US3799353A - Continuous centrifuge - Google Patents

Continuous centrifuge Download PDF

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US3799353A
US3799353A US00297440A US29744072A US3799353A US 3799353 A US3799353 A US 3799353A US 00297440 A US00297440 A US 00297440A US 29744072 A US29744072 A US 29744072A US 3799353 A US3799353 A US 3799353A
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basket
sugar
combination
angle
annular
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K Pause
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B3/00—Centrifuges with rotary bowls in which solid particles or bodies become separated by centrifugal force and simultaneous sifting or filtering

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  • a continuous centrifuge for separating liquid and solid phases of a suspension has a centrifuge basket rotatable about an upright axis and having an upper open end, and a perforate liner in the basket conically diverging towards the upper open end.
  • An annular baffle is mounted adjacent the upper open end and de- 1 fines therewith a radially extending annular outlet gap through which retained solid phase can pass in radially outward direction under centrifugal force.
  • An annular flow-regulating member is mounted on and rotatable with the basket and has a cylindrical surface juxtaposed with spacing from the outer end of the annular gap so that centrifugally ejected solid phase will contact this surface.
  • the flow regulating member is mounted on the basket with slight freedom of axial movement relative thereto.
  • PAIENIED was m 3.799353 SHEU 30F 5 msmanmzsmm 3799353 sum s of, 5
  • centrifuges of this type are well known, and are'particularly frequently employed in the sugar production. It is known to utilize such centrifuges as so-called thin-layer centrifuges which usually have an internal screen. It is also known to provide protection for the screen by mounting at the outlet end of the centrifuge basketan annular plate whichv rotates with the basket and which extends in parallelism with the upper edge of the basket at the outlet end, being spaced therefrom so that an annular channel exists through whichthe material to be ejected, that is the retained solid phase of the suspension, such as sugar, can pass.
  • This space is made large enough so that even larger lumps of mattercan pass through itj
  • the purpose of this arrangement is to provide a protection against rebounding, because lumps of solid matter which could rebound would cause damage or-destruction of the thin screen liner.
  • the arrangement neither intends to nor is capable of producing a thick layer in the interior ofthe centrifuge.
  • Another thick-layer centrifuge determines the thickness of the layer on the conical screen of the basket by a filler plate, and by varying the degree of angular inclination of the basket wall in the region where the solid phase is ejected, the ejection of the solid phase is'to be capable of regulation. Because the inclination of the circumferential wall of the basket cannot'be adjusted, it is not possible to vary the amounts of solid phase which are ejected per unit of time in this construction. Moreover, this particular centrifuge does not make it possible to produce a suspension layer of a particular thickness on the conical basket because the incoming suspension is supplied onto the screen of the basket as a Newtonian'liquid.
  • the pouring weight of the sugar crystals is 0.9 kg/dm, and the sugar mass thus requires only about 57 percent of a volume of space, whereas 43 percent are hollow areas which accommodate syrup. However, only 67 percent of the total syrup weight is contained in these hollows so that 33 percent of the syrup weight is free or unbound. Since in the stirring devices the suspension is mechanically agitaged, the sugar crystals are freely floating in the syrup without any significant relative contact with one another. Such a suspension acts, from a rheological 'point of view, as Newtonian liquid, that is a liquid without flow limit.
  • the flow speed gradient serving as a measure of the speed differentials from layer to layer in the suspension, it is directly proportional to the product of shear stress and fluidity of the suspension, and inwardly proportional to the product of shear stress and the reciprocal value of the fluid ity, that is the coefficient of viscosity.
  • the sum of all flow speed gradients, related to a particular flow cross section, yields the coefficient of flow, that is the median flow speed of a medium is dependent upon the cross section through which it flows.
  • the sugar crystals are retained on a screen through which syrup can pass. This means that as i the syrup moves away the sugar crystals will Finally obtain contact withone another, support one another and no longer reduce their total volume. Given the aforementioned weight and volume data, it will be seen that this occurs when the unbound or free syrup has disappeared through the screen.
  • the specific weight of the residual suspension is now 1.5 kg/dm, of which 60 percent by weight is sugar and 40 percent by weight is syrup.
  • the stiffened suspension has an intrinsic viscosity, from a rehological point of view, that is the speed gradient no longer increases linearly with the shear stress, but instead increases according to an exponential function with an exponent which is greater than I. In this relationship, the coefficient of viscosity and the exponent vary at constant shear stress, but in the relationship of solid to liquid phase.
  • the acceleration acting upon the liquid can reach a substantial multiple of gravitational acceleration without changing the angle of flight.
  • the surface of the liquid will always extend at right angle to the resulting acceleration.
  • the flow behavior at zero speed, related to the angle of slide is also independent of acceleration, which is understandable because the thrust, the shear stress, is directly proportional to the normal force, that is the speed gradient.
  • the boundary of inherently viscous flow behavior of sugar suspensions is at 98 percent by weight of sugar crystals and 2 percent by weight of syrup. If the weight of syrup drops below this point, sugar crystals act as poured material, under the influence of mass force.
  • a further reduction of the syrup proportion decreases the angle of slide further, until when the sugar is dry and the proportion of syrup has dropped to zero, a boundary value is reached which depending on the grain distribution is within a scatter range.
  • the angle of inclination of the peripheral wall of known continuous centrifuge baskets or drums is so chosen that it is smaller than the largest angle of slide in the inherently viscous range of sugar suspensions. This should mean that the sugar layer from which the syrup has been removed cannot leave the basket, because beginning at the condition where the angle of slide ofthe suspension is greater than the angle of inclination of the basket wall, there is a retardation of the flow movement which would rapidly lead to a zero flow speed, if there would not remain a thrust component in axial direction from the beginning of the sugar layer. At the beginning in the range of purely Newtonian flow-behavior this thrust component is substantial, but decreases as the flow limit increases until it reaches zero and than becomes converted into a braking component.
  • the different angle of slide range requires a different angle of inclination of the basket wall, in order to be able to obtain the optimum flow conditions mentioned above, for the particular material.
  • the syrup of white sugar suspensions has a substantially lesser viscosity at a temperature of 7273C. than the molasses of the sugar by-products at a temperature of only 3540C.
  • the greater purity of the syrup with respect to the molasses increases the fluidity of the syrup, even beyond the difference resulting from the temperature differential. This means that the change from Newtonian flow behavior to inherently viscous flow behavior occurs much more rapidly in white sugar suspensions than in suspensions of the other types, and that the change in the flow speed gradient per unit of time is greater in white sugar suspensions.
  • a crystal distribution, related to a median crystal size, can vary with reference to another one, the pouring rate of a one-boil sugar is almost constant. This is all the more true as in a centrifuge a very uniform packing of the crystals can be obtained and the pouring rate mentioned earlier (without the so-called free syrup) represents the boundary between Newtonian flow behavior and inherently viscous flow behavior.
  • the amount of size differential in the crystal mix becomes noticeable when the sugar has pouring characteristic, that is the characteristic which a constant energy gradient, will just be capable of freely flowing through this diameter of the iris diaphram.
  • the area value is 1 1.1 for the sugar type A, and 18.2 for the sugar type B, of 1:1.64 at a dimension MM".
  • Residual moisture of liquid adhereing to the crystal surfaces is' related to the unit weight; this' means that the sugar type B is drier than the sugar type A given residual moisture which is identical in terms of the weight.
  • An additional object of the invention is to provide such a continuous centrifuge in which the dwell time of the solid phase in the centrifuge basket can be regulated at will, independent of the thickness of the layer on the interior of the basket.
  • one feature of the invention resides, in a continuous centrifuge for separating the liquid and solid phases of a suspension, particularly in a sugar centrifuge, in a combination which comprises a centrifuge basket mounted for rotation about an upright axis and having an inner circumferential surface which conically diverges in upward direction to an upper open inlet end of the basket.
  • a perforate liner is provided in the basket, overlaying the inner surface thereof.
  • Admitting means admits a suspension into the basket for centrifugal separation of the liquid and solid phases of the suspension, and for retention of the latter phase as a flowable mass.
  • An annular baffle is mounted adjacent the open outlet end and defines therewith a radially extending annular outlet gap communicating with the interior and having an outer end communicating with the exterior of the basket, for centrifugal ejection of the flowable mass from the basket through this gap.
  • An annular flow-regulating member is rotatable with the basket for regulating the outflow of the mass through the outlet gap and has a surface which concentrically surrounds the baffle at a predetermined fixed radial distance from the outer end of the outlet gap. This surface extends axially beyond the outer end by a distance greater than the slope angle capable of being formed by the mass when centrifugally ejected throught the outlet gap and onto the surface of the member.
  • Mounting means mounts the member on the basket for rotation therewith and for limited axial movement relative thereto and to the baffle.
  • the width of the annular gap is approximately 10 percent greater than the greatest nozzle value of the flowable mass, and the spacing between the outer end of the gap and the surface concentrically surrounding it should also be slightly greater than this greatest nozzle value.
  • a centrifuge so constructed assures that the flow regulating member will'cause, depending upon the contents of solid phase inthe suspension and the pouring angle, a correspondingly thick layer of solid phase on the inner surface of the perforate liner.
  • the precisely defined annular gap permits a predetermined quantity of solid mass to pass through, which mass than contacts the surface concentrically surrounding the gap and forms a pouring angle on this surface.
  • the invention achieves the advantage that a precisely metered ejection of flowable or solid mass takes place, independently of the crystal size of the solid mass, for instance the sugar, related statistically per unit of time. This has not been possible with the continuous centrifuges known heretofore.
  • the invention further provides for the inner portion of the annular baffle to extend conically into the interior of the centrifuge basket.
  • the inner surface of the flow-regulating member is advantageously conically configurated, and the angle of inclination of this surface is smaller than the pouring or slide angle of all solid materials to be processed in the centrifuge.
  • the cone angle may widen in the direction in which the material is ejected, and at the end or side facing away from this direction the flow-regulating member may be delimited by an annular transverse wall portion.
  • the invention further suggests that the annular baffle have a larger diameter than the outlet end of the centrifuge basket itself.
  • the circumferential wall portion of the flow-regulating member having the surface concentrically surrounding the outer end of the outlet gap is advantageously provided as an annular magnetizable core and contacts an annular bead of the annular baffle against which it is pressed by at least three circumferentially distributed spring units.
  • An electromagnet is located above the baffle and the flow-regulating member at one circumferential location, being mounted at a stationary component of the centrifuge, and the movement of the flow-regulating member in upward axial direction away from the basket is delimited by an annular abutment provided on the baffle itself. This assures that when the electromagnet is energized, it lifts the flowregulating member in opposition to the biasing force of the springs until it contacts the aforementioned abutment. Because the electromagnet is stationary and the flow-regulating member turns with reference to it, the flow-regulating member will perform relative to the basket an axial tumbling movement so that during each rotation of the basket each circumferential incremental portion of the flow-regulating member will perform the same axial movement. In other words, the flowregulating member is never moved axially in it entirety, but only increments are moved axially as they pass into and out of the range of the electromagnet.
  • the inclination and axial length of the centrifuge basket influences the development of a thick layer of solid phase.
  • the basket itself and/or the perforate liner be provided with inner surfaces having different angles of inclination, which are greater than the angle of slide of the solid phase which obtains at the particular region of the basket or perforate liner, that is which is assoicated with that degree of liquid removal which has been reached by the solid at the time it moves to a particular surface portion of the basket or liner.
  • FIG. 1 is a graph showing the angle of slide of two sugar layers of different crystal distribution at various degrees of moistness
  • FIG. 2 is another graph showing the angle of slide of the sugar layers of FIG. 1, as related to their contact with a perforate support through which moisture can escape;
  • FIG. 3a is a diagram showing the sugar outflow through an opening with an intercepting member beneath the opening in one position
  • FIG. 3b is similar to FIG. 3a but shows the intercepting member in a different position
  • FIG. 4 is an axial section illustrating the novel centrifuge according to the present invention.
  • FIG. 5 is a graph showing one operational principle of the centrifuge illustrated in FIG. 4.
  • FIGS. 6a and 6b are diagrammatic detail views, illustrating specific details of the centrifuge, FIG. 6b being a section on line A-B of FIG. 60.
  • reference numeral 1 designates the conically configurated centrifuge basket which has a bottom wall 2.
  • a drive shaft 3 Secured to the bottom wall 2 is a drive shaft 3 which can rotate about its longitudinal axis in the diagramatically illustrated bearings 4 (one shown).
  • the basket 1 has a plurality of outlet openings 5 through which the so-called green syrup" is ejected. In the region of the flange 6 there is another plurality of outlet openings 7 for ejection of the so-called high green syrup.
  • a conical baffle 8 is provided which prevents contact of the high green syrup with the centrifuged dry sugar crystals.
  • the drum may be provided, in a manner and at distances known per se, with concentric undercut annular grooves 5a in which the syrup is collected which flows behind the perforate liner insert 9, and'from which it passes through the outlet openings 5 to the exterior of the drum or basket 1.
  • the liner insert 9 is a self-supporting basket-shaped element having a bottom wall 10, a conical circumferential wall 11 and a flange 12 provided on the latter.
  • Screen openings 13 are provided in the bottom wall 10 and communicate with one or more radial channels 14 which in turn communicate with the space IS'defined between the circumferential wall of the basket 1 and the circumferential wall of the insert 9.
  • Screen openings 16 are provided in the circumferential wall 11 and the latter has in the lower region a lesser angle of inclination than in the upper region as shown in FIG. 4.
  • a retarding bell 17 which can be raised and lowered and which is pushed via a sleeve 18 and webs 19 onto a pin or bolt 20 of the wall 10 or the wall 2, like the german Pat. No. 1,272,229.
  • a conduit 21 communicates with the interior of the bell 17 and supplies the suspension into the latter.
  • a nozzle 22 communicates with a conduit 23 through which wash water can be sprayed into the interior of the liner 9, and a known device 24 is provided by means of which the thickness of the layer of sugar 42, that can form on the inner circumferential surface of the wall 11, can be regulated.
  • the liner 9 could also be composed of a supporting screen and a working screen, one overlaying the other and both being mounted and supported on the inner surface of the basket 1.
  • the two angles of inclination of the two portions of the wall 11 are so selected that they are greaterthan the greatest angle of slide of the solid phase that is to be separated in the centrifuge, that is in this case the greatest angle of slide of the white sugar types in their inherent viscosity flow range.
  • This angle of inclination can be accommodated to the changing angle of slide of the, sugar, that is the angle as it changes with progressing removal of syrup.
  • the angle of inclination at every point isalways greater than the greatest angle of slide of the sugar in the liquidremoval phase inwhich the sugar will be at the time it overlies the particular portion of the wall.
  • the finer-crystal sugar B is more ready to slide than the sugar A, when it is ,dry and has a small proportion of syrup admixed with it.
  • a small proportion of syrup in the sugar type B will mean, due to the large only a small change in the friction of the crystals with reference to one another.
  • the same amount of proportion of syrup (by weight) in the sugar type A will cause a'thicker film on the surfaces of the sugar crystals and will reduce the friction (and thus the angle of slide) more than in the case of the sugar type B.
  • the angle of slide refers to the degree of friction between sugar crystals. If the. sugar is on a metal surface,
  • the friction is less. If the sugar is maintained against sliding on an inclined surface, withthe inclination of the surface being greater than the sliding angle of sugar on sugar, than the sugar layer will not move and can be increased to a desired thickness. The angle of inclination of the sugar layer will remain constant, because if additional sugar is poured on, it will slide off and will contact the base support, forming a mound with the constant angle of slide.
  • FIG. 2 where a perforate metal support is shown, which is inclined as illustrated and on which two sugar types A and B are shown to be heaped.
  • a dam or base support provides them from freely sliding off and they are shown in movement which corresponds to the outlet at the lower end of the dam. This movement is not free because the speed at which it takes place is not associated with the existing energy gradient, but is rather significantly less.
  • the outlet opening at the lower end of the dam retaining the layers in FIG. 2 from freely flowing is just large enough for the sugar to pass through in accordance with its nozzle value.
  • sugar type A require a larger outlet gap than sugar type B.
  • the outflow speed corresponds to the energy gradient, reduced by the friction according to the angle of slide.
  • the two layers have been shown to be of approximately identical thickness, so that the speed of sliding of the layer A on the inclined surface would be greater than that of the slide B. In other words, the amount of sugar A flowing through the gap per unit of time is greater than that of the sugar B. An influencing of the speed is possible only by increasing the gap or making the layer thicker.
  • the lower boundary of the quantity of outflow per unit of time thus determines the sugar characteristic and indifferent sugar types this lower boundary varies substantially, as can be determined from the nozzle value. It must be kept in mind in this connection that in the centrifuging of sugar, quantities of sugar must be passed out of the basket which are much too large to subject them to the necessary time required for separation and washing.
  • FIG. 3a shows a container-C which has at its lower end an opening 0 through which sugar can flow at the largest nozzle value that is to be encountered.
  • a slide S Located beneath the container C, extending transversely to the direction of outflow, is a slide S the bottom BW of which is inclined in one direction at a lesser angle than the smallest angle of slide of dry sugar.
  • the slide S is provided with a vertical side wall SW which extends upwardly beyond the plane of the outlet opening 0.
  • the latter is vertically bounded to different extents, that is it will be seen that the right-hand vertical wall of the container C extends downwardly below the lower edge of the left-hand wall which is opposed to it.
  • Sugar passing through the opening will fall onto the bottom wall BW and will form on both sides of the opening its specific pouring angle, as shown in FIG. 3a. Because the slide S is so long that the pouring angle will not make the sugar reach the end of the slide, the friction in the sugar prevents further outflow of sugar once this pouring angle has been reached, that is no further sugar will flow out through the opening 0.
  • the receding slide S would thus yield a corresponding volume at the right which is not filled with sugar. However, this does not in fact take place because as the volume becomes available it is immediately filled by sugar which flow out through the opening 0 so that the sugar in fact never loses contact with the bounding surfaces of the slide S.
  • the existing friction assures that the left-hand portion P of the sugar must remain in position, that is that it cannot follow the slide along. Because of this it loses its support by the bottom wall BW and must slide off.
  • a movement of the slide S towards the left back to the position of FIG. 3a causes the sugar on the slide to move along with the same without changing its volume.
  • the shear surface of the sugar at the outlet 0 is now inclined in the direction of the return movement of the slide S and affords only a small shear resistance.
  • the friction of sugar with respect to the bottom wall BW is increased over what existed before.
  • FIG. 4 shows that the insert 9 has a flange 12 with which there is connected an annular baffle 25 in such a manner as to define a precisely dimensioned annular outlet gap 26 between them.
  • the outer diameter of the baffle 25 is greater, in accordance with the invention, than the greatest diameter of the flange 12 to which it is connected by means 43 FIG. 6 of several profiled connecting components which are so constructed that they permit a proper outflow of the solids through the gap without interfering therewith. If the insert 9 is replaced with the conventional dual supporting and working screens mentioned earlier, than the flange 12 can be omitted and in this case the baffle 25 is directly connected with the flange 6 and forms therewith the gap 26.
  • the baffle 25 is provided with a conical annular portion 27 and it is further provided in the region of its inner diameter with an annular collar 28 having in its outer edge an abutment 29. In the region of the juncture of the collar 28 with the remainder of the baffle 25 there is provided an annular abutment 30.
  • the invention further provides for an annular flowregulating member 31 an inner cylindrical surface 32 of which concentrically surrounds the outer end of the gap 26 with radial spacing thereform.
  • the surface 32 conically diverges in the direction of discharge, that is downwardly in FIG. 4, and at an angle which is smaller than the pouring angle of all solids which are to be centrifuged in the apparatus.
  • annular transverse wall portion 33 At the upper end of the surface 32, that is the end which faces away from the discharge side, there is provided an annular transverse wall portion 33 which is located upwardly of the baffle 25 and whose inner periphery rests on the annular bead 30.
  • the axial length of the surface 32 is so selected that a pouring angle 34 of the centrifugally ejected solid material (sugar) can form when the material issues from the gap 26; this is illustrated in FIG. 4. It will be seen that the flowregulating member 31 in the embodiment of FIG. 4 thus performs the same function as the slide S in FIGS. 30 and 3b.
  • biasing arrangements 35 are equi-angularly distributed about the axes of rotation of the centrifuge and each utilize a bolt 36, a stack of dished springs 38 and nuts 37, so that the springs press the member 31 with a precisely predetermined force against the shoulder or abutment 30.
  • an electromagnet 39 of well known construction, which is located at one circumferential location of the centrifuge basket and is fixedly mounted, for instance on the centrifuge frame 40.
  • An air gap 41 exists between the upper surface of the portion 33 of the member 31 and the underside of the electromagnet 39; this air gap can lifted at that portion which is located beneath the electromagnet 39 until it abuts the abutment 29.
  • the drum 1 with the member 31 rotates.
  • the highest point of the member 31, that is the point where it is raised closest to the electromagnet 39 will shift circumferentially. with respect to the drum or basket 1' so that, during each complete 360 degree rotation of the basket, each point of the member'3l has performed an axial movement withrespect to the basket 1.
  • the axial movement corresponds to an axial movement of the portion 31 between the highest and lowest points, determined by the abutment 29 and 3.0, respectively.
  • the wall 11 of the insert 9 carries a sugar layer 42, than sugar passes through the gap 26 at a quantity which is determined by pouring angle and friction in the' absence of theoperation of the flow-regulating member 31. If, however, the member 31 has imparted to it the tumbling or. 'wobbling movement just described with the aid of the electromagnet 39, than sugar will be ejected through the gap 26 in accordance with the principle described above with respect to FIGS. 3a and 3b. Because the tumbling movement is delimited between two fixed abutments, the extent of axial displacement is the same during each rotation of the basket and, giving a uniform number of rotations, a constant quantity of sugar will be expelled per unit of time.
  • the dwell time of the sugar that is the time during which the sugar will remain in the basket, is determined by the thickness of the layer and is variable by varying this thickness.
  • This movement of the member 31 with respect to the basket 1 between an upper and a lower limit can also be produced by' a stream of liquid under pressure, a
  • the abutment 29 must be located high enough so that it permits a lifting of the member 31 in axial direction to an extent which is greater than the possible or' expected maximum ejection of solid per unit of time.
  • the electromagnet 39 can be supplied with electrical energy by an adjustable transformer (not illustrated because it is well known in the art).
  • the characteristic of the spring arrangemnt 38 is so selected that thecharacteristic line of the springs intersects the characteristic lines of different voltages applied to the electromagnet overthe entire control range for the electromagnet andover the entire air gap variation.
  • FIG. shows this graphically, with the magnetic holding force via the air gap 41 between magnet 39 and member 31 acting as illustrated, given the voltage applied as the parameter. Because the magnetic force does not directly appear, but acts only indirectly as the force of a tilting movement, it is the movement and not the force which has been designated on the ordinate of the graph in F 1G. 5.
  • the arrangements 35 produce a counter moment when themember 31 is tilted by the magnet 39.
  • each unit 35 corresponds to that of each other unit, and because the characteristic is linear, the sum of all spring forces, that is of the counter moments produced by the springs during each phase of rotation, is equal and constant. Therefore, FIG. 5 shows the sum of all of these spring forces.
  • the thickness of the layer 42 is regulated by means of the device 24 which is well known (in german Pat. application P 27 57 475.0-23) to those skilled in the art;
  • the swell time is shortened if this is done, but if the dwell time isto be maintained unchanged than the device 24 must be adjusted so as to provide for a lesser regulation of the thickness so that the thickness can be greater. This also can be effected without interrupting the continuous operation of the centrifuge.
  • a combination comprising a centrifuge basket mounted for rotation about an upright axis and having an inner circumferential surface which conically diverges in upward direction to an upper open outlet end of the basket;
  • admitting means for admitting a suspension into said basket for centrifugal separation of the liquid and solid phases of such suspension, and retention of the latter phase as a flowable mass;
  • annular baffle mounted adjacent said open outlet end and defining therewith a radially extending annular outlet gap communicating with the interior and having an outer end communicating with the exterior of said basket, for centrifugal ejection of the flowable mass from the basket;
  • annular flow-regulating member rotatable with said basket for regulating the outflow of said mass through said outlet gap, said member having a surface concentrically surrounding said baffle at a predetermined fixed radial distance from said outer end of said outlet gap and extending axially beyond said outer end by a distance greater than the slope angle capable of being formed by said mass when centrifugally ejected through said outlet gap and onto said surface of said member;
  • mounting means mounting said member on said basket for rotation therewith and for limited axial movement relative thereto and to said baffle.
  • baffle having a radially inner portion of conical taper which extends through said open outlet end into said basket.
  • said member including an annular wall portion provided with said surface and having two axial ends one of which is open for ejection of said flowable mass, and a transverse wall portion provided on said annular wall portion in the region of the other axial end thereof and extending transversely of the axis of rotation of said basket.
  • annular baffle having an end face facing axially away from said basket and being provided with a raised abutment, said transverse wall portion overlying said end face at least in part and normally contacting said abutment, and at least said annular wall portion being of magnetizable material; and further comprising electromagnet means mounted adjacent to said transverse wall portion at one circumferential locus of said basket slightly spaced from said transverse wall portion along said axis.
  • said mounting means comprises at least three mounting units distributed circumferentially about said upright axis and each comprising spring means permanently tending to bias said transverse wall portion towards said abutment.
  • said perforate liner having an interior circumferential surface facing inwardly of said liner and away from said inner surface; and wherein at least one of said circumferential surfaces diverges from the region of the lower end of said basket to substantially midway between said ends at a smaller 'first angle, and from substantially midway of said basket to said upper end at a larger second angle.

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US00297440A 1971-10-15 1972-10-13 Continuous centrifuge Expired - Lifetime US3799353A (en)

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DE2151476A DE2151476C2 (de) 1971-10-15 1971-10-15 Dickschicht-Strömungszentrifuge

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CH (1) CH563811A5 (ja)
CS (1) CS161809B2 (ja)
DD (1) DD98841A5 (ja)
DE (1) DE2151476C2 (ja)
FR (1) FR2156059B1 (ja)
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Cited By (18)

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US4052303A (en) * 1972-12-11 1977-10-04 Krauss-Maffei Ag Method of operating a centrifugal filter and a filter centrifuge operating according to this method
US4063959A (en) * 1976-03-04 1977-12-20 Braunschweigische Maschinenbauanstalt Continuously operating sugar centrifuge
US4718945A (en) * 1981-07-25 1988-01-12 Braunschweigische Maschinenbauanstalt Ag Sugar centrifuge
US4961722A (en) * 1989-11-30 1990-10-09 Guyan Machinery Co. Conical screen for a vertical centrifugal separator
US5217628A (en) * 1991-05-20 1993-06-08 Lundquist Lynn C Method of batch centrifugal removal of residual liquid waste from recyclable container material
WO1995021697A1 (en) * 1994-02-08 1995-08-17 Stg Holdings Pty Ltd Centrifugal separations apparatus
US5713826A (en) * 1996-05-07 1998-02-03 Waterlink, Inc. Vertical basket centrifuge with feed acceleration and a removable liner
US5788861A (en) * 1996-04-12 1998-08-04 National Conveyors Company Method and apparatus for varying the exposure of drainage screen section within a centrifugal separator
US6267899B1 (en) 1997-04-22 2001-07-31 Stg-Fcb Holdings Pty Ltd. Centrifugal separation apparatus and method of using the same
US6521120B1 (en) 1999-08-19 2003-02-18 Thomas Broadbent & Sons Ltd. Continuous centrifuges
US20030036720A1 (en) * 2001-08-17 2003-02-20 Spencer Dudley W.C. Hemodialysis assembly and method
WO2003033163A1 (en) 2001-10-18 2003-04-24 Wdt (Engineers) Pty Ltd Continuous centrifuge
US20030155312A1 (en) * 2002-02-15 2003-08-21 Ivansons Ivars V. Spin-hemodialysis assembly and method
US20110006016A1 (en) * 2009-07-13 2011-01-13 Gilles Stephen R Centrifugal basket assembly with segmented dam and method
US20150190817A1 (en) * 2012-07-12 2015-07-09 Pieralisi Maip Societa' Per Azioni Centrifugal separator or decanter provided with improved closing system
CN110216010A (zh) * 2019-06-04 2019-09-10 江西离子型稀土工程技术研究有限公司 一种连续离心选矿机气、水复合卸矿方法及装置
CN110216011A (zh) * 2019-06-04 2019-09-10 江西离子型稀土工程技术研究有限公司 一种气、水复合卸矿的连续离心选矿机
CN110237942A (zh) * 2019-07-03 2019-09-17 辽宁科技大学 一种具有复合力场的离心机锥体及水套式离心机

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DE3329648C2 (de) * 1983-08-17 1985-09-05 Krupp Industrietechnik GmbH Werk Buckau Wolf, 4048 Grevenbroich Siebzentrifuge für kontinuierlichen Betrieb, insbesondere Zuckerzentrifuge
GB2166424B (en) * 1984-11-01 1988-07-13 Atomic Energy Authority Uk Improvements in or relating to materials
CN111643953A (zh) * 2020-06-18 2020-09-11 南京浩睿达环保科技有限公司 一种便捷型污水处理设备
CN114894935B (zh) * 2022-05-23 2023-11-21 湖南省长康实业有限责任公司 一种芝麻油防掺假快速检测方法及装置

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Cited By (24)

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US4052303A (en) * 1972-12-11 1977-10-04 Krauss-Maffei Ag Method of operating a centrifugal filter and a filter centrifuge operating according to this method
US4063959A (en) * 1976-03-04 1977-12-20 Braunschweigische Maschinenbauanstalt Continuously operating sugar centrifuge
US4718945A (en) * 1981-07-25 1988-01-12 Braunschweigische Maschinenbauanstalt Ag Sugar centrifuge
US4961722A (en) * 1989-11-30 1990-10-09 Guyan Machinery Co. Conical screen for a vertical centrifugal separator
US5217628A (en) * 1991-05-20 1993-06-08 Lundquist Lynn C Method of batch centrifugal removal of residual liquid waste from recyclable container material
WO1995021697A1 (en) * 1994-02-08 1995-08-17 Stg Holdings Pty Ltd Centrifugal separations apparatus
US5788861A (en) * 1996-04-12 1998-08-04 National Conveyors Company Method and apparatus for varying the exposure of drainage screen section within a centrifugal separator
US5855800A (en) * 1996-04-12 1999-01-05 National Conveyors Company Method for varying the exposure of drainage screen section within a centrifugal separator
US5713826A (en) * 1996-05-07 1998-02-03 Waterlink, Inc. Vertical basket centrifuge with feed acceleration and a removable liner
US6267899B1 (en) 1997-04-22 2001-07-31 Stg-Fcb Holdings Pty Ltd. Centrifugal separation apparatus and method of using the same
US6521120B1 (en) 1999-08-19 2003-02-18 Thomas Broadbent & Sons Ltd. Continuous centrifuges
US20030036720A1 (en) * 2001-08-17 2003-02-20 Spencer Dudley W.C. Hemodialysis assembly and method
WO2003033163A1 (en) 2001-10-18 2003-04-24 Wdt (Engineers) Pty Ltd Continuous centrifuge
EP1446229A1 (en) * 2001-10-18 2004-08-18 WDT (ENGINEERS) PTY Ltd Continuous centrifuge
EP1446229A4 (en) * 2001-10-18 2009-04-01 Wdt Engineers Pty Ltd PASS CENTRIFUGE
US20030155312A1 (en) * 2002-02-15 2003-08-21 Ivansons Ivars V. Spin-hemodialysis assembly and method
US6852231B2 (en) 2002-02-15 2005-02-08 Denco, Inc. Spin-hemodialysis assembly and method
US20110006016A1 (en) * 2009-07-13 2011-01-13 Gilles Stephen R Centrifugal basket assembly with segmented dam and method
US8192634B2 (en) 2009-07-13 2012-06-05 Gilles Stephen R Centrifugal basket assembly with segmented dam and method
US20150190817A1 (en) * 2012-07-12 2015-07-09 Pieralisi Maip Societa' Per Azioni Centrifugal separator or decanter provided with improved closing system
US9968947B2 (en) * 2012-07-12 2018-05-15 Pieralisi Maip Societa' Per Azioni Centrifugal separator or decanter having an electromagnetic closing system
CN110216010A (zh) * 2019-06-04 2019-09-10 江西离子型稀土工程技术研究有限公司 一种连续离心选矿机气、水复合卸矿方法及装置
CN110216011A (zh) * 2019-06-04 2019-09-10 江西离子型稀土工程技术研究有限公司 一种气、水复合卸矿的连续离心选矿机
CN110237942A (zh) * 2019-07-03 2019-09-17 辽宁科技大学 一种具有复合力场的离心机锥体及水套式离心机

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CS161809B2 (ja) 1975-06-10
FR2156059A1 (ja) 1973-05-25
GB1412006A (en) 1975-10-29
DD98841A5 (ja) 1973-07-12
NL7213714A (ja) 1973-04-17
CH563811A5 (ja) 1975-07-15
JPS4847659A (ja) 1973-07-06
DE2151476C2 (de) 1980-10-23
FR2156059B1 (ja) 1980-03-21
DE2151476B1 (de) 1972-12-28
IT968920B (it) 1974-03-20

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