US3652131A - Method for dividing a main stream of particles into part streams and apparatus for carrying out the method - Google Patents

Method for dividing a main stream of particles into part streams and apparatus for carrying out the method Download PDF

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US3652131A
US3652131A US865759A US3652131DA US3652131A US 3652131 A US3652131 A US 3652131A US 865759 A US865759 A US 865759A US 3652131D A US3652131D A US 3652131DA US 3652131 A US3652131 A US 3652131A
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particles
chamber
rotor
stream
outlet
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Bengt J Carlsson
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Motala Verkstad AB
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Motala Verkstad AB
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B27—WORKING OR PRESERVING WOOD OR SIMILAR MATERIAL; NAILING OR STAPLING MACHINES IN GENERAL
    • B27N—MANUFACTURE BY DRY PROCESSES OF ARTICLES, WITH OR WITHOUT ORGANIC BINDING AGENTS, MADE FROM PARTICLES OR FIBRES CONSISTING OF WOOD OR OTHER LIGNOCELLULOSIC OR LIKE ORGANIC MATERIAL
    • B27N3/00—Manufacture of substantially flat articles, e.g. boards, from particles or fibres
    • B27N3/08—Moulding or pressing
    • B27N3/10—Moulding of mats
    • B27N3/14—Distributing or orienting the particles or fibres

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  • ABSTRACT I A method and apparatus for transforming a constant main [30] Foreign Application Priority Data stream of particles into a particle web having a uniform mass particle distribution which varies in a desired manner transw 'f "14265/68 versely of the web by directing the main stream into an annuzlar chamber against a rotating member concentric within the [52] "3o2/28222/330 chamber. The rotating member distributes the main stream "B653 53/04 about the chamber and the particles pass out through a plurality of outlets opening along a plane in the chamber which is i -normal to the longitudinal axis of the chamber.
  • volumetric division which is relatively simple and inexpensive method, provides in the majority of cases good division of material comprising particles of relatively concentrated and stable form sufficient for practical purposes, even though the shape and size of the particles may vary, e.g. such as with sand and like material, if it can only be effected so that a screening effect is avoided.
  • volumetric division provides relatively unsatisfactory results.
  • dividing the main stream into a number of part streams it is usual to lead the main stream to a bunker, from which the desired part streams are proportioned individually.
  • this method becomes expensive and requires the use of much too complicated apparatus.
  • volumetric division is also applied in the case of materials for which it is not suited, with the result that the accuracy of division is not as good as would be desired.
  • the time taken for the particles to pass through the fluid filled space varies greatly about the average value with the properties of the fluid and the particles.
  • the aforesaid variation is substantially caused by variations in the resistance thereof. This resistance is high for rod shaped or flat particles and decreases successively with increased compactness of the particles.
  • the fluid resistance does not vary at all with the orientation of the particle, and the aforesaid variation about the average value is small.
  • the present invention is based on these known conditions and its prime object is to provide for the division of a constant main stream of particles into part streams in accordance with arbitrary wishes and in such a manner that the composition of particles in the part streams is practically the same as in the main stream, and that the flow per unit of time of each part stream comprises a practically constant portion of the flow of the main stream, irrespective of the magnitude of said main stream.
  • the object of a further development of the invention is to form a web of particles from the particle stream, in which the lateral distribution thereof substantially coincides with a certain desired degree of distribution.
  • the main stream is first transformed into a tubular flow of particles being passed axially through a chamber which is substantially in the form of a rotation body and is filled with a fluid, and in which the fluid is maintained in rotation around the axis of the chamber, and in that the tubular stream of particles is then divided circumferentially by being passed into an outlet arranged concentrical with the chamber and which at the periphery thereof is divided peripherally into part outlets.
  • FIGS. 1 and 2 schematically illustrate an apparatus by which the method of the invention can be carried out.
  • FIG. ll shows a vertical section through the apparatus and
  • FIG. 2 a horizontal section taken through the line 2-2 in FIG. I seen in plan.
  • FIGS. 3 and 4 show in vertical section two apparatus embodying the concept of the invention and suited for practical use in dividing a stream of particles into part streams intended for two different types of particles.
  • FIG. 5 shows in side view and partly cut away an apparatus according to the invention for forming a web of particles from the particle stream.
  • FIG. 1 shows a housing 11 in the form of a cylinder having a vertical axis and the two ends of which are closed.
  • a housing 11 in the form of a cylinder having a vertical axis and the two ends of which are closed.
  • an inlet 13 through which a main stream M of particles is passed to a cylindrical chamber 15 enclosed by the housing 11'.
  • the lower portion of the housing is formed as an outlet portion 16.
  • the inner portion of the housing is divided into sectors by means of a number of radial walls 17 (see FIG. 2) all of which terminate at the top thereof in one and the same plane 18 extending at right angles to the cylinder axis.
  • the bottom of the walls 17 are connected to the lower cylinder end wall 19.
  • each part outlet is provided with an exit 21 and the lower end wall 19 is designed (in a manner not specifically shown) so that the particles cannot collect in the part outlet 20, but that the particles which arrive in a part outlet 20 pass continuously out through its exit 21 in the form of a part stream 22 of particles.
  • the chamber 15 is filled with a suitable fluid, which is held in constant rotation around the axis of the chamber by appropriate means (not shown in the drawing).
  • a suitable fluid which is held in constant rotation around the axis of the chamber by appropriate means (not shown in the drawing).
  • the particles in the main flow 14 enter the chamber 15 they are imparted a rotary movement by the fluid rotating in the chamber about the axis of said chamber simultaneously as they fall down through the chamber axially thereof as a result of gravity. They are held at the outer diameter of the chamber by the influence of centrifugal force.
  • the particles will therefore pass through the chamber 15 along essentially helical paths which, for natural reasons, obtain on average different pitch angles for particles of different types, but which for identical particles obtain individually different, haphazardly varying pitch angles.
  • the tangential velocity of the particles will also vary haphazardly around an average value, as a result of turbulence in the fluid, collisions and frictions etc., although this variance at fairly high tangential velocities of the fluid should be relatively much lower for the tangential velocity of the particles than for their axial velocity.
  • the two velocity vectors therefore vary haphazardly each per se, and the pitch angles of the particle paths vary purely haphazardly.
  • Particles which arrive in the chamber at one and the same position, at the inlet 13, and follow paths having different pitch angles, defined purely by chance, will adopt peripheral positions determined by these haphazardly determined angles when they pass one and the same section of the chamber.
  • An example is given in FIGS. 1 and 2 of how a particle which follows a gentle path 23 has reached the peripheral position 24 as it passes section 18, while another particle, which follows a steeper path 25, has reached the periphal position 26 as it passes the same section.
  • the constant tubular flow of particles is divided into desired part flows 22 at the outlet 16 beginning at section 18, the outlet 16 being divided into part outlets 20 in some suitable manner.
  • the described method and apparatus may also be used for dividing a certain restricted total quantity of particles into part quantities in a manner whereby the mass of each part quantity constitutes a specific portion of the mass of the total quantity and whereby the particle composition of each part quantity is the same as in the original total quantity, providing that the total particle number is sufficiently high. It is not necessary and not possible as a matter of fact to maintain constant the main stream 14, which is formed when the restricted total quantity of particles is emptied into the apparatus, and the part streams 22 will not therefore momentarily have either the correct mass or the correct particle composition, although when all the particles have passed through the apparatus the desired division has in any event been obtained.
  • the housing 11 need not be cylindrical, although it is essential that its inner surface is constructed as a rotary body on that portion of the surface which is contacted by the particles to prevent heaping.
  • the cylindrical surface of the rotary body should not at any part thereof form too large an angle to its axis and thereby causing the particles to tend to remain on said cylinder surface.
  • main stream 14 be introduced to the chamber 15 in the proximity of its periphery or in an axial direction, as shown in FIG. 1.
  • the main stream may be introduced at any radial distance from the axis of the chamber 15 and in any direction whatsoever, more or less axially, radially or tangentially.
  • main stream 14 be introduced at one single position 13, as described and illustrated in explaining the principle of the invention.
  • the stream is introduced to the chamber 15 as uniformly distributed around its perphery as possible, e.g. through an annular inlet arranged concentrically with the chamber and as uniformly distributed as possible beforehand around the periphery of the inlet.
  • the chamber 15 need not be completely free adjacent the axis of the chamber.
  • the fluid can also be held in rotation in another manner, e.g. by continuously introducing the fluid and passing it away from the chamber 15, the fluid being introduced at a suitable velocity in a tangential direction.
  • the packing material should also be in the form of a rotary body having the same axis as the inner surface of the housing 11, so that the chamber 15 obtains a cross section having the shape of a true circle.
  • a rotor adapted to maintain rotation of the fluid need not be constructed as a rotary body. However, it is most convenient to design such a rotor as a rotary body which fills the larger portion of the housing 11 radially, so that it forms an annular chamber 15 with relatively small radial extension between the housing 11 and the rotor.
  • the rotor may suitably be provided with low, preferably axial vanes, strips or other projecting members, thereby facilitating entrainment of the fluid.
  • the housing 11 If the housing 11 is surrounded by the same fluid with which the chamber 15 is filled, which is the case when the fluid is air, the housing 11 need not be closed at the ends thereof, but that the said chamber 15 can be made to communicate with the surrounding fluid in a suitable manner.
  • the outlet portion 16 may also be filled out in the centre thereof in a manner whereby said outlet obtains an annular cross section. Neither need the outlet begin at a plane perpendicular to the axis of the chamber, but that the inlet surface 18 of the outlet may have some other suitable configuration, such as conical, for example.
  • the essential feature is that the outlet is concentrical with the chamber 15.
  • the walls 17 which divide the outlet into part outlets need not be radial, but may extend in another direction, and the part outlets may be provided with suitably arranged partitions, in order to stop rotary movement of the particles.
  • the outlet is a sensitive portion of the apparatus. Small errors in design can, if no other measures are taken, lead to considerable error in the division of the main stream into part streams. It is obvious, for example, that if one wall projects up a little higher than the others and that if the particles at the same time meet the outlet in a very gentle path the said wall is liable to impede the part outlet 20 lying there beyond, causing it to receive too small a portion of the main stream 14. It is therefore suitable to brake the rotary movement of the particles as much as possible before said particles reach the inlet surface 18 of the outlet. Obviously the particles must be braked in a manner in which the haphazard distribution of the particles is not affected, i.e. in a manner whereby heaping and similar phenomenon are avoided. In the case of certain types of particles which show smaller tendency to agglomerate, braking can be effected essentially mechanically, e.g. by
  • the flow in the fluid is arranged so that it affects the particle distribution to the part outlet as little as possible, i.e. so that the axial flow velocity through the inlet surface 18 of the outlet is either practically the same at all part outlets Nor is sufficiently low to prevent particle distribution from being impaired to any great extent by varying velocities at the different part outlets.
  • FIG. 3 shows by way of an example, and greatly simplified, an apparatus according to the invention designed for use when there is need to convey the particles by means of the fluid.
  • Like parts in FIG. 3 are identified by the same reference numerals as those used in FIGS. 1 and 2.
  • the Figure illustrate a cylindrical housing 11 having a vertical axis and an outlet portion 16 arranged concentrically with and connected to the housing.
  • the outlet portion includes an annular outlet which is divided up in a desired manner into a number of part outlets 20 by means of partition walls 17 which begin at one and the same horizontal plane 18, said part outlet 20 each having its respective exit 21, and a center portion 28 concentric with the housing 11 and supporting two rotors 29 and 30 arranged within the housing concentrical therewith.
  • the lower rotor 29 is provided with a hollow shaft 31, which is journalled in a suitable manner direct to the frame 28 at 32 and 33, and the lower end of which is provided with a belt plate 34 or the like for driving the rotor 29 from a drive means (not shown) which is arranged in a foundation 35 (only a fragment being illustrated) on which the outlet portion 16 is erected.
  • the upper rotor 30 is provided with a shaft 36 which in turn is journalled in a suitable manner in the bore of the hollow shaft 31 at 3'7 and 38 and which at the bottom is provided with a belt plate 39 or the like for driving the rotor 30 from a drive means not illustrated in the drawing.
  • the rotors 30 and 29 and the center portion 28 of the outlet portion form together an essentially cylindrical filling structure in the center of the housing 11, so that an annular chamber 15 of circle ring shaped horizontal section is formed therebetween and the housing.
  • the upper rotor 30 rotates at a relatively high peripheral velocity and its purpose is to maintain rotation of the air in the upper portion of the annular chamber 115 above the axis of the chamber.
  • the rotor may suitably be provided with strips or vanes 40 extending substantially axially over the larger portion of the length of the rotor.
  • it may also be suitable to use instead of long vanes 40 short projections or vanes 41, separated by relatively large axial spaces, as shown to the right of the Figure.
  • These short vanes may suitably be placed obliquely in relation to each other, alternate vanes having a right hand pitch and a left hand pitch respectively.
  • the housing lll is provided at the top with an end wall 12 in the centre of which is provided a cylindrical inlet 42 through which a main stream 14 of particles is introduced from a feed means 43 (only graphically illustrated in the drawing).
  • an impeller 44 which is supported from the rotor 30 by means of a shaft 45.
  • the impeller 44 is struck by the main stream 14 and distributes the same towards the periphery of the inlet 42, as shown by dotted lines 46, which illustrates approximately how the stream of particles is distributed throughout the apparatus.
  • the main stream 14 roughly formed in the inlet 42 into a tubular shape then falls somewhat concentrically on the upper, slightly conically shaped end wall of the rotor 30, and is then passed under the influence of frictional forces, centrifugal forces, air forces and gravity, along force lines created along said end wall towards the periphery thereof.
  • the forces, with the exception of the gravity force line, acting on the separate particles are deter' mined more or less by chance, which means that the distribution of the particle stream circumferentially is improved during the passage over the end wall of the rotor 30, so that the stream of particles when it reaches the annular inlet 13 to the chamber 15 is relatively uniformly distributed circumferentially.
  • the end wall of the rotor 30 may be provided with projections in the form of pins, radial or spiral vanes or the like, thereby more rapidly to impart to the particles a rotary velocity and thereby prevent large collections of particles on the central portions of the end wall.
  • the particles then pass from the inlet 13 in helical paths down through the annular chamber 15, essentially through the outer portion thereof, whereupon the distribution of particles circumferentially becomes more and more uniform in the tubular particle stream 46 the farther the stream extends into the annular chamber, as described with reference to FIGS. 1 and 2.
  • the purpose of the lower rotor 29 is to brake the rotation of air in the lower portion of the annular chamber 15, and thereby brake the tangential velocity of the particles before they reach the outlet 16.
  • the rotor 29 therefore rotates in the opposite direction to rotor 30.
  • the rotor 29 may also be pro vided with substantially axially extending strips or vanes 47.
  • the dimensions and the speed of rotation thereof is adapted so that the air in the angular chamber 15 below the same rotates with a suitable low velocity in the same direction as the rotor, so that the paths of the particles are on average approximately vertical before they meet the outlet 16, in which the tubular particle stream 46 is divided in the desired manner in the part flows 22.
  • the radial spread of the particle stream is, in itself, unimportant but may vary with the size of the particle stream and should be taken into account when designing the part outlets 20.
  • the partition walls 17 between said outlets should be arranged so that a variation in the radial thickness of the tubular particle stream 46 at the inlet surface of the outlet does not afiect the division of said main stream into part streams.
  • the space between the end wall of the rotor 30 and the end wall 12 of the housing 11 is formed so that a fan effect is avoided to the highest possible extent, which would otherwise cause axial flow through the chamber 15 and through the part outlets and, via different flow resistances in the part outlets and the conduits connected thereto, affect division of the main stream 14.
  • the axial space between the two end walls is ample and the end wall 12 is provided on the inside thereof with radial walls or guide vanes 48, to brake any possible rotation of air therein which could give rise to radially acting pressure differences.
  • a circular opening 49 between the end wall 12 and the housing 11 to create, via the outer atmosphere, pressure equilization between the upper end of the chamber 15 and the outlet 21 of the part outlets, thereby preventing axial air flow into chamber 15.
  • FIG. 4 is another embodiment of an arrangement according to the invention which can be used in the case of particles whose falling velocity in air is low enough to render it suitable to transport the particles by means thereof.
  • the apparatus of FIG. 4 is very similar to the apparatus of FIG. 3, and like parts have been identified with like reference numerals in the two figures.
  • FIG. 4 illustrates a housing 11 having a vertical axis and an outlet portion 16 connected to the housing and which comprises an annular outlet divided into part outlets 20 and arranged concentrically with the housing and a central portion 28 which supports two rotors 29 and 30 arranged concentrically with said housing.
  • the rotors form together with the centre portion 28 of the outlet portion a filling structure occupying the centre portion thereof concentrically with the housing so as to form therebetween and the housing an annular chamber 15 of circle-ring horizontal section;
  • the housing 11 is provided with a completely closed end wall 12 and the main stream 14 of particles is introduced through a supply line 50 connected to the centre of the end wall by means of a stream of air of relatively high velocity, 20 to 40 m/s.
  • a stream of air of relatively high velocity 20 to 40 m/s.
  • the end wall 12 of the housing and the end wall of the rotor 30 are also constructed so that a relatively high air speed is maintained radially therebetween. Since particles are transported to the apparatus substantially by means of air flow it is not necessary to avoid the aforementioned fan effect, nor is it possible to avoid this effect. On the contrary, it may be to advantage to provide the end wall of the rotor with projections or vanes 51 to improve spreading of the particles by an increase in turbulence, an increase in the fan effect being, of course, obtained at the same time.
  • the impeller 44 illustrated in FIG. 3 at the inlet 42 on the end wall of the housing has been omitted in the apparatus of FIG. 4, since it has no function to fullfil.
  • the upper portion of the annular chamber 15 between the housing 11 and the upper rotor 30 has a much wider area than the inlet conduit 50, whereby the axial velocity of the air and therewith the average axial velocity of the particles is low at this point, e.g. 1 m/s or less, thereby allowing the particles time to be uniformly distributed around the circumference of the chamber as they pass the upper rotor 30.
  • the rotor 30 is provided with short vanes 41, as previously mentioned with reference to FIG. 3.
  • the low axial velocity in the upper portion of the annular chamber 15 ensures that no particles will be deposited in this region since the air has a high tangential velocity, which keeps the wall of the housing 11 clean, and the particles are to a large extent retained at the wall of the housing and away from the rotor 30. It is, of course, possible that the finest of the particles reach the rotor, and since the rotor is provided with vanes 41 the difference in tangential velocity between the air and the rotor is much less than the tangential velocity of the air relative to the wall of the housing. Consequently, particles which reach the rotor may be liable to form deposits thereon.
  • the vanes 40 create a very strong turbulence adjacent the rotor, which contributes towards keeping it clean of particles. Possible deposits on the rotor are not able to build up to any large extent, but are torn loose by the centrifugal force and, in the form of separated lumps, are thrown out towards the outer wall of the chamber 15, where they are rapidly broken up into separate particles friction and air eddy currents.
  • the high axial velocity of the air is maintained or increased further in the part outlet 20, depending on whether the particle streams 20 issuing from the part outlets are to be used immediately or are to be conveyed further through long discharge conduits. Further, it is suitable always to provide for a small continuous increase in the axial velocity of the air throughout the whole distance from the lower end of the rotor 29 to the outlet 21 of the part outlet, to prevent stagnation of the boundary layers which may cause particles to be deposited on the wall.
  • FIG. 5 finally illustrates an example of a further develop ment of the invention for converting a continuous, constant stream of particles to a continuous web of particles, in which the distribution of flow is very uniform in both the longitudinal and lateral direction or varies in a desired manner laterally of the longitudinal direction of the web. It is a normal procedure in the particle board and fibre board industry to first arrange particles or fibres into a longitudinally extending continuously growing web, from which appropriate lengths are taken and then under the influence of heat and pressure, normally by pressing in a hot press, are converted to particle and fibre boards.
  • the Figure illustrates schematically an apparatus for forming a particle web.
  • a stream of particles is created with practically a constant flow per unit of time, by proportioning the particles from a bunker by means of a conveyor scale or the like.
  • the stream of chips or particles is then spread by means of one or more so-called chip spreading machines onto support surface which is capable of moving therebeneath in one direction, e.g. a conveyor belt.
  • chip spreading machines When employing known chips spreading machines, the stream of chips is spread onto the support surface in the cross direction of the formed Web by volumetric methods, while distribution of the chips longitudinally is essentially caused by moving the support surface in relation to the chip spreading machine.
  • the chip spreading machines are, of course, practically always constructed so as to spread the stream of chips also over a specific longitudinal section of the support surface, but spreading in the longitudinal direction is for the purpose of screening different chips in the web so that the center layer substantially comprises larger chips and the two outer layers finer chips, and it does not affect the distribution per unit of time longitudinally to any great extent.
  • the total mass or weight of chip web per unit of length is thereby determined by the constant flow per unit of time, obtained by proportioning, and by the speed at which the support surface moves, and can without difficulty be maintained practically constant.
  • the Figure illustrates a device 52 of the aforedescribed type, suitably a device such as that illustrated in FIG. 3.
  • the outlet of the device 52 is divided into a relatively large number of part outlets of equal size, which are extended through outlet lines 53, which are inclined to such an extent that chips are not able to collect at any portion thereof.
  • the exits 21 from the outlet lines 53 for each half of the device 52 are connected in adjacent rows to the upper end wall of their respective distribution box 54 having a planar, relatively steeply declining bottom 55, which terminates short of the lower end wall of the distribution box, so that an opening 56 is formed adjacent the end wall and extending across the entire box.
  • the distribution boxes are shown partly cut away for the sake of clarity.
  • the device 52 together with the distribution boxes 54 are placed over a conveyor belt 57 on which the particle web 58 is formed.
  • a conveyor belt 57 on which the particle web 58 is formed.
  • two ejection rollers 59 Arranged above the conveyor belt 57 and beneath the opening 56 in the distribution boxes are two ejection rollers 59 which are provided with outwardly projecting pegs or the like. The two rollers rotate in opposite directions, so that chips which fall thereon are thrown inwardly of the space between said rollers.
  • a constant stream of chips 14 created in a conventional manner is passed to the device 52 and enters the distribution boxes 54 divided into a number of constant part streams 22 of equal magnitude, which are arranged in rows in side-by-side relationship in the transverse direction of the web 58.
  • the outlet lines 53 are connected with uniform spacing to the distribution boxes 54. It is often desired, however, to provide a somewhat larger quantity of chips along the edges of the web 58, in order to compensate for the increasing width of the web which arises during the pressing operation. This is best provided for by connecting the outlet line 53 to the distribution boxes 54 at a narrower spacing for the outermost outlet lines. Alternatively uniform spacing can, of course, be employed and a larger stream of chips passed to the outermost outlet lines.
  • the chips leave the distribution boxes through the opening 56 and fall down onto the thrower rollers 59, which spread the chips substantially longitudinally along the web 58, to provide in a known manner distribution of different chip sizes vertically of the web with finer chips 60 at the outer surfaces and the coarser chips 61 in the middle.
  • the thrower rollers also spread the particles to a certain extent transversely of the web and thereby create a final equalization of the aforementioned local irregularities in chips distribution in this direction. It is possible that a satisfactory levelling of the local irregularities transversely of the web can be effected solely with suitably constructed thrower rollers, so that the distribution boxes 541 can be omitted.
  • the principal method for transforming a constant stream of particles to a particle web having a uniform mass distribution or a mass distribution which varies transversely of the web in a desired manner means that the flow of particles must first be divided into a suitable number of part flows at constant mass flow and unchanged particle composition, as described in the aforegoing, and that the part flows are then passed to the movable support surface 57 on which the particle web 58 is formed at one or more stations in the longitudinal direction of the web, arranged in side-by-sicle relationship and appropriately spaced in the transverse direction of said web.
  • the method can be applied with all types of particles, although, of course, the device 52 for dividing the main stream 14, the arrangements 54, 59 for levelling the local variations of mass distribution transversely of the web and the support surface 57, on which the particle web 58 is formed, with associated arrangements and devices must be adapted to the type of particles used.
  • a method for dividing a main stream of particles into a plurality of part streams comprising the steps of:
  • An apparatus for dividing a main stream of particles into a plurality of part streams comprising:
  • a substantially vertical cylindrical housing having an inlet end and an outlet end;
  • a rotor rotatably mounted within the housing with its axis of rotation coincident with the longitudinal axis of the housing to define an annular chamber therebetween;
  • said outlet end including a plurality of partition walls extending radially through. said chamber and depending from a single plane concentric with the chamber and substantially normal to the longitudinal axis thereof;
  • controlled means to retard the rotation of the particles around the axis of said chamber in said tubular stream to a desired rotation before said tubular stream reaches the plane of the outlet.
  • outlets from the part outlets are arranged in side-by-side relationship in at least one row.

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  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Wood Science & Technology (AREA)
  • Forests & Forestry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Branching, Merging, And Special Transfer Between Conveyors (AREA)
  • Dry Formation Of Fiberboard And The Like (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Crushing And Pulverization Processes (AREA)
US865759A 1968-10-22 1969-10-13 Method for dividing a main stream of particles into part streams and apparatus for carrying out the method Expired - Lifetime US3652131A (en)

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SE14265/68A SE330475B (xx) 1968-10-22 1968-10-22

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JP (1) JPS5019826B1 (xx)
AT (1) AT310423B (xx)
BE (1) BE740658A (xx)
CA (1) CA939615A (xx)
CS (1) CS160114B2 (xx)
DE (1) DE1952763A1 (xx)
ES (2) ES372715A1 (xx)
FI (1) FI52290C (xx)
FR (1) FR2021251A1 (xx)
GB (1) GB1294446A (xx)
NO (1) NO125261B (xx)
PL (1) PL80269B1 (xx)
SE (1) SE330475B (xx)

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US4203689A (en) * 1978-05-10 1980-05-20 Aluminiumpari Tervezo Es Kutato Intezet Self-adjusting power distributor
US4250774A (en) * 1979-01-31 1981-02-17 Aluminiumipari Tervezo Es Kutato Intezet Self-adjusting powder distributor
EP0070885A1 (en) * 1981-02-09 1983-02-09 Jeremy J Lees METHOD AND DEVICE FOR CONVERTING A FLOW.
US4497345A (en) * 1981-11-04 1985-02-05 Lees Jeremy J Flow conversion device and method
US5667099A (en) * 1994-06-24 1997-09-16 Kao Corporation Method and apparatus for powder distribution
US20120060967A1 (en) * 2009-05-14 2012-03-15 International Tobacco Machinery Poland Sp. Z O.O. Method and Device for Distributing Cut Tobacco for Feeding Cigarette-Making Machines
US20120174983A1 (en) * 2011-01-07 2012-07-12 Conagra Foods Lamb Weston, Inc. Fluid-based article distribution and sorting system
US20130298507A1 (en) * 2010-12-09 2013-11-14 Crealyst Device for filling a container with solid particles comprising a diaphragm
US20140301794A1 (en) * 2013-02-23 2014-10-09 Phillip Douglas Material separator for a vertical pneumatic system
US9394120B2 (en) 2013-02-23 2016-07-19 Phillip Douglas Material separator for a vertical pneumatic system
US10743462B2 (en) 2019-01-11 2020-08-18 Cnh Industrial America Llc Flow splitter for distributing agricultural products and related system

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DE3039384A1 (de) * 1980-10-18 1982-05-19 Ruhrkohle Ag Vorrichtung zum verblasen von (alpha) -halbhydrat und/oder (beta) -halbhydrat
KR102262689B1 (ko) 2016-12-22 2021-06-10 다이치 키겐소 카가쿠 코교 컴퍼니 리미티드 지르코니아 졸(zirconia sol) 및 그 제조 방법

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US2208788A (en) * 1939-07-11 1940-07-23 Daniel J Courtney Separating machine
US2923574A (en) * 1956-09-13 1960-02-02 Fuss Eric William Distributing means with spinner for grain

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US1871853A (en) * 1927-08-09 1932-08-16 Joseph E Kennedy Pneumatic transporting and distributing of pulverized material
US2208788A (en) * 1939-07-11 1940-07-23 Daniel J Courtney Separating machine
US2923574A (en) * 1956-09-13 1960-02-02 Fuss Eric William Distributing means with spinner for grain

Cited By (17)

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Publication number Priority date Publication date Assignee Title
US4203689A (en) * 1978-05-10 1980-05-20 Aluminiumpari Tervezo Es Kutato Intezet Self-adjusting power distributor
US4250774A (en) * 1979-01-31 1981-02-17 Aluminiumipari Tervezo Es Kutato Intezet Self-adjusting powder distributor
EP0070885A1 (en) * 1981-02-09 1983-02-09 Jeremy J Lees METHOD AND DEVICE FOR CONVERTING A FLOW.
EP0070885B1 (en) * 1981-02-09 1986-08-06 LEES, Jeremy J. Flow conversion device and method
US4497345A (en) * 1981-11-04 1985-02-05 Lees Jeremy J Flow conversion device and method
US5667099A (en) * 1994-06-24 1997-09-16 Kao Corporation Method and apparatus for powder distribution
US20120060967A1 (en) * 2009-05-14 2012-03-15 International Tobacco Machinery Poland Sp. Z O.O. Method and Device for Distributing Cut Tobacco for Feeding Cigarette-Making Machines
US8894330B2 (en) * 2009-05-14 2014-11-25 International Tobacco Machinery Poland Sp. Z O.O. Method and device for distributing cut tobacco for feeding cigarette-making machines
US20130298507A1 (en) * 2010-12-09 2013-11-14 Crealyst Device for filling a container with solid particles comprising a diaphragm
US8991139B2 (en) * 2010-12-09 2015-03-31 Crealyst Device for filling a container with solid particles, the device including a diaphragm
US8821078B2 (en) * 2011-01-07 2014-09-02 Conagra Foods Lamb Weston, Inc. Fluid-based article distribution and sorting system
US20120174983A1 (en) * 2011-01-07 2012-07-12 Conagra Foods Lamb Weston, Inc. Fluid-based article distribution and sorting system
US9359151B2 (en) 2011-01-07 2016-06-07 Conagra Foods Lamb Weston, Inc. Fluid-based article distribution and sorting system
US20140301794A1 (en) * 2013-02-23 2014-10-09 Phillip Douglas Material separator for a vertical pneumatic system
US9394120B2 (en) 2013-02-23 2016-07-19 Phillip Douglas Material separator for a vertical pneumatic system
US10106338B2 (en) * 2013-02-23 2018-10-23 Phillip Allan Douglas Material separator for a vertical pneumatic system
US10743462B2 (en) 2019-01-11 2020-08-18 Cnh Industrial America Llc Flow splitter for distributing agricultural products and related system

Also Published As

Publication number Publication date
GB1294446A (en) 1972-10-25
NO125261B (xx) 1972-08-14
CA939615A (en) 1974-01-08
FR2021251A1 (xx) 1970-07-17
ES372715A1 (es) 1972-03-16
FI52290B (xx) 1977-05-02
FI52290C (fi) 1977-08-10
AT310423B (de) 1973-09-25
PL80269B1 (xx) 1975-08-30
BE740658A (xx) 1970-04-01
DE1952763A1 (de) 1970-10-22
SE330475B (xx) 1970-11-16
JPS5019826B1 (xx) 1975-07-10
CS160114B2 (xx) 1975-02-28
ES396067A1 (es) 1974-04-01

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