JP4047386B2 - Method and apparatus for separating heavy fraction of aqueous slurry from light fraction by centrifugal force action - Google Patents

Method and apparatus for separating heavy fraction of aqueous slurry from light fraction by centrifugal force action Download PDF

Info

Publication number
JP4047386B2
JP4047386B2 JP53851197A JP53851197A JP4047386B2 JP 4047386 B2 JP4047386 B2 JP 4047386B2 JP 53851197 A JP53851197 A JP 53851197A JP 53851197 A JP53851197 A JP 53851197A JP 4047386 B2 JP4047386 B2 JP 4047386B2
Authority
JP
Japan
Prior art keywords
separation chamber
slurry
means
rotor means
separation
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
JP53851197A
Other languages
Japanese (ja)
Other versions
JP2000508968A (en
Inventor
アイヒラー,ディートリッヒ
Original Assignee
ファン セパラトール ゲゼルシャフト ミット ベシュレンクテル ハフツング
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to DE19616602.0 priority Critical
Priority to DE1996116602 priority patent/DE19616602A1/en
Priority to DE1996125456 priority patent/DE19625456A1/en
Priority to DE19625456.6 priority
Priority to DE19646494.3 priority
Priority to DE1996146494 priority patent/DE19646494A1/en
Priority to PCT/EP1997/001913 priority patent/WO1997040944A1/en
Application filed by ファン セパラトール ゲゼルシャフト ミット ベシュレンクテル ハフツング filed Critical ファン セパラトール ゲゼルシャフト ミット ベシュレンクテル ハフツング
Publication of JP2000508968A publication Critical patent/JP2000508968A/en
Application granted granted Critical
Publication of JP4047386B2 publication Critical patent/JP4047386B2/en
Anticipated expiration legal-status Critical
Application status is Expired - Lifetime legal-status Critical

Links

Images

Classifications

    • BPERFORMING OPERATIONS; TRANSPORTING
    • B03SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03BSEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
    • B03B5/00Washing granular, powdered or lumpy materials; Wet separating
    • B03B5/28Washing granular, powdered or lumpy materials; Wet separating by sink-float separation
    • B03B5/30Washing granular, powdered or lumpy materials; Wet separating by sink-float separation using heavy liquids or suspensions
    • B03B5/32Washing granular, powdered or lumpy materials; Wet separating by sink-float separation using heavy liquids or suspensions using centrifugal force
    • B03B5/34Applications of hydrocyclones
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B03SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03DFLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00Flotation
    • B03D1/14Flotation machines
    • B03D1/1418Flotation machines using centrifugal forces
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B03SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03DFLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00Flotation
    • B03D1/14Flotation machines
    • B03D1/1431Dissolved air flotation machines
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B03SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03DFLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00Flotation
    • B03D1/14Flotation machines
    • B03D1/1443Feed or discharge mechanisms for flotation tanks
    • B03D1/1456Feed mechanisms for the slurry
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B03SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03DFLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00Flotation
    • B03D1/14Flotation machines
    • B03D1/1443Feed or discharge mechanisms for flotation tanks
    • B03D1/1462Discharge mechanisms for the froth
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B03SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03DFLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00Flotation
    • B03D1/14Flotation machines
    • B03D1/24Pneumatic
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B04CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04CAPPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00Apparatus in which the axial direction of the vortex (flow following a screw-thread type line) remains unchanged Also devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/06Construction of inlets or outlets to the vortex chamber
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B04CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04CAPPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C5/00Apparatus in which the axial direction of the vortex is reversed
    • B04C5/02Construction 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
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B04CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04CAPPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C9/00Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B04CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04CAPPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C9/00Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
    • B04C2009/007Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks with internal rotors, e.g. impeller, ventilator, fan, blower, pump

Abstract

The invention relates to a process and apparatus for the separation of heavier from lighter fractions in aqueous slurries by means of centrifugal force. The slurry is made to spin in the separation chamber under the influence of the differential pressure generated between the inlet and outlet of a cyclone separation chamber (4). The differential pressure, which can amount to several bar, is generated by means of a pressure increasing stage in the form of a transport rotor device (20) which acts in conjunction with a stator arrangement (22); essentially this takes place immediately in front of the inlet of the slurry into the separation chamber (4). The rotor blades of the cyclone rotor device (10) as the rotor blades of the transport rotor device (20) can be mounted on the same rotary shaft (5) in order to induce additional rotary force into the slurry. The separation of floatable fractions in aqueous slurries is effected by the presence of micro gas bubbles introduced into the separation chamber (4). The separated floatable fractions can be removed from the gas bubbles to which they adhere by means of an anti-foaming device driven by the rotary shaft (5) of the transport rotor device (20).

Description

The present invention relates to a method and apparatus for separating a heavy fraction of an aqueous slurry from a light fraction by centrifugal force action.
More particularly, the present invention relates to the cleaning of a liquid slurry having a solid particle fraction that is less than a certain size, i.e., the post-cleaning of a slurry that has already been subjected to pre-cleaning to remove coarse particles, such as by a screen. .
At the time of separation by a centrifugal separator or a hydrocyclone, a pre-washed slurry is introduced into the separation chamber at a high speed to generate a violently rotating laminar flow field in the chamber. Push the fraction into the perimeter path and collect the light fraction of the slurry rather near the longitudinal centerline of the separation chamber. In known centrifuges (U.S. Pat. No. 2,996,187), a suction transport rotor means provided downstream of the separation chamber outlet provides the pressure gradient required to flow the slurry between the separation chamber inlet and outlet. It is generated. Therefore, the pressure gradient between the inlet and the outlet is determined by the suction force of the suction transport rotor means, which, on the contrary, is filled to 1 bar by the suction transport rotor means due to the liquid column present on the suction side. Defined to be able to produce no pressure gradient. Thus, conventional centrifuges can only be used for suspensions where sufficient separation is achieved even at relatively low slurry rotation speeds. In order to process the fraction of aqueous slurries that are more difficult to separate, higher rotational speeds are required in the separation chamber in order to produce correspondingly higher centrifugal forces. This requires a pressure gradient of several bars that cannot be generated by known centrifuges, so it is generally necessary to arrange several small centrifuges in series to reach the desired separation speed. There is. This substantially increases the procurement and operating costs of the separation plant and increases its maintenance frequency. In addition, the throughput of small centrifuges is relatively low, thus limiting the application of systems equipped with such devices to specific use cases.
One particularly relevant issue is the effective separation of suspended particulate matter from aqueous slurry by the action of centrifugal forces. In the case of floating separation, it has been proposed to introduce gas into the slurry circulating in the separation chamber to generate bubbles (US Pat. No. 4,397,741). The heavy fraction separated from the slurry tends to adhere to the bubbles due to the interfacial effect. The bubbles form a so-called buoyant body, so that the heavy fraction can not only gather near the longitudinal centerline of the separation chamber, but also be drawn against the action of gravity. However, the efficiency of the separation is based solely on the tangential introduction of the slurry into the separation chamber, i.e. there is no means to boost the pressure gradient and the size of the bubbles that can be achieved by the known means is too large. The effectiveness of this device is low.
It is an object of the present invention to provide a method and apparatus of the kind described above that can produce the high rotational speeds required to process all kinds of slurries, including those with floating fractions, in a highly effective manner. It is to provide.
With regard to the solution of this object, reference is made to claims 1 and 8. Within the scope of the present invention, surprisingly, the slurry is pressurized just before the inlet to the separation chamber, thereby creating a pressure gradient of several bars necessary for high rotational speeds, substantially complicating the system. It has been found that the problems associated with known centrifuges can be easily eliminated without doing so. For this purpose, transport rotor means are provided upstream of the inlet. The transport rotor means functions as a kind of centripetal accelerator and cooperates with stator means that converts kinetic energy introduced into the slurry by the transport rotor means into pressure energy. As a result, the separation chamber inlet is not dependent on the flow pressure in the conduit through which the slurry is fed to the centrifuge, and is not dependent on the level of the liquid column between the separation chamber inlet and outlet. It is guaranteed that a constant gradient overpressure is always applied to the slurry. This results in an increased rotational speed with a correspondingly increased separation speed. With effective separation that is largely independent of the size of the centrifuge, a separation device having a larger size or diameter than in known systems can be used to achieve a correspondingly favorable effect on operating and procurement costs. it can.
In accordance with a further embodiment of the present invention, the introduction of additional rotational energy into the slurry present in the separation chamber further improves the separation efficiency achieved by providing transport rotor / stator means disposed on the inlet side. Can be increased. This can be achieved by arranging in the separation chamber cyclone rotor means that circulates along the inner wall of the housing by an impeller that can be driven by the same rotation axis as that of the transport rotor means. The cyclone rotor means does not cause turbulence and allows an increase in the rotational speed of the slurry introduced into the separation chamber without depending on the nature of the slurry. The back pressure applied by the cyclone rotor means is then overwhelmed by the pressure applied to the slurry by the transport rotor means at the inlet.
As a result of the means described above, the present invention is also particularly suitable for the floating separation of slurries that are otherwise difficult to separate by centrifugal action, for example to remove printing ink residues from the discharged sludge. In this regard, one further embodiment of the present invention provides for the separation of the slurry in the presence of bubbles, preferably microbubbles. For this purpose, a liquid saturated with microbubbles is introduced into the separation chamber and mixed with the slurry, or the slurry itself is gasified and introduced into the separation chamber in a gasified state. A foam breaking means having a rotationally driven impeller is disposed in the upper mounting housing of the centrifugal separator spaced from the transport rotor means, so that the foam in the foam mixture of bubbles and foreign matter discharged from the separation chamber. The adhering foreign matter can be separated by centrifugal action and discharged separately to the environment.
In general, the centrifuge of the present invention is characterized by a relatively simple structure by allowing all of the rotor means to be disposed on a common rotating shaft. In addition, the centrifuge has a suction effect so that it can be easily completed without adding an additional pump assembly to the flow system as a drive for the slurry to be processed.
Below, based on an embodiment, the present invention is explained still in detail, referring to drawings.
FIG. 1 is a partial longitudinal sectional view of a centrifugal separator according to a preferred embodiment of the present invention.
2A to 2C are an overall view (FIG. 2A), a bottom view (FIG. 2B), and a plan view (FIG. 2C) showing details of the centrifugal separator shown in FIG. 1.
3 is a cross-sectional view taken along line III-III in FIG.
FIG. 4 shows a centrifuge similar to FIG. 1 viewed in the same manner as FIG. 1 for the second embodiment of the present invention.
FIG. 5 shows a centrifugal separator according to a third embodiment of the present invention.
FIG. 6 shows a centrifuge for floating separation according to a fourth embodiment of the present invention.
Reference is now made to FIGS. 1, 2A to 2C and 3 illustrating the centrifuge of the present invention. Reference numeral 1 in FIG. 1 shows a tubular cylindrical housing which transitions to a funnel-shaped bottom 2 which tapers to a lower outlet 3. The housing 1 defines a separation chamber 4 in which a hollow shaft 5 projects coaxially with the longitudinal centerline, the hollow shaft having an open lower end in the axial direction and a funnel-shaped part 2 downward. It terminates at an appropriate distance from the starting surface.
A coupling means 7 is provided at the axially upper end of the hollow shaft 5 protruding from the housing 1, which means a driving means 8 in the form of an electric motor, for example, for rotating the hollow shaft 5 at a suitable rotational speed. It is connected.
In the embodiment of the invention shown, the hollow shaft 5 is supported only by the drive means 8 without bearings. If desired, a suitable bearing assembly may be provided to support the hollow shaft 5 relative to the housing 1.
As shown in FIGS. 2A and 2B, the mounting plate 12 is fixed to an intermediate position in the axial direction of the hollow shaft 5, for example, by welding, and surrounds the hollow shaft 5 with a radial surface. A plurality of impellers 11 are fixed to the lower surface of the mounting plate 12 at equal intervals from each other. These impellers project radially outward from the hollow shaft 5 and extend to the vicinity of the inner periphery of the housing 1. In the illustrated embodiment, four impellers are provided. However, more or fewer such impellers may be provided.
The impeller 11 forms a cyclone rotor means, indicated by reference numeral 10 in FIG. 1, for circulating the fluid slurry introduced into the separation chamber 4 along the inner wall of the housing 1. The resulting centrifugal force promotes the heavy fraction of the slurry to collect near the inner wall of the separation chamber 4 and the light fraction enters and exits into the hollow shaft 5 from where it further becomes less As will be described in detail, it can be discharged to the outside.
As further shown in FIGS. 1, 2 </ b> A to 2 </ b> C, a plurality of impellers 21 are fixed to the upper side of the mounting plate 12, substantially spirally and radially outward from the hollow shaft 5, from the longitudinal center line of the hollow shaft 5. It extends to a point separated by a distance D greater than the diameter d of the arc drawn by the outer end of the impeller 11 of the cyclone rotor means 10, ie the radial dimension of the separation chamber 4. As illustrated, the impeller 21 can protrude by an appropriate short distance from the outer peripheral edge of the mounting plate 12. Preferably, the ratio D: d is 1.25: 1 to 1.75: 1, most preferably about 1.50: 1.
The impeller 21 is part of a transport rotor means which cooperates with the stator means 22 shown in more detail in FIG.
The stator means 22 is a radial surface below the surface of the impeller 21 of the transport rotor means 20, preferably a radius substantially coincident with the inner circumference of the housing 1 from a radially outer position corresponding to the dimension D in FIG. 2A. A plurality of fixed guide elements 23 extending spirally to a position on the inner side in the direction are included. The inner end of the guide element 23 is preferably oriented substantially tangential to the inner circumference of the housing 1. A passage 24 is defined between the adjacent guide elements 23, and the slurry can enter and leave the separation chamber 4 through these passages. Like the impeller 21 of the transport rotor means 20, the guide element 23 of the stator means 22 projects outward and exceeds the peripheral edge of the mounting plate 12, and a flow is formed between the stator means 22 and the transport rotor means 20. It is like that.
As can be further seen from FIG. 1, the radially outer portion of the impeller 21 of the transport rotor means 20 and the guide element 23 of the stator means 22 are flange-shaped configured in an upper mounting housing disposed on the housing 1. Are accommodated in the chamber 25. This upper mounting housing is indicated by reference numeral 6.
The stator means 22 has the purpose of reducing the rotational speed of the slurry produced by the transport rotor means 20. As a result of the decrease in the rotational speed of the slurry, the slurry is subjected to overpressure, and then passes through the passage 24 in a tangential direction to enter and exit the affected area of the separation chamber 4 and the cyclone rotor means 10. Circulated by the cyclone rotor means 10. The rotational speed of the slurry in the separation chamber 4 is dictated by the working surface area and rotational speed of the impeller 11 of the cyclone rotor means 10, the processing capacity and the tangential introduction of the slurry into the separation chamber 4.
In the above embodiment, the cyclone rotor means 10 and the transport rotor means 20 are attached to the same hollow shaft 5 as the drive shaft so as to rotate at the same speed. If desired, the cyclone rotor means 10 and the transport rotor means 20 may be provided with separate drive shafts to operate the two means at different speeds.
As shown in FIG. 1, the slurry is introduced into the pre-chamber 31 of the upper mounting housing 6 through the inlet 30, and this pre-chamber is connected to the transport rotor means 20.
The light fraction of the slurry separated by the action of the cyclone rotor means 10 is poured into the hollow shaft 5 by the pressure gradient generated by the transport rotor means 20, and a plurality of openings 9 formed near the upper end of the hollow shaft 5. Through the hollow shaft 5. From here, the light fraction enters and exits the pre-chamber 32 on the outlet side of the upper mounting housing 6. This pre-chamber surrounds the hollow shaft 5 and is connected to the outlet 33. In the illustrated embodiment of the invention, the slurry enters the centrifuge at substantially the same radial surface as it exits the centrifuge, as is apparent from FIG. However, the inlet and outlet may be located on different radial surfaces, as will be further described below.
As a result of the gravitational action, the separated heavy fraction of the slurry collects at the funnel-shaped bottom 2 of the housing 1 and is discharged from there through the outlet 3 continuously or at appropriate time intervals. Can do. Preferably, the outlet 3 has an adjustable opening width.
FIG. 4 shows a modified and simplified embodiment of the centrifuge according to the invention which is particularly suitable for processing slurries with light fractions or fractions from which foreign substances can be separated. Components that are the same as or similar to the embodiment described above are indicated by the same reference number plus 100. This embodiment substantially eliminates the cyclone rotor means, and thus the circulation of the slurry in relation to the overpressure caused by the transport rotor means 120 and the stator means 122 disposed upstream of the inlet. It differs from the previous embodiment in that it occurs only by introducing a tangential direction into the chamber 104.
As shown in the figure, the transport rotor means 120 has a deformed structure because the impeller 121 extends only to the outer periphery of the mounting plate 112. For this reason, on the outer periphery of the mounting plate 112, an annular space 126 is defined in the upper mounting housing 106, into which slurry flows by the action of the transport rotor means 120 into the affected area of the stator means 122. You can go in and out. It has been found that this deformation can achieve an improvement in the efficiency of the transport rotor means 120, the stator means 122. If desired, such modified transport rotor means may be provided in the embodiment of the invention shown in FIG.
Furthermore, compared to the embodiment described above, the cylindrical section of the housing 101 is shortened by an appropriate dimension and the section 102 that tapers to the outlet 103 is extended accordingly. For further details of the shape, reference can be made to FIGS. 1-3 and the corresponding description.
The following relates to an embodiment of the centrifuge according to the invention which is particularly suitable for the floating fine separation of a prefiltered slurry or sludge that remains after prefiltration, i.e. has a fraction of foreign matter, for example having a dimension of less than 2 mm.
FIG. 5 shows an embodiment of a floating centrifuge. This embodiment relates to the structure of the feeding means for feeding the slurry, the inlet 230 and the pre-chamber 231, the transport rotor means 220 disposed upstream of the inlet in the separation chamber 204, the stator for the upstream pressurization of the slurry. It comprises means 222 as well as cyclone rotor means 210 substantially corresponding to the embodiment of FIG. 1, so that reference can be made to FIG. Components that are the same as or similar to the embodiments described above are indicated by the same reference number plus 200.
As shown, the transport rotor means 220 and cyclone rotor means 210 are disposed on a common drive shaft 254 that does not act simultaneously to discharge separated fractions of the slurry to be treated. Furthermore, compared to the embodiment shown in FIG. 1, the working surface area of the impeller 211 of the cyclone rotor means 210 can be reduced by the reduced axial dimension of the impeller.
As shown, the housing 201 is cylindrical throughout, and therefore a separation chamber 204 that is also cylindrical throughout is formed. The tubular element 255 that passes axially through the bottom 252 of the housing 201 has an end that opens into the separation chamber 204, so that one open end of the tubular element 255 can be properly extended from the bottom 252 of the housing 201. Located apart from each other, the other open end is disposed outside the housing 201. Preferably, the tubular element 255 is attached to the housing 201 so as to be movable in the axial direction. The tubular element 255 serves to discharge a fine foreign matter fraction of the slurry that is separated by floating separation described below.
The liquid or clear product from which foreign material has been removed can be discharged via an outlet 253 that leads tangentially into the separation chamber 204 near the bottom 252 of the housing 201.
Means for introducing a suitable gas, eg, a liquid containing air, into the separation chamber 204 is provided at an axially intermediate position of the housing 201. These means include an annular distribution conduit 256 that surrounds the circumferential portion of the housing 201, which is the housing wall in which the perforations 257 are perforated. An inlet 258 leads into the distribution conduit 256. Accordingly, a liquid containing gas can be pumped into the separation chamber 204 via the inlet 258, the distribution conduit 256 and the perforation 257.
The associated liquid is preferably a liquid in which the gas is distributed in the form of microbubbles, for example having dimensions of less than 100 μm. Such a liquid saturated with microbubbles can be produced, for example, using an apparatus constructed according to DE-A-3733583, which can be referred to and referenced in FIG. The device 259 is connected to a gasification tank 260 into which the liquid to be gasified and a suitable gas can be separately introduced and pressurized.
Water can be used as a suitable liquid. In this regard, a suitable liquid may also be a clear product branch that is discharged via outlet 253, as shown, and this clear product is gasified via pump 261. It is fed into a tank 260 (filled with gas here) and introduced into a device 259 for generating microbubbles.
The microbubbles introduced into the slurry as described above in the separation chamber 204 are bound to the fine suspended foreign matter fraction of the slurry due to their surface tension. In this way, these fine fractions preferably collect near the longitudinal centerline of the centrifuge device under the influence of centrifugal force. Therefore, the microbubbles to which the foreign matter fraction is attached can be discharged from the separation chamber 204 through the central tubular element 255, and a clear product can be produced at the outlet 253.
It is noted that instead of a liquid saturated with microbubbles, gas can also be introduced directly into the separation chamber 204 to generate bubbles in the slurry. In order to produce bubbles with minimal dimensions, the introduction of gas should be done through a diffusion ring (not shown) made of particulate sintered metal that would have to be provided instead of the distribution conduit 256. It is.
Further, the cyclone rotor means 210 is omitted, and the circulation of the slurry similar to the embodiment shown in FIG. 4 causes the pressure-increasing effect of the interaction between the transport rotor means 220 and the stator means 222 and the tangent of the slurry to the separation chamber 204. You may make it based only on direction introduction.
Furthermore, similar to the means described with respect to the embodiment of the present invention shown in FIGS. 1 and 4, the discharge of microbubbles with foreign matter attached results against the action of gravity through the central hollow shaft. be able to. This hollow shaft simultaneously represents a common axis of rotation for the transport rotor means 220 and the cyclone rotor means 210.
FIG. 6 shows a floating centrifugal separator according to a fourth embodiment of the present invention. Components that are the same as or similar to the embodiment described above are indicated by the same reference number plus 300. This fourth embodiment includes a housing 301 that is generally cylindrical, defining a separation chamber 304 that is also generally cylindrical. Upstream of the inlet to the separation chamber 304, transport rotor means 320 and cooperating stator means 322 are provided to pressurize the slurry. The structure and function of these means correspond to the means of the embodiment shown in FIG. 1, so that repeated description can be avoided. As with the embodiment shown in FIG. 4, the cyclone rotor means is omitted.
One feature of the centrifugal separator shown in FIG. 6 is a bubble breaking means indicated by reference numeral 370. The bubble breaking means 370 includes a plurality of impellers 371 that can rotate about a central axis that preferably coincides with the rotational axis of the impeller 321 of the transport rotor means 320. These impellers are disposed in a space 372 in an upper mounting housing 306 disposed above the separating device housing 301. This space 372 is located above the space 373 in the upper mounting housing 369 including the transport rotor means 320 and the stator means 322. The slurry to be treated can be introduced into this space 373 via the inlet 374. More specifically, the slurry in which microbubbles are dispersed can be introduced through the inlet 374. These microbubbles can be introduced into the slurry by the apparatus already described with respect to the embodiment shown in FIG.
The spaces 372 and 373 in the upper mounting housing 369 are sealed to each other, and the upper space 372 includes a lower portion 372 ′ including the impeller 371 of the foam breaking means 370 and a lower portion near the hollow shaft 305. The lower portion 372 'is divided into an upper portion 372' and a circulated upper portion 372 ". The foreign portion outlet 376 communicates with the lower portion 372 '. The peripheral wall of the upper mounting housing 369 extends along the upper portion 372". A plurality of perforations 377 distributed in the circumferential direction are perforated. These perforations connect the interior of the upper portion 372 "to the gas outlet 378, allowing the gas fraction removed from the separated foreign matter to be discharged to the environment.
As already mentioned, the impeller 371 of the bubble breaking means 370 can be attached to the same rotation axis as the rotation axis of the impeller 321 of the transport rotor means 320. This rotating shaft is configured as a hollow shaft 305 that protrudes in the axial direction and enters the separation chamber 304 and has an open lower end. In this open end, foreign matter that has been separated and adhered to the bubbles can enter, and from there rises inside the hollow shaft 305, enters and exits the space 372 of the bubble breaking means 370, and consequently the influence of the impeller 371. Enter and exit the area.
A tangential outlet 380 near the bottom 379 of the separator housing 301 serves to expel a liquid fraction of the slurry, i.e. a clear product free of foreign matter.
In the bubble breaking means 370, the foreign matter adhering to the bubbles entering and leaving the space 372 is circulated by the impeller 371, whereby heavy foreign matters are separated from the bubbles by centrifugal action, and the lower space portion 372 ' Air bubbles gather at the inner periphery and rise in the upper space portion 372 ″ from which they can be expelled into the environment as already described.
Instead of introducing a pre-gasified slurry through the inlet 374, the slurry is caused by gas introduced into the separation chamber 304 separately from the slurry in the presence of bubbles in the separation chamber 304 in accordance with the embodiment shown in FIG. It may be processed.
Further, if desired, cyclone rotor means similar to the embodiment of the invention shown in FIG. 1 may be provided. In this case, the impeller 371 of the bubble breaking means 370, the impeller 321 of the transport rotor means 320, and the impeller of the added cyclone rotor means can be attached to the hollow shaft 305 driven by the drive means 308 in order to rotate together. . It will be appreciated that an independent drive shaft may be provided for driving the impeller, similar to the embodiments of the invention described above.

Claims (14)

  1. The slurry is circulated through the separation chamber under the influence of a pressure gradient existing between the inlet and outlet of the cyclone separation chamber, so that the light fraction of the slurry is separated from the heavy fraction of the slurry, And the light fraction are separately discharged from the separation chamber, the method of separating the heavy fraction of the aqueous slurry from the light fraction by centrifugal force action, the impeller of the rotationally driven transport rotor means, The pressure element is generated in the slurry just before being introduced into the separation chamber by cooperating with a guide element of the stator means provided just before the entrance to the separation chamber to expose the slurry to overpressure. A method characterized by.
  2. To increase the pressure, the slurry is accelerated upstream from a position where it is introduced into the separation chamber from a radially inner position to a radially outer position, decelerated at or near the radially outer position, and the introduction 2. A method according to claim 1, characterized in that it is deflected against a flow in a direction towards the position.
  3. The method according to claim 1 , wherein the slurry is introduced in a tangential direction with respect to the separation chamber .
  4. The method according to claim 1, wherein further rotational energy is introduced into the slurry present in the separation chamber.
  5. The method according to claim 1, wherein the separation of the slurry is carried out in the presence of bubbles.
  6. 6. The method according to claim 5, wherein a liquid saturated with microbubbles is introduced into the separation chamber and mixed with the slurry.
  7. 6. The method of claim 5, wherein the slurry is pressurized and gasified to relax by forming microbubbles and introduced into the separation chamber in a gasified state.
  8. A separation chamber (4, 104, 204, 304) defined in a housing (1, 101, 201, 301) for separating a heavy fraction from a light fraction of an aqueous slurry by centrifugal force action; Means for creating a pressure gradient between the inlet and outlet of the separation chamber to circulate the slurry in the separation chamber; and means for discharging the light fraction from the separation chamber (5, 105 , 255, 305) and means (3, 103, 253, 380) for discharging the heavy fraction of the slurry from the separation chamber, in order to generate a pressure gradient, The transport rotor means (20, 120, 220, 320) driven to rotate about the rotation shaft (5, 105, 254, 305) is the upper mounting housing (6, 10) of the separation device. , Provided in the 206 and 306),
    Stator means (22, 122, 222, 322) in which the transport rotor means is provided immediately upstream of the inlet to the separation chamber to subject it to overpressure substantially immediately before the slurry is introduced into the separation chamber. collected by cooperating centrifuge apparatus characterized by having a larger radial dimension than the radial dimension (d) of the separation chamber (D).
  9. Cyclone rotor means (10, 210) for circulating the slurry introduced into the separation chamber along the inner wall of the housing (1, 201) by the impeller (11, 211) in order to introduce further rotational energy into the slurry. 9. A separating chamber (4, 204), characterized in that the cyclone rotor means is driven by the same rotational axis (5, 254) as the rotational axis of the transport rotor means (20, 220). The centrifugal separator described.
  10. The ratio of the radial dimension (D) of the transport rotor means (20, 120, 220, 320) to the radial dimension (d) of the separation chamber (4, 104, 204, 304) is about 1.25: 1. The centrifuge according to claim 8 or 9, wherein the ratio is 1.75: 1.
  11. 9. Centrifugal device according to claim 8, characterized by means (256-261, 359) for introducing bubbles into the separation chamber (204, 304).
  12. The means (256 to 261, 359) for introducing bubbles includes a gasification tank (260) for introducing gas into the liquid, and the gasification tank for generating microbubbles in the gasification liquid. The centrifuge according to claim 11, further comprising a buffer device (259, 359) in communication with the device.
  13. For separating the foreign matter adhering to the bubbles by centrifugal force action from the mixture of bubbles and foreign matter disposed axially away from the transport rotor means (320) and discharged from the separation chamber (304), 13. Centrifugal separator according to claim 11 or 12, characterized in that it comprises a bubble breaking means (370) having an impeller (371) driven in rotation.
  14. 14. The centrifugal separator according to claim 13, wherein the impeller (371) of the bubble breaking means (370) and the impeller of the transport rotor means (320) are driven by the same rotating shaft (305).
JP53851197A 1996-04-25 1997-04-17 Method and apparatus for separating heavy fraction of aqueous slurry from light fraction by centrifugal force action Expired - Lifetime JP4047386B2 (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
DE19616602.0 1996-04-25
DE1996116602 DE19616602A1 (en) 1996-04-25 1996-04-25 Motor-driven centrifugal separator or hydrocyclone for aqueous suspensions
DE1996125456 DE19625456A1 (en) 1996-06-26 1996-06-26 Slurry separation, e.g. removal of heavy slurry, e.g. dye, from lighter slurry
DE19625456.6 1996-06-26
DE1996146494 DE19646494A1 (en) 1996-11-11 1996-11-11 Slurry separation, e.g. removal of heavy slurry, e.g. dye, from lighter slurry
DE19646494.3 1996-11-11
PCT/EP1997/001913 WO1997040944A1 (en) 1996-04-25 1997-04-17 Process and apparatus for the separation of heavier from lighter fractions in aqueous slurries by means of centrifugal force

Publications (2)

Publication Number Publication Date
JP2000508968A JP2000508968A (en) 2000-07-18
JP4047386B2 true JP4047386B2 (en) 2008-02-13

Family

ID=27216180

Family Applications (1)

Application Number Title Priority Date Filing Date
JP53851197A Expired - Lifetime JP4047386B2 (en) 1996-04-25 1997-04-17 Method and apparatus for separating heavy fraction of aqueous slurry from light fraction by centrifugal force action

Country Status (7)

Country Link
EP (1) EP0904156B1 (en)
JP (1) JP4047386B2 (en)
AT (1) AT203431T (en)
AU (1) AU2387397A (en)
ES (1) ES2162280T3 (en)
HK (1) HK1018889A1 (en)
WO (1) WO1997040944A1 (en)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19811090A1 (en) * 1998-03-13 1999-09-16 Georg Klas Cyclone separator for effluent household gray water
DE102005023258A1 (en) 2004-11-16 2006-11-23 Fan Separator Gmbh Rotary drum for aerobic heating of free-flowing solids
DE102005009683B4 (en) * 2005-03-03 2016-08-18 Fan Separator Gmbh Process for the recovery of solids
DE202007002541U1 (en) * 2007-02-21 2007-07-05 Blum, Holger Hydrocyclone device and hydrocyclone separating battery
JP4775913B2 (en) * 2007-07-13 2011-09-21 ミスズテクノ株式会社 Cyclone filter
GB2461874B (en) * 2008-07-14 2012-11-21 Caltec Ltd Separation system and method
JP6604601B2 (en) * 2014-06-05 2019-11-13 永進テクノ株式会社 Cyclone separator

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2996187A (en) * 1961-08-15 payne
US2701642A (en) * 1951-04-11 1955-02-08 Goodwin Norris Continuous centrifugal separator
US4399027A (en) * 1979-11-15 1983-08-16 University Of Utah Research Foundation Flotation apparatus and method for achieving flotation in a centrifugal field
JPS60501197A (en) * 1983-01-28 1985-08-01
DE3445586C2 (en) * 1984-12-14 1989-03-23 Amberger Kaolinwerke Gmbh, 8452 Hirschau, De
DE4009042C2 (en) * 1990-03-21 1996-12-12 Voith Gmbh J M Apparatus for separating air from Flotationstrüben

Also Published As

Publication number Publication date
JP2000508968A (en) 2000-07-18
EP0904156B1 (en) 2001-07-25
HK1018889A1 (en) 2002-03-22
ES2162280T3 (en) 2001-12-16
AT203431T (en) 2001-08-15
EP0904156A1 (en) 1999-03-31
AU2387397A (en) 1997-11-19
WO1997040944A1 (en) 1997-11-06

Similar Documents

Publication Publication Date Title
US3504804A (en) Centrifugal separator
US3529724A (en) Hydrocyclone filter
US3234716A (en) Apparatus for separating dust and other particles from suspension in a gas
CA1185708A (en) Froth flotation apparatus and method
US3454163A (en) Method of separating solids from liquids
CA1295980C (en) Agitator mill
JP2005042698A (en) Method of purifying crankcase gas
AU596924B2 (en) Improved froth flotation method and apparatus
CA1292459C (en) Continuous flow centrifugal separation
US4921400A (en) Pump and a method of separating gas by such from a fluid to be pumped
US7396373B2 (en) Centrifugal separator for cleaning gases
US4425232A (en) Flotation separation apparatus and method
CA1337774C (en) Flotation machine
US3973930A (en) Drilling mud degasser apparatus and method
FI97024B (en) Method and device for separating gas from gasified material
US3655058A (en) Filtration apparatus
US5755965A (en) Cyclonic de-gasser
US4326863A (en) Centrifugal degasser
US6074554A (en) Aeration system
US3912622A (en) Screening machine with lights removal
AU679853B2 (en) Attrition mill
US4919826A (en) Process and apparatus for separating solids and liquids from an effluent stream
US5062955A (en) Rotating sleeve hydrocyclone
KR100832063B1 (en) Centrifugal Pressurized Separators and Methods of Controlling Same
US4043919A (en) Pressure screen with turbulence chamber means

Legal Events

Date Code Title Description
A621 Written request for application examination

Free format text: JAPANESE INTERMEDIATE CODE: A621

Effective date: 20040402

A131 Notification of reasons for refusal

Free format text: JAPANESE INTERMEDIATE CODE: A131

Effective date: 20051220

A601 Written request for extension of time

Free format text: JAPANESE INTERMEDIATE CODE: A601

Effective date: 20060316

A602 Written permission of extension of time

Free format text: JAPANESE INTERMEDIATE CODE: A602

Effective date: 20060508

A524 Written submission of copy of amendment under section 19 (pct)

Free format text: JAPANESE INTERMEDIATE CODE: A524

Effective date: 20060620

TRDD Decision of grant or rejection written
A01 Written decision to grant a patent or to grant a registration (utility model)

Free format text: JAPANESE INTERMEDIATE CODE: A01

Effective date: 20071106

A61 First payment of annual fees (during grant procedure)

Free format text: JAPANESE INTERMEDIATE CODE: A61

Effective date: 20071122

R150 Certificate of patent or registration of utility model

Free format text: JAPANESE INTERMEDIATE CODE: R150

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20101130

Year of fee payment: 3

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20101130

Year of fee payment: 3

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20111130

Year of fee payment: 4

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20121130

Year of fee payment: 5

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20131130

Year of fee payment: 6

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

EXPY Cancellation because of completion of term