US3612276A - Vortex-type separator apparatus - Google Patents

Vortex-type separator apparatus Download PDF

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Publication number
US3612276A
US3612276A US820261A US3612276DA US3612276A US 3612276 A US3612276 A US 3612276A US 820261 A US820261 A US 820261A US 3612276D A US3612276D A US 3612276DA US 3612276 A US3612276 A US 3612276A
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United States
Prior art keywords
inlet
section
slurry
sump
range
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Expired - Lifetime
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US820261A
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English (en)
Inventor
Thomas William Lowe
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Bird Machine Co Inc
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Bird Machine Co Inc
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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
    • B04C5/14—Construction of the underflow ducting; Apex constructions; Discharge arrangements ; discharge through sidewall provided with a few slits or perforations
    • B04C5/15—Construction of the underflow ducting; Apex constructions; Discharge arrangements ; discharge through sidewall provided with a few slits or perforations with swinging flaps or revolving sluices; Sluices; Check-valves
    • 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

Definitions

  • a vortex separator is provided which is substantially more efficient than prior separators in cleaning fiber slurry at concentrations of 3 percent and above of impurities which will pass a 14-inch hole screen, the separator and its connections to a sump having specified design parameters and features some of which are critical for obtaining such efficiency and others of which are preferred for maximizing it.
  • VORTEX-TYPE SEPARATOR APPARATUS This invention relates to hydrocyclone or vortex-type separators for cleaning fiber slurry of impurities up to a size which will pass a it-inch hole screen, particularly at slurry concentrations of 3 percent and above.
  • lmpurities of the size range involved are commonly present in large quantities for example in waste paper slurry after it has been coarse-cleaned either in the pulper or by coarse screens or other coarse cleaners following the pulper to remove large objects such as tramp iron which will not pass a %-inch hole screen.
  • the remaining impurities include as well as dirt a large amount of metal most usually in the form of staples and bits of paper which are held together by staples and are called in the trade puffed wheat.
  • the object of this invention is to provide a separator of the vortex type which is capable of cleaning high-density slurries of impurities of the specified size range much more effectively than prior cleaners without the use of additional vortex accelerating equipment.
  • separators having a maximum diameter (herein referred to as D") in the range 4% inches to 10 inches provided the slurry feed rate is such as to maintain a pressure drop of at least of the order of 13 p.s.i. for slurry consistency of about 3 percent and higher for greater consistencies (attainable at usual available pressures of 20 to 30 p.s.i. or higher) and provided all the following critical design factors of the separator are observed:
  • the separator has a substantially nonconvergent (usually cylindrical) inlet end which joins a convergent section of frustoconical shape terminating in an apex outlet for separated impurities and has at the opposite inlet end a vortex finder through which accepted stock of the reversed inner vortex is discharged.
  • the apex outlet of the convergent section is connected to s sump, and a connection is provided for supplying elutriation water to the separated impurity fraction adjacent the outlet and before it reaches the sump.
  • the slurry inlet is tangential, feeding below a scroll which guides the first turn of the helically moving slurry below the inlet and has an area equivalent diameter (area equivalent to that of a circle having a diameter) in the range 1 inch to 0.5 D.
  • the included angle of the convergent conical section is in the range 6' to 12 and the total axial length of the nonconvergent and convergent sections from the portion of the slurry inlet furthest from the larger end of the convergent section is in the range D to 7.5 D.
  • the vortex finder inlet is located axially beyond the bottom of the inlet to the separator by a distance in the range 0.5 D to 1.25 D, it is spaced from the convergent section by a distance of at least 0.25 D and it has an inlet area equivalent diameter in the range 1.5 inches to 0.75 D.
  • the apex outlet is connected to the pump by a tube having an area equivalent diameter at least substantially equal to that of the outlet, having a length of l to 3 D and being equipped with a tangential elutriation water feed.
  • D is about 5-7 inches; the axial length of the nonconvergent section from the top of the slurry inlet is about 3 D; the axial length of the convergent action is about 3 D to 3.5 D; the cone angle is about 8; the slurry inley has an area equivalent diameter of about 0.3 D to 0.45 D; and the vortex finder has a substantially circular inlet of a diameter about 0.5 D.
  • FIGURE of the accompanying drawing shows a vortex separator according to the invention in a view partly in vertical section and partly in side elevation.
  • the separator has a tubular body portion designated generally 10 formed of a cylindrical inlet end section 12 and a convergent frustoconical section 14 terminating in a circular apex outlet 16.
  • An inlet i8 is provided at the outer end of the cylindrical section for connection to a source (not shown) of the aforedescribed slurry under the requisite pressure and has a rectangular inlet opening arranged to feed the stock tangentially into the separator under a scroll 20, which extends helically about the wall of section 112 sufficiently to insure that the first spiral turn of the incoming flow about the wall is guided below the inlet.
  • a vortex finder 22 extends through the end of section 12 for connection at its outer end to piping (not shown) for removal of the accepted fraction and has a circular open inner end projecting below the inlet within section 12 as previously specified.
  • Outlet 16 is connected by a divergent frustoconical tube 24 and a gate valve 26 to the inlet 28 of a sump 30 shown as having a transparent wall 32 through which the contents may be observed.
  • a gate valve 35 is provided at the bottom of sump 30.
  • the operating levers 36, 38 of valves 26 and 34 respectively are connected by respective links 40, 42 to the pistons of fluid motors 44, 46 respectively which are supported by arms 48 and 50 respectively attached to the side of the valves.
  • the operating connections to motors 44, 46 which are not shown may be arranged for hand operation or for automatic operation in a timed sequence.
  • a tangential inlet 52 is provided in tube 24 for connection to a source of water under pressure (not shown) for elutriation, preferably arranged as shown to direct the water opposite to the direction of spiral flow of the slurry along the wall section 14.
  • An inlet 54 for connection to such source is also provided in sump inlet 28 to provide water for filling the sump after it is emptied and also preferably for dilution.
  • the slurry entering inlet 18 spirals about the wall of body 10, the impurities separating toward the wall under the shear and centrifugal forces developed.
  • the inner fraction separates to form an inner vortex containing accepted stock within and flowing in reverse direction to the outer vortex containing the impurities.
  • the inner vortex is removed through vortex finger 22 as the accepted fraction while the outer vortex continues its vortical flow from outlet 16 through tube 24 where it receives elutriation water through inlet 52 preferably supplied at around 9 g.p.m.
  • elutriation The function of elutriation at this point is to dilute the concentrated reject flow from outlet 16 in order to separate the solids thereof and to permit acceptable fibers or fibrous matter retained therein to escape with the elutriation water in reverse flow into the inner vortex without carrying impurities with it.
  • This function is accomplished better by injecting the elutriation water into the reject stream counter to its direction of flow which also tends to slow down the flow, enabling better settling out of the rejected impurities in sump 30.
  • Such settling is also facilitated by the addition of elutriation water at lower flows such as 3 g.p.m. throughinlet 54 in sump inlet 28, into which the rejected fraction flows through opened gate valve 26.
  • valve 26 When the. rejected solids have accumulated sufficiently in sump 30 above closed gate valve 34, valve 26 is closed and valve 34 is opened, thereby emptying the sump. Valve 34 is then closed and sump 30 is preferably filled or nearly filled with water via inlet 54 before valve 26 is opened to repeat the cycle.
  • the elutriation water through connection 52 aids in breaking up any mass of solids that may have accumulated above valve 26 while closed, thereby avoiding plugging. Avoidance of plugging and the elutriation function are also aided by making tube 24 divergent as shown, which is preferred.
  • the separator may be mounted in any convenient manner. As shown it is provided with mounting lugs 56 on the outer wall of section 12 for suspending the device from supporting structure with its axis generally vertical.
  • the diameter D of section 12 is from 4.5 to inches, preferably 5-7 inches.
  • the combined axial lengths of sections 12 and 14 from the top of inlet 18 is 5 D to 7.5 D, preferably about 6 D, such length of section 12 being preferably about 3 D and of section 14 being preferably about 3 to 3.5 D;
  • the included cone angle of section 14 is from 6 to 12, preferably about 8.
  • Tangential inlet 18 has an area equivalent diameter of 1 inch to 0.5 D; preferably 0.3 D to 0.45 D;
  • Vortex finder 22 has its inlet spaced below the bottom of inlet 18 by a distance in the range 0.5 D to 1.25 D, has its inlet spaced from section 14 by a distance of at least 0.25 D and has an inlet with an area equivalent diameter in the range 1.5 inches to 0.75 D, being preferably circular with a diameter about 0.5 D;
  • Outlet 16 has an area equivalent diameter in the range 1.5 inches to 0.6 D, being preferably circular as shown;
  • Tube 24 preferably has an axial length of 1 to 3 D and is divergent as shown.
  • valve 26 may be dispensed with by substituting for valve 34 a reject removal system such as a helical conveyor extrusion system capable of removing the solids collected in sump 30 without dumping its liquid content continuously or intermittently.
  • a reject removal system such as a helical conveyor extrusion system capable of removing the solids collected in sump 30 without dumping its liquid content continuously or intermittently.
  • Vortex-type separator apparatus capable of efficiently separating from high-density fibrous slurry impurities in a size range up to a size which will pass a -inch-hole screen at a maintained pressure drop at least of the order of 13 p.s.i., said apparatus comprising:
  • tubular body formed of a substantially nonconvergent section joined to a convergent substantially frustoconical section having an included angle in the range 6 to 12, said body having a maximum diameter D in the range 4% to 10 inches;
  • an inlet for directing said slurry into said nonconvergent section adjacent the outer end thereof and tangentially along the wall thereof, said sectionbeing provided with a helical scroll for guiding said slurry below said inlet, said inlet having an area equivalent diameter in the range 1 inch to 0.5 D;
  • the combined axial lengths of said nonconvergent and convergent sections from the portion of the slurry inlet furthest from the larger end of said convergent section being in the range 5 D to 7.5 D;
  • a vortex finder for removing accepted slurry extending axially into said nonconvergent section, said vortex finder having an inlet spaced axially of said section from the bottom of said slurry inlet by a distance in the range 0.5 D to 1.25 D and from the larger end of said convergent section by a distance of at least 0.25 D and having an inlet area diameter equivalent in the range 1.5' inches to 0.75 D;
  • said convergent section having an outlet for a rejected slurry fraction containing such impurities at the smaller end thereof, said outlet having an area equivalent diameter in the range of which the maximum is 0.6 D and the minimum is 1.5 inches for cone angles of 8 and above and for cone angles less than 8 is the larger of (a) an area equivalent diameter of 1.5 inches or (b) the area equivalent diameter of the outlet of a convergent section having the included angle of less than 8 and a length of (6.75 D)-l inches;
  • connection means includes a tube connecting said outlet to the inlet to said sump, said tube having an area equivalent 5.
  • D is about 5 to 7 inches
  • the axial length of said nonconvergent section from the portion of the slurry inlet furthest from the larger end of said convergent section is about 3 D
  • the axial length of said convergent section is about 3 D to 3.5 D and said included angle thereof is about 8
  • said slurry inlet has an area equivalent diameter of about 0.3 D to 0.45 D
  • said vortex finder has a substantially circular inlet of a diameter about Patent No.

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  • Physics & Mathematics (AREA)
  • Geometry (AREA)
  • Cyclones (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
  • Paper (AREA)
US820261A 1969-04-29 1969-04-29 Vortex-type separator apparatus Expired - Lifetime US3612276A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US82026169A 1969-04-29 1969-04-29

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US3612276A true US3612276A (en) 1971-10-12

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Country Status (6)

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US (1) US3612276A (en:Method)
CA (1) CA927782A (en:Method)
FI (1) FI54863C (en:Method)
GB (1) GB1241537A (en:Method)
NO (1) NO136582C (en:Method)
SE (1) SE365951B (en:Method)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3964996A (en) * 1974-03-20 1976-06-22 Hermann Finckh Metalltuch- Und Maschinenfabrik Classifying unit for fibrous suspensions
US4151083A (en) * 1974-09-10 1979-04-24 Dove Norman F Apparatus and method for separating heavy impurities from feed stock
US4217207A (en) * 1977-12-14 1980-08-12 Liller Delbert I Continuous method of cleaning a slurry of crushed raw coal
US4219409A (en) * 1977-12-14 1980-08-26 Liller Delbert I Inlet line deflector and equalizer means for a classifying cyclone used for washing and method of washing using deflectors and equalizers
US4253945A (en) * 1979-08-10 1981-03-03 Domtar Inc. High consistency pulp cleaning
EP1886722A3 (de) * 2006-08-09 2008-09-24 Voith Patent GmbH Rückstands-Schleuse für Filtereinrichtungen, insbesondere Streichfarbenfilter
US20110192771A1 (en) * 2010-02-09 2011-08-11 World Chemical Co., Ltd. Solid-liquid separator with self-priming pump
WO2017076384A1 (de) * 2015-11-06 2017-05-11 Hans-Joachim Boltersdorf Zyklonsystem
CN106823485A (zh) * 2015-12-07 2017-06-13 山东联星能源集团有限公司 一种新型旋流除砂器
WO2018039741A1 (en) 2016-09-02 2018-03-08 Vulco S.A. A hydrocyclone

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2465060C1 (ru) * 2011-09-26 2012-10-27 Закрытое Акционерное Общество Научно-Производственное Объединение "Тэн" Гидроциклон системы фракционного разделения суспензий руд тонкого помола
RU2465061C1 (ru) * 2011-09-26 2012-10-27 Закрытое Акционерное Общество Научно-Производственное Объединение "Тэн" Гидроциклон системы фракционного разделения суспензий руд тонкого помола

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1686435A (en) * 1924-08-05 1928-10-02 Thomas M Chance Method and apparatus for detecting accumulations of materials in coal washers and ore concentrators
GB516806A (en) * 1937-07-11 1940-01-11 Andre Berges Centrifugal apparatus for the uninterrupted purifying of paper pulp
US2377524A (en) * 1939-11-21 1945-06-05 Hammermill Paper Co Method of and means for separating solid particles in pulp suspensions and the like
US2897972A (en) * 1956-03-28 1959-08-04 Bird Machine Co Separator
US3337050A (en) * 1963-08-12 1967-08-22 Neyrpic Ets Cleaner for cyclone apex discharge
US3501001A (en) * 1967-09-22 1970-03-17 Papcel Celulosy Np Centrifugal separator

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1686435A (en) * 1924-08-05 1928-10-02 Thomas M Chance Method and apparatus for detecting accumulations of materials in coal washers and ore concentrators
GB516806A (en) * 1937-07-11 1940-01-11 Andre Berges Centrifugal apparatus for the uninterrupted purifying of paper pulp
US2377524A (en) * 1939-11-21 1945-06-05 Hammermill Paper Co Method of and means for separating solid particles in pulp suspensions and the like
US2897972A (en) * 1956-03-28 1959-08-04 Bird Machine Co Separator
US3337050A (en) * 1963-08-12 1967-08-22 Neyrpic Ets Cleaner for cyclone apex discharge
US3501001A (en) * 1967-09-22 1970-03-17 Papcel Celulosy Np Centrifugal separator

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3964996A (en) * 1974-03-20 1976-06-22 Hermann Finckh Metalltuch- Und Maschinenfabrik Classifying unit for fibrous suspensions
US4151083A (en) * 1974-09-10 1979-04-24 Dove Norman F Apparatus and method for separating heavy impurities from feed stock
US4217207A (en) * 1977-12-14 1980-08-12 Liller Delbert I Continuous method of cleaning a slurry of crushed raw coal
US4219409A (en) * 1977-12-14 1980-08-26 Liller Delbert I Inlet line deflector and equalizer means for a classifying cyclone used for washing and method of washing using deflectors and equalizers
US4253945A (en) * 1979-08-10 1981-03-03 Domtar Inc. High consistency pulp cleaning
EP1886722A3 (de) * 2006-08-09 2008-09-24 Voith Patent GmbH Rückstands-Schleuse für Filtereinrichtungen, insbesondere Streichfarbenfilter
US20110192771A1 (en) * 2010-02-09 2011-08-11 World Chemical Co., Ltd. Solid-liquid separator with self-priming pump
US8512565B2 (en) * 2010-02-09 2013-08-20 World Chemical Co., Ltd Solid-liquid separator with self-priming pump
WO2017076384A1 (de) * 2015-11-06 2017-05-11 Hans-Joachim Boltersdorf Zyklonsystem
US20190060918A1 (en) * 2015-11-06 2019-02-28 Hans-Joachim Boltersdorf Cyclone system
CN106823485A (zh) * 2015-12-07 2017-06-13 山东联星能源集团有限公司 一种新型旋流除砂器
WO2018039741A1 (en) 2016-09-02 2018-03-08 Vulco S.A. A hydrocyclone
CN109803767A (zh) * 2016-09-02 2019-05-24 乌尔可公司 水力旋流器
EP3507018A4 (en) * 2016-09-02 2020-04-29 Vulco S.A. HYDROCYCLONE

Also Published As

Publication number Publication date
CA927782A (en) 1973-06-05
GB1241537A (en) 1971-08-04
NO136582C (no) 1977-09-28
NO136582B (en:Method) 1977-06-20
FI54863C (fi) 1979-04-10
FI54863B (fi) 1978-12-29
SE365951B (en:Method) 1974-04-08

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