CZ2003948A3 - Method and apparatus for wastewater treatment with enhanced reduction of solids - Google Patents

Abstract

A wastewater treatment process that provides improved reduction of total solids through endogenous respiration while reducing biochemical oxygen demand and utilizing biological nutrient reduction. The wastewater treatment process uses an efficient aeration delivery system to drastically reduce the time needed to oxidize organic matter, and re-circulates, shreds and homogenizes the organic matter and microorganisms and oxygenates the entire mass many more times than traditional systems resulting in a greater biological solids digestion rate.

Description

The present invention relates to a method and apparatus for treating aqueous waste with the design of improved aqueous waste treatment. In particular, the invention relates to methods and apparatus utilizing improved functionality, ease of operation, and aeration techniques to provide improvements in aqueous waste treatment.

BACKGROUND OF THE INVENTION

The present application derives its priority from US provisional application Serial Number 60 / 238,878, the entire contents of which are hereby incorporated by reference.

At present, the processes used in wastewater treatment plants are based on traditional processes that consume energy, materials and work in relatively large quantities, along with extensive land use. The high costs associated with traditional wastewater treatment methods are due to the treatment, handling and monitoring of all components of the wastewater flow with equipment such as pumps, blowers, air compressors, rakes, filters, chemicals, heat, pressures, coagulants, flocculants, precipitants and desiccants. In traditional wastewater treatment systems, wastewater is treated using a high energy consumption process. These procedures include, but are not limited to, aerobic digestion, anaerobic digestion, sludge thickening and solids drying processes.

• · · · · · · · · · · · · · · · · · · · · · · · · · · · · The consequences of these adjustments represent approximately 85% of the operating energy budget of the installation.

In a typical effluent feed stream that is subjected to a effluent treatment, 99.9% of the total effluent stream is water and approximately 0.1% are organic, inorganic and dissolved solids. A conventional feed stream also contains nutrients at various concentrations. The nutrients in the waste water stream that need to be removed have oxygen demand which must be filled to achieve decomposition. In industry, this oxygen demand is referred to as biochemical oxygen demand (BOD). Of about 0.1% of the solids, about 10% to 20% of the settable solids comprise about 35% of the BOD. The remaining 65% of the POI is contained in the dissolved part of the organic matter of municipal waste. See Figure 13.

In solids (sludge) systems in traditional sewage treatment plants, processing energy is consumed to reduce organic matter by digestion to a level of about 50% volume reduction, with the remaining 50% by volume of organic matter being disposed of by a number of means, such as, but not limited to, disposal in the ground, ashing and scattering to the ground. This results in additional energy and cost for solids processing. It would therefore be advantageous to have a system and method that would eliminate most of the consumption requirements for the disposal of organic matter.

It is an object of the present invention to provide an apparatus and method for treating aqueous waste containing organic matter and chemicals.

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Another object of the present invention is to use an activated sludge recirculation process in the treatment zone a

greater aeration efficiency to reduce the time and energy required to decompose organic matter.

Yet another object of the present invention is to substantially reduce the disposal of organic matter in the form of waste active sludge (WAS), which is the deliberate removal of organic deposited solids from the system, and thus to reduce the effort and cost of the solids handling device.

Yet another object of the present invention is to provide an apparatus and method for treating aqueous waste containing high concentrations of industrial type nutrients.

Yet another object of the present invention is modified municipal waste _15, which has the usual concentration of the chemical oxygen demand (COD), BOD, ammonia and phosphorous.

Yet another object of the present invention is to treat industrial heavily polluted waste having high concentrations of COD, BOD, ammonia and phosphorus levels, which can usually be found in animal waste.

Yet another object of the present invention is to provide an apparatus and method for pretreating wastewater downstream of facilities directly in place, such as may be in industrial manufacturing or such as animal waste facilities.

Yet another object of the present invention is to utilize an efficient, recirculating aeration system (RCAS) that provides a combination of aeration, mixing, homogenization and comminution that is superior and attainable than conventional aeration systems.

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Yet another object of the present invention is to provide an apparatus and method with the possibility of easier design, operation, construction, commissioning, management, expansion and maintenance than is possible with conventional waste treatment systems.

Yet another object of the present invention is to provide an apparatus and method that is easier to adapt to changes in processing and flow conditions, and that it is easier to automate, monitor, and control than is possible with conventional waste treatment systems.

It is yet another object of the present invention to provide an apparatus and method that uses a generally smaller base (land area) compared to conventional wastewater treatment plants than conventional wastewater treatment plants.

Yet another object of the present invention is to provide a device and method that are more economical to operate than conventional wastewater treatment systems.

Yet another object of the present invention is to provide an apparatus and method that is cheaper to design and operate than conventional wastewater treatment systems.

Yet another object of the present invention is to provide an apparatus and method that enhance the processing vessel's ability to treat larger amounts of wastewater in aeration tanks by not being limited by the bottom surface area of the vessel to accommodate diffusers in terms of the ability to provide intense aeration.

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Yet another object of the present invention is to provide an apparatus and method that provides a substantially increased decay coefficient (k _d ).

Yet another object of the present invention is to provide an apparatus and method that increases the mean cell residence time (MCRT) over time in conventional waste treatment systems, thereby providing increased destruction of volatile solids and consequently reduced solids handling efforts.

It is yet another object of the present invention to provide an apparatus and method that allows a highly flexible range of nutrient to microorganism (F / M) ratios to be achieved, above and below ranges, in conventional waste treatment systems.

Yet another object to provide the apparatus and method of the present invention is to reduce start-up costs, including, but not limited to, increasing the concentration of liquid admixed, suspended solids (MLSS), lower start-up energy costs and reduced shipping costs of the fermented sludge to achieve a design flow capacity with increased efficiency.

Yet another object of the present invention is to provide an apparatus and method that utilizes conical bottomed vessels for a type of sequential dosing reaction system during triggering conditions for faster initial startup of the apparatus.

Yet another object of the present invention is to provide an apparatus and method that utilizes conical containers 9. ≪ RTI ID = 0.0 > " < / RTI > The bottom shape for a step-by-step type of reaction system, which allows rapid growth of micro-colonies following interrupted conditions, to rapidly grow microorganisms that recover from disruption conditions.

It is yet another object of the present invention to provide a treatment plant that includes fewer wastewater treatment equipment and processes to the desired effluent quality than conventional wastewater treatment systems.

Yet another object of the present invention is to provide a device that separates solids from liquid by fining (settling cleaning) without the need to use a device for wiping, raking or brushing in fining vats.

Yet another object of the present invention is to provide a device that acts as a solids containment zone, including but not limited to fining tubs, filter structures and optional tertiary treatment systems that further capture organic matter and return organic matter to aerobic zones for continued digestion of solids.

Yet another object of the present invention is to provide a device that reduces the total nitrogen content of the waste stream by oxidizing organic nitrogen to a more stable nitrate compound, which is then reduced in the waste stream by a denitrification process.

Yet another object of the present invention is to provide a device that reduces the total phosphorus content of the waste stream by digesting with microorganisms and using it to grow new cells in the decomposition of organic matter.

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It is yet another object of the present invention to provide a treatment method that is directed to zones and not to containers.

Yet another object of the present invention is to provide a system with a structure that adapts to a specific flow rate and a specific treatment process.

Yet another object of the present invention is to utilize the toroidal vortex action of the RCAS system to reduce the amount of pathogenic organisms in the wastewater.

Yet another object of the present invention is to provide an apparatus and method that allow the chemical oxidation of an aqueous solution.

Yet another object of the present invention is to provide means for homogenizing a colony of microorganisms and a substrate that consumes the colony.

Yet another object of the present invention is to provide for the separation of large clusters of microorganisms into smaller clusters of microorganisms.

Yet another object of the present invention is to ensure that the entire cluster of microorganisms, including the center, remains aerobic.

Yet another object of the present invention is to provide a high dissolved oxygen concentration in the aerobic process.

Yet another object of the present invention is to provide an alternative to the cost and need of wastewater lagoons.

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Yet another object of the present invention is to overcome the drawbacks of known wastewater treatment systems and methods.

SUMMARY OF THE INVENTION

In order to represent the uses and capabilities of the present invention, an untreated urban wastewater flow is exemplified as the aqueous waste to be treated. However, embodiments of the apparatus and methods of the present invention can be implemented to treat a variety of wastes.

The term aeration as used in this application refers to the addition of a secondary fluid (liquid or gas) flow to a primary fluid (liquid or gas) flow.

The present invention can treat organic waste water mass by producing intense aeration through RCAS (recirculating aeration system) which provides increased oxygen transfer efficiency resulting in increased oxygen uptake rate by microorganisms and the action, comminution and homogenization of organic matter causing substantially 100% digestion organic matter. This is considerably more efficient use of processing energy compared to traditional treatment processes using traditional aeration, such as diffuse aeration. The present invention also limits or omits many traditional energy consuming devices such as primary clarification equipment, anaerobic digester equipment, aerobic digester equipment, primary treatment lagoons, incinerators and associated equipment, sludge thickening equipment, and transport equipment sludge.

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The present invention allows for more efficient and complete digestion of organic matter in wastewater. Portions of organic matter in wastewater with total BOD are treated in the first aerobic reaction zone and the second aerobic reaction zone through the use of aeration and in the anaerobic treatment zone and anoxic selection zone, where the wastewater is maintained in a state where the aqueous medium does not contain enough dissolved molecular oxygen for easy breathing of microorganisms, which can also be called oxygen deficiency condition. This state of oxygen deficiency generally denotes an environment in which there is chemically bound oxygen, for example in the form of nitrate. Aggressive digestion of organic matter is performed in the anaerobic clarification zones, the first aerobic reaction zone, the anoxic selection zone, and the second aerobic reaction zone.

According to one embodiment of the present invention, there is provided a method of treating an aqueous solution comprising a waste comprising the steps of:

supplying an effluent feed stream to an anaerobic treatment zone in which all aqueous solids are recirculated, mixed and suspended;

supplying low oxygen suspended suspended solids from the anoxic selection zone to the anaerobic treatment zone to maintain a low dissolved oxygen level in the anaerobic treatment zone;

supplying an effluent stream from the anaerobic treatment zone to the first aerobic reaction zone, wherein the effluent from the anaerobic treatment zone is agitated in the first aerobic reaction zone with the activated sludge returning from the clarifying zone, wherein the contents of the first aerobic reaction zone

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The settable solids present in the contents of the first aerobic reaction zone are fractionated, thereby decomposing and oxidizing the solids and other organic matter and accumulating inert solids;

discharging the accumulated inert solids from the first aerobic reaction zone;

supplying the aqueous solution effluent from the first aerobic reaction zone to the anoxic selection zone, wherein the aqueous solution is recirculated and stirred in the anoxic selection zone;

transferring a first portion of the aqueous solution from the anoxic selection zone corresponding to the low oxygen suspended suspended solids to an anaerobic conditioning zone and a second portion of the aqueous solution from the anoxic selection zone to a second aerobic reaction zone;

recirculating and aerating the aqueous solution contained in the second aerobic reaction zone, wherein the settable solids fractionate, thereby decomposing and oxygenating the suspended solids and other organic matter;

supplying a first portion of the aqueous solution from the second aerobic reaction zone to the first aerobic reaction zone;

supplying a second portion of the aqueous solution from the second aerobic reaction zone to a fining zone to deposit or separate solids from the aqueous solution contained therein;

supplying deposited or separated solids from the fining zone corresponding to the returned activated sludge to the first aerobic reaction zone;

supplying the aqueous solution from the clarifying zone to a filtering zone for settling or separating solids from the aqueous solution introduced into the zone; and transferring the liquid portion of the filter zone outlet to

The discharge tank and the outflow portions of the filtration zone, consisting of solids or separated solids, into the inlet effluent stream for reprocessing.

According to another embodiment of the present invention, there is provided a method of biological treatment of an aqueous solution containing waste to reduce organic material, nitrogen and phosphorus, comprising the steps of:

supplying an inlet wastewater stream containing microorganisms to an anaerobic treatment zone in which all aqueous solids are recirculated, mixed and kept in suspension, carrying out a first phase of excess phosphorus absorption by controlling the flow of low-suspended suspended solids oxygen from the anoxic selection zone to the anaerobic treatment zone to maintain a low level of dissolved oxygen in the anaerobic treatment zone;

supplying an effluent stream from the anaerobic treatment zone to the first aerobic reaction zone, wherein the effluent from the anaerobic treatment zone is agitated in the first aerobic reaction zone with the activated sludge returning from the fining zone, the contents of the first aerobic reaction zone being recirculated and aerated the nitrification and settable solids present in the contents of the first aerobic reaction zone are fractionated, thereby decomposing and oxidizing suspended solids and other organic matter together with improving the second phase of excess phosphorus absorption and accumulating inert solids;

discharging the accumulated inert solids from the first aerobic reaction zone;

supplying the aqueous solution effluent from the first aerobic

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0 0 • 000 reaction zone to the anoxic selection zone, the aqueous solution being recirculated and stirred in the anoxic selection zone, and inducing a low oxygen environment in the anoxic selection zone, so that the phosphorus is denitrified and released together with the organic matter in aqueous solution;

transferring a first portion of the aqueous solution from the anoxic selection zone corresponding to the low oxygen suspended suspended solids to an anaerobic conditioning zone and a second portion of the aqueous solution from the anoxic selection zone to a second aerobic reaction zone, at least the second portion of the aqueous solution from the anoxic the selection zone is rich in microorganisms and nutrients;

recirculating and aerating the aqueous solution contained in the second aerobic reaction zone while nitrifying and settling solids are fractionated and comminuted, thereby decomposing and oxygenating suspended solids and other organic matter, and in addition, the second phase of excess phosphorus absorption has improved resulting in the consumption of large quantities of phosphorus by microorganisms;

supplying a first portion of the aqueous solution from the second aerobic reaction zone to the first aerobic reaction zone;

supplying a second portion of the aqueous solution from the second aerobic reaction zone to a fining zone to settle or separate solids from the aqueous solution contained therein;

supplying deposited or separated solids from the fining zone to the first aerobic reaction zone as a reclaimed activated sludge;

supplying the aqueous solution from the clarification zone to the filtration zone to deposit or separate solids from the aqueous solution ·

999 to this zone; and transferring the liquid portion of the filter zone outlet to the discharge tank and the portion of the filter zone outlet, consisting of solids or separated solids, to the inlet effluent stream for reprocessing.

According to a further embodiment of the present invention there is provided an apparatus for treating an aqueous solution comprising a waste comprising:

anaerobic conditioner zone fluidly connected to the ⁰ input, wherein the anaerobic treatment zone receives the incoming flow of waste water through the inlet, the anaerobic treatment zone is recirculated effluent contained therein, so that all the aqueous solids are held in suspension, the anaerobic treatment zone receives the flow of liquid admixed low oxygen suspended solids from the anoxic selection zone to maintain a low dissolved oxygen level in the anaerobic conditioning zone;

first aerobic reaction zone fluidly coupled to the anaerobic treatment zone, wherein the first aerobic ⁰ reaction zone receives effluent from the anaerobic treatment zone, which is mixed with the returned activated sludge received from the refining zone, whereby the contents of the first aerobic reaction zone is recirculated and aerated and whereby the settable solids are fractionated to decompose and oxidize the suspended solids and the other organic matter, the first aerobic reaction zone accumulating inert solids, the accumulated inert solids being discharged from the first aerobic reaction zone;

an anoxic selection zone in fluid communication with the anaerobic ^O treatment zone and the first aerobic reaction zone, wherein

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99, the anoxic selection zone receives an aqueous solution effluent from the first aerobic reaction zone, wherein the aqueous solution in the anoxic selection zone is recirculated and stirred, and wherein the first portion of the aqueous solution from the anoxic selection zone corresponding to the low-oxygen suspended suspended solids, it is fed to an anaerobic conditioning zone;

a second aerobic reaction zone fluidly coupled to the anoxic selection zone and a first aerobic reaction zone, the second aerobic reaction zone receiving a second portion of the aqueous solution from the anoxic selection zone, wherein the aqueous solution in the second aerobic reaction zone is recirculated and aerated, settling settable a solid, and wherein a first portion of the aqueous solution from the second aerobic reaction zone is fed to the first aerobic reaction zone;

a clarifying zone fluidly coupled to the second aerobic reaction zone and to the first aerobic reaction zone, the clarifying zone receiving a second portion of the aqueous solution from the second aerobic reaction zone, wherein settling or separating and entrapping solids from the aqueous solution in the clarifying zone; the settled solids corresponding to the returned activated sludge are fed to the first aerobic reaction zone; and a filter zone fluidly connected to the fining zone, the inlet and the outlet, the filter zone receiving the effluent from the fining zone to separate the solids from the liquid portion of the fining zone content, the first portion of the filtering zone corresponding to the effluent being supplied to the outlet and a second portion of the content of the filter zone, which corresponds to the separated solids, is fed to the inlet and is mixed with the inlet effluent stream for reprocessing.

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These and other objects, features and advantages of the present invention will be somewhat better apparent upon reading the following detailed description of the preferred embodiments with reference to the accompanying drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

Fig. 1 is a graph illustrating the relative concentrations of bio-matter, soluble organic nutrients and total oxygen consumption over time of various waste water treatment processes;

Giant. 2 shows a graph illustrating the rate of conversion of substances to F / M ratio (nutrients to microorganisms) in processes for editing waste water; Giant. 3 shows a table illustrating comparative

data for various wastewater treatment systems;

Fig. 4 shows schematically the layout of an eight-vessel device according to a preferred embodiment of the present invention, illustrating the flexible flow, nitrification, denitrification and phosphorus reduction;

Giant. 5 illustrates schematically the layout of an eight-vessel device according to an alternative embodiment of the present invention;

Fig. 6 shows schematically the layout of a seven-container apparatus according to an alternative embodiment of the present invention, illustrating the braking flow, nitrification and denitrification;

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Giant. 8 of the present specific diagrammatically depicts a layout of a six-vessel device according to an alternative embodiment of the invention, illustrating the flow characteristics of the braked flow and nitrification;

shows schematically the layout of an eight-vessel apparatus according to an alternative embodiment of the invention, illustrating the flow characteristics of the step filling, nitrification, denitrification and phosphorus reduction;

the present specific schematically depicts a layout of a seven-container apparatus according to an alternative embodiment of the invention, illustrating the flow characteristics of filling, nitrification and the present specific step denitrification;

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Fig. 10 shows schematically a layout of a seven-container apparatus according to an alternative embodiment of the invention, illustrating the flow characteristics of the step filling and nitrification;

Fig. 11 shows schematically a waste water treatment system made up of a plurality of treatment zones each comprising a plurality of containers;

Fig. 12 shows schematically the structure of a container according to the present invention, including a block diagram of a zone;

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Figure 13 illustrates the composition of solids in an untreated feed liquid for conventional urban wastewater;

Figure 14 shows a nitrogen cycle for wastewater;

Fig. 15 is a schematic illustration of a recirculating aeration system (RCAS) with an optional bypass aeration device;

Figure 16 is a graph illustrating 30 minute solids deposition relative to MCRT (mean cell residence time);

Figure 17 illustrates how the decay factor k _d is calculated relative to MCRT and the F / M ratio; and

Fig. 18 shows the illustrated processing associated with the captured processing.

Simplified representation of the process in Fig. 5 with filter zone fining containers for returning solids for reuse

DETAILED DESCRIPTION OF THE INVENTION

Treatment of chemical and biological aqueous waste can be accomplished by utilizing and implementing the method and apparatus of the present invention. The present invention purifies aqueous wastes in aqueous solution through a variety of strictly aerobic treatment methods and combinations of treatment methods such as aerobic biodegradation, biological oxidation, chemical oxidation, and physical separation of solids. The present invention is effective in its use of aerobic conditioning methods by reducing chemical dependency reduction. * · *

Nutrient removal agents. These processes take place at various stages of stabilization during the treatment process.

The approximate performance levels (inlet fluid relative to outlet fluid) during the treatment process of the present invention are as follows:

Reduction of 90% to 99.5% of total BOD (Biochemical Oxygen Consumption) concentrations of feed liquid through oxygenation and subsequent gravitational deposition.

Reduction of organic nitrogen through oxygenation to first ammonia, second nitrite and third nitrate.

Reduction of 95% to 99% nitrogen concentrations in the ammonia feed by nitrification.

By denitrifying the reduction of 50% to 99.5% nitrogen concentrations in the nitrites and nitrates resulting from the nitrification process mentioned above.

Reduction of 90% to 99.5% of the total phosphorus concentration of the feed liquid through excess phosphorus absorption (P).

Destruction of up to 99.5% concentrations of all organic suspended solids through intensive oxidation.

The following description explains the processes of the present invention that achieve these performance levels as aqueous solutions progress from one treatment zone to another treatment zone for treatment. The design of the present invention favors a total time of < 4 >

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• 4 • 4 4 hydraulic retention for oxygenation of nutrients in processing zones ranging from about 4 to 8 hours.

Process performance

Treatment of chemical and organic matter that proceeds as aqueous waste is stabilized by either oxygenation or biological means. Stabilization is actually a group of processes. For example, in urban wastewater treatment, stabilizing ammonia, which is converted to nitrogen gas, is a multi-step process. Ammonia (NH ₃ ) is biologically oxygenated to nitrite (NO ₂ ) and is then organically stabilized to nitrate (NO ₃ ). The following and the last phase is known is denitrification. Once this phase is reached, the presence of oxygen is reduced to very low levels and the oxygen in the NO ₃ backbone is used for breathing while nitrogen gas (N ₂ ) is released into the atmosphere.

Another form of treatment is the oxygenation of chemical compounds, which is carried out by aeration. The reaction from oxygenation causes the chemical element or compound to lose electrons. This loss of electrons makes the element or compound more stable.

Biological treatment is one of the most important steps in urban wastewater treatment and a brief explanation of this treatment is useful for understanding the present invention and its apparatus and methods. During biological treatment, micro-organisms consume, convert or consume nutrients (BODs) in wastewater. These nutrients may be of biodegradable organic or chemical nature. With traditional systems, physical treatment of untreated wastewater by sedimentation and disposal removes only around 35% of the POINT in · * AAAA • ♦ A

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ΑΑΑ * · AA ¹ AA * AAA · as a result of the high percentage (around 65% of the BOD) of the BOD contained in the non-settable and dissolved solids contained in the waste. The present invention utilizes a treatment of aerobic digestion by a method of adjusting the suspended growth to treat all BODs in aqueous solution to levels of 95% or greater.

There are two types of solids in liquid waste: 1) organic and 2) inorganic. Inorganic solids are not disturbed or degraded by biological treatment. Thus, as inorganic and inert solids begin to accumulate in the processing system, removal or disposal of these inert solids should take place. This disposal is set at a predetermined ratio of the concentrations of inert solids to organic solids. Because the percentage of inorganic or inert solids contents in most types of urban wastewater is small compared to the total solids load entering the system, the time frame for disposal of inert solids may range substantially between 90 days and 360 days or more. The organic solids content of the typical urban waste stream is approximately 70% to 85% of the solids in the waste water. About 80% to 85% of these solids are usually dissolved solids and are not settable, but 15% to 20% of these solids are settable. However, these settable solids are comminuted during the recirculation process of each of the aerobic processing zones used according to the present invention, allowing their easier consumption by microorganisms.

This comminution improves the aerobic digestion treatment method of the present invention by means of this to this to this to this to to the to be treated to the toe. Allowing colonies of microorganisms and settable solids to be homogenized. This homogenization of settable solids causes all the nutrient substrate to become almost dissolved solids, making it easier to consume microorganism colonies.

As the cluster of microorganism colonies passes through the RCAS system of the present invention, portions of the large cluster are divided into portions of smaller clusters. Reducing the size of the clusters assists in the consumption of substrates by colonies of ⁰ microorganisms by increasing the surface area of the clusters and achieving much closer contact with the necessary nutrients and oxygen.

The digestion of the substrate with colonies of microorganisms proceeds at an increased rate when the colonies of microorganisms remain aerobic throughout their contents. The RCAS system increases the digestion of the substrate by keeping the microorganism colonies in divided small clusters to maintain the aerobic state in the center of these clusters. As the clusters become smaller, the dissolved oxygen concentration within the aerobic zone is readily accessible to the center of the clusters. This also allows a high concentration of dissolved oxygen to be maintained within the aerobic zone.

The aerobic digestion treatment and treatment system of the present invention are provided by living systems that rely on a mixed biological culture to disrupt organic waste. aerobic digestion treatment system of the present invention to grow and maintain in suspension a large population of non-photosynthetic microorganisms, ₀ i.e. biomass which consumes the organic waste. Under aerobic digestion conditions, the reduced organic species are reduced. and oxygenated compounds to end products carbon dioxide and water.

The growth and survival of non-photosynthetic microorganisms depend on the ability of microorganisms to obtain energy through the metabolism of organic matter. The traditional aerobic treatment process results in complete metabolism and synthesis of organic matter, which creates biological growth in large quantities, which must be removed from the process holding system so that it does not become biologically overloaded, while compromising the quality of the outlet liquid. The present invention utilizes a complete aerobic digestion of bio-matter in which the microorganism environment is maintained to the far right of the endogenous respiratory phase of Fig. 2 by controlling and balancing the F / M ratio (nutrient to microorganism; ranging from 0.05 to 0.80) and oxygen supply. This results not only in a complete metabolism and synthesis of organic matter, but also in a substantial reduction of biological solids at the end of the process.

Another feature of the present invention is the use of a nitrification cycle to convert large amounts of organic nitrogen to ammonia, ammonia to nitrite and nitrite to nitrate. The nitrate is then denitrified with the release of nitrogen into the atmosphere, resulting in a reduction of the total nitrogen content in the waste stream.

Yet another feature of the present invention is the consumption of phosphorus entering the system through microorganisms as a source of nutrients for cell wall formation and new cell growth during periods of high oxygen concentrations, such as those occurring in aerobic reaction zones.

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Figure 1 shows the characteristic growth curve of microorganisms, where the relative concentration of bio-matter (on the vertical axis) is plotted as a function of time (on the horizontal axis) After a short period of adaptation to a new environment, microorganisms consume organic matter and reproduce binary This is the log growth phase shown in the leftmost part of the graph of Figure 1. The rate of metabolism in the log growth phase is limited both by the ability of microorganisms to process organic matter and by the amount of dissolved oxygen available to the microorganisms. for breathing (respiration).

The decreasing growth phase shown in FIG. 1 is due to an increase in the lack of organic matter required for the growth of microorganisms. In this decreasing growth phase, the reproduction rate of the microorganisms decreases. The growth of microorganisms in the decreasing growth phase is a function of both the concentration of microorganisms and the concentration of growth-limiting organic matter.

The decreasing growth phase is followed by a steady-state phase. In the steady-state phase of the bio-matter concentration, it reaches its maximum value and the low concentration of the remaining organic matter substantially limits the growth rate of bio-matter, which becomes relatively constant.

The endogenous respiratory phase follows the steady state phase. In the endogenous respiratory phase, viable microorganisms compete for a small amount of organic matter still in the wastewater undergoing treatment. Optionally, ₃ q also results in starvation of microorganisms so that the extinction rate exceeds the reproduction rate. Biomaterial concentration »9 99tt« «

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ΦΦ ΦΦ in aqueous solution therefore decreases during the endogenous respiratory phase. In the present invention, endogenous respiration (ER) is controlled such that the extinction rate of the microorganisms is the same as the growth rate of the microorganisms as verified by the liquid suspended solids concentration (MLSS), which is maintained at a constant concentration relative to the processing criteria.

The wastewater treatment of the present invention will now be described in some detail. In the present invention, the wastewater treatment process takes place in three stages, namely:

(1) Aerobic digestion of biological matter for the consumption of organic impact, including, but not limited to, the reduction of all organic nitrogen and all phosphorus;

(2) entrapment of solids in the speaking and settling zone; and (3) Pretreating entrapped solids from the solids zones by returning the solids back to the aerobic reaction process.

In the treatment method of the present invention, organic waste is consumed by maintaining an environment consisting of high mean cell residence time (MCRT), low nutrient to microorganism (F / M) ratio and intense aeration, whereby the microorganisms are forced to survive in the endogenous respiratory phase.

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The fining and settling phases (separation of solids from liquid (liquid)) by means of gravitational settling. Once the aqueous solution containing the suspended solids enters the fining zone (containers 76, 80, 84 and 88 corresponding to the fining equipment # 1, # 2, # 3 and # 4 of Figure 4) from the aerobic reaction zone # 2 (container 2). 4, whose specific features are explained in detail below, the velocity of the supernatant is slowed to allow solids to settle by gravity. As the settled solids slightly concentrate at the bottom of the refining containers, they are often and quickly removed and transported back to the aerobic reaction zone # 1 (vessel 18) for further treatment.

The supernatant (cleaner aqueous solution) continues the process by a process where it can be further treated with optional tertiary treatments such as tertiary clarification or filtration to nearly completely remove biological and inert matter prior to discharge. The receiving stream, the evaporation tanks, the irrigation of the landscape, the irrigation of agricultural crops or some other kind of disposal can be used for the discharged liquid.

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Aerobic digestion systems, such as the system of the present invention, must grow and suspend a population of microorganisms to consume organic waste. Although, as illustrated in Fig. 1, individual microorganisms grow rapidly, it will take some time to start, or when there are large load changes, to raise the original low concentration of microorganisms to levels high enough to rapidly degrade organic waste. It is therefore becoming important to use MLSS concentration-enhancing procedures at a rapid rate.

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4 • 4 «4 •« 4 44 way. The equipment start-up time for traditional systems ranges from 30 to 45 days for MLSS concentrations reaching acceptable working levels. Using the present invention, the startup time of the device can be reduced to up to 14 days or less. The time required to restart the device after an interruption of operation due to toxic shock loads for microorganisms is reduced compared to the time requirements of traditional devices. These procedures are discussed below.

The common design concept for aerobic digestion systems is the mean cell residence time (MCRT), which is the average time that micro-organisms spend in the system. The MCRT of a traditional treatment system refers to the amount of microbial solids in the activated sludge process due to the amount of solids lost in the effluent and the excess solids removed from the sludge. processing cycle in waste sludge. With the present invention, MCRT refers to the amount of microbial solids in the aerobic treatment process relative to only the amount of solids lost in the effluent, which is unintentional disposal, since there are essentially no volatile solids collected as waste activated sludge. Typical MCRTs for traditional systems are from 15 to 30 days. However, the MCRT values for the present invention start at 30 days and range in size from 150 to 250 days or greater (see Figure 3). MCRT values greater than 30 days may cause traditional aerobic conditioning systems; operational problems. Excessive solids formation in the system, caused by inadequate solids disposal, is a common reason for poor effluent quality due to the retention of higher suspended solids, turbidity, and so on. · · · 9 9 9 9 9 9 9 · 9 9 9 9

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9 9 9

99 reasons for poor discharge quality include extremely old, slow-settling solids, excessive oxidation of solids, and liquefaction of solids. Consequently, it is desirable for traditional aerobic treatment systems to deliberately dispose of excess solids from time to time to maintain MCRT in the ranges shown in Fig. 3. According to the present invention, the removal of excess solids is not necessary due to the possibility of almost total digestion of all organic solids. .

The amounts of solids are expressed as the concentration of MLSS (liquid admixed suspended solids) with the values for the conventional traditional system shown in Figure 3. These typical MLSS values for traditional systems range from 1000 mg / l at the lower end of the range for contact stabilization systems up to 6000 mg / l for complete mixing and extended aeration systems. The amounts of microbial solids (MLSS) in the anaerobic conditioning zone, anoxic selection zone and aerobic reaction zones of the present invention (see, for example, Fig. 4 explained in detail below) range from 2000 to 8000 mg / L or more. The apparatus and method of the present invention can maintain the MLSS concentrations shown in Fig. 3 for almost complete digestion of organic matter of typical urban-type waste and the elevated MLSS concentrations shown in Fig. 3 for almost complete digestion of non-typical industrial-type organic matter through using a device with a system for achieving effective aeration, such as the device used according to the present invention (recirculating aeration system or RCAS). The aeration device used in the present invention is the device described in U.S. Patent 5,893,641 (Garcia), the entire contents of which are hereby incorporated by reference.

The process carried out according to the present invention also achieves the results of complete digestion of organic solids by utilizing the above-mentioned system for (RCAS) for delivery for oxygen transfer, achieving efficient aeration of atmospheric air required by circulation, homogenization and thorough mixing. An additional advantage of the process that utilizes the aeration system of the above type is the mixing and secondary oxygenation of MLSSs located within the aerobic reaction zones. This mixing and secondary oxygenation is accomplished by withdrawing MLSS content from the aerobic reaction zones at their lowest point and discharging the re-oxygenated MLSS back into each respective vessel at a height substantially two-thirds of the distance below the surface of the water level. The secondary oxygenation of MLSS is accomplished by allowing excess trapped air injected through the RCAS and carried along with the aerated MLSS to flow through the conduit into and through the contents of the aerobic reaction zones. The primary and secondary oxygenation of MLSS in the aerobic reaction zones allows the dissolved oxygen (DO) concentration to reach levels in the range of substantially between 3.0 and 5.0 mg / L. The dissolved oxygen concentration in the aerobic reaction zones is maintained at an operating level that exceeds the upper range for traditional aerobic digestion systems, which is 2.0 mg / L. Also for this reason, among other things, the present invention achieves a high

·· · ·

the degree of digestion of organic solids through its efficient oxygenation treatment process.

With higher than usual dissolved oxygen concentrations and with vigorous mixing as achieved with the present invention, a higher decomposition coefficient (k _d ) of organic matter can be achieved than is achieved with traditional aeration systems. The term degradation is the term used to express the destruction (digestion) of volatile (organic) suspended solids in the definition of F / m for MCRT. Traditional aeration systems have a k _d value of between 0.04 and 0.06, with a diameter of 0.05, while in the present invention kd is substantially 0.10 or twice the value for traditional aeration systems, providing greater digestion rates. This is evident from Figure 17, illustrating the definitions and formulas used to determine the degradation coefficient.

Traditional oxygen transfer efficiency is expressed as a percentage of the weight of oxygen that a biological cell achieves compared to the applied weight of gaseous oxygen fed to the reaction apparatus. The rate of oxygen transfer from the air bubbles allowed by RCAS is a function of several factors that vary according to the characteristics of the wastewater, including but not limited to the oxygen transfer factors of the wastewater within the line and the oxygen transfer factors inside the vessel, the oxygen saturation factors for the waste water and the actual dissolved oxygen concentration and oxygen saturation concentration in the aqueous solution.

In a traditional system for aerobic biological treatment, the metabolism of organic matter in wastewater results in an increased amount of biological matter (growth) of microorganisms in ·

30 · system. Excess microorganisms are removed or discarded from the system to maintain the proper balance between the nutrient supply and the mass of microorganisms that exists in the aeration bath where oxygen is supplied. This equilibrium is referred to as the nutrient to microorganism (F / M) ratio.

The person skilled in the art knows that an F / M ratio of from 0.05 to 0.20, which is maintained in traditional aeration baths, defines the operation of extended aeration systems (with extended aeration). Giant. 2 illustrates how an increasing F / M ratio affects the rate of metabolism.

Although the exponential growth phase shown in FIG. 2 is desirable for maximum rate of organic matter removal, at this stage the microorganisms are in diffuse growth and exhibit difficulty in settling the solution by gravity. In addition, there is an excess of unused organic matter in solution that cannot be removed by microorganism colonies in the diffuse growth of a traditional aeration system and therefore passes through the system and out in the effluent. Thus, the operation of traditional aeration systems with a large F / M ratio results in ineffective and inadequate BOD removal.

At a low F / M ratio, the total metabolic activity in the aeration bath is endogenous. At this stage, the metabolism of organic matter is almost complete and microorganisms

5 rapidly agglomerate, flocculate and settle out of solution by gravity. Endogenous phase operation is desirable where high BOD removal efficiency is desired.

Typical F / M ratios of traditional aeration systems range from 0.05 to 0.2 for low velocities required for extended aeration, from 0.2 to 0.2

9 to a greater extent from 0.4 to

According to the present invention ·

31 ··

0,4 for normal treatment speeds; and

1.5 for high treatment rates, but the F / M ratio is maintained in the range of 0.05 to 0.8 for include all of said low speeds, all of said normal speeds, and a portion of said high treatment speeds, allowing a considerable the degree of flexibility in one given design of the conditioning device. This flexibility is particularly evident in that as the flow through the treatment system increases and the organic matter concentration remains the same, the recirculation rate can be increased by simply modulating the aeration device to increase the speed of the recirculation pumps, further increasing the rate of the provided aeration. Thus, with a sufficient amount of available oxygen as achieved using the aeration system as described herein or in US Patent No. 5,893,641, the above F / M ratio ranges for the present invention allow microorganisms not only to completely convert the organic matter , but through intense aeration, the nutrient source decreases as micro-organisms consume it, thus increasing nutrient contention. The micro-organisms consume (consume) each other to survive the endogenous respiratory treatment process, even at a higher F / M ratio of 0.8. The long-term cannibal state of endogenous respiration provides a significant reduction in solids accumulation that occurs with the aerobic digestion process of the present invention. By keeping the F / M ratios at the values of the present invention together with maintaining large amounts of dissolved oxygen as economically possible using the above-mentioned.

32 * · staying within the zones of reason has been made aeration device and system, the oxygenation of organic matter is quickly completed.

As the MCRT of the microorganisms increases, the support for rapid settling of the microorganisms increases, which benefits the clarification process as illustrated in Figures 2 and 16.

In order to better understand the term disposal as used in the present invention, the following explanation is provided below. As the concentration of inert solids increases, such solids should be removed or disposed of to allow sufficient biological microorganisms to be treated. From this measure to remove inorganic or inert solids from the aerobic reactor # 1 as illustrated in Fig. 4, Fig. 5, Fig. 6, Fig. 7, Fig. 8, Fig. 9, Fig. 10 and Fig. 5. 18. When the concentration of inert solids reaches the removal level, a predetermined amount of solids is removed. The concentration of inert solids prior to this disposal steadily increased from extremely low concentrations (approximately 0.001% of settable solids as indicated in Figure 13) in the inlet stream to levels that can reach substantially 50% of the total solids found in the solids. biological treatment zones. When the organic solids are mixed with inert solids, the total weight of the disposed organic solids from the biological treatment zones is substantially between 0.01% and 0.5% compared to the total weight of organic solids entering the biological zone. treatment. This disposal of inert and organic solids should continue periodically until concentration • · · ·

33. · inert substances in the biological treatment zone will not drop to acceptable levels for further processing.

The fining can be defined as separating the bio-matter from the aqueous solution to be treated. Traditional systems for aerobic treatment and separation of solids attempt to retain a set of microorganisms in the system by precipitation and flocculation, but due to the nature of the traditional process and equipment, it is being destroyed along with constraints on operating energy costs. The biological solids are then deposited at the bottom of the clarifier. Most biological solids are then returned to the aeration bath while deliberately removing (removing) from the system a portion of the biological solids (activated sludge) that is the amount of activated sludge that exceeds the design capabilities of the digestion system. The present invention retains the microorganisms in the system by depositing biological solids together with all inorganic solids in the fining zone (refining apparatus # 1, # 2, # 3 and # 4 of Fig. 4) and returning them to the aerobic reaction zone # 1 (vessel 18 according to FIG. 4) for further processing. Care is taken to control the coating depth (accumulated sludge at the bottom of the refining vessel) to a minimum by frequent and extensive collection of the amount of activated sludge returned (RAS) returned to the aerobic reaction zone # 1. This RAS sampling frequency eliminates long residence times of biological solids in the fining zone, which would otherwise become septic, gaseous and float on the fining zone surface. Observation and adjustment of the RAS flow withdrawal should be performed to minimize the hydraulic velocities in the clarifying zone. Higher hydraulic speeds can cause ineffective settling in

34 ' ' ' clarification zone, which results in biological solids being carried away in the effluent.

With the present invention, the hydraulic retention times in aeration cycles are in the process ranges for complete mixing and retarded flow, and partly in the process range with high purity oxygen, while taking advantage of the enhanced aeration process. The extended aeration process usually takes 18 to 36 hours to nearly complete oxygenation (treatment) of the organic matter as shown in Figure 3 (see the rightmost column in this figure). The present invention achieves the same results on organic matter over a period of substantially in the range of 4 to 8 hours. By utilizing a system for effectively providing aeration, the present invention drastically reduces the time required to oxidize the organic matter. This is accomplished by aeration systems that are located in each of the aerobic reaction zones (containers 18 and 20 in Figure 4), the anaerobic conditioning zone (container 8 in Figure 4), and the anoxic selection zone (container 58 in Figure 4). ), wherein each of the respective contents of these zones is recirculated by volume substantially at 100% every two hours. When combining the recirculation rates in percent of the anaerobic conditioning zone together with both the aerobic reaction zone and the anoxic selection zone, the total recirculation processing percentage rate is equal to or greater than 200% of the inlet flow entering the treatment process over a 24 hour period. The aeration system recirculates, comminutes and homogenises organic matter and microorganisms, and oxygenates the entire matter many times more than traditional systems, resulting in a higher rate of digestion of biological solids in a shorter period of time than is possible with

of traditional systems. Typical recirculation rates in conventional conditioning systems range from 25 to 100 percent per day from the inlet flow for full mixing systems, from 25 to 50 percent per day from the inlet flow for the restrained flow system, and from 75 to 150 percent per day from the inlet flow for extended aeration systems.

Recirculation percentages as described for traditional activated sludge treatment systems indicate only the percentage of returned activated sludge recirculation (RAS) compared to the input flow. Although the present invention utilizes this same type of recirculating percent RAS, the present invention also utilizes the above recirculating processing percentages described above, achieving a greater solid digestion rate than is possible with traditional activated sludge treatment systems.

The biological treatment technique of the present invention will now be described in more detail. The cell composition of the microorganisms consists of 70 to 90 percent water, with 10 to 30 percent dry material in weight percent. Of this dry material, 70 to 95 percent are organic and 5 to 30 percent are inorganic. Ninety-five percent of the organic dry material consists of carbon, oxygen, nitrogen, hydrogen and phosphorus, respectively, and other trace materials. The present invention takes advantage of the large percentage of organic substances available to microorganisms by maintaining an extremely long MCRT not only for total oxygenation of organic compounds but also for the consumption of bio-matter (a mass of organic material consisting of living organisms consuming waste in waste water, which? 6.

AAA AAA • A «

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A A A · also contains these same elements. In the activated sludge process, carbon, oxygen, nitrogen and hydrogen are used as the main ones

- constituents of cellular material, wherein phosphorus is used as a constituent of nucleic acids, phospholipids and nucleotides. The compounds are taken up by microorganisms from their environment to perform two basic primary metabolic activities: energy generation through bioenergetics and synthesis of new cellular material through biosynthesis. Microorganisms generate energy for themselves from light, organic and inorganic compounds. The main inorganic compounds used by microorganisms as an energy source are ammonia (NH ₄ ), nitrite (NO ₂ ), dissolved sulfide (H ₂ S) and elemental sulfur. These compounds are oxidized and the energy released is used to maintain cells, synthesize new cellular material, and move microorganisms if they are mobile. There are two types of microorganisms: autotrophic microorganisms that use inorganic carbon for biosynthesis, and heterotrophic microorganisms that use organic carbon for biosynthesis.

Carbon represents up to about 50 percent of the dry mass of microorganism cells. Thus, carbon is a major element used during biosynthesis. Microorganisms use either organic compounds such as fatty acids, amino acids, sugars, organic acids or carbon dioxide (CO ₂ ) as one of their energy sources for the development of new cells. Through biological processes, organic carbon is converted into biosynthesis material of microorganisms and into gases such as carbon dioxide, which can escape into the atmosphere. Through 200% content recirculation ·· ··· ·

In the aerobic reactor with RCAS of the present invention, the microorganisms can come into contact with their carbon source more and more efficiently than traditional systems.

Oxygen and hydrogen are the main gaseous elements used in cellular material. The oxygen source for the cellular material of microorganisms is found in molecular oxygen, organic compounds or even carbon dioxide. The present invention supplies oxygen via an aerobic reaction aeration (RCAS) system directly to an aqueous solution of nutrients and microorganisms. This offers microorganisms the ability to breathe in the easiest way and with the most affordable oxygen source for bioenergy and biosynthesis. The hydrogen source for the cellular material of microorganisms is found in molecular hydrogen and organic compounds. Oxygen as an electron acceptor is used in the classification (sorting) of microorganisms. Oxygen microorganisms are referred to as aerobic, while non-oxygen microorganisms are referred to as anaerobic. The present invention utilizes aerobic microorganisms to stabilize organic compounds and decompose in an aerobic reactor.

Nitrogen is the major source for proteins and nucleic acids for microorganisms and accounts for 14 percent of cellular material. Microorganisms can use inorganic nitrogen in the form of nitrogen gas (N ₂ ), nitrogenous ammonia (NH ₃ + NH ₄ ), nitrite (NO ₂ ) and nitrate (NO ₃ ). The nitrogen gas to be used must first be converted to ammonia (NH ₄ ) and then converted to organic nitrogen, but the nitrogen ammonia (NH ₃ ) can be considered 100% prepared and available for nutritional use by microorganisms. Ammonia Conversion

9 4 9 9 4 445

4 4 944

3.S

4 4

44 for nitrite (NO ₂ - nitrogen dioxide) and nitrate (NO ₃ - nitrogen dioxide) opens the door for microorganisms that use NO ₂ and NO ₃ as their only source of nitrogen. However, a large amount of energy is needed for microorganisms to be able to use this nitrogen as a source of growth. These micro-organisms must oxidize larger quantities of organic compounds to have the energy needed to use NO ₂ and NO ₃ as their nitrogen source. This results in a lower growth rate of microorganisms than using NH ₃ as a nitrogen source. The present invention utilizes this lower growth rate as its advantage of maintaining an extremely long MCRT and a variable F / M ratio to reduce the growth rate of microorganisms. In combination, microorganisms must consume more organic compounds and cannot reproduce so quickly. There are three biological removal processes used for nitrogen removal, which are ammonification followed by nitrification and denitrification. Ammonification and nitrification take place in aerobic reactors, while denitrification takes place in an anoxic selector. Amonification is carried out by heterotrophic microorganisms which take up organic nitrogen in the form of proteins and peptides and decompose these substances into ammonia (ammonia) and ammonium. Autotrophic microorganisms that convert ammonia to NO ₂ and then to NO ₃ carry out nitrification. The third stage in the process is denitrification, in which another group of heterotrophic microorganisms reduces NO ₃ to NO ₂ and then to NO (nitric oxide) and finally to N ₂ for release into the atmosphere.

Microorganisms use phosphorus synthesis, cell maintenance and as energy carriers up to 30 percent of phosphorus input during cellular

Therefore around 10 is consumed • 4 4 44 «• 44« 4 4 4 4 »«

44 4 4 4 444 4 4 ·

4,4444 44 4 «4 4 4

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Hl '4 4 4 4 44 44 4 ♦ 4 · microorganisms and their metabolic processes are used. However, there are three microorganisms with the ability to store phosphorus in larger amounts than required for growth requirements. This is referred to as excess phosphorus absorption. These three, 5 organisms, acinetobacter, pseudomonas and moraxella, are collectively referred to as poly-P bacteria due to their ability to store phosphorus in the form of polyphosphate granules. Poly-P bacteria are able to use polyphosphate as a source of energy when exposed to harsh conditions. Since these bacteria are capable of storing these larger amounts of phosphorus only when in aerobic conditions, the present invention maintains dissolved oxygen in sufficient amounts to provide excess phosphorus absorption in the aerobic reaction zones. The present invention utilizes an anaerobic conditioning zone as an area in which microorganisms achieve the necessary stress conditions to allow these poly-P bacteria to utilize polyphosphate as energy, which reduces the amount of phosphorus in the discharge stream.

In summary, carbon, nitrogen and phosphorus are therefore reduced through bioenergy and biosynthesis through microorganisms. The amount of removal of these nutrients is directly related to the concentration of nutrients and the amount of time these nutrients are exposed to microorganisms. Multiple increases in the number of times nutrients come into contact with 25 microorganisms and oxygen through homogenization, as in the present invention, can speed up the organic digestion process. By creating zones for essentially achieving a hydraulic retention time of 2 hours and by recirculating and re-aerating the entire contents, based on volume, of the aerobic reaction zones 100% every 2 hours.

4, Q · this * hours, before the contents flow out of these zones, an environment for microorganisms is created which accelerates the biological digestion process. All biological solids taken from the solids collection zone and returned to the processing zones are also subject to this accelerated biological digestion. The present invention, as outlined above, provides this effect, and hence from now on it is possible to utilize a structure with a smaller footprint (smaller built-up area) as compared to traditional treatment systems while allowing greater available hydraulic containment capacity.

By utilizing the extended MCRT, the flexible F / M ratio and the increased recirculation as described above, bio-mass consumption can also occur, thereby achieving improved reduction of organic solids in the process through digestion. Only after a predetermined concentration of inorganic solids has been reached is the deliberate destruction of substantially only these inorganic solids, with possible high ²⁰ phosphorus concentrations, being initiated.

Another component of the improved solids reduction (ESR) wastewater treatment system of the present invention is the zones (containers) as part of the overall system. The zones consist of a container or group of containers, which contain ²⁵ to the wastewater treatment. These containers preferably have a certain shape formed by a vertical cylinder having a conical bottom.

However, the wastewater treatment of the present invention is not limited to any preferred container shape. Effective treatment by the method of the present invention is also achievable in 30 square or rectangular containers with flat or

444 4 · * 44 »4 4« ♦ 4 4 4 444 44 4 • 4 4 4 4 4 444 4 4

4,444 44 44,444 4 4

111 · 4444 4444

4 44 44 44 of the invention, per zone.

depicting representing oblique days. Zones are unique to the process designed for this zone. Container design and processing zone design are part of the ESR wastewater treatment system, allowing modularization of the system. The zones illustrated in FIG. 4, a preferred embodiment of the apparatus according to the single-vessel design

Alternative embodiments of the device could assemble a zone having one or more containers performing a unique processing function in that zone. Alternatively, as an example of the large capacity of the ESR wastewater treatment system, the number of containers shown in Figure 11 could be designated as one zone and the add-on modules with the corresponding number of containers in Figure 11 could be added for each desired additional treatment zone until the design criteria for high-volume conditioners will not be met. Alternative designs could include containers of different dimensions that use the same treatment techniques as described herein.

The container design comprises a vertical cylinder with a bottom in the form of a depression, but preferably in the form of a cone (see Fig. 12), to create an environment for improving the desired wastewater flow path during treatment. The use of a conical bottom vessel is essential for settling and concentrating solids in the clarifying zone and is used effectively in processing zones for settling and concentrating phosphorus-rich inorganic solids for periodic withdrawal. The solids are suspended in the RCAS system which receives flow into the pump from the bottom of the aerobic reaction zone. The contents of the aerobic reaction zone are then pumped, aerated, and recirculated to form an aerobic reaction zone.

9 0 9 9 9 0 9 9 9

9 9 9 9 999 9 9 9

9 999 99 99 999 9 by generating velocities during discharge by passing the RCAS back to the aerobic reactor so that the contents of the aerobic reaction zone are well mixed.

Using cylindrical shapes during clarification and propelling the flow through the inflow direction and its located reference point and the direction of the recirculation discharge and its located reference point, the wastewater is directed to proceed in a certain direction, preferably rotationally, at a certain speed and distance over allow the deposited solids to reach the bottom of the container and remain in the container for a period of time so that it is accumulated, concentrated and processed to facilitate the desired treatment. The conical bottom together with the flow characteristics of the advancing effluent improves solids accumulation for accumulation at the central point of reference at the lowest point within the conically shaped bottom (referred to as a solid concentrator). These accumulated deposited solids are then available to be withdrawn through the outlet opening at this lowest point.

The embodiment of Fig. 4 is used to illustrate preferred flow characteristics when the inlet flow comprises conventional BOD, TSS (total suspended solids) and NH ₃ loading, and requires conventional nitrification, denitrification and phosphorus reduction as demonstrated by the inlet flow concentrations for the equipment. for the treatment (treatment) of urban waste water. In Fig. 4, the pre-directed inlet waste water containing suspended solids and biodegradable organic substances passes through the inlet flow line leading to an inlet manifold, which further has withdrawal feeders to each of the containers. This allows you to perform • φ φ φ φ ♦ φ φ φ φ φ · φ φ · · · · · »»

Figure 43 to represent the universal arrangement that can be used as representative of all possible flow characteristics required for varying treatment specifications. The Figure 43 is used to represent the universal arrangement that can be used as representative of all possible flow characteristics required for varying treatment specifications.

Flow and processing procedures

Figure 4 illustrates a preferred embodiment of the enhanced solids reduction (ESR) wastewater treatment system of the present invention that provides full operational flexibility in nitrification, denitrification and phosphorus reduction processing characteristics in conjunction with flow-inhibited flow characteristics preferred process). Due to the efficiency of the preferred embodiment of the present invention and in particular the RCAS system, an economical solution is achieved with improved treatment in wastewater treatment over traditional wastewater treatment processes. The preferred embodiment corresponds to a four-zone biological process and a solids capture processing zone. Biological treatment zones include, but are not limited to, 1) anaerobic zone, 2) aerobic zone, 3) anoxic zone, and 4) additional aerobic zone. The solids collection zone includes, but is not limited to, secondary clarification, tertiary clarification, filtration and chemical blending. However, by altering the flow characteristics through changes in the valves, any of the alternative processing embodiments (as described below) can be realized and used. A preferred embodiment of the treatment according to the present invention is a treatment method which is directed to zones and not to containers.

φφ ··· ·

• φ φ φ φ φ φ φ φ • • • • • • φ φ φ φ φ φ φ φ *

For advantageous braking flow characteristics, the inlet liquid, for which conventional municipal waste water is assumed in this embodiment, is passed through line 2 to a flow manifold 4 that regulates and / or divides the inlet liquid flow into the treatment vessels. In this embodiment, the entire flow of the inlet flow is then routed through line 6 to a vessel 8 (V # 1), which is used as an anaerobic conditioning zone, the volume by volume being recirculated substantially once every two hours using a pump 10. and the aforementioned system

RCAS. The size of the vessel 8 depends on the volume of the inlet flow being processed.

Vessel 8 (anaerobic treatment zone) begins the first phase of excess phosphorus absorption, which is the release of s _in biological phosphorus (Bio-P). This first phase of excess phosphorus absorption is accomplished by maintaining an oxygen deprivation state within the vessel. The dissolved oxygen levels in the anaerobic conditioning zone are maintained at 0.10 mg / L or less, allowing the formation of volatile fatty acids (VFAs) used by the microorganisms in the release of Bio-P. Although this release of Bio-P creates a temporary increase in phosphorus concentration, it also forces microorganisms to metabolize more phosphorus during the later stages of the process. The contents of this zone can be maintained at low dissolved oxygen levels by controlled introduction of low oxygen suspended solids (MLSS) with low oxygen from vessel 58 (anoxic selection zone - V # 3) from line 11 via pump 12 and through line 14. into container 8 (anaerobic conditioning zone).

·· φ * * * * * φ φ ⁹ · · · · · · · · · ·

ΦΦ Φφφφ

The total aqueous solids (TS) from vessel 8 (V # 1) flows through line 16 to vessel 18 (V # 2), which is a dynamic aerobic reaction zone # 1. The vessel 18 also receives another flow, recycled MLSS, coming from vessel 20 (V # 4), which is a dynamic aerobic reaction zone # 2. Flow from vessel 20 comes from line 22 through pump 24 and finally through line 26. Another flow enters vessel 18 from each of the four fining devices (vessel 76, 80, 84, 88 in zone # 5, V # 6, # 7 and # 8) in the form of returned activated sludge (RAS) through the pumps 28, 30, ^{32 and 34} P ^ro RAS and then through conduit 36, 38, 40 and 42 and finally enter vessel 18 through lines 44, 46, 48 and 50. The volume-based content of vessel 18 is recirculated substantially once every two hours using a recirculating guide aeration system (RCAS) as explained below, which is driven by a pump 52. During the recirculation procedure, the contents of the settable solid container 18 become dissolved by pulverization as they pass through the RCAS with the pump 52. The comminution occurs as the solids within the aqueous solution are processed through the RCAS system by the toroidal vortex action of the RCAS system to become a more easily consumable population of microorganisms. The RCAS system also applies intense aeration during the recirculation procedure so that the dissolved oxygen level is essentially maintained at a concentration of 3.5 mg / L or higher. Maintaining dissolved oxygen concentrations at these levels allows nitrosomonas and nitrobactor residing in a colony of microorganisms to oxidize (ammonia) ammonia (NH ₃ ) to nitrite (NO ₂ - nitrogen dioxide) or eventually to · 9 4 · 4 · 4 4

4 «

4 4 4 4 4 09 09 ·

4 4 0 0 9 4. 9 4 9 4

nitrate (NO ₃ - nitrous oxide). With dissolved oxygen concentrations in this zone maintained at 3.5 mg / L or greater, suspended solids and other organic matter are decomposed and oxidized to more stable compounds.

By utilizing large volumes of atmospheric air supplied by RCAS and keeping dissolved oxygen at higher levels (above 3.5 mg / l) than would be maintained by traditional aeration systems (2.0 mg / l to 3.0 mg / l) ), and along with long MCRTs, colonies of microorganisms will enter a biological life cycle regime known as endogenous respiration (ER). In this ER mode, living microorganisms begin to metabolize some parts of their own cellular matter together with any new organic matter they absorb or adsorb from their environment. This assists in improving solids reduction while maintaining a colony of microorganisms by adjusting the nutrient to microorganism ratio (F / M) to allow the colony's extinction rate to be the same as the growth rate of the microorganism colony through the endogenous respiration process.

Another advantage of providing intensive aeration within the reactor (reaction zone) is the improved consumption of large amounts of phosphorus by the microorganisms. The amount of phosphorus absorbed by the microorganisms is greater than the amount of phosphorus released by the microorganisms in vessel 8, as described above. Microorganisms then use this newly acquired phosphorus to develop new cell walls and other energy needs.

Accumulated inert solids are collected via line 5 from vessel 18 (aerobic reactor # 1) when their tata is present. · · · · · · · · · · · · · ·

these concentrations reach a predetermined level. This remains valid for all embodiments of the present invention. This predetermined level could be substantially 50% of the total solids concentration in the vessel 18 or the level at which the process begins to allow nutrients to pass into the process effluent.

The flow exits the vessel 18 through the conduit 54, is fed to the manifold 56 and then is fed to the vessel 58 through the conduit 60 for further processing.

The content by volume of vessel 58 (anoxic selection zone V # 3) is recirculated substantially once every two hours via pump 62. The vessel 58 receives elemental oxygen attached to nitrogen molecules in the form of nitrogen dioxide (NO.) And nitrogen dioxide (NO.) , which was derived primarily from the ammonia conversion process known as nitrification, which takes place inside vessel 18 (aerobic reaction zone # 1). The amount of dissolved oxygen (DO) in vessel 58 is maintained in the range of 0.3 mg / L to 0.5 mg / L. The microorganisms contained within the waste water in the vessel 58 look for oxygen for respiration. With a small amount of dissolved oxygen available, microorganisms are forced to use elemental oxygen in NO ₃ , which is bound with nitrogen. This process is generally called denitrification. Once the bond between nitrogen and oxygen is broken, the microorganisms consume elemental oxygen for breathing, allowing nitrogen to be released into the atmosphere. Microorganisms use this oxygen for the necessary breathing so that they can continue to consume the organic matter that remains in the wastewater.

3Q During these non-toxic conditions, natural release of phosphorus by microorganisms occurs as a pathway for

* Energy conservation during periods of low availability of dissolved oxygen, but in smaller amounts than that occurring in vessel S1 (anaerobic conditioning zone V # 1). Although this creates a temporary increase in phosphorus concentration, microorganisms are also forced to metabolize larger amounts of phosphorus in later processes. The effluent from this process is conducted via line 64 to vessel 20 (aerobic reaction zone # 2 - V # 4) for further processing.

The vessel 20 is used as a dynamic aerobic reactor. The content by volume of the vessel 20 is recirculated and intensively aerated substantially once every two hours using a recirculation aeration system (RCAS) which is driven by the pump 66. Oxygenation of both dissolved and suspended organic matter takes place in the vessel 20 by maintaining a dissolved oxygen level of at least 3.0 mg / l. Nitrosomonas and nitrobactor living in a colony of microorganisms will oxidize (organic) nitrogen to ammonia (NH ₃ ), then to nitrite (NO ₂ - nitrogen dioxide) and eventually to nitrate (NO ₃ nitrogen dioxide). As the aqueous solution containing the colony of microorganisms is aerated in vessel 20 (dynamic aerobic reaction zone # 2) and the dissolved oxygen level increases, the microorganisms begin to consume phosphorus in larger amounts than necessary to sustain life. The amount of phosphorus consumed far exceeds the amount of phosphorus released by the microorganisms into the aqueous solution during its treatment in the anaerobic conditioning zone and the anoxic selection zone (containers 8 and 58). This phenomenon is what is called excess phosphorus absorption. Parts mixed in liquid • 9 · * * ·

• • • • • • •

999 ·· ·· «Φ

9 9 · 999

9

9 9 «

99

9 9

9 9

9 9 9

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999 suspended solids (MLSS) from vessel 20 are recycled for further digestion into vessel 18 (dynamic aerobic reaction zone # 1) through line 22 using a pump 24 and finally discharged through line 26, while the effluent is discharged from vessel 20 through conduit 68 and conduit 70 prior to entering the flow manifold housing 72 (SB Clar Inf) of the clarification zones.

As the inlet flow from line 70 enters the flow clarifier 72 (SB Clar Inf) of the clarification zones, the flow is preferably divided into four equal parts, each part being

led to one in four rippled rippling equipment equipment through knowledge knowledge 74 78 for for time 76 corresponding # 1, for for time 80 corresponding rippling equipment # 2, knowledge 82 for for time 84 corresponding finisher # 3, , and knowledge 86 for for time ! 38 corresponding rippling equipment # 4. Speed

The flow is reduced as the flow enters each of the fining devices, allowing the solids to settle at the bottom of each of the fining devices. The deposited solids are then pushed away from the walls of the fining devices by using a hydraulically operated solid concentrator 90 for container 76 (fining apparatus # 1), a hydraulically operated solid concentrator 92 for container 80 (fining apparatus # 2), a hydraulically operated solid concentrator 94 for container 84 (fining plant # 3) and hydraulically operated solid concentrator 96 for container 88 (fining plant # 4), allowing for further thickening of the solids prior to removal through each of the RAS pumps (returned activated sludge) from the fining zones (pumps) : 28, 30, 32 and 34) and lines for RAS (lines 36, 38, and 42) and sent to vessel 18 (dynamic aerobic reactor)

00 00 »00

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00 # 1) for further processing or modification. Separated liquid from the clarification process exits vessel 76 through line 98, vessel 80 through line 100, vessel 84 through line 102, and vessel 88 through line 104, and these flows are combined in a collection box 106 (CB Clar Eff). Such a clarifying device then drains the effluent through line 108 as the final treated (treated) effluent.

The preferred embodiment of the present invention allows for improved operational flexibility over traditional wastewater treatment systems.

according to FIG

A first alternative embodiment of the present invention is shown in Fig. 5, from which unused lines and equipment of a preferred embodiment of the apparatus 4 are removed. However, all lines used and required for wastewater flow processing with a preferred embodiment of the treatment method are shown. The alternative embodiment shown in Fig. 5 is used when a specific flow arrangement for the device is envisaged and therefore the flexibility of operation offered by the embodiment of Fig. 4 is not required. The inlet flow, which is typically urban waste water, is routed through line 2 to the vessel. 8, which is used as an anaerobic conditioning zone (V # 1), wherein the volume-related content of this zone is recirculated substantially once every two hours using a pump 10. As in the previous preferred embodiment, the contents of the vessel can be maintained at low dissolved oxygen levels by controlled supply of low oxygen MLSS from vessel 58 (anoxic selection zone) via line 10 through pump 12 and line 14 to vessel 85.

·············································· • · · ·········································

Total aqueous solids from vessel 8 (anaerobic conditioning zone) flow through line 16 to vessel 18, which is a dynamic aerobic reaction zone # 1 (V # 2). Vessel 18 also receives another flow, recycled MLSS, coming from vessel 20, which is used as a dynamic aerobic reaction zone # 2. The flow from vessel 20 comes from line 22 via pump 24 and finally through line 26. Another flow enters vessel 18 from each of the four fining devices (vessels 76, 80, 84, 88 as described below) in the form of returned activated sludge ( RAS) via RAS pumps 28, 30, 32 and 34, then through lines 36, 38, 40 and 42, respectively, and finally enters container 18 through lines 44, 46, 48 and 50, respectively. The content, based on the volume, of the container 18 is recirculated substantially once every two hours using a recirculation aeration system (RCAS) as explained below, which is driven by the pump 52. During this recirculation procedure, the contents of the container 18, i.e. the settable solid, become dissolved by comminution as it passes through the RCAS of this zone. Grinding occurs as the solids within the aqueous solution are processed through the RCAS system by the toroidal vortex action of the RCAS system so that they become easier to consume for the population of microorganisms.

Through RCAS, intensive aeration is also applied during recirculation procedures so that the dissolved oxygen level is essentially maintained at a concentration

3.5 mg per liter or more.

The flux exits vessel 18 (aerobic reaction zone # 1) via line 110 to vessel 58 (anoxic selection zone - V # 3). The contents of the container 58 are recirculated substantially once every 4 hours by means of a pump 62. The operation of the container 58 is similar to that described for the container with reference to Figure 4. The outlet flow from the container 58 is routed through a conduit 64 to the container 20 for further treatment.

Vessel 20 is a dynamic aerobic reactor (V # 4). The contents of the container 20 are recirculated and intensively aerated substantially once every two hours using a recirculation aeration system (RCAS) that is driven by the pump 66. The operation of the container 20 is also similar to the operation for the corresponding container described with reference to Figure 4. As explained above, MLSS particles from vessel 20 are recycled for further processing into vessel 18 through line 22 using a pump 24 and finally discharged through line 26, while the effluent from vessel 20 is discharged through line 68 and into line 70 before entering flow manifold boxes 72 (SB Clar Inf) of the clarification zones.

As the inlet flow from line 70 enters the flow clarifier 72 (SB Clar Inf) of the clarification zones, the flow is preferably divided into four equal parts and each part is directed to one of the four clarifying devices (V # 5, V # 6, V # 7, V # 8) through the container line 74 corresponding to the fining plant # 1, the container line 78 corresponding to the fining plant # 2, the container line 82 corresponding to the fining plant # 3, and the container line 86 corresponding to the finishing plant # 3 # 4. The flow rate is reduced as the flow enters each of the fining devices, allowing solids to settle at the bottom or bottom of each of the fining devices. These deposited solids are then pushed away from the vessel walls by the use of a hydraulically operated solid concentrator 90 for container 76, a hydraulically operated solid concentrator 92 for container 80, a hydraulically operated solid concentrator 94 for container 84, and hydraulically controlled solids concentrator 96 for vessel 88, allowing further solids thickening prior to removal through each of the RAS pumps (returned activated sludge) from the clarification zones (pumps 28, 30, 32, and 34) and the RAS line (lines 36, 38). , 40 and 42) and sent via lines 44, 46, 48 and 50 to the container 18 for further processing. Separated liquid from the clarification process exits vessel 76 through line 98, vessel 80 through line 100, vessel 84 through line 102, and vessel 88 through line 104, and these flows are combined in a collection box 106 (CB Clar Eff). Such a clarifying device then drains the effluent through line 108 as the final treated (treated) effluent.

Giant. 18 is a simplified representation of the method shown in FIG. 5, but additionally comprising a filter zone 89 coupled to the outlet of the clarifying devices (line 108). The filter zone receives the aqueous solution (effluent in FIG. 4) through line 108 for further processing. The aqueous solution is fed to a filtration zone where solids are separated and settled from the liquid portion of the aqueous solution. The solids that have been deposited and separated from the liquid portion are passed through line 109 to line 2 for an inlet flow for recurrence nc s x. ✓ processing and reprocessing in the system. The filter zone shown in Fig. 18 may also be incorporated in the system shown in Fig. 4 or in any of the other embodiments of the systems of the present invention explained below.

9 9 9 9 9 9 9 9 99 99 999 9 9 9 9 9 9 9 9

A second alternative embodiment of the invention, shown in Fig. 6, utilizes process # 1 according to the present processing characteristics of an embodiment to provide the present alternative invention for nitrification and denitrification in conjunction with flow-inhibiting flow characteristics. An alternative embodiment of device # 2 is to be used with an alternative embodiment of process # 1. An alternative embodiment of process (processing) # 1 of the present invention is a treatment method that is directed to zones and not containers.

For an alternative embodiment of Process # 1, the inlet liquid, represented as a typical urban wastewater, is passed through line 120 to a vessel 122, which is used as an anoxic selection zone (V # 1), the content by volume of this vessel being recirculated in the vessel. substantially once every two hours using pump 124. Additional flows entering vessel 122 come from vessel 126 (aerobic through line 128 and from vessel 130 reaction zone # 1).

V # 2) (aerobic reaction zone # 2 - V # 3) through line 132 in the form of recycled MLSS, which are used to provide oxygen depletion within vessel 122. Additional flow that enters vessel 122 comes from each one of the four fins. equipment (containers 134, 136, 138 and 140) in the form of reclaimed activated sludge (RAS) through lines 150, 152, 154 and 156, respectively. Container 122 receives elemental oxygen attached to nitrogen molecules in the form of nitrogen dioxide (NO ₃ ) and nitrogen dioxide ( NO ₂ ), which were derived mainly from the ammonia conversion process, takes place in vessels 126 and known as nitrification 130 (aerobic reaction zone # 1 and aerobic reaction zone # 2). Amount of dissolved oxygen in mg / l to 0,5 mg / l. This MLSS from vessel 126 is maintained within the range of 0.3 is allowed through recycling (aerobic reaction zone # 1). using pump 158 and pumping through line 128 and from vessel 130 (aerobic reaction zone # 2) using pump 160 and pumping through line 132 into vessel 122.

The microorganisms contained in the waste water in the vessel 122 (anoxic selection zone) look for oxygen for respiration. With a small amount of available dissolved oxygen, the microorganisms are forced to utilize elemental oxygen in NO ₃ , which is bound with nitrogen gas. This process is generally called denitrification. Once the bond between nitrogen and oxygen is broken, the microorganisms consume elemental oxygen for respiration, allowing nitrogen to be released into the atmosphere.

During oxygen uptake through respiration in the denitrification process in vessel 122 (anoxic selection zone), microorganisms also consume portions of organic matter in the form of fully suspended solids that have been ground and dissolved in the recirculation process in vessels 126 and 130 (aerobic reaction zones # 1 and # (2) to make them more easily consumed by the population of micro-organisms.

Total aqueous solids (TS) from vessel 122 (anoxic selection zone) flows via gravity through line 162 to vessel 126 (aerobic reaction zone # 1) for continued treatment and processing. The content by volume of the vessel 126 is recirculated substantially once every two hours using a recirculation aeration system (RCAS) that is driven by the pump 164. During the recirculation procedure, the contents of the vessel 126, namely the settable solid, become dissolved

through comminution by RCAS in the vessel. The comminution takes place as the solids in the aqueous solution are processed by the RCAS system by the toroidal vortex action of the RCAS system so as to become a more easily consumable population of microorganisms. The RCAS system also applies intense aeration during the recirculation procedure so that the dissolved oxygen level is essentially maintained at a concentration of 3.5 mg / L or higher. Maintaining dissolved oxygen concentrations at these levels allows the nitrosomonas and nitrobactor residing in a colony of microorganisms to oxidize (ammonia) ammonia (NH ₃ ) to nitrite (NO ₂ - nitrogen dioxide) and eventually to nitrate (NO ₃ - nitrous oxide). This process is generally known to those skilled in the art as nitrification. With dissolved oxygen concentrations in this zone maintained at 3.5 mg / L or greater, suspended solids and other organic matter are decomposed and oxidized to more stable compounds.

By utilizing large volumes of atmospheric (Ί air supplied by RCAS) and keeping dissolved oxygen at higher levels (above 3.5 mg / l) than would be maintained by traditional aeration systems (2.0 mg / l to 3.0 mg (1), and at the same time as long MCRTs, colonies of microorganisms will enter a biological life regime

A cycle known as endogenous respiration (ER). In this ER mode, living microorganisms begin to oxidize some parts of their own cellular matter together with any new organic matter they absorb or adsorb from their environment. This helps in improving the ³⁰ solids reduction while maintaining • • · · · · · · · · · • • ···· · · · · · ·· 4 colonies of microorganisms by adjusting the ratio of nutrients to the microorganism (F / M) allowing the colony extinction rate of the microorganisms to be the same as the growth rate of the colony of microorganisms through the ER process (endogenous respiration).

Another advantage of providing intensive aeration within the reactor (reaction zone) is the consumption of certain amounts of phosphorus by the microorganisms.

The flow exiting vessel 126 (aerobic reaction zone # 1) ¹⁰ extends through conduit 166 into vessel 130. Vessel 130 is used as aerobic reaction zone # 2 (V # 3), the content by volume of the vessel being recirculated and intensively aerated essentially once every two hours using a recirculation aeration system (RCAS) 15 driven by a pump 168. Oxygenation of both dissolved and suspended organic matter takes place in the vessel by keeping the dissolved oxygen (DO) level at least 3.0 mg / 1. Nitrosomonas and nitrobactor living in a colony of microorganisms will oxidize (organic) nitrogen to ammonia (NH ₃ ), then to nitrite (NO ₂ - nitrogen dioxide) and eventually to nitrate (NO ₃ - nitrogen dioxide).

A portion of nitrite rich rich suspended solids (MLSS) is recycled using pump 160 through line 132 to vessel 122 (anoxic selection zone 25) to reduce nitrogen via the denitrification process.

The flow also exits under gravity through line 170 to line 172 before entering the flow

30 of the clarification manifold housing 174 (SB Clar Inf) for settling solids from the liquid portion of the wastewater.

It should be noted that this alternative embodiment does not include the container (V # 4) present in the preferred embodiment described above. This vessel is not used until the flow is substantially increased and the need for an additional aerobic reactor arises.

As the inlet flow from line 172 enters the flow clarifier 174 (SB Clar Inf) of the clarification zones, the flow is preferably divided into four equal parts and each part is directed to one of the four clarifying devices (containers 134, 136, 138 and 140) ) through vessel 176 for vessel 134 (corresponding to fining plant # 1), vessel 178 for vessel 136 (corresponding to finishing plant # 2), vessel 180 for vessel 138 (corresponding to finishing plant # 3), and channel 182 for vessel 140 (corresponding to finishing plant) device # 4). The flow rate ⁵ is reduced as the flow enters each of the fining devices, allowing the solids to settle at the bottom or bottom of each of the fining devices. The deposited solids are then pushed away from the conical walls of the clarifying devices by using a hydraulically operated ^O solids concentrator 184 for the container 134, a hydraulically operated solid concentrator 186 for the container 136, a hydraulically operated solid concentrator 188 for the container 138 and a hydraulically operated solid concentrator 190 the container 140, allowing further concentration of the solids ⁵ materials prior to their removal through each of the pumps RAS (returned activated sludge) from the fining zone (pumps 142, 144, 146 and 148) and guidance for (RAS lines 150, 152, 154 and 156 ) and sent to vessel 122 (anoxic reaction zone) for further processing. The separated liquid from the fining process ⁰ exits from the container 134 (fining apparatus # 1) through the line 192, • 9 · 9

CQ .- · · · ♦ 9 · · «

997 from container 13 6 (fining device # 2) through line 194, from container 138 (fining device # 3) through line 196, and from container 140 (finisher # 4) through line 198 and these flows are combined in a collection box 200 (CB Clar Eff). Such a clarifying device then discharges the effluent through line 202 as the final treated (treated) effluent.

FIG. 7 illustrates another alternative embodiment of an apparatus of the present invention that uses an alternative embodiment of Process # 2 to provide nitrification processing characteristics in conjunction with a flow-inhibited flow characteristic. This alternative embodiment of the device is to be used with an alternative embodiment of process # 2. An alternative embodiment of process # 2 of the present invention is a treatment method that is directed to zones and not containers.

According to the embodiment of the present invention shown in Fig. 7, the feed liquid, represented as a typical urban wastewater, is passed through line 210 to a vessel 212, which is used as the aerobic reaction zone # 1. Additional flows entering vessel 212 come from four fining devices (vessels 214, 216, 218 and 220) in the form of returned activated sludge (RAS) via RAS pumps 222, 224, 226 and 228 and are routed to vessel 212 through lines 230, 232, 234 and 236, respectively.

The content by volume of vessel 212 (aerobic reaction zone # 1) is recirculated essentially once every two hours using a recirculation aeration system (RCAS) which is driven by pump 238. During the recirculation procedure, the contents of vessel 212, namely the settable solids , becomes dissolved by pulverization by the RCAS system. · · · · · · · · · · ·

9 9 9 • 9999 · 9 9 · ··· "··· _e • ♦ · · · · · · • · 9 9 · ·· in the container. The comminution takes place as the solids in the aqueous solution are processed by the RCAS system by the toroidal vortex action of the RCAS system so as to become a more easily consumable population of microorganisms. The RCAS system also applies intense aeration during the recirculation procedure so that the dissolved oxygen level is essentially maintained at a concentration of 3.5 mg / L or higher. Maintaining dissolved oxygen concentrations at these levels allows the nitrosomonas and nitrobactor residing in a colony of microorganisms to oxidize (ammonia) ammonia (NH ₃ ) to nitrite (NO ₂ - nitrogen dioxide) and eventually to nitrate (NO ₃ - nitrous oxide). This process is generally known to those skilled in the art as nitrification. With dissolved oxygen concentrations in this zone maintained at 3.5 mg / L or greater, suspended solids and other organic matter are decomposed and oxidized to more stable compounds.

By utilizing large volumes of atmospheric air supplied by RCAS and keeping dissolved oxygen at higher levels (above 3.5 mg / l) than would be maintained by traditional aeration systems (2.0 mg / l to 3.0 mg / l) ), and along with long MCRTs, colonies of microorganisms will enter a biological life cycle regime known as endogenous respiration (ER). In this ER mode, living microorganisms begin to oxidize some parts of their own cellular matter together with any new organic matter they absorb or adsorb from their environment. This helps in improving the reduction of solids while maintaining colonies of microorganisms by adjusting the ratio of nutrients • · * 4 4 4 4 4 ► 4 4 * 4 4 4 ► · 4 · 4444 ¹ 444 444 4 4 « '» 4 4 4 4 « To allow microorganism colony extinction rates to be the same as microorganism colony growth rates through the ER process (endogenous respiration).

Another advantage of providing intensive aeration within the reactor (reaction zone) is the consumption of certain amounts of phosphorus by the microorganisms.

The flow leaving vessel 212 (aerobic reaction zone # 1) exits through line 239 into vessel 240 (aerobic reaction zone # 2 - V # 2) for further treatment. The volume-based content of this vessel 240 is recirculated substantially once every two hours using a recirculation aeration system (RCAS) that is driven by the pump 242. During the recirculation of the contents of vessel 240, additional intensive aeration is applied and the dissolved oxygen level is maintained. substantially to a concentration of 3.0 mg / L or greater. Maintaining dissolved oxygen concentrations at these levels allows microorganisms to be able to convert organic matter, including but not limited to total BOD, as well as organic nitrogen first to ammonia, then to nitrite, and finally to nitrate. This process reduces total nitrogen concentrations to less harmful compounds.

The flow also exits the vessel 240, preferably by gravity, through line 243 to line 244 before entering the flow clarifier housing 246 (SB Clar Inf) of the clarification zones for settling solids from the liquid portion of the wastewater.

It should be noted that the additional aerobic reaction vessels described in the previous embodiments are not in fcfc · fcfcfcfcfc This embodiment is used until the flow is substantially increased and the need for additional aerobic reactors arises.

As the inlet flow from conduit 244 enters the flow clarifier housing 246 (SB Clar Inf) of the clarification zones, the flow is preferably divided into four equal parts and each part is routed to one of the four clarifying devices (containers 214, 216, 218 and 220). through vessel 248 for vessel 214 (corresponding to fining apparatus # 1), vessel 250 for vessel 216 (corresponding to finishing apparatus # 2), vessel 252 for vessel 218 (corresponding to finishing apparatus # 3), and channel 252 to vessel 220 (corresponding to finishing apparatus) # 4). The flow rate is reduced as the flow enters each of the fining devices, allowing the solids to settle at the bottom or bottom of each of the fining devices. The deposited solids are then pushed away from the walls of the clarifying devices by using a hydraulically operated solids concentrator 256 for the container 214, a hydraulically operated solids concentrator 258 for the container 216, a hydraulically operated solids concentrator 260 for the container 218 and a hydraulically operated solids concentrator 262 for the container. 220, allowing further solidification of the solids prior to collection through each of the RAS pumps (returned activated sludge) from the fining zones (pumps 222, 224, 226 and 228) and the RAS line (lines 23 0, 232, 234 and 236); sending to vessel 212 (aerobic reaction zone # 1) for further processing. Separated liquid from the clarification process exits vessel 214 through conduit 264, vessel 216 through conduit 266, vessel 218 through conduit 268, and vessel 220 through conduit 270, and these flows combine in a collector box 272 (CB Clar Eff). Such a clarifying device then discharges the outflow

The liquid through line 274 is the final processed liquid.

Figure 8 illustrates another alternative embodiment of the present invention that utilizes an alternative embodiment of Process # 3 of the present invention to provide processing characteristics of nitrification, denitrification and phosphorus reduction in conjunction with step feed type flow characteristics, providing improved operational flexibility (flexibility) ). The use of this alternative embodiment in conjunction with an alternative embodiment of process # 3 would be advantageous where changes in feed preferences can be expected or parameter changes are needed and the quality of the effluent needs to be improved. This would also apply to changes in nutrient loading in the feed liquid while maintaining the same flow characteristics of the feed liquid. An alternative embodiment of Process # 3 of the present invention is a treatment method that is directed to zones and not containers.

For an alternative embodiment of Process # 3, the feed liquid is a highly contaminated waste that could contain high concentrations of NH ₃ , with high TSS concentrations and high total BOD concentrations, while requiring nitrification, denitrification and phosphorus reduction as might be necessary for the input a liquid which is a stream of industrial, heavily polluted waste.

In an alternative embodiment shown in Fig. 8, the feed liquid containing suspended solids and biodegradable organic substances is passed through line 280 to a manifold box 282 (SB PLT Inf) where it is distributed, with 60% of the total inlet flow flowing into the container 284 ·· ···· # 1) through line 286, 30% of through line 288 to container 290 (anaerobic conditioning zone - In total inlet flow flows (aerobic reaction zone # 1 - V # 2), and 5% is passed through line 292 to vessel 294 (anoxic selection zone - V # 3), while the remaining 5% is routed through line 296 to vessel 298 (aerobic reaction zone # 2 - V # 4).

Vessel 284 receives 60% of the inlet flow of the device and flow from vessel 294 through line 300 using pump 302 and line 304. The volume-related content of vessel 284 is recirculated essentially once every two hours using pump 306.

Vessel 284 (anaerobic treatment zone) begins the first phase of excess phosphorus absorption, which is the release of biological phosphorus (Bio-P). Excess phosphorus absorption is accomplished by maintaining oxygen deficiency states within vessel 284. Dissolved oxygen levels are maintained at 0.10 mg / L or less, causing the release of Bio-P by microorganisms. Although this release of Bio-P creates a temporary increase in phosphorus concentration, it also forces microorganisms to metabolize more phosphorus during the later stages of the process. The contents of this zone can be maintained at low dissolved oxygen levels by controlled introduction of low oxygen suspended liquid suspended solids (MLSS) from vessel 294 (anoxic selection zone) from line 300 via pump 30 and through line 304 to vessel 284 The flow then continues further through line 308 to vessel 290 (aerobic reaction zone # 1) for treatment.

As mentioned above, vessel 290 receives 30% of the inlet flow of the device through line 288 and is used as * 0 * 0 99 9 • 9 9 9 9 9 9

0 «« 0 · 0 98 ι

0 0 0 0 «« ♦ 0 ··

0 * 00 aerobic reaction zone # 1. Further flow entering this vessel comes from vessel 298 through line 310 using pump 312 and then through line 314 leading into vessel 290. Flow from vessel 298 (aerobic reaction zone # 2) is in the form of recycled MLSS. Yet another flow entering the vessel

290, comes from each of the four fining devices, consisting of 316, 318, 320 and 322 containers, in the form of returned activated sludge (RAS) via pumps 324, 326, 328 and 330 to

RAS and finally through lines 332, 334, 336 and 338, respectively.

The content, based on the volume, of the vessel 290 is recirculated substantially once every two hours using a recirculation aeration system (RCAS) which is driven by the pump 340. During the recirculation procedure, the contents of the vessel 284, namely the settable solid, become dissolved by comminution as passes through the RCAS in the vessel.

The comminution takes place as the solids in the aqueous solution are processed by the RCAS system by the toroidal vortex action of the RCAS system so as to become a more easily consumable population of microorganisms. Intensive aeration is also applied during the recirculation procedure so that the dissolved oxygen level is essentially maintained at a concentration of 3.5 mg / L or higher. Maintaining dissolved oxygen concentrations at these levels allows the nitrosomonas and nitrobactor residing in a colony of microorganisms to oxidize (ammonia) ammonia (NH ₃ ) to nitrite (NO ₂ - nitrogen dioxide) and eventually to nitrate (NO ₃ - nitrous oxide). With dissolved oxygen concentrations in this zone maintained at 3.5 mg / L or greater, suspended solids and other organic matter are decomposed and oxygenated to more stable compounds. Through

4 4 4 4 4 · «t t t t t t t t II II II II II II II ti ti ti ti ti ti ti * * · «Aa aa, utilizing large volumes of atmospheric air supplied by RCAS, and keeping dissolved oxygen at levels higher than 3.5 mg / l than would be maintained by traditional aeration systems, and along with long MCRTs, colonies microorganisms enter a biological life cycle regime known as endogenous respiration (ER). In this ER mode, living microorganisms begin to oxidize some parts of their own cellular matter together with any new organic matter they absorb or adsorb from their environment. This assists in improving solids reduction while maintaining a colony of microorganisms by adjusting the nutrient to microorganism ratio (F / M) to allow the colony's extinction rate to be the same as the growth rate of the colony of microorganisms through the ER process (endogenous respiration).

Another advantage of providing intensive aeration within the reactor (reaction zone) is the improved consumption of large amounts of phosphorus by the microorganisms. The amount of phosphorus absorbed by the microorganisms is greater than the amount of phosphorus by the microorganisms released in the vessel 284 (anaerobic conditioning zone) as described above. Microorganisms then use this newly acquired phosphorus to develop new cell walls and other energy needs.

The flow then leaves vessel 290 (aerobic reaction zone # 1) through line 342 to vessel 294 (anoxic selection zone) for further processing. In addition to flow through line 342 from vessel 290, vessel 294 also receives an additional flow of 5% of the inlet flow of device through line 292. The volume-related content of this vessel is recirculated substantially once every two hours.

·· to <

··· · <

9 * by means of pump 344. This anoxic selection point the zone receives elemental oxygen attached to nitrogen molecules in the form of nitrogen dioxide (NO ₃ ) and nitrogen dioxide (NO ₂ ), which was derived primarily from the ammonia conversion process known as nitrification, which takes place inside vessel 290 (aerobic reaction zone # 1). The amount of dissolved oxygen (DO) in vessel 294 is maintained in the range of 0.3 mg / L to 0.5 mg / L. The microorganisms contained within the wastewater in vessel 294 look for oxygen for respiration. With a small amount of available dissolved oxygen (DO), microorganisms are forced to use elemental oxygen in NO ₃ , which is bound with nitrogen. This process is generally called denitrification. Once the bond between nitrogen and oxygen is broken, the microorganisms consume elemental oxygen for breathing, allowing nitrogen to be released into the atmosphere. Microorganisms use this oxygen for the necessary breathing so that they can continue to consume the organic matter that remains in the wastewater.

During these anoxic conditions occurs

The natural release of phosphorus by microorganisms as a way to conserve energy during periods of low availability of dissolved oxygen, but in smaller amounts than occurs in vessel 284 (anaerobic conditioning zone).

Although this creates a temporary but slight increase

As a result of the concentration of phosphorus, microorganisms are also forced to metabolize more phosphorus in later processes. The effluent from this process is passed further via line 346 to vessel 298 (aerobic reaction zone # 2) for further processing.

• ······· ·· · · · · ·

In addition to the flow that enters vessel 298 (aerobic reaction zone # 2) through line 346, 5% of the plant inlet flow is fed to vessel 298 via t.

296. The volume-related content of this zone is _Λ 5 recirculated and intensively aerated essentially once every two hours using a recirculating aeration system (RCAS), which is driven by a pump

348. Oxygenation of both dissolved and suspended organic matter takes place in the vessel by maintaining the dissolved oxygen level at at least 3.0 mg / L. Nitrosomonas and a nitrobactor living in a colony of microorganisms will oxidize (organic) nitrogen to ammonia (NH ₃ ) then nitrite (NO ₂ - nitrogen dioxide) and eventually nitrate (NO ₃ - nitrogen dioxide). As the aqueous solution containing the colony of microorganisms is aerated in the vessel 298 and the dissolved oxygen level increases, the microorganisms also begin to consume phosphorus in greater amounts than necessary to sustain life. The amount of phosphorus consumed far exceeds the amount of phosphorus released by the microorganisms into the aqueous solution during treatment in containers 284 and 294 (anaerobic treatment zone and anoxic selection zone). This phenomenon is what is referred to in the art as excess phosphorus absorption. Parts of Liquid Mixed Suspended Solids (MLSS) from Container 298

5 are recycled to vessel 290 (aerobic reaction zone # 1) through line 310 using a pump 312 and finally discharged through line 314, while the effluent is discharged further through line 350 and into line 352 before entering the flow manifold 354 (SB) Clar Inf).

• · · ·

As the inlet flow from line 352 enters the flow zone manifold 354, the flow is preferably divided into four equal parts and each part is directed to one of the four clarifying devices (vessels 316, 318, 320 and 320).

322) through vessel 356 for vessel 316 (corresponding to fining device # 1), vessel 358 for vessel 318 (corresponding to fining device # 2), conduit 360 for vessel 320 (corresponding to fining device # 3), and conduit 362 for vessel 322 (corresponding finisher # 4). The flow rate is reduced as the flow enters each of the fining devices, allowing the solids to settle at the bottom or bottom of each of the fining devices. The deposited solids are then pushed away from the walls of the fining devices by using a hydraulically operated solid concentrator 364 for container 316 (fining apparatus # 1), a hydraulically operated solid concentrator 366 for (fining apparatus # 2), hydraulically operated solids for container 320 ( fining hydraulically operated concentrator 370 vessel 318 of concentrator 368 of device # 3), and solids for vessel 322 (fining device # 4), allowing further solids concentration prior to removal through each of the RAS pumps (returned activated sludge) from the clarification zones ( pumps 324, 326, 328 and 330) and lines for RAS (lines 332, 334, 336 and 338) and sent to vessel 290 (aerobic reaction zone # 1) for further processing. Separated liquid from the clarification process exits from vessel 316 (fining device # 1) through line 372, from vessel 318 (fining device # 2) through line 374, from vessel 320 (fining device # 3) through line 374, and from vessel 322 (fining device) # 4) Through line 378 and these flows are combined in collection box 380 (CB Clar Eff). The fining zone effluent is discharged through line 382 as the final treated (treated) effluent.

FIG. 9 depicts another alternative embodiment of the present invention that utilizes an alternative embodiment of Process # 4 of the present invention to provide processing characteristics of nitrification and denitrification in conjunction with step-feed type flow characteristics. An alternative embodiment of Process # 4 of the present invention is a treatment method that is directed to zones and not containers.

For an alternative embodiment of Process # 4, the feed liquid is a highly polluted waste that could contain high concentrations of NH ₃ , high concentrations of TSS and high concentrations of total BOD, while requiring nitrification and denitrification for overall nitrogen reduction as might be necessary for input liquid, which is a stream of industrial, heavily contaminated waste.

of the invention, comprising

In an alternative embodiment of the present embodiment shown in Fig. 9, the feed liquid, suspended solids and biodegradable organic substances are passed through line 390 to a manifold box 392 (SB PLT Inf) where it is distributed, with 75% of the total inlet flow flowing through. line 394 to vessel 396 (anoxic selection zone - V # 1), 15% of the total inlet flow is routed through manifold 392 through line 398 to vessel 400 (aerobic reaction zone # 1 - V # 2), and the remaining 10% of total the inlet flow is guided by the manifold box 292 · · · · · · · · · · · · · · · · · · · · · · · · · · · ·

* * * * *

through line 402 to vessel 404 (aerobic reaction zone # 2 - V # 3).

Vessel 396 (V # 1) is used as an anoxic selection zone, receiving 75% of the inlet flow through line 394. Further flow in the form of recycled MLSS is received from vessel 404 (V # 3) through line 406, pump 408 and line 410. The dissolved oxygen level in vessel 396 is maintained at a low concentration below 0.5 mg / L for denitrification. Container 396 is rich in aerobic microorganisms and also contains chemically bonded oxygen in the form of nitrate received from container 404. With levels of dissolved oxygen in the range of up to 0.5 mg / l, aerobic microorganisms are forced to use nitrate for respiration (breathing). for the purpose of waste water denitrification before proceeding for further treatment and processing.

The inlet flow received through line 390 is nutrient rich, while the flow received through line 410 from vessel 404 is rich in nitrates and microorganisms. Thus, by stepwise filling a portion of the inlet flow into the vessel, the organic load entering the device may be increased without any changes to the actual design of the preferred embodiment of the device of the present invention. The content, based on volume, of vessel 396 is recirculated once every two hours via pump 412. The flow leaves vessel 396 through line 414 into vessel 400 for further treatment.

Vessel 400 (V # 2) is used as an aerobic reaction zone # 1 that receives 15% of the total inlet flow through line 398 and flow from vessel 396 through line 414. Another flow comes from each of the four fining devices (containers 416, 418). , 420, 422) in the form of returned activated sludge (RAS).

• ·

73 * • ··· • · ·

The volume content of this vessel is recirculated essentially once every two hours using a recirculation aeration system (RCAS) which is driven by the pump 424. During the recirculation procedure, the contents of the vessel 400, namely the settable solid, become dissolved by comminution as passes RCAS in this zone. The comminution takes place as the solids in the aqueous solution are processed by the RCAS system by the toroidal vortex action of the RCAS system so as to become a more easily consumable population of microorganisms. Intensive aeration is also applied during the recirculation procedure so that the dissolved oxygen level is essentially maintained at a concentration of 3.5 mg / L or higher. Maintaining dissolved oxygen concentrations at these levels allows nitrosomonas and nitrobactor residing in a colony of microorganisms to oxidize (ammonia) ammonia (NH ₃ ) to nitrite (NO ₂ - nitrogen dioxide) and eventually to nitrate (NO ₃ - nitrous oxide). This process is generally known to those skilled in the art as nitrification.

With dissolved oxygen concentrations in this zone maintained at 3.5 mg / L or greater, suspended solids and other organic matter are decomposed and oxidized to more stable compounds. This initial decomposition of organic matter, which is the breaking of organic matter from more complex forms to simpler forms, takes place mainly through the digestive action of aerobic bacteria.

By utilizing the large volumes of atmospheric air supplied by RCAS and keeping dissolved oxygen at higher levels (above 3.5 mg / l) than would be maintained by traditional aeration systems, while at the same time 9

99 9 9 9 β • · «with long MCRTs, colonies of microorganisms will enter a biological life cycle mode known as endogenous respiration (ER). In this ER mode, living microorganisms begin to oxidize some parts of their own cellular matter together with any new organic matter they absorb or adsorb from their environment. This helps to improve solids reduction while maintaining a colony of microorganisms by adjusting the nutrient to microorganism ratio (F / M) to allow the colony's extinction rate to be the same as the growth rate. colony of microorganisms through the ER process (endogenous respiration). The flow leaving vessel 400 (aerobic reaction zone # 1) exits through line 426 to vessel 404 (aerobic reaction zone # 2 - V # 3). An additional 10% of the inlet flow enters vessel 404 (V # 3) from manifold box 392 (SB PLT Inf) through line 402.

The volume content of vessel 404 is recirculated and intensively aerated substantially once every two hours using the recirculation aeration system ²⁰ (RCAS) which is driven by pump 428. During recirculation of vessel content 404, settable solids become further dissolved by comminution by the effect of recirculation pumping in this zone so that they can be further consumed by the micro-organism population. Intensive aeration is also applied during recirculation so that the dissolved oxygen (DO) level is substantially maintained at at least 3.0 mg / L or greater. Nitrosomonas and nitrobactor living in a colony of microorganisms will oxidize (organic) nitrogen to ammonia (NH ₃ ) then nitrite •

9 · 9 9 9 · 9 9 9 9 / 5t ··· (ΝΟ ₂ - nitrogen dioxide) or finally nitrate (NO ₃ nitrogen dioxide) in this zone.

Maintaining dissolved oxygen concentrations above 3.5 mg / L allows the colony of microorganisms to be able to convert organic matter, including but not limited to total BOD, as well as organic nitrogen first to ammonia, then to nitrite and finally to nitrate and others less harmful compounds. This process reduces the concentration of total nitrogen released into the aqueous environment through the denitrification process. The dissolved oxygen in vessel 404 (aerobic reaction zone # 2) maintains a concentration of at least 3.5 mg / L to ensure complete decomposition and oxidation (oxidation) of the organic nutrients in the wastewater flow.

Portions of the contents of vessel 404 are recycled to vessel 396 (anoxic selection zone) in the form of recycled MLSS in line 406 using pump 408 and finally through line 410. MLSSs that are rich in aerobic microorganisms and also contain chemically bound oxygen are denitrified in the vessel 3 96 before returning them to containers 400, 404 for continued treatment of the remaining nutrients.

The effluent from these processes leaves the vessel 404 through line 430 and into line 432 for the fining process. As the outlet fluid from line 432 enters the flow clarifier box 434 (SB Clar Inf) of the clarification zones, the flow is preferably divided into four equal parts and each part is directed to one of the four clarifying devices (vessels 416, 418, 420 and 422). through a conduit 436 for the container 416 (corresponding to the container of the fining apparatus # 1), the conduit 438 for the container

418 (corresponding to fining device # 2), conduit 440 for container 420 (corresponding to fining device # 3), and conduit 442 for * · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · · ·

a container 422 (corresponding to the fining apparatus # 4). The flow rate is reduced as the flow enters each of the fining devices, allowing the solids to settle at the bottom or bottom of each of the fining devices. The deposited solids are then pushed away from the conical walls of the clarifying devices by using a hydraulically operated solid concentrator 444 for container 416, a hydraulically operated solid concentrator 446 for container 418, a hydraulically operated solid concentrator 448 for container 420, and a hydraulically operated solid concentrator 450 for container 416. a container 422, allowing further solidification of the solids prior to collection through each of the RAS pumps (returned activated sludge) from the clarification zones (pumps 452, 454, 456, and 458) and the RAS line (lines 460, 462, 464, and 466); sending to vessel 400 (aerobic reaction zone # 1) for further processing. Separated liquid from the fining process exits vessel 416 through conduit 468, vessel 418 through conduit 470, vessel 420 through conduit 472 and vessel 422 through conduit 474, and these flows are combined in a manifold 476

0 (CB Clar Eff). Such a clarifying device then discharges the effluent through line 478 as the final treated (treated) effluent.

The alternative embodiment shown in Figure 10 illustrates the removed unused lines, unused containers and equipment from the preferred prior embodiment of the device of the invention. However, all lines, containers and equipment used as required to treat the wastewater flow using an alternative embodiment of process # 4 of the present invention are shown.

• ·· ·

4 ·· 4 4

Thus, Figure 10 illustrates an alternative embodiment of an apparatus of the present invention that uses an alternative embodiment of Process # 5 of the present invention to provide nitrification processing characteristics in conjunction with a step feed type flow characteristics. An alternative embodiment of Process # 5 of the present invention is a treatment method that is zone-oriented and not vessel-oriented.

For an alternative embodiment of Process # 5 according to the invention ⁰ , the inlet flow is represented as heavily polluted waste that could contain high NH ₃ concentrations, high TSS concentrations and total high BOD concentrations while at the same time requiring nitrification as might prove necessary for an inlet liquid which is stream ^{5 of} industrial, heavily contaminated waste.

In the present alternative embodiment of the present invention, shown in Fig. 10, the feed liquid containing suspended solids and biodegradable organic substances is passed through line 500 to distribution box 502 (SB PLT Inf) where it is distributed. 50% of the total inlet flow is fed to vessel 504 (aerobic reaction zone # 1 - V # 1) through line 506, 30% of the total inlet flow is passed through manifold box 502 (SB PLT Inf) through line 508 to vessel 510 (aerobic Reaction ⁵ zone # 2 - V # 2), and the remaining 20% of the total inlet flow is passed through manifold box 502 (SB PLT Inf) through line 512 to vessel 532 (aerobic reaction zone # 3 - V # 3).

As noted above, vessel 504 is used as the ₀ aerobic reaction zone # 1, which receives 50% of the total inlet. Further flows come from each of the four ripples. Rj rj 4 4 4 4 5 6 7 8 9

4

44 devices (containers 516, 518, 520, 522) in the form of returned activated sludge (RAS). The content by volume of this vessel 504 is recirculated substantially once every two hours using a recirculation aeration system (RCAS) which is driven by the pump 524. During the recirculation procedure, the contents of vessel 504, namely the settable solid, become dissolved by comminution, as it passes through RCAS in this vessel. The comminution takes place as the solids in the aqueous solution are processed by the RCAS system by the toroidal vortex action of the RCAS system so as to become a more easily consumable population of microorganisms. Intensive aeration is also applied during the recirculation procedure so that the dissolved oxygen level is essentially maintained at a concentration of 3.5 mg / L or higher. Maintaining dissolved oxygen concentrations at these levels allows the nitrosomonas and nitrobactor residing in the colony of microorganisms to oxidize (ammonia) ammonia (NH ₃ ) to nitrite (NO ₂ - nitrogen dioxide) and eventually to nitrate (NO ₃ - nitrous oxide). This process is generally known to those skilled in the art as nitrification.

With dissolved oxygen concentrations in this zone maintained at 3.5 mg / L or greater, suspended solids and other organic matter, including but not limited to carbon BOD, are decomposed and oxidized to more stable compounds. This initial decomposition of organic matter, which is the breaking of organic matter from more complex forms to simpler forms, takes place mainly through the digestive action of aerobic bacteria.

By utilizing the large volumes of atmospheric air supplied by RCAS and keeping dissolved fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc fcfc At higher levels (over 3.5 mg / l) than would be maintained by traditional aeration systems, and along with long MCRTs, colonies of microorganisms will enter a biological life cycle mode known as endogenous respiration (ER). ). In this ER mode, living microorganisms begin to oxidize some parts of their own cellular matter together with any new organic matter they absorb or adsorb from their environment. This assists in improving solids reduction while maintaining a colony of microorganisms by adjusting the nutrient to microorganism ratio (F / M) to allow the colony's extinction rate to be the same as the growth rate of the colony of microorganisms through the ER process (endogenous respiration).

η £ Z E / NW>

Another advantage of providing intense aeration within this vessel is the consumption of certain amounts of phosphorus by the microorganisms.

The flow leaves vessel 504 (aerobic reaction zone # 1) through line 526 and is further directed to vessel 510 for further 20 aerobic processing.

The flow enters vessel 510 from vessel 504 along with 30% of the inlet flow to the device, which is provided by line 508. The vessel 510 is used as an aerobic reaction zone # 2. The content by volume of this vessel is recirculated substantially once every two hours using a recirculating aeration system (RCAS) which is driven by the pump 528. During the recirculation procedure, the contents of the container 510, namely the settable solid, become dissolved by

Pulverizing as passed through the RCAS in this vessel. Another advantage of the RCAS system of vessel 510 (Aerobic Reaction Zone # 2) is: * A * A * A * A * A * A

AA AA

A A

A A

A A

A A ··· ·· · AA ·

A A

A • A A

A A A

A A applied intense aeration so that the dissolved oxygen level is essentially maintained at a concentration

3.5 mg / l or higher. Maintaining dissolved oxygen concentrations at these levels allows the bacteria colony to convert organic matter, including but not limited to total BOD. Organic nitrogen is also converted, first to ammonia, then to nitrite, and finally to nitrate. This process reduces the total nitrogen and total BOD concentrations to less harmful compounds. Again, microorganisms consume additional amounts of phosphorus and reduce phosphorus concentrations in the system.

The flow leaves vessel 510 (aerobic reaction zone # 2) through line 520 and is directed to vessel 532 (aerobic reaction zone # 3). The flow also enters vessel 532 from manifold box 502 (10% of the inlet flow of the device through line 512). The content by volume of this container 532 is recirculated essentially once every two hours using a recirculation aeration system (RCAS) which is driven by the pump 534. During the recirculation procedure, the contents of container 532, namely the settable solid, become dissolved by comminution, as it passes through RCAS in this vessel. Another advantage of the RCAS system of the container 532 is the intensive aeration applied so that the dissolved oxygen level is substantially maintained at a concentration of 3.5 mg / L or higher. Maintaining dissolved oxygen concentrations at these levels allows the bacteria colony to convert organic matter, including but not limited to total BOD. This process reduces total BOD concentrations to less harmful compounds. Again, inevitably, microorganisms consume additional amounts of phosphorus.

• 9 • 9 • 9 • 9 • 9

9

I · * 9 «• 0 9 40» • 9 90 • 49 · 9 9

9,499 4 4 9 • 49,949 4 0 • 94 4 4 0 * 0

04 09 49

The flow exits the vessel 532 via gravity through line 536 and into line 538 before entering the clarification zone flow manifold 540 (SB Clar Inf) to deposit some solids from the liquid portion of the wastewater.

As the outlet liquid from line 538 enters the flow clarifier housing 540 (SB Clar Inf) of the clarification zones, the flow is preferably divided into four equal parts and each part is directed to one of the four clarifying devices (containers 516, 518, 520 and 522) through vessel 542 for vessel 516 (corresponding to fining apparatus # 1), vessel 544 for vessel 518 (corresponding to finishing apparatus # 2), vessel 546 for vessel 520 (corresponding to finishing apparatus # 3), and channel 548 to vessel 522 (corresponding to finishing apparatus) # 4). The flow rate is reduced as the flow enters each of the fining devices, allowing the solids to settle at the bottom or bottom of each of the fining devices. The deposited solids are then pushed away from the conical walls of the fining devices by using a hydraulically operated solid concentrator 550 for container 516 (fining device # 1), a hydraulically operated solid concentrator 552 for container 518 (fining device # 2), a hydraulically operated solid concentrator 554 for the container 520 (fining plant # 3) and the hydraulically operated solid concentrator 556 for the container 522 (fining plant # 4), allowing for further thickening of the solids prior to removal through each of the RAS pumps (returned activated sludge) from the fining zones ( pumps 558, 560, 562 and 564) and a line for RAS (lines 566, 568, 570, and 572) and sent to vessel 504 (aerobic reaction zone # 1) for further processing. Separated liquid from the clarification process • · φ · φ · φ · φ · φ · φ ·

Φ Φ φ φ φ φ φ φ φ φ φ φ φ φ φ φ φ φ φ φ · · · · · · · · · vystup vystup vystup vystup vystup vystup vystup vystup vystup vystup vystup vystup vystup vystup container 518 through line 576, container 520 through line 578, and container 522 through line 580, and these flows are combined in a collection box 582 (CB Clar Eff). Such a clarifying device then discharges the effluent through line 584 as the final treated (treated) effluent.

The recirculating aeration system (RCAS) of Fig. 15 shows one of the main components for performing the waste water treatment method with improved solids reduction according to the present invention. RCAS is an effective means for comminuting, mixing, mixing, circulating, aerating, homogenizing and saturating wastewater, each of the above activities being utilized as required. RCAS is a type of conduit transport system that guides the contents of the vessel through a mechanical pump generating a high flow rate of the contents of the vessel through a differential injection nozzle, the pump and nozzle being preferably located on the outside of each vessel for ease of maintenance. The air passing through the differential injection nozzle is injected into the waste water stream which is then returned to the vessel. As the contents of the container pass through the RCAS system, organic solids are comminuted so that these organic solids dissolve and homogenize for easier digestion by microorganisms. Another advantage of the RCAS system is the destruction of pathogenic microorganisms by means of a toroidal whirling action at the exit of the device (in-line injector / mixer / aerator) that provides agitation.

• 0 0 0 0 0 0

0 0 00 0

0 0 0 0 0 • 0 0 0 0

0000

The RCAS includes a suction line 600 connected to the suction side of the pump 602, a discharge line 604 that includes a row injector / mixer / aeration device 606, such as the device described in US Patent No. 5,893,641 (all of which is hereby incorporated herein by reference ref.), air / oxygen feed line 608 and feed line 610 (to the vessel). The pump 602 removes the waste water from the container 612 containing the aqueous solution, transports it through line 600 to the aeration device 606 for mixing, aerating and mixing. The waste water is then returned to the vessel 612 through the conduit 610, whereby excess atmospheric air trapped in the bubbles flows along with the waste water inside the conduit 610 and is released, causing the effect of secondary aeration, mixing and mixing of the waste water contained in the vessel 612 During the waste water process, this water passes through the aeration device 606, as shown in Fig. 15, where atmospheric air is drawn in through a vacuum (Venturi effect). The waste water and atmospheric air are mixed at the outlet of the in-line aerator 606 and while passed through line 610, wherein the waste water is saturated with oxygen. The aeration device 606 may be an aeration device as described in US Patent No. 5,893,641, or any other aeration device with similar performance to any of the aeration devices described in the present PCT patent application serial number PCT / US01 / 11936 or in US patent application no. Serial No. 09 / 547,447, the entire contents of which are hereby incorporated by reference.

· · «4 4 4 ♦» 9 9 9 4

9 9 9 9 999 9 9 9

999999 99,999 9 9

9 9 9 9 9 9 9 9 9

9 9 9 9 9 9 9 9 9 ·

Oxygen-saturated mixed wastewater passes through line 610 and is then discharged back into vessel 612. Along with saturated wastewater, excess atmospheric air bubbles are carried within line 610 that have been injected into the wastewater flow in an amount greater than that required for complete saturation of waste water 610. When this excess conduit 610 into vessel 612 is combined with saturated waste water, this excess air becomes a source of additional air supplied to the contents of vessel 612, thereby extending the aeration process of the entire contents of vessel 612 by providing an additional oxygen source that can be absorbed by the hitherto unrecirculated contents of the container 612.

advancing inside the air duct discharged from

Alternate flow of some or all of the wastewater through line 614 would allow additional control that is available to reduce aeration while continuing with the mixing and mixing functions of the system.

Under certain conditions, induced pressures can be generated by adding resistance to supply lines with obstructions or friction losses (i.e., reducing line size), fittings, valves, nozzles, and so on.

For certain conditions related to conduit 610, such as specific conduit size requirements, conduit length specific requirements, when RCAS installation is limited to defined limit parameters that do not meet the design requirements for aeration or agitation processes, they may be within conduit 610 induced pressures that would compensate for the environment inside the 610 line.

»4 4 4» 4 443 ► 4 4

4 * 4 44 ► 4 * 444

4

4 4

4 4

4 4

4 4 4 • 4 »4 offset the characteristics of the ducts with different diameters, lengths or required pressure existing in such ducts to achieve the required specific aeration criteria. Compensations that can be expected are represented by adding valves, fittings, in-line mixers, reducing or increasing the diameter of the conduit, or by incorporating a restriction such as orifice into the conduit 610.

Through recirculation processes, oxygen transfer capabilities and the creation of micro-bubbles by RCAS, energy consumption is reduced compared to traditional aeration systems using blowers and compressors. This RCAS efficiency allows the present invention to use a smaller footprint for the overall design of the device.

Bubbles

Aeration of the aqueous solution is important for aerobic digestion of biological nutrients. The smaller the bubbles, the greater the activity of aerobic digestion of bacteria and other microorganisms as a result of breathing (respiration) of easily accessible dissolved oxygen. Given these two facts, the best possible form of bubbles delivered is micro-bubbles.

5

Oxidative (oxidative) biological and chemical processes in the aquatic environment are limited by the low solubility of oxygen in water. This physical limitation, as defined by Henry's Law, states that, while maintaining a constant temperature, the amount of gas that dissolves in the liquid is proportional to the pressure exerted by the gas on the liquid. When using the RCAS system, the following are used: The gas and liquid pressures are raised above atmospheric pressure to increase the amount of oxygen gas that can be dissolved in the waste water.

The solubility of oxygen in pure water is only about 10 ppm (parts per million parts) at ambient temperature and at one atmosphere pressure.

For most aerobic bioprocesses, dissolved oxygen is rapidly consumed, so renewing and replenishing it becomes a factor that limits the speed of the process. Thus, the most critical component of the bioprocess design is the means for converting the oxygen mass into the liquid phase of the process. For an active breathing culture of bacteria, the oxygen in the liquid medium must be replenished as needed at a sufficient rate to maintain the oxygen demand. With the RCAS system used according to the present, dissolved oxygen is replenished and recovered with the bacterium. of the invention at the rate of bacteria.

which exceeds the oxygen demand

Water is usually aerated by forming contact surfaces between the gaseous and liquid phases. This can be done either by introducing an oxygen source into the liquid phase mass or by flowing the dispersed water through the mass of the gas phase (air). Regardless of whether the oxidation process is dominated by the gaseous or liquid phase, the transfer of oxygen mass or other gas is accomplished by introducing bubbles into the liquid phase. The mass transfer efficiency between liquid and gaseous phases largely depends on bubble characteristics. Bubble behavior strongly affects the following mass transfer parameters:

(a) Transfer of oxygen from the interior of the bubble to the interface between the gaseous and liquid phases;

(b) Oxygen transfer through the gas-liquid interface; and 5 (c) Diffusion of oxygen through a relatively standing liquid film surrounding the bubble.

Generally concurring opinion prevails that the most important properties of the air bubbles in the bioprocess is the ₁₀ size. For a given volume of gas, a larger interface between the gas phase and the liquid phase is provided when the gas is dispersed (dispersed) into many small bubbles rather than being in several large ones. It has been verified that small bubbles having dimensions of, for example, 1 to 3 mm, have the following advantageous properties that the large bubbles lack.

Small gas bubbles rise more slowly than large bubbles, allowing longer time for dissolving the gas in the liquid phase. This property is referred to as gas retention, and oxygen concentrations in water can be more than doubled while limiting solubility according to Henry's Law.

Thus, for example, once the saturation limit of 10 ppm oxygen is reached, at least an additional 10 ppm oxygen in small bubbles would be available to replace and replenish the oxygen.

Once the bubble has been formed, the main barrier to the transfer of oxygen to the liquid phase is the film of liquid surrounding the bubble. Biochemical engineering studies have concluded that transmission through this film becomes a speed limiting step in the process and controls the overall rate of mass transfer. However, as the bubbles become smaller, the thickness of this liquid film decreases so that the transfer of gas to the liquid phase mass is no longer delayed.

When air is introduced through a vacuum, as in RCAS, with a velocity and volume equal to the flow rate of the aqueous solution through the pump, micro-bubbles are formed. These microspheres have the size required to remain in suspension through the action of gas retention, which increases the dissolved oxygen concentration above the needs of the bacteria.

Uniqueness of the invention

1) The present invention operates in biological treatment ranges that differ from traditional wastewater treatment or treatment systems.

The present invention utilizes a mean cell residence time (MCRT) ranging from 30 days to over 150 days, while traditional systems cannot achieve such a long residence time.

The nutrient to microorganism (F / M) ratio maintained by the present invention, supported by its efficacy values, is essentially in the range of 0.05 to 0.80, as opposed to the limited range of this ratio as observed in various traditional systems.

The present invention utilizes a wastewater treatment plant with a unique design to treat a total portion of the wastewater BOD using less energy through the plant's processing operation. This treatment, or processing, is designed to substantially reduce, or even eliminate, all biodegradable solids. This unique process has such an effective level of aeration and conditioning.

as a result of recirculation, it enables operation on the efficiency of processes performed during cycles

The objective of the traditional design of the wastewater treatment plant ⁵ is to physically remove as much solids from the inlet stream as possible, and finally to remove or dispose of the solids collected from the treatment system after treatment. The balance of the waste water is treated by various means to various degrees of purity, ¹⁰ which suitably meet the level required for the various types of disposal.

2) The present invention utilizes the construction of fining containers with a conically shaped bottom of containers in which settled solids are collected without the use of mechanical means for concentrating the settled solids.

The waste water inside the vessel is rotated at a sufficiently slow speed to cause the sludge to settle, while at the same time there is no possibility of sludge

2Q adheres to the sides of the conically shaped bottom. The speed of the rotating solids remains slow enough to allow them to settle and not remain in suspension. This is accomplished by means of an accumulation induction system of solids used in the fining apparatus for the controlled rotation of the liquid in the containers.

The traditional fining plant has a mechanical device for transporting sludge to the sludge pit area of the sludge pump for removal. The mechanical means consist of a motor, a gear reducer, a scraper arm, a wiper blade and a wiper blade and a wiper arm.

• ·

• · · ·

• · · ·

3) The present invention (in a preferred embodiment of the device) basically utilizes conventional vessel design and equipment. This allows changes in the use of containers for different processes. All of the containers have substantially the same size and shape to allow the containers to be used as a single processing zone. An example of use as one processing zone could be the use of all vessels as aerobic reactors during start-up procedures. All are designed to be substantially the same and with the same wiring and have essentially the same functional capabilities (if desired). The system has such built-in redundant functions in that each of the vessels has the same size and shape, allowing any of the vessels to be used for any process that is needed, for example, during maintenance work. The arrangement of the vessels and manifolds is such that any processing zone can be expanded incrementally by simply repeating the processing vessels and manifolds as needed to meet the performance requirements and / or discharge capabilities. With the arrangement of the manifolds and containers, additional options are possible for the use of processing containers with little or no operational interruptions. This is made possible by simple changes in the valves.

4) The present invention utilizes the velocity, volumetric capabilities, and flow directions of the RCAS at its discharge point d of the vessel to regulate the rotational speed and process time for mixing and / or settling solids in each zone. For example, an aerobic reactor could be converted to an aerobic digester by:

Separating the aerobic reactor by aerating the contents while at the same time achieving complete solids digestion.

• Decelerate the rotational speed in the anoxic selector to allow solids to settle for transfer to the anaerobic conditioning device.

• Decelerating the rotational speed in the anaerobic conditioning device to allow solids to settle for transfer to the aerobic digester.

• Retaining aerobic digester content while aerating to nearly complete digestion of organic matter.

• Stopping the aerobic digestion process, allowing any inorganic mass to settle at the conical bottom and then removing any inorganic mass for disposal.

• Starting the process again for continued digestion of organic matter.

• wherein, after complete organic digestion, the aerobic digester can be returned to the state in which it serves as an aerobic reactor (aerobic reaction zone or vessel).

5) The present invention reduces the number of pathogenic organisms within the wastewater by using the RCAS system. This is because the turbulence and mixing within the toroidal vortexes in the RCAS creates a strong action that cuts the cell membranes of bacteria, such as colic and faecal coliforms, allowing the electron acceptors of the bacteria to be used

91 • · · · • · · · • · · · • · · · · · • · · • · · ·· ·· ·· 4 4 • · ··· 4 4 • · · · · • · · · · · ·· ·· ·· 44 4 4 4 4 • • · • · oxygen that then oxygenates (oxidize) bacteria, whereas kills them. While in the previous description in connection with links

illustrative embodiments of the present invention have been described with reference to the accompanying drawings, it should be understood that the invention is not limited to these specific embodiments, and that various changes and modifications may be made to those illustrated embodiments by those of ordinary skill in the art without the scope of the present invention would be exceeded. For example, square or rectangular processing vessels having flat or sloping bottoms can be used with the same RCAS efficiency as in traditional processing vessels. The biological process of the present invention operates with sufficient circulation, agitation, aeration and homogenization independently of the RCAS system.

Claims (16)

A method of treating an aqueous solution containing waste, comprising the steps of: supplying an effluent feed stream to an anaerobic treatment zone in which all aqueous solids are recirculated, mixed and suspended; supplying low oxygen suspended suspended solids from the anoxic selection zone to the anaerobic treatment zone to maintain a low dissolved oxygen level in the anaerobic treatment zone; supplying an effluent stream from the anaerobic treatment zone to the first aerobic treatment zone, wherein the effluent from the anaerobic treatment zone is agitated in the first aerobic reaction zone with activated sludge returning from the clarifying zone, the contents of the first aerobic reaction zone being recirculated and aerated, present in the contents of the first aerobic reaction zone are fractionated to decompose and oxidize the solids and other organic matter and accumulate inert solids; discharging the accumulated inert solids from the first aerobic reaction zone; supplying the aqueous solution effluent from the first aerobic reaction zone to the anoxic selection zone, wherein the aqueous solution is recirculated and stirred in the anoxic selection zone; transferring a first portion of the aqueous solution from the anoxic selection zone corresponding to the low oxygen suspended suspended solids to an anaerobic conditioning zone and a second portion of the aqueous solution from the anoxic selection zone to a second aerobic reaction zone; recirculating and aerating the aqueous solution contained in the second aerobic reaction zone, wherein the settable solids fractionate, thereby decomposing and oxygenating the suspended solids and other organic matter; supplying a first portion of the aqueous solution from the second aerobic reaction zone to the first aerobic reaction zone; supplying a second portion of the aqueous solution from the second aerobic reaction zone to a fining zone to deposit or separate solids from the aqueous solution contained therein; supplying deposited or separated solids from the 10 fining zone corresponding to the returned activated sludge to the first aerobic reaction zone; supplying the aqueous solution from the clarifying zone to a filtering zone for settling or separating solids from the aqueous solution introduced into the zone; and 15 transferring the liquid portion of the effluent from the filtering zone to the discharge tank and the portion of the effluent of the filtering zone, consisting of settled or separated solids, into the inlet effluent stream for reprocessing. 2. A process for the biological treatment of an aqueous solution containing waste for the reduction of organic material, nitrogen and phosphorus, comprising the steps of: supplying an inlet wastewater stream containing microorganisms to an anaerobic treatment zone in which all aqueous solids are recirculated, mixed and kept in suspension, carrying out a first phase of excess phosphorus absorption by controlling the flow of low-suspended suspended solids oxygen from the anoxic selection zone to the anaerobic treatment zone to maintain a low level of dissolved oxygen in the anaerobic 30. . . upravovači zone; ..7.F ^ so ^ - Qyy 9 9 supplying an output flow from the anaerobic conditioning zone to the first 9 9 9 9 9 9 an aerobic reaction zone, wherein the effluent from the anaerobic conditioning zone is stirred in the first aerobic reaction zone with the returned activated sludge received from the fining zone, wherein 5, the contents of the first aerobic reaction zone are recirculated and aerated, while nitrification takes place and the settable solids present in the contents of the first aerobic reaction zone are fractionated, thereby decomposing and oxygenating the suspended solids and other organic matter together with the improvement 10 shows a second phase of excess phosphorus absorption and inert solids accumulation; discharging the accumulated inert solids from the first aerobic reaction zone; supplying the aqueous solution effluent from the first aerobic reaction zone 15 to the anoxic selection zone, which aqueous solution is recirculated and stirred in the anoxic selection zone, and inducing a low oxygen environment in the anoxic selection zone so that denitrification and release of the phosphorus co-occurs consumption 20 organic matter contained in an aqueous solution; transferring a first portion of the aqueous solution from the anoxic selection zone corresponding to the low oxygen suspended suspended solids into an anaerobic conditioning zone and a second portion of the aqueous solution from 25 of an anoxic selection zone into a second aerobic reaction zone, wherein at least the second portion of the aqueous solution from the anoxic selection zone is rich in microorganisms and nutrients; recirculating and aerating the aqueous solution contained in the second aerobic reaction zone while in progress 30 nitrification and settable solids are fractionated, whereby the kxsa - 9 μ? · · · · * * * «« «« «« «« «« «« «« «#« # # # # # · Break down and oxygenate suspended solids and other organic matter, and in addition, the second phase of excess phosphorus absorption is improved, resulting in the consumption of large quantities of phosphorus by micro-organisms; supplying a first portion of the aqueous solution from the second aerobic reaction zone to the first aerobic reaction zone; supplying a second portion of the aqueous solution from the second aerobic reaction zone to a fining zone to deposit or separate solids from the aqueous solution contained therein; supplying deposited or separated solids from the fining zone to the first aerobic reaction zone as a reclaimed activated sludge; supplying the aqueous solution from the clarifying zone to a filtering zone for settling or separating solids from the aqueous solution introduced into the zone; and transferring the liquid portion of the filter zone outlet to the discharge tank and the portion of the filter zone outlet, consisting of solids or separated solids, to the inlet effluent stream for reprocessing. containing the associated zone is received 3. Apparatus for treating aqueous solution, waste, comprising: an anaerobic treatment zone through the liquid inlet, wherein the anaerobic treatment input stream of wastewater through the inlet, the anaerobic treatment zone recirculates the waste water contained therein so that all aqueous solids are kept in suspension, the anaerobic treatment zone receives the flow in liquid admixed suspended solids oxygen levels from the anoxic selection zone to maintain a low level of dissolved oxygen in the anaerobic conditioning zone; 94 $ ♦ * * 9 9 9 9 9 A first aerobic reaction zone in fluid communication with the anaerobic treatment zone, the first aerobic reaction zone receiving an anaerobic treatment zone effluent that is mixed with the returned activated sludge received from the clarification 5, wherein the contents of the first aerobic reaction zone are recirculated and aerated, and wherein settable solids are fractionated thereby decomposing and oxygenating suspended solids and other organic matter, the first aerobic reaction zone accumulates inert solids, wherein 10, these accumulated inert solids are discharged from the first aerobic reaction zone; an anoxic selection zone in fluid communication with the anaerobic conditioning zone and the first aerobic reaction zone, wherein the anoxic selection zone receives an aqueous solution effluent from 15 of the first aerobic reaction zone, wherein the aqueous solution in the anoxic selection zone is recirculated and stirred, and wherein the first portion of the aqueous solution from the anoxic selection zone corresponding to the low-oxygen suspended suspended solids is fed to the anaerobic conditioning zone; 20 a second aerobic reaction zone in fluid communication with the anoxic selection zone and the first aerobic reaction zone, the second aerobic reaction zone receiving a second portion of the aqueous solution from the anoxic selection zone, wherein the aqueous solution in the second aerobic reaction zone is recirculated; 25 is aerated, wherein settable solids are fractionated, and wherein a first portion of the aqueous solution from the second aerobic reaction zone is fed to the first aerobic reaction zone; a clarifying zone fluidly connected to the second aerobic reaction zone and the first aerobic reaction zone, the latter 30 The clarification zone receives the second portion of the aqueous solution from the second 4 4 44 # 4 4 44 · «• 4 4 4 4 4 4 4 .. ΤΚ. - 344 • 44 • 44 • 4 • 4 • 4 · 4 · 4 · 4 · 4 · 4 · 4 · 4 · 4 · 4 aerobic reaction zones, whereby settling or separation and entrapment of solids from the aqueous solution occurs in this clarification zone, and wherein the deposited solids corresponding to the returned activated sludge are fed to the first aerobic reaction zone; and a filter zone fluidly connected to the fining zone, the inlet and the outlet, the filter zone receiving the effluent from the fining zone to separate the solids from the liquid portion of the fining zone content, the first portion of the filtering zone corresponding to the effluent being and a second portion of the content of the filter zone, which corresponds to the separated solids, is fed to the inlet and is mixed with the inlet effluent stream for reprocessing. 4. A method of improving the reduction of solids by changing the state of at least one of a plurality of constituents of a contaminated aqueous solution containing nutrients, microorganisms and oxygen to a beneficial state, which comprises greater homogenization and therefore greater proximity availability together with , a physical and chemical process used to treat contaminated aqueous solutions, comprising the steps of: causing velocity changes in at least one direction within at least a portion of said contaminated aqueous solution, causing pressure changes on at least a portion of said contaminated aqueous solution, forming at least one high shear zone that acts on at least a portion of said contaminated aqueous solution, and comminuting agglomerates and solids at least in parts I contaminated aqueous solution to change their state to beneficial state. The method of claim 4, further comprising the step of forming bubbles in at least a portion of said contaminated aqueous solution. The method of claim 4, further comprising the step of mixing and stirring the contaminated aqueous solution to increase its homogenization. The method of claim 5, further comprising the step of mixing and stirring the contaminated aqueous solution to enhance its homogenization. The method of claim 4, further comprising the step of digesting the cells of the microorganisms in the contaminated aqueous solution, changing their state to a beneficial state. The method of claim 7, further comprising the step of digesting the microorganism cells in a contaminated aqueous solution, which changes their state to a beneficial state. 10. The method of claim 6, further comprising the step of cleaving the microorganism cells in a contaminated aqueous solution, which changes their state to a beneficial state. The method of claim 8, further comprising the step of forming bubbles in at least a portion of said contaminated aqueous solution. 12. A method of improving the reduction of solids, with a net yield of biological solids processed to a resulting yield close to the net zero increment of biological solids, through a state change ·· • 0 0 0 • 0 0 0 • 0 000 00 0 «0 0 • 0 000 • 0 0 0 0 0 0 0 0 00 00 of at least one of a plurality of constituents of a contaminated aqueous solution containing nutrients, microorganisms and oxygen to a beneficial state, which includes greater homogenization and hence greater proximity availability together with the possibility of reacting advantageously in at least one biological, physical and chemical process solutions comprising the steps of: causing a change in velocity in at least one direction within at least a portion of said contaminated aqueous solution, causing - pressure variations on at least a portion of said contaminated aqueous solution, forming at least one high shear zone acting on at least a portion of said contaminated aqueous solution, pulverizing agglomerates and solids at least a portion of the contaminated aqueous solution to change their state to a beneficial state, and cleaving at least some of the microorganism cells in the contaminated aqueous solution. The method of claim 12, further comprising the step of forming bubbles in at least a portion of said contaminated aqueous solution. 14. The method of claim 13, further comprising the step of mixing and stirring the contaminated aqueous solution to enhance its homogenization. 15. The method of claim 12, further comprising the step of mixing and stirring the contaminated aqueous solution to enhance its homogenization. when adjusting it by: 100 · Φ «♦ * · · 4 * ♦ · • · · »♦» » 16. A method of increasing the biomass concentration in a conditioning process during startup sequences, resuming operation in the event of a toxic accident, or operating requirements in a retained volume of a contaminated aqueous solution containing nutrients; 5 microorganisms and oxygen, by changing the state of at least one of the plurality of constituents of this solution to a beneficial state, which includes greater homogenization and hence greater proximity availability together with the ability to react advantageously in at least one biological, physical and chemical 10. A process used for treating contaminated aqueous solutions, comprising the steps of: causing velocity changes in at least one direction within at least a portion of said contaminated aqueous solution, causing pressure changes to at least a portion of said 15 contaminated aqueous solution, forming at least one high shear zone that acts on at least a portion of said contaminated aqueous solution, pulverizing aggregates and solids on at least a portion 20 of the contaminated aqueous solution to change their state to a beneficial state, mixing and mixing the contaminated aqueous solution to increase its homogenization, and forming bubbles in at least a portion of said 25 contaminated aqueous solution. Represented by: and'::.·; - 9 ^ 1/25 log growth phase decreasing growth phase steady phase endogenous respiratory phase Relative biomass concentration FIG.1 9 · · ♦ · · · · · «« «« «« «« «« «« «« «« «« « 2/25 exponentially decreasing endogenous growth phase growth phase nmsTpoqeroui gsopqoAy phase