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EP0039039A1 - Dispositif pour le traitement à chaud, notamment le séchage des matières en vrac pulvérulentes - Google Patents

Dispositif pour le traitement à chaud, notamment le séchage des matières en vrac pulvérulentes Download PDF

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Publication number
EP0039039A1
EP0039039A1 EP81103003A EP81103003A EP0039039A1 EP 0039039 A1 EP0039039 A1 EP 0039039A1 EP 81103003 A EP81103003 A EP 81103003A EP 81103003 A EP81103003 A EP 81103003A EP 0039039 A1 EP0039039 A1 EP 0039039A1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
bulk material
heat
reactor
bed reactor
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
EP81103003A
Other languages
German (de)
English (en)
Other versions
EP0039039B1 (fr
Inventor
Günther Ing. grad. Gappa
Josef Dipl.-Ing. Degel
Harald Prof. Dipl.-Chem. Jüntgen
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.)
Bergwerksverband GmbH
Original Assignee
Bergwerksverband 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 Bergwerksverband GmbH filed Critical Bergwerksverband GmbH
Priority to AT81103003T priority Critical patent/ATE8532T1/de
Publication of EP0039039A1 publication Critical patent/EP0039039A1/fr
Application granted granted Critical
Publication of EP0039039B1 publication Critical patent/EP0039039B1/fr
Expired 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
    • 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
    • F26B3/084—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 with heat exchange taking place in the fluidised bed, e.g. combined direct and indirect heat exchange
    • 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
    • F26B25/04—Agitating, stirring, or scraping devices
    • 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
    • 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
    • F26B3/092—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 agitating the fluidised bed, e.g. by vibrating or pulsating

Definitions

  • the invention relates to a method according to the preamble of claim 1 and an apparatus for performing this method, consisting of a fluidized bed reactor with a feed device and a discharge device for bulk material, a feed device and a discharge device for fluidized gas and a heat source connected to the fluidized bed reactor.
  • the invention is therefore based on the object of providing a method and a device of the type mentioned at the outset which ensure uniform heat treatment, in particular drying, of powders, powders, fine dusts and similar fine-particle bulk materials, with the lowest possible energy consumption and education of hot spots and caking should be avoided so that the overall treatment results are very even.
  • the heat treatments in question can in principle be endothermic or exothermic processes, i. H. that heat is supplied or removed by the heat exchange medium.
  • the fluidizing gas can only be used to maintain fluidizing conditions, but it can also be a reaction partner of a chemical reaction that may take place and finally - and preferably - the heat treatment is supported by the fluidizing gas, i. H. Dissipated heat or - particularly preferably - supplied heat to z. B. to dry the finely divided bulk material in a targeted manner. Drying in the sense of the invention means increasing the moisture content of the bulk material. reduce and thereby bring about the desired residual moisture.
  • finely divided means that the bulk goods have an average grain diameter of generally less than 1 mm, but usually less than 0.1 mm and even less.
  • Fluid bed in the sense of the invention is understood to mean the state of the bulk material particles in which they behave like a liquid in a container.
  • the heat exchange medium according to the invention can be of a recuperative or regenerative type; the latter would be a solid as a heat carrier, which is introduced into the fluidized bed reactor and which is separated from the bulk material again after the heat treatment has taken place.
  • a recuperative heat exchanger is preferred, that of a heat transfer medium fluid is flowing through;
  • the method according to the invention is not subject to any fundamental restrictions. The latter also applies to the fluidizing gas and in particular also to the stirring arm, the design of which relates to the heat treatment problem and the shape of the fluid; Bel Mrsreactor can be freely adjusted.
  • the introduction of the required amount of heat means both the supply and the removal of heat into and from the fluidized bed.
  • the required amount of heat is provided by about 1-50% by the fluidizing gas and by about 50-99% by the heat exchange medium; preferably the major part of the heat transport should take place through the heat exchange medium.
  • the feed device for the bulk material includes all of the usual and known device parts for such processes, such as. B. a storage bunker, a metering device, a deagglomerator, a lock; the same applies to the discharge device, which, for. B. can consist of a weir and a lock.
  • the equipment known for this purpose can also be used for the supply and discharge for fluidizing gas, a suitable device for applying the Stirring arm with vortex gas may be provided.
  • a separator for bulk material particles that have been discharged with the fluidizing gas from the fluidized bed reactor is recommended.
  • the agents according to the invention for solids distribution on the agitator arm represent a further advantageous measure for avoiding agglomerate formation in the area of the agitator arm and possibly in the area of the fluidized bed reactor under the agitator arm. It goes without saying that the design of these agents for solids comminution as well as the design of the stirring arm can be realized in different ways, wherein the stirring arm can also have multiple branches, so to speak multi-arm.
  • the means for retaining the bulk material particles immersed in the fluidized bed according to the invention can be weirs, walls and other internals which, in the general direction of transport of the bulk material particles through the fluidized bed reactor from its inlet to its outlet side, form bottlenecks which reduce backmixing (backmixing) of the bulk material particles and so the lingering time spectrum even.
  • those heat exchangers which are designed as a means of retaining the bulk material particles are particularly advantageous and effective, since the heat transfer between bulk material particles and the heat exchanger is improved in the region of the constrictions.
  • An inventive lamellar structure of the heat exchanger for this purpose, for. B. in the manner of radiator fins, is particularly suitable.
  • the height adjustment according to the invention of an overflow device for the bulk material on the fluidized bed reactor facilitates operation in the part-load range and the setting of the residence time of the bulk material particles in the fluidized bed reactor.
  • the objectives according to the invention are achieved particularly well by the cascade-shaped structure of the fluidized bed reactor according to the invention.
  • the connection of individual treatment zones in series is considered, which must be traversed by all bulk material particles.
  • such cascades can be formed by lamellar heat exchangers placed one behind the other in the direction of travel of the bulk material particles.
  • the device according to the invention thus enables a continuous and automated mode of operation, with as much heat-treated material being discharged automatically as untreated material being added.
  • the advantages achieved by the invention are, in particular, in addition to the avoidance of malfunctions due to overheating and caking, in the lower heat requirement due to the happy combination of fluidizing gas and heat exchange medium, with only extremely little energy being required for the transport of the bulk material particles.
  • Another advantage is the minimization of the reactor volume made possible by the invention, the reduction in size of the downstream cyclones for the separation of / fluidizing gas and bulk material particles and the relatively small surface area of the heat exchange medium to be used.
  • the bulk material to be treated is submitted to the original 1; Via a discharge aid 2 it passes through a metering device 3, if necessary with the interposition of a deagglomerator 4, to a lock 5 and from there into the fluidized bed reactor 6. In the latter there are a double-sided stirring arm 7, a means 8 designed as a partition wall for retaining the bulk material particles and a heat exchanger 9 housed.
  • the treated bulk material can leave the fluidized bed reactor 6 via a lock 10.
  • Fluidizing gas for the fluidized bed reactor 6 is drawn in by means of a blower 11 and supplied to a heat energy source 12 leads.
  • the vortex gas heated in this way passes through a rotating union 13 into the agitator arm 7, which is rotated by the drive 14.
  • the fluidizing gas leaving the fluidized bed reactor 6 is freed of entrained bulk material particles in a separator 15 and discharged for further use, while the separated bulk material particles are fed via the lock 16 to the material flow leaving the lock 10.
  • the system parts of the reference numerals 1-5 are, if not absolutely necessary, components of the feed device 17.
  • the lock 10 is part of the discharge device for bulk material.
  • the blower 11 and the rotary union 13 are components of the feed device for fluidizing gas, while the separator 15 is a component of the discharge device for this.
  • the heat energy source 12 can also be used alternatively or additionally for the heat transfer fluid in the heat exchanger 9.
  • the stirring device 18 comprises the drive 14, the rotary union 13, the stirrer shaft 19 and the stirrer arm 7.
  • the stirrer shaft can, for. B. be made hollow, as well as the stirring arm, which is provided with outlet openings 20 for fluidizing gas.
  • the stirring arm 7 is arranged in the lowermost region 21 of the fluidized bed reactor 6.
  • the outlet openings 20 are essentially downward with a directional component aligned against the direction of rotation of the agitator arm.
  • the means 8 designed as a partition for retaining bulk material particles is oriented transversely to the general direction of travel of the solid particles of the fluidized bed 23 in the fluidized bed reactor 6 and leaves an opening 24 in the lowermost region 21 for the stirring arm 7 and the bulk material passage as well as in the uppermost region 25 of the fluidized bed reactor 6 an opening 26 for gas passage.
  • the fluidized bed reactor 6 is round and the stirring device 18 is designed as in FIG. 1.
  • the feed point 27 and the discharge point 28 for the bulk material are arranged close to one another with respect to the circumference of the fluidized bed reactor 6. Between them extends from the reactor wall to the stirrer shaft 19, a means 8 designed as a partition for retaining solid particles, which, as in FIG. 1, leaves openings 26 and 24 exposed. This results in a general transport direction of the bulk material particles, for example in the rotation, within the fluidized bed reactor direction 29 of the agitator arm 7.
  • a plurality of heat exchangers 9 are immersed in the fluidized bed, which span a surface in the axial direction of the fluidized bed reactor and leave constrictions 30 for the bulk material to pass through; due to this design, the heat exchangers also serve as a means of retaining bulk material particles, and due to the special arrangement there is at the same time a cascade-shaped structure of the fluidized bed reactor 6.
  • the heat exchangers designed in this way have a lamellar structure in the most general form.
  • FIG. 3 as a modification of Figures 1 and 2, an elongated fluidized bed reactor 6 is shown, in which the feed point 27 and the discharge point 28 are arranged on the narrow sides and several, here two, complete stirring devices work in series and separately from one another.
  • the heat exchangers 9 are designed as in FIG. 2 and, because of suitable perforations, enable the stirring arms 7 to rotate freely, which of course (as also in FIG. 2) can also be arranged at different heights in relation to the fluidized bed - also several above one another.
  • the arrangement of the heat exchangers transversely to the general direction of travel of the bulk material particles - further heat exchangers can also be provided - again results in a cascade-shaped structure of the fluidized bed reactor.
  • the bulk material is fed in by means of a screw conveyor 31 and the discharge is carried out by means of a height-adjustable overflow device 32.

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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)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Treatment Of Sludge (AREA)
  • Processing Of Solid Wastes (AREA)
EP81103003A 1980-04-29 1981-04-18 Dispositif pour le traitement à chaud, notamment le séchage des matières en vrac pulvérulentes Expired EP0039039B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT81103003T ATE8532T1 (de) 1980-04-29 1981-04-18 Vorrichtung zur waermebehandlung, insbesondere zum trocknen, von feinteiligen schuettguetern.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3016448 1980-04-29
DE3016448A DE3016448C2 (de) 1980-04-29 1980-04-29 Verfahren und Vorrichtung zur Trockung von feinstkörnigen Schüttgütern

Publications (2)

Publication Number Publication Date
EP0039039A1 true EP0039039A1 (fr) 1981-11-04
EP0039039B1 EP0039039B1 (fr) 1984-07-18

Family

ID=6101214

Family Applications (1)

Application Number Title Priority Date Filing Date
EP81103003A Expired EP0039039B1 (fr) 1980-04-29 1981-04-18 Dispositif pour le traitement à chaud, notamment le séchage des matières en vrac pulvérulentes

Country Status (5)

Country Link
US (1) US4439932A (fr)
EP (1) EP0039039B1 (fr)
JP (1) JPS56165881A (fr)
AT (1) ATE8532T1 (fr)
DE (2) DE3016448C2 (fr)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0343817A3 (en) * 1988-05-21 1990-11-14 Kabushiki Kaisha Hikoma Seisakusho Raw sewage drying apparatus
EP0686253A4 (fr) * 1993-03-01 1997-03-12 French Oil Mill Machinery Sechage de germes de ble moulus par broyage humide
EP0819904A1 (fr) * 1996-07-17 1998-01-21 GEA Wärme- und Umwelttechnik GmbH Installation de séchage à vapeur à lit fluidisé
EP0819902A1 (fr) * 1996-07-17 1998-01-21 GEA Wärme- und Umwelttechnik GmbH Installation de séchage à vapeur à lit fluidisé
CN102393127A (zh) * 2011-09-27 2012-03-28 唐山市神州机械有限公司 一种粘性物料干燥成型方法及系统
CN107894157A (zh) * 2017-11-15 2018-04-10 宣城环化化工科技有限公司 一种焦亚硫酸钠的干燥系统
CN112361719A (zh) * 2020-09-23 2021-02-12 上海化工研究院有限公司 一种用于实验室维生素的连续流化床干燥系统
CN113028788A (zh) * 2021-03-17 2021-06-25 龙孟 一种急诊科医疗器械用烘干设备
CN119334076A (zh) * 2024-12-19 2025-01-21 常州润凯干燥科技有限公司 一种均匀布料的固定式沸腾流化床干燥机
CN120403228A (zh) * 2025-07-03 2025-08-01 福建中成新材料科技有限公司 一种硬质合金材料加工用喷雾干燥设备

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102721266B (zh) * 2012-07-05 2014-09-10 江苏港星方能超声洗净科技有限公司 管状物的干燥装置
DE102015121619B4 (de) * 2015-12-11 2018-05-17 Choren Industrietechnik GmbH Fluidisierungsboden mit einem Rührwerk in einem Druckbehälter für Schüttgut und Verfahren zur Fluidisierung von Schüttgut in einem Druckbehälter
CN111644134B (zh) * 2020-05-19 2021-11-30 山东先达农化股份有限公司 一种化工用气液反应沉淀收集装置
CN113532060B (zh) * 2021-07-26 2023-12-29 广州联存医药科技股份有限公司 一种生物工程用药粉干燥装置及其使用方法

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3256612A (en) * 1964-01-02 1966-06-21 Phillips Petroleum Co Process and apparatus for fluidized bed gas-solids contacting
DE1919332A1 (de) * 1968-04-17 1970-01-02 Jiyuichi Nara Wirbelschichtverfahren zum Trocknen von pulverfoermigen Stoffen
FR2067504A5 (en) * 1969-11-05 1971-08-20 Tunzini Gas/solids contacting apparatus
DE2243670A1 (de) * 1972-09-06 1974-03-28 Vyzk Ustav Chemickych Zarschiz Verfahren und einrichtung zum kontinuierlichen trocknen von koernigen stoffen in einer wirbelschicht
DE2338009A1 (de) * 1973-07-26 1975-02-06 Ceskoslovenska Akademie Ved Vorrichtung zur versetzung pulveriger massen in schwebezustand
FR2334411A1 (fr) * 1975-12-09 1977-07-08 Richter Gedeon Vegyeszet Procede et appareil de fluidisation
US4075766A (en) * 1976-07-19 1978-02-28 General Signal Corporation Apparatus for the treatment of divided solid material
DE2820077A1 (de) * 1977-05-12 1978-11-23 Zucker & Staerkeind Verfahren und vorrichtung zur wirbelschichtbehandlung von fliessunwilligen haufwerken

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2336017A (en) * 1940-12-28 1943-12-07 Kellogg M W Co Accumulator for finely divided solids
US2761769A (en) * 1952-07-17 1956-09-04 Gulf Research Development Co Fluidized catalytic apparatus
GB755579A (en) * 1953-08-01 1956-08-22 Keller G M B H Improvements in or relating to arrangements for continuously drying moist material
FR1494753A (fr) * 1966-04-21 1967-09-15 Perfectionnements aux sécheurs-atomiseurs
JPS4827266B1 (fr) * 1968-07-13 1973-08-21
US4043051A (en) * 1975-02-24 1977-08-23 Delbert Lussenden Method and apparatus for drying grain

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3256612A (en) * 1964-01-02 1966-06-21 Phillips Petroleum Co Process and apparatus for fluidized bed gas-solids contacting
DE1919332A1 (de) * 1968-04-17 1970-01-02 Jiyuichi Nara Wirbelschichtverfahren zum Trocknen von pulverfoermigen Stoffen
FR2067504A5 (en) * 1969-11-05 1971-08-20 Tunzini Gas/solids contacting apparatus
DE2243670A1 (de) * 1972-09-06 1974-03-28 Vyzk Ustav Chemickych Zarschiz Verfahren und einrichtung zum kontinuierlichen trocknen von koernigen stoffen in einer wirbelschicht
DE2338009A1 (de) * 1973-07-26 1975-02-06 Ceskoslovenska Akademie Ved Vorrichtung zur versetzung pulveriger massen in schwebezustand
FR2334411A1 (fr) * 1975-12-09 1977-07-08 Richter Gedeon Vegyeszet Procede et appareil de fluidisation
US4075766A (en) * 1976-07-19 1978-02-28 General Signal Corporation Apparatus for the treatment of divided solid material
DE2820077A1 (de) * 1977-05-12 1978-11-23 Zucker & Staerkeind Verfahren und vorrichtung zur wirbelschichtbehandlung von fliessunwilligen haufwerken

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0343817A3 (en) * 1988-05-21 1990-11-14 Kabushiki Kaisha Hikoma Seisakusho Raw sewage drying apparatus
EP0686253A4 (fr) * 1993-03-01 1997-03-12 French Oil Mill Machinery Sechage de germes de ble moulus par broyage humide
EP0819904A1 (fr) * 1996-07-17 1998-01-21 GEA Wärme- und Umwelttechnik GmbH Installation de séchage à vapeur à lit fluidisé
EP0819902A1 (fr) * 1996-07-17 1998-01-21 GEA Wärme- und Umwelttechnik GmbH Installation de séchage à vapeur à lit fluidisé
CN102393127A (zh) * 2011-09-27 2012-03-28 唐山市神州机械有限公司 一种粘性物料干燥成型方法及系统
CN107894157A (zh) * 2017-11-15 2018-04-10 宣城环化化工科技有限公司 一种焦亚硫酸钠的干燥系统
CN112361719A (zh) * 2020-09-23 2021-02-12 上海化工研究院有限公司 一种用于实验室维生素的连续流化床干燥系统
CN113028788A (zh) * 2021-03-17 2021-06-25 龙孟 一种急诊科医疗器械用烘干设备
CN119334076A (zh) * 2024-12-19 2025-01-21 常州润凯干燥科技有限公司 一种均匀布料的固定式沸腾流化床干燥机
CN120403228A (zh) * 2025-07-03 2025-08-01 福建中成新材料科技有限公司 一种硬质合金材料加工用喷雾干燥设备

Also Published As

Publication number Publication date
ATE8532T1 (de) 1984-08-15
JPS56165881A (en) 1981-12-19
DE3016448A1 (de) 1981-11-05
US4439932A (en) 1984-04-03
DE3016448C2 (de) 1985-07-18
EP0039039B1 (fr) 1984-07-18
DE3164849D1 (en) 1984-08-23

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