WO1988008410A1 - Procede de traitement d'eaux usees biologiques a taux eleve utilisant le recyclage de boues activees - Google Patents

Procede de traitement d'eaux usees biologiques a taux eleve utilisant le recyclage de boues activees Download PDF

Info

Publication number
WO1988008410A1
WO1988008410A1 PCT/US1988/001317 US8801317W WO8808410A1 WO 1988008410 A1 WO1988008410 A1 WO 1988008410A1 US 8801317 W US8801317 W US 8801317W WO 8808410 A1 WO8808410 A1 WO 8808410A1
Authority
WO
WIPO (PCT)
Prior art keywords
waste water
zone
anoxic
anaerobic
process according
Prior art date
Application number
PCT/US1988/001317
Other languages
English (en)
Inventor
Glen T. Daigger
James R. Borberg
Liliana M. Morales
Original Assignee
Hampton Roads Sanitation District
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hampton Roads Sanitation District filed Critical Hampton Roads Sanitation District
Publication of WO1988008410A1 publication Critical patent/WO1988008410A1/fr
Priority to KR1019890701582A priority Critical patent/KR920002164B1/ko

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1205—Particular type of activated sludge processes
    • C02F3/1215—Combinations of activated sludge treatment with precipitation, flocculation, coagulation and separation of phosphates
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/308—Biological phosphorus removal
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the present invention relates to improvements in the treatment of municipal and industrial waste water using activated sludge and, in particular, to an improved treatment process for removing organic matter (generally expressed as BOD), as well as phosphorous and nitrogen nutrients at a high rate from waste water using an activated sludge recycle.
  • organic matter generally expressed as BOD
  • phosphorous and nitrogen nutrients at a high rate from waste water using an activated sludge recycle.
  • the activated sludge process has proven to be an effective means for removal of biological oxygen demand (BOD) from waste water and for producing high quality effluent with reduced total suspended solids concentrations.
  • BOD biological oxygen demand
  • the process has been extensively described in the literature and, in general, includes the steps of maintaining an aeration system in which the waste water is fed to a suspension of microorganisms which are responsible for removing excess bacteria and producing a clarified effluent.
  • bacteria cannot metabolize solid organics, they convert certain solid particles to soluble organics prior to metabolism by virtue of enzymes on the cell surface capable of hydrolizing the complex organics to simple organic molecules. It is known that the bacteria must have a suitable environment with all of the proper nutrients. The environment must also provide good mixing for adequate contact 'between the microorganisms and the pollutants being metabolized and may involve an aerobic system with excess dissolved oxygen or an anaerobic system without dissolved oxygen. In either case, the known activated sludge processes require sufficient nitrogen, phosphorous, iron and trace metals for good growth of the microorganisms, without high concentrations of heavy metals.
  • filamentous microbes which adversely effect sedimentation.
  • filamentous bacteria can predominate over normal bacteria.
  • the proliferation of filamentous species which do not settle adequately in the clarifier produce a filamentous biomass which is difficult and expensive to separate from the treated waste water.
  • UCT process Another recent development, known as the UCT process, was developed by the University of Cape Town during the mid-1980's and discloses the recycle of activated sludge to the anoxic zone of the system, together with a recycle of nitrified recycle to the anoxic zone and a third recycle from the anoxic zone itself to the anaerobic zone.
  • the superior performance achieved by the process according to the invention results from two critical improvements over the known activated sludge methods.
  • the present invention uses a unique multi-stage reactor configuration for the anaerobic, anoxic, and aerobic zones.
  • the process operates in a very high-rate mode, i.e., with much lower hydraulic residence times and far greater throughput than conventional systems.
  • the use of a multi-stage reactor configuration in accordance with the invention takes advantage of the inherent kinetics of phosphorus removing bacteria In the anaerobic zone the phosphorus removing bacteria remove soluble organics from the influent waste water. Because the uptake rates are a function of the concentration of organics, the rates become accelerated by using a series of small, complete mixed reactors, rather than a single, large mixed reactor. Thus, the overall rate of phosphorous uptake is accelerated because the concentration of residual organics remains relatively high in the first few reactors. As detailed below, the observed results show extremely high rates of organic matter uptake which, in the anaerobic zone, correspond to high phosphorus release.
  • the staging in accordance with the present invention is a significant factor in the anoxic zone, but for a different reason.
  • the objective is to obtain complete denitrification so that essentially no nitrate is recycled to the anaerobic zone through the anoxic recycle.
  • the unique staging and use of recycle according to the invention helps to accomplish that desired result -because most of the denitrification occurs in the first stage of the anoxic zone. Thus, little nitrate passes into the last stage of the anoxic zone, and even less into the anaerobic zone.
  • the high throughput of treated effluent in the process according to the invention maximizes the phosphorus removal capabilities and results in a system with a much higher proportion of active bacteria (often referred to as "active mass"). Because the biomass is biologically more active, required removal rates may be accomplished using much smaller reactors, thereby substantially reducing the size and cost of an effective .waste water treatment system.
  • active mass active bacteria
  • the observed results according to the invention also suggest fundamental differences in the kinetics of phosphorus removal for high-rate and low-rate processes. It has now been discovered, for example, that phosphorus removal is adversely affected by an aerobic hydraulic residence time greater than 4 hours. Conventional activated sludge processes, particularly the UCT process, would typically use an aerobic hydraulic residence time far greater than 4 hours. The longer residence times lead to lower energy levels in the phosphorus removing organisms and poorer phosphorus removal kinetics and may be caused by overoxidation of stored organic material.
  • Process influent (municipal waste water which may or may not have received primary treatment) enters an initial anaerobic reactor zone with mixing (but with no aeration) to maintain biological solids in suspension.
  • Denitrified mixed liquor from the downstream anoxic reactor zone is added to this initial zone, typically at a flow rate of 0.5 to two times the waste water influent flow rate.
  • the anaerobic reactor zone contains microorganisms capable of accumulating quantities of phosphorous in excess of that required for simple cell growth and reproduction.
  • the hydraulic residence time in this zone is typically 0.5 to 2 hours.
  • the combined waste water and denitrified mixed liquor flows to a downstream anoxic reactor zone which is also mixed but not aerated.
  • Settled sludge (return activated sludge) from the clarifier and nitrified mixed liquor from the downstream aerobic zone are also added to this zone.
  • nitrate-nitrogen contained in the return activated sludge and nitrified mixed liquor serve as a terminal electron acceptor for denitrifying microorganisms and is converted to nitrogen gas. This gas is released to the atmosphere in the anoxic reactor zone and in the downstream aerobic zone, thereby resulting in nitrogen removal.
  • Return activated sludge flow rates typically range from 0.5 to 2 times the influent waste water flow.
  • Nitrified recycle rates vary depending on the degree of nitrogen removal desired, although they seldom exceed 4 times the influent waste water flow.
  • the hydraulic residence time in the anoxic reactor zone is typically 0.5 to 2 hours.
  • the effluent from the anoxic zone then flows to the aerobic reactor zone.
  • Dissolved oxygen is added by mechanical and/or compressed air diffusion means to maintain a residual dissolved oxygen concentration of 0.5 mg/l or ore .
  • nitrifying organisms convert ammonia-and organic-nitrogen originally present in the influent waste water to nitrate-nitrogen. Uptake of residual organic matter and phosphorus also occurs in this zone.
  • effluent from the aerobic zone flows to the clarifier where the biological solids settle, a portion of which may be returned to the biological process leaving a clear supernatant with reduced levels of organic matter, phosphorus, and nitrogen. This supernatant is removed and becomes the process effluent.
  • Phosphorous removal occurs due to removal of excess sludge (waste activated sludge) produced in the process which can be removed either from the clarifier underflow, as shown in the accompanying Figures, or as mixed liquor directly from the biological reactor.
  • the mixing pattern in the various reactor zones represent some degree of plug flow as characterized by a sequence of complete mix reactors.
  • the reactor zones may be physically separate structures, or segments within a single structure.
  • the process according to the present invention varies from the prior art processes in two important respects.
  • Second, the present invention does not require the return of settled sludge from the clarifier to an initial anaerobic contact zone, but instead utilizes settled sludge in recycle to the anoxic zone. Theoretically, this recycle could compromise sludge settling characteristics. However, it has been found that it actually optimizes phosphorus removal due to the nitrate recycle to the anaerobic zone which has been minimized.
  • nitrate contained in the activated sludge recycle is added directly to the anaerobic zone.
  • the process according to the invention uses only denitrified mixed liquor added to the anaerobic zone. Nitrate addition to the anaerobic zone is thought to adversely effect phosphorus removal.
  • the recycle produces a consistently good settling sludge and accomplishes superior phosphorus removal in comparison to the prior art waste water treatment processes with a BOD/TPO. ratio of less than 20.
  • the present invention calls for a mean cell residence time (defined as the mass of solids in the biological reactor divided by the mass of solids removed from the process on a daily basis) of approximately six days for reactor temperatures of 20°C or greater and twelve days for reactor temperatures between 10°C and 20°C.
  • a mean cell residence time defined as the mass of solids in the biological reactor divided by the mass of solids removed from the process on a daily basis
  • FIGURE 1 of the drawings is a block flow diagram showing the basic process steps in accordance with the present invention.
  • FIGURE 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
  • FIGURE 3 is a graphical representation of the operating conditions and performance characteristics of a pilot plant study conducted in accordance with the invention.
  • FIGURE 4 is a comparative graphical representation of the effect of waste water TBOD/TPO 4 on effluent soluble phosphate for two prior art systems and the process according to the invention.
  • FIGURE 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 FIGURE 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).
  • 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.
  • the influent flows via line 112 to a series of biological reactors (also shown in detail in FIGURE 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, 123 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.
  • FIGURE 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.
  • flexibility may be provided in the reactor configuration by using interconnecting piping system to vary the number of tanks in service.
  • 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, 12 ⁇ a, 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.
  • FIGURE 1 also illustrates the typical operating mode maintained throughout a normal reaction cycle.
  • 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.
  • the number of cells in service may be varied depending on the desired effect on process performance characteristics.
  • FIGURE 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.
  • FIGURE 2 also illustrates the use of a third anoxic reactor cell 117 (ANX2) during Phase IV-D of the pilot plant program.
  • ANX2 anoxic reactor cell
  • 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 by 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.
  • 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.
  • 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.
  • FIGURE 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 2 /O" mode, i.e., in accordance with the teachings of U.S. Patent No. 4,056,465.
  • 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-3 when the nitrified recycle was reduced to 60% and the return activated sludge increased to 100%.
  • Phase IV-D 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.
  • 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.
  • 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.
  • Phase V-C additional phosphate was added to the pilot plant influent to stress the system.
  • 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.
  • 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- ⁇ 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- ⁇ 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 or chophosphate 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.
  • 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.
  • DO dissolved oxygen
  • 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.
  • TSS total suspended solids
  • Phases III-A, III-B, and III-C apparent negative TSS removal efficiencies were reported. This anomaly was thought to result from sampling problems.
  • 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.
  • 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- ⁇ 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/PO4 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.
  • anaerobic effluent, anoxic effluent, and aerobic effluent samples were collected directly from the last cell of the respective reactor zones.
  • 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°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.
  • Effluent soluble (0.45- ⁇ membrane filter) BOD 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.
  • Tables 5 and 6 also illustrate the significant differences in phosphorous removal capability between the process according to U.S. Patent No. 4,056,465 (Phase VI of the pilot plant program) and the process according to the present invention.
  • Table 5 under the column "SVI" shows improved settling characteristics of the sludge during phase VI.
  • 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).
  • FIGURE 4 of the drawings compares the overall phosphorous removal capabilities of the present invention to the process disclosed in U.S. Patent No.
  • FIGURE 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. Patent No. 4,056,465 process. The latter study was conducted at the City of Fayetteville, Arkansas, 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.

Landscapes

  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Molecular Biology (AREA)
  • Analytical Chemistry (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

Un procédé de traitement (100) d'eaux usées biologiques à taux élevé pour extraire les matières organiques, les substances nutritives à base d'azote et de phosphore d'eaux usées publiques consiste à mélanger un courant d'arrivée d'eaux usées dans une zone de réaction anaérobie initiale (113-115) pour maintenir les solvants biologiques en suspension avec une liqueur mélangée dénitrifiée provenant d'une zone de réaction anoxique aval (116-118), en général à un débit compris entre 0,5 et deux fois le débit de l'eau usée. La zone de réaction (119-124) sert à sélectionner les micro-organismes pouvant accumuler des quantités de phosphore en excès par rapport aux quantités requises pour une reproduction et une croissance cellulaire simple. L'extraction du phosphore s'effectue en enlevant l'excès de boue (boue activée par les déchets) produite dans le procédé (100), cette boue pouvant être extraite d'un courant de fond clarificateur (125) ou sous la forme d'une liqueur mélangée directement du réacteur biologique (127).
PCT/US1988/001317 1987-04-21 1988-04-21 Procede de traitement d'eaux usees biologiques a taux eleve utilisant le recyclage de boues activees WO1988008410A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
KR1019890701582A KR920002164B1 (ko) 1987-12-25 1988-12-23 당뇨병의 치료제

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US4082687A 1987-04-21 1987-04-21
US040,826 1987-04-21

Publications (1)

Publication Number Publication Date
WO1988008410A1 true WO1988008410A1 (fr) 1988-11-03

Family

ID=21913189

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1988/001317 WO1988008410A1 (fr) 1987-04-21 1988-04-21 Procede de traitement d'eaux usees biologiques a taux eleve utilisant le recyclage de boues activees

Country Status (2)

Country Link
AU (1) AU1707288A (fr)
WO (1) WO1988008410A1 (fr)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1990015029A1 (fr) * 1989-06-01 1990-12-13 Commonwealth Scientific And Industrial Research Organisation Traitement des eaux usees
US5013441A (en) * 1988-07-20 1991-05-07 Goronszy Mervyn C Biological nutrient removal with sludge bulking control in a batch activated sludge system
WO1993004990A1 (fr) * 1991-09-09 1993-03-18 I. Krüger Systems As Procede et systeme de retrait biologique de l'azote des eaux usees
WO1993013023A1 (fr) * 1991-12-23 1993-07-08 I. Krüger Systems As Procede d'epuration d'eaux polluees
US5254254A (en) * 1991-01-26 1993-10-19 Korea Advanced Institute Of Science And Technology Biological method of treating wastewater in batch with porous biomass carrier
WO1997033835A2 (fr) * 1996-03-14 1997-09-18 Deep Shaft Technology Inc. Elimination des substances nutritives biodegradables d'un effluent
ES2128250A1 (es) * 1996-12-27 1999-05-01 Infilco Espanola S A Sistema de eliminacion biologica de nitrogeno y fosforo en un proceso que utiliza fangos activos.
EP2808305A1 (fr) * 2013-05-27 2014-12-03 Jerzy Slusarczyk Procédé de traitement biologique de l'eau usée
WO2015070512A1 (fr) * 2013-11-15 2015-05-21 玉溪师范学院 Réacteur de traitement d'eaux usées d-a2/o ayant deux séries d'opérations alternées anaérobie/anoxique
EP3456408A1 (fr) * 2017-09-13 2019-03-20 Depuracion Biologica Y Bacteriologica de Aguas Residuales, S.L. Installation de purification de boues
WO2023146505A3 (fr) * 2022-01-27 2023-08-31 Yildiz Teknik Universitesi Doner Sermaye Isletme Mud Système et procédé de traitement d'eaux usées et d'élimination de nutriments

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1994011313A1 (fr) * 1992-11-06 1994-05-26 THE MINISTER FOR PUBLIC WORKS for and on behalf ofTHE STATE OF NEW SOUTH WALES Elimination biologique du phosphore des eaux usees

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3994802A (en) * 1975-04-16 1976-11-30 Air Products And Chemicals, Inc. Removal of BOD and nitrogenous pollutants from wastewaters
US4056465A (en) * 1976-04-12 1977-11-01 Air Products And Chemicals, Inc. Production of non-bulking activated sludge
US4162153A (en) * 1976-04-12 1979-07-24 Air Products And Chemicals, Inc. High nitrogen and phosphorous content biomass produced by treatment of a BOD-containing material

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3994802A (en) * 1975-04-16 1976-11-30 Air Products And Chemicals, Inc. Removal of BOD and nitrogenous pollutants from wastewaters
US4056465A (en) * 1976-04-12 1977-11-01 Air Products And Chemicals, Inc. Production of non-bulking activated sludge
US4162153A (en) * 1976-04-12 1979-07-24 Air Products And Chemicals, Inc. High nitrogen and phosphorous content biomass produced by treatment of a BOD-containing material

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"THEORY, DESIGN AND OPERATION OF NUTRIENT REMOVAL ACTIVATED SLUDGE PROCESSES", prepared by the University of Cape Town, City Council of Johannesburg, and the National Institute for Water Research of the CSIR. Pretoria, South Africa, 1984. See pages 7-2, 7-15, 7-20 and 7-21. *

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5013441A (en) * 1988-07-20 1991-05-07 Goronszy Mervyn C Biological nutrient removal with sludge bulking control in a batch activated sludge system
WO1990015029A1 (fr) * 1989-06-01 1990-12-13 Commonwealth Scientific And Industrial Research Organisation Traitement des eaux usees
US5254254A (en) * 1991-01-26 1993-10-19 Korea Advanced Institute Of Science And Technology Biological method of treating wastewater in batch with porous biomass carrier
WO1993004990A1 (fr) * 1991-09-09 1993-03-18 I. Krüger Systems As Procede et systeme de retrait biologique de l'azote des eaux usees
WO1993013023A1 (fr) * 1991-12-23 1993-07-08 I. Krüger Systems As Procede d'epuration d'eaux polluees
WO1997033835A3 (fr) * 1996-03-14 1997-11-06 Deep Shaft Tech Inc Elimination des substances nutritives biodegradables d'un effluent
WO1997033835A2 (fr) * 1996-03-14 1997-09-18 Deep Shaft Technology Inc. Elimination des substances nutritives biodegradables d'un effluent
ES2128250A1 (es) * 1996-12-27 1999-05-01 Infilco Espanola S A Sistema de eliminacion biologica de nitrogeno y fosforo en un proceso que utiliza fangos activos.
EP2808305A1 (fr) * 2013-05-27 2014-12-03 Jerzy Slusarczyk Procédé de traitement biologique de l'eau usée
WO2014191345A1 (fr) * 2013-05-27 2014-12-04 Jerzy Slusarczyk Procédé de traitement biologique des eaux usées
AU2014273259B2 (en) * 2013-05-27 2018-11-08 Jerzy Slusarczyk Method of biological wastewater treatment
WO2015070512A1 (fr) * 2013-11-15 2015-05-21 玉溪师范学院 Réacteur de traitement d'eaux usées d-a2/o ayant deux séries d'opérations alternées anaérobie/anoxique
EP3456408A1 (fr) * 2017-09-13 2019-03-20 Depuracion Biologica Y Bacteriologica de Aguas Residuales, S.L. Installation de purification de boues
WO2023146505A3 (fr) * 2022-01-27 2023-08-31 Yildiz Teknik Universitesi Doner Sermaye Isletme Mud Système et procédé de traitement d'eaux usées et d'élimination de nutriments

Also Published As

Publication number Publication date
AU1707288A (en) 1988-12-02

Similar Documents

Publication Publication Date Title
US4867883A (en) High-rate biological waste water treatment process using activated sludge recycle
US5480548A (en) Wastewater biological phosphorus removal process
US5601719A (en) Biological nutrient removal process for treatment of wastewater
EP0603316B1 (fr) Procede et systeme de retrait biologique de l'azote des eaux usees
AU2007238520B2 (en) Method and system for nitrifying and denitrifying wastewater
US6485645B1 (en) Biological process for removing phosphorus involving a membrane filter
US6406629B1 (en) Biological process for removing phosphorous involving a membrane filter
US6562237B1 (en) Biological nutrient removal using the olaopa process
US5650069A (en) Dual-stage biological process for removing nitrogen from wastewater
US6163932A (en) Process, using ammonia rich water for the selection and enrichment of nitrifying micro-organisms for nitrification of wastewater
US5811009A (en) Method and system for improved biological nitrification of wastewater at low temperature
WO2004002904A1 (fr) Procede et reacteur biologique sequentiel combine pour les boues activees-films biologiques
Barnard Biological nutrient removal: Where we have been, where we are going?
CN1102130C (zh) 生物除去污水和废水中的氮和磷的系统和方法
US5536407A (en) Nitrification and denitrification wastewater treatment process
WO1988008410A1 (fr) Procede de traitement d'eaux usees biologiques a taux eleve utilisant le recyclage de boues activees
Subramaniam et al. Efficient biological nutrient removal in high strength wastewater using combined anaerobic-sequencing batch reactor treatment
KR100430382B1 (ko) 고농도 유기물, 질소, 인 함유 축산폐수의 처리 방법 및 그에 사용되는 처리 시스템
Wang et al. Simultaneous nitrification and de-nitrification in MBR
CA2314383A1 (fr) Procede biologique d'enlevement du phosphore comprenant une membrane filtrante
GB2228930A (en) Removal of nitrogen and phosphorus from sewage
Cheng et al. Enhanced biodegradation of organic nitrogenous compounds in resin manufacturing wastewater by anoxic denitrification and oxic nitrification process
Yang et al. Nitrification and denitrification in the wastewater treatment system
KR100420647B1 (ko) 연속 유입 회분식 오폐수 처리방법
KR20010076873A (ko) 혐기-호기-무산소 시스템을 이용한 침출수의 고농도유기물 및 질소 제거 방법

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AU BR JP KR

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE BJ CF CG CH CM DE FR GA GB IT LU ML MR NL SE SN TD TG