WO1999065830A1 - Mediated biological-abiotic waste treatment - Google Patents
Mediated biological-abiotic waste treatment Download PDFInfo
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- WO1999065830A1 WO1999065830A1 PCT/US1998/025302 US9825302W WO9965830A1 WO 1999065830 A1 WO1999065830 A1 WO 1999065830A1 US 9825302 W US9825302 W US 9825302W WO 9965830 A1 WO9965830 A1 WO 9965830A1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1257—Oxidation ditches
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1205—Particular type of activated sludge processes
- C02F3/1231—Treatments of toxic sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Definitions
- the invention belongs to biological-abiotic systems for waste treatment, and more specifically is a method for mediated degradation and reduction of carbonaceous BOD or COD, toxic and recalcitrant organics, and nutrients, for improved oxygen transfer, and for minimization of the excess biosolids.
- Phosphorus removal systems are conducted via, first, exposing the recycle sludge to facultative anaerobic conditions wherein acetic acid is formed and phosphorus is released, and, second, exposing biomass in the sludge to aerobic conditions wherein the so-called luxurious uptake of phosphorus is believed to occur.
- the process rate is limited by a low driving force of biological processes due to a low oxygen concentration in the liquid.
- a small part of biomass may be aerobic.
- Increasing the oxygen concentration is very expensive because it requires either the use of pure oxygen or a drop in the oxygen mass transfer rate due to lower driving force of the oxygen transfer. Accordingly, aeration is not efficient and expensive.
- Phosphorus can be easily removed with reagents, primarily, iron or aluminum ions in forms of insoluble phosphates.
- the process can be conducted in biological reactors so that little equipment is required.
- the stoichiometric iron and aluminum requirements are only 0.88 mg Fe and 0.28 mg Al per lmg P 2 O 4 .
- the actual metal requirement is significantly greater.
- Chemical nitrogen removal involves difficult processes and is not practiced for low nitrogen concentrations in municipal and many industrial wastewater types.
- a co-precipitation of phosphorus and nitrogen (ammonia) as struvite (MgNH 4 PO 4 ) have also been discussed, but not practiced yet.
- the use of reagents contributes to the sludge mass. Increased mass of the excess sludge is cited as the argument against chemical phosphorus removal.
- Anaerobic, aerobic, and coupled or combined anaerobic-aerobic biological systems are also used for treatment of dilute and concentrated industrial waste for organics and nutrients removal, as well as for removal and destruction of toxic and recalcitrant organics, heavy metals, sulfur containing compounds, and other applications.
- biological processes may suffer problems similar to those experienced with advanced systems and also application specific problems. For example, in some applications, toxicity is a problem, in other applications, odorous constituents are emitted, while in others the process stability is difficult to control.
- Aerobic biological processes make use of oxygen.
- the field (really obtainable) oxygen transfer efficiency in kgO/kW-hr
- the field (really obtainable) oxygen transfer efficiency is low, especially at elevated oxygen concentrations in the aeration steps and in presence of specific admixtures, such as surfactant.
- Relentless research during at least fifty years has resulted in significant though only incremental improvements. The aeration remains the most energy demanding and costly operation in most treatment plants.
- an objective of the present invention is to provide a simple, reliable, efficient, stable, and economical system for removal of organics, nutrients, toxic and recalcitrant organics and other target constituents, while improving oxygen transfer efficiency and generating little or no waste biological solids.
- this method can be a method of biological wastewater treatment with biomass in a system comprising at least one aerobic biological wastewater treatment step, whereby the target organic and inorganic constituents in the said wastewater and the recuperable oxidation-reduction mediator specie charged in the system become at least partially oxidized to form new biomass, carbon dioxide, water, and nitrites and nitrates, and/or at least one step of oxidizing the said biomass, wherein the said biomass is repeatedly treated in the said aerobic and biomass oxidizing steps, whereby the said recuperable oxidation-reduction mediator species become reduced in the said biomass oxidation step to a lower oxidation state while oxidizing and minimizing biomass.
- This can also be a method of biological wastewater treatment with biomass in a system comprising at least one aerobic biological wastewater treatment step, whereby the target constituents in the said wastewater and the recuperable oxidation-reduction mediator species charged in the said system are oxidized to form new biomass, carbon dioxide, water, and nitrites and nitrates and higher valence recuperable oxidation-reduction mediator species, at least one denitrification step, whereby the said nitrites and nitrates are reduced to form gaseous nitrogen forms and the said abiotic species are converted to the lower valence, a step of charging at least one recuperable oxidation-reduction mediator species in the said system.
- Selected recuperable oxidation-reduction mediator species can precipitate phosphorus as insoluble phosphates from the said wastewater in the said system simultaneously with other process steps.
- Some ion exchange mediator species can also remove phosphorus via ion exchange mechanisms.
- the said wastewater is defined herein as domestic or industrial wastewater, aqueous industrial, agricultural and production materials, industrial, agricultural and production gases, polluted air, gaseous and vent emissions, solid waste, materials of plant, animal, or fossil origin, and solid industrial, agricultural or production streams, and combinations thereof. It is understood that gaseous pollutants can be washed with a liquid and treated in the present system, while solid materials can be converted to slurries with water.
- the said aerobic step can be selected from the group comprising oxygen enriched steps (including high purity oxygen), air aerated aerobic treatment, nitrification treatment, to a lesser degree anoxic treatment, denitrification treatment, reduction of halogenated organics, facultative anaerobic treatment, and combinations thereof.
- the said biological reduction step can be selected from the group comprising anoxic treatment, denitrification treatment, facultative anaerobic treatment, ferric iron reduction, sulfate reduction, carbonate reduction (methanation), and combinations thereof.
- the said step of biomass oxidation is preferably anaerobic, ferric ion reduction, or facultative anaerobic step.
- the said recuperable oxidation-reduction mediator species with variable oxidation state can be selected from the group comprising zero-valence metal pieces, metallic ions, metal- containing oxyions, nonbiodegradable and insoluble inorganic constituents with variable oxidation-reduction states, nonbiodegradable and insoluble organic constituents with variable oxidation-reduction states, and combinations thereof.
- the said metallic and metal-containing species include metals selected from the group comprising iron, nickel, cobalt, manganese, vanadium, and combinations thereof.
- Ion exchange resins with oxidation-reduction groups also known as redox exchanger
- redox exchanger similarly activated and modified natural organic and inorganic materials known to skillful in art or specifically developed in the future for particular applications can also be used as recuperable abiotic species in this process.
- FIG. 1 shows lines a and b separating the domain of stability of water and the oxidation and reduction domains of water.
- a range of pH from 6 to 8.5 generally considered as acceptable for biological processes is hatched in Fig.1.
- iron is found in a higher valence as an insoluble Fe(OH) 3 , or as divalent ions Fe 2 , and at lower oxidation-reduction potentials (ORP) in the presence of sulfides, as ferrous sulfide, and at pH greater than approximately 8.35 as ferrous carbonate.
- the iron species of the main interest here are trivalent (ferric) and divalent (ferrous) forms.
- ferric and ferrous species are respectively an oxidant and a reducing agent.
- Solid line in Fig. 1 separates oxidizing and reducing conditions for these species. Accordingly, process steps conducted at pH and ORP above the solid line are called herein oxidation steps, and those below solid line are reduction steps.
- the domain of metallic (zero-valence) iron is located low in Fig.1 beyond the domain of water stability. Therefore, metallic iron can be added to the system and converted into recuperable ferric and ferrous species, but metallic iron cannot be recuperated in known biological systems.
- ferrous ions are oxidized to ferric ions either by oxygen supplied through aeration or via reduction of nitrites and nitrates mainly to molecular nitrogen, or by halogenated organics.
- biomass oxidation it is oxidized mainly to carbon dioxide and water by ferric ions becoming ferrous ions.
- ferrous and ferric ions are repeatedly used in the said aerobic, nitrification, denitrification, and the said biomass oxidation steps.
- Insoluble ferric forms are enmeshed with the sludge and retained (recuperated) in the system.
- ferric hydroxide is also a coagulant for the biomass. It beneficially enhances sludge separation.
- batch processes the repetition of these steps occurs in the same space on a time sequence.
- continuous flow systems the steps are repeated in spatially separated steps in different reservoirs by recycling the sludge composed of biomass and the said abiotic species in solid form between these steps.
- the recycled biomass can be separated from the wastewater being treated and further directed for the repeated treatment, or it can be directed for the repeated treatment together with the said wastewater as mixed liquor.
- the spatial separation can be provided due to concentration gradients within a single tank with nonhomogeneous mixing.
- Nonhomogeneous mixing can be either due to concentration gradients within incompletely mixed tank, or due to unsteady-state (time variable) concentration gradients within biological flocks and films. Therefore, it is biomass (or sludge including the biomass and insoluble forms of oxidation-reduction mediator species) that is repeatedly treated in at least one step of oxidizing terminal reducing agents (hydrocarbons and/or biomass) wherein the recuperable oxidation-reduction species are reduced, and at least one step of reducing terminal oxidizers (oxygen, air, nitrites and nitrates, or some halogenated and other toxic and recalcitrant organics) whereby the recuperable oxidation-reduction mediator species are oxidized while the wastewater may be, but not necessarily, repeatedly treated in these steps.
- oxidizing terminal reducing agents hydrocarbons and/or biomass
- reducing terminal oxidizers oxygen, air, nitrites and nitrates, or some halogenated and other toxic and recalcitrant organics
- the recuperable oxidation-reduction mediator species function as intermediate oxidation- reduction agents.
- iron concentration is provided at the level needed to remove phosphorus. This is usually a small concentration.
- iron used for binding phosphates is rapidly evacuated from the system and new iron needs to be continuously fed.
- concentration of iron ions can be from a fraction of lg/L to several grams per liter, that is at least one to several orders of magnitude greater than in phosphorus removal systems. At these concentrations, a constantly present pool of charged iron is created in the system.
- This "oxidation capacity" is much greater than that of oxygen in conventional air aeration systems and exceeds that of high purity oxygen systems by a factor greater than two.
- the "reducing power" of ferrous ions used in denitrification steps can also exceed that of the purchased organics. Unlike organics, for example methanol, in denitrification processes, recuperable iron ions do not constitute BOD that needs to be removed after the conventional denitrification step.
- Recyclable iron ions do not contribute to the growth of biomass in denitrification and post denitrification steps as organics do. On the contrary, the biomass is oxidized in the recuperation cycle of iron ions. Significantly increased oxidation-reduction capacity (or driving force) in the system results in dramatic increases in rates and efficiency of denitrification and sludge oxidation steps. It is understood that iron is used here as an example and many other recuperable oxidation-reduction mediator specie types can also be used. It is also understood that when selecting the said species, skillful in art can consider physical-chemical and other properties of specific recuperable species.
- Cobalt and nickel are other practicable species to be used in the present method.
- a simplified pH-ORP diagram for cobalt is given in Fig.2.
- cobalt and nickel exist in zero-, di-, and tri-valence states.
- nickel and cobalt in zero-valence state can exist within the domain of water stability.
- a portion of the area of stability of cobalt and nickel within the stable water domain corresponds to conventional anaerobic processes, particularly, many methanogenic processes having ORP approximately -250 to -400 mV. Therefore, metallic (zero-valence) cobalt, or nickel, can be formed in anaerobic processes from tri-, and di-valence forms.
- Zero-valence species are very powerful reducing agents for many toxic and recalcitrant constituents found in many wastewater, solid wastes, contaminated soils, and other wastes. These reductions are described in U.S. Patent No. 5,348,629 and co-pending patent application No. PCT US98/08649 which are made a part of this application by inclusion.
- nickel and cobalt can form poorly soluble hydroxides and oxides. Accordingly, they can also be retained and recuperated in biological processes, including aerobic and some anoxic steps.
- the method further provides at least one recuperable alkalinity control specie.
- Such specie can be selected from calcium, zinc, aluminum, iron, nickel, cobalt, cesium, and combinations thereof. Effects of such species are described in the US Patent No. 5,798,043 which is made a part of the present application by inclusion.
- the present method can be conducted in a multi step system.
- the sequence of the said steps is selected from a group comprising sequential treatment steps, parallel treatment steps, parallel-sequential treatment steps, treatment steps in a racetrack arrangement, treatment steps with recycling the said wastewater and the said biomass among and between the said steps, and combinations thereof.
- the operation mode of at least one step in the said system is selected from a group comprising continuous operation, batch operation, continuous operation with flow equalization, and combinations thereof.
- the said batch operation steps are selected from the group comprising aerobic treatment, nitrification treatment, anoxic treatment, denitrification treatment, biomass oxidation treatment, facultative anaerobic treatment.
- the said batch operation steps are selected from the group comprising filling step, filling-stripping step, reacting step, reacting-stripping step, settling step, decanting step, and combinations thereof.
- the said wastewater can be repeatedly treated in at least two functional zones for conducting the steps selected from the group comprising oxygen enriched treatment, aerobic treatment, nitrification treatment, anoxic treatment, denitrification treatment, facultative anaerobic treatment, sulfate reduction, carbonate reduction, sludge conditioning, biomass oxidation treatment, and combinations thereof.
- the said biomass in the said system is composed of microorganisms selected from the group comprising obligate aerobic, facultative aerobic, nitrifying, denitrifying, ferrous iron oxidizing, ferric iron reducing, anoxic, facultative anaerobic, sulfate reducing, methanogenic, obligate anaerobic, and mixtures thereof.
- the present method can provide at least one step of anaerobic sludge conditioning to produce biomass enriched with methanogens, and at least one step of feeding at least a portion of the said conditioned sludge with enhanced content of methanogens in at least one step of the said system.
- the present method can be conducted in a system comprising at least one denitrification step, at least one step of the said biomass oxidation (or other reduction step), a step of treating the said biomass repeatedly in the said denitrification and biomass oxidation steps, and a step of charging in the said system at least one recuperable abiotic specie with a variable oxidation state.
- the present process can be carried out in an apparatus comprising at least one biological wastewater treatment zone with aerobic conditions, and/or at least one denitrification zone with the use of recuperable oxidation-reduction mediator species in a lower oxidation state, and at least one zone of oxidizing the said biomass with the use of recuperable oxidation-reduction mediator species in a higher oxidation state.
- Transferring means for the repeated treatment of the said biomass in the said biological treatment zones can also be provided.
- At least two of the said biological treatment zones and the sludge oxidation zone can be combined in a single reservoir.
- At least two of the said zones can be combined in the same space in a single reservoir.
- the new apparatus can be a multi zone system.
- the zone connection in the said multi zone system is selected from a group comprising sequential treatment zones, parallel treatment zones, parallel-sequential treatment zones, treatment zones in a racetrack arrangement, treatment zones with recycling the said wastewater and the said biomass among and between the said zones, and combinations thereof.
- An apparatus can further be provided with a zone of anaerobic treatment of the said wastewater.
- Fig. 1 is a simplified pH-ORP diagram for iron.
- Fig. 2 is a simplified pH-ORP diagram for cobalt.
- Fig. 3 is a flowchart of a denitrification process with biomass oxidation in a sideline zone with reducing conditions.
- Fig. 4 is a flowchart of a process of Fig.1 with an added aerobic process step following the denitrification stage.
- Fig. 5 is a flowchart of a process of Fig.2 with an added aerobic process step preceding the denitrification step.
- Fig. 6 is a flow chart of a portion of a treatment system with two sequential aerobic-denitrification zones and a single dedicated biomass oxidation zone.
- Fig. 7 is a flowchart of a denitrification process with a dedicated biomass oxidation zone in the sludge recycle line.
- Fig. 8 is a race track system with an aerobic, denitrification and biomass oxidation zones.
- Fig. 9 is a cross section of a denitrification-aeration-biomass oxidation unit.
- Fig. 10 is a modified Biolac system with added denitrification-biomass oxidation zones.
- Fig. 11 is a system with improved oxygen transfer making use of chemosorption by the recuperable oxidation-reduction mediator species.
- Fig. 12 is a system with zero-valence metal form of the recuperable oxidation-reduction mediator species.
- FIG. 3 is a flowchart of a denitrification process with biomass oxidation in a sideline zone with reducing conditions.
- This embodiment is operated as follows.
- the system is charged with a recuperable oxidation-reduction mediator species having variable oxidation state, for example, with iron salt, whereby iron can change between the higher valence ions (trivalent ferric ions) and lower valence ions (divalent ferrous ions).
- Wastewater loaded with organics and nitrites and/or nitrates is fed via line 1 in the denitrification zone 2.
- organics are biologically oxidized to carbon dioxide and water and a new biomass is formed.
- nitrites and/or nitrates are partially reduced to molecular nitrogen and nitrous and nitric oxides (gaseous nitrogen forms), and the remaining nitrites and nitrates oxidize ferrous ions to ferric with the conversion to gaseous nitrogen forms.
- a portion of the mixed liquor from zone 2 is directed via line 3 to the final sludge separator 4 (a clarifier or other means), the clarified treated wastewater is evacuated via line 5 and the separated sludge is recycled to zone 2 via line 9.
- the other portion of the mixed liquor is directed via line 7 in the biomass oxidation zone 6 and returned back in zone 2 via line 8.
- ferric ions oxidize biomass and revert to ferrous ions; the latter are recycled in zone 2 to be used in denitrification process.
- Biomass oxidation causes a dramatic excess sludge reduction.
- Iron ions form insoluble phosphates which particles become enmeshed in the sludge and are removed from the system with the excess sludge.
- pH range of biological treatment virtually insoluble ferric hydroxide and sparingly soluble ferrous hydroxide are formed. Accordingly, iron ions charged in the system circulate between zones 2 and 6 and the sludge separator 4.
- Nitrites and nitrates are removed by oxidizing ferrous ions to ferric.
- methanol or other purchased organics are used instead.
- ferric ions are further used to oxidize biomass thus reducing the excess sludge. This is an unexpected benefit of the present invention. Because iron ions are used for denitrification and biomass oxidation, there is always an excess iron insuring complete phosphorus removal. In contrast to conventional phosphorus removal methods with metal salt additions, losses of the charged iron are very low. Accordingly, iron ions and other similar species are called herein the recuperable abiotic species.
- the iron losses are due to binding phosphorus, and due to some loss of iron hydroxides with a small quantity of waste sludge.
- the iron lost with sludge is a coagulant that would be added to the sludge later in the sludge treatment processes. Therefore, all charged iron is beneficially used in the system.
- sludge oxidized in the present process is well mineralized and easy to dewater. It will not need stabilization in a dedicated sludge treatment process.
- the waste sludge can by hydrolyzed by using chemical, thermal, or anaerobic biological hydrolysis, and the said recuperable oxidation-reduction mediator species can be almost completely recovered for the use in the present process.
- Fig. 4 is a flowchart of a process of Fig.3 with an added aerobic process step 10 following the denitrification stage 2.
- a recycle line 15 can also be provided.
- This embodiment can be used for removal of the influent nitrogen in forms different from nitrites and nitrates.
- wastewater influent can include organic and/or ammonia nitrogen.
- nitrogen is converted into nitrates and nitrites in the aerobic zone 10 and recycled in the denitrification zone 2 via line 15.
- the rest of the operations are the same as previously described and will not be repeated. Due to oxidation to ferric ions, loss of iron with the effluent will be virtually eliminated.
- Fig. 5 is a flowchart of a process of Fig.4 with an added aerobic process step 12 preceding the denitrification step 2.
- This figure also shows a mixed liquor recycle line 15 between zones 2 and 12, a mixed liquor recycle line 16 between zones 19 and 6, and a line 14 for feeding a portion of the influent to zone 6.
- zone 12 organics are converted to new biomass, carbon dioxide, and water, and nitrogen is largely converted into nitrites and nitrates.
- Zones 2 and 6 are operated as previously described.
- the aerobic zone 10 serves as a zone of thorough organics removal and iron oxidation. Additional nitrification can also occur in this zone.
- Recycle line 15 is optional and should preferably be used when treating wastewater with high nitrogen content.
- Recycle line 16 can be used to deliver ferric ions directly to the biomass oxidation zone 6 to oxidize more biomass. Additionally, recycles via lines 15 and 16 equalize the influent organics and nitrogen concentrations. Line 14 provides direct feed of organics with a portion of the influent to the biomass oxidation zone 6 for consumption of excess ferric ions in the system.
- Fig. 6 is a flow chart of a portion of a treatment system with two sequential aerobic- denitrification zones 12 and 2a and 17 and 2b and a single dedicated biomass oxidation zone 6.
- Fig. 7 is a flowchart of a denitrification process with the dedicated biomass oxidation zone in the sludge recycle line.
- the wastewater influent is fed via line 1 in the aerobic zone 12 where organics are converted to new biomass, carbon dioxide and water, and nitrogen species are oxidized to nitrites and nitrates.
- the mixed liquor is directed via line 13 into zone 2 for denitrification with ferrous ions.
- mixed liquor goes via line 3 to an aerobic zone 10 for thorough removal of organics and oxidation of ferrous ions to ferric, which form ferric hydroxide.
- a mixed liquor carrying biomass and flocculated ferric hydroxide enter the sludge separator 4.
- the clarified treated wastewater is discharged via line 5.
- the separated sludge comprising biomass, ferric hydroxide, and the accumulated inert constituents is evacuated via line 9. It is further directed in part to the aerobic zone 12, while the balance of the sludge is fed through line 19 to the biomass oxidation zone 20 and further via line
- sludge from zone 20 can be fed via line 22 in zone 12.
- Biomass is partially oxidized in zone 20 by ferric ions becoming ferrous ions.
- Fig. 8 is a layout of a race track system with an aerobic, denitrification and sludge oxidation zones.
- This embodiment comprises an influent line 1, a circular aerobic zone 12 embracing a circular denitrification zone 2, the central biomass oxidation zone 6, and the line 3 leading to the sludge separator.
- the sludge separator and sludge return means are not shown.
- Brush aerators 23 are aerating and propelling mixed liquor in zone 12.
- Propeller mixers 24 and 25 propel and mix mixed liquor in zones 2 and 6 respectively.
- Zones 12, 2, and 6 communicate hydraulically with the use of gates 13, 7 and 8.
- This layout corresponds to the flow chart shown in Fig.4 and is operated as previously described.
- Other modification of racetrack layouts and equipment can be used as known to skillful in art at the time of design. Present teachings are sufficient for designing the process variants not shown in this specification.
- Fig. 9 is a cross section of a denitrification-aeration-biomass oxidation unit.
- This system comprises a reservoir 28 accommodating functional zones 2, 6 and 10 as described in Fig. 4. Accordingly, the system is operated as previously described. Only specific features related to this particular layout are discussed.
- zone 2 is exposed above zone 6 and the sludge comprising the biomass and iron hydroxides is densified in zone 6. This reduces the volume of the biomass oxidation zone 6.
- the sludge can be lifted from zone 6 to zone 2 via standpipe 7, which can be fitted with an airlift, a pump, a jet pump, or other lifting means.
- Aerators 26 and clarifiers 4 are shown in zone 10.
- This embodiment does not have well defined borders separating zones 2, 6, and 10, and many lines shown in Fig.2 for connecting these zones are absent.
- Other modifications of combined layouts and equipment can be used as known to skillful in art at the time of design. Present teachings are sufficient for designing the process variants not shown in this specification.
- Fig. 10 is a modified Biolac system with added denitrification-biomass oxidation zones.
- Biolac is described in U.S. Patent Nos. 4,287,062, 4,797,212, and 5,472,61 1.
- the present system comprises a reservoir 28 accommodating functional zones 12, 2, 6, and 10 as described in Fig. 5. Accordingly, the system is operated as previously described. Only specific features related to this particular layout are discussed.
- zone 2 is exposed above zone 6 and the sludge comprising the biomass and iron hydroxides is densified in zone 6. This reduces the volume of the biomass oxidation zone 6.
- the sludge can be lifted from zone 6 to zone 2 via standpipe 7, which can be fitted with an airlift, a pump, a jet pump, or other lifting means.
- Floating aerators 26 are shown in aerobic zones 12 and 10. Floating clarifiers (not shown) can also be installed within the reservoir 28. In contrast to other described systems, this embodiment has floating and moving aerators 26 and a floating and moving sludge transfer means 7. Sludge transfer means 7 can be provided with a pump, an airlift, a jet pump, or other means for moving fluids. Aerators 26 and the sludge transfer means 7 are connected to and suspended from a floating air pipe 27, which is connected to an air conduit 29. Structural support for the floating assembly including elements 7, 26, and 27 is provided by a cable 30 and anchors 31. Optional curtains 32 can be provided for a better separation of the denitrification zone 2 from the aerobic zones 12 and 10.
- zones 2 and 6 can be accommodated over a flat bottom using partitions, walls of the reservoir 28 can be vertical, and a conventional clarifier for sludge separation can be installed within or beyond the reservoir 28.
- aerobic, anaerobic, and sludge conditioning zones can be accommodated in a Biolac system with a flat bottom side by side, or aerobic zones can be exposed above anaerobic zones.
- a calming means can be provided between the vertically stacked anaerobic and aerobic zones.
- the race track flows can be used in the modified Biolac.
- the anaerobic zones can communicate with aerobic zones with the help of water moving means (pumps, water jets, airlifts, or other).
- Addition of calcium, for example lime, to the present system is also beneficial.
- aerobic zones such as zones 10 and 12
- carbon dioxide is stripped and insoluble calcium carbonate is formed. This insoluble compound is retained in the system and transferred in the denitrification zones 2 and further in biomass oxidation zones 6.
- carbon dioxide is formed and not well stripped and some volatile fatty acids can also be formed, thus producing acidification of the media in these zones.
- calcium carbonate will convert to calcium bicarbonate thus buffering pH. It is possible to maintain near optimal pH values in all zones in this system for nitrification, denitrification, and iron oxidation.
- Addition of small quantities of catalysts, for example, manganese or copper salts further increases the rate and efficiency of iron oxidation in the system.
- Powdered (pulverized) activated carbon (PAC), and or powdered or fine-crushed coal can also be used to increase the rate and efficiency of oxidation- reduction processes in the present system.
- PAC pulverized activated carbon
- losses of PAC are very small. Therefore, it can be charged once and small losses can be periodically replenished.
- Fig. 11 is a system with improved oxygen transfer making use of chemosorption by the recuperable oxidation-reduction mediator species.
- the system includes an influent line 1, a substrate oxidation unit 2, wherein the fed oxidizer is the mediator species in oxidized form, as ferric ions, a line 41 connecting reactor 2 to the mediator species oxidation unit 40, wherein the mediator species are oxidized by the terminal oxidizer.
- the terminal oxidizer is fed via line 44, the residual gases, including gases stripped from the liquid being treated are released at the surface of the open tank 40 or via line 45. Thus "oxygenated" liquid is recycled to the reactor 2 via line 43.
- the mixed liquor is than transferred by line 42 in the sludge separation unit 4, from where the effluent is discharged via line 5 and the separated sludge carrying the recuperated mediator species in largely insoluble form is returned to the reactor 2 via line 9.
- the feed of reduced mediator species capable of chemosorption of gaseous oxidizers in the unit 40 greatly increases both the rate and the percentage of the oxygen dissolution and binding by the secondary (mediating) oxidizer, as compared to corresponding conventional aeration systems.
- Oxygen, air, ozone, hydrogen peroxide, or other oxidizing agent, or a combination of several terminal oxidizers can be used. Any known gas-liquid contacting apparatus can be used as unit 40.
- the oxidation unit 40 can be a vessel under atmospheric pressure, or it can be pressurized. In pressurized system with air, substantial fraction of oxygen becomes bound in the chemosorption process, while nitrogen becomes dissolved. Dissolved nitrogen can be used as a flotation gas in the sludge separation unit 4, which in such a case should be a flotation unit. In pure oxygen systems with complete oxygen utilization, the unit 40 can be operated almost without gaseous emissions.
- the process of Fig. 11 differs from that of Fig.4 in that the unit 40 serves only to convert the recuperable mediator species into the oxidized state, while reactor 10 is a biological reactor wherein conversions of organic substrates and growth of biomass also occur.
- Fig. 12 shows an anaerobic reactor 50 with strongly reducing conditions.
- a special sludge conditioning zone 51 in hydraulic communication with the reactor 50 can be also used.
- methanogenic conditions can predominate thus lowering the oxidation reduction potentials to the level of reducing certain metallic ions to zero- valence metal form.
- cobalt and nickel can be reduced under such conditions to metallic state. In such a state they also become the recuperable oxidation-reduction mediator species.
- Other reducing agents for example hypophosphite, formic acid, can be added to produce such metal reductions.
- reactor 50 can be used together with aerobic reactor 10 and other units as previously described.
- Various additional recycle lines, such as line 59, can also be provided.
- the recuperable oxidation-reduction species can be introduced as zero-valence metals with simultaneous reduction of target species.
- a filter with iron bed or a bed made of iron and electroconducting forms of carbon can be used to reduce nitrites and nitrates, and/or various toxic and recalcitrant organics.
- iron is dissolved and introduced in the system.
- pH values pH values
- dissolved iron precipitates within the filter mostly as ferrous hydroxide which can be dislodged from the filter by backwashing. Dissolution of iron can be further accelerated and reduction of target constituents also improved by feeding a stream containing ferric ions in the said filters.
- Such filters can be included in the described or otherwise modified biological treatment system, or they can be used as tertiary treatment filters after secondary clarifiers in biological systems. In either case, such filters can reduce nitrites/nitrates and toxic organics, and precipitate phosphorus. The metal- containing backwash from these filters will be directed to biological treatment steps and used as previously described.
- the pool of recuperable oxidation-reduction species in biological treatment systems with fluctuating flows and concentrations helps to smooth the dynamic variations in the output parameters (effluent quality) and in demands for aeration and other operating conditions. For example, during a low organics loading rate in a biological treatment of BOD (COD) with or without nutrients removal the oxidized forms of the recuperable oxidation-reduction species accumulate in the system. During the period of greater than average loading rate, the previously accumulated oxidized species are reduced thus minimizing the peak oxygen demand. Respectively, the aeration system does not need to be designed for the maximum BOD and ammonia nitrogen loading rates. It can correspond to a somewhat prudently greater than the average loading rate.
- FIGs. 1 and 2 define significant properties of recuperable oxidation-reduction mediator species. These figures also clearly show that the boundaries between oxidation and reduction domains are different for the selected species. Moreover, some species can divide the total oxidation-reduction domain of biological processes into more than two oxidation and reduction domains. Accordingly, definition of oxidizing and reducing biological steps should be coordinated with the properties of selected recuperable oxidation-reduction mediator specie.
- Biological processes can be graded from oxidizing to reducing as follows: high purity oxygen systems, air aerated systems including nitrification, denitrification systems, ferric iron reduction systems, sulfate reduction systems, carbonate reduction (methanation) systems.
- Corresponding primary oxidizers are oxygen, oxygen of air, nitrites and nitrates, ferric iron, sulfates, and carbonates. Halogenated and some other "oxidized" organics can also be primary oxidizers.
- Hydrocarbons consisttituents of wastewater or purchased reagents
- biomass organic content of biomass
- recuperable oxidation-reduction mediator species are the secondary oxidizing species (electron acceptors) in their oxidation reactions of the terminal reducing agents and they are the secondary reducing agents (electron donors) in their reduction reactions with the primary oxidizers.
- High purity oxygen and carbon dioxide reduction systems are almost always oxidation and reducing steps in the context of this method.
- all other steps in the oxidation-reduction scale can be either oxidation or reduction steps depending on the position of the boundary line (or lines) in the pH-ORP diagram for the selected recuperable oxidation-reduction mediator specie, or a combination of such species. It is understood that a combination of several recuperable oxidation- reduction mediator species can be used simultaneously.
- the present invention meets the objectives: to provide a simple, reliable, efficient and economical system for removal of organics and nutrients with low generation of sludges.
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- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Toxicology (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
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CA 2299328 CA2299328A1 (en) | 1998-06-18 | 1998-11-23 | Mediated biological-abiotic waste treatment |
EP19980960512 EP1027294A1 (en) | 1998-06-18 | 1998-11-23 | Mediated biological-abiotic waste treatment |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/100,160 | 1998-06-18 | ||
US09/100,160 US5919367A (en) | 1997-12-01 | 1998-06-18 | Biological-abiotic waste treatment |
Publications (1)
Publication Number | Publication Date |
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WO1999065830A1 true WO1999065830A1 (en) | 1999-12-23 |
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ID=22278387
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PCT/US1998/025302 WO1999065830A1 (en) | 1998-06-18 | 1998-11-23 | Mediated biological-abiotic waste treatment |
Country Status (4)
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EP (1) | EP1027294A1 (en) |
CA (1) | CA2299328A1 (en) |
RU (1) | RU2225366C2 (en) |
WO (1) | WO1999065830A1 (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1165447A1 (en) * | 1999-02-11 | 2002-01-02 | Zeolite Australia Limited | Process for the removal of suspended and other material from waste water |
US10329179B2 (en) | 2009-09-18 | 2019-06-25 | The Texas A&M University System | Zero valent iron systems and methods for treatment of contaminated wastewater |
US10377648B2 (en) | 2009-09-18 | 2019-08-13 | The Texas A&M University System | Selenium removal using aluminum salt at conditioning and reaction stages to activate zero-valent iron (ZVI) in pironox process |
US11084742B2 (en) | 2014-12-19 | 2021-08-10 | The Texas A&M University System | Activated hybrid zero-valent iron treatment system and methods for generation and use thereof |
CN115140847A (en) * | 2022-07-05 | 2022-10-04 | 南京大学 | Mediator-enhanced wastewater deep biological denitrification method |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN116199334B (en) * | 2023-03-29 | 2024-03-12 | 北京工业大学 | Method for strengthening biological denitrification efficiency of low-temperature activated sludge by chlorophyll |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4029575A (en) * | 1972-06-09 | 1977-06-14 | Ewing Engineering Company | Phosphorus removal from waste water |
US5587079A (en) * | 1995-04-21 | 1996-12-24 | Rowley; Michael V. | Process for treating solutions containing sulfate and metal ions. |
-
1998
- 1998-11-23 EP EP19980960512 patent/EP1027294A1/en not_active Withdrawn
- 1998-11-23 CA CA 2299328 patent/CA2299328A1/en not_active Abandoned
- 1998-11-23 RU RU2000106522A patent/RU2225366C2/en not_active IP Right Cessation
- 1998-11-23 WO PCT/US1998/025302 patent/WO1999065830A1/en not_active Application Discontinuation
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4029575A (en) * | 1972-06-09 | 1977-06-14 | Ewing Engineering Company | Phosphorus removal from waste water |
US5587079A (en) * | 1995-04-21 | 1996-12-24 | Rowley; Michael V. | Process for treating solutions containing sulfate and metal ions. |
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1165447A1 (en) * | 1999-02-11 | 2002-01-02 | Zeolite Australia Limited | Process for the removal of suspended and other material from waste water |
EP1165447A4 (en) * | 1999-02-11 | 2003-04-23 | Zeolite Australia Ltd | Process for the removal of suspended and other material from waste water |
US10329179B2 (en) | 2009-09-18 | 2019-06-25 | The Texas A&M University System | Zero valent iron systems and methods for treatment of contaminated wastewater |
US10377648B2 (en) | 2009-09-18 | 2019-08-13 | The Texas A&M University System | Selenium removal using aluminum salt at conditioning and reaction stages to activate zero-valent iron (ZVI) in pironox process |
US11208338B2 (en) | 2009-09-18 | 2021-12-28 | Evoqua Water Technologies Llc | Selenium removal using aluminum salt at conditioning and reaction stages to activate zero-valent iron (ZVI) in pironox process |
US11084742B2 (en) | 2014-12-19 | 2021-08-10 | The Texas A&M University System | Activated hybrid zero-valent iron treatment system and methods for generation and use thereof |
CN115140847A (en) * | 2022-07-05 | 2022-10-04 | 南京大学 | Mediator-enhanced wastewater deep biological denitrification method |
CN115140847B (en) * | 2022-07-05 | 2023-11-03 | 南京大学 | Mediator-enhanced wastewater deep biological denitrification method |
Also Published As
Publication number | Publication date |
---|---|
EP1027294A1 (en) | 2000-08-16 |
CA2299328A1 (en) | 1999-12-23 |
RU2225366C2 (en) | 2004-03-10 |
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