US2858020A - Method and apparatus for separating slurry and like suspensions - Google Patents

Method and apparatus for separating slurry and like suspensions Download PDF

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Publication number
US2858020A
US2858020A US535192A US53519255A US2858020A US 2858020 A US2858020 A US 2858020A US 535192 A US535192 A US 535192A US 53519255 A US53519255 A US 53519255A US 2858020 A US2858020 A US 2858020A
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US
United States
Prior art keywords
slurry
casing
chamber
outlet
separating
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Expired - Lifetime
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US535192A
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English (en)
Inventor
Bek Steen Jacob
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FLSmidth and Co AS
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FLSmidth and Co AS
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B28—WORKING CEMENT, CLAY, OR STONE
    • B28C—PREPARING CLAY; PRODUCING MIXTURES CONTAINING CLAY OR CEMENTITIOUS MATERIAL, e.g. PLASTER
    • B28C1/00—Apparatus or methods for obtaining or processing clay
    • B28C1/02—Apparatus or methods for obtaining or processing clay for producing or processing clay suspensions, e.g. slip
    • B28C1/06—Processing suspensions, i.e. after mixing
    • B28C1/08—Separating suspensions, e.g. for obtaining clay, for removing stones; Cleaning clay slurries
    • 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
    • B04C5/02—Construction of inlets by which the vortex flow is generated, e.g. tangential admission, the fluid flow being forced to follow a downward path by spirally wound bulkheads, or with slightly downwardly-directed tangential admission
    • B04C5/04—Tangential inlets
    • 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
    • B04C5/28—Multiple arrangement thereof for parallel flow
    • 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
    • B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
    • 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
    • B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
    • B04C2009/005—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks with external rotors, e.g. impeller, ventilator, fan, blower, pump

Definitions

  • Thisinvention relates to the separation of slurry and like suspensions into fractions containing fine and coarse particles and is concerned more particularly with a novel apparatus, by which such separating operations can be performed at a rapid rate and with a lower power cost than heretofore.
  • the invention also includes a method, by the use of which a sharp separation may be obtained without heavy wear on the equipment and high power consumption.
  • separating chambers of circular cross-section having a tangential inlet opening and outlets for the two fractions at opposite ends.
  • One such separating chamber is a hydrocyclone, which has a casing of inverted frustoconical shape with the inlet near its upper end.
  • a centrifugal pump is connected to the inlet opening of the casing and the velocity of the slurry flowing to the pump is converted in the pump into pressure and the pressure is converted back into velocity in the inlet opening.
  • This double conversion of one form of energy into another involves considerable frictional loss and is an objectionable feature of a hydrocyclone.
  • the double conversion mentioned is avoided in another form of hydrocyclone called a centriclone, in which a rotary impeller in the form of a vane wheel is mounted in the casing and imparts the desired velocity to the slurry immediately after it has entered the casing.
  • a centriclone in which a rotary impeller in the form of a vane wheel is mounted in the casing and imparts the desired velocity to the slurry immediately after it has entered the casing.
  • the apparatus of the invention is superior to those heretofore used in that it provides the desired relatively high output rate with a lower power cost.
  • the apparatus includes a plurality of separating chambers arranged in a circular series and a single means for introducing the suspension to be separated into the chambers through tangential inlets.
  • the chambers are mounted with their axes parallel and the chambers may be of the hydrocyclone type with frustconical lower ends, or they may be substantially cylindrical.
  • the suspension is introduced into the chambers by an impeller of vane wheel form, which rotates in a plane through the cham- 2 ber inlets and to which the suspension is fed at its axis. in its rotation, the impeller introduces the suspension into the chambers at high velocity and the coarse particle fraction leaves each chamber at the lower end, while the fine particle fraction issues at the top.
  • the sharpness of separation between two. fractions of slurry leaving a separating chamber varies directly with the time taken by the slurry in passing through the chamber.
  • a chamber of the small dimensions necessary to obtain the desired centrifugal action a long period of travel of the slurry through the chamber requires that the chamber have a small inlet and that the slurry have a high feed velocity.
  • the resistance to flow of slurry is high both in the inlet and within the chamber, particularly with thick slurry and, as a result, the apparatus is subjected to heavy wear and the power consumption is high.
  • the practice of the method of the invention makes possible a sharp separation of slurry and like suspensions without the objectionable features mentioned and the method involves proportioning the rate, at which the slurry is fed into a separating chamber, the velocity of flow, and the size of the inlet opening of the chamber, so that the slurry is continually fed into the chamber at a rate greater than the chamber can handle and the excess amount is continually withdrawn from the cham ber shortly after it enters the chamber.
  • the excess slurry so withdrawn is combined with the slurry being fed into the chamber.
  • a high inlet velocity is obtained without the necessity of employing an inlet passage of reduced size, so that wear and power consumption are reduced.
  • the remaining slurry undergoing separation has a high velocity, so that its travel through the separating chamber is such as to afford the desired sharpness of separation.
  • FIG. 1 is a view in elevation with parts broken away of one form of the new apparatus suitable for the practice of the new method
  • Fig. 2 is a sectional view on the line 22 of Fig. 3;
  • Fig. 3 is a sectional view on the line 3-3 of Fig. 1;
  • Fig. 4 is a view similar to Fig. 2 showing a modified construction.
  • the separating apparatus shown in Figs. 1-3, incl. comprises a casing 10 having a central opening through its top encircled by a hub 11 enclosing a shaft 12 mounted for rotation in suitable bearings and carrying at its lower end within the casing an impeller in the form of a vane wheel made up of a hub 13 and a plurality of radial blades 14.
  • the shaft may be driven in any suitable way as, for example, by belts 15 encircling pulleys 16 at the upper end of the shaft.
  • the bottom wall 17 of the casing has a central opening, through which slurry is introduced at the axis of the impeller through a pipe 18 connected to the bottom of the casing around the opening.
  • the casing has a hollow peripheral section 19 subdivided to form a plurality of cavities 20 equiangularly spaced about the casing.
  • Each cavity or chamber has a cylindrical upper section and an opening 21 lying in the plane of rotation of the impeller serves to connect the upper section of each chamber to the interior of the casing and acts as a peripheral outlet opening from the casing and a tangential inlet into the upper section of the chamber.
  • An outlet plate 22 is mounted in the upper section of each chamber above the opening and is provided with an axial outlet tube 23, which extends downwardly into the chamber and terminates below the level of the inlet 21.
  • each chamber has an outlet opening through its upper end lying offset from the axial outlet tube of the plate in the chamber and a 3 fine .particle .fraction outlet passage 24 leads upwardly at an angle to the vertical from .the top outlet opening from the upper section of each chamber to a circular duct 25, 'which overli'es' all :of ithe passages .24 and ihaS alCOm mon discharge outlet r
  • the 'rupper section of each chan-iber :or cavity .20 acts as a separating chamber'which, in the construction shown in Figs. 1-3, incl., includes a frusto conicalldischarge section 27 connected to the bottom of the casing 110 in line with the upper section of the cavity.
  • Each of the sections has abottom outlet Z8 discharging into a circular duct 29*ha v ing anout1et'30.
  • a discharge passage 31 for-med "the 'bottom 17 f casing leads upwardly from a tangential outlet opening in the upper section of each cavity 20 below the inlet 21 into that cavity.
  • Each passage opens at its other end into the casing to discharge slurry into the path of the impeller at a place where the velocity of the slurry in the casing is substantially the same as the velocity of the slurry travelling through the passage.
  • the slurry issuppl ied to the casing at such a rate that more slurry is fed into each chamber than thec'ham-ber is capable of handling.
  • the slurry accordingly, enters each chamber at high velocity and, shortly after the entrance of the slurry, the excess quantity thereof is removed through the tangential outlet and the discharge passage 31 and returned to the casing.
  • the remaining slurry then travels at high velocity and along a helical path of low pitch through the sections 27 of the chamber.
  • the coarse particle fraction' is discharged through out-lets 28 into the common duct 29, While :the hue particle fraction escapes through the outlet tubes 23 and outlet passages 24 into the common duct. '25.
  • the rotational movement will continue in the time fractions as they travel through the outlet passages 23 into the upper sections of the chambers above the plates 22.
  • the rotational movement of the fine fractions continues and the hue fractions travel upwardly through pipes 24 into the duct 25 against the pressure of the ffluid in the duct.
  • the fractions enter the space above the plates 22 they move outwardly to the peripheries of the spaces, while still maintaining their rotational movement.
  • the fluid can enter the passages 24 more easily than would be-the case if the passages 24 Were verticallyaligned with the-axial passages 23.
  • the rotational energy of the fluid is transformed into pressure energy, which'helps to overcome the back pressure of the fluid in the duct 25.
  • there -is'litt1e energy lost in friction and most of the energy of the rotational movement is transformed into pressure energy serving the purpose indicated above.
  • g t canstmctio i us a d, a hs pa a ch mb has a section 27 of inverted frusto-conical form, but it is .not necessary that the section :be of such form.
  • Fig. 1 In the modified construction illustrated in Fig.
  • the separator chamber section 32 is cylindrical and it is attached to the bottom 17 of the casing 10' in alignment with a cavity 20' having a tangential inlet T21 and a top 22 having an outlet .passage 23, .In .order to reduce the pressure, at which the coarse .particle'fraction leaves section 32, the lower end of the section is provided with an annular trough 33and an outlet pipe 34 for the coarse particle fraction leads from an opening through the outer wall of the trough in a direction opposite to the direction of flow within the section and discharges the fraction into a duct 29.
  • each separating chamber was in the plane of the impeller wheel and was mm.
  • the diameter of the impeller wheel was 40.0 and .the wheel was opermad a 0 R- Suc an pparatus ha ng 91 99?- rating chambers had a capacity of about .100 cubic meters of slurry per hour.
  • a method of separating slurry and like suspensions into fractions containing fine and coarse particles in a separating chamber of circular cross-section having va tangential inlet and outlets at its ends for the fractions which comprises feeding the suspension into the chamber through the inlet at a rate greater than can be separated in the ,chamber and continuously withdrawing the excess suspension from the chamber adjacent the inlet and combining the suspension withdrawn with that being .fed.
  • An apparatus for separating slurry and like'suspensions into fractions containing coarse and fine particles which comprises a casing of circular section having a plurality of outlet openings through its peripheral wall in spaced relation, an impeller mounted within the casing for rotation on the casing axis, a plurality of separating chambers disposed about the casing with their axes parallel to the casing axis, the chambers being cylindrical and having tangential inlets, axial fine fraction outlets at their upper ends, and tangential coarse fraction outlets at their lower ends, means for rotating the impeller, and means for feeding the suspension to be separated to the impeller at its axis of rotation.

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  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Cyclones (AREA)
  • Centrifugal Separators (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
US535192A 1954-09-20 1955-09-19 Method and apparatus for separating slurry and like suspensions Expired - Lifetime US2858020A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
GB27195/54A GB772303A (en) 1954-09-20 1954-09-20 Improvements in the separation of slurries into fractions of differing particle content

Publications (1)

Publication Number Publication Date
US2858020A true US2858020A (en) 1958-10-28

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US535192A Expired - Lifetime US2858020A (en) 1954-09-20 1955-09-19 Method and apparatus for separating slurry and like suspensions

Country Status (4)

Country Link
US (1) US2858020A (fr)
BE (1) BE541456A (fr)
FR (1) FR1131345A (fr)
GB (1) GB772303A (fr)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3682302A (en) * 1969-03-01 1972-08-08 Paul Bernutat Air separator
DE2926751A1 (de) * 1978-07-06 1980-01-31 Oishikikai Mfg Co Einrichtung zum ausscheiden von fremdstoffen aus papierstoffsuspensionen
US20070107465A1 (en) * 2001-05-04 2007-05-17 Battelle Energy Alliance, Llc Apparatus for the liquefaction of gas and methods relating to same
US20100186446A1 (en) * 2001-05-04 2010-07-29 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
US20100291756A1 (en) * 2008-01-30 2010-11-18 Siltronic Ag Method for the production of a semiconductor structure
US20110094263A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams
US20110094261A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Natural gas liquefaction core modules, plants including same and related methods
US8544295B2 (en) 2007-09-13 2013-10-01 Battelle Energy Alliance, Llc Methods of conveying fluids and methods of sublimating solid particles
US8555672B2 (en) 2009-10-22 2013-10-15 Battelle Energy Alliance, Llc Complete liquefaction methods and apparatus
US9217603B2 (en) 2007-09-13 2015-12-22 Battelle Energy Alliance, Llc Heat exchanger and related methods
US9254448B2 (en) 2007-09-13 2016-02-09 Battelle Energy Alliance, Llc Sublimation systems and associated methods
US9574713B2 (en) 2007-09-13 2017-02-21 Battelle Energy Alliance, Llc Vaporization chambers and associated methods
US10655911B2 (en) 2012-06-20 2020-05-19 Battelle Energy Alliance, Llc Natural gas liquefaction employing independent refrigerant path

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US762866A (en) * 1901-08-12 1904-06-21 Henry A Allen Ore-separator.
US2671560A (en) * 1950-06-14 1954-03-09 Stamicarbon Multiple hydrocyclones
US2734630A (en) * 1952-01-25 1956-02-14 van der wal

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US762866A (en) * 1901-08-12 1904-06-21 Henry A Allen Ore-separator.
US2671560A (en) * 1950-06-14 1954-03-09 Stamicarbon Multiple hydrocyclones
US2734630A (en) * 1952-01-25 1956-02-14 van der wal

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3682302A (en) * 1969-03-01 1972-08-08 Paul Bernutat Air separator
DE2926751A1 (de) * 1978-07-06 1980-01-31 Oishikikai Mfg Co Einrichtung zum ausscheiden von fremdstoffen aus papierstoffsuspensionen
US20070107465A1 (en) * 2001-05-04 2007-05-17 Battelle Energy Alliance, Llc Apparatus for the liquefaction of gas and methods relating to same
US20100186446A1 (en) * 2001-05-04 2010-07-29 Battelle Energy Alliance, Llc Apparatus for the liquefaction of a gas and methods relating to same
US9217603B2 (en) 2007-09-13 2015-12-22 Battelle Energy Alliance, Llc Heat exchanger and related methods
US9574713B2 (en) 2007-09-13 2017-02-21 Battelle Energy Alliance, Llc Vaporization chambers and associated methods
US8544295B2 (en) 2007-09-13 2013-10-01 Battelle Energy Alliance, Llc Methods of conveying fluids and methods of sublimating solid particles
US9254448B2 (en) 2007-09-13 2016-02-09 Battelle Energy Alliance, Llc Sublimation systems and associated methods
US20100291756A1 (en) * 2008-01-30 2010-11-18 Siltronic Ag Method for the production of a semiconductor structure
US20110094261A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Natural gas liquefaction core modules, plants including same and related methods
US8899074B2 (en) 2009-10-22 2014-12-02 Battelle Energy Alliance, Llc Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams
US8555672B2 (en) 2009-10-22 2013-10-15 Battelle Energy Alliance, Llc Complete liquefaction methods and apparatus
US20110094263A1 (en) * 2009-10-22 2011-04-28 Battelle Energy Alliance, Llc Methods of natural gas liquefaction and natural gas liquefaction plants utilizing multiple and varying gas streams
US10655911B2 (en) 2012-06-20 2020-05-19 Battelle Energy Alliance, Llc Natural gas liquefaction employing independent refrigerant path

Also Published As

Publication number Publication date
BE541456A (fr) 1959-08-14
GB772303A (en) 1957-04-10
FR1131345A (fr) 1957-02-20

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