CN1409693A - Improvements in flotation/fractionation systems for treating liquids and in separation of liquids to be treated thereby - Google Patents
Improvements in flotation/fractionation systems for treating liquids and in separation of liquids to be treated thereby Download PDFInfo
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- CN1409693A CN1409693A CN00816986A CN00816986A CN1409693A CN 1409693 A CN1409693 A CN 1409693A CN 00816986 A CN00816986 A CN 00816986A CN 00816986 A CN00816986 A CN 00816986A CN 1409693 A CN1409693 A CN 1409693A
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- 239000007788 liquid Substances 0.000 title claims abstract description 181
- 238000005188 flotation Methods 0.000 title claims abstract description 26
- 230000006872 improvement Effects 0.000 title claims abstract description 6
- 238000000926 separation method Methods 0.000 title claims description 63
- 238000005194 fractionation Methods 0.000 title abstract description 11
- 239000006260 foam Substances 0.000 claims abstract description 29
- 239000002245 particle Substances 0.000 claims abstract description 18
- 239000002699 waste material Substances 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 28
- 230000008676 import Effects 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 20
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 claims description 19
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 19
- 238000000605 extraction Methods 0.000 claims description 19
- 239000012530 fluid Substances 0.000 claims description 18
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 17
- 239000001301 oxygen Substances 0.000 claims description 17
- 229910052760 oxygen Inorganic materials 0.000 claims description 17
- 238000001914 filtration Methods 0.000 claims description 16
- 229910002651 NO3 Inorganic materials 0.000 claims description 15
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 15
- 125000004122 cyclic group Chemical group 0.000 claims description 13
- 239000000203 mixture Substances 0.000 claims description 9
- 239000000758 substrate Substances 0.000 claims description 9
- 230000004087 circulation Effects 0.000 claims description 8
- 238000002347 injection Methods 0.000 claims description 8
- 239000007924 injection Substances 0.000 claims description 8
- 238000005086 pumping Methods 0.000 claims description 7
- 238000005273 aeration Methods 0.000 claims description 5
- 239000000284 extract Substances 0.000 claims description 5
- 230000004323 axial length Effects 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 239000012466 permeate Substances 0.000 claims description 2
- 238000007789 sealing Methods 0.000 claims description 2
- 230000005484 gravity Effects 0.000 abstract 2
- 230000002776 aggregation Effects 0.000 abstract 1
- 238000004220 aggregation Methods 0.000 abstract 1
- 241000238634 Libellulidae Species 0.000 description 33
- 102000004169 proteins and genes Human genes 0.000 description 33
- 108090000623 proteins and genes Proteins 0.000 description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 15
- 230000008569 process Effects 0.000 description 10
- 239000002028 Biomass Substances 0.000 description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 239000008246 gaseous mixture Substances 0.000 description 5
- 230000001105 regulatory effect Effects 0.000 description 4
- 241000238424 Crustacea Species 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000004804 winding Methods 0.000 description 3
- 241000894006 Bacteria Species 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 239000003657 drainage water Substances 0.000 description 2
- 238000005187 foaming Methods 0.000 description 2
- 230000008595 infiltration Effects 0.000 description 2
- 238000001764 infiltration Methods 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
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- 238000001704 evaporation Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000002414 normal-phase solid-phase extraction Methods 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
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Classifications
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- A—HUMAN NECESSITIES
- A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
- A01K—ANIMAL HUSBANDRY; AVICULTURE; APICULTURE; PISCICULTURE; FISHING; REARING OR BREEDING ANIMALS, NOT OTHERWISE PROVIDED FOR; NEW BREEDS OF ANIMALS
- A01K63/00—Receptacles for live fish, e.g. aquaria; Terraria
- A01K63/04—Arrangements for treating water specially adapted to receptacles for live fish
- A01K63/045—Filters for aquaria
-
- A—HUMAN NECESSITIES
- A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
- A01K—ANIMAL HUSBANDRY; AVICULTURE; APICULTURE; PISCICULTURE; FISHING; REARING OR BREEDING ANIMALS, NOT OTHERWISE PROVIDED FOR; NEW BREEDS OF ANIMALS
- A01K61/00—Culture of aquatic animals
- A01K61/50—Culture of aquatic animals of shellfish
-
- A—HUMAN NECESSITIES
- A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
- A01K—ANIMAL HUSBANDRY; AVICULTURE; APICULTURE; PISCICULTURE; FISHING; REARING OR BREEDING ANIMALS, NOT OTHERWISE PROVIDED FOR; NEW BREEDS OF ANIMALS
- A01K63/00—Receptacles for live fish, e.g. aquaria; Terraria
- A01K63/04—Arrangements for treating water specially adapted to receptacles for live fish
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- Life Sciences & Earth Sciences (AREA)
- Environmental Sciences (AREA)
- Marine Sciences & Fisheries (AREA)
- Animal Husbandry (AREA)
- Biodiversity & Conservation Biology (AREA)
- Zoology (AREA)
- Physical Water Treatments (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Removal Of Floating Material (AREA)
- Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
- Biological Treatment Of Waste Water (AREA)
Abstract
An improvement in a fractionation/flotation system for separating liquid containing particles of varying mass or specific gravity. A reactor vessel comprises a fractionation column and a foam aggregation chamber surmounting the column. Liquid containing the waste is pumped into the fractionation column via a first inlet and a second inlet at intermediate locations where the first inlet entry is higher than the second inlet. A waste reducing gas is injected into the second inlet immediately prior to the liquid entering the fractionation column. The separating apparatus comprises an elongated passageway, a primary lip for liquid containing particles to flow over, a secondary lip lower than the primary lip for liquid to flow over. Flow is diverted within the passageway by a suction pipe. Liquid in the pipe contains particles of relatively lower mass or specific. Liquid containing particles of higher mass or specific gravity flows out over the secondary lip.
Description
Technical field
The present invention relates to be used to comprise the improved control device of the flotation/fractionating system of reactor and particle separator.The present invention can be used as (but non-only can be used as) protein skimmer especially, comes the auxiliary treatment holding tank to contain biomass and from the liquid of the refuse of aquatic class.
In whole specification sheetss, unless need in addition in the literary composition, word " comprises (comprise) " or variant is interpreted as being meant as " comprising (comprises) " or " comprising (comprising) " and comprises the whole or whole group of being stated but do not get rid of any other whole or whole group.
Background technology
Known use comprises the flotation/fractionating system of reactor vessel in water treatment field, as " protein skimmer " of common name, to maintain the aquatic class in the holding tank.In U.S. patent No.4834872, narrated a kind of example of employed one type protein skimmer in the prior art.Such protein skimmer provides liquid from the aftertreatment of body round-robin, oxygenation in described liquid wherein, and remove remaining biomass and nitrite, its degree of treatment reaches and it can be returned in the aquarium (aquarium) or analogue that therefrom takes out described liquid and handle.Though it is effectively that this protein skimmer is applied to small-sized aquarium, because the complicacy of its design, it is not suitable for handling the liquid of comparatively large vol, and the latter is aquatic class large-scale holding tank operation is included.
In bigger tank systems, owing to the validity of cost adopts protein skimmer than simple types.In the Figure 1A of accompanying drawing and 1B, illustrate two kinds of examples of the prior art systems of in the larger slot system, using.
Figure 1A is depicted as a kind of protein skimmer design, and it comprises the single pump 11 of use, and described pump pumps through import 13 liquid from holding tank 15.The outlet 17 of pump 11 imports liquid the mid-way of the main fractionating tower 21 of reactor vessel 23 through pipe winding device 19.Described pipe unit 19 comprises the Venturi tube 25 of polyphone with it, is used for injecting ozone/oxygen mixture from concentrating the source (not shown) to pipe unit through inlet line 27, and enters separation column 21 subsequently.Reactor vessel 23 is included in the collection chamber 29 on the separation column 21, is used to collect foam, foam be in separation column 21, inject the liquid carry ozone/oxygen mixture secretly, and tower in have a come-up bubble of this gaseous mixture liquid infiltration produce.Outlet line 31 links to each other with the bottom of separation column 21, so that remove the liquid portion of the processing of bottom from reactor vessel 23, and it is returned in the holding tank 15.
As described in the U.S. patent No.4834872, by the oxygenizement of foaming through the ozone/oxygen mixture of separation column 21, reduced the nitrite and the nitrate that neutralized, and the biomass of any remnants is adsorbed by the buoyant foam that is produced, and finally is collected in the collection chamber 29.
The total amount of liquid of process reactor vessel 23 decides by the control of pump 11.This total amount influences the residence time value of liquid in reactor vessel, and to guaranteeing that it is important have the enough time to make eradicating nitrate, nitrite and biomass in the process of liquid in staying in described reactor vessel.Pump 11 also influences the flow velocity through the liquid of Venturi tube 25, thereby and influence liquid and flow the ozone carried secretly and the quantity of oxygen.Basically, the Venturi tube of flowing through speed is fast more, and the ozone that liquid stream is carried secretly and the volume of oxygen are big more.Moreover it is fast more that resulting fluid enters separation column 21, and caused turbidity is big more in separation column.Amount of gas in reactor vessel 23 has determined the pressure head of described tower, thereby and has determined the quantity of resulting liquid in separation column 21.Therefore, wish flow rate of liquid maximum, because under any circumstance Venturi tube has limited flow velocity inherently through Venturi tube 25.Also wish to be fixed on the quantity of the liquid in the reactor vessel 23, make its surface just at separation column 21 and below collection chamber 29 junctions.This has promoted the gathering at collection chamber 29 inner foams, and makes it to keep dry, thereby prevents from unnecessarily to lose liquid in flotation/fractionation treating processes.
The problem that is produced in this system is, can not control in such a way the operation of pump 11, promptly, make all parameters that influence by it carry out the best setting, particularly when realizing the optimum operation efficient of described system, a parameter must be adjusted and under the situation that another is not adjusted.
For example, when the flow rate of liquid maximum of Venturi tube 25 of wishing to flow through for aeration and flotation purpose, thereby when making the gas volume that is incorporated in the separation column 21 maximum, this can cause the too fast and amount of fluid in separation column of total treatment capacity to reduce.This be increase by the pressure head that the reactor vessel that is provided directly is provided for the ratio of gas in the reactor vessel and liquid due to.The minimizing of this amount of fluid can cause liquid level to be lower than separation column 21 and the very big distance in collection chamber 29 junctions, makes to be reduced by gaseous mixture institute liquid volume to be processed, and not every foam can both be collected in the collection chamber.For making the processing optimizing of liquid, the height of liquid need be in maximum value in reactor vessel.
Opposite is, the quantity maximum of the liquid reactor vessel 23 in, and the flow rate of liquid that need enter separation column 21 is reduced to a certain degree, makes the ratio minimizing pressure head wherein of in described tower gas and liquid, and makes the amount of fluid increase.Yet this causes the reduction of the aeration degree of the decline of turbidity and liquid and ozone and oxygen, and it is required that aeration is that liquid is suitably handled, though because the decline that total treatment capacity produces increases the residence time.
Although can reach rational compromise proposal, but because for making biomass be adsorbed in foam, thereby and from solution, be removed and the degree of the foaming that produces, depend on this fact of proteinic quantity that in liquid, contains nitrite and nitrate, and make this problem aggravation.The protein that exists from needs carry out liquid that the groove of liquid fractionation and flotation introduces is many more, and then the foam that wherein produces is many more.Because depending on, the proteinic quantity in liquid occupies the aquatic organism kind that is stored in the holding tank 15, and the operation of complete and pump 11 is irrelevant, thereby need with the total treatment capacity of influence and thereby the control of pump of the liquid residence time of influence in reactor vessel 23, with influence turbidity and in described tower the control of the flow rate of liquid of the process Venturi tube 25 of amount of fluid dissociate.
In the design of the protein skimmer shown in Figure 1B, solved this problem, wherein adopt the pipe winding device that comprises Venturi tube 25 19 from the pipe-loop on the suction side, and produce and to comprise its isolating recirculation pipe loop 33, described tube loop has its oneself pump 35.The operation of this second pump 35 is independent mutually with the main import pump 11 of the total treatment capacity of control, thereby independent mutually with total treatment capacity, the control of second pump has determined the flow velocity through the liquid of Venturi tube 25, and the quantity of the liquid in reactor vessel 23.
As depicted in the figures, the outlet 17 of first pump 1 links to each other with separation column 21 in the mid-way 36 along tower, thereby directly injects liquid to be processed therein.Therefore the flow velocity of pump 11 has determined total treatment capacity and the liquid residence time in reactor vessel 23.Recirculation pipe loop 33 has the import 37 that links to each other with the bottom of immediate separation column 21, with extraction liquids therefrom and offer second pump 35.The outlet 39 of second pump 35 links to each other with the pipe winding device 19 that comprises Venturi tube 25.The outlet of Venturi tube 25 is injected into the middle part of separation column 21 with liquid, and the position 36 of liquid is injected in the outlet 17 that this position 41 is lower than pump 11 to tower.This makes untreated liquid carry through first pump 11, thereby will be permeated by the ascending gas mixture that the outlet from Venturi tube 25 at 41 places, position is injected, increased the turbidity in tower, thereby has strengthened contacting between liquid and the gaseous mixture.The additional benefits that recirculation loop had is, is independent of the speed of pump 11, increased the residence time of liquid in reactor vessel.Outlet pipe 31 links to each other with the bottom of separation column 21, thereby removes treated liquid and it is returned in the holding tank 15 from reactor vessel 23.
On main import 13 and outlet 31 pipelines, be respectively arranged with flow velocity valve 43 and 45, so that total treatment capacity is adjusted.
Though this double pump protein skimmer design is better than previous single pump design, thereby wherein can independent controlled variable realize maximum operation efficiency, it is not that effectively because it needs second pump really, and its expense is not low on cost.In addition, it also needs to carry out balance by continue adjusting the liquid optimal number that flow velocity valve is arranged in the tower, condition be generated biomass absorption foamy quantity thereon must be depended on proteinic quantity in liquid.Then, through the adjustment of flow velocity valve, directly influence total treatment capacity, the latter is preferably maximized.
In this two kinds of protein skimmers design, generally constitute by suction pipe from the import 13 of holding tank 15.Described pipe has simply and is set directly in the holding tank or the indoor opening end of skimmer, and liquid flows to the skimmer chamber from holding tank, handles to extract out from groove.Protein skimmer is commonly used to assist the primary filter or the treating processes of the liquid in holding tank, as biofilter, and simply with liquid sucking-off from the same source of primary filter or treating processes, without any preliminary filtration or separation phase.Thereby described protein skimmer can be accepted big biomass particle, and described particle is difficult to absorption and floatingly selects in described system.This has constituted extra burden to the effectiveness of protein skimmer and the balance of system, carrying out described system balancing is for operation effectively, reduce or remove being rendered as proteinic nitrite and nitrate, and remove the solid of suspension and from liquid, remove solid by flotation with molecular level.
Summary of the invention
The purpose of one aspect of the invention provides the improved control of flotation/fractionating system, and it is with respect to the prior art systems of this paper aforementioned type, and cost is more effective and more efficient.
The present invention's purpose on the other hand provides particulate initial gross separation from liquid, promotes the further processing that it is undertaken by flotation/fractionating system or other means.
According to one aspect of the present invention, provide from the liquid that comprises refuse and removed refuse, as a kind of improvement of the flotation/fractionating system of biosolids, nitrate or nitrite, described system comprises: a separation column; Foam collection chamber on separation column; The liquid that is used for containing refuse is introduced the liquid gatherer of separation column; Be used for pumping unit through liquid-inlet device pumping liquid; Be used for before liquid is about to import separation column, in liquid, inject the gas of minimizing refuse such as the gas injection apparatus of air, oxygen or ozone; Be used to extract the foam extraction plant that is collected in foam collection chamber inner foam; With the liquid take-up gear of deriving the liquid of handling from the bottom of separation column; Improvements are:
The liquid gatherer is divided into:
(a) first liquid-inlet, the liquid that is used for containing refuse imports in the mid-way along described separation column axial length, and described first liquid-inlet has flow regulator, imports the flow velocity of the liquid in the described tower with control; With
(b) second liquid-inlet, be used for to contain simultaneously the liquid of refuse, mid-way at the described separation column axial length that is lower than described first liquid-inlet imports, described second liquid-inlet has the described gas injection apparatus that polyphone is provided with, and is used for injecting to the liquid that is about to import second liquid-inlet in the described separation column gas of described minimizing refuse;
Wherein said branching out after the present described pumping unit outlet;
And wherein can remain on best quantity, thereby make the foam that has wherein adsorbed refuse can accumulate in the described collection chamber by controlling the liquid of described setter in described separation column.
Preferably, described gas injection apparatus comprises Venturi tube, sucks the throat of described Venturi tube by the gas of the described minimizing refuse of this Venturi tube, thereby permeates in the liquid that contains refuse of the Venturi tube of flowing through, and it is carried out aeration.
Preferably, the gas of described minimizing refuse is the mixture of oxygen and ozone.
According to another aspect of the present invention, a kind of improved method is provided, be used for using flotation/fractionating system to remove refuse such as biosolids, nitrate or nitrite are controlled from the liquid that contains refuse, described system comprises: a separation column; Foam collection chamber on described separation column; Be used to extract the foamy foam extraction plant that is collected in the foam collection chamber; With the liquid take-up gear of deriving the liquid of handling from the bottom of separation column; Described method comprises:
The liquid that will contain refuse from same source, under pressure imports first and second mid-ways of separation column, and the described second position is lower than described first location;
Before liquid is about to import second mid-way of separation column, liquid as described in the gas that reduces refuse imported as air, oxygen or ozone; With
Be adjusted in the flow velocity of the liquid that first mid-way imports, will remaining on optimal number, thereby the foam that has adsorbed refuse on it accumulated in the described collection chamber at the liquid in the described separation column.
The gas of preferred described minimizing refuse is the mixture of oxygen and ozone.
Provide to be used to separate the device that contains quality or the vicissitudinous particulate liquid of proportion more on the other hand according to of the present invention, having comprised:
The passage of an extension, it has: (a) have the antetheca of elementary lip, be used for making and contain described particulate liquid and flow into described passage; (b) have the tail wall that is lower than the secondary lip that described elementary lip is provided with, be used to make liquid flow to cross and flow out described passage; (c) substrate of the described channel bottom of sealing is crossed described elementary lip so that flow into the liquid flow of described passage, and is full of this elementary lip and flows through the secondary lip;
Be arranged on the flow divert device in the described passage, be used to make fluid diversion wherein, thereby in described passage, make liquid produce spiral cyclic part laminar flow and discharge section laminar flow; With
The liquid extraction device is used to extract the particulate liquid of carrying secretly in the described cyclic part than inferior quality or proportion of containing, and makes the liquid that contains waste particles flow out described passage and the secondary lip of flowing through.
Preferably, described flow divert device comprises circulation tube parallel with substrate with described wall and that be provided with at interval.
Preferably, described liquid extraction device comprises the hole of a plurality of linear arrangement, and described hole axially is provided with on spaced positions along suction pipe, and described extraction plant also comprises suction unit, be used for applying negative pressure, thereby from described cyclic part, extract liquid to the inside of circulation tube.
Preferably, described prefilter comprises the solid phase extraction device, and it has the solid that import in the face of jet flow (cascadingflow) extracts wherein to be held.
Preferably, described liquid extraction device links to each other with the import of flotation/fractionating system, is used for removing the described particulate refuse that the liquid that is included in extraction is carried secretly.
Preferably, described flotation/fractionating system is limited by the previous either side of the present invention.
Provide to be used to separate the method that contains quality or the vicissitudinous particulate liquid of proportion more on the other hand according to of the present invention, having comprised:
To contain described particulate jet flow and enter a passage through elementary lip;
Liquid-flow in described passage is turned to, with generation spiral cyclic part laminar flow and discharge section laminar flow; With
Extract the particulate liquid of carrying secretly in the described cyclic part of containing than inferior quality or proportion;
Will be in containing that described discharge section is carried secretly than quality or proportion particulate liquid are discharged described passage through the secondary lip greatly.
Description of drawings
Figure 1A is a kind of synoptic diagram of known protein skimmer design, it is characterized by single pump and import;
Figure 1B is the synoptic diagram of another kind of known protein skimmer design, it is characterized by double pump device and circulation loop;
Fig. 2 is the skeleton view of aquatic organism class tank systems;
Fig. 3 is the orthographic plan of Fig. 2;
Fig. 4 is the side-view of the service end of the tank systems shown in Fig. 2 and 3, and the pipeline that has schematically illustrated protein skimmer and tank systems pipe arrangement is arranged;
Fig. 5 is the sectional view of tank systems along the B-B of Fig. 3;
Fig. 6 is the sectional view of particle separator;
Fig. 7 shows the principle of operation synoptic diagram that uses improved protein skimmer design of the present invention; With
Fig. 8 is the exploded view according to the actual protein skimmer design of embodiment.
Embodiment
Implement best mode of the present invention with reference to Fig. 2 to 8 explanation, wherein the present invention includes a tank systems that is used for the aquatic organism class, thereby described system enough greatly can a large amount of fish of effective for commercial purposes fairly largely disposal.Described tank systems has carried out substantial explanation in the International Patent Application PCT/AU00/00800 of the applicant's correspondence, the document is incorporated by reference here.
As shown in Fig. 2 to 5, tank systems 101 comprises a big major trough 111, and this groove is divided into holding tank 115 and filtration unit district 117 by internal partition 113.The dashpot 119a and the 119b of a pair of longitudinal extension are provided, have made a dashpot be arranged at arbitrary vertical end of major trough 111.
A pair of main pump 121a and 121b, its pipeline network by on the suction side is connected in corresponding dashpot 119a and 119b and filtration unit district 117, and be connected in major trough 111 by pipeline in the correspondence of outlet side, be used for making fluid in major trough 111 circulations through dashpot and filtration unit;
The auxiliary filter that is protein skimmer 125 forms, it comprises a pneumatic flotation/fractionating system, be used for handling the liquid that contains refuse such as biosolids, nitrite and nitrate, described auxiliary filter is connected with the suction pipe 141 of particle separator 127 with liquid through service pump 105;
The fluid cooler device that is the refrigerating system form, it comprises water cooler or evaporating coil 175, condenser (not shown) and the compressor (not shown) that is arranged in the discharge chamber 155; With
Main pump 121, protein skimmer 125 and fluid cooler device all are arranged on an end of described system 101, near the end wall 111a of described major trough, in service space independently.
Thereby but the groove discharger effectively provides an edge of a knife that makes the water jet flow by elementary lip 129a, with continuous runner through separator 127, this runner is through secondary lip 129b and " V " shape top drip water pond (drip tray) 149, with the middle part in direct fluid protein skimmer 125 or filtration unit district 117.
The filtration unit that is biofilter 131 forms is arranged in the district 117.Biofilter 131 is known design types, but its biomass by the bioball that comprises many its inside growth activity bacteriums constitutes.
Described bacterium is a food with the water of the biofilter of flowing through and the ammonia in the fluid and nitrite, thereby and will be coated with ammonia and nitrite in water and the fluid clearly, described ammonia and nitrite are Crustacean or other hydrocoles institute excretory contained in holding tank.Thereby when having the Crustacean that lives in the holding tank part 115, contained water 123 plays important filtration and cleaning action in 131 pairs of holding tank parts 115 of biofilter.
In the present embodiment, by injecting abundant water 123 to holding tank making it continuously, and provide the solid stream of water to filtration unit district 117 from holding tank 115 through elementary lip 129a jet flow.Thereby, discharger from the top of holding tank 115, the elementary lip 129a of next-door neighbour's groove discharger, be solid stream of water from holding tank 115 drainage waters 123.
Narrate liquid and particle separator 127 now in more detail, as shown in Figure 6, described separator comprises the extension passage 133 that is defined by antetheca 135, rear wall 137 and substrate 139, be provided with elementary lip 129a at the top of described antetheca 135, be provided with secondary lip 129b at the top of described rear wall 137, and the bottom of described substrate 139 closed channels, so that the liquid that flows to passage through elementary lip 129a can be full of described passage and flow out through secondary lip 129b.
Closeer at interval from the hole of managing 141 ends farthest 143 of described tank systems service end 103, for example, be spaced apart 50 millimeters, for example be increased to 200 millimeters at interval gradually from the pipe near-end of service end 103.The inlet hole general diameter is 8 millimeters, but all these sizes all can change according to the desired particular type through the concrete flow velocity of the water of separator 127 and the aquatic organism class held in described major trough 111 that reaches.
As previously described, described protein skimmer 125 is operated to service pump 105 pumping liquids and waste particles from passage 133 by through suction pipe 141 and connected inlet line 151.This liquid that contains refuse is pumped in the reactor vessel 153 through the liquid-inlet device then, and described reactor vessel 153 comprises a separation column 153a, is provided with collection chamber 153b on described separation column 153a.In described liquid, inject the gaseous mixture and the refuse of ozone and oxygen, with reduce and in nitrite and nitrate component, biomass is adsorbed on the foam that forms on the liquid-vapo(u)r interface, then described foam rise also is collected in the collection chamber 153b.Liquid is made the liquid of handling sink to the bottom of separation column 153a, and through suitable return mechanism liquid is returned to holding tank by described separation column 153a by fractionation by this way.
Protein and solid foam are carried in containing that interim ground will be collected in collection chamber 153b secretly, discharge through foam outlet pipe 157, to carry out processing subsequently.
Xiang Shuizhong injects ozone and has not only promoted pneumatic flotation/fractionation process, but also the filtration of nitrate and nitrite from described water is provided, and described nitrate and nitrite are deleterious to the aquatic organism class.
An importance of the present embodiment is the special arrangement of pump 105 to the liquid-inlet device between the separation column 153a.The liquid-inlet device consists essentially of a duplexure that is connected with the outlet line 159 of pump 105.This outlet line comprises a flow rate regulating valve 161, and it is connected with the second liquid-inlet pipeline 165 with the first liquid-inlet pipeline 163 through unitor 167.Outlet line 163 and 165 imports the liquid that contains refuse in the mid-way along separation column 153a shaft length.The mid-way 163a of the first liquid-inlet pipeline 163 is higher than the mid-way 165a of the second liquid-inlet pipeline 165.
Flow control valve 191 is connected with each branch road of duplexure, makes except that the flow rate regulating valve 161 of the outlet 159 of service pump 105, provides flow rate regulating valve 191a along inlet line 163, provides flow rate regulating valve 191b along inlet line 165.
In inlet line 165, comprise the gas injection apparatus that is Venturi tube 169 forms, be used for before being about to enter the mid-way 165a of separation column 153a, introduce the gas that reduces refuse in the liquid that contains refuse, this gas is the gaseous mixture of ozone and oxygen in the present embodiment.
The outside of described protein skimmer comprises the outlet line 173 that is connected with the outlet of separation column 153a, and it is near the bottom of protein skimmer, and its liquid that will handle imports in the discharge chamber 155.Outlet line 173 also provides in its control valve 193 and aperture 195 to the path of discharging chamber 155, with the control fluid from the exit velocity of separation column 153a with enter the gas that in flotation/fractionation process, is incorporated in the water as ozone and oxygen.The terminal 173a of outlet line enters fluid at the top of discharging chamber 155 from reactor vessel.Go out as shown, discharge holding tank 111 ends that chamber 155 is arranged on adjacent service district end 103, and liquid is returned in the holding tank.
A key character of this liquid-inlet device arrangement is, the quantity of the liquid in reactor vessel, in fact can be provided with by independent adjusting flow regulator 191a, not influence total treatment capacity, the latter is determined by pump speed and variable valve 161 and control valve 193.This makes the pressure head in reactor vessel 153 to change, the quantity that is present in the liquid in the tower with decision, and must not change total treatment capacity, the quantity that is present in the liquid in the described tower preferably just is lower than the junction of separation column 153a and collection chamber 153b.
Should be understood that scope of the present invention is not limited to specific embodiments described here.For example the present invention can be used for other fluid treatment appts, wherein wishes the separation that the particulate relative mass that contains according to it or proportion provide liquid, or wherein uses flotation/fractionating method to handle the liquid that contains solid and refuse.
Claims (21)
1. remove the flotation/fractionating system of refuse such as biosolids, nitrate or nitrite from the liquid that comprises refuse, described system comprises: a separation column; Foam collection chamber on described separation column; The liquid that is used for containing refuse is introduced the liquid gatherer of separation column; Be used for pumping unit through liquid-inlet device pumping liquid; Be used for before liquid is about to import separation column, in liquid, directly inject the gas of minimizing refuse such as the gas injection apparatus of air, oxygen or ozone; Be used to extract the foam extraction plant that is collected in foam collection chamber inner foam; With the liquid take-up gear of deriving the liquid of handling from the bottom of separation column; Improvements are:
The liquid gatherer is divided into:
(a) first liquid-inlet, the liquid that is used for containing refuse imports in the mid-way along described separation column axial length, and described first liquid-inlet has flow regulator, is used for controlling the flow velocity that imports the liquid in the described tower; With
(b) second liquid-inlet, be used for to contain simultaneously the liquid of refuse in the importing of the mid-way of the described separation column axial length that is lower than described first liquid-inlet, described second liquid-inlet has the described gas injection apparatus that polyphone is provided with, and is used for the gas of the described minimizing refuse of injection before the liquid of second liquid-inlet in will importing described separation column;
Wherein said branching out after the present described pumping unit outlet;
Wherein by the described setter of control, the liquid in described separation column can remain on best quantity, thereby makes the foam that has wherein adsorbed refuse can accumulate in the described collection chamber.
2. the system as claimed in claim 1, wherein said gas injection apparatus comprises Venturi tube, gas by the described minimizing refuse of this Venturi tube sucks the throat of described Venturi tube, carries out aeration thereby permeate in the liquid that contains refuse of the Venturi tube of flowing through and to it.
3. system as claimed in claim 1 or 2, the gas of wherein said minimizing refuse is the mixture of oxygen and ozone.
4. be used for removing the method that refuse such as biosolids, nitrate or nitrite are controlled to using flotation/fractionating system from the liquid that contains refuse, described system comprises: a separation column; Foam collection chamber on described separation column; Be used to extract the foamy foam extraction plant that is collected in the foam collection chamber; With the liquid take-up gear of deriving the liquid of handling from the bottom of separation column; Described method comprises:
The liquid that will contain refuse from same source, under pressure imports first and second mid-ways of separation column, and the described second position is lower than described first location;
Before liquid is about to import second mid-way of separation column, liquid as described in the gas that reduces refuse injected as air, oxygen or ozone; With
Be adjusted in the flow velocity of the liquid that first mid-way imports, so that the liquid in separation column is remained on optimal number, thereby the foam that has adsorbed refuse on it accumulated in the described collection chamber.
5. method as claimed in claim 4, the gas of wherein said minimizing refuse are the mixtures of oxygen and ozone.
6. be used to separate the device that contains quality or the vicissitudinous particulate liquid of proportion, comprise:
The passage of an extension, it has: (a) have the antetheca of elementary lip, be used for making and contain described particulate liquid and flow into described passage; (b) have the tail wall that is lower than the secondary lip that described elementary lip is provided with, be used to make liquid flow to cross and flow out described passage; (c) substrate of the described channel bottom of sealing so that flow channel liquid flow cross described elementary lip, and be full of this elementary lip and flow through the secondary lip;
Be arranged on the flow divert device in the described passage, be used to make fluid diversion wherein, thereby in described passage, make liquid produce spiral cyclic part laminar flow and discharge section laminar flow; With
The liquid extraction device is used to extract the particulate liquid of carrying secretly in the described cyclic part than inferior quality or proportion of containing, and makes the liquid that contains waste particles flow out described passage and the secondary lip of flowing through.
7. device as claimed in claim 6, wherein said flow divert device comprise the circulation tube with described wall and substrate parallel longitudinal and interval setting.
8. device as claimed in claim 7, wherein said circulation tube the position is set, than antetheca and more close bottom of lip and tail wall.
9. as claim 7 or 8 described devices, wherein said liquid extraction device comprises the hole of a plurality of linear arrangement, described hole axially is provided with on spaced positions along suction pipe, described extraction plant also comprises suction unit, be used for applying negative pressure, thereby from described cyclic part, extract liquid to the inside of circulation tube.
10. device as claimed in claim 9, wherein said hole are arranged on half one in the face of the described pipe of antetheca, so that it is located in the interior liquid circulation part of described passage.
11. device as claimed in claim 10, wherein said hole are arranged on the last quartile of described half one of described pipe.
12. device as claimed in claim 11, wherein said hole be arranged on vertical line into about 45 degree places.
13. as each device in the claim 6 to 12, wherein said liquid extraction device links to each other with the import of flotation/fractionating system, is used for removing what the liquid of extraction was carried secretly comprising described particulate refuse.
14. device as claimed in claim 13, each limits wherein said flotation/fractionating system such as claim 1 to 3.
15. as each described device in the claim 6 to 14, wherein said secondary lip is with the guiding fluid filtration unit of discharging.
16. device as claimed in claim 15, wherein said filtration unit is a biofilter.
17. be used to separate the method that contains quality or the vicissitudinous particulate liquid of proportion, comprise:
To contain described particulate liquid jet and enter a passage through elementary lip;
Liquid-flow in described passage is turned to, with generation spiral cyclic part laminar flow and discharge section laminar flow;
Extract the particulate liquid of carrying secretly in the described cyclic part of containing than inferior quality or proportion; With
Containing than big quality or proportion particulate liquid of will carrying secretly in described discharge section discharged described passage through the secondary lip.
18. from the liquid that comprises refuse, remove the flotation/fractionating system of refuse such as biosolids, nitrate or nitrite, basically as here at as described in the accompanying drawing.
19. be used for using flotation/fractionating system to remove the method that refuse such as biosolids, nitrate or nitrite are controlled, basically as here at as described in the accompanying drawing from the liquid that contains refuse.
20. be used to separate the device that contains quality or the vicissitudinous particulate liquid of proportion, basically as here at as described in the accompanying drawing.
21. be used to separate the method that contains quality or the vicissitudinous particulate liquid of proportion, basically as here at as described in the accompanying drawing.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AUPQ3753 | 1999-10-29 | ||
| AUPQ3753A AUPQ375399A0 (en) | 1999-10-29 | 1999-10-29 | Crossflow tank system for aquatic life |
| WOPCT/AU00/00800 | 2000-06-30 | ||
| PCT/AU2000/000800 WO2001001765A1 (en) | 1999-06-30 | 2000-06-30 | Cross-flow tank system for aquatic life |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1409693A true CN1409693A (en) | 2003-04-09 |
Family
ID=3817904
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN00816986A Pending CN1409693A (en) | 1999-10-29 | 2000-10-30 | Improvements in flotation/fractionation systems for treating liquids and in separation of liquids to be treated thereby |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP1409412A1 (en) |
| JP (1) | JP2003534892A (en) |
| CN (1) | CN1409693A (en) |
| AU (2) | AUPQ375399A0 (en) |
| BR (1) | BR0014630A (en) |
| CA (1) | CA2427191A1 (en) |
| IL (1) | IL149385A0 (en) |
| WO (1) | WO2001032562A1 (en) |
| ZA (1) | ZA200203725B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109399770A (en) * | 2011-08-03 | 2019-03-01 | 埃沃克拉有限公司 | The method of the disposal of industrial wastes |
| CN114223607A (en) * | 2021-12-22 | 2022-03-25 | 湖南省河洲生态甲鱼养殖有限公司 | Soft-shelled turtle transportation device and transportation method |
| CN114727590A (en) * | 2019-11-19 | 2022-07-08 | 海化实验室有限公司 | Slag skimmer for aquarium |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1713323B1 (en) * | 2004-02-05 | 2009-09-16 | Clarity WTS AS | Improved protein skimmer |
| HRP20221199T1 (en) | 2018-04-13 | 2023-01-06 | Andfjord Salmon AS | Efficient land-based fish farm |
| CN110068484B (en) * | 2019-04-29 | 2024-02-20 | 中国矿业大学 | Underground water sample collecting device and method |
| NO346901B1 (en) * | 2021-01-11 | 2023-02-20 | Redox As | A Separation Unit for a Protein Skimmer |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3210972C2 (en) * | 1982-03-25 | 1986-08-07 | Alu Plast Aluminium-Plastik Recycling GmbH, 5440 Mayen | Sink separator for plastic mixtures |
| DE4033223A1 (en) * | 1990-10-19 | 1992-04-23 | Gabriel Volpe | Foamer-type water purifier for e.g aquarium water - which mixes water drawn from pump with air and fed to sepn. chamber having downwardly sloping partition |
| GB9300218D0 (en) * | 1993-01-07 | 1993-03-03 | Grantham David J | A hydraulic separation device |
| US5670039A (en) * | 1995-05-26 | 1997-09-23 | Harris; Ronald B. | Linear solids removal unit |
| US5736034A (en) * | 1996-08-27 | 1998-04-07 | James W. Phillips | Protein removal system |
| DE19719798C1 (en) * | 1997-05-10 | 1999-02-11 | Forschungszentrum Juelich Gmbh | Process for removing biomass from a liquid using a flotation reactor |
-
1999
- 1999-10-29 AU AUPQ3753A patent/AUPQ375399A0/en not_active Abandoned
-
2000
- 2000-10-30 IL IL14938500A patent/IL149385A0/en unknown
- 2000-10-30 CN CN00816986A patent/CN1409693A/en active Pending
- 2000-10-30 JP JP2001534723A patent/JP2003534892A/en active Pending
- 2000-10-30 CA CA002427191A patent/CA2427191A1/en not_active Abandoned
- 2000-10-30 WO PCT/AU2000/001331 patent/WO2001032562A1/en not_active Application Discontinuation
- 2000-10-30 EP EP00972461A patent/EP1409412A1/en not_active Withdrawn
- 2000-10-30 AU AU11185/01A patent/AU1118501A/en not_active Abandoned
- 2000-10-30 BR BR0014630-7A patent/BR0014630A/en not_active Application Discontinuation
-
2002
- 2002-05-10 ZA ZA200203725A patent/ZA200203725B/en unknown
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109399770A (en) * | 2011-08-03 | 2019-03-01 | 埃沃克拉有限公司 | The method of the disposal of industrial wastes |
| CN114727590A (en) * | 2019-11-19 | 2022-07-08 | 海化实验室有限公司 | Slag skimmer for aquarium |
| CN114727590B (en) * | 2019-11-19 | 2024-03-05 | 海化实验室有限公司 | Skimming tool for aquarium |
| CN114223607A (en) * | 2021-12-22 | 2022-03-25 | 湖南省河洲生态甲鱼养殖有限公司 | Soft-shelled turtle transportation device and transportation method |
| CN114223607B (en) * | 2021-12-22 | 2023-09-22 | 湖南省河洲生态甲鱼养殖有限公司 | Soft-shelled turtle transporting device and transporting method |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2003534892A (en) | 2003-11-25 |
| ZA200203725B (en) | 2002-08-21 |
| AUPQ375399A0 (en) | 1999-11-25 |
| CA2427191A1 (en) | 2001-05-10 |
| IL149385A0 (en) | 2002-11-10 |
| AU1118501A (en) | 2001-05-14 |
| EP1409412A1 (en) | 2004-04-21 |
| WO2001032562A1 (en) | 2001-05-10 |
| BR0014630A (en) | 2002-07-02 |
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