US 4,867,883 AGrant
High-Rate Biological Waste Water Treatment Process Using Activated Sludge Recycle
Issue Date:1989-09-19
•14 Claims
•4 Drawing Sheets
Abstract
A high-rate biological waste water treatment process for removing organic tter, phosphorus and nitrogen nutrients from municipal waste water comprising the steps of mixing the influent waste water in an initial anaerobic reactor zone to maintain the biological solvents in suspension with a denitrified mixed liquor from a downstream anoxic reactor zone, typically at a flow rate of 0.5 to two times the waste water flow rate. The reactor zone serves to select microorganisms capable of accumulating quantities of phosphorus in excess of that required for simple cell growth and reproduction. The phosphorus removal occurs due to the removal of excess sludge (waste activated sludge) produced in the process wherein such sludge can be removed from the clarifier underflow or as a mixed liquor directly from the biological reactor.
Metadata
Assignee
- Hampton Roads Sanitation District of the Commonwealth of Virginia
Inventors
- Glen T. Daigger
- James R. Borberg
- Liliana M. Morales
Application Information
Application Number:US 2058588
Filing Date:1988-06-13
Priority Date:1987-04-21
Art Unit:136
Classifications
IPC:
C02F 330
Field of Search:
210605;612;614;622;624;626;630;903;906
Patent Drawings (4 sheets)
Description
Brief Description of the Drawings
FIG. 1 of the drawings is a block flow diagram showing the basic process steps in accordance with the present invention;
FIG. 2 is a simplified process flow diagram depicting an exemplary embodiment for the anaerobic, anoxic and aerobic reactor cells used in accordance with the present invention;
FIG. 3 is a graphical representation of the operating conditions and performance characteristics of a pilot plant study conducted in accordance with the invention; and
FIG. 4 is a comparative graphical representation of the effect of waste water TBOD/TPO.sub.4 on effluent soluble phosphate for two prior art systems and the process according to the invention.
Detailed Description of the Presently Preferred Exemplary Embodiment
With respect to FIG. 1 of the drawings, the basic treatment steps and equipment necessary for carrying out the activated sludge treatment method according to the present invention is shown generally as 100. The process flow diagram of FIG. 1 depicts the steps and equipment used in the pilot plant program (discussed, infra), and represents the complete liquid process schematic, including the steps of screening, preaeration, primary clarification, biological treatment and secondary clarification.
Pilot plant influent (shown as 101) consisting of raw plant influent waste water is continuously fed to a conventional grinder pump 102 positioned upstream of influent screens 103 which include fine mesh screens designed to protect the downstream pilot plant facilities from plugging. The screened waste water passes into a large holding tank 104 (known in the art as a "day tank"), with overflow directed in a continuous manner to the drain system (shown generally as 105) for eventual recycling and treatment. The waste water is pumped from the day tank to the treatment plant using progressive cavity pumps 106 and 107 into preaeration facilities consisting of a square high density polyethylene Nalgene container 108 which allows the influent to undergo preaeration for a specified time period (in the case of the pilot plant, an average hydraulic residence time of about 50 minutes). The air is metered through rotometer 109 and introduced into preaeration tank 108 through a fine bubble ceramic tube diffuser (not shown).
Following preaeration, waste water flows by gravity into the circular primary clarifier 110. The clarifier contains a galvanized steel effluent collection launder and includes means for removing sludge manually from the bottom of the clarifier through a valve and hose into line 111.
After primary clarification, the influent flows via line 112 to a series of biological reactors (also shown in detail in FIG. 2 of the drawings) consisting of twelve completely mixed cells in series shown as items 113, 114, 115, 116, 117, 118, 119, 120, 121, 122, 13 and 124, respectively. Each cell consists of one polyethylene Nalgene container as described above. Dye testing is conducted during start-up in order to verify that each cell is completely mixed and that the overall configuration provides an approximate plug flow pattern.
Anaerobic cells 113, 114 and 115, and anoxic cells 116, 117 and 118 are mixed using submerged mechanical mixers (not shown), with the mixing adjusted to maintain biological solids in suspension while minimizing oxygen transfer into the mixed liquor. The anaerobic and anoxic cells are not normally covered (except during wintertime operation) and thus are not operated under air-tight conditions. Air is added to each aerobic cell through a single fine bubble ceramic diffuser (not shown) identical to that used in the preaeration cell, with the air being metered into each cell through a conventional rotometer.
FIG. 1 thus depicts an exemplary reactor design using three anaerobic cells, three anoxic cells, and six aerobic cells shown as items 119, 120, 121, 122, 123 and 124. As those skilled in the art will appreciate, flexibility may be provided in the reactor configuration by using interconnecting piping system to vary the number of tanks in service. For example, bypass piping may be provided to allow the second anaerobic cell 114, the second anoxic cell 117, and the second and fifth aerobic cells 120 and 123, to be taken out of service, if desired. Recycle streams in the form of return activated sludge (shown as 125), anoxic recycle 126, and nitrified recycle 127 are conveyed using progressing cavity pumps 125a, 126a, 127a and 127b, respectively, through flexible hoses. This allows the location for recycle flows to be easily changed, resulting in various operating modes and process configurations.
FIG. 1 also illustrates the typical operating mode maintained throughout a normal reaction cycle. Typically, two anaerobic, two anoxic, and six aerobic cells are operated, providing a hydraulic residence time of about 6.5 hours (based on an average influent flow for pilot plant operations of 1.8 gpm). The return activated sludge and nitrified recycle flow are directed to the first anoxic cell 116 and anoxic recycle flow 126 is directed to the first anaerobic cell 113. In alternative embodiments, the number of cells in service may be varied depending on the desired effect on process performance characteristics.
FIG. 2 of the drawings represents a block-flow diagram for a portion of the pilot plant program at the end of Phase I in which reactor cell 114 (ANA2) was removed from service by using the illustrated bypass piping which served to reduce the total anaerobic liquid volume. The desired plug flow (but with increased staging) was accomplished by placing a baffle in the first anaerobic cell (see the dashed diagonal line through cell 113), thereby creating a shorter initial contact zone. FIG. 2 also illustrates the use of a third anoxic reactor cell 117 (ANX2) during Phase IV-D of the pilot plant program. The results of these reactor configuration changes on overall process performance are represented in the various Tables discussed below.
Mixed liquor 128 from the complete biological reactor, i.e. the series of reactor cells, flows to secondary clarifier 130 having a similar construction as the primary clarifier. Settled solids are removed from secondary clarifier 130 through line 129 by a progressing cavity pump 125a which operates continuously. A scum baffle (not shown) may be provided to minimize scum carryover into the secondary effluent. The clarifier effluent 131 flows b gravity to storage tank 132, and then to the plant drain system 133.
Waste activated sludge is pumped by a progressing cavity pump 134 from the last aerobic cell of the biological reactor (typically cell 124) and delivered to a waste activated sludge holding tank 135. Both the pump speed and pumping cycle must be adjusted to control the total volume of waste activated sludge removed from the process. Typically, waste activated holding tank 135 consists of a Nalgene container identical to that used for the preaeration tank and the biological reactor cells. Tank 135 permits accurate measurement of the daily waste activated sludge volume and provides a source of "seed sludge" in the event upsets or mechanical failures lead to significant solids loss. The volume of waste activated sludge pumped to holding tank 135 should be measured daily and used to adjust the setting on pump 134. Collected sludge 136 is then discharged to drain system 137. An overflow may also be provided on tank 135.
Example I
The activated sludge process according to the present invention was demonstrated by a pilot plant study segregated into a series of phases during which the overall conditions and operating objectives were held relatively constant. The general objective of the pilot plant program was to construct a test facility that would provide a reasonable simulation of a full-scale plant facility.
A nominal two gallon-per-minute (gpm) capacity was selected for the pilot plant study, based on the minimum primary and secondary clarifier size considered acceptable. The aeration basin consisted of a series of completely mixed tanks arranged in series, each having the required mixing, aeration, and recycle pumping facilities. The combined pilot plant unit processes included preaeration, primary clarification, biological treatment, and secondary clarification.
Feed to the pilot plant consisted of actual raw plant waste water in order to test the effects of factors such as toxic shock loads and dilute waste waters on process performance. The influent waste water was also varied on a diurnal basis in a fashion similar to that experienced at the plant from which the influent originated.
FIG. 3 of the drawings shows the operating periods, including plant performance, and a listing of major operation factors and occurrences during each of the successive phases of the pilot plant study.
Phase I of the pilot plant operation established baseline performance under constant flow conditions. As indicated above, diurnal influent flow variations were maintained for all phases except Phase I. Constant flow conditions, i.e., no diurnal variations were maintained for all recycled flows throughout Phases I-VI.
Phase II of the pilot plant program established baseline performance conditions under diurnal flow conditions; Phase III determined the effects of process loading on process performance during warm weather conditions; Phase IV involved process performance during wintertime operating conditions; Phase V determined the effect of alternative reactor configurations and solids handling recycles on process performance; and Phase VI determined performance characteristics of the pilot plant program when operated in the "A.sup.2 /O" mode, i.e., in accordance with the teachings of U.S. Pat. No. 4,056,465.
During Phases I through IV-C, two anaerobic cells, two anoxic cells and six aerobic cells were placed in operation. As such, the anaerobic, anoxic and aerobic zones represented approximately 20, 20, and 60%, respectively, of the total reactor volume. A baffle was inserted into the first anoxic cell at the end of Phase I in an attempt to increase the degree of staging. The anoxic recycle was maintained at approximately 100% of the average plant influent flow throughout this entire period. The nitrified recycle was maintained at approximately 100% and the return activated sludge flow was maintained at approximately 60% of the average plant influent flow for most of the period except during Phases IV-A and IV-B when the nitrified recycle was reduced to 60% and the return activated sludge increased to 100%.
During Phases IV-D and IV-E and all of Phase V, reactor configurations and recycle rates were significantly changed to investigate the effect of those parameters on overall system performance. During Phase IV-D, another anoxic reactor was placed in service, for a total of three reactors. Two anaerobic and six aerobic tanks were used as before. During Phase IV-E, the third anoxic reactor was taken out of service but another anaerobic reactor was added. The baffle previously inserted was also removed at that time. The anoxic recycle and nitrified recycle flow rates were maintained at 100% of plant influent flow and the recycle activated sludge flow was maintained at 60% of influent flow throughout that period.
During Phase V-C, additional phosphate was added to the pilot plant influent to stress the system. During Phase V-D, the third anoxic reactor was placed back in service (for a total of anaerobic and three anoxic reactors) and two aerobic reactors were taken out of service (making a total of four). The anoxic recycle and nitrified recycle flow rates were maintained at 100% of influent flow and the return activated sludge rate was maintained at 60% of influent flow. This same reactor configuration was maintained during Phase V-E, but the nitrified recycle rate was increased to approximately 690 percent of influent flow. No preaeration system was used during Phases IV-C through V-A.
During Phase VI, the pilot plant was operated :n the "A.sup.2 /O" mode, i.e., following the teaching of U.S. Pat. No. 4,056,465 with settled sludge returned to an initial anaerobic contact zone.
Table 1 summarizes influent waste water characteristics experienced during the pilot plant program. Periods of steady-state operation are presented separate from the average values for the entire period; however, the data for the steady-state period are included in the average values for the entire period. The influent waste water had a BOD concentration ranging from approximately 110 to 200 mg/l and a TSS concentration ranging from approximately 120 to 185 mg/l. Approximately 35 to 50 percent of the BOD was soluble, as defined by filtration through an 0.45-.mu. membrane filter. The COD/BOD ratio varied from approximately 1.8 to 2.7, with an average of 2.5. The soluble COD (0.45-.mu. membrane filter) was approximately 30 percent of the total COD. The suspended solids were approximately 80 percent volatile. Hydrogen sulfide values ranged from 1.9 to 8.8 mg/l on the average, and were highest in the late summer (August and September) and lowest in the winter.
Total phosphate concentrations varied from 4.0 to 6.8 mg-P/l, and soluble orthophosphate concentrations varied from 2.4 to 4.2 mg-P/l. TKN concentrations varied from 21.5 to 29.3 mg-N/l, while ammonia concentrations varied from 13.8 to 18.9 mg-N/l. Influent NOX (Nitrite plus nitrate) concentrations were negligible.
Table 2 summarizes the preaeration system performance. When in service, the preaeration system increased the dissolved oxygen (DO) concentration of the influent waste water to approximately 3 mg/l. From 20 to 45 percent of the influent hydrogen sulfide was also removed. Soluble COD removal ranged from 0 to 25 percent.
Tables 3 and 4 summarize the performance of the preaeration and primary treatment systems. The total suspended solids (TSS) removal efficiency initially averaged 30 to 35 percent (Phases I and II), which was somewhat less than typically expected for domestic waste water. During Phases III-A, III-B, and III-C, apparent negative TSS removal efficiencies were reported. This anomaly was thought to result from sampling problems. Thus, between Phases III-C and III-D, the primary clarifier was tapped to allow adequate flushing of the sample line prior to sample collection. Following this modification, TSS removal efficiencies of 30 to 60 percent were observed.
Removal patterns for total BOD, total COD, total phosphate, and TKN were similar to but less pronounced than those observed for TSS. These observations are consistent with the hypothesis that the primary effluent samples contained non-representative quantities of TSS during Phases III-A, III-B and III-C. The increase in total and soluble phosphate during Phases V-C and V-CS was a result of phosphate addition to stress the system. Approximately 10 to 30 mg/l of soluble COD (10 to 15 percent of influent values) and approximately 5 to 15 mg/l of soluble BOD (5 to 30 percent of influent values) were removed through preaeration and primary treatment. In contrast, the concentration of soluble phosphate tended to increase slightly.
Tables 3 and 4 also show measured primary effluent characteristics for the test period. The values reported for Phases III-A, III-B, and III-C indicate the general characteristics of the waste water. Measured total BOD concentrations ranged from approximately 90 to 130 mg/l. The soluble BOD concentration (0.45-.mu. membrane filter) ranged from 30 to 70 mg/l, and represented 25 to 50 percent of the primary effluent total BOD. The COD/BOD ratio is similar to that of the influent waste water, as is the soluble fraction of COD. Reported TSS values were variable but were less than 90 mg/l after Phase III-D (when sampling was considered to be the most representative). The TSS were approximately 80 percent volatile.
The total and soluble phosphate concentrations in the primary effluent were similar to the influent values. The total BOD/P04 ratio of the primary effluent averaged about 20, while the soluble BOD/soluble PO4 ratio ranged from about 10 to 15. The exceptions are Phases V-C and VI-B, where phosphate was added. These ratios indicate a waste water that is reasonably well suited for biological phosphorus removal (i.e., with sufficient organic matter present to drive phosphate removal). The TKN, ammonia, and NOX (nitrite plus nitrate) concentrations were as expected for a waste water of this type.
Table 5 (two pages) summarizes process operating conditions for the various operating phases, while Table 6 summarizes overall performance.
During the course of the pilot plant study, flow-proportioned grab composite samples were collected at the following locations:
raw influent
preaeration effluent
primary effluent
anaerobic effluent
anoxic effluent
aerobic effluent
return activated sludge
secondary effluent
The anaerobic effluent, anoxic effluent, and aerobic effluent samples were collected directly from the last cell of the respective reactor zones. For example, anaerobic effluent was collected directly from the third anaerobic cell (115 on FIG. 1). Samples from each location were collected every 2 hours and an aliquot proportional to pilot plant influent flow at the time of collection was transferred to a large container. These containers were stored in a 4.degree. C. refrigerator at all times. Sample date corresponded to the calendar day (midnight to midnight). Following completion of the 24-hour sampling cycle, each sample was thoroughly mixed and a representative sample transferred to a smaller container for later analysis.
Grab samples were also collected through each cell of the biological reactor by the pilot plant operator. These samples were centrifuged immediately upon collection and then filtered through prewashed 0.45 .mu. membrane filters. The collected solids were discarded and the filtrate retained for analysis. Individual samples for the various cells of the biological reactor were collected in a sequential fashion according to the calculated reactor flow-through times, so that a "slug" of influent waste water could be followed through. The filtered samples were analyzed for nutrient concentrations.
The overall performance data collected during the pilot plant program is summarized in Table 6 and demonstrates that a biological nutrient removal process in accordance with the invention to achieve high levels of phosphorus and nitrogen removal with low hydraulic residence times, e.g., enhanced nitrogen and hydraulic residence times as low as 3.7 hours for summertime conditions and slightly over 7 hours for winter conditions. Secondary treatment standards (30 mg/l BOD, 30 mg/l TSS) were also routinely satisfied.
The results of the pilot plant study also indicate that 67 percent of the total phosphorus on a yearly basis could be removed with only seasonal variations in continuous nitrogen removal. Effluent soluble (0.45-.mu. membrane filter) BOD.sub.5 consistently averaged 1 mg/l, except during start-up, transition periods, and during cold weather operation when they were slightly higher. Effluent total phosphorus concentrations routinely averaged 1.5 mg/l or less, and removal efficiencies ranged from 75 to more than 90 percent during periods of good performance.
Essentially complete nitrification was observed during several phases of the pilot plant program. Total nitrogen removal approached 70 percent during these same periods. Reduced total nitrogen removal was observed when nitrification was not complete However, during these periods not all of the available nitrogen was converted to nitrate, thus limiting the mass of nitrogen that could be denitrified in the anoxic zone. Effluent alkalinity values ranged from 65 to 108 mg/l, and effluent pH values always exceeded 7. However, effluent alkalinities would be greater than expected if denitrification had not occurred in the biological process.
The results of pilot study also suggest that biologically enhanced phosphorus removal may be adversely affected by long aerobic hydraulic residence times and by an oxidation-reduction potential in the anaerobic zone greater than about -150 mv. Incomplete denitrification of in the anoxic zone could also adversely affect anaerobic zone oxygen reduction potential due to the recycle of nitrate from the anoxic to the anaerobic zone by the anaerobic recycle. In this regard, the anaerobic zone hydraulic residence time did not appear to affect phosphorus removal over the range of approximately 0.7 to 2.4 hours.
Tables 5 and 6 also illustrate the significant differences in phosphorous removal capability between the process according to U.S. Pat. No. 4,056,465 (Phase VI of the pilot plant program) and the process according to the present invention. For example, Table 5 under the column "SVI" shows improved settling characteristics of the sludge during phase VI. However, Table 6 also shows the significantly reduced phosphorous removal capabilities of the '465 process during periods of increased phosphorous loading (compare the removed phosphorous levels during phases V-C and V-CS with the levels in phases VI-B and VI-BS). Likewise, FIG. 4 of the drawings compares the overall phosphorous removal capabilities of the present invention to the process disclosed in U.S. Pat. No. 4,056,465 and a third conventional system using the '465 process over a longer period of time. FIG. 4 plots the data for each of the phases (except for Phases III-A and III-B, when poor phosphorous removal was observed due to underloading problems), as well as data from a recently completed biological phosphorous removal and nitrification pilot plant study using the U.S. Pat. No. 4,056,465 process. The latter study was conducted at the City of Fayetteville, Ark., Wastewater Treatment Plant. The results of this comparison indicate excellent phosphorous removal capability for the pilot plant using the process according to the invention and suggest a potential higher phosphorous removal capability for waste water characteristics typically considered unsuitable for biological phosphorous removal.
Claims
What is claimed is:
1. In a biological waste water treatment process, a method for removing organic matter, phosphorus and nitrogen from influent waste water comprising the steps of: (a) introducing influent waste water to an upstream-most one of an anaerobic reactor in an anaerobic zone which includes multiple serially fluid-connected one of said anaerobic reactors; (b) introducing effluent from a downstream-most one of said anaerobic reactors in said anaerobic zone to an upstream-most one of an anoxic reactor which is serially fluid-connected to other downstream anoxic reactors; (c) introducing the effluent from a downstream-most one of said anoxic rectors in said anoxic zone to a downstream aerobic zone which includes multiple serially fluid-connected aerobic reactors in which dissolved oxygen is brought into contact with said anoxic zone effluent to produce a nitrified mixed liquor and wherein an upstream one of said anoxic reactors has a hydraulic residence time which is substantially equal to the hydraulic residence time of another downstream one of said anoxic reactors; (d) separating the effluent from said aerobic zone into a layer of activated sludge and a clarified supernatant having reduced levels of nitrogen and phosphorus; (e) recycling a portion of said activated sludge to the process stream entering said upstream-most one of said anoxic reactors in said anoxic zone; (f) removing a portion of said activated sludge as waste; (g) recycling to said upstream-most one of said anaerobic reactors a portion of said anoxic zone effluent from at least said downstream-most one of said anoxic reactors; and (h) recycling to said upstream-most one of said anoxic reactors said nitrified mixed liquor produced in said aerobic zone.
2. A process according to claim 1, wherein said effluent from said downstream-most one of said anoxic reactors in said anoxic zone is introduced into said upstream-most aerobic reactor and thereafter into each of said serially fluid-connected downstream aerobic reactors.
3. A process according to claim 1, wherein the time required to complete steps (a), (b), (c) and (d) define a mean cell residence time of about six days for process temperatures of 20.degree. C. or higher.
4. A process according to claim 1, wherein the time required to complete steps (a), (b), (c) and (d) define a mean cell residence time of about 12 days for process temperatures of between 10.degree. and 20.degree. C.
5. A process according to claim 1 further comprising the step of substantially denitrifying the liquor in said anoxic zone to reduce the recycle of nitrate from said anoxic zone to said anaerobic zone.
6. A process according to claim 1 wherein said aerobic zone accumulates quantities of phosphorus in excess of that required for cell growth and reproduction of microorganisms in said waste water;
7. A process according to claim 1, wherein said anoxic zone denitrifies said waste water thereby releasing nitrogen gas;
8. A process according to claim 1, wherein said step (a) further comprises the step of maintaining biological solids in suspension in said anaerobic zone.
9. A process according to claim 1, wherein the flow rate of said recycled portion of said anoxic zone effluent in step (g) is about 0.5 to 2.0 times the flow rate of said influent waste water.
10. A process according to claim 1, wherein the hydraulic residence time for step anoxic zone is about 0.5 to 2.0 hours.
11. A process according to claim 1, wherein the flow rate of said recycling activated sludge in step (e) to said anoxic zone is about 0.5 to 2.0 times the flow rate of said influent waste water.
12. A process according to claim 1, wherein the flow rate of said recycled nitrified mixed liquor from said aerobic zone is less than about four times the flow rate of said influent waste water.
13. A process according to claim 1, wherein the concentration of dissolved oxygen in said aerobic zone is at least 0.5 mg/l.
14. A process according to claim 1, wherein the hydraulic residence time for said anaerobic zone is about 0.5 to 2.0 hours.