US2377524A - Method of and means for separating solid particles in pulp suspensions and the like - Google Patents

Method of and means for separating solid particles in pulp suspensions and the like Download PDF

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Publication number
US2377524A
US2377524A US305449A US30544939A US2377524A US 2377524 A US2377524 A US 2377524A US 305449 A US305449 A US 305449A US 30544939 A US30544939 A US 30544939A US 2377524 A US2377524 A US 2377524A
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pulp
suspension
chamber
outlet
impurities
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US305449A
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Edward W Samson
Alfred H Croup
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Hammermill Paper Co
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Hammermill Paper Co
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
    • B04C5/08—Vortex chamber constructions
    • B04C5/081—Shapes or dimensions
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
    • B04C5/24—Multiple arrangement thereof
    • B04C5/26—Multiple arrangement thereof for series flow

Definitions

  • This invention relates to a centrifugal method and means of separatingfrom or in a fluid suspension, solid particles whose reactions to centrifugal force are only slightly different from each other or from that of the suspending fluid.
  • centrifugal force reactions depend upon the relative specific weights of the particles but they depend very largely also upon the shape and other factors which play a part in the ease or diificulty with which the particles are propelled by centrifugal force through the fluid.
  • Shives which are small bundles of fibers themselves that have not been fully separated and which, if left in the pulp, will produce a defect in the paper, have a reaction to centrifugal force which is so nearly the same as that of the individual fibers that they are hardly separable by centrifugal action from the regular fibers. This is particularly true of the longer shives, but these, notably, may be removed fairly well byscreening.
  • the present invention is capable of eliminating a part of the shives. especially the shorterones, and is particularly adapted for the rapid and efficient separation and removal from the pulp suspension, at convenient mill consistencies, of a large percentage of the other impurities mentioned, either before or after the addition of paper-making ingredients, such as size, dyes, and fillers.
  • the impurities which the present invention is particularly designed to remove from pulp may be said to be equivalent to spherical particles'of 40 to mesh size, having a specific gravity of 1.01 to 1.08 and capable of settling in still water at the rate of between 5 and 25 centimeters per minute.
  • such equivalent particles having a settling rate down to 3 cm. per minute may be removed from the pulp to a certain extent but particles of slower settling rate are hardly separable.
  • the settling rate of particles in still water gives in itself a fair indication as to their reaction to centrifugal force since this settling rate is affected by considerations quite similar to those which enterinto the centrifugal force reaction.
  • some of the impurities which the present invention is capable of effectively removing from pulp at convenient mill consistencies will settle in still water at a rate as low as 5 centimeters per minute, or even lower, and since many of the fibers or small flocks of fibers and other desirable ingredients have almost the same settling rates, the difliculty of removing the impurities by centrifugal action will be appreciated.
  • the invention involves the subjection of a stream of pulp or other suspension to centrifugal action, induced by the stream itself, without revolving mechanical devices, under such conditions as to bring about the continuous separation of a substantially purified pulp or other suspension or fluid from a fraction containing most of the impurities.
  • This separation in the case of pulp purification, may be effected just after the coarse screening of the pulp in the mill or at some subsequent stage. It may, if desired, be eflected just in advance of the delivery of the pulp to the paper machine, in which case the impurities must be separated not only from the fibers but also from the other paper-making ingredients.
  • the invention calls for the tangential introduction of the pulp, or similar material to be Purified, into a chamber having a small, substantially cylindrical portion at'its top and a long,
  • An outlet for the constant withdrawal of a fraction, containing the bulk of the impurities, is provided at the bottom of the chamber and an outlet for the purified material, which preferably extends downwardly into the chamber, is provided at the center of the top.
  • the construction and arrangement is such that as the material, for example a water suspension, is introduced into the chamber at a relatively high velocity, in the neighborhood of 25 feet per second, a vortex or vortical whirl is created and a centrifugal force is set up upon the particles, those having a slightly higher specific gravity, or which are otherwise thrown more readily and forcibly outward, being brought against or near the wall of the cone while the lighter particles, or those affected less by the centrifugal action, are carried or remain more nearly toward the inner surface of the downwardly moving and rotating stream.
  • the vortex or vortical whirl causes an upwardly moving and whirling stream at the center of the chamber within the downwardly moving stream.
  • the centrifugal force acting upon the particles varies directly with the square of the velocity and inversely with the radius of the path of the motion.
  • the velocity tends to decrease slightly as the material advances toward the apex of the cone, due to the retarding effect of friction, but this may be more than offset by the tendency to increase the velocity as the pressure of the fluid drops and is converted into kinetic energy. It will be understood that a substantial pressure drop will take place between the inlet and outlet of the chamber. At the same time the radius of the whirling motion is decreasing, with the effect of increasin the centrifugal force.
  • the centrifugal force upon the particles will not decrease but will, in fact, increase as the material progresses along the conical wall. Moreover, whatever increase takes place will be more or less uniform, i. e., there will be no abrupt change.
  • the upwardly moving stream at the center of the vortex has a hollow core extending from the lower to the upper outlet. If the lower'outlet is in free communication with the atmospherathe interior of the hollow core is maintainedat substantially atmospheric pressure but if the lower end ofthe device is immersed in liquid, there is a tendency to produce a sub-atmospheric pressure within the core due to the removal of air bubbles in the stream leaving the top of the device. This has the further tendency of reducing the diameter of the hollow core by the pumping up of liquid from below the lower outlet, thereby al so tending to carry dirt back into the ascending stream.
  • the apex of the device is arranged to discharge into the free atmosphere, so that the center or the vortex is filled with 'air at atmospheric pressure, the outflow at the apex need not be quite as reat as if the latter is immersed in the liquid and an opportunity is afiorded for the dirt to be carried back into the ascending stream.
  • the size of the discharge opening at the apex ofthe conical portion of the chamber is of considerable imefiiciency will be discussed in tain parts, the conditions or operation and the of eliminating a certain percentage of a standardized material constituting the impurityfl-i'rom a given quantity of a standard type of Pulp in suspension. All factors, such as the recover of fibers from the dirty fraction, have been taken into account in making the emciencydeterminations. The bearin 01 certain factors upon such reater detail hereinafter.
  • the partially purified material may be passed through another similar separator and thus subjected to] further purification. As many successive treatments of this character may be carried out as required to bring about the desired ultimate purity'of the pulp. when this fractionation method is employed in two or more stages, the separation in a single unit need not be carried to the maximum possible extent. A smaller percentage of the impurities maybe removed in each stage. 80 also,
  • the fraction containing the bulk of the impurities withdrawn from the apex of the conical portion of the separator may be subjected to further treatment to avoid the loss of the good fibers necessarily included in the dirty fraction.
  • a somewhat greater portionof the original suspension may be taken as the dirty fraction in the first stage thus insuring greater purity of the clean fraction; and the subsequent repetition of the treatment upon the dirty. fraction will prevent the excessive loss of good fibers.
  • pluralityof units may be operated in parallel portance, as alreadyexplained. It must be such.
  • the separating chamber is preferably of very simple construc-' tion, having a substantially cylindrical top portion 10 and-an elongated, conical, lower portion H.
  • the inner wall oi?v the chamber, particularly the inner surface of the conical portion H,
  • the chamber is formed, preferably, of a suitable metal capable of resisting the corrosive action of the pulp i or other material to be handled. If desired, the inner surface of the chamber may be simply coated or otherwise protected for this purpose.
  • An inlet I2 is arranged to permit the tangential introduction of the material to be purified or fractionated into the cylindrical portion of the separator; This inlet may be disposed in a plane perpendicular to the axis of the chamber or may be inclined slightly toassist in directing the streamof material toward the apex of the cone as it whirls around the inner surface of the chamber. Other special arrangements for insuring the smooth and uniform introduction of the material tangentially into the chamber may be employed, if desired. At the lower end or apex of the conical portion ll there is provided From these pressures'the various dimensions and the nature of the material, the velocity and other conditions of flow of the material at various points may be determined with the aid of empirical data.
  • the specific dimensions of the separator may be varied considerably within limits, particularly when a change in one dimension is oflset by corresponding changes in other dimensions or in operating conditions, it has been found that very good results may be obtained from a construction in which the cylindrical'portion or the chamber is approximately 3'inches in diameter and about 1% inches in depth while the conical portion, considering the apex as if extended to a point, has an altitude'of about 33 inches.
  • the inlet I2 may have a diameter of approximately half an inch while the outlet l3 may be slightly less than a quarter of an inchin diameter and the outlet I! may have a diameter of slightly more thanhalf an inch.
  • the outlet tube IS in this typical unit extends to a point about 1.75 inches below the center line of the inlet I2, andabout three-quarters of an inch below the juncture of the'cylindrical and conical portions.
  • the center line of the inlet 42 is about three-eighths of an inch below the end l6 of the chamber.
  • the optimum size of the lower outlet I I is an opening i3 which may, if desired, be variable I or adjustable as to size,'although it should be kept constantly open to permit the continuous discharge of a portion of the material introduced into the chamber.
  • a pipe l4 may be connected in any convenient way with the tip of the conical portion, to receivefthe. material discharged through the opening 13 and convey it to a closed chamber (not shown) or to any other desired point. The pipe l4 should be so formed and consomewhat smaller than forunbeaten pulp.
  • an outlet tube I5 is provided at the center or a closure member l6 which otherwise closes the top of the cylindrical portion In.
  • the tube l5 preferably extends into the chamber to aP int inward of the axis of the inlet pipe i2.
  • Suitable pressure gauges l1. l8 and I9 may conveniently be provided in the several tubes l2, I4 and I5, respectively, to en- I able the determination of the pressure of the material entering the chamber at the inlet and being withdrawn from the chamber at the two outlets.
  • the pressure of the material so discharged may be about 12 pounds per square inch.
  • the various linear dimensions given for the first model described may be varied simultaneously in the same ratio from about 0.65 to 1.36 times the specified values without reducing the efilciency below two-thirds of the maximum. Taking into account this permissible range of variations in the several linear dimensions as a whole,- it will be possible to vary any single dimension through a somewhat greater total range than indicated above, without unduly reducing the efilciency of the device.
  • the pressure of the material at the inlet may be varied widely, say from about 6 to 80 pounds per square inch, although it is preferably kept between 15 and 65; the pressure at the outlet l or b may be varied from about 2 to 18 or even 22 pounds per square inch, while the pressure atthe outlet l3 or g is preferably atmospheric.
  • the velocity of the material entering the chamber through the inlet l2 may be varied between about and 70 feet per second.
  • the mean outward component of the velocity over the lower outlet may be varied from 6 to 55 feet per second, and that over the upper outlet between 8 and 45 feet per second without reducing the efilciency below two-thirds of the maximum, provided the velocity in question is produced by a proper choice of dimensions and pressures and consistency within the preferred ranges given elsewhere.
  • the volume of flow through the outlet l3 should be. between 2 and 35% of the volume of all input in order to maintain an efiiciency of the character mentioned.
  • the result of varying the diameter of the outlet I5 is to increase the purity of the clean fraction of the stock as the diameter decreases but this is at the expense of the percentage of the total stock which is removed as the clean fraction.
  • Aplurality of the separators may be employed in parallel where the capacity of a single separator is insufficient to handle the amount of pulp to be purified in a given time.
  • a system of fractionation may be employed in which a certain extent of purification is obtained in each of the successive stages.
  • a typical in- .stallation may comprise a multiplicity of the separators, some in parallel to increase the capacity of the installation as whole and some in series to improve the purity of the final product and reduce the loss of good fibers.
  • the pulp to be purified is delivered through a pipe 20 to a pump or series of pumps 2
  • the purified pulp is withdrawn through a line 24 connected with the tops of the plurality of separators 23 and may deliver the pulp to any convenient point.
  • a fairly large dirty fraction may be withdrawn through a line 25 connected with the apex of each of the separators 23 or connected with a vessel into which the apices of the separators discharge.
  • about 2 0 gallons per minute of pulp containing the removed impurities may be withdrawn through the line 25.
  • a pump 26 which also receives fresh water to theextent of about 1163 gallons per minute through a line 21 and delivers the mixture through a line "to a further group of separators 29 in parallel. About 180 units in the group 29 will be required to handle the material delivered. by the pump 26.
  • the purified fraction from the units 29 may be withdrawn through a line 30 and passed to the pump 2
  • About 2920 gallons per minute may be so delivered through the line 30.
  • the heavier fraction, containing the impurities to be removed, will be withdrawn through the, apex of each of the units 29 and passed through a line 3
  • About 410 gallons per minute may be so withdrawn and. diluted at the pump with about 380 gallons per minute of fresh water delivered through a line 33. The mixture is then.
  • the purified fraction in the amount of about 210 gallons per minute is delivered to the pump 32 while the dirty fraction in the amount of about 29.5 gallons per minute is withdrawn through the line 43, connecting with the apex of each of the separators.
  • pulp in the amount of 7580 gallons per minute may be purified by discarding only between 29 and 30 gallons per minute with the bulk of the impurities contained therein.
  • the clean fraction discharged from the first group of separators 23, through the line 24' may be subjected to a further separating treatment. This is in the event that a higher purity of the final product is sought.
  • the partially purified material may be delivered to a pump 44, which will discharge itthrough a line 45 into another group of separators 46, about 498 in number, from which the purified fraction may be withdrawn through a line 41 and delivered to any convenient point.
  • the dirty fraction withdrawn through a line 48 may, in this case, -be deliveredto the pump 2
  • suilicient water should be added to the fraction returned from the separators I. or otherwise added in advance the separators II to insure the proper consistency of the material delivered to these separatorafl
  • the number of separator units 40 could, if desired, be reduced to 430 if a pulp thickener is used tolraise the consistency of the ingoing pulp to 0.5fper cent as for the other units.
  • an outlet tube having a diameter between one-eighth and onequarter thatof said cylindrical portion extend ing through said closure member and axially into said chamber, a continuously unobstructed outlet at the apex of said conical portion of ap-, proximately one-quarter'the cross-sectional area of said outlet tube, and an inlet disposed tan gentially of said cylindrical portion.
  • a chamber having a short cylindrical portion of between 2.0 and 4.2 inches in diameter and having a long conical portion exaxiaily from said cylindrical portion toward an apex, said conical portion having a length between 5 and 15 times the diameter of gentially of said cylindrical portion and having a diameter of between 0.175 and 0.65 inch, an
  • said conical portion extending axially from said cylindrical portion toward an apex, said conical portion having a length between 10 and times its greatest diameter, an inlet arranged tangentially of said cylindrical 'portion and having a diameter of about half an inch, an outlet at the apex of said conical portion having a diameter of about onequarter of an inch, and an outlet at the center ofsaid cylindrical portion about half an inch.
  • a method of separating, from a pulp suspension, solids having a settling rate of as low as 5 centimetersper minute in still water which comprises spinning saidsuspension to produce a vortex of gradually decreasing diameter, continuously withdrawing a portion or the suspension a diameter of I from thepoint of minimum diameter, and causameter.
  • a method of separating, from a pulp suspension, solids having a settling rate of between 5 and 25 centimetersper minute in still water which comprises spinning said suspension .in an elongated conical path to produce avortex of gradually and constantly decreasing diameter; continuously withdrawing a portion of the suspension from the point of minimum diameter,
  • a method of separating, from, a pulp suspension, substances having a settling rate of between 5 and 25 centimeters per minute in still water which comprises spinning said suspension and causing it to advance from the base to the apex of a conical path having an angle at its apex of not more than.l5 degrees, continuously withdrawing a portion of the suspension at the apex of said conical path, causing the balance of the suspension to return freely and without obstruction toward thebase of the conical path at the interior thereof, and withdrawing at least a part of said balance of the suspension from a point along the axis of the cone.
  • a method of separating, from a pulp suspension, substances having a settling rate of between 5 and 25 centimeters per minute in still water which comprises spinning said suspension in a conical path starting with a diameter of 'said cylindrical portion, an inlet arranged tanoutlet at the apex of said conical portion having a diameter of between 0.14 and 0.40 inch, and an outlet at the center of said cylindrical portion having a diameter of between 0.37 and 0.75 inches 2.0 and 4.2 inches in diameter, a long conical pornot more than about 5 inches at its base and advancing toward the apex at an angle to the axis of said path of not more than about .7 degrees,
  • 9,-A method of separating, from a pulp suspension, substances having a settling rate of less than 25 centimeters per minute in still water which comprises introducing said suspension tangentially into an elongated vessel tapering gradually from a point adJacent the point of introduction toward an apex at a turbulence creating velocity so as to produce a vortex, continuously withdrawing a portion of the suspension at said apex, causing the balance of the suspension to return freely and without obstruction in the opposite direction at the interior of the vortex from points inward ofsaid apex, and withdrawing at least a part or said balance at a'point inwardly of the plane of the axis along which the suspension is introduced.
  • a method of removing'from a pulp suspen sion impurities having nearly the same centrifugal force reaction as the pulp fibers which comprises continuously introducing a stream of'the pulp suspension tangentially into a closed chamber, confining said stream to a 'path of constantlybut gradually decreasing radius, thereby exerting a; gradual inward force in opposition to the centrifugal force generated upon the impurities, and causing thepulp suspension to move without interruption along the wall of the chamber toward thepoint of minimum radius and then in the-opposite direction adjacent the-axis of the chamber, continually withdrawing a portion at' the.
  • a method of removing from a pulp suspension impurities of nearly the same centrifugal force reaction as the pulp fibers which comprises continuously introducing a stream of the pulp suspension tangentially into a closed chamber, confining said stream to a path of constantly but gradually decreasing radius, thereby exerting a gradual inward force in opposition to the centrifugal force generated upon the'impurities.
  • the pulpsuspension to advance without interruption along the wall of'the chamber toward the point of minimum radius and then in the opposite direction adjacent the axis of the chamber, the axial distance from the plane of maximum radius to the plane of minimum radius of said path being at least 10 times said maximum radius, continually withdrawing a portion at'the point of minimum radius in the path of said stream, and continually withdrawing another portion of the material at a point alon the axis of the chamber in a plane of relatively great radius.
  • a method of removingfrom a pulp suspension impurities of nearly the same centrifugal force reaction as the pulp fibers which comprises subjecting a continuous stream of the suspension to an uninterrupted whirling motion along an elongated conical path and then freely in the opposite axial direction within the conical path but leaving an air space in the region of said axis, continually withdrawing into free air a sufaera e-i ficient fraction of the suspension from a point adjacent the apex of said path to cause a positive outward flow, returning the balance of the suspension constituting the major fraction of the original stream adjacent the axis of the vortex toward the larger end of the conical path, and continually withdrawing at least a part of. said major fraction froma point along said axis removed from said apex.
  • a method of separating, from a pulp suspension, substances having a settling rate of less than 25 centimeters per minute in still water which comprises spinning said liquid suspension and causing it to advance from the base to the apex of a long conical path having a major diameter of not more than five inches and an angle at its apex of not more than 15 degrees, continuously withdrawing a portion of the suspension at the apex of said conical path, causing the balance of the suspension to return freely and without obstruction toward :the base of the conical path at theinterior thereof, withdraw.- ing at least a part of said balance of the suspension from a point along the axis ofthe' conical path' removed from the apex, and subject; ing at least one of the withdrawn portions to the same separating treatment.
  • Apparatus for the separation of solids from liquid suspension which comprises a pluralityof separator units, each unit comprising a vessel having an elongated conical'portion having a maximum diameter not exceeding 5 inches and a length at least five times the maximum diameter, a tangentially disposed inlet adjacent the larger endof said conical portion, and outlets adjacent the smaller and larger ends of said conical portion for the removal of fractions of the liquid suspension, means for delivering streams of said liquid suspension under pressure to a portion of said units in parallel, and means connected with the outlets at the larger ends of said units for delivering the fractions of said suspension removed through said outlets in streams under pressure to another portion of said plurality of units.
  • Apparatus for separating solid particles from liquid suspension which comprises a chamber of circular transverse cross-section, a relatively large portion of said chamber being of gradually decreasingradius from one end thereof to the other, the interior wall of said portion of said chamber being smooth and free from ob structions and abrupt changes in direction and having a maximum diameter not exceeding five inches, a tangentially disposed inlet adjacent the larger end of said portion for the introduction of a suspension to be purified, an outlet for the removal of a fraction of the suspension adjacent the smaller end of said portion of the chamber, and a larger outlet adjacent the center of the larger end of said portion for the removal of another fraction of the suspension, the length of said portion of the chamber being at least four times but not more than about fifteen times its maximum diameter.
  • a centrifugal separator for removing solids from liquid suspension comprising a chamber which consists primarily of a conical portion whose length is more than four times but not more than about fifteen times its greatest diameter, an inlet disposed tangentially of said chamber adjacent the larger end of said conical portion, an outlet at the apex of said conical portion, a second outlet through the opposite end of said chamber axially alined with said first mentioned outlet, said second outlet being 01' greater area than said outlet at the apex and having a diameter less than one-quarter the greatest diameter of said conical portion.
  • a centrifugal separator for removing solids from liquid suspension comprising a chamber which consists primarily of a. conical portion 1 whose length is more than four times but not more than about fifteen times its greatest diameter, an inlet disposed tangentially of said chamber adjacent the larger end of said conical portion. an outlet at the apex of said conical portion, a second outlet through the opposite end of said chamber axially alined with said first mentioned outlet, said outlet at the apex having a diameter less than one-sixth the greatest diameter oi said conical portion.
  • a centrifugal separator for removing solids from liquid suspension comprising a chamber which consists primarily of a conical portion whose length is more than four times but not more than about fifteen times its greatest diameter, an inlet disposed tangentially of said chamber adjacent the larger end of said conical portion, an outlet at the apex of said conical portion, a second outlet through the opposite end of said chamber axially alined with said first mentioned outlet, said outlet at the apex having a diameter less than one-sixth the greatest diamter of said conical portion, and said second outlet having a diameter less than one-fourth of the greatest diameter of said conical portion.
  • a method of removing irom a liquid suspension of solids impurities having nearly the same centrifugal force reaction as said solids which comprises continuously introducing a stream of the suspension tangentially into a closed chamber, confining said stream to a path of constantly but gradually decreasing radius, thereby exerting a gradual inward force in opposition to the centrifugal force generated upon the impurities, and causing the suspension to move without interruption along a confining wall toward the point of minimum radius and then in the opposite direction adjacent the axis of the path, continually withdrawing a portion at the point of minimum radius in the path of said stream, and continually withdrawing another portion of the material at the center of the chamber in a region of relatively great radius.

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US2642185A (en) * 1949-01-15 1953-06-16 Stamicarbon Process for the refining of starch
US2648433A (en) * 1948-02-16 1953-08-11 Mij Voor Kolenberwerking Stami Process and apparatus for controlling the density of the apex discharge of a cyclone
US2654479A (en) * 1938-12-28 1953-10-06 Directie Van De Staatsmijnen D Separation of suspensions of solid matter in liquids
DE894194C (de) * 1947-01-23 1953-10-22 Vickerys Ltd Verfahren und Vorrichtung zum Betrieb von Wirbelabscheidern fuer die Verarbeitung von Papierstoff u. dgl.
US2692677A (en) * 1951-02-09 1954-10-26 Dorr Co Process for classifying magnetized or magnetizable solids
US2702630A (en) * 1949-06-18 1955-02-22 Sharples Corp Classification of particles
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US2792910A (en) * 1953-10-14 1957-05-21 Redniss Alexander Cyclone separator
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DE1017551B (de) * 1953-02-17 1957-10-17 Stamicarbon Verfahren und Vorrichtung zur Trennung einer fluessigen Suspension von Feststoffgemengen
US2835387A (en) * 1948-03-25 1958-05-20 Stamicarbon Centrifugal method and means for continuously fractionating solid particles in liquid suspension thereof
US2840524A (en) * 1954-09-23 1958-06-24 Dorr Oliver Inc Hydrocyclone countercurrent washing system
DE1034472B (de) * 1955-06-15 1958-07-17 Kamyr Ab Verfahren und Vorrichtung zur Verwertung der Abwaerme der beim Entleeren von kontinuierlichen Zellstoffkochern anfallenden Daempfe und Gase
DE1036030B (de) * 1953-04-21 1958-08-07 Rotareaed Corp Verfahren und Anlage zum kontinuierlichen Entgasen und Reinigen von in Fluessigkeit aufgeschwemmter Papiermasse
US2849930A (en) * 1952-09-24 1958-09-02 Nichols Engineering And Res Co Method and apparatus for treating pulp suspensions and other fluids for removal of undesired particles and gases
US2878934A (en) * 1957-11-01 1959-03-24 Smith Paper Mills Ltd Howard Method and apparatus separating dirt from aqueous suspensions of pulp fibres
US2897972A (en) * 1956-03-28 1959-08-04 Bird Machine Co Separator
DE1063121B (de) * 1956-06-25 1959-08-13 Shell Res Ltd Kontinuierliches Verfahren zum Regenerieren gebrauchter Filterhilfsmittel
US2920761A (en) * 1952-09-24 1960-01-12 Nichols Engineering And Res Co Apparatus for separating and deaerating pulp suspension
US2927693A (en) * 1955-03-10 1960-03-08 Horace Freeman Cleaning of paper pulp suspensions
US2931503A (en) * 1953-04-21 1960-04-05 Clark & Vicario Corp Conditioning paper-making stock
US2954871A (en) * 1956-07-30 1960-10-04 Pan American Petroleum Corp Cyclonic separation of drilling fluids
US2975896A (en) * 1955-05-02 1961-03-21 Hirsch Siegfried Hydrocyclone for fibres suspension
US3037628A (en) * 1953-06-22 1962-06-05 Dominion Tar And Chemical Co Apparatus for separating dirt from aqueous suspensions of pulp fibers
US3136723A (en) * 1959-02-27 1964-06-09 Bass Brothers Entpr Inc Hydrocyclones
US3280976A (en) * 1962-04-17 1966-10-25 Coal Industry Patents Ltd Hydraulic classifier with underflow discharge control
US3352745A (en) * 1960-02-29 1967-11-14 Svenska Cellnlosa Aktiebolaget Process of separating fibrous pulp into springwood and summerwood fibers by centrifuging
US3372803A (en) * 1964-07-30 1968-03-12 Chembestos Corp Means and method for removing iron from asbestos ore
US3399770A (en) * 1966-01-19 1968-09-03 Beloit Corp Method for centrifugal separation of particles from a mixture
US3404778A (en) * 1964-11-18 1968-10-08 Bauer Bros Co Hydrocyclone
US3425545A (en) * 1963-08-02 1969-02-04 Rudolf Zemanek Method and apparatus for separating fibrous suspensions
US3441135A (en) * 1966-11-25 1969-04-29 Donaldson Co Inc Particle classification device and method
US3472371A (en) * 1966-10-04 1969-10-14 Ronald Percy Ayerst Sorting fibrous material
US3485356A (en) * 1967-04-11 1969-12-23 Alsace Mines Potasse Method for the treatment of ores containing slime-forming impurities
US3486619A (en) * 1968-01-24 1969-12-30 Wikdahl Nils Anders Lennart Method of removing impurities from a fiber suspension
US3487923A (en) * 1968-08-28 1970-01-06 Canadian Patents Dev Apparatus for separating aqueous suspensions of solid particles
US3503503A (en) * 1967-07-05 1970-03-31 Jean Claude Ramond Apparatus for the purification of liquid suspensions
DE1417056B1 (de) * 1958-03-01 1970-08-06 Voith Gmbh J M Rohrschleuder zum Reinigen von Faserstoffaufschwemmungen
US3612276A (en) * 1969-04-29 1971-10-12 Bird Machine Co Vortex-type separator apparatus
US3735869A (en) * 1970-10-29 1973-05-29 Union Carbide Corp Cyclone particle separator
US3831746A (en) * 1969-07-03 1974-08-27 R Hughart Recovering filter aid particles from filter cake
US3928186A (en) * 1973-07-24 1975-12-23 Boise Cascade Corp Combined pulp cleaning system including high and low pressure drop hydrocyclone cleaners
US4097375A (en) * 1977-01-31 1978-06-27 Luhring Chicago Industries Hydrocyclone separator
US4107033A (en) * 1976-03-20 1978-08-15 Hermann Finckh Maschinenfabrik Apparatus for cleaning fibrous suspensions of low stock consistency
US4155839A (en) * 1977-11-28 1979-05-22 The Black Clawson Company Reverse centrifugal cleaning of paper making stock
US4235363A (en) * 1979-07-09 1980-11-25 Liller Delbert I Method of installing replacable sleeve in fixed vortex finder
US4280902A (en) * 1979-07-04 1981-07-28 Kamyr Aktiebolag Separation of dense impurities from a fluid
US4364822A (en) * 1981-04-13 1982-12-21 Rich Jr John W Autogenous heavy medium process and apparatus for separating coal from refuse
US4378289A (en) * 1981-01-07 1983-03-29 Hunter A Bruce Method and apparatus for centrifugal separation
WO1986001130A1 (en) * 1984-08-02 1986-02-27 B.W.N. Vortoil Rights Co. Pty. Ltd. Cyclone separator
US4764287A (en) * 1984-08-02 1988-08-16 B.W.N. Vortoil Rights Co. Pty. Ltd. Cyclone separator
US4964994A (en) * 1989-03-21 1990-10-23 Amoco Corporation Hydrocyclone separator
US5078549A (en) * 1989-07-19 1992-01-07 J. M. Voith Gmbh Hydrocyclone
DE9207991U1 (de) * 1992-06-13 1992-09-03 Eckert, Otto, 6970 Lauda-Königshofen Fliehkraftabscheider für ein Gas-Flüssigkeitsgemisch
WO1997006871A1 (en) * 1995-08-11 1997-02-27 The Black Clawson Company Extended dwell reverse hydrocyclone cleaner
US5667686A (en) * 1995-10-24 1997-09-16 United States Filter Corporation Hydrocyclone for liquid - liquid separation and method
US5769243A (en) * 1996-07-30 1998-06-23 Thermo Black Clawson Inc. Through-flow cleaner with improved inlet section
EP1123723A1 (en) * 2000-02-10 2001-08-16 Fernando H. Garcia Plant for separating solid particles from a liquid phase
US20090188635A1 (en) * 2008-01-28 2009-07-30 Andritz Oy Method and apparatus for treating pulp
US20130008840A1 (en) * 2011-07-06 2013-01-10 Pesetsky Serge Particle separator
US20150330687A1 (en) * 2014-05-14 2015-11-19 Lg Electronics Inc. Oil separator and air conditioner having the same
US11162149B2 (en) * 2016-06-01 2021-11-02 Keller Technologies, Inc. Refiner for lactose and high lactose products

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1289516B (de) * 1959-04-01 1969-02-20 Bauer Bros Company Hydrozyklon
DE1293129B (de) * 1959-07-01 1969-04-24 Bauer Bros Company Verfahren und Vorrichtung zur Reinigung von Suspensionen

Cited By (77)

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US2704603A (en) * 1955-03-22 meaders
US2654479A (en) * 1938-12-28 1953-10-06 Directie Van De Staatsmijnen D Separation of suspensions of solid matter in liquids
US2590691A (en) * 1945-07-31 1952-03-25 Directie Staatsmijnen Nl Process for the separation of solid substances of different specific gravity and grain size
US2573192A (en) * 1946-12-09 1951-10-30 Directie Staatsmijnen Nl Cyclone
DE894194C (de) * 1947-01-23 1953-10-22 Vickerys Ltd Verfahren und Vorrichtung zum Betrieb von Wirbelabscheidern fuer die Verarbeitung von Papierstoff u. dgl.
US2504944A (en) * 1947-03-10 1950-04-18 Buckeye Cotton Oil Company Apparatus for purifying raw cotton linters
US2648433A (en) * 1948-02-16 1953-08-11 Mij Voor Kolenberwerking Stami Process and apparatus for controlling the density of the apex discharge of a cyclone
US2835387A (en) * 1948-03-25 1958-05-20 Stamicarbon Centrifugal method and means for continuously fractionating solid particles in liquid suspension thereof
US2531785A (en) * 1948-09-10 1950-11-28 Johnson & Son Inc S C Wax refining
US2642185A (en) * 1949-01-15 1953-06-16 Stamicarbon Process for the refining of starch
US2702630A (en) * 1949-06-18 1955-02-22 Sharples Corp Classification of particles
US2754968A (en) * 1950-03-09 1956-07-17 Stamicarbon Treatment of liquid materials in a hydrocyclone
US2737857A (en) * 1950-07-01 1956-03-13 Kimberly Clark Co Hydraulic apparatus
US2649963A (en) * 1950-12-05 1953-08-25 Stamicarbon Apparatus for continuously separating solids in or from liquid suspensions thereof
US2692677A (en) * 1951-02-09 1954-10-26 Dorr Co Process for classifying magnetized or magnetizable solids
US2920761A (en) * 1952-09-24 1960-01-12 Nichols Engineering And Res Co Apparatus for separating and deaerating pulp suspension
US2849930A (en) * 1952-09-24 1958-09-02 Nichols Engineering And Res Co Method and apparatus for treating pulp suspensions and other fluids for removal of undesired particles and gases
DE1017551B (de) * 1953-02-17 1957-10-17 Stamicarbon Verfahren und Vorrichtung zur Trennung einer fluessigen Suspension von Feststoffgemengen
US2931503A (en) * 1953-04-21 1960-04-05 Clark & Vicario Corp Conditioning paper-making stock
DE1036030B (de) * 1953-04-21 1958-08-07 Rotareaed Corp Verfahren und Anlage zum kontinuierlichen Entgasen und Reinigen von in Fluessigkeit aufgeschwemmter Papiermasse
US3037628A (en) * 1953-06-22 1962-06-05 Dominion Tar And Chemical Co Apparatus for separating dirt from aqueous suspensions of pulp fibers
US2809567A (en) * 1953-09-16 1957-10-15 Bauer Bros Co Apparatus for separating solids from a liquid suspension
US2792910A (en) * 1953-10-14 1957-05-21 Redniss Alexander Cyclone separator
US2840524A (en) * 1954-09-23 1958-06-24 Dorr Oliver Inc Hydrocyclone countercurrent washing system
DE1092445B (de) * 1955-03-10 1960-11-10 Nichols Engineering & Res Corp Vorrichtung zum Ausscheiden unerwuenschter Teilchen aus Fluessigkeiten
US2927693A (en) * 1955-03-10 1960-03-08 Horace Freeman Cleaning of paper pulp suspensions
US2975896A (en) * 1955-05-02 1961-03-21 Hirsch Siegfried Hydrocyclone for fibres suspension
DE1034472B (de) * 1955-06-15 1958-07-17 Kamyr Ab Verfahren und Vorrichtung zur Verwertung der Abwaerme der beim Entleeren von kontinuierlichen Zellstoffkochern anfallenden Daempfe und Gase
US2897972A (en) * 1956-03-28 1959-08-04 Bird Machine Co Separator
DE1063121B (de) * 1956-06-25 1959-08-13 Shell Res Ltd Kontinuierliches Verfahren zum Regenerieren gebrauchter Filterhilfsmittel
US2954871A (en) * 1956-07-30 1960-10-04 Pan American Petroleum Corp Cyclonic separation of drilling fluids
US2878934A (en) * 1957-11-01 1959-03-24 Smith Paper Mills Ltd Howard Method and apparatus separating dirt from aqueous suspensions of pulp fibres
DE1417056B1 (de) * 1958-03-01 1970-08-06 Voith Gmbh J M Rohrschleuder zum Reinigen von Faserstoffaufschwemmungen
US3136723A (en) * 1959-02-27 1964-06-09 Bass Brothers Entpr Inc Hydrocyclones
US3352745A (en) * 1960-02-29 1967-11-14 Svenska Cellnlosa Aktiebolaget Process of separating fibrous pulp into springwood and summerwood fibers by centrifuging
US3280976A (en) * 1962-04-17 1966-10-25 Coal Industry Patents Ltd Hydraulic classifier with underflow discharge control
US3425545A (en) * 1963-08-02 1969-02-04 Rudolf Zemanek Method and apparatus for separating fibrous suspensions
US3372803A (en) * 1964-07-30 1968-03-12 Chembestos Corp Means and method for removing iron from asbestos ore
US3404778A (en) * 1964-11-18 1968-10-08 Bauer Bros Co Hydrocyclone
US3399770A (en) * 1966-01-19 1968-09-03 Beloit Corp Method for centrifugal separation of particles from a mixture
US3472371A (en) * 1966-10-04 1969-10-14 Ronald Percy Ayerst Sorting fibrous material
US3441135A (en) * 1966-11-25 1969-04-29 Donaldson Co Inc Particle classification device and method
US3485356A (en) * 1967-04-11 1969-12-23 Alsace Mines Potasse Method for the treatment of ores containing slime-forming impurities
US3503503A (en) * 1967-07-05 1970-03-31 Jean Claude Ramond Apparatus for the purification of liquid suspensions
US3486619A (en) * 1968-01-24 1969-12-30 Wikdahl Nils Anders Lennart Method of removing impurities from a fiber suspension
US3487923A (en) * 1968-08-28 1970-01-06 Canadian Patents Dev Apparatus for separating aqueous suspensions of solid particles
US3612276A (en) * 1969-04-29 1971-10-12 Bird Machine Co Vortex-type separator apparatus
US3831746A (en) * 1969-07-03 1974-08-27 R Hughart Recovering filter aid particles from filter cake
US3735869A (en) * 1970-10-29 1973-05-29 Union Carbide Corp Cyclone particle separator
US3928186A (en) * 1973-07-24 1975-12-23 Boise Cascade Corp Combined pulp cleaning system including high and low pressure drop hydrocyclone cleaners
US4107033A (en) * 1976-03-20 1978-08-15 Hermann Finckh Maschinenfabrik Apparatus for cleaning fibrous suspensions of low stock consistency
US4097375A (en) * 1977-01-31 1978-06-27 Luhring Chicago Industries Hydrocyclone separator
US4155839A (en) * 1977-11-28 1979-05-22 The Black Clawson Company Reverse centrifugal cleaning of paper making stock
US4280902A (en) * 1979-07-04 1981-07-28 Kamyr Aktiebolag Separation of dense impurities from a fluid
US4235363A (en) * 1979-07-09 1980-11-25 Liller Delbert I Method of installing replacable sleeve in fixed vortex finder
US4378289A (en) * 1981-01-07 1983-03-29 Hunter A Bruce Method and apparatus for centrifugal separation
US4364822A (en) * 1981-04-13 1982-12-21 Rich Jr John W Autogenous heavy medium process and apparatus for separating coal from refuse
WO1986001130A1 (en) * 1984-08-02 1986-02-27 B.W.N. Vortoil Rights Co. Pty. Ltd. Cyclone separator
US4764287A (en) * 1984-08-02 1988-08-16 B.W.N. Vortoil Rights Co. Pty. Ltd. Cyclone separator
AU592063B2 (en) * 1984-08-02 1990-01-04 Conoco Specialty Products Inc. Cyclone separator
GB2187401A (en) * 1984-08-02 1987-09-09 Bwn Vortoil Rights Co Pty Ltd Cyclone separator
US4964994A (en) * 1989-03-21 1990-10-23 Amoco Corporation Hydrocyclone separator
US5078549A (en) * 1989-07-19 1992-01-07 J. M. Voith Gmbh Hydrocyclone
DE9207991U1 (de) * 1992-06-13 1992-09-03 Eckert, Otto, 6970 Lauda-Königshofen Fliehkraftabscheider für ein Gas-Flüssigkeitsgemisch
US5938926A (en) * 1995-08-11 1999-08-17 Thermo Black Clawson Extended dwell reverse hydrocyclone cleaner
WO1997006871A1 (en) * 1995-08-11 1997-02-27 The Black Clawson Company Extended dwell reverse hydrocyclone cleaner
EP0863784A1 (en) * 1995-08-11 1998-09-16 The Black Clawson Company Extended dwell reverse hydrocyclone cleaner
EP0863784A4 (en) * 1995-08-11 1999-01-20 Black Clawson Co REVERSE HYDROCYCLONE CLEANER WITH EXTENDED RETENTION
US5667686A (en) * 1995-10-24 1997-09-16 United States Filter Corporation Hydrocyclone for liquid - liquid separation and method
US5769243A (en) * 1996-07-30 1998-06-23 Thermo Black Clawson Inc. Through-flow cleaner with improved inlet section
EP1123723A1 (en) * 2000-02-10 2001-08-16 Fernando H. Garcia Plant for separating solid particles from a liquid phase
US20090188635A1 (en) * 2008-01-28 2009-07-30 Andritz Oy Method and apparatus for treating pulp
US7951263B2 (en) 2008-01-28 2011-05-31 Andritz Oy Method and apparatus for treating pulp
US20130008840A1 (en) * 2011-07-06 2013-01-10 Pesetsky Serge Particle separator
US9399182B2 (en) * 2011-07-06 2016-07-26 Johnson Electric S.A. Particle separator
US20150330687A1 (en) * 2014-05-14 2015-11-19 Lg Electronics Inc. Oil separator and air conditioner having the same
US11162149B2 (en) * 2016-06-01 2021-11-02 Keller Technologies, Inc. Refiner for lactose and high lactose products

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