WO1997040944A1 - Process and apparatus for the separation of heavier from lighter fractions in aqueous slurries by means of centrifugal force - Google Patents

Process and apparatus for the separation of heavier from lighter fractions in aqueous slurries by means of centrifugal force Download PDF

Info

Publication number
WO1997040944A1
WO1997040944A1 PCT/EP1997/001913 EP9701913W WO9740944A1 WO 1997040944 A1 WO1997040944 A1 WO 1997040944A1 EP 9701913 W EP9701913 W EP 9701913W WO 9740944 A1 WO9740944 A1 WO 9740944A1
Authority
WO
WIPO (PCT)
Prior art keywords
deposition chamber
means
slurry
characterized
separation
Prior art date
Application number
PCT/EP1997/001913
Other languages
German (de)
French (fr)
Inventor
Dietrich Eichler
Original Assignee
Fan Separator Gmbh
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
Application filed by Fan Separator Gmbh filed Critical Fan Separator Gmbh
Priority claimed from DE1997504134 external-priority patent/DE59704134D1/en
Publication of WO1997040944A1 publication Critical patent/WO1997040944A1/en
Priority claimed from US09/177,597 external-priority patent/US6036871A/en

Links

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

Method and apparatus for depositing of the heavier aqueous slurries from the lighter fractions using

centrifugal force

The invention relates to a method and a device for separating the heavier aqueous slurries from the lighter fractions by centrifugal force.

The invention particularly relates to the purification of liquid slurries with a content of solid particles below a certain size, that is, to the clearing of pulps which have been subjected by screens or the like. Already a pre-cleaning to remove coarser particles.

In the deposition by means of centrifugal separators and hydrocyclones a prepurified slurry at high speed in a deposition chamber is introduced so that it forms a strong rotating laminar flow field, so that the heavier fractions of the slurry are pushed by centrifugal force to an outer diameter web while the accumulate lighter fractions of the slurry is preferably close to the central longitudinal axis of the deposition chamber. In a known centrifugal separator (US-A-2,996,187) the required for flow of the slurry between the inlet and outlet of the deposition chamber pressure difference is applied by a Saugtransportrotoreinrichtung which is downstream of the outlet of the deposition chamber. The pressure drop between inlet and outlet is therefore determined by the suction force of the Saugtransportrotoreinrichtung and which in turn is determined by the intake side pending liquid column so that a pressure differential can be created by only less than 1 bar by means of the Saugtransportrotoreinrichtung. The known centrifugal separator can therefore only be used for suspensions in which a sufficient separation effect is obtained even at relatively low rotational speeds of the pulp. To treat less easily depositable components from aqueous slurries, higher rotational speeds are required in the deposition chamber to generate correspondingly high centrifugal forces. This would require a pressure differential of a few bars, which can not be applied by known centrifugal separators so that you had to arrange generally several small-sized centrifugal succession to get to a desired deposition rate. This increases the cost significantly the capital and operating costs of the capture plant and increases their maintenance requirements. The throughput of the small-sized centrifugal separators is also comparatively low, so that the use of so-equipped plants is limited to certain applications.

A particular problem prepares the effective separation flotierbarer particulate matter from aqueous slurries using centrifugal force. In the US-A-4,397,741 is proposed for the flotation separation, in addition to introduce a gas into the circular in a deposition chamber slurry to generate gas bubbles, which are expected of them believe that adhere by interfacial effects the separated heavier components of the slurry. The gas bubbles form quasi float so that the heavier fractions can also be deducted against gravity effect preferentially collect not only near the center longitudinal axis of the deposition chamber, but. However, the effectiveness of this known device is low because the deposition effect alone is based on a tangential introduction of the slurry into the Abscheidunsgkammer by druckgefälleerhöhende measures are entirely absent, and also achievable with the known means gas bubbles have too large a size.

The invention has for its object to provide a method and a device of the initially mentioned kind, which provides the required high rotational speeds in order to treat all types of pulps including those with floatable units with high efficiency.

To solve this problem, reference is made to the claims 1 and 8. FIG. Surprisingly it has been found in the invention that the problems associated with known centrifugal separators problems can be eliminated in a simple manner without substantial complication of the system characterized by the pressure drop required for high rotational speeds of a few bar by pressurizing the slurry immediately before the inlet into the deposition chamber is applied. For this purpose, a transport rotor means is upstream of the inlet provided, which acts in the manner of a radial accelerator and cooperates with a stator which, converts the kinetic energy, which has been introduced from the transport rotor means in the slurry in pressure energy. This ensures that the inlet side of the deposition chamber is always a sufficient gradient pressure is exerted on the slurry, over which the pulp is led to the centrifugal separator which is independent of a flow pressure in a line, and also independent of the height of the liquid column between the inlet and the outlet of the deposition chamber. can Infolgedesssen an increased speed of rotation are applied with correspondingly increased deposition rate. Characterized in that an effective deposition is largely independent of the dimensions of the centrifugal separator can be used with larger dimensions or larger diameters than known systems under correspondingly favorable impact on the operating and investment costs separator.

The improvements achieved by the provision of the inlet side arranged Transportrotor- / Statoreinrichtungen in the deposition efficiency can be further increased if additional rotational energy is introduced according to a development of the invention in the present in the deposition chamber turbidity. This can be done in that a cyclone rotor means is positioned in the deposition chamber, which can be driven by the same rotational axis as the rotor transportation device. The cyclone rotor assembly allows increased turbulence-free and the type of the introduction of the slurry into the deposition chamber independent rotation speeds, whereby the counter-pressure exerted by the cyclone rotor means is overcome by the pressure that the einlasseitige transport rotor means exerts on the pulp.

Through the measures described, the invention in particular for the flotation separation of otherwise difficult separable by means of centrifugal force slurries, for example, for removing ink residues from elutriated waste paper materials is suitable. A related development of the invention therefore provides that the deposition of the slurry is carried out in the presence of gas bubbles, preferably in the presence of microbubbles. For this purpose a interspersed with microbubbles liquid may be introduced into the deposition chamber for mixing with the slurry, or the slurry itself is gassed and gassed introduced into the deposition chamber. A arranged in a housing top part of the centrifugal separator at an axial distance to the transport rotor means

Foam destruction device with rotatably driven rotor blades may be provided to deposit by means of centrifugal action adhering to the gas bubbles in a foreign substances discharged from the deposition chamber frothy gas bubbles impurity mixture and to discharge separated to the outside.

Overall, a centrifugal separation according to the invention is characterized by a relatively uncomplicated structure by all said rotor means may be arranged on a common rotary shaft. The centrifugal separator also has suction effect and can therefore easily without pumping additional units in a flow system are integrated as a driver for a slurry to be treated.

The invention is explained below with reference to embodiments and the drawing. Show it:

Fig. 1 in a partially longitudinally sectioned view of a centrifugal separator according to a preferred embodiment of the invention, Fig. 2A-2C a detail of the centrifugal separator of FIG. 1 in an overall view (Fig. 2A), bottom view (FIG. 2B) and plan view (Fig. 2C) .

Fig. 3 is a sectional view taken along the

Section line III-III in Fig. 1,

Fig. 4 is a view similar to FIG. 1 a

The centrifugal separator of Fig. 1 according to a second embodiment of the invention,

Fig. 5 shows a centrifugal separator according to a third modified embodiment of the invention, and

Fig. 6 shows a centrifugal separator for the

Flotation separation according to a fourth embodiment of the invention.

Reference is now made to FIGS. 1, 2A-2C and 3, which show a centrifugal separator according to the invention. The reference numeral 1 in Fig. 1 relates to a tubular cylindrical housing, which merges into a funnel-shaped bottom portion 2 tapers towards a discharge opening 3 at the bottom. The housing 1 defines a separation chamber 4, in coaxial with the central longitudinal axis of a hollow shaft 5 extends, which ends with its lower axial open end at a suitable distance from the plane from which the funnel-shaped portion 2 extending downwardly.

At the top, the housing 1 projecting axial end of the hollow shaft 5, a clutch device 7 is provided, which is in the form of an electric motor connected to a drive means 8, for example, to enable the hollow shaft 5 with a suitable rotational speed in rotation.

In the illustrated embodiment of the invention, the hollow shaft 5 is superimposition supported only by the driving means. 8 If desired, to support the hollow shaft 5 relative to the housing 1, a suitable storage arrangement could be provided.

As shown by FIGS. 2A and 2B is fixed at an intermediate axial position of the hollow shaft 5, a mounting plate 12, for example welded, which surrounds the hollow shaft 5 in a radial plane. a plurality of rotor blades 11 are at the bottom of the mounting plate 12 at equal angular distances from each other fixed that protrude from the hollow shaft 5 radially outwardly to near the inner periphery of the housing. 1 In the illustrated embodiment, four rotor blades 11 are provided. However, there may be more or less be provided such rotor blades.

The rotor blades 11 form a cyclone rotor means, which bears the general reference numeral 10 in Fig. 1, to cause an inserted into the deposition chamber 4 liquid slurry necessarily lead to a circular movement along the inner wall of the housing 1. As a result of the occurring centrifugal forces by the heavier fractions of the slurry near the inner wall of the deposition chamber 4 will accumulate while the lighter fractions move inwardly into the hollow shaft 5 and can be discharged from there to the outside, which will be discussed in more detail later.

As shown in FIG. 1, 2A to 2C show further is secured on top of the mounting plate 12, a plurality of rotor blades 21 of the hollow shaft 5, starting substantially spiral radially outwardly to a location at a distance D from the center longitudinal axis of the hollow shaft 5 extend, the large than the diameter d of a circular arc or described by the outer ends of the rotor blades 11 of the cyclone rotor means 10 of the radial dimension of the separation chamber 4. The rotor blades 21 may, as shown, to extend a suitable short dimension on the outer peripheral edge of the mounting plate 12th Preferably, the ratio is D: d between about 1.25: 1 to 1.75: 1, most preferably at about 1.50: 1st

The rotor blades 21 are part of a transport rotor means for supporting 1 the general reference numeral 20 in Fig. And cooperates with a stator 22, which is shown in more details in Fig. 3.

The stator 22 includes a plurality of stationary vanes 23 which extend in a radial plane below the plane of the rotor vanes 21 of the transport rotor means 20, preferably a spiral, from a radially outer point entprechend the dimension D in Fig. 2A at a radially inner location, which substantially coincides with the inner periphery of the housing. 1 The guide elements 23 are preferably aligned with their inner end portions substantially tangent to the inner circumference of the housing. 1 Between adjacent vanes 23 passages 24 are defined through which the slurry can pass into the deposition chamber. 4 The guide elements 23 of the stator 22 project as the rotor blades 21 of the rotor transportation device 20 outside beyond the peripheral edge of the mounting plate 12 also, so that a fluid connection is created between the stator 22 and the rotor transportation device 20th As shown in Fig. 1 further shows, the radially outer regions of the rotor blades 21 of the transport rotor 20 and the vanes 23 of the stator are housed 22 in a flanschtörmigen chamber 25 which is formed in a cylinder disposed above the housing 1 attachment housing, which bears the general reference numeral 6 ,

The stator 22 has the function of a rotational speed of the pulp, caused by the transport rotor means 20 to decelerate, so that the slurry is pressurized to a pressure before it enters tangentially via the passages 24 into the separation chamber 4 and in the sphere of influence of the cyclone rotor means 10 where her a circular motion is imposed by the cyclone rotor means 10th The rotational speed of the pulp in the deposition chamber 4 is influenced by the effective area and rotational speed of the rotor blades 11 of the rotor cyclone device 10, the flow rate and through the tangential entry of the slurry into the deposition chamber. 4

In the above embodiment, the cyclone rotor means 10 and transport rotor means 20 are mounted on the same hollow shaft 5 as the drive shaft so that they rotate at the same speed. If desired, separate drive shafts for the cyclone rotor means 10 and transport rotor means 20 could be provided to run it at different speeds.

The slurry is, as Fig. 1 shows, inserted over a Einlasstutzen 30 in a hall 31 of the top housing 6, which is in communication with the transport means 20 rotor.

The lighter by the action of the cyclone rotor means - 10 -

10 deposited fractions of the slurry are caused by the system established by the transport rotor means 20 pressure drop to a flow into the hollow shaft 5 and leave the hollow shaft 5 through a plurality of openings 9, which are formed near the upper end of the hollow shaft. 5 From there, they pass into a vestibule exit side 32 in the Aufsatzgehause 6, which surrounds the hollow shaft 5 and is in communication with an outlet connection 33rd

In the illustrated embodiment of the invention, the pulp enters at substantially the same radial level in the centrifugal separator, at which it leaves this, as shown in FIG. 1. However, the inputs and OUTLET FITTING might as will be explained later, also lie on different radial planes.

The separated heavier components of the slurry accumulate consecutive gravity in the funnel-shaped bottom portion

2 of the housing 1 and can from there through the dispensing opening

3 are discharged continuously or at appropriate time intervals to the outside. Preferably, the extraction opening 3 has an adjustable opening width.

Fig. 4 shows a modified simplified embodiment of a centrifugal separator according to the invention especially suitable for the treatment of pulps with easily separable impurity proportions. Same or similar components as the embodiment described above bear the same reference numerals increased by the number one hundred. This c embodiment differs from the preceding described essentially in that the cyclone rotor means is omitted, and hence the circular movement is made solely on the basis of the tangential introduction of the slurry into the deposition chamber 104 and the excess pressure, through the upstream of the inlet angordneten transport rotor means 120 and stator 122 is applied.

As shown, the transport rotor assembly 120 has a modified embodiment by the rotor blades 121 extend only to the outer periphery of the mounting plate 112 so that aussenumfanglich the mounting plate 112, an annular space is defined 126 in Aufsatzgehause 106, in which the slurry under the action of the transport rotor means 120 can flow to reach the area of ​​influence of the stator 122nd It has been found that an improvement in the efficiency of Transportrotor- / Statoreinrichtungen 120, 122 can be achieved by these measures. If desired, such a modified transport rotor means could also be provided in the embodiment of the invention of Fig. 1

Further, the cylindrical portion of the housing 101 is reduced as compared to the embodiment described above to a suitable degree and the taper extending to the outlet opening section 103 extended 102 accordingly. With respect to further details of construction may be made to FIGS. 1 through 3 and the accompanying description.

In the following, especially lower for the flotation fine separation of prefiltered slurries or sludges with remaining after the prefiltration residual fraction of foreign materials dimension, for example, are 2 mm or less, suitable reference is made to embodiments of centrifugal separators according to the invention.

Fig. 5 shows an embodiment of a flotation centrifugal separator that in terms of the structure of feeding means for feeding the slurry consisting of the insertion support 230 and the antechamber 231, the upstream of the inlet arranged in the deposition chamber 205 transport rotor assembly 220 stator assembly 222 to the upstream pressure of the may become turbid and the cyclone rotor 210 substantially corresponds to the embodiment of FIG. 1 so that refers to this. Same or similar components as the embodiment described above bear the same reference numerals increased by the number two hundred.

As shown, the transport rotor assembly 220 and the cyclone rotor means 210 are arranged on a common drive shaft 254 which is not the same time serves for the discharge of a deposited share slurry to be treated. Further, the effective area of ​​the rotor blades 211 of the cyclone rotor means 210 may be compared with the embodiment of FIG. 1 is reduced by the axial dimensions of the rotor blades are reduced.

As shown, the housing 201 has a continuous cylindrical configuration, so that a likewise cylindrical throughout the deposition chamber is formed 204th A ground 252 of the housing 201 axially passing through the end tubular member 255 having open ends projecting into the interior of the deposition chamber 204 so that an open end of the tubular member 255 at a suitable distance from the bottom 252 of the housing 201 comes to rest, while the other open end is arranged outside of the housing two hundred and first Preferably, the; nrformige member 255 relative to the housing 201 held axially versc ebbar. The rohrformige member 255 serves to Abfunr the deposited using the method described below flotation separation fine foreign material content of the pulp. The purified from the contaminants of liquid or clarified effluent may be discharged via a OUTLET FITTING 253 which opens near the bottom 252 of the housing 201 tangentially into the deposition chamber 204th

At an intermediate axial location of the housing 201, a means for introducing one, a suitable gas such as air, containing liquid is provided into the deposition chamber 204th The device comprises an annular distribution manifold 256 which surrounds a peripheral area of ​​the housing 201, in which the housing wall of perforations 257 is penetrated. In the distribution line 256 also opens a Einlasstutzen 258. The liquid with the gas, therefore, the perforations can be directed into the interior of the deposition chamber 204 257 256 and the Einlasstutzen 258, the distribution line.

The liquid is preferably one in which the gas in the form of micro-bubbles with a dimension of for example 100 microns or less distributed. Such micro-bubbles of gas permeated liquids, for example can be provided with a device, which bears the reference numeral 259 in Fig. 5 and may be formed according to DE-A-3733583, on which, therefore reference may be made. The device 259 is connected to a gassing vessel 260 into which the liquid to be gassed, and a suitable gas can be separately introduced and pressurized.

As the liquid water can be used. They may be also, as shown, to act a branched part of the discharged through the OUTLET FITTING 253 clear run by being passed through a pump 261 in the gassing vessel 260, loaded there with the gas and introduced into the apparatus 259 for producing the microbubbles ,

In the deposition chamber 204 to the introduced in the manner described in the pulp microbubbles connect due to its surface tension with the fine floatable foreign matter content of the slurry, which therefore accumulate under the applied centrifugal preferably close to the center longitudinal axis of the centrifugal separator. The microbubbles with the adhering foreign matter content can be discharged from the deposition chamber 204, therefore, on the central tubular member 255, while the clarified effluent can be taken from OUTLET FITTING 253rd

it should be noted that instead of a permeated with micro bubbles of gas liquid, the gas could also be introduced directly into the deposition chamber 204 to produce in the pulp gas bubbles. In order to provide gas bubbles with the smallest possible dimensions, the introduction of the gases through a diffuser ring should (not shown) be made from a fine-grain sintered metal, which would provide in place of the distribution line 256th

Further, the cyclone rotor means could be omitted 210 so that the circular motion of the slurry, similarly to the embodiment of FIG. 4 alone is based on the pressure-increasing effect of the cooperating Transportrotor- and Statoreinrichtungen 220, 222 as well as the tangential introduction of the slurry into the deposition chamber 204 would ,

Further, the discharge of the microbubbles could be performed 1 and 4 through a central hollow shaft against the force of gravity with adhering thereto foreign matter in a manner similar to the embodiments of the invention shown in Fig., Which would at the same time represent the common axis of rotation Transportrotoreinrichung 220 and cyclone rotor 210.

Fig. 6 shows a flotation centrifugal separator according to a fourth embodiment of the invention. The same or similar components as in the above embodiments have the same reference numerals increased by the number three hundred. The fourth embodiment of the invention comprises a continuous cylindrical housing 301 which defines a cylindrical deposition chamber also 304th Upstream of an inlet into the deposition chamber 304, a transport rotor assembly 320 and a cooperating stator 322 are for pressurizing the slurry provided, whose construction and operation to that of the embodiment of FIG. 1 correspond, so that a description thereof is omitted. Similar to the embodiment of FIG. 4 is a cyclone rotor means is omitted.

A feature of the centrifugal separator of FIG. 6 is a foam destruction device, which bears the general reference numeral 370. The foam destruction device 370 includes a plurality of, about a central axis, which preferably coincides with the axis of rotation of the rotor blades 321 of the transport rotor means 320, rotatable rotor blades 371, which are disposed in a space 372 in a cylinder disposed above the separation housing 301 Aufsatzgehause 306th The space 372 is above a transport rotor assembly 320 and stator 322 disposed in the containing space 373 Aufsatzgehause 369, in which the pulp to be treated may be introduced through a Einlasstutzen 374th In particular, over the 374 Einlasstutzen a slurry are dispersed in the micro gas bubbles are introduced. The Mirkrogasblasen can, as indicated at 359, are introduced by means of a device in the pulp, as described in connection with the embodiment according to Fig. 5.

The spaces 372 and 373 in Aufsatzgehause 369 are sealed against each other, and further, the upper space 372 into a lower, the rotor blades 371 of the foam destruction device 370 containing the area 372 'and an upper portion 372' 'is divided, the lower near the hollow shaft 305 with the portion 372 'is in fluid communication. In the lower portion 372 'opens a Fremdstoffauslasstutzen 376. The peripheral wall of the attachment housing 369 is formed along the upper portion 372' 'through which a plurality of peripherally distributed perforations 377, which connect the interior of the upper portion 372' 'with a Gasauslasstutzen 378 in order of to dissipate away the deposited contaminants gaseous components to the outside.

The rotor blades 371 of the foam destruction device 370 may, as mentioned, be mounted on the same axis of rotation as the rotor blades 321 of the transport rotor means 320th The axis of rotation is formed as a hollow shaft 305 which projects axially into the deposition chamber 304 and has a lower open end into which can deposited adhering to the gas bubbles foreign substances enter from where they rise up inside the hollow shaft 305 and into the space 372 of the foam destruction device 370 and get into the sphere of influence of the rotor blades 371st - 17 -

A near the bottom 379 of the Abseheidungsgehäuses 301 tangentially einmündender OUTLET FITTING 380 serves to dissipate the freed of the impurities liquid components of the pulp or of the clear run.

In the foam destruction means 370, the entered the room 372, adhering to the gas bubbles foreign substances by the rotor blades 371 placed in a circular movement, so that the heavier impurities due to centrifugal effects are separated from the gas bubbles and 'accumulate on the inner circumference of the lower space portion 372 , In contrast, the gas bubbles rise upwards into the upper space portion 372 '', from where they can be discharged in the aforementioned manner to the outside.

Instead of introducing a vorbegasten slurry over the Einlasstutzen 374, a treatment of the pulp in the deposition chamber 304 may also be carried out in the presence of gas bubbles, that the gas separated from the pulp in accordance with the embodiment of FIG. Is introduced into the deposition chamber 304. 5

Further, a cyclone rotor means as in the embodiment of the invention of FIG. 1 could if desired be similarly provided. In this case, the rotor blades in succession 371 of the foam destruction device 370, the rotor blades 321 of the transport rotor assembly 320 and the rotor blades of the added cyclone rotor means for rotation in unison by the driving means 308 would be mounted on the driven hollow shaft 305th However, it is understood that independent drive shafts for driving the said rotor blades can be provided similarly as with the other above-described embodiments of the invention.

Claims

claims
1. A method for separating the heavier aqueous from the lighter fractions pulps by means of centrifugal force, wherein the slurry is caused under the influence of a prevailing between an inlet and outlet of a cyclone separation chamber pressure gradient, to a circular movement in the deposition chamber so that the lighter of the heavier fractions of the slurry to separate and the heavy and lighter fractions are discharged separately from the deposition chamber, characterized in that the pressure differential is applied by a pressure increase stage substantially immediately prior to the intake of the slurry into the deposition chamber.
2. The method according to claim 1, characterized in that the slurry to increase the pressure from a radially inner to a radially outer region accelerated upstream of the inlet into the deposition chamber, is deflected at or decelerated near the radially outer area and a flow towards the inlet becomes.
3. The method of claim 1 or 2, characterized in that the slurry is introduced substantially tangentially into the deposition chamber.
4. The method according to any one of claims 1 to 3, characterized in that additional rotational energy is introduced into the receptacle located in the deposition chamber turbidity.
5. The method according to any one of the preceding claims, characterized in that the deposition is carried out of the pulp in the presence of gas bubbles. - 19 -
6. The method according to claim 5, characterized in that a interspersed with microbubbles liquid is introduced into the deposition chamber for mixing with the slurry.
7. The method according to claim 5, characterized in that the pulp druckbegast, laid with the formation of microbubbles and is inserted in the gasified state in the deposition chamber.
8. centrifugal separator for the separation of the heavier aqueous slurries from the lighter fractions by means of centrifugal force, with a deposition chamber
(4104204304) and a device for generating a pressure difference between an inlet and outlet of the deposition chamber so that the pulp in the deposition chamber is made to a circular motion, means (5,105,255,305) for removing the lighter fractions, and means ( 3,103,253,380) for the discharge of the heavier fractions of the slurry from the deposition chamber, characterized in that for generating a pressure gradient is a about a rotation axis
(5,105,254,305) rotatably driven Transport¬ rotor means (20,120,220,320) in a Aufsatzgehause
(6106206306) is arranged of the separating device, which transport rotor means with an immediately upstream of the inlet of the deposition chamber provided stator means (22,122,222,322) cooperating and a radial dimension (D) which is greater than the radial dimension (d) is the deposition chamber to the turbid put under a pressure substantially immediately before introduction into the deposition chamber.
9. centrifugal separator according to claim 8, characterized is that in the deposition chamber (4,204) is a cyclone rotor means (10,210) for introducing additional rotational energy disposed in the slurry, which is of the same axis of rotation (5,254) as the transport rotor means (20.220) is driven.
10. centrifugal separator according to claim 8 or 9, characterized in that the ratio of the radial dimension (D) of the transport rotor means (20,120,220,320) for the radial dimension (d) of the deposition chamber (4,104,204,304) is between about 1.25: 1 and 1.75: 1 lies.
11. centrifugal separator according to claim 8, characterized by means (256 to 261.359) for introducing gas bubbles into the deposition chamber (204.304).
12, centrifugal separation apparatus according to claim 11, characterized in that said means (256 to 261.359) for introducing gas bubbles a gassing vessel (260) for introducing a gas into a liquid and in fluid communication with the gasification expansion device (259.359) for generating microbubbles included in the fumigated liquid.
13, centrifugal separation apparatus according to claim 11 or 12, characterized by a Aufsatzgehause (306) with axial distance to the transport rotor means (320) arranged foam destruction device (370) with a rotatably driven rotor blades (371) for separation by centrifugal force from adhering to the gas bubbles foreign substances in one of the deposition chamber (304) discharged frothy gas bubbles impurity mixture.
14, centrifugal separation apparatus according to claim 13, characterized in that the rotor blades (371) of the foam destruction device (370) and which are driven transport rotor means (320) from the same axis of rotation (305).
PCT/EP1997/001913 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 WO1997040944A1 (en)

Priority Applications (6)

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

Applications Claiming Priority (7)

Application Number Priority Date Filing Date Title
AT97919374T AT203431T (en) 1996-04-25 1997-04-17 Apparatus for separating the heavier fractions from the lighter aqueous turbid by means of centrifugal force
JP53851197A 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
AU23873/97A AU2387397A (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
DE1997504134 DE59704134D1 (en) 1996-04-25 1997-04-17 Apparatus for separating the heavier fractions of the lighter aqueous turbid by means of centrifugal force
EP19970919374 EP0904156B1 (en) 1996-04-25 1997-04-17 Apparatus for the separation of heavier from lighter fractions in aqueous slurries by means of centrifugal force
US09/177,597 US6036871A (en) 1996-04-25 1998-10-23 Method and device for separating heavier from lighter parts of aqueous slurries by means of centrifugal force effects
HK99104026A HK1018889A1 (en) 1996-04-25 1999-09-17 Apparatus for the separation of heavier from lighter fractions in aqueous slurries by means of centrifugal force

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US09/177,597 Continuation US6036871A (en) 1996-04-25 1998-10-23 Method and device for separating heavier from lighter parts of aqueous slurries by means of centrifugal force effects

Publications (1)

Publication Number Publication Date
WO1997040944A1 true WO1997040944A1 (en) 1997-11-06

Family

ID=27216180

Family Applications (1)

Application Number Title Priority Date Filing Date
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

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)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6669845B2 (en) * 1998-03-13 2003-12-30 Georg Klass Cyclone separator
WO2008101532A1 (en) * 2007-02-21 2008-08-28 Holger Blum Hydro cyclone device and hydro cyclone installation
GB2461874A (en) * 2008-07-14 2010-01-20 Caltec Ltd Separation system and method
US7980002B2 (en) 2004-11-16 2011-07-19 Röhren-und Pumpenwerk Bauer Gesellschaft mbH Rotary drum for the aerobic heating of pourable solids

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102005009683B4 (en) * 2005-03-03 2016-08-18 Fan Separator Gmbh Process for the recovery of solids
JP4775913B2 (en) * 2007-07-13 2011-09-21 ミスズテクノ株式会社 Cyclone filter
JP6604601B2 (en) * 2014-06-05 2019-11-13 永進テクノ株式会社 Cyclone separator

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2701642A (en) * 1951-04-11 1955-02-08 Goodwin Norris Continuous centrifugal separator
US2996187A (en) * 1961-08-15 payne
US4397741A (en) * 1980-08-29 1983-08-09 University Of Utah Apparatus and method for separating particles from a fluid suspension
DE3390449T1 (en) * 1983-01-28 1985-01-24
EP0186021B1 (en) * 1984-12-14 1990-10-24 Firma AMBERGER KAOLINWERKE GMBH Device for recovering of sand, in particular finest sand
EP0447887A1 (en) * 1990-03-21 1991-09-25 J.M. Voith GmbH Apparatus for the separation of air from flotation turbid liquids

Patent Citations (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
US4397741A (en) * 1980-08-29 1983-08-09 University Of Utah Apparatus and method for separating particles from a fluid suspension
DE3390449T1 (en) * 1983-01-28 1985-01-24
EP0186021B1 (en) * 1984-12-14 1990-10-24 Firma AMBERGER KAOLINWERKE GMBH Device for recovering of sand, in particular finest sand
EP0447887A1 (en) * 1990-03-21 1991-09-25 J.M. Voith GmbH Apparatus for the separation of air from flotation turbid liquids

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6669845B2 (en) * 1998-03-13 2003-12-30 Georg Klass Cyclone separator
US7980002B2 (en) 2004-11-16 2011-07-19 Röhren-und Pumpenwerk Bauer Gesellschaft mbH Rotary drum for the aerobic heating of pourable solids
WO2008101532A1 (en) * 2007-02-21 2008-08-28 Holger Blum Hydro cyclone device and hydro cyclone installation
GB2461874A (en) * 2008-07-14 2010-01-20 Caltec Ltd Separation system and method
GB2461874B (en) * 2008-07-14 2012-11-21 Caltec Ltd Separation system and method
US9073064B2 (en) 2008-07-14 2015-07-07 Caltec Limited Cyclonic separation system comprising gas injection means and method for separating a fluid mixture

Also Published As

Publication number Publication date
JP4047386B2 (en) 2008-02-13
ES2162280T3 (en) 2001-12-16
AT203431T (en) 2001-08-15
EP0904156A1 (en) 1999-03-31
HK1018889A1 (en) 2002-03-22
JP2000508968A (en) 2000-07-18
EP0904156B1 (en) 2001-07-25
AU2387397A (en) 1997-11-19

Similar Documents

Publication Publication Date Title
US3439810A (en) Centrifugal separator
US5534118A (en) Rotary vacuum distillation and desalination apparatus
US5277803A (en) Water clarification method and apparatus
EP0462852B1 (en) Process and apparatus for the separation of a continuous fluid phase and a disperse phase and their application
JP5314826B2 (en) How to clean crankcase gas
US20090159523A1 (en) Rotary annular crossflow filter, degasser, and sludge thickener
AU679853B2 (en) Attrition mill
US5094674A (en) Device for separation of air from flotation slush
CA1185708A (en) Froth flotation apparatus and method
US5062955A (en) Rotating sleeve hydrocyclone
US4528091A (en) Particle classifier
FI114382B (en) Central vacuum cleaner dust extraction method and arrangement
US4280902A (en) Separation of dense impurities from a fluid
US5229014A (en) High efficiency centrifugal separation apparatus and method using impeller
CN1569302B (en) Methods for centrifugally separating mixture and centrifugal separators
EP0491926A1 (en) Orbital separator and method of orbitally separating a mixture
US7025890B2 (en) Dual stage centrifugal liquid-solids separator
JP2882880B2 (en) Circular grit traps, apparatus for performing a central supply tank, such as a coarse classifier or settling tank of circular structures, methods and methods of use thereof
US4094794A (en) Hydrocyclone
US20070163215A1 (en) Centrifugal separator for cleaning gases
US3516551A (en) Cyclone separator
CA2203108A1 (en) Method and equipment for the purification of a liquid
CN101707916B (en) Multi-cyclone sediment filter
JPH09502218A (en) Liquid / solid separation
US7314441B2 (en) Method for separating particulate matter from a fluid stream

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AL AM AU AZ BA BB BG BR BY CA CN CU CZ EE GE HU IL IS JP KE KG KP KR KZ LC LK LR LS LT LV MD MG MK MN MW MX NO NZ PL RO RU SD SG SI SK TJ TM TR TT UA UG US UZ VN AM AZ BY KG KZ MD RU TJ TM

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH KE LS MW SD SZ UG AT BE CH DE DK ES FI FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN ML MR NE SN TD

DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
121 Ep: the epo has been informed by wipo that ep was designated in this application
WWE Wipo information: entry into national phase

Ref document number: 1997919374

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 09177597

Country of ref document: US

WWP Wipo information: published in national office

Ref document number: 1997919374

Country of ref document: EP

NENP Non-entry into the national phase in:

Ref country code: CA

WWG Wipo information: grant in national office

Ref document number: 1997919374

Country of ref document: EP