EP1432502A1 - Flocculation apparatus and method for treating colloidal suspensions - Google Patents

Flocculation apparatus and method for treating colloidal suspensions

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Publication number
EP1432502A1
EP1432502A1 EP02779131A EP02779131A EP1432502A1 EP 1432502 A1 EP1432502 A1 EP 1432502A1 EP 02779131 A EP02779131 A EP 02779131A EP 02779131 A EP02779131 A EP 02779131A EP 1432502 A1 EP1432502 A1 EP 1432502A1
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EP
European Patent Office
Prior art keywords
outer housing
inner cone
suspension
cone
flocculation
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.)
Granted
Application number
EP02779131A
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German (de)
French (fr)
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EP1432502B1 (en
Inventor
Christian Schröder
Michael Sievers
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Clausthaler Umwelttechnik Institut CUTEC
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Clausthaler Umwelttechnik Institut CUTEC
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Publication of EP1432502A1 publication Critical patent/EP1432502A1/en
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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/27—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices
    • B01F27/272—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices with means for moving the materials to be mixed axially between the surfaces of the rotor and the stator, e.g. the stator rotor system formed by conical or cylindrical surfaces
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION 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
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D3/00—Differential sedimentation
    • B03D3/06—Flocculation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/27—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices
    • B01F27/272—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices with means for moving the materials to be mixed axially between the surfaces of the rotor and the stator, e.g. the stator rotor system formed by conical or cylindrical surfaces
    • B01F27/2723—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices with means for moving the materials to be mixed axially between the surfaces of the rotor and the stator, e.g. the stator rotor system formed by conical or cylindrical surfaces the surfaces having a conical shape
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/27—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices
    • B01F27/272—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices with means for moving the materials to be mixed axially between the surfaces of the rotor and the stator, e.g. the stator rotor system formed by conical or cylindrical surfaces
    • B01F27/2724—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices with means for moving the materials to be mixed axially between the surfaces of the rotor and the stator, e.g. the stator rotor system formed by conical or cylindrical surfaces the relative position of the stator and the rotor, gap in between or gap with the walls being adjustable

Definitions

  • the invention relates to a flocculation apparatus for conditioning colloidal suspensions with a suspension inlet, a suspension outlet and with an inner cone, which is mounted centrally in a conical outer housing, the inner cone and / or the outer housing being rotatable relative to one another and a gap space between the inner cone and the outer housing for the flow of suspensions.
  • the suspension is conventionally mixed with a flocculant and / or flocculant and mechanically processed in a flocculent.
  • the flocculation itself is in one
  • the .5 rapid mixer unit carried out so that the flakes are formed.
  • the flakes are shaped in a flake apparatus, the resulting flakes being pelletized and rounded off by shear forces and flake erosion, so that the desired property of the flakes, e.g. B. Improve the drainage capacity or thickening again
  • the flocculant and / or flocculant! 5 is dispersed in a suspension by turbulent flow movements.
  • the formation and adsorption reaction times of the flocculation chemicals are very short and it is important to ensure that the substances are mixed in homogeneously in order to optimize the flocculation results.
  • the flocculants and / or flocculants are conventionally mixed in with stirred tanks or with tube reactors with plug flow, such as injection mixers, inline turbo mixers and pumps.
  • the sewage sludge flow runs from the top of the cone base down to the cone tip, with flocculants being inserted into the cone gap space of the pelletizing reactor.
  • the conical pelleting zone the flake pellets roll in a circle on the pelleting surface.
  • the conditioning process is controlled by a cone stirrer to generate a circulation flow.
  • the essential parameters such as particle size distribution, porosity or the specific surface of the sewage sludge, are set reproducibly.
  • the object of the invention was therefore to create a flocculation apparatus which can be variably adapted to the ambient conditions.
  • the object is achieved with the generic flocculation apparatus in the form of a cone stirrer in that the inner cone and / or outer housing is axially displaceably mounted and an actuator for controlled axial displacement of the inner cone and / or outer housing is operatively connected to the inner cone and / or outer housing.
  • the reaction volume in the flocculation apparatus is thus variable and can be adapted to the ambient conditions. Due to the axial displacement of the inner cone and / or outer housing, the gap width of the flow space between the inner cone and the outer housing can be easily adjusted. As a result, both the dwell time at different volume flows can be kept constant and the flow regime can be adapted to changing mass flows.
  • the suspension inlet is preferably in the area of the cone base of the inner cone and outer housing and the suspension outlet is in the area of the cone tip of the inner cone and outer housing.
  • the suspension flow preferably runs from the cone base to the cone tip. It has been found that the flocculation results are reproducible and optimal with such a flow direction.
  • the surface of the inner cone and / or the inner surface of the outer housing should be profiled, for example, by milled longitudinal grooves. As a result, the flow is implemented faster.
  • the axis of rotation of the inner cone is preferably approximately perpendicular, the suspension inlet being arranged above the suspension outlet. In this way, a natural suspension flow is forced from top to bottom.
  • the angle of inclination of the inner cone should be relatively small and should be about 2 to 30 degrees.
  • conventional cone stirrers have an inclination angle of 35 degrees and cylinder stirrers have an angle of 0 degrees. It was recognized that optimal reproducible and controllable flocculation results can be achieved with a small inclination angle.
  • a mixer for generating a highly turbulent suspension flow is preferably arranged immediately before the inlet of the suspension.
  • the mixer is preferably integrated with the flocculation apparatus in one device.
  • the conditioning of colloidal suspensions such as e.g. B. sewage sludge, with the flocculation apparatus according to the invention is preferably carried out by:
  • the speed of the inner cone and / or outer housing can be regulated as a function of a flake size distribution.
  • FIG. 1 sectional view of the flocculating apparatus with axially displaceable inner cone
  • Figure 2 - sectional view of a rapid mixer for generating a highly turbulent suspension flow.
  • FIG. 1 shows the flocculation apparatus 1 according to the invention in a sectional view.
  • the flocculation apparatus 1 essentially consists of a conical outer housing 2 and an inner cone 3, which is arranged centrally in the outer housing 2.
  • the inner cone 3 is rotatably mounted on a driven shaft 4.
  • a suspension stream is introduced into the flocculation apparatus 1 through a suspension inlet 5 in the region of the cone base of the inner cone 3.
  • the suspension then flows together with the flocculant and / or flocculant in the gap between the inner cone 3 and the outer housing 2 in the axial direction from the cone base to the cone tip and flows out through a suspension outlet 6 in the region of the cone tip.
  • the angle of inclination of the inner cone 3 and correspondingly the angle of inclination of the outer housing 2 is relatively small and is in the range of approximately 2 to 30 degrees. Since the radii of the inner cone 3 for the suspensions through which flow flows change during the flow, the centrifugal forces generated are not constant due to the changing circumferential speed along the driven shaft 4. In contrast to cylindrical stirrers, the flow conditions are not uniform over the length of the circular or conical gap. If the flocculation apparatus 1 is flowed through by the cone base of the inner cone 3 in the direction of the truncated cone tip, the suspension is initially subjected to greater shear forces when entering the cone base, since the basic flow is greatest there due to the higher peripheral speed. The shear forces decrease continuously in the direction of the decreasing radii of the inner cone 3, so that flake structures that have already been formed are not or only barely destroyed later.
  • the outer housing 2 is considerably longer than the inner cone 3, so that the inner cone 3 is axially displaceable in a wide range.
  • the flocculation apparatus 1 can also be constructed in such a way that the outer housing 2 can be displaced axially relative to the inner cone 3. It is also conceivable that the outer housing 2 can be rotated.
  • the axial displacement of the inner cone 3 relative to the outer housing 2 means that the gap width between the inner cone 3 and the outer housing 2 can be variably adjusted.
  • the axial displacement can be implemented, for example, with a spindle stroke drive as an actuator, which interacts with the shaft 4.
  • the motor shaft of a drive motor is fixedly connected to a guide sleeve which is operatively connected to the shaft 4 by means of a feather key connection, so that the shaft 4 can be displaced axially relative to the motor shaft.
  • the shaft 4 is preferably mounted in an angular contact ball bearing 7, the bearing housing preferably being square in order to guide it in the groove of a guide rail. This ensures that after the coupling by the angular contact ball bearing 7, there is no longer any rotation which could act on the spindle lifting drive.
  • FIG. 2 shows a rapid mixer 8 with a suspension inlet 9 and a suspension outlet 10.
  • the suspension outlet 10 is immediately in front the suspension inlet 5 of the flocculation apparatus 1 switched.
  • the rapid mixer 8 has a main rotor 11 through which the outside flows inwards, which is equipped with employed, blade-shaped blades which carry the suspension in the conveying direction.
  • the flocculant and / or flocculant is fed to the rapid mixer 8 via four nozzles 12 distributed over the circumference.
  • the medium After mixing in the main rotor 1 1, the medium enters an intermediate stator 13, the jacket of which is extended beyond the area of the main rotor 1 1 to reduce wear.
  • An auxiliary rotor 14 is provided in the flow direction behind the stator 1 3. This arrangement of series-connected main rotor 1 1, stator 1 3 and auxiliary rotor 14 ensures homogeneous mixing of the medium within a certain dwell time.
  • the rotor speed should be continuously adjustable up to about 2800 N / min.
  • the conditioning process can be regulated with four different degrees of freedom with the aid of the arrangement of a rapid mixer 8 connected in series and a flocculation apparatus 1.
  • the flocculant and / or flocculant is mixed homogeneously in the rapid mixer and total flocculation of the suspension is carried out.
  • the amount of flocculant and / or flocculant introduced and the amount of mixing energy can be variably adjusted by adjusting the speed of the rapid mixer 8.
  • the flocculation device discretizes the flocculation.
  • the different sized aggregates of the total flocculation are eroded, reflocculated, compacted and evened out by shear stress.
  • the speed and the reaction volume of the apparatus can be changed in the flocculating apparatus 1.
  • the flakes can be exposed to an adapted shear force regime over a wide range.
  • the setting of the rapid mixer 8 and of the flocculation apparatus 1 is thus dependent on the volume flow and in particular the size of the flakes and the size of the flakes.
  • the flake size and the flake size distribution have namely z.
  • the rapid mixer 8 is now regulated so that the flocculant and / or flocculant is mixed homogeneously and completely with the suspension. Sufficient energy must flow into the suspension flocculant and / or flocculant mixture so that each suspension particle has the possibility of combining with flocculant and / or flocculant. On the other hand, only so much energy may be used that the flakes are not destroyed again during or immediately after their formation. For this purpose, the speed must be set accordingly in a known and scientifically investigated manner.
  • the speed and the gap width between the inner cone 3 and the outer housing 2 are varied in the flocculating apparatus 1.
  • the change in gap width causes both a change in volume and thus a change in the axial parameters such as dwell time, axial speed, axial Reynolds number and axial camp number, as well as a change in the radius ratio and thus a change in the Taylor and rotational camp number.
  • the flow conditions can thus be variably adjusted over a wide range.
  • the flake size distribution is preferably optically determined and the rapid mixer 8 and the flocculation apparatus 1 are regulated such that an optimal flake size distribution results. This enables conditioning in a closed, self-adapting control system.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)
  • Mixers Of The Rotary Stirring Type (AREA)
  • Diaphragms For Electromechanical Transducers (AREA)
  • Polarising Elements (AREA)
  • Application Of Or Painting With Fluid Materials (AREA)

Abstract

A flocculation apparatus and method for treating colloidal suspensions. The apparatus includes a suspension inlet, a suspension outlet and an inner cone mounted centrally in a conical outer housing. The inner cone and/or the outer housing is rotatable relative to one another and a gap for through-flow of suspensions is present between the inner cone and the outer housing. In the method, continuously measuring a flock size distribution of a suspension stream passed into the flocculation apparatus is provided. Additionally provided is axially displacing the inner cone and/or outer housing as a function of the flock size distribution and the suspension volume flow rate.

Description

Flockungsapparat und Verfahren zur Konditionierung von kolloidalen Suspensionen Flocculation apparatus and method for conditioning colloidal suspensions
Die Erfindung betrifft einen Flockungsapparat zur Konditionierung von kolloidalen Suspensionen mit einem Suspensionseinlauf, einem Suspensionsauslauf und mit einem Innenkegel, der zentrisch in einem kegelförmigen Außengehäuse gelagert ist, wobei der Innenkegel und/oder das Außengehäuse relativ zueinander rotierbar und zwischen dem Innenkegel und dem Außengehäuse ein Spaltraum zur Durchströmung mit Suspensionen ist.The invention relates to a flocculation apparatus for conditioning colloidal suspensions with a suspension inlet, a suspension outlet and with an inner cone, which is mounted centrally in a conical outer housing, the inner cone and / or the outer housing being rotatable relative to one another and a gap space between the inner cone and the outer housing for the flow of suspensions.
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Zur Verbesserung von spezifischen Eigenschaften einer Suspension, z. B. der Entwässerbarkeit oder Eindickfähigkeit, wird die Suspension herkömmlicherweise mit einem Flockungsmittel und/oder Flockungshilfsmittel versetzt und in einem Flockungsapparat mechanisch aufbereitet. Die Flockung selbst wird in einerTo improve specific properties of a suspension, e.g. B. the drainability or thickening ability, the suspension is conventionally mixed with a flocculant and / or flocculant and mechanically processed in a flocculent. The flocculation itself is in one
.5 Rapid-Mischer-Einheit durchgeführt, so dass die Flocken entstehen. Die Ausformung der Flocken erfolgt in einem Flockenapparat, wobei durch Scherkräfte und Flockenerosion die entstandenen Flocken pelletiert und abgerundet werden, so dass sich die gewünschte Eigenschaft der Flocken, z. B. Erhöhung der Entwässerungsfähigkeit oder Eindickung nochmals verbessern.5 rapid mixer unit carried out so that the flakes are formed. The flakes are shaped in a flake apparatus, the resulting flakes being pelletized and rounded off by shear forces and flake erosion, so that the desired property of the flakes, e.g. B. Improve the drainage capacity or thickening again
! 0 kann. Allerdings dürfen die Scherkräfte nicht zu groß sein, weil dann die Flocken dann wieder zerstört werden und sich die spezifischen Flockeneigenschaften verschlechtern können.! 0 can. However, the shear forces must not be too great, because then the flakes can be destroyed again and the specific flake properties can deteriorate.
Mit dem Rapid-Mischer wird das Flockungsmittel und/oder Flockungshilfsmittel !5 in eine Suspension durch turbulente Strömungsbewegungen dispergiert. Dabei sind die Formations- und Adsorptionsreaktionszeiten der Flockungschemikalien sehr kurz und es ist zur Optimierung der Flockenbildungsergebnisse auf eine homogene Einmischung der Substanzen zu achten.With the rapid mixer, the flocculant and / or flocculant! 5 is dispersed in a suspension by turbulent flow movements. there the formation and adsorption reaction times of the flocculation chemicals are very short and it is important to ensure that the substances are mixed in homogeneously in order to optimize the flocculation results.
Die Einmischung von Flockungsmitteln und/oder Flockungshilfsmitteln erfolgt herkömmlicherweise mit Rührkesseln oder mit Rohrreaktoren mit Pfropfenströmung, wie zum Beispiel Injektions-Mischern, Inlineturbo-Mischern und Pumpen.The flocculants and / or flocculants are conventionally mixed in with stirred tanks or with tube reactors with plug flow, such as injection mixers, inline turbo mixers and pumps.
Von M. Reiter, M. Schmidt und U. Wiesmann: Der durchströmte Zylinderrührer im Bereich der wirbelbehafteten Strömung - ein Apparat mit interessanten Eigenschaften, V. T.- Verfahrenstechnik 14 ( 1 980) Nr. 9, Seiten 578 bis 582 wurde die Flockenbildung mit einem Zylinderrührer untersucht. Dieser besteht aus zwei koaxialen Zylindern, von denen entweder der innere, der äußere oder beide Zylinder mit unterschiedlicher Drehzahl gleichläufig oder gegenläufig rotieren. Dabei wurde festgestellt, dass die optimale Energieeintragszahl abhängig von der Verweilzeit im Zylinderrührer ist.By M. Reiter, M. Schmidt and U. Wiesmann: The flow through the cylinder stirrer in the area of the vortex-affected flow - an apparatus with interesting properties, VT process engineering 14 (1 980) No. 9, pages 578 to 582, the flocculation with a cylinder stirrer examined. This consists of two coaxial cylinders, of which either the inner, the outer or both cylinders rotate in opposite or opposite directions at different speeds. It was found that the optimal energy input depends on the dwell time in the cylinder stirrer.
In A. Hemme, R. Polte, P. Ay: Peletierungsflockung - die Alternative zur herkömmlichen Schlammkonditionierung in Aufbereitungs-Technik 36 ( 1 995) Nr. 5, Seiten 2226 bis 235 ist die Schlammkonditionierung mit einem kegelförmigen Pelletierungsapparat beschrieben. Der Klärschlammstrom verläuft von oben von der Kegelbasis nach unten zur Kegelspitze, wobei Flockungshilfsmittel in den Kegelspaltraum des Pelletierungsreaktors eingefügt wird. In der konischen Pelletierzone rollen die Flocken-Pellets kreisend auf der Pelletierfläche ab. Hierbei werden nur die mechanisch stabilen Pellets mit einer bestimmten Größe und Festigkeit ausgetragen. Der Konditionierprozess wird durch einen Kegelrührer zur Erzeugung einer Zirkulationsströmung gesteuert. Für die optimale Konditionierung von Klärschlämmen wechselnder Qualität und Zusammensetzung unter Berücksichtigung sonstiger Verfahrensparameter ist es erforderlich, dass die wesentlichen Parameter, wie zum Beispiel Partikelgrößenverteilung, Porosität oder die spezifische Oberfläche des Klärschlamms reproduzierbar eingestellt wird.A. Hemme, R. Polte, P. Ay: Peletization Flocculation - the alternative to conventional sludge conditioning in treatment technology 36 (1 995) No. 5, pages 2226 to 235 describes sludge conditioning with a conical pelletizer. The sewage sludge flow runs from the top of the cone base down to the cone tip, with flocculants being inserted into the cone gap space of the pelletizing reactor. In the conical pelleting zone, the flake pellets roll in a circle on the pelleting surface. Here only the mechanically stable pellets with a certain size and strength are discharged. The conditioning process is controlled by a cone stirrer to generate a circulation flow. For the optimal conditioning of sewage sludge of varying quality and composition, taking into account other process parameters, it is necessary that the essential parameters, such as particle size distribution, porosity or the specific surface of the sewage sludge, are set reproducibly.
Aufgabe der Erfindung war es daher, einen Flockungsapparat zu schaffen, der variabel an die Umgebungsbedingungen angepasst werden kann.The object of the invention was therefore to create a flocculation apparatus which can be variably adapted to the ambient conditions.
Die Aufgabe wird mit dem gattungsgemäßen Flockungsapparat in Form eines Kegelrührers dadurch gelöst, dass der Innenkegel und/oder Außengehäuse axial verschiebbar gelagert ist und ein Aktuator zur gesteuerten axialen Verschiebung des Innenkegels und/oder Außengehäuses in Wirkverbindung mit dem Innenkegel und/oder Außengehäuse steht.The object is achieved with the generic flocculation apparatus in the form of a cone stirrer in that the inner cone and / or outer housing is axially displaceably mounted and an actuator for controlled axial displacement of the inner cone and / or outer housing is operatively connected to the inner cone and / or outer housing.
Damit ist das Reaktionsvolumen in dem Flockungsapparat variabel und kann an die Umgebungsbedingungen angepasst werden. Durch die axiale Verschiebung des Innenkegels und/oder Außengehäuses kann die Spaltweite des Durchflussraums zwischen Innenkegel und Außengehäuse leicht verstellt werden. Hierdurch kann sowohl die Verweilzeit bei unterschiedlichen Volumenströmen konstant gehalten werden, als auch das Strömungsregime an sich ändernde Massenströme angepasst werden.The reaction volume in the flocculation apparatus is thus variable and can be adapted to the ambient conditions. Due to the axial displacement of the inner cone and / or outer housing, the gap width of the flow space between the inner cone and the outer housing can be easily adjusted. As a result, both the dwell time at different volume flows can be kept constant and the flow regime can be adapted to changing mass flows.
Der Suspensionseinlauf befindet sich vorzugsweise im Bereich der Kegelbasis des Innenkegels und Außengehäuses und der Suspensionsauslauf im Bereich der Kegelspitze des Innenkegels und Außengehäuses. Auf diese Weise verläuft der Suspensionsstrom vorzugsweise von der Kegelbasis zur Kegelspitze. Es hat sich herausgestellt, das bei einer solchen Strömungsrichtung die Flockungsergebnisse reproduzierbar und optimal sind. Die Oberfläche des Innenkegels und/oder die Innenfläche des Außengehäuses sollten zum Beispiel durch eingefräste Längsnuten profiliert sein. Hierdurch wird die Strömung schneller umgesetzt.The suspension inlet is preferably in the area of the cone base of the inner cone and outer housing and the suspension outlet is in the area of the cone tip of the inner cone and outer housing. In this way, the suspension flow preferably runs from the cone base to the cone tip. It has been found that the flocculation results are reproducible and optimal with such a flow direction. The surface of the inner cone and / or the inner surface of the outer housing should be profiled, for example, by milled longitudinal grooves. As a result, the flow is implemented faster.
Die Rotationsachse des Innenkegels steht vorzugsweise annähernd senkrecht, wobei der Suspensionseinlauf oberhalb von dem Suspensionsauslauf angeordnet ist. Auf diese Weise wird eine natürliche Suspensionsströmung von oben nach unten erzwungen.The axis of rotation of the inner cone is preferably approximately perpendicular, the suspension inlet being arranged above the suspension outlet. In this way, a natural suspension flow is forced from top to bottom.
Überraschend hat sich herausgestellt, das der Neigungswinkel des Innenkegels relativ gering sein sollte und etwa 2 bis 30 Grad betragen sollte. Im Unterschied hierzu weisen herkömmliche Kegelrührer einen Neigungswinkel von 35 Grad und Zylinderrührer einen Winkel von 0 Grad auf. Es wurde erkannt, das mit einem geringen Neigungswinkel optimale reproduzierbare und steuerbare Flockungsergebnisse erzielt werden können.It has surprisingly been found that the angle of inclination of the inner cone should be relatively small and should be about 2 to 30 degrees. In contrast to this, conventional cone stirrers have an inclination angle of 35 degrees and cylinder stirrers have an angle of 0 degrees. It was recognized that optimal reproducible and controllable flocculation results can be achieved with a small inclination angle.
Unmittelbar vor dem Suspensionseinlauf ist vorzugsweise ein Mischer zur Erzeugung einer hochturbulenten Suspensionsströmung angeordnet. Der Mischer ist hierbei mit dem Flockungsapparat vorzugsweise in einem Gerät integriert.A mixer for generating a highly turbulent suspension flow is preferably arranged immediately before the inlet of the suspension. The mixer is preferably integrated with the flocculation apparatus in one device.
Die Konditionierung von kolloidalen Suspensionen, wie z. B. Klärschlamm, mit dem erfindungsgemäßen Flockungsapparat erfolgt vorzugsweise durch:The conditioning of colloidal suspensions such as e.g. B. sewage sludge, with the flocculation apparatus according to the invention is preferably carried out by:
- kontinuierliches Erfassen einer Flockengrößenverteilung eines in den Flockungsapparat geleiteten Suspensionsstroms,continuous detection of a floc size distribution of a suspension stream fed into the flocculation apparatus,
- axiale Verschiebung des Innenkegels und/oder Außengehäuses in Abhängigkeit von einer Flockengrößenverteilung und dem Suspensionsvolumenstrom. Zudem kann die Drehzahl des Innenkegels und/oder Außengehäuses in Abhängigkeit von einer Flockengrößenverteilung geregelt werden.- Axial displacement of the inner cone and / or outer housing depending on a flake size distribution and the suspension volume flow. In addition, the speed of the inner cone and / or outer housing can be regulated as a function of a flake size distribution.
Es wird somit ein kontinuierlicher gesteuerter Prozess ermöglicht, bei dem eine Flockengrößenverteilung zum Beispiel optisch fortlaufend aufgenommen wird und als Regelgröße für den Flockungsapparat dient. Die Strömungsumsetzung, die Verweilzeit und das Reaktionsvolumen wird hierbei durch die axiale Verschiebung des Innenkegels beziehungsweise des Außengehäuses an die Suspensionseigenschaften und die Flockengrößenverteilung angepasst. This enables a continuously controlled process in which a flake size distribution, for example, is optically recorded continuously and serves as a controlled variable for the flocculation apparatus. The flow conversion, the dwell time and the reaction volume are adapted to the suspension properties and the flake size distribution by the axial displacement of the inner cone or the outer housing.
Die Erfindung wird nachfolgend anhand der beigefügten Zeichnungen näher erläutert. Es zeigen:The invention is explained below with reference to the accompanying drawings. Show it:
Figur 1 - Schnittansicht des Flockungsapparates mit axial verschiebbaren Innenkegel;Figure 1 - sectional view of the flocculating apparatus with axially displaceable inner cone;
Figur 2 - Schnittansicht eines Rapid-Mischers zur Erzeugung einer hochturbulenten Suspensionsströmung.Figure 2 - sectional view of a rapid mixer for generating a highly turbulent suspension flow.
Die Figur 1 lässt den erfindungsgemäßen Flockungsapparat 1 in einer Schnittansicht erkennen. Der Flockungsapparat 1 besteht im wesentlichen aus einem kegelförmigen Außengehäuse 2 und einem Innenkegel 3, der zentrisch in dem Außengehäuse 2 angeordnet ist. Der Innenkegel 3 ist rotierbar auf einer angetriebenen Welle 4 gelagert.FIG. 1 shows the flocculation apparatus 1 according to the invention in a sectional view. The flocculation apparatus 1 essentially consists of a conical outer housing 2 and an inner cone 3, which is arranged centrally in the outer housing 2. The inner cone 3 is rotatably mounted on a driven shaft 4.
Ein Suspensionsstrom wird durch eine Suspensionseinlauf 5 im Bereich der Kegelbasis des Innenkegels 3 in den Flockungsapparat 1 eingeleitet. Die Suspension durchströmt dann zusammen mit dem Flockungsmittel und/oder Flockungshilfsmittel den Spaltraum zwischen dem Innenkegel 3 und dem Außengehäuse 2 in axialer Richtung von der Kegelbasis zur Kegelspitze und strömt durch einen Suspensionsauslauf 6 im Bereich der Kegelspitze aus.A suspension stream is introduced into the flocculation apparatus 1 through a suspension inlet 5 in the region of the cone base of the inner cone 3. The suspension then flows together with the flocculant and / or flocculant in the gap between the inner cone 3 and the outer housing 2 in the axial direction from the cone base to the cone tip and flows out through a suspension outlet 6 in the region of the cone tip.
Der Neigungswinkel des Innenkegels 3 und entsprechend der Neigungswinkel des Außengehäuses 2 ist relativ gering und liegt im Bereich von etwa 2 bis 30 Grad. Da sich die Radien des Innenkegels 3 für die durchströmten Suspensionen während der Durchströmung ändern, sind die entstehenden Zentrifugalkräfte auf Grund der sich ändernden Umfangsgeschwindigkeit entlang der angetriebenen Welle 4 nicht konstant. Im Unterschied zu Zylinderrührern sind die Strömungsverhältnisse nicht über der Länge des Kreis- oder Kegelspaltes einheitlich. Wenn der Flockungsapparat 1 von der Kegelbasis des Innenkegels 3 in Richtung der Kegelstumpfspitze durchströmt wird, wird die Suspension beim Eintritt an der Kegelbasis zunächst größeren Scherkräften ausgesetzt, da dort die Grundströmung auf Grund der höheren Umfangsgeschwindigkeit am Größten ist. Die Scherkräfte nehmen in Richtung der kleiner werdenden Radien des Innenkegels 3 kontinuierlich ab, so dass bereits gebildete Flockenstrukturen später nicht oder nur kaum zerstört werden.The angle of inclination of the inner cone 3 and correspondingly the angle of inclination of the outer housing 2 is relatively small and is in the range of approximately 2 to 30 degrees. Since the radii of the inner cone 3 for the suspensions through which flow flows change during the flow, the centrifugal forces generated are not constant due to the changing circumferential speed along the driven shaft 4. In contrast to cylindrical stirrers, the flow conditions are not uniform over the length of the circular or conical gap. If the flocculation apparatus 1 is flowed through by the cone base of the inner cone 3 in the direction of the truncated cone tip, the suspension is initially subjected to greater shear forces when entering the cone base, since the basic flow is greatest there due to the higher peripheral speed. The shear forces decrease continuously in the direction of the decreasing radii of the inner cone 3, so that flake structures that have already been formed are not or only barely destroyed later.
Das Außengehäuse 2 ist erheblich länger als der Innenkegel 3, so dass der Innenkegel 3 axial in einem weiten Bereich verschiebbar ist. Alternativ kann der Flockungsapparat 1 aber auch so aufgebaut sein, dass das Außengehäuse 2 axial relativ zum Innenkegel 3 verschoben werden kann. Es ist auch denkbar, dass das Außengehäuse 2 rotierbar ist.The outer housing 2 is considerably longer than the inner cone 3, so that the inner cone 3 is axially displaceable in a wide range. Alternatively, the flocculation apparatus 1 can also be constructed in such a way that the outer housing 2 can be displaced axially relative to the inner cone 3. It is also conceivable that the outer housing 2 can be rotated.
Durch die axiale Verschiebung des Innenkegels 3 gegenüber dem Außengehäuse 2 kann die Spaltweite zwischen Innenkegel 3 und Außengehäuse 2 variabel angepasst werden. Die axiale Verschiebung kann zum Beispiel mit einem Spindelhubantrieb als Aktuator realisiert werden, der mit der Welle 4 zusammen wirkt. Die Motorwelle eines nicht dargestellten Antriebsmotors ist fest mit einer Führungshülse verbunden, die mit einer Passfederverbindung in Wirkverbindung mit der Welle 4 steht, so dass die Welle 4 axial gegenüber der Motorwelle verschoben werden kann. Die Welle 4 ist vorzugsweise in einem Schrägkugellager 7 gelagert, wobei das Lagergehäuse vorzugsweise quadratisch ist, um dieses in der Nut einer Führungsschiene zu führen. Damit ist sichergestellt, dass nach der Kupplung durch das Schrägkugellager 7 keine Rotation mehr auftritt, die auf den Spindelhubantrieb wirken könnte.The axial displacement of the inner cone 3 relative to the outer housing 2 means that the gap width between the inner cone 3 and the outer housing 2 can be variably adjusted. The axial displacement can be implemented, for example, with a spindle stroke drive as an actuator, which interacts with the shaft 4. The motor shaft of a drive motor, not shown, is fixedly connected to a guide sleeve which is operatively connected to the shaft 4 by means of a feather key connection, so that the shaft 4 can be displaced axially relative to the motor shaft. The shaft 4 is preferably mounted in an angular contact ball bearing 7, the bearing housing preferably being square in order to guide it in the groove of a guide rail. This ensures that after the coupling by the angular contact ball bearing 7, there is no longer any rotation which could act on the spindle lifting drive.
Die Figur 2 zeigt einen Rapid-Mischer 8 mit einem Suspensionseinlauf 9 und einem Suspensionsauslauf 10. Der Suspensionsauslauf 10 ist unmittelbar vor den Suspensionseinlauf 5 des Flockungsapparats 1 geschaltet. Der Rapid- Mischer 8 hat einen von außen nach innen durchströmten Hauptrotor 1 1 , der mit angestellten, schneidenförmigen Schaufeln ausgestattet ist, die die Suspension in Förderrichtung mitreißen. Das Flockungsmittel und/oder Flockungshilfsmittel wird über vier über den Umfang verteilte Stutzen 12 dem Rapid-Mischer 8 zugeführt. Nach der Durchmischung im Hauptrotor 1 1 gelangt das Medium in einen zwischengelagerten Stator 13, dessen Mantel zur Verringerung von Verschleiß über den Bereich des Hauptrotors 1 1 hinaus verlängert ist.FIG. 2 shows a rapid mixer 8 with a suspension inlet 9 and a suspension outlet 10. The suspension outlet 10 is immediately in front the suspension inlet 5 of the flocculation apparatus 1 switched. The rapid mixer 8 has a main rotor 11 through which the outside flows inwards, which is equipped with employed, blade-shaped blades which carry the suspension in the conveying direction. The flocculant and / or flocculant is fed to the rapid mixer 8 via four nozzles 12 distributed over the circumference. After mixing in the main rotor 1 1, the medium enters an intermediate stator 13, the jacket of which is extended beyond the area of the main rotor 1 1 to reduce wear.
In Durchströmungsrichtung hinter dem Stator 1 3 ist ein Hilfsrotor 14 vorgesehen. Diese Anordnung von hintereinander geschaltetem Hauptrotor 1 1 , Stator 1 3 und Hilfsrotor 14 gewährleistet eine homogene Durchmischung des Mediums innerhalb einer bestimmten Verweilzeit. Die Rotordrehzahl sollte stufenlos bis zu etwa 2800 N/min einstellbar sein.An auxiliary rotor 14 is provided in the flow direction behind the stator 1 3. This arrangement of series-connected main rotor 1 1, stator 1 3 and auxiliary rotor 14 ensures homogeneous mixing of the medium within a certain dwell time. The rotor speed should be continuously adjustable up to about 2800 N / min.
Mit Hilfe der Anordnung aus hintereinander geschaltetem Rapid-Mischer 8 und Flockungsapparat 1 ist der Konditionierungsprozess mit vier unterschiedlichen Freiheitsgraden regelbar. In dem Rapid-Mischer wird das Flockungsmittel und/oder Flockungshilfsmittel homogen eingemischt und es wird eine Totalflockung der Suspension durchgeführt. Hierbei sind die Menge des eingebrachten Flockungsmittel und/oder Flockungshilfsmittels und die Höhe der Mischenergie durch Anpassung der Drehzahl des Rapid-Mischers 8 variabel einstellbar.The conditioning process can be regulated with four different degrees of freedom with the aid of the arrangement of a rapid mixer 8 connected in series and a flocculation apparatus 1. The flocculant and / or flocculant is mixed homogeneously in the rapid mixer and total flocculation of the suspension is carried out. The amount of flocculant and / or flocculant introduced and the amount of mixing energy can be variably adjusted by adjusting the speed of the rapid mixer 8.
Mit dem Flockungsapparat wird die Flockung diskretisiert. Hierbei werden die unterschiedlich großen Aggregate der Totalflockungen durch Scherkraftbeanspruchung erodiert, reflockuliert, kompaktiert und vergleichmäßigt. Hierzu ist in dem Flockungsapparat 1 die Drehzahl und das Reaktionsvolumen des Apparates veränderbar. Hierdurch können die Flocken in einem weiten Bereich einem angepassten Scherkraftregime ausgesetzt werden. Die Einstellung des Rapid-Mischers 8 und des Flockungsapparates 1 erfolgt somit in Abhängigkeit von dem Volumenstrom und insbesondere der Flockengröße und der Flockengrößenverteilung. Die Flockengröße und die Flockengrößenverteilung hat nämlich z. B. einen entscheidenen Einfluss auf die Entwässerungs- und Eindickfähigkeit von Suspensionen wie z. B. Klärschlamm. Für eine optimale Entwässerung ist es entscheidend, dass eine bestimmte Flockengrößenverteilung vorliegt. Kleine Strukturen, wie ungeflockte Primärteilchen, sowie kleinste Fraktale in der Flockensuspension mindern z. B. das Entwässerungsergebnis oder das Sedimentationsverhalten. Ebenso wirken sich Struktur-instabile Flocken negativ aus.The flocculation device discretizes the flocculation. The different sized aggregates of the total flocculation are eroded, reflocculated, compacted and evened out by shear stress. For this purpose, the speed and the reaction volume of the apparatus can be changed in the flocculating apparatus 1. As a result, the flakes can be exposed to an adapted shear force regime over a wide range. The setting of the rapid mixer 8 and of the flocculation apparatus 1 is thus dependent on the volume flow and in particular the size of the flakes and the size of the flakes. The flake size and the flake size distribution have namely z. B. a decisive influence on the drainage and thickening ability of suspensions such. B. sewage sludge. For optimal drainage, it is crucial that there is a certain flake size distribution. Small structures, such as non-flocculated primary particles, as well as smallest fractals in the flock suspension reduce e.g. B. the drainage result or the sedimentation behavior. Structurally unstable flakes also have a negative effect.
Der Rapid-Mischer 8 wird nunmehr so geregelt, dass das Flockungsmittel und/oder Flockungshilfsmittel homogen und vollständig mit der Suspension vermengt wird. Dabei muss soviel Energie in das Suspensions-Flockungsmittel und/oder Flockungshilfsmittel-Gemisch fließen, dass jedes Suspensionsteilchen die Möglichkeit hat, sich mit Flockungsmittel und/oder Flockungshilfsmittel zu verbinden. Auf der anderen Seite darf nur so viel Energie eingesetzt werden, dass die Flocken nicht während oder sofort nach ihrer Entstehung wieder zerstört werden. Hierzu ist die Drehzahl entsprechend in bekannter und wissenschaftlich vielfältig untersuchter Weise einzustellen.The rapid mixer 8 is now regulated so that the flocculant and / or flocculant is mixed homogeneously and completely with the suspension. Sufficient energy must flow into the suspension flocculant and / or flocculant mixture so that each suspension particle has the possibility of combining with flocculant and / or flocculant. On the other hand, only so much energy may be used that the flakes are not destroyed again during or immediately after their formation. For this purpose, the speed must be set accordingly in a known and scientifically investigated manner.
In dem Flockungsapparat 1 wird die Drehzahl und die Spaltweite zwischen Innenkegel 3 und Außengehäuse 2 variiert. Durch die Spaltweitenänderung wird sowohl eine Volumenänderung und damit eine Änderung der axialen Kennwerte wie Verweilzeit, axiale Geschwindigkeit, axiale Reynoldszahl und axiale Campzahl, sowie eine Änderung der Radienverhältnisse und damit eine Änderung der Taylor- und rotationeilen Campzahl bewirkt. Damit können die Strömungsverhältnisse in einem weiten Bereich variabel eingestellt werden. Hierzu wird neben dem Volumenstrom vorzugsweise optisch die Flockengrößenverteilung bestimmt und der Rapid-Mischer 8 und der Flockungsapparat 1 so geregelt, dass eine optimale Flockengrößenverteilung resultiert. Hierdurch ist die Konditionierung in einem geschlossenen selbstadaptierenden Regelsystem möglich. The speed and the gap width between the inner cone 3 and the outer housing 2 are varied in the flocculating apparatus 1. The change in gap width causes both a change in volume and thus a change in the axial parameters such as dwell time, axial speed, axial Reynolds number and axial camp number, as well as a change in the radius ratio and thus a change in the Taylor and rotational camp number. The flow conditions can thus be variably adjusted over a wide range. For this purpose, in addition to the volume flow, the flake size distribution is preferably optically determined and the rapid mixer 8 and the flocculation apparatus 1 are regulated such that an optimal flake size distribution results. This enables conditioning in a closed, self-adapting control system.

Claims

Ansprüche Expectations
1 . Flockungsapparat ( 1 ) zur Konditionierung von kolloidalen Suspensionen mit einem Suspensionseinlauf (5), Suspensionsauslauf (6) und mit einem zentrisch in einem kegelförmigen Außengehäuse (2) gelagerten Innenkegel1 . Flocculation apparatus (1) for the conditioning of colloidal suspensions with a suspension inlet (5), suspension outlet (6) and with an inner cone centrally located in a conical outer housing (2)
(3), wobei der Innenkegel (3) und/oder das Außengehäuse (2) relativ zueinander rotierbar sind und zwischen dem Innenkegel (3) und dem Außengehäuse (2) ein Spaltraum zur Durchströmung mit Suspensionen ist, dadurch gekennzeichnet, dass der Innenkegel (3) und/oder das Außengehäuse (2) axial verschiebbar gelagert ist und ein Aktuator zur gesteuerten axialen Verschiebung des Innenkegels (3) und/oder Außengehäuses (2) in Wirkverbindung mit dem Innenkegel (3) und/oder Außengehäuse (2) steht.(3), the inner cone (3) and / or the outer housing (2) being rotatable relative to one another and a gap between the inner cone (3) and the outer housing (2) for the flow of suspensions, characterized in that the inner cone ( 3) and / or the outer housing (2) is axially displaceably mounted and an actuator for controlled axial displacement of the inner cone (3) and / or outer housing (2) is in operative connection with the inner cone (3) and / or outer housing (2).
2. Flockungsapparat ( 1 ) nach Anspruch 1 , dadurch gekennzeichnet, dass der Suspensionseinlauf (5) im Bereich der Kegelbasis des Innenkegels (3) und Außengehäuses (2) und des Suspensionsauslaufs (6) im Bereich der Kegelspitze des Innenkegels (3) und Außengehäuses (2) ist, und dass der Suspensionsstrom von der Kegelbasis zur Kegelspitze verläuft.2. Flocculation apparatus (1) according to claim 1, characterized in that the suspension inlet (5) in the region of the cone base of the inner cone (3) and outer housing (2) and the suspension outlet (6) in the region of the cone tip of the inner cone (3) and outer housing (2), and that the suspension flow runs from the cone base to the cone tip.
3. Flockungsapparat ( 1 ) nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass die Oberfläche des Innenkegels (3) und/oder die Innenfläche des Außengehäuses (2) profiliert ist.3. flocculating apparatus (1) according to claim 1 or 2, characterized in that the surface of the inner cone (3) and / or the inner surface of the outer housing (2) is profiled.
4. Flockungsapparat ( 1 ) nach Anspruch 3, dadurch gekennzeichnet, dass das Profil aus Längsnuten gebildet ist.4. flocculating apparatus (1) according to claim 3, characterized in that the profile is formed from longitudinal grooves.
5. Flockungsapparat ( 1 ) nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass die Rotationsachse des Innenkegels (3) annähernd senkrecht steht und der Suspensionseinlauf (5) oberhalb von dem Suspensionsauslauf (6) angeordnet ist.5. flocculating apparatus (1) according to any one of the preceding claims, characterized in that the axis of rotation of the inner cone (3) approximately is vertical and the suspension inlet (5) is arranged above the suspension outlet (6).
6. Flockungsapparat ( 1 ) nach einem der vorhergehenden Ansprüche, dadurch gekennzeichnet, dass ein Mischer zur Erzeugung einer hochturbulenten6. flocculation apparatus (1) according to any one of the preceding claims, characterized in that a mixer for generating a highly turbulent
Suspensionsströmung unmittelbar vor dem Suspensionseinlauf (5) angeordnet ist.Suspension flow is arranged immediately before the suspension inlet (5).
7. Flockungsapparat ( 1 ) nach einem der vorhergehenden Ansprüche dadurch gekennzeichnet, dass der Neigungswinkel des Innenkegels (3) etwa 2 bis7. Flocculation apparatus (1) according to one of the preceding claims, characterized in that the angle of inclination of the inner cone (3) is approximately 2 to
30°C beträgt.Is 30 ° C.
8. Verfahren zur Konditionierung von Suspensionen mit einem Flockungsapparat (1 ) nach einem der vorhergehenden Ansprüche, gekennzeichnet durch8. A method for conditioning suspensions with a flocculation apparatus (1) according to one of the preceding claims, characterized by
- kontinuierliches Erfassen einer Flockungsgrößenverteilung eines in den Flockungsapparats ( 1 ) geleiteten Supensionsstroms,- Continuous detection of a flocculation size distribution of a suspension stream conducted into the flocculation apparatus (1),
- axiale Verschiebung des Innenkegels (3) und/oder Außengehäuses (2) in Abhängigkeit von der Flockengrößenverteilung und dem Suspensionsvolumenstrom.- Axial displacement of the inner cone (3) and / or outer housing (2) depending on the flake size distribution and the suspension volume flow.
9. Verfahren nach Anspruch 7, gekennzeichnet durch Regelung der Drehzahl des Innenkegels (3) und/oder Außengehäuses (2) in Abhängigkeit von einer Flockengrößenverteilung. 9. The method according to claim 7, characterized by controlling the speed of the inner cone (3) and / or outer housing (2) as a function of a flake size distribution.
EP02779131A 2001-10-02 2002-09-26 Flocculation device and method for treating colloidal suspensions Expired - Lifetime EP1432502B1 (en)

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DE10148760A DE10148760A1 (en) 2001-10-02 2001-10-02 Colloidal sewage treatment has two concentric axial variable-position profiled rotating cones
DE10148760 2001-10-02
PCT/DE2002/003654 WO2003031040A1 (en) 2001-10-02 2002-09-26 Flocculation apparatus and method for treating colloidal suspensions

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020007978A1 (en) 2018-07-04 2020-01-09 Bma Braunschweigische Maschinenbauanstalt Ag Method and arrangement for separating solids and liquids in suspensions, in particular sewage sludge, by adding flocculants

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102006016067B3 (en) * 2006-04-04 2008-01-03 Clausthaler Umwelttechnikinstitut Gmbh, (Cutec-Institut) Flakes forming device
CH702186A2 (en) 2009-11-03 2011-05-13 Sanoxys Ag Device for dewatering of earth materials.
US20110240129A1 (en) * 2010-04-01 2011-10-06 Flsmidth A/S Thickener floccuant control by in-situ aggregate size analysis
SE546177C2 (en) * 2021-04-26 2024-06-18 Valmet Oy Mixing assembly and method for controlling mixing of green liquor and a flocculation agent

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE289754C (en) 1900-01-01
US2793847A (en) * 1955-12-29 1957-05-28 Marie J Steele Industrial gas purifier
US2969960A (en) * 1957-06-05 1961-01-31 Mobay Chemical Corp Mixing apparatus
US3420506A (en) * 1967-04-03 1969-01-07 Mobay Chemical Corp Mixing apparatus
CA950448A (en) * 1970-04-03 1974-07-02 Agfa-Gevaert N.V. Turbulent nucleate-grained silver-halide-reactants mixing method
GB1397927A (en) 1971-06-22 1975-06-18 Tate & Lyle Ltd Separation of suspended solids from liquids
CS171494B1 (en) * 1974-04-29 1976-10-29
DE2458862A1 (en) 1974-12-12 1976-06-16 Wacker Chemie Gmbh USE OF A CENTRIC ROTARY MIXER FOR CONTINUOUS MIXING OF SOLIDS WITH SOLIDS AND / OR FLOWABLE MASSES AND / OR GASES
US4295973A (en) * 1979-03-16 1981-10-20 Fram Industrial Filter Corp. Process for separating solids from suspensions of influent
US4414184A (en) * 1981-02-23 1983-11-08 Union Carbide Corporation Apparatus for mixing chemical components
US5088831A (en) * 1988-02-09 1992-02-18 Sunds Defibrator Industries Aktiebolag Device for treating material mixtures
DD289754A5 (en) * 1989-12-08 1991-05-08 Ingenieurhochschule Koethen,De DEVICE FOR PELLETING FLOCKING OF SOLIDS FROM FLAKABLE SUSPENSIONS
DE4433039B4 (en) * 1994-09-16 2006-11-16 Richard Frisse Gmbh Devices for processing dispersions
JPH1029213A (en) * 1996-07-15 1998-02-03 Toray Dow Corning Silicone Co Ltd Liquid material continuous mixing apparatus
US6808305B2 (en) * 2002-03-25 2004-10-26 Sharpe Mixers, Inc. Method and apparatus for mixing additives with sludge in a powered line blender

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO03031040A1 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020007978A1 (en) 2018-07-04 2020-01-09 Bma Braunschweigische Maschinenbauanstalt Ag Method and arrangement for separating solids and liquids in suspensions, in particular sewage sludge, by adding flocculants

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ATE299394T1 (en) 2005-07-15
US20040262230A1 (en) 2004-12-30
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DE10148760A1 (en) 2003-04-17
DE50203636D1 (en) 2005-08-18

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