WO1997035655A1 - Systeme de traitement de l'eau - Google Patents

Systeme de traitement de l'eau Download PDF

Info

Publication number
WO1997035655A1
WO1997035655A1 PCT/US1997/004606 US9704606W WO9735655A1 WO 1997035655 A1 WO1997035655 A1 WO 1997035655A1 US 9704606 W US9704606 W US 9704606W WO 9735655 A1 WO9735655 A1 WO 9735655A1
Authority
WO
WIPO (PCT)
Prior art keywords
influent
inert particles
contact chamber
floes
impeller
Prior art date
Application number
PCT/US1997/004606
Other languages
English (en)
Inventor
Robert Dash
Pei Kuang
Donald G. Nyberg
Stephen R. Ramsay
Dietmar J. Berger
Original Assignee
Microsep International (Canada) Corporation
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
Application filed by Microsep International (Canada) Corporation filed Critical Microsep International (Canada) Corporation
Priority to AU25401/97A priority Critical patent/AU2540197A/en
Publication of WO1997035655A1 publication Critical patent/WO1997035655A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/0003—Making of sedimentation devices, structural details thereof, e.g. prefabricated parts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/0015—Controlling the inclination of settling devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/02—Settling tanks with single outlets for the separated liquid
    • B01D21/04—Settling tanks with single outlets for the separated liquid with moving scrapers
    • B01D21/06—Settling tanks with single outlets for the separated liquid with moving scrapers with rotating scrapers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/18—Construction of the scrapers or the driving mechanisms for settling tanks
    • B01D21/186—Construction of the scrapers or the driving mechanisms for settling tanks with two or more scrapers fixed at different heights on a central rotating shaft
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/18—Construction of the scrapers or the driving mechanisms for settling tanks
    • B01D21/20—Driving mechanisms
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/2405—Feed mechanisms for settling tanks
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/245—Discharge mechanisms for the sediments
    • B01D21/2461—Positive-displacement pumps; Screw feeders; Trough conveyors

Definitions

  • the present invention generally relates to gravitational separation by sedimentation and. more particularly, to systems for continuously separating suspended solid materials from a feed stream by gravity settling.
  • Sedimentation devices which incorporate settling tanks are well known to separate suspended solids from streams of liquid, such as ground water, process water, creek water, stream and river water and lake water, by gravity settling.
  • various chemical flocculating agents e.g., polyelectrolyte polymers
  • coagulating agents e.g., mineral salts
  • settling of floe particles can be enhanced in certain circumstances by mixing the flocculating agents with inert particles such as sand.
  • inert particles such as sand.
  • the mixing of flocculating agents and inert particles with the influent is accomplished outside the sedimentation (or settling) tank proper, say in a pipe or mixing chamber and, may be accompanied by mechanical stirring of the mixture to provide contact opportunity and time for the resulting floes to grow.
  • Turbidity in water is caused by suspended matter, such as clay. silt. finely divided organic and inorganic matter, soluble colored organic compounds, and plankton and other microscopic organisms.
  • Turbidity is an expression of the optical properties resulting from light being scattered and absorbed rather than transmitted in straight lines through the water. Turbidity is measured with nephelometric measurements and compared using nephelometric turbidity units (NTU) which are basically a comparison of the intensity of light scattered by a sample of water in question with a standard reference suspension.
  • NTU nephelometric turbidity units
  • COLOR in water is comprised of "apparent color” which results from a combination of soluble and suspended impurities and "true color” which is a measurement of only the color resulting from soluble impurities after the suspended material has been filtered out.
  • True color usually results from metallic ions such as iron and manganese. Color is measured in "color units” which is a comparison of a water sample with a standard sample which has a value of zero.
  • the present invention in very general terms, provides a sedimentation device for treating water having a mixing chamber with at least two impellers, a down flow zone and an up-flowing clarification zone.
  • the input and the mixing characteristics of the mixing chamber being controlled so as to require short residence time in the mixing chamber of the influent being treated.
  • the present invention provides an improved sedimentation device for treating water, such as but not limited to ground water, process water, creek water, stream and river water, lake water, and the like, (as opposed to waste water, such as mineral slurries, ore slurries, pulp and paper recausticizing slurries, flue gas scrubbing slurries, coal refuse slurries, and municipal and industrial wastes and sewage) in which the water is in the mixing chamber for a short time while still providing good clarity in the clarified effluent.
  • Influents which the sedimentation device of the invention is intended to treat include all sources from which potable water can be obtained by treating the influent to remove color and insoluble sediments detrimental to human consumption.
  • a process for influent liquid treatment by sedimentation by combining a flow of pretreated influent, flocculant and inert particles in a solids contact chamber with at least two impellers for or about 180 seconds or more to produce a flocculated mixture, passing the flocculated mixture from the solids contact chamber into a down-flow zone, passing the flocculated mixture through the down-flow zone, without further mechanical agitation, into a settling zone and removing the clarified influent from an upper region of the settling zone and settled floes and other settled materials from a lower region of the settling zone.
  • an apparatus for influent treatment by sedimentation having a solids contact chamber having a pretreated influent inlet, a flocculant inlet, an inert particles inlet and at least two impellers to produce a flocculated mixture, a settling zone below the solids contact chamber having a settled floes and other settled materials outlet, a down flow zone connecting the solids contact chamber to the settling zone such that the down-flow zone passes the flocculated mixture from the solids contact chamber into the settling zone without mechanical agitation, and a clarification zone above the settling zone.
  • a process for influent liquid treatment by sedimentation by combining a flow of pretreated influent, flocculant and inert particles in a solids contact chamber with at least two impellers for about 180 seconds or more to produce a flocculated mixture, passing the flocculated mixture from the solids contact chamber into a down-flow zone, passing the flocculated mixture through the down-flow zone utilizing differential sedimentation into a settling zone and removing the clarified influent liquid from an upper portion of the settling zone and removing settled floes and other settled materials from a lower region of the settling zone.
  • FIG. 1 is a cross-sectional view of a sedimentation device in accordance with one embodiment of the present invention, parts of which are shown schematically;
  • FIG. 2 is a cross-sectional view of a sedimentation device in accordance with another embodiment of the present invention, again with parts shown schematically;
  • Figure 3 is a graph showing the reduction in the color as a function of mixing time for highly colored well water
  • Figure 4 is a graph showing the reduction in turbidity as a function of mixing time for the same highly colored well water of Figure 3;
  • Figure 5 is a graph showing the reduction in the color as a function of mixing time for creek water
  • Figures 6 and 7 are graphs showing the impact of inert particle carriers on turbidity and color
  • Figure 8 is a graph showing the impact of G value on turbidity as a function of flocculation time.
  • the sedimentation devices of each of the embodiments shown in Figures 1 and 2 include a settling tank or main vessel 2 in which separation by sedimentation principally occurs utilizing ballasted flocculation.
  • the settling tank 2 is cylindrical in configuration, but a rectangular or other shaped configuration can be used.
  • vessel 2 is defined by a sidewall 1 1 and a bottom wall 13.
  • bottom wall 13 slopes downward at an angle in the range of or about 50° to or about 70° toward a collection cone 15 formed centrally in the bottom wall 13 of the tank 2 to prevent any sludge from building up on the bottom wall 13 as the floes settle in the settling tank 2.
  • a sloping bottom wall 13 of any angle from 0° to 15° is used in combination with a raking mechanism 37.
  • a collection system (e.g., launder) 17 is mounted in the sidewall 1 1 of the vessel 2.
  • the collection system includes an outlet pipe 19 and an overflow weir 60, which defines the liquid level 29 in the tank 2.
  • Centrally disposed in the tank is a generally cylindrical vessel 23 which for purposes of identification herein will be referred to as a down-flow vessel.
  • the down-flow vessel 23 can be supported from the bridge 24 as shown (or other trusswork which traverses the tank) or can be supported by extensions (not shown) extending inwardly from the inner walls of the settling tank 2.
  • the down-flow vessel 23 serves to partition the settling floes and treated water from the clarified effluent rising along the sides of the settling tank 2. Attached to the lower portion 21 of the down-flow vessel 23 at junction 38 is truncated cone 40. Although cone 40 is not necessary in all circumstances, it assists in bringing the settled floes to the center of the settling tank 2 for more efficient collection by collection cone 15.
  • solids contact chamber 14 is supported by adjustable hangers 26 and comprises an upwardly or downwardly telescoping section that allows the volume of the solids contact chamber 14 to be controllably varied depending on the operating needs. It can now be appreciated that the outer surface 30 of chamber 14 and the inner surface 32 of down-flow vessel 23 define a down-flow zone 34; the function and operation of the down-flow zone 34 will be described in more detail below.
  • Baffle plates/vortex breakers 36 can optionally be mounted in the solids contact chamber 14.
  • the baffle plates 36 are vertically mounted at four spaced-apart positions within the solids contact chamber 14 and extend radially across the vessel for 1/12 to 1/10 the diameter of the solids contact chamber.
  • the baffles prevent disruptive vortexes or swirls from being established in the solids contact chamber that might break up the floes or entrap air.
  • four baffles are provided, but the number and configuration of the plates is a matter of design choice.
  • at least one inlet feed 43 is provided in fluid communication with the interior of the solids contact chamber 14.
  • inlet feed 43 a stream of influent is fed in to the interior of chamber 14 through a distributor 44.
  • the distributor 44 is sized relative to the influent flow rate to distribute the influent evenly in the solids contact chamber.
  • a mixing impeller 47 and lower in the chamber 14 adjacent the outlet of distribufor 44 is mounted above the outlet of distributor 44.
  • a mixing impeller 47 and lower in the chamber 14 adjacent the outlet of distribufor 44 are mounted above the outlet of distributor 44.
  • a mixing impeller 47 and lower in the chamber 14 adjacent the outlet of distribufor 44.
  • Preferably two impellers are used as shown.
  • Upper impeller 47 is preferably either a marine or hydrofoil type impeller which provides gentle mixing for additional flocculation time without destroying the floes already formed. The upper impeller 47 maintains suspension of the floes and inert particles prior to their transport out of the chamber 14.
  • Lower impeller 64 is preferably a turbine type impeller which provides higher speed/higher shear mixing.
  • the impellers 47 and 64 coupled to the drive unit 25 through shaft 7 or to an auxiliary rotary drive (not shown).
  • an outlet 16 located near the impeller 64 in the solids contact chamber 14 is an outlet 16 which, as will be explained in greater detail below, injects recycled inert particles into the chamber from a hydrocylcone underflow.
  • a polymer or flocculating agent injection outlet 48 is located near the impeller 64 in the solids contact chamber 14. In practice, it is particularly advantageous to introduce the inert particles and flocculant as close together as possible so that the flocculant and inert particles come together quickly.
  • the inert particles and flocculant are injected together in an inlet feed stream.
  • the inert particles employed in the system are typically 150 micrometers in diameter or less, but should be sufficiently large to maintain a relatively high settling velocity in the down flow zone after floes have formed around them.
  • the inert particles also aid in taking advantage of the differential sedimentation phenomena based on the heterogenous curvilinear flocculation theory.
  • Impeller 64 is rotated to provide just enough agitation to produce sufficient mixing of the suspended solids with the influent, inert particles and flocculant to promote the formation of floes without inducing shear that would break the formed floes apart.
  • Impeller 47 is operated to impart just enough turbulence to maintain the solids in suspension with as little shear as possible as floes are forming.
  • the mixing in mixing chamber 14 advantageously utilizes the differential sedimentation phenomena for floe production with the addition of the inert particles.
  • the floes and treated water that overflow the top edge 3 of the solids contact chamber 14 into the down flow zone 34 are generally uniformly mixed.
  • Lower impeller 64 provides higher velocity gradient (G) values, compared to the upper impeller 47, in the initial mixing area to induce floe formation.
  • Upper impeller 47 provides more gentle mixing to provide additional flocculation time without destroying the floes already formed.
  • two impellers are shown, it is within the scope of the invention to use more than two impellers to induce floe formation in the lower portion of mixing chamber 14 and to provide more gentle mixing in the upper portion.
  • the impellers between the lower impeller and upper impeller can be turbine, marine or hydrofoil type impellers, likewise the velocity gradient values can be varied by the tip speed or shape of the impellers to provide the desired mixing conditions.
  • the solids contact chamber 14 is designed and sized to provide short residence times and that the hydraulic velocities aid in keeping the inert particles suspended.
  • the impellers 47 and 64 provide uniform mixing of the flocculant, influent and inert particles over the range of normal load operations.
  • the fluid velocity changes from about 150 meters/hour at arrow 49 to about 50 meters/hour at arrow 50.
  • the velocities through the down flow zone 34 generally are dependent upon the relative diameters of the solids contact chamber 14 and the down-flow vessel 23, at least to a first-order approximation.
  • the relative diameters of the solids contact chamber 14 and the down-flow vessel 23, are sized such that the down flow velocities are relatively high without creating shear in the liquid that would break up the floes.
  • the fluid flow velocity decreases at arrow 51 , accelerates in the space of truncated cone 40 at arrow 52 and then decelerates as the flow exits truncated cone 40 at arrow 53.
  • the clarified effluent rises in clarification zone 5 and through the settling plates 4 (e.g., at a velocity about 20 meters/hour and higher) and, finally, overflows into the launder 17.
  • drive unit 25 of conventional construction is mounted on the bridge 24 to drive the impeller 47, impeller 64, and optional raking mechanism 37.
  • the rotation rates of the two impellers and raking mechanism can, of course, be different; typically, the impellers rotate at a much faster rate than the raking mechanism.
  • the raking mechanism 37 is of conventional construction and is mounted to rake settled solids across the bottom or floor 13 of the tank to the collection cone 15 such that no sludge build up occurs on the bottom wall.
  • an optional deflection cone 9 is connected to the shaft 7 for rotation. Sludge scraper 60 attached to shaft 7 below bearing 62 rotates within collection cone 15 to prevent the build up of sludge in the cone.
  • high shear pump 8 breaks the bonds between the sludge and inert particles to assist the separation device 6 in separating the inert particles, which are recycled into the solids contact chamber 14 through separating device underflow 16, and the sludge which is discharged through outlet 18 of separating device 6.
  • a flush-out connection 10 can be provided in conduit 66. Concomitant with the removal of thickened, settled solids via the collection cone 15, clarified effluent is removed at the liquid surface 29 in the settling tank 2 via the launder 17 and launder outlet 19.
  • Various suitable launder arrangements which can be used in the present invention are well known in the sedimentation art.
  • the interior of the settling tank 2 can be understood to comprise a zone for receiving and mixing the stream of influent, inert particles and flocculant; a down-flow zone with no mechanical agitation and/or no or very little shear for directing clarified liquid and floes to the bottom of the settling tank; and an up-flow zone in which clarified liquid is withdrawn.
  • the inert particles are recycled from the sediment (i.e., sludge) collected at the bottom of the clarification zone and the re-introduced (i.e., recycled) inert particles are normally provided from the separation device after being separated from the mixture of settled solids and inert particles that were previously removed from the settling vessel 2.
  • the above-described sedimentation device is a unique combination of a chemical reactor and clarifier within a single vessel. It is a compact unit that can be used in a liquid-solid separation process with an improved separation efficiency (i.e., high capacity) due to short residence times in the solids contact chamber 14.
  • the improved separation efficiency is due as much to the high settling rates in the clarification zone as it is to the short residence times in the solids contact chamber.
  • the inert particles function as nuclei for binding with fine suspended solids by a long chain polyelectrolyte to produce large and dense floes.
  • the floes formed in such a way settle rapidly and are easily separated from the liquid phase.
  • the inert particles also work as a flocculation aid and provide a large surface area that substantially increases the probability of particle collision, speeding the agglomeration of the floes and enhancing separation efficiency.
  • the overall size of the clarifier is significantly reduced and the capital equipment costs are reduced.
  • various process steps will be described employing the above-described sedimentation device.
  • PROCESS STEP 1 Pre-treatment of influent (e.g., to screen, adjust pH, add coagulant and to provide other chemical/physical conditioning) as required.
  • influent e.g., to screen, adjust pH, add coagulant and to provide other chemical/physical conditioning
  • the influent is analyzed and pretreatment is provided based on what is required to bring the influent into a normal processing range.
  • the solids contact chamber 14 is used to bring the influent to be treated, the chemical flocculant, and the inert particles together in a controlled manner which results in rapid flocculation of suspended solids which then overflow into the down-flow zone 34.
  • the short residence time in the solids contact chamber preferably in the range of or about 180 seconds to or about 480 seconds, more preferably of or about 360 seconds or more, results in much smaller equipment requirements to accomplish an equivalent level of water purification.
  • the reactions, both chemical and physical, which occur in the solids contact chamber 14 are controlled to provide adequate mixing and contact of the suspended solids with the flocculant to provide floes.
  • the mixing is not so turbulent or long lasting so as to break up the delicate floes produced. Adequate but not excessive mixing and adequate but not excessive residence time are based on the influent characteristics and coagulation mechanisms.
  • Nominal Range residence time in solids contact chamber (seconds) 360 180 to 480 inert particles added 3 to 5 1 to 100
  • the down-flow zone 34 in the sedimentation device provides a transportation path into the settling tank free of mechanically induced turbulence and no or a minimum of shear for the floes and treated influent mixture.
  • the operational parameters on this step are such that (a) no turbulence is induced and any shear which occurs does not destroy the floes and (b) that the path to the settling tank is downward and efficient.
  • this zone is around the outer surface 30 of the solids contact chamber 14 and is surrounded by the inner surface 32 of down-flow vessel 23.
  • Down-flow vessel 23 prevents "short circuiting" of the floes and treated influent to the clarification zone 5.
  • this zone is rectangular or circular.
  • the treated influent and floes pass through the down-flow zone without further mechanical agitation.
  • the configuration of the down-flow zone 34 insures that the treated influent and floes pass downward to the bottom of the settling tank 2 without substantial deleterious turbulence or shear. Typically, flow rates of less than 60 meters/hour are maintained in this transition region so that the floes are not destroyed.
  • the clarification zone 5 can operate with or without separator, lamella plates 4 or tube settlers. In the system without lamella plates, a rise rate of 20 meters/hour or higher can be used compared to rise rates of 1 to 2 meters/hour in conventional system clarifiers. The higher rise rates for this system compared to the conventional system result primarily from the use of the inert particles and polymer added to the influent. The use of lamella plates can be used to increase the capacity of the system with rise rates exceeding about 100 meters/hour.
  • the upper part of the clarification zone 5 contains a collection system 17 for directing the clarified effluent to the system outlet 19. The sludge sedimented from the influent is collected at the bottom of the collection cone 15 and pumped to a separation device 6.
  • the sludge/inert particle separation operation separates the inert particles from the sludge using a high shear recirculation pump 8 to transport the sludge mixture to the separating device 6.
  • the inert particles are then recycled into the solids contact chamber 14 to be reused.
  • the sludge is transported out of the system to be disposed of using known devices such as a belt press.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)

Abstract

L'invention concerne un dispositif de sédimentation destiné à traiter l'eau des rivières, l'eau des lacs, l'eau souterraine et autres sources d'eau pour la consommation et les processus industriels. Ce dispositif comporte une chambre de mélange, une zone à écoulement descendant et une zone de clarification à écoulement montant. L'intensité du brassage et le débit de la chambre de mélange sont régulés de façon à obtenir un mélange adéquat et des temps de séjour courts.
PCT/US1997/004606 1996-03-25 1997-03-21 Systeme de traitement de l'eau WO1997035655A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU25401/97A AU2540197A (en) 1996-03-25 1997-03-21 Water treatment system

Applications Claiming Priority (8)

Application Number Priority Date Filing Date Title
US62131796A 1996-03-25 1996-03-25
US08/621,317 1996-03-25
US66140996A 1996-06-07 1996-06-07
US08/661,409 1996-06-07
US67175896A 1996-06-28 1996-06-28
US08/671,758 1996-06-28
US71875496A 1996-09-23 1996-09-23
US08/718,754 1996-09-23

Publications (1)

Publication Number Publication Date
WO1997035655A1 true WO1997035655A1 (fr) 1997-10-02

Family

ID=27505163

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1997/004606 WO1997035655A1 (fr) 1996-03-25 1997-03-21 Systeme de traitement de l'eau

Country Status (2)

Country Link
AU (1) AU2540197A (fr)
WO (1) WO1997035655A1 (fr)

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1197474A1 (fr) * 2000-10-10 2002-04-17 Patrick W. Hanlon Traitement de l'eau par floculation effilée
FR2822080A1 (fr) * 2001-03-15 2002-09-20 Vivendi Water Systems Procede et installation de traitement des eaux par floculation lestee et separation gravitaire a mode de fonctionnement variable
FR2828878A1 (fr) * 2001-08-22 2003-02-28 Didier Brouillet Dispositif d'epuration des eaux usees
FR2863908A1 (fr) * 2003-12-22 2005-06-24 Otv Sa Procede et reacteur de traitement par floculation
WO2012020168A3 (fr) * 2010-08-11 2012-04-05 Clewer Oy Clarificateur
US8470172B2 (en) 2007-01-09 2013-06-25 Siemens Industry, Inc. System for enhancing a wastewater treatment process
US8540877B2 (en) 2007-01-09 2013-09-24 Siemens Water Technologies Llc Ballasted sequencing batch reactor system and method for treating wastewater
US8623205B2 (en) 2007-01-09 2014-01-07 Siemens Water Technologies Llc Ballasted anaerobic system
US8840786B2 (en) 2007-01-09 2014-09-23 Evoqua Water Technologies Llc System and method for removing dissolved contaminants, particulate contaminants, and oil contaminants from industrial waste water
US9651523B2 (en) 2012-09-26 2017-05-16 Evoqua Water Technologies Llc System for measuring the concentration of magnetic ballast in a slurry
CN109879385A (zh) * 2019-03-04 2019-06-14 凌海峰 一种污水处理的絮凝沉淀池
CN111604161A (zh) * 2020-05-25 2020-09-01 中钢集团山东矿业有限公司 一种尾矿综合利用生产线及方法
US10919792B2 (en) 2012-06-11 2021-02-16 Evoqua Water Technologies Llc Treatment using fixed film processes and ballasted settling
US11207614B2 (en) 2019-07-23 2021-12-28 University Of Kentucky Research Foundation Single stage clarifier and mixing assembly
WO2022228973A1 (fr) * 2021-04-26 2022-11-03 Valmet Ab Ensemble de mélange et procédé de commande de mélange de liqueur verte et d'un agent de floculation
US11596912B2 (en) 2019-07-23 2023-03-07 University Of Kentucky Research Foundation Single stage clarifier and mixing assembly

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2301718A1 (de) * 1972-12-14 1974-06-27 Simmering Graz Pauker Ag Verfahren zur trennung von fluessiger und fester phase und raeumer zum entfernen des bodensatzes in einer anlage zur durchfuehrung des verfahrens
WO1990009222A1 (fr) * 1989-02-16 1990-08-23 Golconda Engineering & Mining Services Pty. Ltd. Procede de clarification
US5478468A (en) * 1993-09-10 1995-12-26 Sumitomo Heavy Industries, Ltd. Coagulating sedimentation processing apparatus

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2301718A1 (de) * 1972-12-14 1974-06-27 Simmering Graz Pauker Ag Verfahren zur trennung von fluessiger und fester phase und raeumer zum entfernen des bodensatzes in einer anlage zur durchfuehrung des verfahrens
WO1990009222A1 (fr) * 1989-02-16 1990-08-23 Golconda Engineering & Mining Services Pty. Ltd. Procede de clarification
US5478468A (en) * 1993-09-10 1995-12-26 Sumitomo Heavy Industries, Ltd. Coagulating sedimentation processing apparatus

Cited By (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1197474A1 (fr) * 2000-10-10 2002-04-17 Patrick W. Hanlon Traitement de l'eau par floculation effilée
FR2822080A1 (fr) * 2001-03-15 2002-09-20 Vivendi Water Systems Procede et installation de traitement des eaux par floculation lestee et separation gravitaire a mode de fonctionnement variable
WO2002074691A2 (fr) * 2001-03-15 2002-09-26 Otv Sa Traitement des eaux par floculation lestee et separation gravitaire a mode de fonctionnement variable
WO2002074691A3 (fr) * 2001-03-15 2003-02-20 Otv Sa Traitement des eaux par floculation lestee et separation gravitaire a mode de fonctionnement variable
US7001525B2 (en) 2001-03-15 2006-02-21 Otv Sa Method for the treatment of water by ballasted flocculation and gravity separation with variable function modes
FR2828878A1 (fr) * 2001-08-22 2003-02-28 Didier Brouillet Dispositif d'epuration des eaux usees
FR2863908A1 (fr) * 2003-12-22 2005-06-24 Otv Sa Procede et reacteur de traitement par floculation
WO2005065832A1 (fr) * 2003-12-22 2005-07-21 Otv Sa Procede et reacteur de traitement par floculation
US7648638B2 (en) 2003-12-22 2010-01-19 Otv S.A. Method for treating wastewater
US7906018B2 (en) 2003-12-22 2011-03-15 Otv S.A. System for treating wastewater
US8623205B2 (en) 2007-01-09 2014-01-07 Siemens Water Technologies Llc Ballasted anaerobic system
US8506800B2 (en) 2007-01-09 2013-08-13 Siemens Industry, Inc. System for enhancing a wastewater treatment process
US8540877B2 (en) 2007-01-09 2013-09-24 Siemens Water Technologies Llc Ballasted sequencing batch reactor system and method for treating wastewater
US8673142B2 (en) 2007-01-09 2014-03-18 Siemens Water Technologies Llc System for enhancing a wastewater treatment process
US8702987B2 (en) 2007-01-09 2014-04-22 Evoqua Water Technologies Llc Methods for enhancing a wastewater treatment process
US8840786B2 (en) 2007-01-09 2014-09-23 Evoqua Water Technologies Llc System and method for removing dissolved contaminants, particulate contaminants, and oil contaminants from industrial waste water
US8845901B2 (en) 2007-01-09 2014-09-30 Evoqua Water Technologies Llc Ballasted anaerobic method for treating wastewater
US8470172B2 (en) 2007-01-09 2013-06-25 Siemens Industry, Inc. System for enhancing a wastewater treatment process
US10023486B2 (en) 2007-01-09 2018-07-17 Evoqua Water Technologies Llc Ballasted sequencing batch reactor system and method for treating wastewater
WO2012020168A3 (fr) * 2010-08-11 2012-04-05 Clewer Oy Clarificateur
US10919792B2 (en) 2012-06-11 2021-02-16 Evoqua Water Technologies Llc Treatment using fixed film processes and ballasted settling
US9651523B2 (en) 2012-09-26 2017-05-16 Evoqua Water Technologies Llc System for measuring the concentration of magnetic ballast in a slurry
CN109879385B (zh) * 2019-03-04 2020-05-08 广东健恒环境产业有限公司 一种污水处理的絮凝沉淀池
CN109879385A (zh) * 2019-03-04 2019-06-14 凌海峰 一种污水处理的絮凝沉淀池
US11207614B2 (en) 2019-07-23 2021-12-28 University Of Kentucky Research Foundation Single stage clarifier and mixing assembly
US11596912B2 (en) 2019-07-23 2023-03-07 University Of Kentucky Research Foundation Single stage clarifier and mixing assembly
CN111604161A (zh) * 2020-05-25 2020-09-01 中钢集团山东矿业有限公司 一种尾矿综合利用生产线及方法
WO2022228973A1 (fr) * 2021-04-26 2022-11-03 Valmet Ab Ensemble de mélange et procédé de commande de mélange de liqueur verte et d'un agent de floculation

Also Published As

Publication number Publication date
AU2540197A (en) 1997-10-17

Similar Documents

Publication Publication Date Title
CA2266583C (fr) Systeme de traitement des eaux et des eaux usees avec recyclage interne
US5730864A (en) Installation for treating an untreated flow by simple sedimentation after ballasting with fine sand
US6010631A (en) Method and installation for treating an untreated flow by simple sedimentation after ballasting with fine sand
WO1997035655A1 (fr) Systeme de traitement de l'eau
CN1318312C (zh) 含有悬浮物的液体尤其是水的净化方法及装置
US4999115A (en) Method and apparatus for use in separating solids from liquids
RU2006126705A (ru) Способ и реактор обработки флокуляцией
KR100810334B1 (ko) 응집분리장치
CN107108289B (zh) 改进的压载的净化系统
EP0016690B1 (fr) Dispositif pour séparer des solides de suspensions dans un courant liquide
JP3676208B2 (ja) 固液分離槽
EP0168538A1 (fr) Dispositif de clarification
US4295973A (en) Process for separating solids from suspensions of influent
WO1997035654A1 (fr) Systeme de traitement des eaux usees
KR200220590Y1 (ko) 부유물질 분리기능을 갖는 하수처리용 원심분리장치
EP1268027A1 (fr) Flottaison par milieux flottants solides
WO1999033541A1 (fr) Precipitateur de coagulation
US20030155306A1 (en) Apparatus and method for the treatment of a contaminated fluid
JP4535419B2 (ja) 凝集沈澱装置
JP2003181207A (ja) 凝集沈殿装置
EP0625074B1 (fr) Floculation tourbillonnaire de solide en suspension dans un liquide
JP3676658B2 (ja) 循環流式凝集分離装置
MXPA99003136A (en) Water and wastewater treatment system with internal recirculation
JP3051500B2 (ja) 沈降濃縮装置
CA1087997A (fr) Appareil de decantation des solides dans des liquides

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

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

121 Ep: the epo has been informed by wipo that ep was designated in this application
REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

NENP Non-entry into the national phase

Ref country code: CA

NENP Non-entry into the national phase

Ref country code: JP

Ref document number: 97534507

Format of ref document f/p: F

122 Ep: pct application non-entry in european phase