WO2000021633A1 - Systeme combine d'hydrocyclone et de filtre utile pour le traitement de liquides - Google Patents

Systeme combine d'hydrocyclone et de filtre utile pour le traitement de liquides Download PDF

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Publication number
WO2000021633A1
WO2000021633A1 PCT/US1999/024113 US9924113W WO0021633A1 WO 2000021633 A1 WO2000021633 A1 WO 2000021633A1 US 9924113 W US9924113 W US 9924113W WO 0021633 A1 WO0021633 A1 WO 0021633A1
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WO
WIPO (PCT)
Prior art keywords
liquid
hydrocyclone
filtration
fluid stream
fluid
Prior art date
Application number
PCT/US1999/024113
Other languages
English (en)
Inventor
Dwain E. Morse
Raffael V. M. Jovine
Michael P. Morse
Dean E. Hendrickson
Original Assignee
Zpm, Inc.
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 Zpm, Inc. filed Critical Zpm, Inc.
Priority to AU64318/99A priority Critical patent/AU6431899A/en
Priority to CA002313696A priority patent/CA2313696A1/fr
Priority to EP99952007A priority patent/EP1037695A1/fr
Publication of WO2000021633A1 publication Critical patent/WO2000021633A1/fr

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Classifications

    • 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
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1431—Dissolved air flotation machines
    • 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
    • B03D1/00—Flotation
    • B03D1/02—Froth-flotation processes
    • 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
    • B03D1/00—Flotation
    • B03D1/02—Froth-flotation processes
    • B03D1/028—Control and monitoring of flotation processes; computer models therefor
    • 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
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1412—Flotation machines with baffles, e.g. at the wall for redirecting settling solids
    • 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
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1418—Flotation machines using centrifugal forces
    • 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
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1418—Flotation machines using centrifugal forces
    • B03D1/1425—Flotation machines using centrifugal forces air-sparged hydrocyclones
    • 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
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1443—Feed or discharge mechanisms for flotation tanks
    • B03D1/1462—Discharge mechanisms for the froth
    • 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
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1493—Flotation machines with means for establishing a specified flow pattern
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C11/00—Accessories, e.g. safety or control devices, not otherwise provided for, e.g. regulators, valves in inlet or overflow ducting
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
    • B04C3/06—Construction of inlets or outlets to the vortex chamber
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
    • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
    • B04C5/14—Construction of the underflow ducting; Apex constructions; Discharge arrangements ; discharge through sidewall provided with a few slits or perforations
    • 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
    • C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/20—Nature of the water, waste water, sewage or sludge to be treated from animal husbandry
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
    • C02F2103/322—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters from vegetable oil production, e.g. olive oil production
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
    • C02F2103/327—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters from processes relating to the production of dairy products

Definitions

  • This invention relates generally to large scale industrial liquid conditioning and
  • filtration systems and more specifically to liquid conditioning components, methods and systems including membrane filtration technologies to separate particulates, gases and fluid bound compounds from fluid streams.
  • Filtration technologies that are used to separate particulate matter and gases from fluid solutions such as wastewater are often compromised with the buildup of particulate matter on the membranes or filter media which renders the filter useless and severely disrupts the filtering process. For example, traditional static filtration mechanisms force
  • microorganisms accumulate along the surface of the filters, retarding the flow of fluid through the filters and often irreversibly degrading the performance ofthe filter surface.
  • tubular and fiber based filters are mounted on inert support media such as sintered steel or ceramics and achieve reliable performance under aggressive and harsh chemical conditions while avoiding heavy buildup of clogging agents. While these filters have proved efficient, they often
  • Filter systems differ and are selective for defined size classes of particulates and dissolved compounds. Surfaces of filters can reject compounds based on charge and their ability to diffuse through filters. Membrane filters are generally defined in terms of microfiltration, ultrafiltration, nanofiltration and reverse osmosis filtration based on the
  • Membrane filters are rated based on the flux of cleaned water across the membrane in given defined environmental conditions. The flux rate, defined as the rate
  • precleaning technologies Fundamental to the concept of precleaning technologies is the removal of components from the fluid stream that obstruct fluid flow across filters.
  • precleaning approaches include, clarification technologies and screening and removal of large particulates.
  • dispersants are generally not compatible with membrane filters.
  • cationic polymers attract negatively charged compounds and collect on the filter surface disrupting the filtration process. This severely limits the potential utility of polymeric coagulants as effective precleaning agents and are therefore generally avoided. For this
  • polymeric coagulants and other chemical treatments methods may be used prior to and in conjunction with the membrane filtration system.
  • the present invention is directed to the use of a conditioning chamber in combination with various forms of filtration systems designed to remove particulates, including solids, microbes colloids and microscopic gas bubbles in a fluid stream.
  • the combination of pre-treating fluid with the hydrocyclone system prior to filtering the fluid stream in filtering systems results in a dramatically more efficient fluid treatment system and at a significantly reduced cost.
  • Various embodiments ofthe invention are directed to one or more hydrocyclone systems in isolation or in combination with separation tanks in the fluid stream before, or interspersed between, various filtration systems.
  • Preferred embodiments include hydrocyclone systems that reduce the load of filter fouling components from the fluid
  • Such points include the source of the fluid load components where these components are generated, collection points where
  • the separation tank ofthe present invention incorporates features which optimize
  • TKN Total Dissolved Solids
  • TDS Total Dissolved Solids
  • prefilter chemical treatment is permissible and greatly improves the operation of the overall system.
  • Figure 1 is a block diagram of the liquid conditioning system according to one embodiment ofthe invention
  • Figure 2 is a side perspective view of one embodiment of a conditioning chamber
  • Figure 3 is a top plan view of a liquid conditioning chamber
  • Figure 4 is a cross-sectional view of a liquid conditioning chamber
  • Figure 5 is a cross-sectional view of another embodiment of a liquid conditioning chamber
  • Figure 6 is a cross-sectional view of a liquid conditioning chamber
  • Figure 7 is a partial cross-sectional view of a collector apparatus
  • Figure 8 is a cross-sectional view along lines 10 -10 of Figure 7;
  • Figure 9 is a perspective view ofthe collector apparatus of Figure 7;
  • Figure 10 is a partial vertical cross-sectional view along lines 12-12 of Figure 9;
  • Figure 11 is a cross-sectional view of one embodiment of a skimmer apparatus
  • Figure 12 is a block diagram of the fluid conditioning system described in
  • Figure 13 is a block diagram of the fluid conditioning system described in
  • Figure 14 is a block diagram of the fluid conditioning system described in
  • Example 3; Figure 15 is a block diagram of the fluid conditioning system described in
  • Figure 16 is a block diagram of the fluid conditioning system described in
  • Figure 17 is a cross-sectional view of one embodiment of a hydrocyclone system
  • Figure 18 is a cross-sectional view of another embodiment of a hydrocyclone
  • TSS Total Suspended Solids
  • FOG are encountered in the fluid stream, a major source of contaminants is encountered in the effluent from the cannery.
  • a three pass chemistry enhanced system is appropriate.
  • Each pass constitutes the pumping of the cannery effluent through a hydrocyclone system (defined as a cylinder or chamber into which a fluid stream is directed and swirled on the inside wall, thereby generating centrifugal forces in the fluid) which is independently sparged and from which the contaminants are floated to the surface of a flotation or
  • the fluid before the first pass, the fluid is pumped from a collection sump and the pH is adjusted to reduce the surface charges to relative electro-neutrality or near zero Zeta-potential (ZP).
  • ZP Zeta-potential
  • the fluid is pumped from the sump source directly over a coarse screen to remove large solids and debris from the stream. From a collection box of the screening device the fluid is
  • a high molecular weight, high charge density cationic polyacrylamide polymer or other cationic reagent is injected at a concentration as required (e.g., 10- 15 ppm C-498, Cytec Industries).
  • a liquid conditioning system according to a first embodiment of the present invention, generally designated 30, includes a plurality of modularized components to progressively process an influent carrier liquid stream 32 originating from a solution source (not shown).
  • the respective modules include a conditioning chamber 36 which may be a hydrocyclone system disposed downstream of
  • the conditioning chamber 36 or hydrocyclone system may be open
  • conditioning chamber 36 or hydrocyclone system may be closed at the top which results in a closed liquid vortex creating a partial vacuum or significantly lower than atmospheric gas pressure when liquid is passed through.
  • the input to the conditioning chamber provides for the application of agents to modify the surface chemistry, such as chelating agents, detergents, surfactants, gases, salts, acids and flocculants, at 37, to promote the coagulation and/or modify the desired
  • a separation or flotation tank 130 Positioned proximate the conditioning chamber output is a separation or flotation tank 130.
  • the unique modularized construction above allows efficient particle and gas flotation and separation for a wide spectrum of industries and applications while minimizing the footprint, and consequently the size, ofthe overall system. Particles or particulate matter
  • the input to the conditioning chamber or hydrocyclone 36 also allows for delivery, at 37, of surface chemistry such as
  • liquid or solid coagulant agents and polymer compounds or other forms of applied energy e.g., electromagnetic, sonic, ionic, and the like
  • applied energy e.g., electromagnetic, sonic, ionic, and the like
  • One form of energy is disclosed in co-pending
  • the particles may then be extracted from the liquid by introducing large quantities of air, or gas bubbles, to which the particles have a greater likelihood of
  • gas bubbles such as air, ozone, or chlorine
  • the conditioning chamber 36 that preferably comprises an air-sparged hydrocyclone or referred to just as a hydrocyclone.
  • the hydrocyclone creates a predetermined spectrum of bubble sizes from less than one micron to several hundred microns in very large quantities.
  • the air-to-water ratio created in the chamber ranges from approximately 2:1 to 50:1, with relative velocities of particles and bubbles of approximately one meter per second. These high ratios and velocities ensure that bubbles and particles collide instantaneously to form an association. This is especially important for small colloidal particles.
  • the relatively large ratio of gas/water and small bubble size creates orders of magnitude more surface area for gas transfer from the solution into the
  • a fundamental principle of the hydrocyclone is derived from the centrifugal acceleration of particles, colloidal suspensions, oils and waters in the spinning fluid ribbon along the inside wall of the hydrocyclone tube. This causes classification by relative densities as well as kinetic coalescence of oil-in-water emulsion, forming larger
  • the other advantage is the sparging of gases through the walls ofthe porous hydrocyclone wall. This permits large volumes of gases, such as air, to be sheared by the spinning fluid layer into bubbles of a large size range.
  • the velocity ofthe fluid ribbon determines the bubble size inside the fluid layer and in combination with surfactants the bubble size can be controlled to
  • the hydrocyclone of the present invention offers several advantages over other flotation systems. For example, air to water ratios of 2:1 - 100:1 can be utilized rather than the maximal 0.15:1 in DAF systems.
  • the bubble size can be optimally tuned to match the particle or suspension components that need to be removed from the fluid stream.
  • this portion of the fluid stream is very effective at mixing and instantaneously dispersing chemical additives that improve the formation and stability
  • hydrocyclone 36 ensures instantaneous reaction and adjustment of the surface chemical forces in the hydrocyclone system.
  • Many applications of the hydrocyclone system require no chemical enhancements such as the use of polymers.
  • chemical enhancements when chemical enhancements are used, sufficient chemical quantities to achieve optimal flotation are often achieved at a concentration of 10 - 30% of those used in DAF or chemical precipitation. This results in operational cost savings as well as reducing the overall chemical burden on the fluid treatment system.
  • the tube includes an interior wall 42 (Fig.
  • FIG. 6 An enlarged cylindrical hollow housing 48 is disposed concentrically around the first tube to form an annular chamber 50.
  • the chamber includes a gas inlet 448 (Fig.
  • the porous tube 40 may be of a porosity having pore sizes within the range of about 20 to 40 microns. The shearing action of the high velocity water passing by the pores creates bubbles ranging from sub-micron to several hundred microns in size.
  • the hydrocyclone 36 further includes a solution input apparatus or accelerator 52 mounted to the proximal end ofthe housing 48 of the hydrocyclone.
  • the input apparatus may take many forms and acts to manipulate and tangentially direct the flow of input liquid into a helical ribbon- like stream through the liquid passage 42 to eventually exit into the separation tank 130.
  • Figure 3 illustrates one form of input apparatus comprising a fixed restrictor 54
  • the restrictor preferably generates an essentially continuous ribbon of solution that swirls around the inner wall of the hydrocyclone. To avoid turbulence that can disrupt the
  • the hydrocyclone 36 may be an open top, induced air hydrocyclone in which the hydrocyclone is not gas sparged.
  • the accelerator head 52 is opened to the atmosphere (see opening
  • hydrocyclone system operates on the principle that high gravity loading centrifucated fluid induces very small bubbles dissolved in the fluid to move through the thin layer of fluid and contact the appropriately sized contaminants in the fluid to form bubble-particle aggregates.
  • the accelerator head 52 also two has opening 51 and 53 for inserting chemicals wherein the openings normally remain sealed. While within the hydrocyclone 36, the bubble-particle aggregates spiral down the length of the
  • the bubble-particle aggregates float to the surface ofthe separation tank to further aggregate into a large mass aggregation where the aggregation can be removed with a
  • the hydrocyclone system 36 may be a closed top, no air hydrocyclone system, whereby the accelerator head 52 is totally closed to the atmosphere as shown in Figure 18. In this embodiment, there is no gas sparging.
  • the hydrocyclone 36 preferably includes at its outlet a collector apparatus, generally designated 80, to capture and controUably direct substantially particle-free solution.
  • the collector apparatus 80 includes a conical- shaped splay section 82 coupled axially to the hydrocyclone outlet via a coupling ring 84
  • the splay section is formed with a plurality of radially spaced-apart splay vectors (not shown) to urge the separated solution into a modified downwardly directed flow.
  • the splay section may also be formed in a straight cylindrical configuration without any loss in performance.
  • the collector apparatus 80 further includes a torus-shaped trough 90 (see Figure 8) formed with an annular slot 102 and mounted to the distal end ofthe splay section 82.
  • the slot includes an engagement edge or skimmer 101 positioned axially in-line with the expected laminar separation between particle-rich froth, and relatively particle-free solution to skim the separated particle-free solution
  • the trough includes a unidirectional solution stop 103 ( Figure 8) and an outlet formed into an
  • the central portion ofthe trough defines an exit passage
  • the separation tank 130 is positioned downstream ofthe hydrocyclone 36 and is substantially filled with the output ofthe hydrocyclone.
  • the separation tank may take the form of a modified dissolved air flotation (DAF) tank ( Figure 2), with an open top to receive the separated solution and the froth from the hydrocyclone.
  • a froth skimmer 135 having a plurality of paddles 137 is positioned at the surface ofthe tank to
  • an effluent outlet 140 is formed near the bottom portion ofthe tank.
  • the separation tank 130 is positioned downstream from a solution source that generates an untreated carrier liquid containing one or more varieties of particles or gases.
  • a solution source that generates an untreated carrier liquid containing one or more varieties of particles or gases.
  • untreated carrier liquid originates from four separate sources: a cannery source; a vat
  • untreated carrier liquid untreated wastewater
  • untreated wastewater is first filtered through a coarse screen to remove large solids and then collected in a large reservoir tank.
  • the untreated wastewater may optionally be pre-treated at this point by adding surface chemistry, at 37, to urge the
  • the pH ofthe water may also be adjusted at this point.
  • the water is then pumped to the hydrocyclone 36.
  • the hydrocyclone input apparatus 52 receives the carrier liquid stream and restricts the stream to a narrow ribbon, consequently accelerating the
  • the sparged gas plenum 448 injects gas bubbles into the solution stream.
  • the bubbles collide with particles in the solution and gases dissolved in the water transfer from the higher concentration in the water to the lower concentration in the bubbles. This process forms a froth that floats towards the center of the containment
  • hydrocyclone on the solution creates a non-turbulent flow between the relatively particle- free solution and the particle-rich froth. It has been discovered that by controlling the ribbon, a more uniform and turbulent-free ribbon through the hydrocyclone results.
  • the outwardly splaying solution is selectively captured by the trough 115 and directed
  • the performance of the collector apparatus is substantially improved by employing the optional skimming apparatus 116
  • the effluent from the collection tank is then pumped into a second
  • hydrocyclone for a second pass.
  • this pass which is treated at the same (or slightly higher) flow rate compared to the first pass, the pH may be adjusted and cationically treated effluent is divided into a parallel hydrocyclone systems where a very high molecular weight anionic, polyacrylamide polymer may be injected (e.g., 5 ppm A-130
  • the effluent is then further treated in a series of filtration membrane steps which include in sequence bag filtration, ultrafiltration and reverse osmosis which will be described in greater detail in the Examples. Other filtration steps maybe included such as disc filtration, sand filtration, cross membrane filtration and fine screen filtration. These filtration steps remove particulates less than 2 mm in diameter.
  • the treated effluent may then be further treated in activated carbon filters and chlorine dioxide and ozone treatments.
  • Alternative chemical combinations than the ones stated previously may be used in activated carbon filters and chlorine dioxide and ozone treatments.
  • fluid streams containing petrochemical products and metal contaminants may require alternative coagulants instead of pH adjustment before the first
  • Inorganic compounds such as aluminum salts or organic coagulants such as polyamines may be more appropriate conditioning agents than pH adjustments. These can be injected into the fluid stream, ahead ofthe hydrocyclones or directly into the hydrocyclones.
  • Other agents that can be used to improve flotation include detergents or surfactants (e.g., non-ionic nonyl-phenols or anionic sodium
  • dodecyl sulfate that reduce the surface tension of the fluid and thereby reduce the bubble size as the gas is sheared off the wall of the sparge tubes.
  • Hydrocyclones containing only surfactants have been very successful at emulsion breaking of both polar and non-polar oils, found in the food processing and petrochemical industries respectively.
  • Other claimed combinations may include metal chelating agents that are
  • VOC light organic compounds
  • the initial disinfecting gas may be stripped or removed in subsequent passes through hydrocyclones sparged with inert or non-reactive gasses such as nitrogen or air.
  • inert or non-reactive gasses such as nitrogen or air.
  • Examples or removal rates of reactive gasses in non-chemical applications with hydrocyclones are commonly 30 - 50% per pass. Sequential passes of fluid through hydrocyclones have removed VOC and reactive gasses to non-detectable levels.
  • the ai ⁇ water ratios can be adjusted to 7: 1 - 10:1. This introduces more bubbles and opportunities for particles and microbes to attach and be floated out ofthe system, even if they are less tightly associated than in chemically enhanced systems. In streams that contain free oils or in oil-in-water emulsions, high G forces or acceleration can also be advantageous.
  • several smaller ID sparge tubes may be run in parallel. For example, a 2" ID sparge tube for a given flow rate produces proportionately higher
  • membrane filtration systems are attainable. Some of these systems are illustrated in the
  • Example I which is illustrated in Figure 12, shows an example of non-chemical treatment of effluent from several sources in olive processing.
  • Effluent or waste water is collected from several sources such as a cannery source 202, a vat room source 204, a flume source 206 and a pitter source 208.
  • Waste water or effluent is then filtered through coarse screens 210 to remove large solids and debris from the effluent sources.
  • the effluent is then collected in a large storage tank 212 of approximately 10 6 gallons and the effluent is at an ambient temperature of approximately 70° - 90 °F.
  • the effluent is then pumped and divided into a parallel row of three hydrocyclone systems 214A - 214C
  • each hydrocyclone system feeds effluent into an attached separation tank 30 as shown in Figure 2 which removed the bulk of the froth and associated bubble-particle aggregates by froth skimmer 138.
  • Each hydrocyclone has an inner diameter of 6" and a length of 28". The average flow of effluent through each hydrocyclone is
  • hydrocyclone ranges from 2.5 psi to 6 psi. Thickness ofthe helical film ranges from 1/4 inch to 1 inch and the air to water ratio ranges from 2:1 to 10:1.
  • the effluent was then pumped to a second central volume control tank 216 where resulting froth and bubble-particle aggregates are skimmed off of the surface of the
  • a bag filter system 222 comprised of static filtration bags (not cross flow) with 100 micron pore size (10 bags of approximately 3
  • the membrane 224 comprised of 6 banks of 8" type JX constant pressure, variable flow filters manufactured by Osmonics.
  • the membrane consists of spiral wound polyvinylidene diflouride.
  • the water was pumped through volume control tank 226 to a reverse osmosis filtration step at 228.
  • the reverse osmosis filter comprised of a constant flow, variable pressure trilaminate type AG, Osmonic filter.
  • the effluent was then passed through an activated carbon filter 230 and a chlorine dioxide and ozone disinfection step 232.
  • the hydrocyclone system processing resulted in significant improvement to the
  • the bag filter replacement time increased to 4 - 8 hours.
  • the chart below demonstrates the increase in runtime (defined as time from the start ofthe first bank of filter to startup of last bank. Banks are operated sequentially to a minimum flux before switching to the next bank), flux, number of banks used to treat the same volume of water and the runtime to shut down.
  • hydrocyclone systems ofthe present invention for treating the fluid stream demonstrate a significant increase in runtime of the ultrafilters with a
  • Example II which is illustrated in Figure 13, illustrates an example of non-
  • the object was microbe removal from a 350,000 gallon storage tank and to treat up to 400,000 gallons
  • the wastewater or effluent from the cheese processing source 240 was pumped to a collection sump 242 and then pumped to a 350,000 gallon volume control or equalization tank 244.
  • the effluent was then pumped to three parallel hydrocyclone systems 246 with inner diameters of 6" and lengths of 27".
  • Each hydrocyclone system
  • the effluent was delivered through the hydrocyclone systems 246 and into
  • microbes from growing in the stored water.
  • the effluent was then pumped and filtered through a nylon fiber screen 248 manufactured by Laikos.
  • the pH of he effluent was then adjusted by the additional
  • Example III which is illustrated in Fig. 14, shows an example of treatment of
  • TSS Total Suspended Solids
  • COD Chemical Oxygen Demand
  • the waste water from the source 240 was pumped into a collection sump and then
  • Each hydrocyclone system was capable of processing 320 gallons per minute.
  • Each hydrocyclone system had a stainless steel porous tube with 40 um pore size.
  • the plenum pressure of the gas ranged from 3 to 5 psi, air:water ratio was maintained at 4:1 and the water temp averaged at 128° F.
  • the pH of the effluent was
  • the effluent was delivered through the hydrocyclone systems 246 and into separation tanks 30 as illustrated in Figure 2 which removed froth by froth skimmer 138.
  • the effluent was then pumped and filtered through a nylon fiber screen 248 manufactured by Laikos.
  • the pH ofthe effluent was adjusted by the addition of NaOH
  • Example IV shown in Figure 15, demonstrates an example of non-chemical
  • the objective was fat/oil/grease [FOG] removal to increase flux rates and to increase run time before filter failure.
  • the effluent was recirculated through a cooling tower 256 to cool the effluent to less than 40° F and then pumped to a first series of two hydrocyclones 258 in series
  • the hydrocyclone systems 258 each have a positive displacement blower type.
  • the flow rate of the water ranged from 5 to 12 GPM. The water was
  • the effluent was then pumped to a surge tank 262 where the effluent was heated to roughly 120° F.
  • the effluent was then pumped to an ultrafiltration system with polysulfone membranes manufactured by Koch with pore sizes of 0.02 um.
  • the effluent was then pumped to an ultrafiltration system with polysulfone membranes manufactured by Koch with pore sizes of 0.02 um.
  • the overall flux rate ofthe ultrafilter showed a 40%
  • Example V shown in Figure 16, is similar to Example 4, but uses the addition of
  • Effluent from an 80,000 gallon poultry chiller 254 was circulated through a cooling tower 256 to cool the effluent to 40° F.
  • the effluent was pumped to the first hydrocyclone 258 ofthe type described in Example IV. However, prior to the effluent
  • hydrocyclones system 2508 a high molecular weight medium charge density, cationic polyacrylamide polymer was added to the effluent source at a concentration of
  • polyacrylamide polymer was added [A- 130 HMW Cytec Industries at 5 ppm]. After passage through the hydrocyclone system set 260 the effluent passed through attached separation tanks 30 for the removal ofthe froth.
  • the effluent was then pumped to a surge tank 262 from where the effluent was then pumped to an ultrafiltration system with polysulfone membranes manufactured by

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  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Biotechnology (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Physical Water Treatments (AREA)

Abstract

L'invention concerne un procédé servant à traiter un liquide provenant d'une source de liquide et à séparer des matières particulaires du liquide, qui comporte les étapes consistant à: prévoir une source de liquide; pomper ladite source de liquide (3) dans au moins un système d'hydrocyclone (30), ladite source de liquide étant injectée par gaz (448); recueillir ladite source de liquide (130) et éliminer les particules séparées en flocons (137) de la surface; et filtrer ladite source de liquide à l'aide d'au moins un filtre.
PCT/US1999/024113 1998-10-13 1999-10-13 Systeme combine d'hydrocyclone et de filtre utile pour le traitement de liquides WO2000021633A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
AU64318/99A AU6431899A (en) 1998-10-13 1999-10-13 Combined hydrocyclone and filter system for treatment of liquids
CA002313696A CA2313696A1 (fr) 1998-10-13 1999-10-13 Systeme combine d'hydrocyclone et de filtre utile pour le traitement de liquides
EP99952007A EP1037695A1 (fr) 1998-10-13 1999-10-13 Systeme combine d'hydrocyclone et de filtre utile pour le traitement de liquides

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US10417598P 1998-10-13 1998-10-13
US60/104,175 1998-10-13

Publications (1)

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WO2000021633A1 true WO2000021633A1 (fr) 2000-04-20

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010041090A1 (fr) * 2008-10-07 2010-04-15 Sveuciliste U Dubrovniku Procédé et installation de navire pour l'inactivation d'organismes planctoniques dans un ballast d'eau par des forces hydrodynamiques
CN105858965A (zh) * 2016-05-18 2016-08-17 中北大学 超重力强化纳米零价铁-臭氧法深度处理硝基苯废水的方法及装置
WO2016153458A1 (fr) * 2015-03-20 2016-09-29 Mcdonald Robert Ramsey Système de filtration d'eau à 3 étages à collecteur avec élimination des métaux lourds
ES2628029R1 (es) * 2016-01-27 2017-11-13 Sanicitrus, S.L. Sistema de depuración, desinfección y reutilización del agua empleada en medios de lavado y tratamiento de productos cosechados
CN115285988A (zh) * 2022-08-31 2022-11-04 浙江碳一新能源有限责任公司 一种闪蒸干燥装置及其提高球形石墨pH值的纯化工艺和球形石墨
WO2022232877A1 (fr) * 2021-05-04 2022-11-10 University Of Tasmania Système de filtre

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US3784468A (en) * 1971-09-20 1974-01-08 Exxon Production Research Co System and method for separating heavier and lighter components of liquid mixtures
US4031006A (en) * 1976-03-12 1977-06-21 Swift And Company Limited Vortex coagulation means and method for wastewater clarification
US4960509A (en) * 1989-07-17 1990-10-02 Colorado School Of Mines Ore flotation device and process
EP0473566A2 (fr) * 1990-08-28 1992-03-04 Kamyr, Inc. Hydrocyclone à aspersion gazeuse
US5224604A (en) * 1990-04-11 1993-07-06 Hydro Processing & Mining Ltd. Apparatus and method for separation of wet and dry particles
US5240600A (en) * 1990-07-03 1993-08-31 International Environmental Systems, Inc., Usa Water and wastewater treatment system
WO1993023335A1 (fr) * 1992-05-19 1993-11-25 Milos Krofta Vase clarificatoire pour eau dote d'une premiere isolation de filtrat et d'un lavage a contre-courant et d'une production de bulles ameliores
US5529190A (en) * 1995-02-06 1996-06-25 Ahlstrom Machinery, Inc. Gas sparged hydrocyclone with foam separating vessel
WO1997020775A1 (fr) * 1995-12-07 1997-06-12 Purac Ab Appareil et procede de flottation
US5679257A (en) * 1994-04-06 1997-10-21 John T. Towles Industrial waste water treatment
WO1998024727A1 (fr) * 1996-12-02 1998-06-11 Z.P.M., Inc. Procede et dispositif multimodaux de traitement d'une solution
WO1999003592A1 (fr) * 1997-07-15 1999-01-28 Zpm, Inc. Procede et systeme de conditionnement de fluide

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3784468A (en) * 1971-09-20 1974-01-08 Exxon Production Research Co System and method for separating heavier and lighter components of liquid mixtures
US4031006A (en) * 1976-03-12 1977-06-21 Swift And Company Limited Vortex coagulation means and method for wastewater clarification
US4960509A (en) * 1989-07-17 1990-10-02 Colorado School Of Mines Ore flotation device and process
US5224604A (en) * 1990-04-11 1993-07-06 Hydro Processing & Mining Ltd. Apparatus and method for separation of wet and dry particles
US5240600A (en) * 1990-07-03 1993-08-31 International Environmental Systems, Inc., Usa Water and wastewater treatment system
EP0473566A2 (fr) * 1990-08-28 1992-03-04 Kamyr, Inc. Hydrocyclone à aspersion gazeuse
WO1993023335A1 (fr) * 1992-05-19 1993-11-25 Milos Krofta Vase clarificatoire pour eau dote d'une premiere isolation de filtrat et d'un lavage a contre-courant et d'une production de bulles ameliores
US5679257A (en) * 1994-04-06 1997-10-21 John T. Towles Industrial waste water treatment
US5529190A (en) * 1995-02-06 1996-06-25 Ahlstrom Machinery, Inc. Gas sparged hydrocyclone with foam separating vessel
WO1997020775A1 (fr) * 1995-12-07 1997-06-12 Purac Ab Appareil et procede de flottation
WO1998024727A1 (fr) * 1996-12-02 1998-06-11 Z.P.M., Inc. Procede et dispositif multimodaux de traitement d'une solution
WO1999003592A1 (fr) * 1997-07-15 1999-01-28 Zpm, Inc. Procede et systeme de conditionnement de fluide

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010041090A1 (fr) * 2008-10-07 2010-04-15 Sveuciliste U Dubrovniku Procédé et installation de navire pour l'inactivation d'organismes planctoniques dans un ballast d'eau par des forces hydrodynamiques
WO2016153458A1 (fr) * 2015-03-20 2016-09-29 Mcdonald Robert Ramsey Système de filtration d'eau à 3 étages à collecteur avec élimination des métaux lourds
US10829400B2 (en) 2015-03-20 2020-11-10 Aqua Clara International Incorporated Manifold 3-stage water filtration system with heavy metals removal
ES2628029R1 (es) * 2016-01-27 2017-11-13 Sanicitrus, S.L. Sistema de depuración, desinfección y reutilización del agua empleada en medios de lavado y tratamiento de productos cosechados
CN105858965A (zh) * 2016-05-18 2016-08-17 中北大学 超重力强化纳米零价铁-臭氧法深度处理硝基苯废水的方法及装置
CN105858965B (zh) * 2016-05-18 2023-04-14 中北大学 超重力强化纳米零价铁-臭氧法深度处理硝基苯废水的方法及装置
WO2022232877A1 (fr) * 2021-05-04 2022-11-10 University Of Tasmania Système de filtre
CN115285988A (zh) * 2022-08-31 2022-11-04 浙江碳一新能源有限责任公司 一种闪蒸干燥装置及其提高球形石墨pH值的纯化工艺和球形石墨
CN115285988B (zh) * 2022-08-31 2023-11-10 碳一新能源集团有限责任公司 一种闪蒸干燥装置及其提高球形石墨pH值的纯化工艺和球形石墨

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EP1037695A1 (fr) 2000-09-27
CA2313696A1 (fr) 2000-04-20

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