EP0819902A1 - Installation de séchage à vapeur à lit fluidisé - Google Patents

Installation de séchage à vapeur à lit fluidisé Download PDF

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Publication number
EP0819902A1
EP0819902A1 EP97105736A EP97105736A EP0819902A1 EP 0819902 A1 EP0819902 A1 EP 0819902A1 EP 97105736 A EP97105736 A EP 97105736A EP 97105736 A EP97105736 A EP 97105736A EP 0819902 A1 EP0819902 A1 EP 0819902A1
Authority
EP
European Patent Office
Prior art keywords
unit
fluidized bed
chamber
heat exchanger
steam
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Withdrawn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
EP97105736A
Other languages
German (de)
English (en)
Inventor
Ulrich Dr.-Ing Schaberg
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.)
GEA Waerme und Umwelttechnik GmbH
Original Assignee
GEA Waerme und Umwelttechnik 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
Priority claimed from EP96111495A external-priority patent/EP0819900A1/fr
Priority claimed from EP96118518A external-priority patent/EP0819903A1/fr
Priority claimed from EP96118517A external-priority patent/EP0819901A1/fr
Application filed by GEA Waerme und Umwelttechnik GmbH filed Critical GEA Waerme und Umwelttechnik GmbH
Priority to EP97105736A priority Critical patent/EP0819902A1/fr
Publication of EP0819902A1 publication Critical patent/EP0819902A1/fr
Withdrawn legal-status Critical Current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
    • 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

Definitions

  • the invention relates to a system for steam fluidized bed drying of water-containing solids, in particular of broken wet brown coal, according to the characteristics in the preamble of claim 1.
  • EP 0 537 263 B1 includes a device Drying a particulate wet material state of the art with superheated steam.
  • Such a system includes a cylindrical housing a number of parallel substantially vertical elongated ones Chambers, which are arranged in a ring.
  • the Moisture is placed in a chamber and then transported in flight flow from chamber to chamber, here dried and discharged at the end.
  • the discharge of the Dry material is carried out by a screw conveyor.
  • a circulation fan for the recirculation of the vortex medium is integrated in the dryer container. Also the coarse dust separation from the vapors takes place in the dryer container. As a result, a compact design without complex Pipe routing reached.
  • Lignite is used on a large scale for production and delivery burned by electrical energy in power plants. Due to the high water content of 50% to 60% of the Raw lignite requires an upstream drying. This makes a rational use of energy in incinerators in a steam power plant process, a gas-steam combination process with integrated upstream Coal gasification or fluidized bed combustion plant enables. Also for the production of secondary products like briquettes, coke or coal dust is one Reduction of water content to 12% to 18% required.
  • the direct drying takes place through evaporation of the coal water in an inert atmosphere with the help of hot flue gas as an energy source in fan mills (flue gas grinding drying).
  • Indirect drying is done using a heat exchanger made, being on the energy supply side condensed heating steam is used.
  • On the On the side of the energy dissipation is the one to be dried Brown coal by contact with the heat exchanger wall and by convective heat transfer of the resulting Hydrocarbon vapor is heated.
  • This principle is used for example in so-called plate dryers and Tube dryers applied.
  • Steam fluidized bed drying also belongs to the prior art, as for example in the DE 37 24 960 A1 or DD 224 649 A1 is described.
  • the broken wet brown coal is used fluidized by steam as a fluidizing medium. Through contact the wet brown coal with the heat exchanger wall and by convective heat transfer of the resulting hydro vapor as well as the drag air becomes the wet brown coal heated and expelled water.
  • each drying unit comprises in a modular design in a vertical stacking arrangement an extraction unit for dried brown coal, a steam fluidized bed dryer unit with integrated Heat exchanger unit and nozzle base unit as well a feed unit for wet lignite.
  • This Concept ensures the availability of a power plant with more than 7500 operating hours per year the coal predrying is not affected.
  • the wet brown coal becomes a drying unit abandoned via a rotary valve.
  • the deduction of the Dry brown coal is made mechanically by means of screw conveyors. This facility has proven itself. Through the Movement of the relatively moving parts of the Trigger unit can, however, show signs of wear come.
  • the invention is therefore based on the object of a system for steam fluidized bed drying of water-containing To further develop solids in plant technology.
  • the dry material can be introduced into a fume cupboard pneumatic fluid can be removed.
  • a first advantage of this configuration is that Moving away from mechanical discharge to a pneumatically assisted one Discharge system. This can in particular the wear and the susceptibility to malfunction of the system are reduced will. Furthermore, this version enables very compact design of a fume cupboard and an integration the extraction unit in the housing of the drying system.
  • the fume cupboard for steam fluidized bed dryers suitable with round container dimensions. Is too easy regulation of the amount removed possible by controlling the medium.
  • Another advantage is that the deduction cooling of the dry goods can be carried out. By introducing cool compared to the dry goods The temperature of the dry material is reduced. This is particularly advantageous when drying of lignite, which is caused by cooling in the process a lower one, suitable for further use Temperature level is brought.
  • the medium circulated can be closed so that no or only insignificant losses occur.
  • the pumped medium is purchased in the district purchase Appropriate filters and coolers directed and via a blower returned to the trigger.
  • Cooling takes place when lignite is dried the dry lignite during the discharge from the System without loss of hydrocarbon vapor. The discharged coal is then dry and cooled. she can be transported open atmospherically.
  • the system for steam fluidized bed drying can be designed both for operation at atmospheric pressure as well as for operation with overpressure. With overpressure operated systems one speaks of a pressure-charged Steam fluidized bed drying.
  • the facility is suitable for drying a wide variety of water-based Solids. Because of their compact modular structure and high performance, it is particularly suitable for drying broken wet brown coal in Power plants.
  • a trigger in an S-shaped configuration includes one Inlet chamber and a downstream outlet chamber.
  • a nozzle unit for the pumped medium arranged, which the dry material over a Drain chamber from a downstream discharge chamber separating swell weir promotes.
  • the dry goods are deflected in the fume cupboard.
  • the Dry material flows in the feed chamber under the influence gravity down, then goes into the drain chamber deflected and here by the medium as a suspension element transported away.
  • the inlet chamber is expedient and the drain chamber through a common wall in some areas separated from each other.
  • the inlet chamber is on the bottom and the drain chamber in communication so that the Dry goods can pass here.
  • the discharge chamber is connected by a swell weir the discharge chamber. From here the dry goods conveyed for further use and from the steam fluidized bed dryer led out.
  • Dry brown coal for example, can be used with the pneumatic Pumped medium as a suspension element directly in a Firing system can be introduced.
  • the heat exchanger unit circular with vertical Central longitudinal axis of the fluidized bed dryer unit essentially radially extending heat exchanger tubes.
  • This embodiment enables a very compact design the drying system with efficient use of the available construction volume.
  • the drying plant is characterized by a round geometry of their housing. This is especially for one pressure-charged drying system advantageous. Conveniently is the radial compressor for the circulation of the Vortex medium arranged inside the housing.
  • the heat exchanger tubes can be straight or curved, e.g. serpentine, extend. Here can their axes of extension exactly at right angles to Central longitudinal axis of the fluidized bed dryer unit or run at an angle other than 90 °.
  • the heat exchanger unit through a partition into at least two segment-like Fluidized bed cells divided.
  • the heat exchanger unit is preferably divided into several fluidized bed cells with dimensions, which ensure stable fluid bed operating conditions. This will result in intense heat transfer and achieved a high drying success. Also regarding the process control results in a significant improvement a drying plant because the fluidized bed in the fluidized bed cells reacted much less sensitive to changing operating parameters, for example at different moisture levels of the abandoned Bulk goods.
  • Each fluidized bed cell is a grate nozzle bottom and a Deduction assigned. This results in one from individual units modular nozzle base unit and a fume cupboard. The installation or removal of individual units is simple. This also leads to a significant relief of maintenance or repair work.
  • the internal steam distribution chamber also functions as integrated additional heating of the drying system.
  • each installation consists of two to each other relatively movable parts, part of which is on the outside Tube sheet and the other part fixed to the inner tube sheet is. This can cause thermal stresses or elongations due to occurring temperature differences be met.
  • the water vapor emerges from the steam collecting chamber individual fluid bed cells and can be a corresponding Aftertreatment with dust removal or fine grain separation be fed.
  • a fabric filter is recommended with associated compressed gas cleaning, in particular with compressed steam, as a dedusting device.
  • the filter cake is periodically cleaned by means of compressed gas cleaned from the fabric filter.
  • the secluded Dust can be removed separately from the drying system and forwarded for further use.
  • the separated dust is in the fume cupboard the drying plant and discharged with the dry material.
  • a drying plant according to the invention becomes granular from above Fluid material flows through from the bottom upwards.
  • the fluid that is expelled from the moist material is used as the vortex medium Steam used.
  • the amount of vortex medium and the flow rate are adjusted so that the bed of solids changes into a fluidized bed.
  • the vortex speed is above the vortex point and remains approximately constant regardless of what needs to be dried Mass flow. This is achieved through the recirculated Steam cycle.
  • the weight is in the fluidized bed the solid grains opposed by the directed flow force of the vortex medium almost canceled.
  • the fluidized bed of solids behaves then liquid-like and flows through the heat exchanger unit.
  • there is intensive heat transfer due to high turbulence and that contained in the moist material Water Water is evaporated. In this way, a reliable drying of the solid to almost any residual water content can be achieved.
  • FIG. 1 shows a system 1 for steam fluidized bed drying of hydrated FG, preferably broken wet brown coal.
  • a trigger unit is arranged vertically one above the other 2 for dry goods TG, a fluidized bed dryer unit 3 with integrated nozzle base unit 4 and heat exchanger unit 5 and a task unit 6 for to recognize the wet material FG.
  • the aforementioned units 2, 3, 4, 5, 6 are compact in a pressure-resistant housing 7 arranged.
  • Wet brown coal in a grain size range of
  • the feed unit 6 is 0 to 10 mm via a system allocated from two rotary feeders 8, 9.
  • the cellular wheel sluice 8 is filled with wet brown coal has been closed, a pressure equalization to the rotary valve 9 and the Wet lignite is transferred to the rotary valve 9.
  • the cellular wheel sluice 9 is then sealed off from the outside and the wet brown coal over chutes 10, 11, Funnels 12, 13 and pipes 14, 15 in the fluidized bed dryer unit 3 transferred.
  • the heat exchanger unit 5 circular design with heat exchanger tubes 16, which extends to the vertical central longitudinal axis ML of the fluidized bed dryer unit 3 radial extend.
  • the heat exchanger unit 5 is vertical aligned partition walls 17 in a total of eight segment-like Fluidized bed cells 18 divided.
  • the wet lignite passes through the pipes 14, 15 the vapor collection chamber 19 and gets into the individual Fluid bed cells 18.
  • the wet lignite falls then downwards against the upward flowing fluid World Cup.
  • the WM fluidizing medium comes from wet lignite expelled and cleaned hydro steam for Use which over individual grate nozzle bases 20 of the nozzle base unit 5 introduced into the fluidized bed cells 18 becomes.
  • the brown coal bed goes above the heat exchanger unit 5 into the fluidized bed.
  • the fluidized bed continues through the heat exchanger unit 5, and the fluidized lignite flows through the fluidized bed cells 18.
  • the lignite is removed from the fluidizing medium WM put in a floating state.
  • the Amount of vortex medium WM and the flow velocity are designed so that in each fluidized bed cell 18th a homogeneous fluidized bed is created. Then there are extraordinarily good conditions for heat transfer in front.
  • the hydrocarbon vapor KWD expelled then enters the steam collection chamber 19 and from there for post-treatment into a dedusting device 21.
  • Dry brown coal (dry goods TG) is over the fume cupboard 2 deducted from Appendix 1.
  • the trigger unit 2 comprises a total of eight deductions 22, which are each assigned to a fluidized bed cell 18 are. From the deductions 22, the dry goods TG through Introduction of a pneumatic conveying medium FM transported away.
  • Each trigger 22 includes an S-shaped configuration funnel-like inlet chamber 23 and one downstream of it Drainage canister 24.
  • a nozzle unit 26 is arranged at the bottom 25 of the drainage chamber 24.
  • the nozzle unit 26 is supplied with fluid FM via a pipeline 27.
  • the medium FM then flows in the drain chamber 24 upwards and thereby promotes the dry goods TG a swell weir 28 in one of the drain chamber 24 downstream discharge chamber 29.
  • Dry material TG is continuously removed from the discharge chamber 24 the inlet chamber 23 pulled into the outlet chamber 24.
  • Inlet chamber 23 and outlet chamber 24 are through a wall 30 separated from each other in their upper region. Under the wall 30 is a passage 31 for the transfer of the Dry goods TG from the inlet chamber 23 into the outlet chamber 24th
  • the heat exchanger unit 5 designed circular. This encloses the heat exchanger unit 5 a central steam distribution chamber 35.
  • the steam distribution chamber 35 is on the pipe 36 supplied with heating steam HD.
  • the pressure of the heating steam HD is usually around 10 bar.
  • the system pressure a pressurized steam fluidized bed drying system is usually 4 bar.
  • the heating steam HD is evenly distributed in the steam distribution chamber 35 and enters the heat exchanger tubes 16 a. Condensed on the way through the heat exchanger tubes 16 heating steam HD. The condensate is then outside via a condensate manifold, not shown here dissipated.
  • the tube pitch of the heat exchanger tubes 16 is larger on the outside than on the inside.
  • the division differences are shown in a technically simplified manner with reference to FIG. 4.
  • the inside pipe division is marked with t1, the outside pipe division with t2.
  • the distance between two adjacent heat exchanger tubes 16 ', 16''on the outer tube plate 38 is consequently greater than the distance between the heat exchanger tubes 16', 16 '' on the inner tube plate 39.
  • the vertical passage cross section Q v between the heat exchanger tubes 16 ', 16'' consequently increases from the inside out. This change in area causes uneven flow conditions in the fluidized bed.
  • V-shaped installation 40 which compares the vertical passage cross section Q v is provided between the adjacent heat exchanger tubes 16 ', 16''. In this way, a uniform distribution of the flow conditions is achieved, so that there are approximately constant fluidized bed conditions.
  • FIG. 4 shows two possible design variants of an installation 40 shown.
  • the left illustration shows a rotationally symmetrical displacement body 41 in Shape of a cone
  • the right representation shows a truncated cone Displacement Body 42.
  • FIG 5 shows another embodiment of the vertical passage cross section equalizing Installation 43 shown.
  • the installation 43 has components which are movable relative to one another 44, 45.
  • the outer component 44 is conical and forms a displacer 46.
  • the displacement body 46 Centrally from one Starting from the tip, the displacement body 46 has a Hole 47 on.
  • Component 45 is a centering rod 48 formed, which with sliding seat in the bore 47th is led.
  • the displacement body 46 is on the outside Tube plate 49 and the centering rod 48 on the inner tube plate 50 committed.
  • the dedusting device is 21 integrated into the vapor collection chamber 19.
  • the dedusting device 21 comprises fabric filters 51, in which the from the fluidized bed dryer unit 3 escaping hydrocarbon vapor from its KWD Dust load is freed.
  • the dust-laden Hydro vapor KWD expediently radially in the direction indicated by the arrows (KWD) the fabric filter 51 out.
  • the fabric filter 51 is a pneumatic one Cleaning device 52 arranged. Be over nozzles 53 the fabric filter 51 is pressurized with compressed air and the deposited filter cake is blown off.
  • the separated dust falls down into a collecting funnel 54.
  • a collecting funnel 54 is here for the sake of clarity only in the right half of the picture Figure 1 shown.
  • the dust arrives via a pipeline from the collecting funnel 54 55, which passes through the vapor collection chamber 19, in the trigger 22. To avoid a pressure short circuit, the dust is given to the trigger 22 in the inlet chamber 23.
  • the outer wall 56 of the receiving funnel 54 also serves for Routing of hydrocarbon vapor KWD above the fluidized bed dryer unit 3, so that it is radial in the fabric filter 51 occurs.
  • the cleaned hydro vapor KWD is then above the cleaning device 52 via a central suction line 57 sucked in by means of a radial compressor 58.
  • the radial compressor 58 is in the housing 7 below the Fluidized bed dryer unit 3 arranged.
  • the cleaned one Hydro vapor KWD emerges radially here is used as a vortex medium WM through inlet openings 59 in the Grate nozzle bottoms 20 initiated.
  • Excess hydrocarbon vapor KWD can be drawn off 60 removed from Appendix 1 and for example in an external turbine can be used.

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  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Drying Of Solid Materials (AREA)
EP97105736A 1996-07-17 1997-04-08 Installation de séchage à vapeur à lit fluidisé Withdrawn EP0819902A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP97105736A EP0819902A1 (fr) 1996-07-17 1997-04-08 Installation de séchage à vapeur à lit fluidisé

Applications Claiming Priority (7)

Application Number Priority Date Filing Date Title
EP96111495A EP0819900A1 (fr) 1996-07-17 1996-07-17 Installation pour le séchage à lit fluidisé par vapeur de lignite brut
EP96111495 1996-07-17
EP96118518A EP0819903A1 (fr) 1996-07-17 1996-11-19 Installation de séchage de lignite
EP96118517A EP0819901A1 (fr) 1996-07-17 1996-11-19 Installation de séchage de lignite
EP96118517 1996-11-19
EP96118518 1996-11-19
EP97105736A EP0819902A1 (fr) 1996-07-17 1997-04-08 Installation de séchage à vapeur à lit fluidisé

Publications (1)

Publication Number Publication Date
EP0819902A1 true EP0819902A1 (fr) 1998-01-21

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Application Number Title Priority Date Filing Date
EP97105736A Withdrawn EP0819902A1 (fr) 1996-07-17 1997-04-08 Installation de séchage à vapeur à lit fluidisé

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EP (1) EP0819902A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101445739B (zh) * 2008-12-26 2012-07-25 清华大学 一种水平移动床式褐煤干燥方法
WO2012163222A1 (fr) * 2011-05-31 2012-12-06 Li Bairong Appareil et système de fabrication de produits de charbon de qualité
CN103217009A (zh) * 2013-04-10 2013-07-24 山西鑫立能源科技有限公司 入炉煤矸石热废气调湿脱水的水汽排汽导出器

Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB715836A (en) * 1950-12-13 1954-09-22 Smidth & Co As F L Improvements relating to heat-exchange processes for heating or cooling powdered material
DE1268065B (de) * 1959-03-20 1968-05-09 Arenco Ab Schwebebett-Trockner
CH462721A (de) * 1967-01-13 1968-09-15 Shionogi & Co Trocknungsvorrichtung zum kontinuierlichen Trocknen von pulver- oder granulatförmigem Material
DE1604826A1 (de) * 1966-08-11 1970-08-13 Reinhard Becker Getreidetrockner fuer aussetzenden Betrieb
DE2217578A1 (de) * 1971-04-16 1972-11-02 Aktieselskabet Niro Atomizer, Soeborg (Dänemark) Vorrichtung zum Trocknen feuchter Pulver und Verfahren zum Betreiben einer derartigen Vorrichtung
EP0039039A1 (fr) * 1980-04-29 1981-11-04 Bergwerksverband GmbH Dispositif pour le traitement à chaud, notamment le séchage des matières en vrac pulvérulentes
DE3025924A1 (de) * 1980-07-09 1982-02-04 Dieter 5060 Bergisch Gladbach Popp Fluessigkeitsgekuehlter stuetzboden fuer eine wirbelschichttrockner
AT380331B (de) * 1978-10-31 1986-05-12 Waagner Biro Ag Fliessbetttrockner fuer schuettgueter, insbesondere kohle
EP0343407A1 (fr) * 1988-05-11 1989-11-29 Waagner-Biro Aktiengesellschaft Dispositif pour introduire la matière à fluidiser dans un lit fluidisé, en particulier une installation de séchage
WO1992001201A1 (fr) * 1990-07-09 1992-01-23 Niro A/S Appareil pour le sechage d'une matiere particulaire humide a l'aide de vapeur surchauffee
WO1994012838A1 (fr) * 1992-11-25 1994-06-09 Amax Coal Industries, Inc. Procede et appareil de sechage et de briquetage de charbon
EP0713070A1 (fr) * 1994-11-21 1996-05-22 Powdering Japan K.K. Dispositif de lit fluidisé pour le séchage ou le refroidissement de poudre, et procédé de séchage ou de refroidissement de poudre l'utilisant

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB715836A (en) * 1950-12-13 1954-09-22 Smidth & Co As F L Improvements relating to heat-exchange processes for heating or cooling powdered material
DE1268065B (de) * 1959-03-20 1968-05-09 Arenco Ab Schwebebett-Trockner
DE1604826A1 (de) * 1966-08-11 1970-08-13 Reinhard Becker Getreidetrockner fuer aussetzenden Betrieb
CH462721A (de) * 1967-01-13 1968-09-15 Shionogi & Co Trocknungsvorrichtung zum kontinuierlichen Trocknen von pulver- oder granulatförmigem Material
DE2217578A1 (de) * 1971-04-16 1972-11-02 Aktieselskabet Niro Atomizer, Soeborg (Dänemark) Vorrichtung zum Trocknen feuchter Pulver und Verfahren zum Betreiben einer derartigen Vorrichtung
AT380331B (de) * 1978-10-31 1986-05-12 Waagner Biro Ag Fliessbetttrockner fuer schuettgueter, insbesondere kohle
EP0039039A1 (fr) * 1980-04-29 1981-11-04 Bergwerksverband GmbH Dispositif pour le traitement à chaud, notamment le séchage des matières en vrac pulvérulentes
DE3025924A1 (de) * 1980-07-09 1982-02-04 Dieter 5060 Bergisch Gladbach Popp Fluessigkeitsgekuehlter stuetzboden fuer eine wirbelschichttrockner
EP0343407A1 (fr) * 1988-05-11 1989-11-29 Waagner-Biro Aktiengesellschaft Dispositif pour introduire la matière à fluidiser dans un lit fluidisé, en particulier une installation de séchage
WO1992001201A1 (fr) * 1990-07-09 1992-01-23 Niro A/S Appareil pour le sechage d'une matiere particulaire humide a l'aide de vapeur surchauffee
WO1994012838A1 (fr) * 1992-11-25 1994-06-09 Amax Coal Industries, Inc. Procede et appareil de sechage et de briquetage de charbon
EP0713070A1 (fr) * 1994-11-21 1996-05-22 Powdering Japan K.K. Dispositif de lit fluidisé pour le séchage ou le refroidissement de poudre, et procédé de séchage ou de refroidissement de poudre l'utilisant

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101445739B (zh) * 2008-12-26 2012-07-25 清华大学 一种水平移动床式褐煤干燥方法
WO2012163222A1 (fr) * 2011-05-31 2012-12-06 Li Bairong Appareil et système de fabrication de produits de charbon de qualité
US9328958B2 (en) 2011-05-31 2016-05-03 Li Bairong Apparatus and system for manufacturing quality coal products
CN103217009A (zh) * 2013-04-10 2013-07-24 山西鑫立能源科技有限公司 入炉煤矸石热废气调湿脱水的水汽排汽导出器
CN103217009B (zh) * 2013-04-10 2015-04-22 山西鑫立能源科技有限公司 入炉煤矸石热废气调湿脱水的水汽排汽导出器

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