Controlling wastewater treatment by monitoring oxygen utilization rates

• US 5,989,428 A
• Filed: 12/22/1997
• Issued: 11/23/1999
• Est. Priority Date: 06/21/1996
• Status: Expired due to Term

• Current Assignee: Mervyn Charles Goronszy
• Original Assignee: Mervyn Charles Goronszy
• Inventors: Goronszy, Mervyn Charles
• Primary Examiner(s): Wyse, Thomas G.
• Application Number:
  US08/973,554
• Time in Patent Office: 701 Days
• Field of Search: 210/614, 210/605, 210/607, 210/622-629, 210/96.1, 210/903, 210/921, 210/141-143, 210/195.1, 210/195.3
• US Class Current: 210/605
• CPC Class Codes: C02F 2203/004 comprising a selector reactor for promoting floc-forming or other bacteria
• CPC Class Codes: C02F 3/006 Regulation methods for biological treatment
• CPC Class Codes: C02F 3/1263 Sequencing batch reactors [SBR]
• CPC Class Codes: C02F 3/301 Aerobic and anaerobic treatment in the same reactor
• CPC Class Codes: C02F 3/308 Biological phosphorus removal
• CPC Class Codes: Y02W 10/10 Biological treatment of water, waste water, or sewage
• CPC Class Codes: Y10S 210/903 Nitrogenous
• CPC Class Codes: Y10S 210/921 Flow equalization or time controlled stages or cycles

Abstract

A method and apparatus for treating waste material to remove selected components form the waste is described using a reactor or a series of reactors in fluid communication with each other for receiving the waste to be treated as influent. The influent forms a biomass including the waste and microorganisms and is treated by controlling the metabolic activity of the microorganisms by monitoring the oxygen utilisation rate or the potential oxygen utilisation rate of the biomass so as to determine the required amount of oxygen to be supplied to the biomass and to determine the period of aeration of the biomass in order to maintain a predetermined oxygen utilisation rate or value so as to remove the selected components of the waste. The preferred selected components to be removed are nitrogenous, carbonaceous and/or biological phosphorus containing materials or derivatives.

Claims

1. A method of treating waste material forming at least a part of a biomass comprising a single activated sludge in a variable depth bioreactor using controlled intermittent and successive aeration sequencing and liquid decantation to concurrently grow and maintain a culture of autotrophic, heterotrophic and facultative micro-organisms in the sequentially aerated single activated sludge for the biological removal of the organic carbon, nitrogen and phosphorus components from wastewater admitted to the bioreactor, said biomass being located in a variable depth operated reactor having at least two interconnected zones in series connection in which one of the zones is a first reaction zone and the other zone in a second or last zone, wherein at least a part of the treated contents of the second zone of the reactor is recycled to a partially segregated non-aerated volume of the first reactor zone for admixture with incoming influent waste, at least during an aeration sequence of operation of the second or last of the variable depth operated reactor, wherein the method comprises using one dissolved oxygen concentration sensor or probe means for automatically and continuously monitoring dissolved oxygen concentration in the biomass in the second or last zone of the variable depth reactor, said sensor or probe means being located in the biomass at a location such that at least that part of the biomass in that location is in motion during the time of automatically and continuously measuring the dissolved oxygen concentration, whereby the single sensor or probe means is used to cause operation of an oxygen input means during input into and aeration of the wastewater in the second or last zone, in combination with computer means to operate algorithms in order to operate to a set protocol of successively increasing dissolved oxygen concentration from zero to about 2.5 Mg/L in discrete predetermined adjustable time increments to optimize the retention of adsorbed organic substance within the biomass while maintaining co-current and optimal nitrification and denitrification during aerated operation, with phosphorus release during non-aeration and phosphorus uptake during adjacent and reactive influent aeration sequences, with the detection and automatic calculation of the oxygen utilization rate of that biomass in the second or last variable volume zone which adjusts the length of each aeration sequence exposure of the biomass, said determination and adjustments being characterized by the biomass in the second or last zone of the reactor having a potential oxygen uptake rate, measured using an aerated admixture of 80%/20% single sludge biosolids/influent mixture, being in excess of about three times the measured uptake rate of the single sludge biosolids as measured by the single dissolved oxygen sensor, such that combined with the preset oxygen transfer rate and the potential oxygen uptake causes a limitation to the nitrogen oxidation product to essentially nitrite nitrogen form, and to cause by aerated mixing in the second or last variable volume zone a concurrent reduction reaction of the nitrite nitrogen to essentially nitrogen gas, in such a way that at the end of the aeration sequence, the biomass oxygen utilization rate is automatically controlled to an operating set point, adjunctively with the introduction of air into one or more partially segregated volumes within the first zone of the reactor to partially limit the release of phosphate in the biological phosphorus removal mechanism, such that the first zone of the biological reactor can be continuously and automatically controlled to limit oxic, anoxic and anaerobic successive reaction environments in the first zone of the variable depth biological reactor.

2. The method of claim 1, wherein the waste is domestic, industrial or commercial wastewater, including human wastes, body washing wastewater, clothes washing wastewater, food preparation wastewater, and combinations thereof.

3. The method of claim 2, wherein the last reaction zone is more than 50 percent of the total reaction volume, and the first zone receives mixed or unmixed contents, recycled from the second or last reactor zone for admixture with incoming waste.

4. The method of claim 1, wherein up to 40 percent of the design depth of the variable depth reactor is removed during the decantation step at a rate that does not cause removal of settled solids from within a settled sludge layer in the reactor.

5. The method of claim 1, wherein the second or last reactor zone is provided with oxygen transfer diffusion grids located at or towards the floor or base of the principal reactor.

6. The method of claim 5, wherein the bioreactor is provided with at least one air supply line provided with at least one motor operated control valve, so that the motor/operated control valve(s) can be alternately opened for a set program of air-on operation in a cycle and then closed.

7. The method of claim 6, wherein all of the motor operated control valves are operated in unison during the aeration sequence, or some of the valves are closed, or all of the valves are opened and closed according to a preset sequence of operation.

8. The method of claim 1, wherein the net fluid oxidation reduction potential of the combined liquid stream passing through the initial reaction zone obtains a value of less than about -150 mV as compared to a hydrogen reference electrode.

9. The method of claim 1, wherein up to 40 percent of the total bioreactor volume is introduced into the first zone during a time which is equivalent to the cycle time less the liquid removal air-on/off time sequence.

10. The method of claim 1, wherein the-cyclic air-on time exposure of the biomass and the amount of recycled treated waste admixed with the influent wastewater is sufficient to yield a less than -150 mV oxidation reduction potential in a time of less than 80 minutes.

11. The method of claim 1, wherein the oxidation reduction potential of segregated sludge in the second or last reaction zone falls substantially to less than -150 mV within 90 minutes into the air-off sequence.

12. The method of claim 1, wherein the solids concentration of the biologically activated sludge of the second or last mixed reaction zone is up to about 5000 mg/L.

13. The method of claim 1, wherein the bioreactor is formed with vertical walls of reinforced concrete or structural steel or formed as a slope walled lagoon structure having earthen, concrete stabilized, membrane lined or concrete retaining walls.

14. The method of claim 1, wherein the biomass remains in motion for up to 10 minutes after interruption of-the supply of air or oxygen.

15. The method of claim 1, wherein the values of dissolved oxygen concentration are automatically sensed and monitored in situ substantially continuously but not less than at intervals of 10 to 20 seconds during the total air-on and air-off sequences of each cycle.

16. The method of claim 1, wherein the use of the cycles of operation are managed by the measurement of the oxygen utilization rate in order to adjust it to appropriate values to provide for the satisfaction of reactor stoichiometiric oxygen demand which permits a single air supply to service one or more two zones of the bioreactor.

17. The method of claim 1, wherein the dissolved oxygen concentration sensor or probe is an electronic oxygen sensor able to measure the rate of change of dissolved oxygen concentration as a 4-20 milliamp primary control signal.

18. The method of claim 17, wherein the oxygen sensor is located within the second reactor about 30 cm from the surface of the second reactor floor, or in a full-flow conduit or pipe through which part of the liquid/solid material from the second reactor flows to the influent admission reactor.

19. The method of claim 1, wherein the TKN loading on the activated sludge is up to about 0.01 kg TKN/kgMLSS/M² /d for typical domestic sewage applications.

20. The method of claim 1, wherein the total phosphorus loading of activated sludge solids is up to about 0.002 kg Phosphorus/kgMLSS/M² /d for typical domestic sewage applications.

21. The method of claim 1, wherein the dissolved oxygen concentration in the principal reactor is controlled to less than 0.7 mg/L (average) for 75 percent of the air-on time and to between 2 and 3 mg/L for the remaining air-on time period.

22. The method of claim 1, further comprising:

microbially treating the wastewater in the presence of a micro-organism population acclimated to the wastewater contaminants and their concentrations in the wastewater, said micro-organism including,

nitrifying micro-organisms capable of converting nitrogen to at least nitrite nitrogen,

facultative micro-organisms capable of denitrifying nitrite and optionally nitrifying organisms capable of converting nitrite to nitrate nitrogen, and

facultative micro-organisms capable of reducing nitrate to nitrite nitrogen to nitrogen gas and phosphorus removal micro-organisms capable of biologically removing available soluble phosphorus.

23. The method according to claim 1, wherein the mixed liquor solids concentration in the second or last reactor is sensed and recorded at the moment that the air supply to that reactor in terminated and the oxygen uptake rate is sensed, recovered and analyzed following termination of the process oxygen supply and the liquid level at the time of closure of the influent valve to the reactor plus two minutes.

24. The method of claim 23, wherein the sensed process values are processed and used to determine:

the waste sludge pumping time,

the duration of the air-on sequence for the next cycle,

the mass flow rate of air for the next cycle,

adjustment of the dissolved oxygen concentration set-points,

such that the process conditions are sufficient to maintain the set-point oxygen uptake rate in the principal reactor determined at the end of the previous aeration sequence.

25. The method of claim 1, wherein a pH correction is made to the influent wastewaters.

26. The method of claim 1, further including a flow path of admixed components from the first zone of the bioreactor wherein the flow path has successive passes from adjacent the reactor floor to the liquid surface of the reactor in transit to an adjacent zone of the bioreactor, in which the mixing energy associated with the flow path near the reactor floor of the first reactor compartment is a minimum of 3 times the mixing energy associated with the flow path near to the liquid surface in succession thereby causing localized energy pulsation, nucleation and flocculation of the admixture.

27. The method of claim 1, wherein the set-point oxygen uptake rate is experimentally determined and is up to 20±

4 mgO₂ /gVSS/hour (referenced to 20°

C.).

28. The method of claim 1, wherein in which there are four bioreactors, or four modules forming the bioreactor and a flow splitter arrangement for distributing influent waste to each bioreactor or each module wherein each bioreactor or each module functions an a single bioreactor.

29. The method of claim 28, wherein each bioreactor comprises an influent position, configured inflow admixture compartments and an effluent decanting device comprising a moving liquid receiving channel designed to exclude surface floating material to effectively remove up to 40% of the bioreactor depth.

30. The method of claim 28, wherein the oxygen uptake rate or measured potential oxygen uptake rate in the initial admixture reactor is at least 20 mgO₂ /gVSS/hr.

32. The apparatus of claim 31 further including computer means for carrying out the process of claim 1.

31. An apparatus for biologically removing carbon, nitrogen and phosphorus from wastewater, in the form of a partially enclosed water-retaining, multi-zone, variable-depth, cyclically-aerated reactor comprising at least a first hydraulic zone and a last hydraulic zone separated by a partial wall structure allowing fluid communication and transfer between the zones at least during a part of an air-on sequence, an aerator for selectively exposing the contents of the reactor to repeated air-on and air-off sequences, said first hydraulic zone provided with an inlet for introducing influent wastewater to the first zone during at least the air-on sequence, said last hydraulic zone for allowing separation of the wastewater into at least supernatant clear liquor, an aerator including a grid air bubble generation system for providing combined mixing and oxygen transfer in at least the last hydraulic zone mounted on the floor of the reactor and a means for directing a flow of process air to the reactor for in-reactor oxygen transfer at least two different mass flow rates during the air-on sequence, means for interrupting the flow of influent wastewater to the first hydraulic zone at least during a part of the air-off sequence, means for removing liquid contents from the last hydraulic zone to a position remote from the reactor during at least the air-off sequence, means for transferring the contents from the last hydraulic zone to the first inlet hydraulic zone at least during the air-on sequence, means for interrupting influent wastewater flow and the flow of process air to the reactor during at least a part of the air-off sequence, means for reducing the amount of supernatant clear liquid retained in the last hydraulic zone during the air-off sequence to a preselected lower level using a motor-driven decanter comprising a horizontal weir box, fitted with a positive floating solids excluding scum guard, connected by at least one downcomer member to a rotating drum shaft provided with liquid retaining seals and airlock release pipes, means for automatically maintaining an optimum mixture of process acclimated heterotrophic, autotrophic and facultative micro-organisms and wastewater through the continuous measurement of the rate of change of dissolved oxygen concentration in the reactor together with measurement of the potential oxygen utilization rate of the biomass, said rate change of dissolved oxygen being measured by a single dissolved oxygen sensor located in the biomass, such that at least part of the biomass is in motion at the time the measurement is taken in order to provide an indication of the utilization rate as a function of time, a means for analyzing successive rates of change of oxygen concentration taken at the end of each air-on sequence in the last hydraulic zone, a means for continuously measuring the rate of change of dissolved oxygen concentration at the beginning of each air-on sequence, means for adjusting set point operating positions of the rate of change of dissolved oxygen in the last hydraulic zone of the reactor taking into account process air flow rate, air-on time adjustment and mixed heterotrophic, autotrophic and facultative micro-organism culture, means for adjusting and operating with at least four set point positions for the dissolved oxygen concentration as a function of time profile in each air-on cycle in the last hydraulic zone in order to achieve an indication of the termination of the air-on sequence set point dissolved oxygen concentration rate of use, means for automatically adjusting the

operating time duration of each total cycle and successive cycle, means for operating with and determining the duration of air-off sequence time in successive cycle times in the last hydraulic zone, means for operating with and determining the time-based flow rate of process air introduced to the reactor, and means for determining and executing the time of operation within each cycle for the removal of a predetermined volume of a mixture of biomass and wastewater in successive air-off sequences from the reactor.