the lower end of the discharge cell, for example via a discharge screw.
  • the container is sealed at the discharge end as well as at the entry device by means of a lock device in order to allow the machining process to take place under excess pressure.
  • Particles entrained by the steam are separated on the way from the process room to a (steam) discharge using swirl-generating blades and a dedusting device, in order to then feed the dust-free steam to the process room after reheating in a heating device via an inflow floor.
  • Such facilities are from, for example EP 1 956 326 B1 , EP 2 146 167 B1 , EP 1 070 223 B1 , US 5,357,686 A , EP 0 153 704 A2 and the EP 2 457 649 A1 known.
  • This object is achieved according to the invention in that, in order to support a transport of the batch from the inlet cell to the outlet cell and / or a swirling of the batch in the process space of the inflow floor, has first unevenness, and / or at least temporarily a second fluidizing agent, in particular in the form of superheated steam , essentially parallel to the inflow floor by means of first nozzles at least in the Inlet cell can be fed, and / or first flow guide members above the inflow floor and / or second, flow guide members below the inflow floor are provided.
  • the area of the inflow floor in the inlet cell is larger than, preferably twice as large, the respective area of the inflow floor of the intermediate cells.
  • the feed device for the batch 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 height of the upper extensions of the fluidized bed.
  • the feed device loosens the batch by mechanical transport, preferably by means of mechanically acting paddles, in particular a screw conveyor, and / or preheated and / or via
  • Flight transport preferably by supplying it with a third fluidizing agent, in particular in the form of superheated steam by steam injection into the screw conveyor, which feeds the inlet cell.
  • a third fluidizing agent in particular in the form of superheated steam by steam injection into the screw conveyor, which feeds the inlet cell.
  • the inflow floor 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 can be characterized in that the inflow floor has the first unevenness in the form of recessed recesses and / or at least over the first quarter of the process space.
  • the inflow base be inclined upward at its edge facing the container and otherwise be essentially horizontal, the edge preferably being 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 in at a pressure of at least 2 bar above the mean pressure in the container and / or in the first quarter of the process space.
  • a shielding of the heating device can be provided, the shielding preferably expanding conically in the process space from top to bottom, the first nozzles extending between the shielding and the inflow floor, and / or the shielding second openings and / or second bumps, preferably in the form of recessed recesses.
  • the wall between the outlet cell and the inlet cell extends down to the level of the inflow floor, and / or the walls between the inlet cell and a first intermediate cell, between the intermediate cells and between the last intermediate cell and the outlet cell a vertical Have a distance to the inflow floor, in particular to the edge of the inflow floor.
  • first flow guide members are provided and / or adjustable between the first nozzles.
  • first second flow guide members are provided in a dished end as part of a follow-up device of the fan device, the fan device preferably comprising a blower within the follow-up device.
  • Preferred devices according to the invention are characterized in that second second flow guide members are provided in a dished end and / or are attached and / or adjustable on the guide apparatus, preferably each being rotatable about an axis of rotation that extends essentially perpendicular to the inflow floor or vertically.
  • third second flow guide members are attached to and / or adjustable on the inflow floor support members, preferably in each case rotatable about an axis of rotation extending essentially parallel to the inflow floor or horizontally.
  • the number, orientation and / or arrangement of the first and / or second openings, the first and / or second bumps, the first nozzles and / or the first and / or second flow guide members for the targeted application of horizontal to the batch Transport pulses in the direction of the outlet cell and / or vertical swirling pulses is determined or can be changed.
  • orientation in particular the second second and / or third second flow guide members, and / or the supply from the second fluidization means to the first nozzles can be changed via an adjustment device that can be operated from outside the container.
  • FIGS. 1a and 1b show a device according to the invention in the form of a fluidized bed evaporation dryer 1000 with an entry 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 precisely, the pulp is introduced into the process space 23, in which a fluidized bed 2 can be produced by flowing an inflow base 24 with superheated steam to dry the pulp. Dried pulp can then be discharged from the container 21 by means of a discharge device 3, while particles entrained in the steam from the process space 23 within the container 21 are separated off, inter alia by means of a dust collector 4 above the fluidized bed 2.
  • the particle-freed steam finally arrives in part to a steam outlet 5 and partly to a heating device in order to be overheated again by means of a heater 6, so that it can be fed again to the process space 23 through the inflow floor 24 with the interposition of a fan device or a blower 7. This results in a closed circuit of part of the steam.
  • walls 25 are arranged vertically aligned and extend essentially from an outer wall of the heater 6 to a wall of the container 21 in order to form cells between them in the process space 23.
  • the walls 25 can extend down to the inflow floor 24, but must then have openings or form a free space between them and the inflow floor 24.
  • the cells formed by the walls 25 are open at the top, so that the vapor serving as the fluidizing agent flows from bottom to top through the cells and entrains the material or particles to be treated and, if necessary, transports them into a downstream cell.
  • a first swirl is generated between the process space 23 and an expansion cone 26 via blades 29 above the walls 25.
  • the vertical flow of the steam in the process space 23 is thereby deflected in order to lead to a swirl flow in the expansion cone 26. Due to the swirl the steam together with the entrained particles are thus directed onto the wall of the container 21, which causes the particles to slow down, namely by wall friction, so that the braked particles then fall back along the wall into the process space 23.
  • the expansion cone 26 there is a decrease in the flow speed, which leads to a broadening of the steam flow out of the cells.
  • the expansion cone 26 and an upper region 27 adjoining the same have no internals, that is to say represent a free space in which, with the separation of particles, the flows from the cells spread apart and at least partially mix.
  • 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 together with the steam enter a central separator in the form of the dust collector 4 in the lid 28 of the container.
  • the ribs 36 ensure that the particles are decelerated, which promotes separation.
  • the inner contour of the cover 28 is shaped to deflect the flow.
  • the entry device 1 enters the pulp to be treated into a first cell in the process space 23, which is referred to below as the inlet cell 201.
  • the fluidizing agent does not flow through the last cell or outlet cell 202 provided with the discharge device 3 or only to a small extent, so that material entering this cell 202 from above or along the inflow floor 24 reaches the bottom area and via the discharge device 3 , especially as in the EP 2 146 167 B1 described, can be removed.
  • a process control according to the EP 2 457 649 A1 be used.
  • the feed device 1 is arranged in such a way that it brings the pulp into the middle of the inlet cell 201, at the level of the upper extensions of the fluidized bed 2, which represents a lower installation than known devices. In addition, it ensures that the pulp is loosened and preheated into the inlet cell 201.
  • it comprises a screw conveyor 400 with rotatable paddles 401, as in FIG Figure 2 shown.
  • a feed area 402 wet material, that is to say pulp to be dried, is fed in and steam is applied directly from a first steam feed 403, and clumped pulp is comminuted by mechanical energy input from the rotating paddles 401.
  • the screw conveyor 400 is attached to the container 21 via a docking area 406 and ensures that the pulp is preheated and loosened together with an excess amount of steam that immediately escapes upwards in the container 21 into the inlet cell 201.
  • the inlet cell 201 preferably covers a larger area of the inflow base 24 than each of the remaining cells, so that the supplied pulp is brought into contact with an increased amount of steam on an enlarged floor area, which also counteracts clumping works. Because in the inlet cell 201, the pulp is still the wettest. A doubling of the size of the inlet cell 201 compared to the rest of the cell has proven 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 clumping, as described below with respect to FIG Figures 3a to 3c , 4a and 4b is described.
  • An apron 300 delimits the annular process space 23 to the inside.
  • a steam supply pipe 301 opens above the inflow base 24 between the apron 300 and the heater 6 in order to supply steam via nozzles 302 to at least a first quarter of the cells across the inflow base 24, as in FIG Figure 3a shown. This leads to a flow from the apron 300 radially to the wall of the container 21, see flow lines 311.
  • the steam supply pipe 301 is arranged in the ring section of the inlet cell 201 in order to loosen up there increasingly with transverse steam, since the pulp there too still carries the largest amount of water.
  • guide plates 303 are arranged between the nozzles 302 to ensure the cross flow in each cell. The nozzles 302 and the guide plates 303 thus represent flow directors, the steam supply via the nozzles 302 additionally leading to heating and water evaporation from the pulp.
  • the inflow base 24 and the apron 300 are formed with perforated plates 304a, 304b and 305 in order to guide the flow in a targeted manner. All perforated plates 304a, 304b and 305 have holes for the passage of superheated steam, while some of these perforated plates, namely perforated plates 304b and 305, also have unevenness for guiding said steam.
  • the perforated plates 305 of the apron 300 support a flow along the apron 300 down to the inflow floor 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 im substantially perpendicular to the inflow floor 24, namely from the apron 300 via the inflow floor 24 back to the apron 300 is enforced.
  • a further circular flow of the same direction of rotation is caused by perforated plates (not shown) with unevenness in a base extension which is inclined upward in the direction of the open ends of the cells and which corresponds to an edge 307 contacting the wall of the container 21
  • Figure 3b represents, namely, along the inflow floor 24, the edge 307 and the wall back to the inflow floor 24.
  • a transport area 306 runs between the perforated plate 304b and the edge 307 and thus between the two vertical, same-directional circular flows, which ensures a horizontal circular path from the inlet cell 201 to the outlet cell 202 for conveying the pulp in the process space 23.
  • the nozzles 302, guide plates 303 and perforated plates 304a, 304b and 305 can differ for each cell in order to take into account the progressive 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.
  • the Figures 4a and 4b show, by way of example, a perforated plate 304b which has a multiplicity of holes 341 and scales 342. Specifically shows Figure 4a a lower side 343, on which the perforated plate 403b in the area of the scales 342 each has a large opening for superheated steam, which is in an unevenness on the upper side 344, the in Figure 4b is shown, leads and can thus provide the superheated steam with a directional pulse.
  • Many different geometrical designs are conceivable; it is also conceivable that the in the Figures 3b and 3c
  • the flow lines 312 shown do not run exactly radially, but are inclined in the direction of the flow lines 313 so as to serve to transport the pulp.
  • the fan 7, which is provided according to FIG. 1 a within a dished bottom 22 a of the bottom 22, serves to convey superheated steam from the heater 6, which is often also referred to as a vapor stream and which enables fluidization in the fluidized bed 2.
  • the need for vapor flow or drying vapor in the individual cells of the process space 23 is different, since the pulp to be dried loses moisture from the inlet cell 201 in the direction of the outlet cell 202. Since the vapor stream enters the individual cells via the inflow floor 24 essentially in parallel via the blower 7, the vapor is distributed in accordance with the pressure loss which arises when the individual cells are supplied with flow. This pressure loss is primarily influenced by the pressure loss of the inflow floor 24 and the mass of the fluidized bed 2 located above it.
  • the pulp not only has to be dried in the process space 23, but at the same time as drying it has to be transported from the inlet cell 201 to the outlet cell 202.
  • Both the transport and the swirling and thus drying can be influenced by a targeted selection of the number, orientation and / or arrangement of the holes 341, the scales 342, the nozzles 302 and the guide plates 303.
  • the holes 341 and scales 342 in the perforated plates 304a, 304b and 305 as well as the guide plates 303 are permanently installed in the fluidized bed evaporation dryer 1000. The following is an alternative structure for this with reference to the Figures 5a - 5d described.
  • FIG. 5a shows a top view of a dished end 22'a of a second exemplary embodiment of a fluidized bed evaporation dryer according to the invention, in which, in addition to a blower 7 ', a plurality of baffles 501 of a secondary diverter 500 are arranged, which are used to condition the flow in the dished end 22'a, namely for guiding said flow radially outward, as through the flow paths A in Figure 5a shown.
  • the guide apparatus 500 comprises further baffles 502 and 503 with different orientations, as best shown in FIG Figure 5b shown, which is a partial perspective of the area below a Inflow floor 24 'within a floor 22' with the dished bottom 22'a.
  • FIG. 5b An inflow base support member 24'a is also shown, along which the flow conditioned by the after-directing apparatus 500 rises in accordance with the flow path B, and either through openings in the essentially horizontally extending inflow base 24 'or an edge 240' inclined towards the wall of the base 22 '. for this purpose enters the process space or is circulated in the area of the floor 22 'below the inflow floor 24'.
  • each adjustable baffle 600 can be rotated about an axis of rotation 601 via an adjusting device 602.
  • the adjusting device 602 can either be adjusted manually when the fluidized bed evaporation dryer according to the invention is opened, or else from outside the fluidized bed evaporation dryer, even in the drying operation of the same.
  • adjustable guide plates 700 can be arranged directly below the inflow floor.
  • FIG 6 Shown in a perspective view, according to which the adjustable guide plates 700 are arranged substantially parallel to the inflow base 24 ′′ in the region of the inflow floor support members 24 ′′ b, and can be rotated about an axis of rotation 701, as indicated by the arrow F.
  • the inflow floor support members 24 "b are in turn supported by the inflow floor support members 24" a, which are attached to the wall of the floor.
  • adjustable guide plates 600 and 700 can be combined with special perforated plate designs as well as guide plates above the inflow floor. Such a combination opens up a precise adjustment of the flow required for the respective pulp in order to optimize drying from an inlet cell to an outlet cell.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Drying Of Solid Materials (AREA)
EP18214410.5A 2014-04-30 2015-03-09 Wirbelschichtverdampfungstrockner Active EP3486591B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102014106122.5A DE102014106122A1 (de) 2014-04-30 2014-04-30 Wirbelschichtverdampfungstrockner
EP15710008.2A EP3137832B1 (de) 2014-04-30 2015-03-09 Wirbelschichtverdampfungstrockner
PCT/IB2015/051707 WO2015166358A1 (de) 2014-04-30 2015-03-09 Wirbelschichtverdampfungstrockner

Related Parent Applications (2)

Application Number Title Priority Date Filing Date
EP15710008.2A Division EP3137832B1 (de) 2014-04-30 2015-03-09 Wirbelschichtverdampfungstrockner
EP15710008.2A Division-Into EP3137832B1 (de) 2014-04-30 2015-03-09 Wirbelschichtverdampfungstrockner

Publications (2)

Publication Number Publication Date
EP3486591A1 EP3486591A1 (de) 2019-05-22
EP3486591B1 true EP3486591B1 (de) 2020-06-17

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ID=52682789

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EP18214410.5A Active EP3486591B1 (de) 2014-04-30 2015-03-09 Wirbelschichtverdampfungstrockner
EP15710008.2A Active EP3137832B1 (de) 2014-04-30 2015-03-09 Wirbelschichtverdampfungstrockner

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EP15710008.2A Active EP3137832B1 (de) 2014-04-30 2015-03-09 Wirbelschichtverdampfungstrockner

Country Status (8)

Country Link
US (1) US10330385B2 (pl)
EP (2) EP3486591B1 (pl)
DE (1) DE102014106122A1 (pl)
DK (2) DK3137832T3 (pl)
PL (1) PL3137832T3 (pl)
RU (1) RU2673041C2 (pl)
UA (1) UA120365C2 (pl)
WO (1) WO2015166358A1 (pl)

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DE102014106122A1 (de) 2014-04-30 2015-11-05 Bma Braunschweigische Maschinenbauanstalt Ag Wirbelschichtverdampfungstrockner
EP3009776A1 (en) * 2014-10-15 2016-04-20 ASJ-IPR ApS An apparatus for drying bulk particulate material and a method of drying bulk particulate material
WO2018152471A1 (en) * 2017-02-20 2018-08-23 Nous, Llc Fluidized bed system
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
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
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
DE102024114533A1 (de) 2024-05-23 2025-11-27 Lübbers FTS GmbH Wirbelschichtvorrichtung und Verfahren zum Trocknen und/oder Kühlen eines Gutes und getrocknetes und/oder gekühltes Produkt
CN119015868B (zh) * 2024-09-04 2025-07-11 安庆师范大学 一种化工尾气除杂脱硫用流化床反应器

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Publication number Priority date Publication date Assignee Title
DE102014106122A1 (de) 2014-04-30 2015-11-05 Bma Braunschweigische Maschinenbauanstalt Ag Wirbelschichtverdampfungstrockner
EP3009776A1 (en) 2014-10-15 2016-04-20 ASJ-IPR ApS An apparatus for drying bulk particulate material and a method of drying bulk particulate material

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EP3137832A1 (de) 2017-03-08
US10330385B2 (en) 2019-06-25
PL3137832T3 (pl) 2020-04-30
RU2673041C2 (ru) 2018-11-21
RU2016146789A (ru) 2018-05-30
US20170045293A1 (en) 2017-02-16
DK3137832T3 (da) 2019-11-18
UA120365C2 (uk) 2019-11-25
DE102014106122A1 (de) 2015-11-05
RU2016146789A3 (pl) 2018-05-30
DK3486591T3 (da) 2020-08-31
WO2015166358A1 (de) 2015-11-05
EP3137832B1 (de) 2019-08-14
EP3486591A1 (de) 2019-05-22

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