US3172851A - Centrifuging liquid-solids mixtures - Google Patents

Centrifuging liquid-solids mixtures Download PDF

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Publication number
US3172851A
US3172851A US3172851DA US3172851A US 3172851 A US3172851 A US 3172851A US 3172851D A US3172851D A US 3172851DA US 3172851 A US3172851 A US 3172851A
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solids
liquid
discharge opening
bowl
conveyor
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
    • B04B1/20—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles discharging solid particles from the bowl by a conveying screw coaxial with the bowl axis and rotating relatively to the bowl

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  • This invention relates to separating solids from liquidsolid mixtures. More specifically, this invention relates to the separation from a liquid-solids mixture of solids of relatively small particle size and having little difference in density from the liquid of the mixture.
  • a screw conveyor Disposed axially within the rotor is a screw conveyor rotating at a speed different from the speed of the rotor.
  • the solids settle against the wall of the rotor and the conveyor engages the settled solids and plows them up a beach to discharge them through the second opening.
  • the liquid-vapor interface in such an apparatus has been set by the position of the first opening through which liquid discharges and invariably the inter face has been well outward from the second opening. The solids, therefore, in their travel up the beach inward of the liquid-vapor interface drain before discharging through the second opening with reduced moisture content.
  • FIGURE 1 is an elevational view partly in section and partly schematic, of an apparatus embodying the invention.
  • FIGURE 2 is a graph indicating the predictability of the apparatus and process of the invention in accomplishing a concentration.
  • my invention involves the process of separating solids from a liquid-solids mixture, the solids being of relatively small particle size and having little difference in density from the liquid, including the steps of feeding the mixture to a zone of centrifugation at a feed point, settling the solids, discharging the separated liquid at a first position, engaging the settled solids with a conveying surface and moving the solids with the surface axially away from the first position and the feed point and toward a second position radially outward from the first position to form automatically a dam of settled solids adjacent the second position, the dam extending inward of the first position to block substantially the flow of liquid to the second position, and discharging the separated solids outward from the second position.
  • the invention further involves apparatus by which the process of the invention may be accomplished.
  • an apparatus embodying my invention is generally designated 1t
  • the apparatus comprises a frame 12 including a pair of spaced aligned bearing units 14.
  • a rotor 16 comprises a peripheral wall and a pair of spaced end walls with shaft extensions mounted to rotate within the bearing units 14.
  • a constant speed motor may be connected to the rotor driving pulley 22.
  • Rotatably mounted within the rotor as shown is a conveyor element 24 having helical flights 26 and a feed opening 28 intermediate its ends.
  • a conveyor drive shaft 30 which extends axially within an opening of shaft 18, is adapted to drive the conveyor at a speed diiferent from that of rotor 16, receiving its power from rotor 16 through a gearbox 32 of structure similar to that disclosed in the above-identified Gooch patent.
  • Pulley 34 may also be driven by a motor of variable speed to control the speed differential between the conveyor 24 and rotor 16, in a manner also well known in the art. Feed is delivered to opening 28 through feed tube 36.
  • the leftward end Wall of the rotor as shown in FIG- URE 1 is formed with a large opening 38 spaced inwardly from the outermost inside surface of the peripheral wall of the rotor.
  • the opening 38 is preferably covered by a conventional adjustable plate with a smaller opening 49 in registry with opening 38 and providing liquid discharge to a radial level a, the level of the liquid interface.
  • a radially outward directed opening 42 comprising the solids discharge opening, the edge of this opening over which solids may discharge is at a level b outward from the level a of opening 40.
  • a filler section having for instance a frusto-conical inner surface comprising beach 44 up which the solids may be moved toward the opening 42 by the flights 2.6.
  • the outer edges of the flights are cut to terminate adjacent the beach in this area.
  • a cover 46 is partitioned to collect separately the discharged solids and liquid as is conventional.
  • the feed comprising a liquidsolids mixture is continuously introduced through feed tube 36 and feed opening 28 into the rotor 16 at a feed point.
  • the solids are permitted to settle against the wall of the rotor (FIGURE 1).
  • the separated liquid is dis charged through opening 40 to define the liquid-vapor interface at level a.
  • the rotor 16 and conveyor 24 are rotated in the same direction but at slightly different speeds to effect a rightward movement by the flights 26 of the solids toward the solids discharge port 42.
  • the solids with which the invention is particularly applicc ble are moved rightwardly, they presumably form in a short time a dam D immediately to the left of opening 42 blocking the passage of liquid out through this opening.
  • Continued movement of the solids causes a portion of the solids comprising the dam to continuously discharge through the port with reduced moisture content.
  • Other solids continuously move up to replace those discharged and to comprise the darn.
  • a liquid-solids mixture comprising dilute beer and yeast was fed to a nozzle centrifuge.
  • Typical of such a machine is the Nozljector centrifuge available from The Sharples Corporation of Philadelphia, Pennsylvania. From the nozzles of this centrifuge the solids discharged in a yeast slurry which analyzed at 9.62% solid matter, the remainder water and solubles.
  • This slurry was fed in the first example below to the conventional apparatus of the general type described in the afore entioned patent of F. P. Gooch. In the second example the slurry was fed to an apparatus embodying the invention.
  • Example I The nozzle discharge was delivered to an apparatus of the type described by Gooch and designated P-3000 by its manufacturers, The Sharples Corporation.
  • the rotor had an inside length of approximately 30%" and an inside diameter of about 14". It was driven at 4000 rpm. and the conveyor was rotated in the same direction at a differential of 15 r.p.m.
  • the solids discharge port was positioned inward of the liquid discharge port to provide a beach up which solids could be scrolled to drain before discharge.
  • the radial dilferential between the two ports was set at A Feed was delivered to the rotor at 150 pounds per hour dry basis. The operation was not stable on extended runs in that after a quarter of an hour or so at a constant rate the liquid efiluent that had been clear started to surge and was alternately clear and full of yeast.
  • Example 2 The apparatus was modified from Example 1 in accordance with the invention, all other conditions remaining the same.
  • the level of the liquid discharge port was moved inward to become inward of the solids discharge port. With this differential it was observed that on start-up all of the feed liquid at the beginning discharged from the solids discharge end as would be expected. After some two or three minutes liquid flow at this end stopped and liquid began to discharge from the liquid discharge port and two or three minutes subsequent yeast discharged continuously from the solids discharge port with good stability of operation over several hours.
  • This discharge analyzed at 19.0% solids.
  • the feed rate was increased and clear eifluent was obtained at rates of dry solids basis yeast discharge of over 400 pounds per hour at 16.6% dry substance content.
  • FIG- URE 2 indicates the predictable relationship between pounds dry substance and the percent dry substance of the discharge.
  • the solids discharge port be outward of the liquid discharge port, for if the solids discharge port is equal to or inward of the liquid discharge port the inability to scroll of the solids with which the invention is applicable results in surging of the discharges and instability. Further, by having the solids discharge out- Ward the force of the inward liquid makes discharge of the solids that much easier.
  • the invention is not only applicable to the separation of yeast solids from diluted beer, this being merely an example, the invention has other applicability, for instance, in the concentration of corn gluten and in other slurries, the solids of which have heretofore been regarded as non-scrollable.
  • I have thus developed an apparatus and process which may be used successfully in the concentration of solids which are not normally susceptible to processing in a worm-type centrifuge.
  • the apparatus and process involve a simple modification to a presently available machine to produce results which are totally new and wholly unexpected. These results are characterized by clean liquid discharge, continuous stable operation, and better concentration of solids than heretofore available from the centrifugal processing of these certain mixtures.
  • a process for separating solids from a liquid-solids mixture including the steps of (a) feeding the mixture to a zone of centrifugation at a feed point, the zone having a liquid discharge opening adjacent one end and a solids discharge opening at the other end and outward of said liquid discharge opening but inward from the outermost periphery of the zone,
  • the settled solids form a dam extending inward of the solids discharge opening, the dam being relatively impervious to the liquid and substantially blocking its escape through the solids discharge opening.
  • a centrifuge for separating solids from a liquidsolids mixture, the solids being of relatively small particle size and having little diiferencc in density from said liquid comprising (a) a hollow bowl mounted to rotate about an axis and having a portion of its inner surface decreasing in diameter approaching one end and having a solids discharge opening at the said end and a liquid discharge opening at the opposite end, the solids discharge opening being outward from the liquid discharge opening,
  • a helical conveyor disposed within the bowl and on said axis and extending substantially the inside length of the bowl and having flights with distal edges generally complementing the contour of the inside of the bowl, the conveyor being adapted in turning relative to the bowl to move settled solids inward over said portion to said solids discharge opening, the solids discharge opening being of more than ample dimension to pass without restriction material which is available to it,
  • (d) means to drive the bowl and the conveyor at different speeds whereby the solids in being moved by the conveyor toward the solids discharge opening form a darn extending inward of the solids discharge opening, the dam being relatively impervious to the liquid and substantially blocking its escape through the solids discharge opening.

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  • Centrifugal Separators (AREA)
US3172851D 1962-08-31 Centrifuging liquid-solids mixtures Expired - Lifetime US3172851A (en)

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Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3321131A (en) * 1964-10-21 1967-05-23 Bird Machine Co Centrifuge
US3431115A (en) * 1966-01-21 1969-03-04 Pennsalt Chemicals Corp Process for making bakers' cheese
US3494542A (en) * 1968-05-27 1970-02-10 Pennwalt Corp Centrifuging process and apparatus
DE2344507A1 (de) * 1972-09-06 1974-03-14 Pennwalt Corp Dekantierzentrifuge
US4575370A (en) * 1984-11-15 1986-03-11 Pennwalt Corporation Centrifuge employing variable height discharge weir
US4957475A (en) * 1988-05-11 1990-09-18 Flottweg Gmbh Solid-bowl helical centrifuge
US5257968A (en) * 1991-06-06 1993-11-02 Alfa Laval Separation Inc. Inflatable dam for a decanter centrifuge
US5261869A (en) * 1992-04-06 1993-11-16 Alfa Laval Separation, Inc. Decanter centrifuge having discontinuous flights in the beach area
US5342279A (en) * 1992-08-18 1994-08-30 Alfa Laval Separation Inc. Decanter centrifuge having dual motor drive
US5509882A (en) * 1994-09-12 1996-04-23 Tetra Laval Holdings & Finance S.A. Decanter centrifuge having an offset conveyor flight to aid rinsing
EP1304170A1 (de) * 2000-02-10 2003-04-23 KOTOBUKI ENGINEERING & MANUFACTURING CO LTD Zentrifugalabscheider
US20080257836A1 (en) * 2007-04-17 2008-10-23 Laughlin Henry J Centrifugal separator and method for separating heavy and light matter in a substance
WO2024132340A1 (de) * 2022-12-21 2024-06-27 Gea Westfalia Separator Group Gmbh Verfahren zur gewinnung von hochdichtem quark

Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US535306A (en) * 1895-03-05 stewaet
GB372679A (en) * 1930-10-11 1932-05-12 Separator Ab Improvements in scaping worms for centrifugal bowls
US2612314A (en) * 1949-03-28 1952-09-30 Lewis L Huelsdonk Centrifuge
US2625320A (en) * 1950-06-20 1953-01-13 Bird Machine Co Centrifuge for rapid extraction of fine particles from suspensions
US2679974A (en) * 1947-01-15 1954-06-01 Sharples Corp Bearing construction for continuous centrifuge
US2711854A (en) * 1952-05-14 1955-06-28 Aktiebolag Separator Centrifuge for separating sludge from liquids
US2733856A (en) * 1952-12-04 1956-02-07 Sludge centrifuge
US2743865A (en) * 1952-05-24 1956-05-01 Johan E A Graae Centrifugal separator
US2766930A (en) * 1951-12-14 1956-10-16 Starcosa Maschinen Und Appbau Centrifugal separator
US2795635A (en) * 1953-08-28 1957-06-11 Phillips Petroleum Co Centrifuge
US2862658A (en) * 1952-05-28 1958-12-02 Separator Ab Method and apparatus for centrifugal separation of a mixture of solids and two liquids
US3096282A (en) * 1957-12-30 1963-07-02 Sharples Corp Improvement in centrifuges

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US535306A (en) * 1895-03-05 stewaet
GB372679A (en) * 1930-10-11 1932-05-12 Separator Ab Improvements in scaping worms for centrifugal bowls
US2679974A (en) * 1947-01-15 1954-06-01 Sharples Corp Bearing construction for continuous centrifuge
US2612314A (en) * 1949-03-28 1952-09-30 Lewis L Huelsdonk Centrifuge
US2625320A (en) * 1950-06-20 1953-01-13 Bird Machine Co Centrifuge for rapid extraction of fine particles from suspensions
US2766930A (en) * 1951-12-14 1956-10-16 Starcosa Maschinen Und Appbau Centrifugal separator
US2711854A (en) * 1952-05-14 1955-06-28 Aktiebolag Separator Centrifuge for separating sludge from liquids
US2743865A (en) * 1952-05-24 1956-05-01 Johan E A Graae Centrifugal separator
US2862658A (en) * 1952-05-28 1958-12-02 Separator Ab Method and apparatus for centrifugal separation of a mixture of solids and two liquids
US2733856A (en) * 1952-12-04 1956-02-07 Sludge centrifuge
US2795635A (en) * 1953-08-28 1957-06-11 Phillips Petroleum Co Centrifuge
US3096282A (en) * 1957-12-30 1963-07-02 Sharples Corp Improvement in centrifuges

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3321131A (en) * 1964-10-21 1967-05-23 Bird Machine Co Centrifuge
US3431115A (en) * 1966-01-21 1969-03-04 Pennsalt Chemicals Corp Process for making bakers' cheese
US3494542A (en) * 1968-05-27 1970-02-10 Pennwalt Corp Centrifuging process and apparatus
DE2344507A1 (de) * 1972-09-06 1974-03-14 Pennwalt Corp Dekantierzentrifuge
US4575370A (en) * 1984-11-15 1986-03-11 Pennwalt Corporation Centrifuge employing variable height discharge weir
EP0182150A2 (de) * 1984-11-15 1986-05-28 Pennwalt Corporation Zentrifuge mit Überlaufwehr variabler Höhe
EP0182150A3 (de) * 1984-11-15 1987-12-23 Pennwalt Corporation Zentrifuge mit Überlaufwehr variabler Höhe
US4957475A (en) * 1988-05-11 1990-09-18 Flottweg Gmbh Solid-bowl helical centrifuge
US5257968A (en) * 1991-06-06 1993-11-02 Alfa Laval Separation Inc. Inflatable dam for a decanter centrifuge
US5261869A (en) * 1992-04-06 1993-11-16 Alfa Laval Separation, Inc. Decanter centrifuge having discontinuous flights in the beach area
US5342279A (en) * 1992-08-18 1994-08-30 Alfa Laval Separation Inc. Decanter centrifuge having dual motor drive
US5509882A (en) * 1994-09-12 1996-04-23 Tetra Laval Holdings & Finance S.A. Decanter centrifuge having an offset conveyor flight to aid rinsing
EP1304170A1 (de) * 2000-02-10 2003-04-23 KOTOBUKI ENGINEERING & MANUFACTURING CO LTD Zentrifugalabscheider
EP1304170A4 (de) * 2000-02-10 2004-08-25 Kotobuki Giken Kogyo Kk Zentrifugalabscheider
US20080257836A1 (en) * 2007-04-17 2008-10-23 Laughlin Henry J Centrifugal separator and method for separating heavy and light matter in a substance
US7527587B2 (en) * 2007-04-17 2009-05-05 Laughlin Henry J Centrifugal separator and method for separating heavy and light matter in a substance
WO2024132340A1 (de) * 2022-12-21 2024-06-27 Gea Westfalia Separator Group Gmbh Verfahren zur gewinnung von hochdichtem quark

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DE1432873C3 (de) 1974-01-03
DE1432873A1 (de) 1969-03-20

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