WASTEWATER BIOSORPTION WITH DISSOLVED AIR FLOTATION

BACKGROUND

Aspects and embodiments of the present invention are directed toward systems and methods for the treatment of wastewater.

SUMMARY

in accordance with an embodiment of the present invention there is provided a method of facilitating increased operating efficiency of a wastewater treatment system. The method comprises configuring a dissolved air flotation (DAF ⁾ unit in a wastewater treatment system in fluid communication between a contact tank and a biological treatment unit to remove solids from a portion of a first mixed liquor output from, the contact tank prior to the portion of the first mixed liquor entering the biological treatment unit and to recycle at least, a portion of the solids to the contact tank, the recycle of the at least a portion of the solids to the contact tank reducing an amount of biological oxygen demand to be treated in the biological treatment unit as compared to the wastewater treatment system operating in the absence of recycling the at least a portion of the solids to the contact tank,.

in some embodiments, greater than 50% of the solids are recycled from the DAF unit to the contact tank.

In some embodiments, the method comprises recycling solids from the DAF unit to the contact tank in an amount sufficient to increase biogas productio of an anaerobic digester of the wastewater treatment system having an inlet in fluid communication with an outlet of the DAF unit, at least a second portion of the solids removed in the DAF unit being directed into the anaerobic digester.

In some embodiments, the method comprises recycling solids from the DAF unit to the contact tank in an amount sufficient to reduce the energy consumption of the wastewater -treatment system.

In accordance with an embodiment of the present invention there is provided a wastewater treatment system. The wastewater treatment system comprises a contact tank having a first inlet, a second inlet, and an outlet and a dissolved air flotation tank having an inlet in fluid communication with the outlet of the contact tank, a first outlet, and a second outlet. The wastewater treatment system further comprises an aerated anoxic tank having a first inlet in fluid communication with the outlet of the contact tank, a second inlet, and an outlet and aerobic tank having a first inlet in fluid communication with the outlet of the aerated anoxic tank, a second inlet in fluid communication with the first outlet of the dissolved air flotation tank, and an outlet. The wastewater treatment system further comprises a ciarifier having an inlet in fluid communication with the outlet of ^" the aerobic tank and an outlet in fluid communication with the second inlet of the contact tank and with the second inlet of the aerated anoxic tank.

In accordance with another embodiment of the present invention there is provided a method of treatin wastewater, The method comprises introducing the wastewater into a contact tank,, mixing the wastewater with activated sludge in the contact tank to form a mixed liquor, transporting a first portion of the mixed liquor to a dissolved air flotation tank, separating the first portion of the mixed liquor in the dissolved air flotation tank to form a dissolved air flotation tank effluent and waste bioso!kls, transporting a second portion of the mixed liquor to an aerated anoxic treatment tank, biologically treating the second portion of the mixed liquor in. the aerated anoxic treatment, tank to form an anoxic mixed liquor, transporting the anoxic mixed liquor to an aerobic treatment, tank, transporting the dissolved air flotation tank effluent to the aerobic treatment tank, biologically treating the anoxic mixed liquor and the dissolved air flotation tank effluent in the aerobic treatment tank to form an aerobic mixed liquor, transporting the aerobic mixed liquor to a ciarifier, separating the aerobic mixed liquor in the ciarifier to form a clarified effluent and a return activated sludge, recycling a first portion of the return activated sludge to the contact tank, and recycling a second portion of the return activated sludge to the aerated, anoxic treatment tank.

In accordance with an embodiment of the present invention there is provided a wastewater treatment system. The wastewater treatment system comprises a contact tank having a first inle configured to receive wastewater to be treated, a second inlet, and an outlet. The contact tank is configured to mix the wastewater to be treated with activated sludge to form a first mixed liquor. The system further comprises a DAF unit having an inlet in flui communication -with the outlet of the contact tank, a solids outlet, a DAf unit effluent outlet, and a gas inlet. The gas inlet is configured to introduce gas into the DAF unit to facilitate the flotation of suspended matter from the first mixed liquor and the removal of the suspended matter from the DAF unit. The solids outlet, is in fluid communication with the first inlet of the contact tank, and configured to transfer at least a portion of the suspended matter from the DAF unit to the first inlet of the contact tank. The system further comprises a. biological treatment unit having a first inlet in fluid communication with the outlet of the contact tank, a second inlet, a third inlet in fluid communication with the DAF unit effluent outlet, and an outlet. The biological treatment unit is configured to biologically break down organic components of the first mixed liquor and of an effluent from the DAF unit to form a. second mixed, liquor. The system further comprises a elarifier having an inlet in fluid communication with the outlet of the biological treatment unit, an effluent outlet, and a return activated sludge outlet in fluid communication with the second inlet of the contact tank and with the second inlet of the biological treatment unit. The elarifier is configured to output a clarified effluent through the effluent outlet and a return activated sludge though the return activated sludge outlet.

In accordance with some aspects of the wastewater treatment system, the biological treatment unit includes an aerated anoxic region having a first inlet in fluid communication with the outlet of the contact tank, a second inlet, and an outlet and an aerobic region having a first inlet in fluid communicati n with the outlet of the aerated anoxic region, a second inlet in .fluid communication with the DAI ⁷ uni effluent outlet, and an outlet.

In accordance with some aspects of the wastewater treatment system, the aerated anoxic region and the aerobic region ar included in a same treatment tank.,

in accordance with some aspects of the wastewater treatment system, the aerated anoxic region and the aerobic region are separated by a partition.

In accordance with some aspects of the wastewater treatment system, the aerated anoxic region is included in a first treatment tank and the aerobic region is included in a second treatment tank distinct from the first treatment tank.

in accordance with some aspects of the wastewater treatment system, the

wastewater treatment system comprises a first sub-system including the contact tank and the DAP unit which is physically separated from a second sub-system including the biological treatment unit and the clarifier.

In accordance with some aspects of the wastewater treatment system, the contact tank and the aerated anoxic region are included in a same tank.

In accordance with some aspects of the wastewater treatment system, the wastewater treatment system, further comprises an anaerobic digester having an inlet in fluid communication with the solids outlet of the DAP unit and an outlet.

In accordance with some aspects of the wastewater treatment system, the outlet of the anaerobic digester is in fluid communication with at least one of the contact tank and the biological treatment unit.

In accordance with some aspects of the wastewater treatment system, the wastewater treatment system further comprises a primary clarifier having an inie in fluid communication with a source of the wastewater to be treated and a solids-lean outlet in fluid communication with the contact tank.

In accordance with some aspects of the wastewater treatment system, the wastewater treatment system further comprises a thickener having an inlet in fluid communication with a solids-rich outlet, of the primary clarifier and an outlet n fluid communication with the anaerobic digester.

In accordance with some aspects of the wastewater treatment system, the primary clarifier further comprises a solids-rich outlet in fluid communication with the DAF unit.

In accordance with another embodiment of the present invention there is provided a method of treating wastewater. The method comprises introducing the wastewater into a contact tank including an activated sludge, mixing the wastewater with activated sludge in the contact tank to form a mixed liquor, and directing a first portion of the mixed liquor to a DAP unit. The method farther comprises separating the first portion of the mixed liquor in the DAF unit to form a DAF unit effluent and separated biosolids, directing at least a portion of the separated biosolids from the DAF unit to the contact tank, directing a second portion of the mixed liquor to a biological treatment unit, directing the DAF unit effluent to the biological treatment unit, biologically treating the mixed liquor and the DAF unit effluent in the biological treatment unit to form a biologically treated mixed liquor, and directing the biologically treated mixed liquor to a cl antler. The method further .comprises separating the biologically treated mixed liquor in the ciarifier to form a clarified effluent and a return activated sludge, recycling a first portion of the return, activated sludge to the contact tank, recycling a second portion of the return activated sludge to the biological treatment unit, and directing the clarified effluent to a treated wastewater outlet.

In accordance wi h some aspects of the method of treating wastewater wherein the biological treatment, unit includes an aerated anoxic treatment unit and an aerobic treatment unit, the method further comprises directing the second portion of the mixed liquor to the aerated anoxic treatment unit, treating the second portion of the mixed liquor In. the aerated anoxic treatment unit to form an anoxic mixed liquor, directing the anoxic mixed liquor the aerobic treatment, unit, directing the OAF unit effluent to the aerobic treatment unit, treating the anoxic mixed liquor and the OAF unit effluent in the aerobic treatment tank to form an aerobic mixed liquor, directing the aerobic mixed liquor to the ciarifier, separating the aerobic mixed liquor in the ciarifier to form the clarified effluent and the return activated sludge, and recyclin the second portion of the return activated sludge to the aerated anoxic treatment unit.

In accordance with some aspects of the method of treating wastewater, the first portion of the return activated sludge and the second portion of the return activated sludge comprise about 100% of ail return activated sludge formed in the ciarifier.

in accordance with some aspects of the method of treating wastewater, the first portion of the return activated sludge comprises between about 10% and about 20% of all return activated sludge .recycled from the ciarifier.

In accordance with some aspects of the method of treating wastewater, the first portion of the mixed liquor comprises between about one third and about two thirds of all mixed liquor formed in the contact tank.

In accordance with some aspects of the method of treating wastewater, the DA.F unit removes between about 60% and about 100% of suspended solids in the first portion of the mixed liquor from the first portion of the mixed liquor.

in accordance with some aspects of the method of treating wastewater, an amount of suspended solids removed in the DAF unit is adjusted based upon a concentration of a bacteria in the biological treatment unit. Ιχι accordance with some aspects of the method of treating wastewater, the DAF unit removes between about 40% and about 80% of biological oxygen demand in the first port ion of the mixed liquor from the first portion of the mixed liquor.

In accordance with some aspects of the method of treating wastewater, the method further comprises treating at !east a portion of the wast biosolids in an anaerobic digester to produce an anaerobieaSly digested sludge.

in accordance with some aspects of the method of treating wastewater, the method further comprises recycling at least a portion of the anaerobical!y digested sludge to at least one of the contact tank and the biological treatment unit.

In accordance with some aspects of the method of treating wastewater, the method further comprises separating the water to be treated into a solids-lean portion and a solids-rich portion, directing the solids-rich portion into a thickener to produce a soKds- rich output and a solids-lean effluent, directing the solids-lean portion into the contact tank, directing the solids-rich output from the thickener into the anaerobic digester, and directing the solids-lean effluent of the thickener into the contact tank.

In accordance with another embodiment of the present invention there is provided method of facilitating increased operating efficiency of a wastewater treatment system. ^' The method comprises providing a DAF unit in a wastewater treatment system in fluid communication between a contact tank and a biological treatment, unit, the DAF unit configured to remove solids from a portion of a first mixed liquor output from the contact tank prior to the portion of the first mixed liquor entering the biological treatment unit and to recycle at least a portion of the solids to the contact tank, reducing the amount of biological oxygen demand to be treated in the biological treatment uni as compared to the wastewater treatment system operating in the absence of the DAF unit, and providing for a solids-liquid separation unit in fluid communication downstream of the biological treatment unit to recycle a return activated sludge formed from a mixed liquor output from the biological treatment unit to the contact tank.

In accordance with some aspects, the method further comprises providing for between about 10% and about.20% of the return activated sludge formed to be recycled to the contact tank. In accordance with some aspects, the method farther comprises adjusting an amount of return activated sludge recycled to the contact tank based upon a concentration of a bacteria in the biological treatment, unit.

In accordance with some aspects, the method further comprises providing an anaerobic digester having an inlet in fluid communication with an outlet of the DAF unit and an outlet in fluid communication with at least one of an inlet of the contact tank and an inlet of the biological treatment unit

BRIEF DESCRIPTION OF DRAWINGS

The accompanying drawings are not intended to be drawn to scale. In the drawings, each identical or nearly identical component that is illustrated in various figures is represented by a like numeral. For purposes of clarity, not every component may be labeled in every drawing, in the drawings:

FIG. 1 is a block, flow diagram, of a wastewater treatment system in accordance with an embodiment of the present invention;

FIG. 2 is a block flow diagram of a wastewater treatment system in accordance with another embodiment of the present invention;

FIG- 3 is a block flow diagram of a wastewater treatment system in accordance with another embodiment of the present invention;

FIG. 4 is a block flow diagram of a wastewater treatment system in accordance with another embodiment of the present invention;

FIG. 5 is a block, flow diagram of a wastewater treatment system in accordance with another embodiment of the present, invention:

FIG. 6 is a block flow diagram of a wastewater treatment system in accordance with another embodiment of the present invention;

FIG. 7 is a block flow diagram of a wastewater treatment system in accordance with another embodiment of the present invention;

FIG. 8 is a block flow diagram, of a wastewater treatment system in accordance with another embodiment of the present invention;

FIG. 9 is a block flow diagram of a wastewater treatment system in accordance with another embodiment of the present in vention: FIG, 1.0 is a block flow diagram of a wastewater treatment system in accordance with another embodiment of the present invention;

FIG. 1 1 illustrates a first set of results of a test, of a system in accordance with an embodiment of the present invention; and

FIG. 12 illustrates a second set of results of a test of a sy stem in accordance with an embodiment of the present invention,

DETAILED DESCRIPTION

This invention is not limited in its application to the details of construction and the arrangement of components set forth in the followin description or illustrated in the drawings. The invention is capable of other embodiments and. of being practiced or of being carried out in various ways. Also, the phraseology and terminology used herein is for the purpose of description and. should not be regarded as limiting. The use of "including," "comprising," "having," "containing," ^' "involving," and variations thereof herein is meant to encompass the items listed thereafter and equivalents thereof as well as additional items.

As the term is used herein, an "upstream" unit operation refers to a first unit operation which is performed upon, a fluid undergoing treatment prior to a second unit operation. Similarly, an "upstream" treatment vessel or portion thereof refers to a first. treatment vessel or portion thereof in which a first unit operation is performed prior to a second unit, operation performed in a second treatment vessel or portion thereof. A "downstream" unii operation refers to a second unit operation which is performed opon a fluid undergoing treatment subsequent to a first unit operation. Similarly, a

"downstream ^' ' treatment vessel or portion, thereof refers to a second treatment vessel, or portion thereof in which a second unit operation is performed subsequent to a first unit operation performed in a first treatment vessel, or portion thereof. An upstream unit operation and/or treatment vessel having an outlet in "direct fluid communication" with an inlet of a downstream unit operation and/or treatment vessel directs material output from the outlet of the upstream unit operation and/or treatment vessel into the inlet of the downstream unit operation and/or treatment vessel without any intervening operations performed on the material. A first unit operation and/or treatment vessel described- herein as being in -fluid communication with a second unit operation and/of treatment vessel should be understood as being in. direct fluid communication with the second unit operation and/or treatment vessel unless explicitly described as ^' otherwise. Conduits which provide fluid communication between a first and a second unit operation and/or treatment vessel are to be understood as providing direct fluid communication between the first and second unit operation and/or treatment vessel unless explicitly described as otherwise.

Various unit operations and/or treatment vessels disclosed herein separate fluid and/or sl dge into a solids-rich portion and a solids-lean portion wherein the solid-lean potion has a lower concentration of solids than the solids-rich portion. As the term is used herein, an "effluent" of a unit operation and/or treatment vessel refers to the solids- lean portion of the separated fluid and/or sludge. "Recycle" of material refers to directing material from an outlet: of a downstream unit operation and/or treatment vessel to an inlet of a unit operation and/or treatment vessel upstream of the downstream unit operation and/or treatment vessel.

Co-pending U.S. application serial number 13/210,487, titled "Contact

Stabilization Prime Float Hybrid" is incorporated herein by reference .in its entirety for all purposes.

Aspects and embodiments of the present invention are directed, toward systems and methods for treating wastewater. As used herein the term "wastewater" includes, for example, municipal wastewater, industrial wastewater, agricultural wastewater, and any other form of liquid to be treated containing undesired contaminants. Aspects and embodiments of the present invention may be utilized for primary wastewater treatment, secondary wastewater treatment, or both. Aspects and embodiments of the present invention may remove sufficient contaminants from wastewater to produce product water that may be used for, for example, irrigation water, potable water, cooling water, boiler tank water, or for other purposes.

In some embodiments, the apparatus and. methods disclosed herein provide advantages with regard to, for example, capital costs, operational costs, and

environmental-friendliness as compared to conventional biological wastewater treatment systems. In some embodiments a dissolved air flotation system, is included in a main stream of waste ater emering a biological wastewater treatment system. The dissolved air floatation system may remove a significant amount of biologicai oxygen demand, for example, particulate biologicai oxygen demand, irom wastewater prior to the wastewater entering the biological treatment portion of the wastewater treatment system. This provides for a reduction in the size of the biological treatment portion of the wastewater treatment system for a given wastewater stream, as compared to a conventional wastewater treatment, system and a commensurate reduced capital cost for the overall system. Utilization of the dissolved air flotation system also reduces the requirement for aeration in the biologicai. treatment portion of the treatment system to effect oxidation of the biologicai oxygen demand of the wastewater, reducing operating costs. The amount of waste sludge generated by the biological treatment, portion of the treatment system is also reduced, reducing the amount of waste which would need to be disposed of or otherwise further treated. The material, removed from the wastewater in the dissolved air flotation system may be utilized to produce energy, for example, in the form of biogas in a downstream anaerobic digestion system, The biogas may be used to provide salable energy through combustion or through use in, for example, fuel cells.

A first enibodimen , indicated generally at MX), is illustrated in. FIG. 1.

Wastewater from a source of wastewate 105 is directed into a contact tank Ϊ 10 through an inlet of the contact tank, in the contact tank 1 10, the wastewater is mixed with activated sludge recycled through a conduit 175 from a downstream biological treatment process described below. In some embodiments, the contact tank 1 10 is aerated to facilitate mixing of the wastewater and the acti vated sludge. The aeration gas may b an oxygen containing gas, for example, air. The contact tank 1 10 may be provided with sufficient oxygen such that aerobic conditions are maintained in. at least a portion of the contact tank 1.10. For example, the contact tank 110 may be aerated. Suspended and dissolved solids in. the wastewater, including oxidizable biologicai materials (referred to herein as Biological Oxygen Demand, or BOD), are absorbed into the activated sludge in the contact tank, forming a first mixed liquor. A portion of the BOD may aiso be oxidized in the contact tank 1 10. The residence time of the wastewater in the contact tank may be sufficient for the majority of the BOD to be absorbed by the activated sludge, but no so long as for a significant amount of oxidation of the BOD to occur, in sorae embodiments, for exam le, less than about 10% of the BOD entering the contact tank 1 10 is oxidized i the contact lank. The residence time of the wastewater in the contact tank is in some embodiments from about 30 minutes to about two hours, and in some embodiments, from about 45 minutes to about, one hour. The residence time may be adjusted depending upon factors such as the BOD of the influent wastewater. A wastewater with a higher BOD may require longer treatment in the contact tank 1.10 than wastewater wi h a lower BOD.

A first portion of the first mixed liquor formed in the contact tank is directed into a dissolved air flotation (DAF) system .120 through conduit 1 1 . The DAF system may include a vessel, tank, or other open or closed containment unit configured to perform a dissolved air flotation operation as described below. For the sake of simplicity a dissolved air flotation system will be referred to herein as a "OAF unit." The DAF unit 120 may function as both a thickener and a clarifier. F G. i illustrates two DAF units 120 operating in parallel, however, other embodiments may have a single DAF unit or more than two DAF units. Providing multiple DAF units provides for the system to continue operation if one of the DAF units is taken out of service for cleaning or maintenance.

Before entering the DAF untt(s), air or another gas may be dissolved In the first mixed liquor under pressure. The pressure may be released as the first mixed liquor enters the DAF itnit(s) .1 0, resulting in the gas coming out of solution and creating bubbles in the mixed liquor, in some embodiment , instead of dissolving gas into the first mixed liquor, a fluid, for example, water having a gas, for example, air, dissolved therein, is introduced into the DAF unit(s) 120 with the first mixed liquor. Upon the mixing of the first mixed liquor and the gas-cotitaining fluid, bubbles are produced. The bubbles formed in the DAF unitfs) 120 adhere to suspended matter in the first mixed liquor, causing the suspended matter to float to the surface of the liquid in the DAF unit(s) 120, where it may be removed by, for example, a skimmer.

in some embodiments, the first mixed liquor is dosed with a coagulant, for example, feme chloride or aluminum sulfate prior to or after introduction into the DAF unitfs) 120. The coagulant facilitates floccuiation of suspended matter in the first mixed liquor. in the DAB iraii(s) 120 at least a portion of the solids present in the influent first mixed liquor, including solids from the influent wastewater an from the recycled activated sludge, are removed by a dissolved air flotation process. At least a portion of any oil that may be present in the first mixed liquor may also be removed in the DAF unit(s) 120, In some embodiments, a majority, for example, about 60 or more, about 75% or more, or about 90% or more of the suspended solids in the first mixed liquor introduced into the DAF unites) 120 is removed and about 40% or more, for example, about 50%- or more or about 75% or more of the BOD is removed. Removal of the BOD may include ennieshrnent and adsorption in the first mixed liquor and/or oxidation of the BOD and the formation of reaction products such as carbon dioxide and water, in other embodiments, up to about 100% of the suspended solids is removed in the DAF unii(s) 120 and a majority, for example, up to about 80% of the BOD is removed.

in some embodiments, suspended solids removed in the DAF unit(s) 120 are sent out of the system as waste solids through a conduit 125. These waste solids may be disposed of, or in some embodiments, may ^' be treated in a downstream process, for example, an anaerobic digestion process or anaerobic membrane bioreactor to produce useful, products, for example, bioga and or usable product w ter.

In other embodiments, at least a portion of the suspended solids removed in the DAF unitfs) 120 are recycled back to the contact tank 1 10 through conduits 125 and ί 26. Conduit 126 may branch off of conduit 1.25 as illustrated, or may be connected to a third outlet of the DAF unit(s) 120, in which case suspended solids removed in the DAF tmit(s) 120 are recycled back to the contact tank 1 10 through conduit 126 only. The amount of solids recycled from DAF nnit(s) 120 to the contact, tank 1 10 may range from about 1 % to about 1 0% of a total, amount of solids removed from the first mixed liquor in. the DAP unit(s) .120. The amount of solids recycled from DAF umt(s) 120 to the contact tank 1 10 may be a majority of a total amount of solids removed from the first mixed liquor in the DAF unitCs) 1 20, for example, greater than about 50%, between about 50% and about 95%, or between about 60% and about 80% of the total amount of solids removed from the first mixed liquor in the DAF uirit(s) 120.

Recycling solids removed in the DAF unit(s) 120 to the contact, tank 1 10 is counter to the conventional operation of wastewater treatment systems including DAF units. Typically. DAF units are utilized in wastewater treatment systems to remove solids from the wastewater, thus reducing the need for biological treatment of these removed solids and reducing the energy requirements of the wastewater treatment system by, for example, reducing the amount of air needed to be supplied to an aerated biological treatment vessel to oxidize the removed solids. It is counter to conventional operation of wastewater treatment systems 10 re-introduce floated solids separated from mixed liquor from a contact tank in DAF unitis) hack to the contact, tank. Typically, after solids are separated from mixed liquor from a contact tank in OAF unit(s), reintroducing the separated solids into mixed liquor in the contact tank and force the solids to go through the same separation process in the DAF tmif(s) again reducing the efficiency of the system. Such a solids recycle from DAF unitis) to a contact tank directly upstream of the DAF unitis) would cause a need for a greater amount of contact tank capacity and a greate amount of DAF ^' unit capacity. Such a solids recycle from DAF unitis) to a contact, tank directly upstream of the DAF uniti s) would also require more air flow to the DAF unit(s) to remove the recycled solids from the mixed liquor i addition to any solids that would be present in the absence of the solids recycle. It has been discovered, however, that benefits may be- achieved by the counterintuitive re- introduction of solids removed in DAF urtii(s) back into the contact tank of a wastewater treatment system from which mixed liquor is supplied to the DAF unitis).

For example, by -recycling the solids removed by the DAF unit(s) 120 to the contact tank 1 10, the amount of total suspended solids fTSS) in the contact tank 1 10 may be increased as compared to methods not including a recycle of solids from the DAF unites) 120 to the contact tank 1 10. The. increased TSS level in the contact tank 1 10 may provide for additional soluble BOD to be adsorbed in the contact tank 1 10 as compared to a contact tank 110 having a lower level of TSS. In some embodiments, a desirable TSS level in. the contact tank; 1 10 may be: between about 1 ,200 mg/L and about 3,500 mg/L.

The remo val of the additional soluble BOD in the contact tank 110 due to the .higher TSS level in the contact tank 110, resulting from the recycle of solids from the DAF unit(s) 120 to the contact tank 110» provides for the removal of this additional BOD as solids in the DAF unft(s) 120. The- additional BOD removed as solids in the DAF unitis) 120 may be directed to an anaerobic digester (for example, anaerobic digester 490 ilktsirated in P G, 4) rather than an aerated biological treatment unit (for example, biological treatment unit 130), thus reducing the need for aeration power in the biological treatment unit and increasing the amount of biogas that could be produced in the anaerobic digester.

When supplied with recycled solids from the DAF tioit(s) 120, the contact tank 11.0 may have a hydraulic retention time (HR ) of between about 15 minutes and about one hour and a. solids retention time (SRT) of between about 0,5 days and about two days to effectively adsorb soluble BOD. in other embodiments, the SRT in the contact tank may he between about 0.2 and about 0.4 days. When the contact tank 1 10 includes TSS in a range of between about 1 ,200 mg/L and about 3,500 rng/L, a sludge age (SRT) in the contact tank may range from about one to about two days.

Recycling solids removed in the DAF unit(s) 120 to the contact tank 110 provides for the contact tank 1 10 to function as a high rate activated sludge system while the DAF unit(s) 120 function a solids-liquid separator. Recycling solids removed in the DAF unite s) 120 to the contact tank 1 10 provides for greater oxidation of BOD in the contact tank 1 10 than in systems where solids removed from the DAF unh(s) 120 are not recycled to the contact tank because the solids recycled to the contact tank includes living bacteria capable of oxidizing BOD. For example, in systems and methods where solids removed in the DAF imii{s) 120 are recycled to the contact tank 11 , oxidation of greater than about 10% of the BOD in wastewater influent to the contact tank 1.1.0 may be oxidized in the contact tank. 1 10. Recycling solids removed in the DAF uuit(s) 120 to the contact tank 1 10 may thus reduce the amount of BOD that needs to he treated in downstream unit operations, for example, in the biological treatment unit 130 discussed below, thus reducing the power requirements for the downstream unit operations. The SRT of the contact tank 1.1.0 may be adjusted to optimize BOD removal of particulate, colloidal and soluble BOD fractions.

Effluent from the DAF unit(s) 120 is directed through conduit 124 into the biological treatment unit 130, vvhich may include one or more treatment tanks. In some embodiments, the biological treatment unit 130 may comprise a contact stabilization vessel. A portion of the effluent may be recycled (recycle system not shown in FIG. 1) to supply gas bubbles to the DAF unitfs) 120. A gas may be dissolved into the recycled portion of effluent, which is then directed hack into the DAF u t(s) 120 and mixed with influent first mixed liquor,

A second portion of the first mixed liquor formed in the contact tank is directed into the biological treatment unit 1 30 through a conduit 115. In some embodiments, about a half of the first mixed liquor formed in the contact tank is directed into the DAF umt(s} 120 and about a half of the first mixed liquor .formed in the contact tank is directed through the conduit ί 15 into the biological treatment unit 130. In other embodiments, between about one third and two thirds of the first mixed liquor formed in the contact tank is directed into the DAF imit(s) 120 and the remainder of the first mixed liquor formed in the contact tank is directed through the conduit 115 into the biological treatment unit 130. The amount of the first mixed liquor directed into the DAF unit(s) 120 as opposed to the biological treatment unit 130 may be varied based upon such factors as the concentration of the first mixed liquor and the effectiveness of the first mixed liquor at enmeshing BOD in the contact tank 110.

For example, if it was desired to -remove a greater rather than a lesser amount of solids in the DAF unit(s) 120, a greater fraction of the first mixed liquor from the contact tank would be directed to the DAF unitf ) 120 when the first mixed liquor had a lower rather than a higher concentration of solids. Similarly, if it was desired to remove a greater rather than a lesser amount of BOD in the DAF unit(s) 120, a greater fraction o the first mixed liquor from the contact tank would lie directed to the DAF uriii(s) .120 when the first mixed liquor had a lesser rather than a greater effectiveness at enmeshing BOD in the contact tank.

In the biological treatmen unit 130,. the effluent from the DAF ttnit(s) .120 and the first mixed liquor formed in the contact tank .1 10 are combined to form a second mixed liquor which is biologically treated, hi some embodiments, biological treatmen of the second mixed iiquor in the biological, treatment unit 130 includes oxidation of BOD in the second mixed liquor. To this end, oxygen may be supplied to the second mixed liquor in the biological treatment unit 130 by aeration with an oxygen containing gas, for example, air. In some embodiments, the biological treatment unit 130 is supplied with sufficient oxygen for aerobic conditions to be created in the biological treatment unit 130. in other embodiments, the amount of oxygen supplied is insufficient to meet the entire oxygen ^' demand of the second mixed liquor, and the biological treatment unit 13 , or at least a portion thereof, may be maintained in an anoxic or anaerobic condition.

Nitrification and denitrifiearion of the second mixed liquor may occur in different portions of the aerated biological treatment unit 130, The residence time of the second mixed liquor in the biological treatment unit 130 may be sufficient to oxidize

substantially ail. BOD in the second mixed liquor. Residence time for the second mixed liquid in the biological treatment unit 130 may be from about, three to about eight hours. This residence time may be increased if the influent wastewater to be treated and/or the second mixed liquor contains a high level of BOD or decreased if the influent wastewater to be treated and/or the second mixed liquor includes a low level of BOD.

Biologically treated mixed liquor from the biological treatment unit 130 is directed through a conduit 135 into a separation apparatus, which may include, for example, a elarifier 140, a gra vity separation apparatus, and/or another form of separation apparatus. Effluent from the elarifier 140 may be directed to a product water outlet through a conduit 145 or be sent, on for further treatment. Activated sludge separated from effluent in the elarifier may be recycled back upstream to a wastewater inlet of the system, the source of wastewater, the contact tank 1.1.0 through conduits 155 and 175, and/or the biological treatment unit 1.30 through conduits 155 and 165. in some embodiments 100% of the activated sludge separated in the elarifier is recycled upstream. In some embodiments between about 1 % and about 20% of the recycled sludge is directed to the wastewater inlet and contact, tank through the conduit 175 and between about 80% and 90% of the .recycled sludge is directed into the biological treatment unit 130 through the conduit 165. The amount of recycled sludge directed to the wastewater inlet and contact tank through the conduit 175 may be set at a higher end of this range when the incoming wastewater has a high level of BOD and/or when the recycled sludge is less rather than more effective at enmeshing BOD in the contact tank 1.10. The amount of recycled sludge directed to the wastewater inlet and contact tank through the conduit 175 may be set at a lower end of this range when the incoming wastewater has a low level of BOD and/or when the recycled sludge is more rather than less effective at enmeshing BOD in the contact tank 1 1 . The amount of activated sludg separated in the eiarifier 140 which is recycled to the contact tank 1 1 and/or biological treatment unit 130 may also be adjusted based on a fraction of die first mixed liquor from (he contact tank 1.10 which is directed to the DAF umt(s) 120, the amount of activated sludge which is removed in the DAF urtitsts) 120, and/or the amount of activated sludge removed in the DAF units(s) 120 which is recycled to the contact tank 110, The amount of activated sludge which, is recycled to the contact tank 1 10 and/or biological treatment unit 130 may be an amount equal to or greater than an amount required to maintain a desired population of bacteria in the biological treatment unit 130 to perform biological treatment of the second mixed liquor within a desired timeframe and/or to protect against depletion of the bacteria! population in the event of temporary disruptions in the operation of the treatment system. For example, the amounts of activated sludge which is recycled to the contact tank 110 or biological treatment unit .130 may be set such that sufficient bacteria containing solids are present in the biological treatment unit 130 to result in a S.RT of between about one and about 1 days in the biological treatment unit 130. Similarly,, an amount or fraction of the firs mixed liquor directed into the DAF unit(s) 120 may be adjusted based on the amount of activated sludge recycled from the eiarifier 140, the efficiency of removal of solids in the DAF unif(s) 120 and/or the concentration of one or more types of bacteria in the biological treatment unit 130 to, for example, establish or maintain a desired population of bacteria in the biological treatment unit 130,

in the embodiment illustrated in FIG. i, and in the additional embodiments described below, it should be understood that th various conduits illustrated may be provided with, for example, pumps, valves, sensors, and control systems as needed to control the flow of fluids therethrough. These control elements are not illustrated in the figures for the sake of .simplicity,

in another embodiment, indicated generally at 200 in FIG. 2, the biological treatment unit 130 includes an aerobic region 150 and an aerated anoxic region .160. The aerobic region .150 is in fluid communication downstream of the aerated anoxic region 160 and receives biologically treated anoxic mixed liquor irora the aerated anoxic region. In some embodiments, the aerobic region 150 may be formed in a same vessel or tank as the aerated anoxic region .160 and separated therefrom by a partition or weir 195. In other embodiments, the aerobic region 150 may be physically separate from the aerated anoxic region 160. For example, ihe aerobic region 150 and the aerated anoxic region 1:60 may occupy distinct vessels or tanks or may be otherwise separated from one another. In further embodiments the contact tank 1 10 may be combined with the aerated anoxic region 160 in the same tank.

In the system of FIG. 2 effluent from the DAP anit(s) 120 is directed into the aerobic region 150 without first passing through the aerated anoxic region 160. in other embodiments- the effluent from the DAP unit(s) 1 0 may be introduced into the aerated anoxic region 1 0 and then directed into the aerobic region 150.

Another embodiment, indicated generally at 300, is illustrated in FIG. 3. I this embodiment, the wastewater treatment system 300 is broken into two separate but interconnected subsystems, one subsystem 300A including a contact tank 210 and DAF wnt(s) 220, and a second subsystem 3008 including a biological treatment unit 23 and a separation apparatus 240. In the first subsystem 300A influent wastewater from a source of wastewater 205 A is directed into the contact tank 21 . In the contact tank, the wastewater is mixed with activated sludge recycled through a conduit 275 from a biological treatment process included in subsystem 3GGB described below. In some embodiments, the contact tank 210 i aerated to facilitate mixing of the wastewater and die activated sludge. Suspended and dissolved solids in the wastewater are

adsorbed absorbed into the activated sludge in the contact tank 210, forming a first mixed liquor. A portion of the BOD in the influent wastewater may be oxidized in the contact tank 21 . The residence time of the wastewater in the contact tank may be sufficient for the majority of the BOD to be adsorbed/absorbed by the activated sludge, but. no so long- as for a significant amount of oxidation of the BOD to occur, hi some embodiments, for example, less than about 10% of the BOD entering the contact tank 210 is oxidized in the contact tank. The residence time of the wastewater in. the contact tank: is in some embodiments from about 30 minutes to about two hours, and in some embodiments, from about 45 minutes to about one hour. The residence time may be adjusted depending upon factors such as the BOD of the influent, wastewater. A wastewater with a higher BOD may require longer treatment in the contact tank 210 than wastewater with a lower BOD. A first portion of die first mixed liquor formed m the contact tank is directed into a DAF unit 220 through conduit 214, FIG. 3 illustrated two DAF units 220 operating in parallel., however other embodiments may have a single DAF* unit or more than two DAF units. Providing multiple DAF units provides for the system to continue operation if one of the DAF units is taken out of service for cleaning or maintenance. A second portion of the first mixed liquor formed in the contact tank is directed into the biological, treatment unit. 230 in the second subsystem 300B through conduit 215. in some embodiments, about a half of the first mixed liquor formed in the contact tank is directed into the DAF unitis) 220 and about a half of the first mixed liquor formed in the contact tank is directed through the conduit 215 into the biological treatment unit 230, In other embodiments, between about one third and two thirds of the first mixed liquor formed in the contact tank is directed into the DAF umt(s) 220 and the remainder of the first mixed liquor formed in the contact tank is directed through the conduit 2.15 into the biological treatment unit 230. The amount of the first mixed liquor directed into the DAF unitis) 220 as opposed to the biological treatment unit 230 may be varied based upon such factors as the concentration of the first mixed liquor and the effectiveness of the first mixed liquor at enmeshing BOD in the contact tank. 10.

I the DAF unii(s) 220 at least a portion of the solids present in the influent first mixed liquor, including solids from the influent wastewater and from the recycled activated sludge, are removed by a dissolved air flotation process such as thai described above with reference to DAF onit(s) 120. The removed suspended solids may be sent out of the system as waste solids through a waste conduit 225. These waste solids may be disposed of or treated in a downstream process, for example, an anaerobic digestion process or anaerobic in.emb.rane bioreactor to produce biogas and/or usable product water. Effluent from the DAF nnit(s) 220 is directed to an outlet 235 from, which it may be used as product water or sent on for further treatment.

In some embodiments, a portion of the suspended solids removed from the first mixed liquor in the DAF unitis} 220 may be recycled to the contact lank 210 through conduits 225 and 226 in a similar manner as the recycle of suspended solids removed in the DAF tmit( s) 120 to the contact tank 1 10 described above with reference to FIG. 1. In t&e second subsystem 300B, influent wastewater from a source o wastewater 205B is introduced into the biological treatment unit 230, The source of waste water 205B may be the same as or different from the source of wastewater 205 A. In the biological treatment unit 230 the wastewater and the first mixed liquor formed in t e contact tank 210 are combined to form a second mixed iiquor which is biologically treated. In some embodiments, biological treatment of the second mixed liquor in. the biological treatment unit 230 may include oxidation of BOD in the second mixed, liquor. To this end, oxygen may be. supplied to the second mixed iiquor in the biological treatment unit 230 by aeration with an oxygen containing gas, for example, air. In some embodiments, the biological treatment unit 230 is supplied with sufficient oxygen for aerobic conditions to be created in the biological treatment unit 230. In other

embodiments, the amount of oxygen supplied is insufficient to meet the entire oxygen demand of the second mixed iiquor and the biological treatment unit 230, or at least a portion thereof, may be maintained in an anoxic or anaerobic condition. Nitrification and denitrifieation of the second mixed liquor may occur in different portions of the aerated biological treatment unit 230,

Residence time for the second mixed liquid in the biological treatment tank 230 may be from about three to about, eight, hours. This residence time may be increased if the influent wastewater to be treated and/or the second mixed liquor contains a high level of BOD or decreased if the wastewater and/or the second mixed liquor includes a low level of BOD.

Biologically treated mixed liquor from th biological treatment uni t 230 is directed through a conduit 235 into a separation apparatus, which may include, for example, a elarifier 240. Effluent from, the elarifier 240 may be directed to a product water outlet through a conduit 245 or be sent on for further treatment. Activated sludge separated from effluent in the elarifier may be recycled back upstream to the biological treatment unit 230 and/or to the contact tank 21.0 in subsystem 300.A through a conduit 255. In some embodiments about 100% of the activated, sludge separated in the elarifier is recycled upstream. In some embodiments from about. 10% to about 20% of the recycled sludge is directed to the wastewater inlet and contact tank through a conduit.275 and from about 80% to about 90% of the recycled sludge is directed into the biological treatment unit 230 through a conduit 265.

Utilizing OAF units as described above in a wastewater treatment system provides several advantages over similar wastewater treatment systems operated without. DAF units. Because the DAF units remove a significant portion of suspended solids from influent wastewater without the need for oxidation of these solids, the size of other components of the system may be reduced, resulting in a lower capital cost for the system. For example, primary elarifiers may be omitted from the wastewater treatment system. Due to the reduced amount of oxidized solids to be- removed from the system, a final clarifier, such as the cl rifier 140, may be reduced in size, in some embodiments by about 50%. Because a lower amount, of BOD enters the biological treatment unit (for example, the biological treatment unit 130), the size of the biological treatment unit may be reduced, in some embodiments by about 30%. There Is also a lesser requirement for oxygen in the biological treatment unit which allows for the capacity and power requirements of an aeration system in the biological treatment unit to also be reduced, in some embodiments by about 30%. The reduced size of the components of the treatment system provides for a decreased footprint of the system. For example, a wastewater treatment plant with a capacity to treat. 35 million gallons per day (MOD) of wastewater with an influent BOD of 200 mg/L would require about 150,000 t of treatment units with a conventional design approach; with embodiments of the present invention the footprint could be reduced to about 75,000 it.

in other embodiments of systems and methods in accordance with the present invention, a wastewater treatment system, such as any of those described above, may further include an anaerobic treatment unit (an anaerobic digester). o -limiting examples of components or portion of anaerobic systems that can be utilized in one or more configurations of the wastewater treatment systems include, but are not limited to, the DYSTOR® digester gas holder system, the CROWN® disintegration system, the PEARTH® digester gas mixing system, the PFF© spiral guided digester gas holder, the PPT© vertical guided digester holder, the DUO-DECK™ floating digester cover, and the PPT© heater and heat exchanger system, from Evoqua Water Technologies, The anaerobic digester may be utilized to treat mixed liquor, which may include suspended solids, sludge, arid/or solids-rich or solids-lean, fluid streams, from one or more other treatment units of the wastewater treatment system. At least a portion of an anaerobiea!ly treated sludge produced in the anaerobic digester may be recycled back to one or more other treatment units of the wastewater treatment system. The nature and function of the anaerobic digester and associated recycle streams may be similar to those described in co-pending U.S. patent application number 13/034269, titled "Hybrid aerobic and anaerobic wastewater and sludge treatment systems and methods " published as US 2011/0203992 A 1 , which is herein incorporated by reference in its entirety for all purposes.

The systems and components of embodiments of the invention may provide cost advantages relative to ther wastewater treatment, systems through the use of biological treatment processes in combination with anaerobic digestion. The wastewater treatment systems and processes of embodiments of the present invention can reduce sludge production through the use of various unit operations including aerobic and anaerobic biological processes and recycle streams. The wastewater treatment processes also overcome, some of the technical difficulties associated with use of some anaerobic wastewater treatment processes, by, for example, concentrating or strengthening the sludge introduced into the anaerobic digester. Additionally, costs associated with use of a co ventional aerobic stabilization unit are typically reduced because less aeration would typically be required in the aerobic processes due to the use of the anaerobic digester and various recycle streams. The various processes can also generate methane as a product of the anaerobic digestion process, which can be used as an energy source. In certain embodiments, a large portion of the chemical oxygen demand (COD) and BOD present in influent wastewater to be treated can be reduced using the anaerobic digester. This can reduce the aeration and oxygen requirements, and thus, operation costs of the waste water treatment system, and increase the amount of methane produced that can be used as an energy source. Additionally, because anaerobic digestion can be- used to reduce COD and BOD in the sludge, the sludge yield can also be reduced. The reduction of COD and/or BOD in the anaerobic treatment unit may also provide for a reduction in size of the stabilization tank or other aerobic treatment unit in the wastewater treatment syst m as compared to systems not utilizing the anaerobic digester.

Embodiments of the present invention may provide for the recirculation of aerobic bacteria, anaerobic bacteria, or both through various unit operations of the treatnien t s stem..

It was previously believed that methanogens were strict anaerobic bacteria that would die quickly in an aerobic environment. Various aspects of the invention, however, invol ve treatment systems and subsystems, unit operations, and components thereof that accommodate or increase the survivability of methanogenic organisms. One

advantageous feature of the treatment systems of the present application involves providing a large amount of methanogens through the anaerobic recycle to a contact stabilization process through the unique internal anaerobic sludge recycle path. At least a portion of the methanogenic bacteria retur to the anaerobic digester, thereb seeding the anaerobic digester with methanogenic bacteria to join the existing population of the viable methanogens in the anaerobic digester. This reduces the need for the anaerobic digester to have a size and resultant hydraulic residence time or solids retention time to maintain a stable methanogenic bacteria population in the absence of bacterial seeding, as in previously known processes.

The concentration of seeding methanogenic bacteria, on basis of a count of microorganisms, provided at the input of the anaerobic digester may- in some

embodiments be at least a target percentage, such as about 10% or more, of the concentration, of the methanogenic bacteria present in. the anaerobiealiy digested sludge stream exiting the anaerobic digester. In some embodiments, this percentage may be, for example, about 25% or more, about 33% or more, about 50% or more, or about 75% or more.

The anaerobic digester of systems in accordance with the present invention may be sized smaller than those .in previously known systems. The methanogenic bacteria! seeding of the anaerobic digester also provides for a safety factor against disruptions of the anaerobic digestion process. In the e vent of anaerobic digestion process upset or failure, the anaerobic digesters of the presently disclosed systems would recover faster than that the anaerobic digesters in previously known systems because the seeding of the anaerobic digester with roethanogenie bacteria would add to the rate of replenishment of meihanogenie bacteria in the anaerobic reacto due to the growth of these bacteria therein, reducing the time required for the anaerobic digester to achieve a desired concentration of methanogenic bacteria.

The advantage of methanogen recycle can be estimated as follow:

_& ^V

Where

θ ~ Solids retention time in anaerobic digester (days)

X _a - concentration of methanogens

Q = influent and effluent flow rate

a ¹ ' s= concentration of methanogens in the inlet stream, which is normally considered zero for conventional activated sludge process.

If about 50% of methanogens survive in the short solid retention time contact, stabilisation process and are recycled back to anaerobic digester, the solids retention time of the anaerobic digester could be doubled, or the size of the anaerobic digester decreased by half. For example, in previously known systems a. hydraulic retention time in an anaerobic digester was in man instances set at between about 20 and about 30 days. With a treatment system operating in accordance some embodiments of the present application, this hydraulic retention time ma be reduced by about 50% to between about 10 and about 15 days.

In some embodiments of the apparatus and methods disclosed herein, a hydraulic retention time in a treatment system contact stabilization vessel may be about one hour or less. A significant portion of methanogens can be recycled in. the short, solid retention time contact stabilizati n aerobic process, which can reduce the capita! cost and operational cost of the anaerobic digester(s). For example, the tank volume of the anaerobic digesier{s} could be decreased to bring the safet factor to a range closer to those anaerobic digesier(s) without a methanogen recycle process. Wit smaller volume, the capital cost of the anaerobic digester and the mixing energy consumption of the anaerobic digestion process would both decrease, which will make apparatus and processes in accordance with the present disclosure more cost effective than previously known apparatus and processes,

in other embodiments, the seeding of the anaerobic digester with recycled methanogenk bacteria may provide for decreasing the hydraulic residence time of sludge treated in the digester. This would result in a decreased cycle time, and thus an increased treatment capacity of the treatment system. Increasing the amount of rnefhanogens re-cycled to the anaerobic digester, by, for example, increasing an amount of mefhanogen- containing sludge directed into the digester, would provide greater opportunity to decrease the hydraulic residence time in the digester and increase- the treatment capacity of the system.

If a significant portion of methanogens can be recycled in the aerobic contact stabilization process, the capital cost and operational cost of the anaerobic digesters could be decreased. For example, the tank volume of the anaerobic digesters could be

decreased to bring the safety factor to a range closer to those anaerobic, digesters in systems not including a methanogen recycle process. With smaller volume, the capita! cost of the anaerobic digesters and the mixing energy consumption of the anaerobic digesters will, both decrease, which will make the wastewater treatment process more cost effective.

In certain embodiments, the contact tank is constantly seeded with nitrification bacteria (such as ammonia oxidizing and nitrite oxidizing biomass) which can survive the anaerobic digester and which can be recycled back to the aerobic environment. For example, nitrification and de-nitrification can take place in. the contact tank. Nitrification ^• may be carried, out by two groups of slow-growing autotrophs ^* ammonium-oxidizing bacteria (AOB), which convert ammonia to nitrite, and nitrite-oxidizing bacteria (NOB), which oxidize nitrite to nitrate. Both are slow growers and strict aerobes. In some embodiments of treatment systems disclosed herein, the nitrification bacteria are introduced to and/or grown in a contact tank, where they are captured in the floe. Some of the nitrification bacteria will pass out from, the contact tank and lie sent to an anaerobic digester,

it. was previously believed that the strictly anaerobic conditions of the anaerobic digester would kill the nitrification bacteria. Various aspects of the invention, however. involve treatment s stems and subsystems, unit operations, ami components thereof that accommodate or increase the survivability of nitrification organisms in anaerobic and anoxic conditions that may occur in some biological nutrient removal processes.

Nitrification bacteria which survive the anaerobic digester and are returned to the aerobic part of the treatment process may enhance the nitrification process performance in wa s that can lower capital costs, for example by providing for a reduced aerobic treatment vessel size and or reduced aerobic treatment hydraulic retention time and/or an increased safety factor that would render the nitrification process more stable in response to disruptions to the treatment process. Disruptions to the treatment process encompass deviations from desired operating parameters which may be caused by, for example, interruptions in flow of materia] through the treatment system or a loss of temperature control at one or more unit operations. The survival rate of nitrification bacteria in an anaerobic digester could be increased by decreasing a hydraulic residence time in the anaerobic digester, which would be accomplished if the anaerobic digester were seeded with recycled methanogens, as described above.

A wastewater treatment system, indicated generally at 400 in FIG, 4, includes an anaerobic treatment, unit 490, referred to herein as an anaerobic digester. The wastewater treatment system of FIG, 4 includes a contact tank 410, a DAF unit 420, a stabilization tank 430, a clanfier 440, and associated fluid conduits 414. 424, 435, 445, 455. 465, and 475 which are similar in structure and function to the contact tank 1 .10, DAF unit 120, biological treatment unit 130, clarifier 140, and associated fluid conduits .1 .14, 124, 135, 145, 1.55, 165, and 175 of the system illustrated in FIG, 1. and described above.

singular DAF unit 420 is illustrated in FIG. 4, although in alternate embodiments the treatment system may use multiple DAF units as described above with reference to the treatment system of FIG. L

In the system of FIG. 4, wastewater from a source of wastewa ter 405 is directed into a primary clarifier 412 through an inlet of the primary clarifier. A solids-rich fluid stream from the clarifier is directed through conduit 404 into an inlet of a thickener 480, which may comprise, for example, a gravity belt thickener. A solids-lean effluent from the primary clarifier 412 is directed into an inlet of the contact tank 410 through conduit 402. A solids-rich output stream from the thickener 480 is directed to an inlet of the anaerobic digester 490 through conduit 484. A so!ids-lean effluent From the thickener is directed to an inlet of the contact tank 410 through condui t 482. The anaerobic digester is also supplied with suspended solids removed from mixed liquor in the DAP unit 420 through conduits 425 and 4 4.

In some embodiments, a portion of the suspended solids removed from the mixed liquor in the DAF unit 420 may be recycled to the contact tank 410 through conduits 425 and 426 in a similar manner as the recycle of suspended solids removed in the DAF uttiti ^' s) 120 to the contact tank i 10 described above with reference to FIG. 1.

The solids-rich output stream from the thickener 480 and any suspended solids from the DAF unit 420 introduced into the anaerobic digester 490 are combined and anaerobtcally digested in the anaerobic digester. The anaerobic digestion process can be operated at temperatures between about 20*C and about.75°C, depending, on the types of bacteria utilized during digestion. For example, use of rnesophilic bacteria typically re-quires operating temperatures of between about 20*C and about 45°C, while

thermophilic bacteria typically require operating temperatures of between about 50°C and about 75 ^a C. In certain embodiments, the operating temperature may be between about 25 *C and about 35 ^C C to promote rnesophilic activity rather than, thermophilic activity. Depending on the other operating parameters, the retention time in the anaerobic digester can be between about seven and about 50 days retention time, and in some embodiments, between about 15 and about 30 days retention time. In certain embodiments, anaerobic digestion of mixed liquor in the anaerobic digester may result in a reduction in oxygen demand of the mixed liquor of about 50%.

A first portion of an anaerobically digested sludge produced in the anaerobic digester may be recycled through an outlet of the anaerobic digester and into the

stabilization tank 430 through conduit 492. This recycle stream may Facilitate retaining sufficient solids in. the system to provide a desired residence time in the stabilization tank. The anaerobically digested sludge recycled to the stabilization tank may also seed the stabilization tank with nitiilication bacteria to enhance the nitrification activity within the stabilization tank as described above. The anaerobically digested sludge recycled into the stabilization tank may also contain methanogenic bacteria which are subsequently returned to the anaerobic digester to enhance the rfo mance of the anaerobic digester as descri ed above.

In embodiments where the stabilization tank 430 includes an aerated anoxic region and an aerobic region, such as in the biological treatment unit 130 of FIG. 2 described above, the portion of the anaerobically digested sludge recycled to the stabilization tank may be. directed into the aerated anoxic region of the stabilization tank. A second portion of the anaerobic-ally digested sludge produced in the- anaerobic digester may be sent out of the system as waste solids through a conduit 495. The first portion of the aoaerobicaliy digested sludge recycled into the stabilization tank 430 may be any amount between about 0% and about 100% of the anaerobically digested sludge produced in and output, from the anaerobic digester, with the second portion, making up the balance, sent out of e system as waste solids through conduit 495. In some embodiments, between about 0% and about 80% of the anaerobically digested sludge is recycled from one or more outlets of the anaerobic digester to one or more other unit operations of the treatment system,

in another embodiment of the wastewater treatment system, indicated generally at 500 in FIG. 5, the .first portion of the anaerobically digested sludge produced in the anaerobic digester is recycled through an outlet of the anaerobic digester and into the inlet of the contact tank 410 through conduit 494, rather than into the stabilization tank 430. This recycle stream may facilitate providing sufficient activated sludge in the contact tank to absorb/absorb or enmesh BOD present in the influent wastewater. The anaerobically digested sludge recycled to the contact, tank may also seed the contact tank with nitrification bacteria to enhance the nitrification activity within the contact tank as described above. The anaerobically digested sludge recycled into the contact tank may also contain methanogenic bacteria which are subsequently returned to the anaerobic digester to enhance the performance- of the anaerobic digester as described above. The first portion of the anaerobically digested sludge recycled into the contact tank 410 may be any amount between about 0% and about 100% of the anaerobically digested sludge produced in and output from the anaerobic digester, with a second portion, making up the balance, sent out of the system as waste solids through conduit 495, in another embodiment of the wastewater treatment system, indicated generally at 600 in FIG. 6, a first portion of the anaerobicaily digested sludge produced in the anaerobic digester may be recycled through an outlet of the anaerobic digester and into the inlet of the contact tank 410 through conduit 494, and a second portion of the anaerobicaily digested sludge may be recycled through an outlet of the anaerobic digester and into the stabilization tank 430 through conduit 492. These recycle streams may provide the benefits described above with regard to systems 400 and 500. A third portion of the anaerobicaily digested sludge may be directed to waste through conduit 495. The sura of the first portion of the anaerobicaily digested sludge and the second portion of the anaerobic sludge may be any amount between about 0% and about 1.00% of the aoaerobically digested sludge produced in and output from the anaerobic digester, with the third portion, making up the balance, sent out of the system as waste solids through conduit 495. The recycled anaerobic sludge may be split in any desired ratio between the first portion and the second portion. The first potion may comprise from about 0% to about I < ⁾ < ^} ¾· of all the anaerobicaily digested sludge produced in and output from the anaerobic digester with the sum of the second portion and the third portion making up the balance.

Another embodiment of the wastewater treatment system, indicated generally at 700 in FIG. 7, is similar to that illustrated in FIG. 6, however the thickener 480 is not utilized. Rather, the solids-rich fluid stream from the clarifier is directed through conduit 406 into an inlet of the DAF unit 420. The DAF unit 420 of the system illustrated in FIG. 7 performs the function of the thickener 480 of the system Illustrated in FIG. 6. The utilization of the DAF unit 420 to perform the function of the thickener may reduce or eliminate the need for a thickener in the system, which may reduce both capital and operational costs of the system. A first portion of the anaerobicaily digested sludge created in the anaerobic digester 490 is recycled to the contact tank 10 and a second portion is .recycled to the stabilization tank 430 to provide the benefits described above. A third portion of the anaerobicaily digested sludge is directed to waste through conduit 495,

Further embodiments may include any combination of features of the systems described above. For example, in some embodiments, a first portion of the solids-rich ^• fluid stream from the elarifier is directed through conduit 406 into ao inlet of the DAF unit 420, while a second portion is directed in to a thickener 480. In any of the above embodiments, the stabilization tank 430 may include an aerated anoxic region and an aerobic region. A first portion of the anaerbbicaliy digested sludge recycled to the stabilization tank may be directed into the aerated anoxic region of the stabilization tank and a second portion may be recycled to the aerobic region. The ratio the amount of recycled anaerobic sludge directed to the aerated anoxic region to the amount of recycled anaerobic sludge directed to the aerobic region may be any ratio desired. Any of the above embodiments may include mul tiples of any of the treatment units and/or conduits illustrated.

EXAMPLES

Example 1

A wastewater treatment system 1000 was configured as illustrated in FIG. .10, where the indicated unit operations and conduits have the same structure and function as the identically indicated unit operations and conduits in FIGS. 4-7. The wastewater treatment system 1000 was used to examine the effects of recycling removed solids from the DAF unit 420 to the contact tank 410. By gradually increasing the amount, of removed solids from the DAF unit 420 recycled to the contact tank 410 from 0% of the solids removed in the DAF unit to about 90% of the solids removed in the DAF unit over the course of three weeks, the suspended solids ( LSS) content of contact tank was brought up from 600 mg L to over 1200 mg/L. The DAF dissolved solids conten increased from 3 -4% prior to beginning the recycle of solids from the DAF unit to the contact tank to above 5% after beginning the recycle of solids from the DAF unit to the contact tank. The total suspended solids (TSS) removal efficiency of the DAF unit increased from about 75% to over 85%. The COD removal of the DAF unit increased from about 70% to about 80% over the course of the testing. These results are illustrated in the charts of FIG. I I and FIG. 12.

These results show that recycling removed solids from a DAF unit to a contact tank in a system such as that illustrated in FIG. 10 may provide for a greater amount of suspended solids in the contact tank. The increased amount of suspended solids in the contact tank increases the amount of suspended and soluble COD and BOO which may be removed from wastewater influent to the contact tank and

absortsed adsorbed/enraeshed in the suspended solids and/or which may be oxidized in the contact tank. Recyclin removed solids from a OAF unit to a contact tank in a system such a that illustrated in FIG. 10 increases the efficiency of the removal of suspended solids in the AF unit These effects may decrease the load on downstream unit, operations and may reduce operating costs of the system as a. whole and/or may reduce capita! costs of the system by providing for smaller downstream processing units to be utilized. Further, a greater amount soluble BOD/COD from wastewater influent to the system may be removed as solids in the DAF unit and may be sent from the DAF unit to an anaerobic digester instead of an aerobic treatment unit, operation, reducing the aeration power requirements of the system and increasing the amount of biogas that could he produced.

Prophetic Example i

In thi prophetic example, a water treatment system was configured as illustrated in FIG. 1 with the biological treatment unit .130 comprising a single tank.

Assumptions of Feed:

The system was fed wastewater at a rate of 57,600 gallons/day (gpd), 40 gallons per minute (gpm). The wastewater was assumed to be. typical of municipal wastewater, having a total BOD (tBOD) of 140 rog/i. (6? lbs/day} of which 43% (60 nig/I, 29 lbs/day) was particulate (non-soluble) BOD (pBOD), and 57% (80 mg/i, 38 ibs/da ) was soluble BOD (sBOD). The wastewater wa also assumed to include 100 mg I (48 ibs/day) of suspended solids (SS), of which .1 lbs/day (48 lbs/day SS ~ 29 lbs/day pBOD) was assumed to be inert (non-biological) material, and 6 lbs/day of ammonia.

HDT Assumptions;

The hydraulic detention time (HDT) in the contact tank 1 10 was assumed to be 45 minutes and the hydraulic detention time (HDT) in the biological treatment, unit 130 was assumed to be five hours. Row Rate Through Contact Tank;

The ratio of return sludge sent from the clariiler 140 to the contact tank was set at 2.4 lb/lb of ^' tBQD, for a (2.4>(6? ibs/day tJBOD) =* 160 lbs/day recycled sludge or 2,880 gpd (2.0 gpm), assuming a recycled sludge solids loading of 6,660 rag/1. The total flow through the contact tank was thus 57,600 gpd + 2,880 gpd = 60,480 gpd (42 gpm).

From laboratory bench scale testing, it. was found that in the contact tank, approximately 50% of the sBOD was removed, with approximately 2/3 of the amount removed converted to SS, and approximately 1/3 of the amount removed oxidized, for example, converted to carbon dioxide and water. Thus, it was assumed that in the contact tank 14 lbs/day of sBOD was converted to SS and 5 ibs/day of pBOD was oxidized. The total solids passed through the contact tank was thus 160 Ibs/day recycled sludge + 48 ibs/day suspended solids from influent wastewater + 1.4 Ibs/day sBOD converted to SS - 5 lbs pBOD oxidized = 217 ibs/day. The mixed liquor suspended solids (MLSS) leaving the contact tank was thus ((217 lbs/day)/(60,480 gpd))(453592.4 mg/3b)(0.2641721 gal/l) = 430 mg/L

The iBOD leaving the contact tank was 67 ibs/day input. - 5 lbs/day oxidized = 62 ibs/day (121. mg i). The sBOD leaving the contact tank was 38 lbs/day in - 14 ibs/day converted to SS - 5 ibs/day oxidized = 19 Ibs/day (37 mg 1). The pBOD leaving the contact tank was 29 ibs/day influent + 14 lbs/day converted from sBOD = 43 lbs da (84 .mg 1).

Flow Split into DAF and Biological Treatment Tank:

The How out of the contact tank was split between the DAF units 120 and the biological treatment unit 1.30. 46,5% (101 lbs/day, 28,080 gpd, 19.5 gpm) of the output of the contact tank was directed to the DAF units and 53.5% ii l6 lbs/day, 32.400 gpd, 22.5 gpm _. ) was directed into the biological treatment unit,

it was assumed that ail recycled sludge directed to the DAF units (160 ibs/day introduced into contact tank ~ 1 16 Ibs day returned to biological treatment tank ~ 44 ibs/day) was removed in the DAF process. BOD influent to Biological Treatment Unit;

The total BOD to be treated in the biological treatment unit includes the BOD from the contact tank (53.5% of 62 !bs/day - 33 lbs/day) in 32,400 gpd of influent plus BOD from the DAF units. The p ^' BOD influent to the DAF units was 46.5% of 43 lbs/day output from contact tank = 20 lbs/day. The sBOD influent to the DAF units was 46.5% of .19 lbs/day output from the contact tank = 9 lbs/day at a flow rate of 28,800 gpti Assuming 80% of the pBOD was removed in the DAF units, the tBOD flowing from the DAF units to the biological treatment tank was (0.2* 20 lbs/day pBOD) + 9 lbs/day sBOD = 13 lbs/day tBOD. Thus the total influent BOD to the biological treatment tank was 33 ibs/day from the contact tank 4- .13 lbs/day from the DAF units = 46 lbs/day.

Solids in Biological Treatment Tank:

The biological treatment unit was sized to accommodate a BOD loading of 29 .lbs/1.000 it ⁵ , a common loading in the industry. This meant that the volume of the biological treatment unit was (46 Ibs day influent tBOD)/(29 lbs 1000 ft ^"' tBOD loading) - .1 ,600 if ( 12,000 gal). This volume resulted in a HDT in the biological treatment trait of (12,000 gal/57,600 gpd)(24hr/day) = 5 hours. The total solids in. the biological treatment unit was set at 220 lbs, for a total MLSS of (220 lbs/12,000 gaf X0.264 ga.i/I)(453,592 rng/Sb) = 2200 nig/1. Assuming a sludge yield of 95% of the BOD results in an amount of waste sludge produced in the biological treatment unit of (0.95}(46 lbs/day tBOD) - 44 Ibs/day waste sludge. The waste sludge age would thus be {220 lbs total so1kis)/(44 lbs day waste sludge) = 5.2 days.

Biological Treatment Tank Oxygen Requirements:

It was assumed that 0.98 lbs of oxygen were required to oxidize a pound of BOD and 4.6 lbs of oxygen were required to oxidize a pound of ammonia. The oxygen requirement of the biological treatment unit was thus (0.98 lbs O^ ib BOD)(46 lbs tBOD/day) + (4.6 lbs 0? ib anunonia)(6 lb/day ammonia) = 72.6 lb/day <¼ (3 lb Oj/hr). Using a FCF (field Correction Factor - a correction factor to compensate for the reduced oxygen absorbing ability of mixed sludge in the biological treatment tank as opposed to clean water) of 0.5, this Jesuits in a specific oxygen utilization rate (SOUR) of 6 lbs 0?/hr. Assuming diffused air was supplied to the biological treatment tank from a aeration system submerged by nine feet and a 6% oxygen transfer capability (OTE), the biological treatment unit would require a f ow of (6 lbs ϋ¾¾·)ί i/ . 6)( l/60

hour/min)(l /I .429 l/g 0?.X453.6 g lb)(0.()35 ffVi ) - 18.5 ft ^' Vmin (sefm), or if aerating with air with approximately 20% 0 , 92.6 scfm.

Cla ifier:

The clarifier was assumed to have a 61 ft volume. 57,600 gpd flowed into the clarifier, resulting in an overflow of 57,600 gpd/61 ft ^" = 944 gallon per ft ² per day (gpsfcl) overflow rate. Assuming an MLSS of 2200 mg/1 from the biological treatment tank and targeting a recycled sludge (RAS) concentration of 6600 mg/1 and 50% of overflow recycled as RAS gives a RAS flow rate of 20 gpm (28,800 gpd). It was assumed that 18 gpm RAS was recycled to the biological treatment tank and 2 gpm to the contact tank. The solids loading of the clarifier was thus (57,600 gpd infl uent wastewater + 28,800 gpd RASX2200 mg/1 MLSSX 1/453592.4 lb mg}(3.79 !/gal)/(61 ft ³ ) = (1 88 lbs/day)/ ( 1 ft ² ) = 26 lb/ ft -day.

Solids Wasted:

Solids wasted in DAF units: 101 lbs/day (assuming 100% efficiency).

Rati of sludge wasted to BOD treated: (101 lbs/day )/(67 lbs/day tBOD in wastewater influent) - 1.5

With the addition of the DAF units to the treatment system in the above example, the amount of tBOD to be treated in the biological treatment tank was reduced from 62 lbs/day to 46 lbs/day, a reduction of 26%. This provided for a reduced required size for the biological treatment tank, to obtain a desired solids loading and resulted in a decrease in the required amount of air needed to treat this tBOD in the biological treatment tank. This would translate Into a cost savings for both capital costs, for a reduced size of the biological treatment tank and aeration system, as well as a decreased operating cost due to the reduced amount of aeration required. Prophetic Example 2

A simulation was performed using BIOWIN™ simulation software (EnviroSim Associates Ltd., Ontario, Canada) to compare the performance of a wastewater treatment system in accordance with an embodiment of the present invention with and without an anaerobic sludge recycle.

The wastewater treatment system without the anaerobic sludge recycle included was configured as illustrated in FIG. 8, indicated generally at.800. This system is similar to that illustrated, in FIG, 4, but with no anaerobic sludge recycle conduit 492 and with the addition of a membrane bioreactor (MBR) 510 which recei es a solids lean effluent from the clarifier 440 through conduit 442, The MBR produces a product water permeate which is removed from the system through conduit 445, and a solids-rich retentate, which is recycled to the DAF unit 480 through conduit 444, The MBR 510 was simulated to perform, complete nitrification of the solids lean effluent from the clarifier 440.

The performance of the wastewater treatment of FIG, 8 was simulated and compared to the simulated performance of the wastewater treatment, system 900 of FIG. 9, Wastewater treatment system 900 of FIG. 9 is similar to wastewater treatment system 800 of FIG, 8, ^' but with the addition of an anaerobic sludge recycle conduit 492 recycling anaerobically digested sludge from the anaerobic digester 490 to the stabilization tank 430 though conduit 492. In the simulation of the wastewater treatment system 900. 45% of the anaerobically digested sludge output from the anaerobic digester 490 was recycled to the stabilization tank 430, and 55% of the anaerobically digested sludge output from the anaerobic digester 490 was sent to waste.

The simulation of the performance of both systems 800 and 900 assumed an influent wastewater flow rate of 100 MGD. The influent wastewater was assumed to have a COD of 500 mg/L, a total suspended solids (TSS) of 240 mg/L, a Total KjeldaM Nitrogen (T N) of 40 mg L, and a temperature of 1.5*0.

The results of the simulation indicated that the anaerobically digested sludge recycle of the system 900 resulted in a decrease in the total oxygen requirement for treating the influent wastewater as compared to the system 800 of from 1 13,891 kg O^/day to 102,724 kg Oj day . a savings of about 10%. Assuming an oxygen transfer energy requirement of .1.5 kg Oj kwh, this reduction in oxygen consumption would reduce the power requirements associated with providing the oxygen from 75,988 kwh/day to 68,483 kwh/day, a savings of 7.515 kwh/day.

The results of the simulation indicated that the anaerobically digested sludge recycle of the system 900 resulted in an increase in the amount of methane produced as compared to the system 800 from .1 ,348 scfm t 1 ,652 scfm, an increase of about 23%. Assuming that 35% of the methane chemical energy could he converted to electricity, the potential electricity generation from the methane produced would increase from 104,51 1 kwh/day to 128,989 kwh/day.

Combining the energy reduction .from the reduced oxygen requirement with the energy gain from the increased methane production results in an energy savings of about 3 ,982 kwh/day for the system 900 including the anaerobically digested sludge recycle as compared to the system 800 without the anaerobically digested sludge recycle.

The results o the simulation also indicated that adding the anaerobicall digested sludge recycle of the system 900 to the system 800 resulted in a reduction in biomass (sludge) production from 81,003 pounds per day to 61 , 167 pounds per day, a reduction of about 25%.

This simulation data indicates that the addition of an anaerobically digested sludge recycle to wastewater treatment systems in accordance with the present invention may result in a significant reduction in power consumption and a significant decrease in waste sludge production, both of which would result in cost savings and enhanced environmental-friendliness of the wastewater treatment system.

Prophetic Example 3

Calculations were performed to compare the performance of a wastewater treatment system in accordance with an embodiment of the present invention with and without a recycle of solids removed in a DAP unit of the system to a contact tank of the system. The wastewater treatmen system was configured as illustrated in FIG. 10.

It was assumed that the system was provided with 40 million gallons per day of wastewater influent with a BOD level of 250 mg/L (83,400 ihs/day) and suspended solids of 252 mg/L (84,000 lbs/day). It was assumed that the biological treatment tank 430 operated with a solids retention time (S T) of 5 days, a mixed liquor suspended solids (MLSS) concentration of 3,000 mg L and a BOD loadin of 45 lbs/1 ,000 cubic feet (20.4 kg/28.3 cubic meters) and that all solids separated in the clarifier 440 were recycled to the contact, tank 410. The hydraulic detention time (HDT) of ^" the contact tank 410 was assumed to be 25 minutes for the system operating without the _: DAF to contact tank solids recycle and one hour for the system operating with the DAF to contact tank solids recycle. The increase in HDT in the contact tank for the system when operating with the DAF to contact tank solids recycle was to provide for the increased MLSS in the contact tank to adsorb additional soluble BOD in the contact tank as compared to the system operating withou the D AF to contact tank solids recycle, For the system operating with a recycle of solids from the DAF unit to the coo tact tank, it was assumed that, the DAF unit removed 308,000 lbs/day (1 9,706 kg/day) of solids from the mixed liquor passing through it and recycled 190,000 lbs/day (86, 1.83 kg/day, 62% of the solids removed) to the contact tank while directing 1 1 8,000 ibs/da (53,524 kg/day) of solids to the anaerobic digester 490.

A comparison of the results of the calculations comparing the system with and without th DAF to contact tank solids recycle is .illustrated in Table 1 below:

Table ί

Parameter System operated without System, with 62% DAF ~

DAF -> Contact tank Contact tank recycle recycle

BOD treated in biological 41 , 200 (18,688 kg day) 20,600 (9,344 kg/day) treatment tank (lbs/day)

Aeration energy (both

conusor tank and biological 600 4.1

treatment tank, kW)

Solids to anaerobic digester 103,000 (46,720 kg/day) 1 15,000 (52, 163 kg/day) (lbs/day)

Solids destroyed (lbs/day) 43,900 (19,913 kg/day) 55,900 (25,356 kg day)

Biogas produced (mcfd/day) 0.6 ( 18,633 cubic 0.84 (23,730 cubic

meters/day) meters/day Ί

Biogas energy (assuming 1 ,880 2,390

40% conversion efficiency,

kW)

Net energy gain (kW) 1 ,280 1 ,880

These results show that providing a wastewater treatment system as configured in FIG. 1 with a recycle of solids removed in a DAF unit to a contact tank can significantly reduce the energy required to operate the system as compared to an equivalent system without the recycle of solids from, the DAF unit to th contact tank. Adding the DAF to contact tank solids recycle results in less BOD being sent for treatment in the biological treatment tank (a reduction of (41,200 - 20,600)/4 i ,200 ~ 50% in the present example) which lowers the need for aeration in the biological contact tank, A greater amount of biogas ((0.84 - 0.66)/0.66 - 27% more in the present example) is produced when adding the DAF to contact tank solids recycle to the system. The combined gain in biogas production and decrease in aeration energy requirements results in a net energy gain of 1 ,880 - 1 ,280 = 600 kW when adding the DAF to contact tank solids recycle to the system. At an estimated $0.1 kVV energy cost, this net energy gain would yield a cost sa vings of abou t $530,000 per year.

Having thus described several aspects of at least one embodiment of this invention, it is to be appreciated various alterations, modifications, and improvements will, readily occur to those skilled in the art. Such alterations, modifications, and improvements are intended to be part of this disclosure, and are intended to be within the spirit and scope of the invention. Accordingly, the foregoing description and drawings are by way of example only.

What is claimed is;