EP0120342B1 - Verfahren und Vorrichtung zur Erzeugung eines massenstrom- oder volumenstromkonstanten Gas-Feststoffteilchen-Freistrahls bestimmter Geschwindigkeit - Google Patents

Verfahren und Vorrichtung zur Erzeugung eines massenstrom- oder volumenstromkonstanten Gas-Feststoffteilchen-Freistrahls bestimmter Geschwindigkeit Download PDF

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Publication number
EP0120342B1
EP0120342B1 EP84102247A EP84102247A EP0120342B1 EP 0120342 B1 EP0120342 B1 EP 0120342B1 EP 84102247 A EP84102247 A EP 84102247A EP 84102247 A EP84102247 A EP 84102247A EP 0120342 B1 EP0120342 B1 EP 0120342B1
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EP
European Patent Office
Prior art keywords
metering
priority
metering groove
groove
flow
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.)
Expired - Lifetime
Application number
EP84102247A
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German (de)
English (en)
French (fr)
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EP0120342A2 (de
EP0120342A3 (en
Inventor
Kurt Prof. Dr.-Ing. Leschonski
Stefan Dipl.-Ing. Röthele
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Sympatec System Partikel Technik GmbH
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Sympatec System Partikel Technik GmbH
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Priority to AT84102247T priority Critical patent/ATE55556T1/de
Publication of EP0120342A2 publication Critical patent/EP0120342A2/de
Publication of EP0120342A3 publication Critical patent/EP0120342A3/de
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F15—FLUID-PRESSURE ACTUATORS; HYDRAULICS OR PNEUMATICS IN GENERAL
    • F15D—FLUID DYNAMICS, i.e. METHODS OR MEANS FOR INFLUENCING THE FLOW OF GASES OR LIQUIDS
    • F15D1/00—Influencing flow of fluids
    • F15D1/08—Influencing flow of fluids of jets leaving an orifice
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B05—SPRAYING OR ATOMISING IN GENERAL; APPLYING FLUENT MATERIALS TO SURFACES, IN GENERAL
    • B05B—SPRAYING APPARATUS; ATOMISING APPARATUS; NOZZLES
    • B05B7/00—Spraying apparatus for discharge of liquids or other fluent materials from two or more sources, e.g. of liquid and air, of powder and gas
    • B05B7/14—Spraying apparatus for discharge of liquids or other fluent materials from two or more sources, e.g. of liquid and air, of powder and gas designed for spraying particulate materials
    • B05B7/1404—Arrangements for supplying particulate material
    • B05B7/1477—Arrangements for supplying particulate material means for supplying to several spray apparatus
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/30—Mixing gases with solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/40—Static mixers
    • B01F25/42—Static mixers in which the mixing is affected by moving the components jointly in changing directions, e.g. in tubes provided with baffles or obstructions

Definitions

  • the invention relates to a method and a device for generating a mass flow or volume flow constant gas-solid particle free jet of a certain speed in which the solid particles are completely and uniformly dispersed.
  • Metering-dispersing devices for the generation of mass flow constants, dispersed gas-solid particle free jets are required wherever the dry handling of stored fine particles requires that they first be mechanically picked up and then a basic operation, which requires a defined dispersion, mass flow or are to be supplied or metered in at a constant volume flow.
  • Examples of such technical applications are the charging of air classifiers, the generation of gas-solid two-phase flows, the measurement of particle size distributions from the analysis of field effects in the gas-solid free jet, mechanical coating processes in which e.g. a gas-solid jet with a predetermined mass flow and defined particle velocities is to be supplied to a surface prepared for melting, and the generation of test aerosols.
  • the particle size range which requires measures to disperse the particles, starts at about 50 ⁇ m.
  • the measures become more demanding with increasing fineness, because the adhesive forces between the particles increase with decreasing particle size.
  • the invention has for its object to provide a method and a device with which a gas-solid particle free jet with completely dispersed particles under about 50 pm to a few pm can be generated with a mass flow or volume flow constant across the cross section.
  • the method according to the invention comprises several steps.
  • a compressed solid particle mass flow of constant cross section is first generated and then completely absorbed by a gas in a closed flow channel.
  • the solid particles are accelerated and completely dispersed and then the gas-solid particle mixture formed is released as a free jet from the flow or dispersion channel.
  • the invention provides that the gas / solid particle mixture is directed several times against an impact surface before being discharged from the flow channel. In this way, the particle agglomerates are safely separated into their individual particles and immediately taken up again by the gas stream, so they cannot separate or separate. However, the particles are not crushed.
  • a preferred embodiment of the method provides that the mixture is directed along a zigzag path before being discharged from the flow channel against impact surfaces.
  • the gas-solid particle mixture can also or additionally be directed via a baffle cascade consisting of several baffles which are inclined alternately to one or the other side.
  • the invention proposes a metering-dispersing device for generating a mass flow or volume flow constant gas-solid particle free jet of a certain speed, a metering device for the solid particles to be metered for generating a volume flow or mass flow constant solid particle flow and a flow channel with injector , which receives the solid particle stream emitted by the metering device with a suction mouth and which has a dispersing device behind the injector in front of an outlet nozzle for the gas-solid particle mixture.
  • several baffles which are successively hit by the gas / solid particle mixture, are provided in the dispersing device in front of the outlet nozzle.
  • the baffles are preferably arranged in the form of a baffle cascade with a zigzag contour.
  • the contour can be asymmetrical.
  • the baffles are expediently roughened somewhat in order to promote a bounce in different directions, and a straight channel section is formed as an acceleration section between the baffle surfaces and the outlet nozzle.
  • a further embodiment of the device provides that the injector of the flow channel has a central tube within a propellant gas chamber surrounding it, which is spaced apart a narrowing inlet nozzle opens into an annular gap, behind which the dispersion unit with the baffles is arranged.
  • the distance between the mouth of the central tube and the inlet nozzle is preferably variable from a few millimeters to a few tenths of a millimeter.
  • the central tube can be held to be longitudinally displaceable. The degree of dispersion of the particles in the gas stream can thus be changed and adjusted before hitting the impact surfaces.
  • the uptake of the compressed particles into the suction mouth of the flow channel is expediently supported by a mechanical predispersion device, in particular in the form of a rotating brush, to which a gas supply is optionally assigned.
  • the metering device has a metering groove which can be rotated about an axis and has the cross section of the solid particle mass flow to be produced, to which the solid particles can be supplied in excess from a dispersing device, in particular with a vibrating conveyor trough, the delivery point of which is arranged at a distance above the metering groove.
  • a stripping device arranged downstream of the dispensing point of the metering device in the direction of rotation of the metering groove, the distance of which from the metering groove can be adjusted to remove excess solid particles in a defined manner
  • a compacting device arranged downstream of the metering groove of the stripping device, in particular a press roller which distributes the solid particles evenly and easily into the metering groove condensed.
  • the suction port of the flow channel plunges into the metering groove in the direction of rotation of the metering groove behind the compression device.
  • the dosing groove can be located in differently designed carriers.
  • the metering groove is designed to be open at the top in the top of a turntable rotatable about a vertical axis of rotation.
  • the metering groove is located at the edge of the turntable, preferably in a wide ring protruding upwards.
  • the metering groove is formed in the outside of an endless conveyor belt rotating around two horizontally spaced deflection rollers and the stripping device, the compression device and the suction port of the flow channel interact with the upper horizontal belt section, for which purpose Deflection pulleys are at a sufficient distance or the conveyor belt is of sufficient length.
  • the metering groove is formed in the inside of a wheel rim which is rotatable about a horizontal axis of rotation and faces the axis of rotation.
  • the wheel rim can be driven at such a high speed that the added solid particles are completely held in the metering groove due to the centrifugal force. They can then be removed from this at any point, directly or with the predispersion device.
  • the wheel rim can also be driven at a somewhat lower but still so high speed that the solid particles are carried along to approximately the apex and detach from the dosing groove when the apex is reached and are passed directly into the suction mouth of the flow channel.
  • the wheel rim can be driven at a somewhat lower but still so high speed that the solid particles fall back cataract-like well before reaching the apex and fall freely out of the metering groove into a collecting funnel at the suction mouth of the flow channel.
  • the metering groove is provided with transverse ribs to support the conveyance of the solid particles.
  • the material or the solid particles can be fed to the turntable, which can be rotated about a vertical axis of rotation, using a conventional mechanical metering device via a conveyor trough, in particular an oscillating conveyor trough.
  • This type of feed is also possible in the metering groove provided on the inside of a wheel rim.
  • a fluidized bed device is used for this purpose, in the fluidized bed chamber which is open at the top, the wheel rim is immersed with a lower segment so far that the metering groove fills from the side.
  • predispersion is already achieved in the fluid bed.
  • the two embodiments with the metering groove on the inside of a wheel rim and on the outside of a conveyor belt have the advantage that they are narrow transversely to the direction of movement of the metering groove and therefore several devices can easily be combined to form multiple arrangements in order to provide a wide, but in the To produce a high level of continuous gas-solid flat jet.
  • One embodiment of these two devices therefore provides that, in order to generate such a wide free jet or flat jet, a plurality of metering and dispersing devices are arranged in parallel next to one another in such a way that the emerging free jets unite to form a wide flat jet at a certain distance from the outlet plane of the outlet nozzles . With such a device, exactly continuous coatings can be achieved over large widths.
  • the flow channel consisting of suction channel, injector and baffle cascade is flat, ie the channel is not circular in cross section but rectangular with the width and the low height of the flat jet to be generated.
  • the material is fed into the suction mouth of the flow channel directly from a fluidized bed channel, the length of which corresponds to the width of the suction channel.
  • the fluidized bed channel is an elongated channel open at the top, the upper part of which is separated from the lower part into which the fluid (gas or air) is introduced by a sieve to be flowed upwards.
  • the lower edge region of the fluidized bed channel has an elongated slot or a slot-shaped opening in one side wall through which the predispersed particles are sucked directly into the suction mouth of the flow channel.
  • the outlet nozzle of the baffle cascade leaves a wide flat jet that is homogeneous immediately after the outlet.
  • a cylindrical metering brush or roller the distance of which from the opposite wall can be adjusted, in the suction mouth of the flow channel for setting the emerging particle stream.
  • a metering device comprises a turntable 10 which can be rotated about a vertical axis and which on the outer edge forms an upwardly open annular metering groove 2 with a sharp-edged crown in an upwardly projecting rim Has.
  • This is fed from an oscillating conveyor trough 1 to a vibration metering device 22, see FIGS. 2 to 4, in excess of a constant solid particle mass or volume flow, which is improved with regard to its constancy by further measures on the turntable.
  • the turntable 10 On the inside of the metering groove 2, the turntable 10 has elongated openings 32 between radial webs 33, see FIGS. 3 and 5. In this way, excess material, as well as material discharged by a cleaning brush 19, can fall to both sides of the metering groove 2 and into one Overflow funnel 23 and out of this into a collecting vessel 24, see FIG. 4.
  • the bulk material cone resulting from the laterally flowing excess on the metering groove 2 rotating under the vibrating conveyor trough 1 is first sheared to a preselected bed height with a scraper device 3 with a scraper blade 36, which is shown in detail in FIG. 6, and then with a fixed bed height Compacting device 4 in the form of a rotatable, by its own weight pressing roller 4 ', which shows in detail in Fig. 7, so far on the same bulk properties easily and evenly compressed that the cross section of the metering groove 2 is completely and evenly filled.
  • a rotating cylindrical brush 5 ' is provided in the direction of movement of the metering groove 2 behind the press roll 4' as a predispersion device 5, in particular for goods which are difficult to flow.
  • This is encapsulated in a housing 43, to which air can be directed through an air supply 40.
  • the previously homogenized constant solid particle mass flow 8 is whirled up from the metering groove 2 into the suction mouth of a flow channel connected to its housing 43 in the area of the brush 5 'via a suction mouthpiece 42 in front of a damming weir 41 reaching into the metering groove 2 and completely from the suction mouthpiece picked up and vacuumed. In this way, the solid particles are constantly metered into the flow channel.
  • the flow channel consists of a suction channel 6, an injector 9 and a baffle cascade 15 with an outlet nozzle 16.
  • the injector shown in FIG. 12 has a longitudinally adjustable, conically tapering central tube 11 in a hollow cylindrical housing 26 with an end cover 27, through which the gas-solid mixture sucked out of the metering groove 2 is fed into and discharged into an inlet nozzle 13 formed in front of its mouth.
  • the mouth of the central tube 11 forms an annular gap 12 with the inlet nozzle 13.
  • propellant gas inlet openings are formed in the propellant gas chamber 28 formed between the inner wall of the housing 26 and the outer wall of the central tube 11 before the mouth of the central tube 11 in the wall of the housing 29 provided.
  • a baffle cascade 15, according to FIG. 13, is connected directly to the injector 9 for complete deagglomeration by means of targeted particle wall collisions.
  • This has a straight mixing channel 14 on the inlet side.
  • This is followed by a flat or rotationally symmetrical zigzag-shaped channel piece made of successively arranged, zigzag-shaped baffles 17, which are set at an angle of 20 ° to 70 ° against the main flow direction.
  • baffle cascade 15 They prevent unhindered passage of the solid particles in that they protrude at least as far into the free outlet cross section of the mixing channel 14 that the particles flowing into the baffle cascade 15 do not find any free, unimpeded flow through the cascade under imaginary axial movement and large agglomerates break open inevitably against wall impacts while finely dispersed and fine particles tend to flow around the impact surfaces.
  • the gas-solid flow leaves through a channel section 18 as an acceleration section, in which the dispersed solid particles are accelerated to almost the same final speed, and the outlet nozzle 16 leaves the baffle cascade 15 and thus the (dispersion) ) Flow channel as free jet 7.
  • the dispersion begins when the solid mass flow 8 is taken up in the injector 9.
  • the suction of the solid particles from the metering groove 2 of the turntable 10 and the increasing acceleration and mixing with transport air as it passes through the suction channel 6 and the injector 9 leads to a separation and separation of the solid particles and agglomerates.
  • the propellant gas volume flow V T flowing through the annular gap 12 with an admission pressure PT of up to 10 bar induces a suction flow V s in the central tube 11 of the injector 9.
  • the gap between the mouth of the central tube 11 and that which can be set to gap widths s from a few millimeters to tenths of a millimeter Inlet nozzle 13 acts on the propellant gas volume flow like a throttle.
  • the particle-laden propellant gas flow in the subsequent mixing duct 14 accelerates to high speeds, so that on the one hand the negative pressure required for the suction power of the suction duct 6 arises and on the other hand the flow forces in the shear flow in the annular gap 12 create a shear stress on the solid particles present in the form of agglomerates cause that lead to dispersion.
  • 9 wall and particle impacts on the entire pneumatic conveying path up to the outlet from the injector cause additional dispersion.
  • a targeted dispersing effect due to wall joints at defined angles between 20 ° and 70 ° is only achieved in the baffle cascade 15 connected downstream of the injector 9 before leaving its outlet nozzle 16.
  • the flow velocities within the injector 9 and the baffle cascade 15 always remain below 100 m / s, so that in the specified particle size range up to about 50 ⁇ m no comminution, but only dispersion, is brought about.
  • Dispersing devices in which the particles only flow through the shear gradient of an injector and / or through a straight tube do not achieve a degree of dispersion of more than 80%.
  • baffles 17 The arrangement of three baffles 17 has been found to be the optimum. In a sufficiently large setting range of gap width s and pre-pressure p T , the almost complete dispersion with values between 97% and 100% can be ensured.
  • the operation of the device can be seen from the following example.
  • the achievable solid mass flow is primarily determined by the speed of the turntable 10, which can be up to 100 rpm, the diameter and the cross section of the metering groove 2.
  • Our own studies have shown that commercially available fine limestone at 10 rpm and a diameter of 20 cm and a cross section of the metering groove of 12 mm 2 can be achieved with a mass flow of 10 kg / h and a mass flow fluctuation of less than 4%.
  • the metering device 22 is metered in excess up to three times the amount. Two thirds initially remain on and in the metering groove 2.
  • the stripping device 3 reduces the predominant part of the resulting bulk material cone during the first equalization, while the press roll 4 'only results in a slight reduction in the compression.
  • Geometric enlargements or reductions in the cross section of the metering groove 2 and the dimensions of the turntable 10 allow adaptation to larger or smaller mass flow ranges.
  • FIGS. 2 to 4 show views of a metering-dispersing device 30 which, as a compilation of the devices for generating a gas-solid free jet, e.g. is used for the dry analysis of diffraction spectra to determine the particle size distribution from the swarm of solid particles.
  • the disperse material to be analyzed is placed in a storage or feed hopper 21 of the metering device 22 and flows via its vibrating conveyor trough 1 onto the metering groove 2 of the turntable 10.
  • the direction of movement on the predispersion device 5 is approximately the same as the suction direction in the suction channel 6.
  • FIG. 5 shows, as a construction detail, the cross-sectional area 31 of the metering groove 2 of the turntable 10 and the spoke construction with elongated, curved openings 32 between radial webs 33 of the turntable 10, which is perforated to expel the excess.
  • the steep side walls 34 which converge at the upper edge of the metering groove 2 the metering groove 2 ensure an unimpeded discharge of the excess and a defined unwinding option for the press roll 4 'for the compression, without a second, undesirable solid bed being able to form on the end faces of the side walls 34 of the metering groove 2.
  • FIG. 6 shows, in an enlarged representation, the scraper device 3 from a pivotable, rotatable blade holder 35 with a scraper blade 36, which can be variably locked in the angle of attack.
  • a compacting device 4 is shown with a massive press roll 4 'high weight with adjustable compression spring 37 to determine the compression conditions.
  • the press roll 4 ' is mounted in a bracket which is guided in a stationary manner by means of a vertical rod 38 and is supported on the compression spring 37 by means of a nut 39 screwed to its end, which in turn rests on a wall of a housing or mounting bracket (not shown).
  • a predispersion device 5 is shown in the form of the rotating brush 5 '.
  • the rotating brush 5 ' is rotatably installed in the housing in such a way that it extends fully into the metering groove 2 and receives the goods transported in its direction of rotation.
  • the air supply 40 ensures that the suction channel 6 connected via the suction nozzle 42 receives the material pre-dispersed in sufficient air just above the upper edge of the metering groove.
  • the back-up weir 41 which closes the cross section of the metering groove 2, is provided on the housing 43 in the direction of movement of the metering groove 2 behind the mouth of the suction mouthpiece 42, which together with the brush ensures the constant transfer of the mass flow into the suction mouthpiece 42.
  • a larger air supply and a suction mouthpiece 42 directly associated with the metering groove 2 are dispensed with.
  • the suction channel 6 is connected near the upper apex of the brush 5 ', so that the material is first lifted out of the metering groove for predispersion.
  • the brush 5 ' rotates counter to the transport direction of the solid mass flow and causes a deflection and raising to the level of the suction channel 6 supported by the air drawn in.
  • the suction of the air takes place through the metering groove 2 emptied of the material, so that the absorption of the material is supported by the air flowing after it.
  • the housing 43 is encapsulated against external air and is placed in a largely sealing manner on the turntable 10 above the metering groove 2.
  • the cross section of the metering groove 2 of the turntable 10 can be adapted to the particle sizes distributions and to cover a wide mass flow range up to a few 10 kg / h have a size of a few mm 2 to a few cm 2 .
  • the metering device 22 can also have a screw conveyor, a fluidized bed channel or another known organ as the conveyor element in addition to a vibrating conveyor channel 1.
  • the metering groove 2 is provided on the outside of an endless, V-belt-shaped conveyor belt 58 which runs around two deflecting rollers 59 arranged at a horizontal distance.
  • the deflection roller 59 on the right in the illustration is driven by a motor, not shown.
  • the conveyor belt has a horizontally running upper belt section and a parallel lower belt section. At the left end of the upper belt section, the vibrating conveyor trough 1 of the metering device 22 opens and, above the metering groove 2, enters the material to be metered in excess.
  • steel strips 61 or other stabilizing protective parts are inserted into these.
  • the excess material removed from the dosing groove 2 again falls into a common overflow funnel 60 and is fed back to the feed material funnels 21 of the dosing devices 22.
  • the mutual distance between the plurality of devices 50 results from the exit angle of the free jets 7 and the distance between the working plane 54 of the wide flat jet 53 and the outlet plane 55 of the outlet nozzles 16.
  • the metering groove 2 is provided in the inside of a wheel rim 63 of a wheel which can be rotated about a horizontal axis of rotation, with spokes 65 tapering obliquely onto a hub 64.
  • the wheel rotates around a horizontal axis; the wheel rim 63 is thus vertical.
  • the material can in turn be fed into the metering groove 2 in the region of the lowest point by means of a vibrating conveyor trough.
  • a task is preferred here by means of a fluidized bed device 66 which has a box 67 which is open at the top and whose lower part is separated from the upper part by a sieve 68.
  • the lower part is designed as an air box, into which air inlets 69 open laterally.
  • the material to be fed is added to the top of the screen 68 in a known manner.
  • a fluidized or fluidized bed forms above the screen 68.
  • the assignment of the fluidized bed device 66 to the wheel rim 63 is such that it immerses in the fluidized bed 71 with a lower segment 70.
  • the particles can enter the metering groove 2 from the side and fill it. Since the wheel rim rotates at a higher speed and the metering groove 2 is equipped on the inside with ribs 72 to promote the carry-along of the goods, the goods are lifted out of the fluidized bed.
  • the speed is chosen to be lower so that the material is released from the metering groove 2 before the upper apex and in free fall as a mass flow of solid particles 76 into a collecting funnel 77 of the intake duct 6 falls into it.
  • the stripping device 3, the compression device 4 and the predispersion device 5 can be arranged on the inner radius over the entire circumference of the wheel rim 63, in special cases also the removal with the suction channel 6 without predispersion device 5 and in particular at the apex Handover under gravity can take place in free fall.
  • the "cataracting" behavior of an incompletely centrifuged material known from tube mills, granulation plates and the like can be used in order to take over the solid particle mass flow 76 in free fall even in the case of detachment before reaching the apex in the collecting funnel 77.
  • the ribbing of the metering groove 2 is then particularly expedient, if not necessary, for forced delivery from the fluidized bed.
  • the goods can be transferred to the horizontal injector 9 both parallel and normal to the axis of rotation of the wheel rim 63.
  • the face of the wheel rim facing the injector 9 must remain freely accessible so that the drive is to be moved to the opposite side and out of the area of the Fluid bed is to be brought out.
  • the oblique spokes 65 serve this purpose.
  • a plurality of metering-dispersing devices 75 can be arranged coaxially with one another, so that in turn common drive shafts 73 for all wheel rims 63 and common drive shafts 74 for the press rolls and optionally brushes can be provided, as shown in FIG 22 is shown.
  • common drive shafts 73 for all wheel rims 63 and common drive shafts 74 for the press rolls and optionally brushes can be provided, as shown in FIG 22 is shown.
  • the distance between the individual devices 75 the same considerations apply as for the multiple arrangement according to FIG. 17.
  • a metering and dispersing device can also be used to generate a wide flat jet, in which the feed of a mass or volume flow constant solid-particle flow directly into a so-called plane, i.e. elongated flat flow channel takes place from the width of the flat jet 53 to be generated.
  • the suction channel 6 of the flow channel which is formed in a block 80 parallel to a fluidized bed channel 81 of the metering device fed by a metering device (not shown), the injector 9 and the baffle cascade 15 of the flow channel are each flat, i.e. linearly elongated of the width and proportional to the height of the flat jet 53 to be generated, as shown in FIG. 23 schematically.
  • An elongated fluidized bed channel 81 into which a metering device feeds the material, is connected upstream of the flow channel for a mass or volume flow constant feed.
  • a sieve 82 At the bottom right-hand edge of the fluidized bed 83 which is set in operation in FIG. 23 there is a slot-shaped outlet opening 85 just above the sieve 82, to which the suction channel 6, which is curved downward in the exemplary embodiment shown, is connected.
  • a cylindrical metering brush 86 which could be replaced by a metering roller, is provided in the lower wall of the suction channel at the suction mouth. its distance a to the opposite wall in FIG. 23 of the flat suction channel 6 and / or its speed can be adjusted to control the particle stream emerging from the fluidized bed 83. A good excess metering on a rotating metering groove according to the other exemplary embodiments is omitted in this embodiment.
  • a uniform, mass or volume flow constant flow of material can be removed from the fluid bed 83. It is sucked in directly by the suction channel 6 and dispersed in the flat injector 9 and the downstream flat baffle cascade 15. The resulting wide flat jet 53 is then homogeneous immediately after it emerges from the outlet nozzle 16.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Dispersion Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Nozzles (AREA)
  • Weight Measurement For Supplying Or Discharging Of Specified Amounts Of Material (AREA)
  • Air Transport Of Granular Materials (AREA)
EP84102247A 1983-03-02 1984-03-02 Verfahren und Vorrichtung zur Erzeugung eines massenstrom- oder volumenstromkonstanten Gas-Feststoffteilchen-Freistrahls bestimmter Geschwindigkeit Expired - Lifetime EP0120342B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT84102247T ATE55556T1 (de) 1983-03-02 1984-03-02 Verfahren und vorrichtung zur erzeugung eines massenstrom- oder volumenstromkonstanten gasfeststoffteilchen-freistrahls bestimmter geschwindigkeit.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3307406 1983-03-02
DE3307406 1983-03-02

Publications (3)

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EP0120342A2 EP0120342A2 (de) 1984-10-03
EP0120342A3 EP0120342A3 (en) 1987-08-19
EP0120342B1 true EP0120342B1 (de) 1990-08-16

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US (2) US4573801A (OSRAM)
EP (1) EP0120342B1 (OSRAM)
JP (1) JPS6012165A (OSRAM)
KR (1) KR930002494B1 (OSRAM)
AR (1) AR242002A1 (OSRAM)
AT (1) ATE55556T1 (OSRAM)
BR (1) BR8400978A (OSRAM)
DD (1) DD212653A1 (OSRAM)
DE (1) DE3482967D1 (OSRAM)
RU (1) RU1787263C (OSRAM)
ZA (1) ZA841337B (OSRAM)

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US4945050A (en) * 1984-11-13 1990-07-31 Cornell Research Foundation, Inc. Method for transporting substances into living cells and tissues and apparatus therefor
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US4660986A (en) 1987-04-28
ATE55556T1 (de) 1990-09-15
ZA841337B (en) 1984-10-31
KR930002494B1 (ko) 1993-04-02
JPS6012165A (ja) 1985-01-22
DD212653A1 (de) 1984-08-22
EP0120342A2 (de) 1984-10-03
US4573801A (en) 1986-03-04
EP0120342A3 (en) 1987-08-19
JPH0380071B2 (OSRAM) 1991-12-20
AR242002A1 (es) 1993-02-26
RU1787263C (ru) 1993-01-07
KR840007940A (ko) 1984-12-11
BR8400978A (pt) 1984-10-09
DE3482967D1 (de) 1990-09-20

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