WO1993025303A1 - Procede et appareil de traitement de matieres particulaires dans une chambre a lit fluidise - Google Patents

Procede et appareil de traitement de matieres particulaires dans une chambre a lit fluidise Download PDF

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Publication number
WO1993025303A1
WO1993025303A1 PCT/DK1993/000181 DK9300181W WO9325303A1 WO 1993025303 A1 WO1993025303 A1 WO 1993025303A1 DK 9300181 W DK9300181 W DK 9300181W WO 9325303 A1 WO9325303 A1 WO 9325303A1
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WO
WIPO (PCT)
Prior art keywords
fluidized bed
chamber
dilution gas
particulate material
air
Prior art date
Application number
PCT/DK1993/000181
Other languages
English (en)
Inventor
Ove Hansen
Original Assignee
Niro Holding A/S
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 Niro Holding A/S filed Critical Niro Holding A/S
Priority to AU43098/93A priority Critical patent/AU4309893A/en
Priority to PCT/DK1993/000181 priority patent/WO1993025303A1/fr
Publication of WO1993025303A1 publication Critical patent/WO1993025303A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1872—Details of the fluidised bed reactor

Definitions

  • the present invention relates to a method of processing a particulate material containing an inflammable component in a fluidized bed chamber.
  • the particulate material may be wet granules of tablet materials containing an inflammable component, such as alcohol, acetone, or another solvent, and possibly also water.
  • an inflammable component such as alcohol, acetone, or another solvent, and possibly also water.
  • the fluidizing gas which is usually air or another oxygen containing gas.
  • the mixture of the oxygen containing gas and the evaporated inflammable component may under certain circumstances be explosive or inflammable, so that an accidental spark caused for example by static electricity may give rise to an ex ⁇ plosion or a fire.
  • the prepared batch of the wet granules is then transferred to a fluidized bed dryer, in which atmospheric air is used as fluidizing gas.
  • the exhaust air leaving the fluidized bed may contain such a proportion of the in ⁇ flammable component that a risk of explosion or ignition may exist, especially at the beginning of the drying process before the granulated material has been sufficiently cooled down due to adiabatic evaporation of the volatile inflammable component and due to contact with the normally cool fluidi ⁇ zing air.
  • the present invention provides a method and apparatus by means of which the risk of an explosion in connection with the processing of a particulate material containing an in ⁇ flammable component in a fluidized bed may be efficiently eliminated or considerably reduced in a rather economic manner.
  • the present invention provides a method of processing a particulate material containing an inflammable component in a fluidized bed chamber being defined by side walls and having a perforated bed plate, said method comprising passing flui ⁇ dizing oxygen containing air upwardly through the perfora- tions of the bed plate for fluidizing the particulate materi ⁇ al so as to form a fluidized bed on the bed plate and so as to carry off inflammable component from the particulate material, introducing dilution gas into the fluidized bed chamber at least at one position spaced from said chamber side walls and mixing the dilution gas with the fluidizing air and with the inflammable component above the fluidized bed, the amount of dilution gas introduced being sufficient to substantially reduce the explosion risk of the mixture containing oxygen and inflammable component, and discharging the gas mixture from the upper part of the fluidized bed chamber.
  • dilution gas being introduced into the fluidized bed chamber and mixed with the fluidizing air reduces the propor- tion of the inflammable component in the mixture and thereby reduces the explosion risk. It has been found that the mixing of the dilution gas with the spent fluidizing air and the inflammable component is improved when the dilution gas flows outwardly from such a position which is spaced from the chamber side walls. If desired, dilution gas may additionally be introduced through one or more inlet openings defined in the side walls of the chamber.
  • the dilution gas introduced may, for example, be nitrogen or another inert gas.
  • the dilu- tion gas is preferably atmospheric air.
  • the inflammable component contained in the fluidizable parti ⁇ culate material may be a gas which is absorbed or adsorbed by the particulate material.
  • how ⁇ ever the particulate material is made by mixing one or more powdered components with liquid comprising a volatile liquid, such as acetone or ethyl alcohol, or mixtures of such liquids with water.
  • the inflammable component may, alterna ⁇ tively, comprise a solid powdered substance being composed by combustible particles which are so small that they are en- trained by the fluidizing air flowing from the fluidized bed to the fluidizing air discharge.
  • the dilution gas or air may be introduced into and mixed with the fluidizing air in any suitable manner above and pre- ferably immediately above the fluidized bed so as to not substantially interfere with the fluidized bed.
  • said at least one position of introducing dilution gas is preferably located centrally within such chamber. This means that one or more dilution gas outlets may be arranged centrally above a sub ⁇ stantially circular or substantially square bed plate.
  • one or more dilution gas outlets may be arranged in mutually spaced positions along a longitu ⁇ dinal symmetry axis and possibly also along a transverse symmetry axis.
  • the dilution gas may be directed outwardly into the fluidized bed chamber in one coherent or in several separated flows defining an annular pattern. It has been found that when the dilution gas is directed outwardly into the fluidized bed chamber in one or more outwardly directed flows a good mixing with the upwardly flowing fluidizing air may be obtained. It should be understood that any suitable type of mixing devices could be arranged within the fluidized bed chamber for impro ⁇ ving a uniform mixing of the dilution gas with the spent fluidizing air.
  • the amount of inflammable component released from the parti ⁇ culate material may vary during the processing period. Usual- ly, the amount of inflammable component released decreases as the processing proceeds.
  • the flow of dilution gas introduced into the fluidized bed chamber may be controlled in response to the amount of inflammable component carried off from the particulate material.
  • the concentration of inflammable component in the gas phase within the processing chamber may be currently measured by suitable sensing means, and the flow of dilution gas introduced may be increased when the proportion of inflammable component increases and vice versa.
  • the flow of dilution gas introduced into the fluidized bed chamber is maintained substantially constant, while the flow of fluidi- zing air is being controlled so as to keep the concentration of inflammable component within predetermined limits.
  • the flow of dilution gas may be controlled.
  • the particulate material may be introduced into the fluidized bed chamber in a hot condition, for example because it is supplied directly from a high speed mixer and granulator.
  • the particulate material contains a volatile, inflam ⁇ mable liquid component this means that a relatively high proportion of inflammable vapour is released from the par- ticulate material during the first part of the processing period.
  • dilution gas may be introduced into the fluidized bed chamber for a certain period of time prior to passing fluidizing air through the perforations of the bed plate. Thereafter, the flow of fluidizing air may be gradual ⁇ ly increased till the desired maximum value has been reached without passing a predetermined concentration level of the inflammable component in the exhaust gas.
  • the release of inflammable component from the particulate material may also be controlled by controlling the tempera ⁇ ture of the fluidizing air supplied to the fluidized bed chamber.
  • the fluidizing air supplied may be below or at room temperature during the first part of the processing period, and when part of the inflammable liquid component has been vaporized from the particulate material. which is thereby cooled down, the temperature and/or the flow rate of the fluidizing air may be increased.
  • the gas mixture may be exhausted from the fluidized bed chamber at a rate so as to create a pressure within the fluidized bed chamber slightly below the atmospheric pressure so as to prevent leakage of gas through the walls defining said chamber.
  • the supply of dilution gas, the supply of fluidizing air, the temperature of the fluidizing air, and/or the exhaust rate of gas mixture may be controlled by suitable electronic control means, such as a microprocessor, whereby the relative content of inflammable component of the gas mixture may be kept below a predetermined safe value while the particulate material is being processed in the most efficient and economic manner.
  • suitable electronic control means such as a microprocessor
  • the present invention provides an apparatus for processing a particulate material containing an inflammable component, said apparatus comprising a fluidi ⁇ zed bed chamber being defined by side walls and having a perforated bed plate arranged therein, means for supplying particulate material to be processed on to the bed plate, means for supplying fluidizing air upwardly through the bed plate so as to fluidize the particulate material thereon, means for feeding dilution gas into the fluidized bed chamber and for mixing the dilution gas with the fluidizing air above, and preferably immediately above the fluidized bed formed on the bed plate, the dilution gas feeding and mixing means comprising at least one dilution gas outlet spaced from the chamber side walls, and means for discharging the gas mixture from the upper part of the fluidized bed chamber.
  • the dilution gas feeding and mixing means are preferably located immediately above the fluidized bed and preferably positioned centrally within the fluidized bed chamber.
  • the said at least one dilution gas outlet may comprise one or more outlet openings or nozzles which are directed outwardly and transversely to the upwardly directed fluidizing air flow.
  • the feeding and mixing means may comprise any type of baffles or impellers or other mixing means pro ⁇ moting a uniform mixing of the dilution gas with the upwardly flowing fluidizing air.
  • the dilution gas outlet which may define a substantially annular outlet opening, may, for example, be defined between a lower edge of a downwardly extending axial supply tube and a cover plate axially spaced therefrom.
  • the gas mixture discharging means may comprise a filtering device of any type for filtering solid particles from the gas mixture being discharged, and the filtering device may, for example, comprise one or more bag filters.
  • the method and apparatus according to the invention are applicable not only for drying a particulate material contai ⁇ ning an inflammable component, but also for any other kind of processing a particulate material in a fluidized bed, such as granulating. Furthermore, the invention is applicable not only in connection with fluidized bed apparatuses to which the particulate material is fed batchwise, but also to flui ⁇ dized bed apparatuses to which the particulate material is fed and discharged continuously.
  • the latter type of fluidized bed apparatuses may be of the back mixed type which may be connected to a further fluidized bed apparatus of the plug- flow type.
  • Fig. 1 is a side view and a partially sectional view of a fluidized bed apparatus in which dilution air is introduced through openings defined in the peripheral wall of the flui ⁇ dized bed chamber,
  • Fig. 2 is a side view and partially sectional view of an embodiment of the fluidized bed apparatus according to the invention
  • Fig. 3 is a copy in black and white of a coloured computer simulated flow distribution pattern in the fluidized bed ap ⁇ paratus shown in Fig. 1,
  • Fig. 4 is a flow distribution pattern corresponding to that shown in Fig. 3 in the apparatus shown in Fig. 2,
  • Fig. 5 is a representation showing at various levels the variation in alcohol concentration along a diameter of the fluidized bed chamber of the apparatus shown in Fig. 1
  • Fig. 6 is a representation as that in Fig. 5 for the appara- tus shown in Fig. 2
  • Fig. 7 is a graphic representation in which the contents of ethyl alcohol in the gas mixture discharged from a fluidized bed apparatus as that shown in Fig. 2 is plotted versus the processing time
  • Fig. 8 is a graphic representation corresponding to that shown in Fig. 7, but when no dilution air is introduced into the apparatus.
  • Fig. 1 diagrammatically illustrates a fluidized bed apparatus comprising an upright housing 10 having a substantially horizontal bed plate 11 arranged in its lower end portion.
  • the upper part of the apparatus may be stationarily suspended while the lower part of the apparatus containing the particu ⁇ late material to be fluidized and a plenum chamber 13 is movable by means of rollers or wheels 12 which are mounted at the lower end of the housing 10.
  • the plenum chamber 13 having an inlet 14 for fluidizing air is defined in the lower end of the housing 10 below the bed plate 11.
  • a filtering device 15 which may, for example, comprise a number of bag filters, is arranged within a filtering chamber 16, which is defined in the upper end of the housing 10, and from which gas may be discharged through an outlet 17 communicating with the fil ⁇ tering chamber 16 above the filtering device 15.
  • a fluidized bed chamber 18 is defined in the housing 10 between the bed plate 11 and the filtering device 15. This fluidized bed chamber 18 may contain a fluidized bed 19 positioned above the bed plate 11 and formed by a fluidized particulate material.
  • Dilution air or gas may be introduced into the fluidized bed chamber 18 immediately above the fluidized bed 19 by means of a dilution gas supply and mixing device 20.
  • the supply and mixing device 20 comprises an annular manifold chamber 21 encircling the fluidized bed chamber 18.
  • the mani ⁇ fold chamber 21 communicates with an annular pattern of peripherally spaced openings 22 formed in the peripheral wall of the housing 10 immediately above the fluidized bed 19.
  • Dilution gas or air may be supplied to the manifold chamber 21 through an inlet 23.
  • the dilution gas supply and mixing device 20 shown in Fig. 2 corresponds to that shown in Fig. 1, and corresponding apparatus parts have been designated by the same reference numerals.
  • the dilution gas supply and mixing device 20 shown in Fig. 2 comprises a tube section 24 extending axially and centrally downwardly within the fluidized bed chamber 18.
  • the tube section 24 has an open end 25 closely spaced from the upper surface of the fluidized bed 19.
  • the end opening of the tube section 24 is covered by a cover plate 2 which is axially spaced from the open end 25 of the tube section 24 so as to define an annular, substan ⁇ tially axially directed nozzle opening 27 between the open end 25 of the tube 24 and the cover plate 26.
  • Dilution gas or air may be supplied to the axial tube section 24 through an inlet 28 and as shown in Fig. 2 the tube section 24 and the inlet 28 may together form a tube bend.
  • Figs. 1 and 2 may be operated as follows:
  • dilution air or gas may be supplied to the inlets 23 and 28, respectively, while gas is withdrawn from the filtering chamber through the outlet 17, for example by means of a suction fan (not shown) communica ⁇ ting therewith.
  • the dilution gas or air may also be supplied to the inlets 23 or 28 by means of a pressure fan (not shown) or another pressurized gas source.
  • cool fluidizing air may be supplied to the plenum chamber 13 through the inlet 14 from a suitable pressurized air source, such as a pressure fan, whereby the particulate material on the bed plate 11 is eventually flui- dized so as to form the fluidized bed 19.
  • a suitable pressurized air source such as a pressure fan
  • the dilution gas flowing radially into the fluidized bed chamber 18 through the openings 22 and the nozzle opening 27, respectively, is mixed with and dilutes the fluidizing air having passed the fluidized bed 19 and having received an inflammable component therein so that the risk of ignition and explosion of the gas mixture is eliminated or substantially reduced.
  • the diluted gas mixture being exhausted through the outlet 17 is filtered in the filtering device 15.
  • the relative amount of the in ⁇ flammable component contained in the gas mixture exhausted through the outlet 17 may be sensed by means of a sensing device 29, and the temperature of the particulate material on the bed plate 11 may be sensed by means of a temperature sensing device 30.
  • the operation of the apparatuses shown in Figs. 1 and 2 may be controlled by means of an electronic control device 31, such as a microprocessor, which may re ⁇ ceive measuring signals from the sensing devices 29 and 39 and from possible other detectors.
  • Fig. 3 illustrates the gas flow pattern within the upper part of the fluidized bed chamber 18 of the apparatus shown in Fig. 1, while Fig. 4 illustrates the corresponding flow pattern within the apparatus according to the invention shown in Fig. 2.
  • the illustrations in Figs. 3 and 4 have been obtained by computer simulation using the software FLUENT supplied by Fluent Inc., Hanover, New Hampshire, USA (former- ly Creare. X Inc.).
  • the flow pattern shown in Fig. 3 has been generated by com ⁇ puter numeric simulation of a situation where the inner diameter of the fluidized bed chamber 18 above the fluidized bed is 1.28 m, while the velocity of the fluidizing air in the fluidized bed is 1.165 m/sec with an air flow of 6138 kg/h.
  • the velocity of the dilution air flowing in the flui ⁇ dized bed chamber 18 through the openings 22 is 15 m/sec, and the amount of dilution air is 6890 kg/h.
  • the alcohol con ⁇ centration in the fluidizing air having passed the fluidized bed 19 is set to 0.1 kg/kg dry air, and in case of complete mixing of dilution gas and fluidizing air the alcohol con ⁇ centration is calculated to be 0.0471 kg alcohol/kg dry air.
  • the computer simulated flow pattern shown in Fig. 4 is based on an apparatus of the type shown in Fig. 2, where the inner diameter of the fluidized bed chamber 18 above the fluidized bed 19 is 1.28 m, the velocity of the fluidizing air in the fluidized bed is 1.165 m/sec, and the fluidizing air is supplied in an amount of 6138 kg/h. Dilution air is supplied though the axial tube section 24 at a velocity of 22 m/sec and in an amount of 4181 kg/h. The dilution air is flowing outwardly through the annular nozzle opening 27 at a velocity of 15.3 m/sec.
  • Figs. 5 and 6 The variation in alcohol concentration in the fluidized bed chamber 18 of the apparatuses shown in Figs. 1 and 2 is illustrated also in Figs. 5 and 6, and these illustrations are based on the numeric values obtained by the computer simulation described above in connection with Figs. 3 and 4.
  • Figs. 5 and 6 the variation in alcohol concentration dia ⁇ metrically across the circular fluidized bed chamber 18 is shown by graphs 34 and 35, respectively, at various uniformly axially spaced levels (indicated by broken lines) .
  • the mutual axial spacing "s" of the levels corresponds to an alcohol concentration of 0.1 kg alcohol/kg dry air. This means that the vertical distance between each of the horizontal broken lines and the adjacent graph thereabove indicates the frac ⁇ tional alcohol concentration at the respective location. From Figs.
  • a fluidized bed apparatus of the type shown in Fig. 2 was used for drying a wet, granulated material containing ethyl alcohol in order to demonstrate that it was possible to keep the peak concentrations of alcohol below a predetermined safety level.
  • the flow of dilution air supplied through the tube section 24 was substantially constant during the entire process, and the flow of fluidizing air supplied to the plenum chamber 13 was approximately the same so that half of the air supplied to the fluidized bed chamber 18 was fed through the tube section 24 and half of the air was fed through the plenum chamber 13.
  • Fig. 7 is a graphical representation showing the concentra- tion of ethyl alcohol in the air exhausted through the outlet 17 and plotted versus the processing time in the fluidized bed apparatus.
  • the lower explosion limit for ethanol at 33.000 ppm and a safety level at 8250 ppm are indicated by broken lines 32 and 33, respec- tively. From Fig. 7 it is apparent that the concentration of alcohol in the exhaust air did not exceed the safety level 33 during processing in the fluidized bed apparatus.
  • the arrows 34 and 35 indicate the start of supplying fluidi ⁇ zing air and the time where fluidization has been obtained, respectively *
  • the graph B in Fig. 8 shows the calculated concentration profile of ethanol in the discharge air during processing. It is noted that during the first few minutes of the processing the concentration of ethanol exceeds the lower explosion limit 32, and the concentration of ethanol is above the safety level 33 indicated in Fig. 7 during the complete processing.
  • the temperatures and the amounts of dilution and fluidizing air or gas supplied may be controlled so as to maintain the concentration of the in- flammable component below a desired level while at the same time obtaining the best possible processing conditions from an economic point of view.
  • the cross-sectional shape of the fluidized bed chamber 18 may have any round or elongated shape, such as square, rectangular, elliptical, etc.
  • the central tube section 24 may then be replaced or supplemented by two or more such tube sections arranged centrally or along one or two symmetry axes of the chamber cross-section.
  • Such tube sections 24 may also be combined with peripheral openings 22 as shown in Fig. 1.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention se rapporte à un appareil de traitement de matières particulaires contenant un composé inflammable tel que de l'éthanol ou un autre solvant. Ledit appareil se compose d'une chambre à lit fluidisé (18) dans laquelle est disposée une plaque d'assise (11). On peut fluidiser les matières particulaires sur la plaque d'assise (11) en envoyant de l'air de fluidification vers le haut, par des perforations pratiquées dans la plaque d'assise (11). Afin d'éliminer le risque d'explosion dans l'air de fluidification après qu'il soit passé dans le lit fluidisé (19) formé sur la plaque d'assise (11), l'appareil comprend des moyens (20) d'alimentation de la chambre à lit fluidisé (18) en gaz de dilution. Le gaz de dilution est introduit dans la chambre à lit fluidisé au moins en un point, à une certaine distance des parois latérales de la chambre, situé de préférence au centre de la chambre à lit fluidisé (18) de manière à obtenir un mélange homogène du gaz de dilution avec l'air de fluidification contenant le composé inflammable, immédiatement au-dessus du lit fluidisé (19). Le mélange gazeux non explosif peut ensuite être évacué par la partie supérieure de la chambre de traitement.
PCT/DK1993/000181 1992-06-05 1993-05-25 Procede et appareil de traitement de matieres particulaires dans une chambre a lit fluidise WO1993025303A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AU43098/93A AU4309893A (en) 1992-06-05 1993-05-25 A method and an apparatus for processing a particulate material in a fluidized bed chamber
PCT/DK1993/000181 WO1993025303A1 (fr) 1992-06-05 1993-05-25 Procede et appareil de traitement de matieres particulaires dans une chambre a lit fluidise

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US07/894,747 1992-06-05
PCT/DK1993/000181 WO1993025303A1 (fr) 1992-06-05 1993-05-25 Procede et appareil de traitement de matieres particulaires dans une chambre a lit fluidise

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Publication Number Publication Date
WO1993025303A1 true WO1993025303A1 (fr) 1993-12-23

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AU (1) AU4309893A (fr)
WO (1) WO1993025303A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0696471A1 (fr) * 1994-08-11 1996-02-14 Glatt Maschinen- und Apparatebau AG Procédé et installation pour déplacer des matériaux particulaires

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1365137A (en) * 1970-12-16 1974-08-29 Metallgesellschaft Ag Process for thermally treating fine grained solids in an internal ly heated fluidized bed
US4305210A (en) * 1976-12-01 1981-12-15 A/S Niro Atomizer Apparatus for processing a powdered or particulate product

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1365137A (en) * 1970-12-16 1974-08-29 Metallgesellschaft Ag Process for thermally treating fine grained solids in an internal ly heated fluidized bed
US4305210A (en) * 1976-12-01 1981-12-15 A/S Niro Atomizer Apparatus for processing a powdered or particulate product

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0696471A1 (fr) * 1994-08-11 1996-02-14 Glatt Maschinen- und Apparatebau AG Procédé et installation pour déplacer des matériaux particulaires
US5693362A (en) * 1994-08-11 1997-12-02 Glatt Maschinen-Und Apparatebau Ag Process and apparatus for moving and treating a particulate material

Also Published As

Publication number Publication date
AU4309893A (en) 1994-01-04

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