[go: up one dir, main page]

WO1992008533A1 - Traitement de dispersions - Google Patents

Traitement de dispersions Download PDF

Info

Publication number
WO1992008533A1
WO1992008533A1 PCT/GB1991/002003 GB9102003W WO9208533A1 WO 1992008533 A1 WO1992008533 A1 WO 1992008533A1 GB 9102003 W GB9102003 W GB 9102003W WO 9208533 A1 WO9208533 A1 WO 9208533A1
Authority
WO
WIPO (PCT)
Prior art keywords
dispersion
additive
suspension
salt
separating
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.)
Ceased
Application number
PCT/GB1991/002003
Other languages
English (en)
Inventor
Hans Johann Heidenreich
Daniel Jonathan Shaw
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
MULTISERV INTERNATIONAL Ltd
Original Assignee
MULTISERV INTERNATIONAL Ltd
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 MULTISERV INTERNATIONAL Ltd filed Critical MULTISERV INTERNATIONAL Ltd
Publication of WO1992008533A1 publication Critical patent/WO1992008533A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/0205—Separation of non-miscible liquids by gas bubbles or moving solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/0208—Separation of non-miscible liquids by sedimentation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/0217—Separation of non-miscible liquids by centrifugal force
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/04—Breaking emulsions
    • B01D17/047—Breaking emulsions with separation aids
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents

Definitions

  • the invention relates to the treatment of dispersions, typically aqueous dispersions, and particularly to the separation of the solid phases or liquid and solid phases of highly stable aqueous dispersions (including emulsions and colloidal suspensions).
  • dispersions which can be treated by the invention include emulsions comprising water and used working fluids.
  • Some specific examples include used metal working fluids and dyestuff dispersions.
  • Some specific examples include used metal working emulsions consisting of an aqueous dispersion phase and a dispersed phase consisting substantially of mineral and synthetic oils stabilised by surfactants, emulsifiers etc. and aqueous dispersions containing dyestuffs, pigments, resins, hydrocarbons, etc.
  • a method of separating the phases of a dispersion comprising adding an additive in the form of a suspension of a separating agent in a carrier therefor to the dispersion, intimately mixing the suspension and the dispersion, and separating the phases.
  • the suspension is a homogeneous suspension of two or more separating agents.
  • at least one agent is in the form of particles of sub micron size.
  • one agent is a clay such as bentonite and the other is a salt.
  • the salt may be selected from a wide range of salts which will tend to separate the phases of the dispersion. Such salts may be trivalent as in the case of aluminium sulphate or ferric chloride or ferrous sulphate or bivalent as in the case of magnesium chloride and calcium chloride. It is preferred that the salt is bound up in the clay and the carrier comprise water containing a dissolved salt (which may be the same as or di ferent from that in the clay) .
  • a stabilising agent is present to stabilise the suspension in the form of fine clay / salt composite particles.
  • the stabilising agent is preferably selected from a wide range of surfactants; it is much preferred that the agent be an amphoteric surfactant and be in isoelectronic state in the suspension and one which does not foam when the suspension is mixed with the dispersion.
  • Specific preferred classes of suitable emphoteric surfactants include N-aminopropionate ⁇ and N- iminodipropionate ⁇ ; such surfactants can be prepared by the condensation of fatty primary amines and acrylic amines.
  • the surfactant may be presented as a salt.
  • the choice of stabilising agent will depend on the nature of the agents in the suspension, especially the salt.
  • the stabilising agent will typically make up a low proportion, say 0.1% by weight, of the additive.
  • the clay is preferably a polar clay having a three layer structure.
  • Preferred are natural and synthetic bentonites including montmorillonite .
  • Preferably a sodium type montmorillonite is used.
  • the clay will be in about the same weight concentration as the salt, or may be slightly less.
  • the invention provides a method as defined, wherein the additive comprises a suspension comprising an aqueous phase containing dissolved salt, e.g. aluminium sulphate and a solid phase comprising particles of bentonite of about 0.1 micron in diameter and having a layered structure, aluminium sulphate being present as interlayers within the layers of the bentonite, an amphoteric surfactant being present to stabilise the particles in the suspension.
  • the suspension has a pH of about 3.
  • the dispersion to be treated is an aqueous dispersion, such as a dispersion of waste metal working oils and water.
  • the method is carried out by supplying the dispersion under pressure to a first mixing chamber, adding the additive to the dispersion adjacent its point of entry into the first mixing chamber, causing the mixture of dispersion and additive to be mixed by turbulent passage through the first mixing chamber, passing the mixture into a second mixing chamber and optionally adding gas thereto, causing the gasified mixture to be mixed by turbulent passage through the second mixing chamber, adding a flocculant to the mixture as it emerges from the second mixing chamber and then isolating the separate phases one from the other.
  • the materials are passed through each mixing chamber along a cyclonic path.
  • the passage along the cyclonic path is caused solely by the pressure applied to the mixture.
  • the suspension is added in the form of a fine spray to a pressurised supply of the dispersion entering the first elongate mixing chamber adjacent one end thereof and the two are thoroughly mixed as they travel towards an outlet adjacent the other end thereof.
  • the mixing takes place solely by the flow, and the interior of the vessel is free of baffles and like structures so that eddy currents can pass in different directions.
  • the centrifugal acceleration is between about 250g and about 350g.
  • the mixing in the second mixing chamber may be arranged to take place in similar fashion.
  • the suspension is preferably supplied as a spray or atomised by being sprayed through a full cone nozzle by which a fine spray of uniform cone pattern is produced.
  • the nozzle has paths which cause the suspension to undergo both axial flow and tangential flow.
  • the particles of the organic phase of the dispersion can be isolated very efficiently at the later stage and the COD value of the separated aqueous phase is very low.
  • the gas is introduced, this is preferably in the form of small bubbles.
  • the bubbles are of about 400 micron average diameter; the gas is air and the bubbles are produced by an aerator. Most preferably the aerator is arranged to produce bubbles at the rate of about 30 billion bubbles/cu.m.
  • the flocculant is added at the rate of about 0.5% by volume of the total volume of the treated dispersion.
  • the flocculant can be cationic, anionic or amphoteric, according to the nature of the phases of the dispersion.
  • the flocculant is cationic and has a molecular weight of about 4 to about 10 million.
  • the mixture containing the flocculant is passed through an elongate reaction chamber before the phases are isolated.
  • the elongate reaction chamber comprises a looped pipe system, and has inlets for the optional addition of other agents .
  • bentonite and the sodium ions are replaced by the aluminium.
  • aluminium sulphate recry ⁇ tallises from solution into the bentonite layers to form composite aluminium sulphate- bentonite particles of needle like morphology as a solid phase in a liquid phase of water containing some dissolved aluminium sulphate.
  • the surfactant stabilises the microsuspension and because the surfactant is in an isolectronic state foaming is largely avoided.
  • the organic phase of the dispersion is destabilised and coalesces with the bentonite of the microsuspension to form separate droplets of organic material in the aqueous phase.
  • the flocculant is added the particles coalesce or agglomerate to form a layer of organic material which can be separated from the aqueous phase. Because the aluminium sulphate is already dissolved in the water of the microsuspension the destabilising reaction takes place quickly.
  • the cyclonic circulating system of mixing set out above ensures that the maximum reaction potential is realised.
  • the invention provides a method of making an additive for use in separating the phases of a dispersion, the method comprising dissolving a salt in water, adding a clay to k the solution, the clay being in the form of submicron particles and of layered form so as to cause the salt solution to penetrate the layers by capillary action.
  • the proportion of ingredients is selected so that the salt solution forms an aqueous phase to a solid phase comprising the salt bound up in the clay.
  • the method includes the step of adding the defined stabilising agent to stabilise the suspension.
  • the invention provides an additive for use in separating the phases of a dispersion, the additive comprising a suspension formed of an aqueous phase comprising a solution of a salt and a solid phase comprising a clay having a salt bound up therewith, the clay being in the form of sub-micron particles.
  • the clay is in the form of particles of about 0.1 micron diameter.
  • the suspension preferably contains a stabiliser, typically a surfactant, as defined.
  • the invention provides apparatus for use in separating phases of a dispersion comprising a tank for holding the dispersion to be treated; means for transferring the dispersion to a first mixing chamber under pressure; means for adding a spray of separating additive to the pressurised dispersion adjacent its entry to the first mixing chamber; means for turbulently passing the dispersion and additive through the first mixing chamber; means for adding gas to the mixed dispersion and additive, where required; means for transferring the mixed dispersion and additive and optional gas to a second mixing chamber; means for turbulently passing the dispersion and additive and optional gas through the second mixing chamber; means for adding flocculant to the optionally gasified mixture of dispersion and additive; optionally means for adding other agents to the flocculated mixture; and means for isolating the resultant separate phases one from the other.
  • the invention provides a method of mixing two liquids, one being a dispersion and the other a separating agent therefor, the method comprising intimately mixing the two fluids together in a cyclonic fashion through a common vessel, solely under pressure.
  • the separating agent is in the form of a suspension.
  • the two fluids are mixed together from one end of an elongate cylinder towards the other end. Most preferably the separating agent is sprayed onto the dispersion and then the mixture is urged together through the vessel .
  • the invention provides a method of separating the organic and aqueous phases of a dispersion comprising adding a separating agent to the dispersion to form particles of organic material, adding bubbles of gas, and subjecting the gasified mixture to turbulent mixing to trap bubbles of the gas within agglomerations of the particles.
  • a separating agent to the dispersion to form particles of organic material
  • adding bubbles of gas and subjecting the gasified mixture to turbulent mixing to trap bubbles of the gas within agglomerations of the particles.
  • the gas is air and the bubbles are about 400 micron average diameter.
  • the basic apparatus comprises a reservoir 10 of the dispersion to be treated, a first mixing chamber 20 and a second mixing chamber 30, a reaction chamber 40, a separation tank 50, a hopper 60 of separation additive, an aerator 70 and a hopper 80 containing flocculant.
  • the tank 10 is connected to the first mixing chamber 20 by a pipe 11 which extends from the base of the tank to an inlet 21 adjacent the roof 22 of the first mixing chamber.
  • a centrifugal pump 12 having wide spaced apart plates is present in the pipe 11 and a branch pipe 13 is connected to the pipe 11 via a three way valve 14 for recirculating dispersion so as to mix the dispersion to be treated and to regulate pressure of dispersion in the pipe 11.
  • a pressure gauge 15 is present in the pipe 11 adjacent the chamber 20.
  • a pipe 23 leads from the reservoir 60 containing additive of the invention and opens into the roof 22 of the chamber 20 via a metal spray nozzle.
  • the chamber 20 is an empty steel walled cylinder having an outlet 23 adjacent the floor.
  • the pressured dispersion to be treated is forced into the chamber 20 and to the outlet 23 in a cyclonic fashion, additive being added in spray form as the dispersion enters the chamber 20.
  • a pipe 24 leads from the outlet 23 to an inlet 31 adjacent the roof 32 of the scond mixing chamber 30.
  • An aerator 70 for generating air bubbles is mounted adjacent to the pipe 24 and is connected thereto by valves 71,72 for the introduction of small air bubbles into the additive - containing dispersion in the pipe 24.
  • the aerator 70 is selected so that the bubbles are of 400 micron average diameter and produced at the rate of 30 billion bubbles/cu.m.
  • the aerator 70 has an air inlet 73.
  • the second mixing chamber 30 is of frustoconical form, as shown, and has an outlet pipe 33 in the roof 32, and is shaped so that the material introduced into the inlet will flow in a cyclonic manner and then emerge at the outlet 33.
  • a valved pipe 81 leads from the hopper 80 to an inlet 34 in the outlet pipe 33.
  • a pipe 41 leads from the pipe 33 to the reaction chamber system 40 which is of looped pipe form. As shown, an inlet 42 for the optional addition of additives is present in the pipe 41.
  • a pipe 51 leads to the separation tank 50 which has an outlet tap 52 for removal of the aqueous phase. The organic phase is passed to other tanks, not shown, for collection.
  • the method of the invention is performed as follows.
  • the aqueous dispersion to be treated is pumped by pump 12 along the pipe 11 to the first mixing chamber 20 at a pressure of about 3.5 bar, regulated by the pressure gauge 15.
  • the pressure level is ensured by means of the three way valve 14 which, as illustrated, provides a feedback system which also serves as a means of mixing the waste dispersion.
  • the hopper 60 contains a microsuspension comprising aluminium sulphate bound up in a bentonite clay in an aqueous phase containing dissolved aluminium sulphate.
  • the suspension may however be selected from those specified earlier.
  • the microsuspension is introduced into the first mixing chamber 20 via the fixed metal full cone nozzle which is arranged to generate a fine spray of the microsuspension.
  • the two components are encouraged to circulate in a cyclonic fashion down through the chamber to the outlet 24 at which point they are passed towards the second mixing chamber 30.
  • the mixture remains in the first chamber 20 for a very short time period, which is considered to be insufficient for the pH to rise above the value at which foaming of the liquid can occur.
  • the inhibition of foaming is important as foam will reduce the degree of contact between the microsuspension and the dispersion and initiate premature floatation.
  • the aerator 70 is arranged to generate tiny air bubbles, about 400 micron average diameter, at the rate of about 30 billion/cu.metre. These are introduced into the microsuspension/dispersion in the pipe 24. The aerated mixture is then passed to the second mixing chamber 30.
  • the second reaction chamber 30 is constructed as the first but the outlet 33 is at the top of the reaction chamber as opposed to the base.
  • the diagram illustrates the primary and secondary cyclonic circulation of the mixture, which is arranged to avoid the build up of solid material on the interior walls by control of the centrifugal forces generated.
  • the flocculant in the hopper 80 is added to the gasified mixture at a point just above the outlet of the second mixing chamber 30 as it is the region of maximum turbulence.
  • the flocculant acts as a bridging agent and encourages the agglomeration and precipitation of all the micro-agglomerations (pin-point floe) formed as a result of the turbulent mixing of the microsuspension and the dispersion.
  • the flocculated aerated mixture is passed through the looped reaction chamber 40, to allow the organic agglomerates to form a separate organic phase layer. If additives are required, they can be introduced via the inlet 42.
  • the two phases are passed to the tank 50, where the organic phases can be separated in known manner.
  • the organic phase tends to form a sludge or precipitate when allowed to stand in a tank.
  • the air introduced as bubbles escapes from the interstitial sites within the precipitate so increasing the density and leaving a honey-comb like structure within the solid mass.
  • the microsuspension may be prepared using a homogeniser; the salt may be ferric chloride or a bivalent salt or the like; the surfactant may be other than that named; the gas need not be air; the flocculant may be anionic.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Colloid Chemistry (AREA)

Abstract

Une dispersion stable comprenant de l'eau et des fluides moteurs usés est décomposée en eau pure et en déchets jetables lorsqu'on la fait réagir avec un additif composé d'un agent de séparation mis en suspension avec un porteur. De préférence, l'agent de suspension se compose d'un agent tensioactif amphotérique. De préférence, on effectue l'addition en soumettant le mélange produit à une turbulence, après quoi les phases sont isolées.
PCT/GB1991/002003 1990-11-15 1991-11-13 Traitement de dispersions Ceased WO1992008533A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB9024860.0 1990-11-15
GB909024860A GB9024860D0 (en) 1990-11-15 1990-11-15 Treatment of dispersions

Publications (1)

Publication Number Publication Date
WO1992008533A1 true WO1992008533A1 (fr) 1992-05-29

Family

ID=10685429

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/GB1991/002003 Ceased WO1992008533A1 (fr) 1990-11-15 1991-11-13 Traitement de dispersions

Country Status (3)

Country Link
AU (1) AU8879691A (fr)
GB (1) GB9024860D0 (fr)
WO (1) WO1992008533A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2308312A (en) * 1994-07-27 1997-06-25 Fsk Inc Oil separating method
EP1146016A1 (fr) * 2000-04-14 2001-10-17 Fariwar Umwelttechnik GbR Procédé de prétraitement des eaux chargées de matière organique
WO2004037729A1 (fr) * 2002-10-23 2004-05-06 Halliburton Energy Services, Inc. Procedes de fabrication de compositions pour le traitement de l'eau et compositions elles-memes
US6960303B2 (en) 2002-05-16 2005-11-01 Halliburton Energy Services, Inc. Alum pellets
US8926838B2 (en) * 2007-02-09 2015-01-06 Environmental Stewardship Solutions Method for recovering suspended solids from residual effluents
US11008227B2 (en) * 2019-07-29 2021-05-18 Eco Water Technologies Corp Wastewater purification system

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3932282A (en) * 1972-09-05 1976-01-13 Tenco Hydro/Aerosciences, Inc. Dissolved air floatation system
US3948770A (en) * 1973-08-03 1976-04-06 Exxon Research And Engineering Company Method for clarifying oily water mixtures
US3950296A (en) * 1972-04-28 1976-04-13 The Dow Chemical Company Reversible coacervation of anion-containing aqueous disperse systems with amphoteric polyelectrolytes
DE2527987A1 (de) * 1975-06-24 1977-01-13 Piepho Abwassertech Ralf F Mittel zur abwasserreinigung und verfahren zu seiner herstellung
EP0000674A1 (fr) * 1977-07-21 1979-02-07 TECHNIME S.A. Société anonyme dite: Procédé de cassage d'émulsions et moyens permettant de mettre en oeuvre ce procédé.
FR2448939A1 (fr) * 1979-02-13 1980-09-12 Degremont Procede pour faciliter la separation, par flottation, notamment d'emulsions
US4492636A (en) * 1983-02-11 1985-01-08 Eaton Corporation Process for cleaning metal working fluids for re-use
EP0306559A1 (fr) * 1987-09-08 1989-03-15 RWO Maschinenfabrik Armaturen- und Apparatebau GmbH Installation de flottation
EP0350174A2 (fr) * 1988-06-20 1990-01-10 Somafer S.A. Traitement de dispersions aqueuses

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3950296A (en) * 1972-04-28 1976-04-13 The Dow Chemical Company Reversible coacervation of anion-containing aqueous disperse systems with amphoteric polyelectrolytes
US3932282A (en) * 1972-09-05 1976-01-13 Tenco Hydro/Aerosciences, Inc. Dissolved air floatation system
US3948770A (en) * 1973-08-03 1976-04-06 Exxon Research And Engineering Company Method for clarifying oily water mixtures
DE2527987A1 (de) * 1975-06-24 1977-01-13 Piepho Abwassertech Ralf F Mittel zur abwasserreinigung und verfahren zu seiner herstellung
EP0000674A1 (fr) * 1977-07-21 1979-02-07 TECHNIME S.A. Société anonyme dite: Procédé de cassage d'émulsions et moyens permettant de mettre en oeuvre ce procédé.
FR2448939A1 (fr) * 1979-02-13 1980-09-12 Degremont Procede pour faciliter la separation, par flottation, notamment d'emulsions
US4492636A (en) * 1983-02-11 1985-01-08 Eaton Corporation Process for cleaning metal working fluids for re-use
EP0306559A1 (fr) * 1987-09-08 1989-03-15 RWO Maschinenfabrik Armaturen- und Apparatebau GmbH Installation de flottation
EP0350174A2 (fr) * 1988-06-20 1990-01-10 Somafer S.A. Traitement de dispersions aqueuses

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2308312A (en) * 1994-07-27 1997-06-25 Fsk Inc Oil separating method
US5811013A (en) * 1994-07-27 1998-09-22 Fsk Inc. Oil separating method
EP1146016A1 (fr) * 2000-04-14 2001-10-17 Fariwar Umwelttechnik GbR Procédé de prétraitement des eaux chargées de matière organique
US6881346B2 (en) 2002-05-16 2005-04-19 Halliburton Energy Services, Inc. Methods of treating phosphate in a body of water
US6960303B2 (en) 2002-05-16 2005-11-01 Halliburton Energy Services, Inc. Alum pellets
WO2004037729A1 (fr) * 2002-10-23 2004-05-06 Halliburton Energy Services, Inc. Procedes de fabrication de compositions pour le traitement de l'eau et compositions elles-memes
US8926838B2 (en) * 2007-02-09 2015-01-06 Environmental Stewardship Solutions Method for recovering suspended solids from residual effluents
US11008227B2 (en) * 2019-07-29 2021-05-18 Eco Water Technologies Corp Wastewater purification system
US11084737B1 (en) 2019-07-29 2021-08-10 Eco World Water Corp. System for treating wastewater and the like

Also Published As

Publication number Publication date
GB9024860D0 (en) 1991-01-02
AU8879691A (en) 1992-06-11

Similar Documents

Publication Publication Date Title
US4031006A (en) Vortex coagulation means and method for wastewater clarification
US4203837A (en) Process for removal of discrete particulates and solutes from liquids by foam flotation
US6960294B2 (en) Apparatus for the separation of solids from liquids by dissolved gas floatation
CA2301583C (fr) Dispositif melangeur
US6146525A (en) Apparatus and methods for separating particulates from a particulate suspension in wastewater processing and cleaning
US20040031742A1 (en) Methods and apparatus for oil demulsification and separation of oil and suspended solids from produced water
US3994808A (en) Treating contaminated liquids
US6949195B2 (en) System and method for removing contaminants from liquid
Palaniandy et al. Dissolved air flotation (DAF) for wastewater treatment
Colic et al. The development and application of centrifugal flotation systems in wastewater treatment
Van Ham et al. The effect of air distribution on the induced air flotation of fine oil in water emulsions
WO1992008533A1 (fr) Traitement de dispersions
Rubio et al. Treatment of washrack wastewater with water recycling by advanced flocculation–column flotation
US5133870A (en) Treatment of aqueous dispersions
CN105668858A (zh) 处理压缩机排出的含油污水的方法及配套设备
CA2635792A1 (fr) Installation de traitement de l'eau produite par craquage
JP3582036B2 (ja) 気液接触装置
Moosai et al. Oily wastewater cleanup by gas flotation
Colic et al. New developments in mixing, flocculation and flotation for industrial wastewater pretreatment and municipal wastewater treatment
US20120298588A1 (en) Removal of contaminants from water systems
JP2892604B2 (ja) 溶解空気浮選および同様な気液接触操作の為の方法と装置
Puget et al. Comparative study of flotation techniques for the treatment of liquid effluents
KR100759201B1 (ko) 계면활성제의 특성과 이송펌프의 압력분사를 이용하여 기포의 크기를 조절할 수 있는 계면활성제 미세기포 발생장치와 방법
KR20000056761A (ko) 미세기포발생장치를 이용한 폐수처리시스템 및 폐수처리방법
CN118221208B (zh) 一种超空化微气泡发生装置及发生方法

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AT AU BB BG BR CA CH CS DE DK ES FI GB HU JP KP KR LK LU MC MG MN MW NL NO PL RO SD SE SU US

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE BF BJ CF CG CH CI CM DE DK ES FR GA GB GN GR IT LU ML MR NL SE SN TD TG

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: CA