WO2000037369A1 - Bioreacteur a membrane immerge destine au traitement d'eau contenant de l'azote - Google Patents

Bioreacteur a membrane immerge destine au traitement d'eau contenant de l'azote Download PDF

Info

Publication number
WO2000037369A1
WO2000037369A1 PCT/CA1999/001205 CA9901205W WO0037369A1 WO 2000037369 A1 WO2000037369 A1 WO 2000037369A1 CA 9901205 W CA9901205 W CA 9901205W WO 0037369 A1 WO0037369 A1 WO 0037369A1
Authority
WO
WIPO (PCT)
Prior art keywords
mixed liquor
membranes
tank
time
bioreactor
Prior art date
Application number
PCT/CA1999/001205
Other languages
English (en)
Inventor
Henry Behmann
Hidayat Husain
Hervé BUISSON
Michele Payraudeau
Original Assignee
Zenon Environmental Inc.
Omnium De Traitement Et De Valorisation
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 Zenon Environmental Inc., Omnium De Traitement Et De Valorisation filed Critical Zenon Environmental Inc.
Priority to AU17639/00A priority Critical patent/AU766535B2/en
Priority to CA 2355087 priority patent/CA2355087A1/fr
Priority to US09/856,504 priority patent/US6616843B1/en
Priority to EP19990960738 priority patent/EP1140706A1/fr
Publication of WO2000037369A1 publication Critical patent/WO2000037369A1/fr

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
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • C02F3/1273—Submerged membrane bioreactors
    • 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
    • C02F3/006—Regulation methods for biological treatment
    • 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
    • C02F3/20—Activated sludge processes using diffusers
    • 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
    • C02F3/22—Activated sludge processes using circulation pipes
    • C02F3/223—Activated sludge processes using circulation pipes using "air-lift"
    • 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
    • C02F3/301—Aerobic and anaerobic treatment in the same reactor
    • 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
    • C02F3/302—Nitrification and denitrification treatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/005—Processes using a programmable logic controller [PLC]
    • C02F2209/006—Processes using a programmable logic controller [PLC] comprising a software program or a logic diagram
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/04—Oxidation reduction potential [ORP]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/14—NH3-N
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/15—N03-N
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/22—O2
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/44—Time
    • 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

  • This invention relates to a process and apparatus for treating municipal, industrial, agricultural or other wastewater feeds in a submerged membrane bioreactor. Specifically, the invention concerns the removal of ammonia and total nitrogen in a single tank submerged membrane bioreactor through the processes of nitrification and denitrification.
  • Excessive nitrogen is often introduced into the environment through the discharge of municipal, industrial, agricultural and other wastewaters.
  • Such wastewater feeds contain organic nitrogen primarily in the form of proteins and ammonia.
  • ammonia and other sources of total nitrogen are partially oxidized to produce nitrites and nitrates which can be hazardous to the environment.
  • discharging excessive amounts of total nitrogen into rivers and lakes contributes to their eutrophication which is characterized by frequent algal blooms and reduced levels of free oxygen available to plants and fish.
  • Recently, many jurisdictions have started to regulate the amounts of total nitrogen and ammonia that may be discharged from wastewater treatment plants.
  • bacteria in a bioreactor are used to alternately nitrify and denitrify the water.
  • a two step process converts ammonia into nitrites and nitrates.
  • bacteria primarily of the genus Nitrosomonas oxidize the ammonia and convert it to nitrite.
  • bacteria primarily of the genus Nitrobacter oxidize the nitrite and convert it to nitrate. Since oxidation occurs in both steps of the nitrification process, an aerobic environment is required.
  • nitrate is converted to ammonia and nitrogen gas by other bacteria (which could include the bacteria mentioned above after they have switched functions) and fungi which remove oxygen from the nitrate.
  • Anoxic conditions are needed to encourage the growth of such bacteria.
  • the nitrogen gas leaves the process and joins the atmosphere and the ammonia is treated by further nitrification and denitrification steps.
  • nitrogen By cycling back and forth between nitrification and denitrification steps, or aerobic and anoxic conditions in the bioreactor, nitrogen continuously leaves the water reducing the levels of total nitrogen and ammonia in the wastewater.
  • a membrane bioreactor typically comprises a plurality of ultraporous or microporous membranes submerged in a tank of wastewater with suction applied to one side of the membranes. Clean water permeates through the membrane walls but bacteria and suspended solids are rejected by the membranes and remain in the tank to be biologically treated. To prevent pollutants in the tank from rapidly fouling the pores of the membranes, the membranes are typically kept awash in air bubbles. Without aeration, the membranes would quickly foul and lose their permeability, but the aeration prevents anoxic conditions and denitrification from occurring in the membrane bioreactor.
  • Multistage systems have been used to provide both aerobic and anoxic conditions for nitrogen treatment.
  • an aerated membrane bioreactor is used to provide an aerobic environment suitable for digesting BOD and nitrifying ammonia.
  • a second bioreactor, without a membrane, provides an anoxic environment for denitrifcation and partially treated wastewater (mixed liquor) continually flows between the two tanks.
  • Nitrogen has also been treated in commercial applications in a single tank membrane bioreactor where the oxygen content in the bioreactor is varied to produce alternating aerobic and anoxic conditions.
  • permeation through the membranes typically stops during the anoxic phase to avoid membrane fouling in the absence of membrane aeration.
  • the loss of permeation during the anoxic phase significantly reduces the daily yield of filtered permeate through the membranes and is a disadvantage of these systems.
  • Japanese Patent Application No. HE I 5-220346 discusses a system combining the single tank and multistage systems described above.
  • the system has an anoxic tank for denitrification and a membrane bioreactor for nitrification and digesting BOD with mixed liquor recirculating between them. Filtered effluent is permeated through submerged membranes filters in the membrane bioreactor. If the rate of denitrification in the anoxic tank is insufficient, the air supply to the membrane bioreactor is discontinued, to bring the tank into anoxic conditions. However, when the air supply to the membrane bioreactor is disconnected, permeation through the submerged membrane filter is also stopped to prevent membrane fouling. Again the average yield of the system is compromised.
  • Japanese Patent Application HI 6-181645 describes a single tank membrane bioreactor for treating nitrogen which is cycled between aerobic and anoxic conditions by alternately turning an air supply to the membranes off and on.
  • an attempt was made to continue to permeate effluent through the membranes during the anoxic phase.
  • Each anoxic phase was started with a minimum level of mixed liquor in the bioreactor and the level of mixed liquor was allowed to rise to a maximum level by the end of the anoxic phase so that a reduced amount of permeate could be withdrawn during the anoxic phase.
  • the yield of the system was reduced because permeate was not withdrawn at the full rate during the anoxic phase and yet it was found that the membranes still fouled quickly.
  • the present invention is directed at an apparatus for treating feed water with pollutants containing nitrogen in a bioreactor having:
  • the invention is further directed at a process wherein the membrane scouring bubble supply, located below the membrane or membranes, continuously provides large scouring bubbles to clean the membranes.
  • Treated water is permeated through the membranes continuously at a high rate of yield but the large bubbles do not transfer sufficient oxygen to the feed water to create aerobic conditions throughout the reactor.
  • the large scouring bubbles create an airlift effect which causes a recirculation pattern in the mixed liquor but oxygen is depleted from the mixed liquor or diluted as the mixed liquor travels away from the membranes.
  • the concentration of dissolved oxygen is reduced in a region below or adjacent to the bottom of the membranes, and at least this region is anoxic when air is supplied by the scouring bubbles alone. If necessary, the large scouring bubbles are captured in a hood after they have scoured the membranes to provide an oxygen lean source of further scouring bubbles.
  • the oxygenating bubble supply is operated intermittently and provides small bubbles of air or oxygen to intermittently produce aerobic conditions in at least part of the tank.
  • Minimum and maximum periods of aeration and non-aeration through the oxygenating bubble supply are preselected but the level of dissolved oxygen (DO) or oxygen reduction potential (ORP) in the tank is measured by sensors and assists in controlling the aerating bubble supply.
  • DO dissolved oxygen
  • ORP oxygen reduction potential
  • a period of aeration is terminated if it is within the time limits and the level of DO or ORP in the tank exceeds a maximum value and a period of non-aeration is terminated if it is within the time limits and the level of DO or ORP in the tank drops below a minimum value.
  • Figure 1 is a representation of an apparatus according to an embodiment of the invention.
  • Figure 2 is a flow chart showing a method of controlling the apparatus according to an embodiment of the invention.
  • FIGS 3, 4 and 5 are graphs showing the results of experiments conducted with an embodiment of the invention.
  • Figures 6 and 7 are graphs showing the results of experiments conducted with another embodiment of the invention.
  • FIGS 8, 9, 10 and 11 are graphs showing the results of experiments conducted with another embodiment of the invention.
  • the reactor 10 has a tank 12 which is initially filled with feed water 13 through an inlet 42 and a feed valve 40.
  • the feed water 13 is typically propelled to the tank 12 from a reservoir not illustrated through a screened grinder pump also not illustrated, although the feed water 13 may also be delivered to the tank 12 by gravity flow depending on the arrangement of the treatment plant.
  • biological processes alter the feed water 13 and it is referred to as mixed liquor 15.
  • a membrane module 16 mounted in the tank 12 has upper and lower headers 18 in fluid communication with the lumens 20 of hollow-fibre membranes 22.
  • the tank 12 is kept filled with mixed liquor 15 to a water level 14 which is above the level of membranes 22 by controlling feed valve 40 to add feed water 13 as necessary.
  • the membranes 22 preferably have an average pore size between 0.01 microns and 10 microns and more preferably have an average pore size between 0.02 microns and 1 micron.
  • Suitable membranes include those manufactured by Zenon Environmental Inc. and sold under the ZEEWEED trade mark but other submerged outside-in membranes may be used such as those manufactured by Mitsubishi Rayon or Kubota.
  • the membrane module 16 is preferably placed in the tank 12 at least 15 cm and less than 4.5 m, and more typically between 0.3 m and 1.3 m, from the bottom of the tank 12 to allow fluid to reach the bottom of the membrane module 16.
  • the membrane modules 16 may be located in the middle of the tank 12 or along one wall of the tank 12.
  • Water is permeated continuously through a permeate line 24 joining a permeate pump 23 to the headers 18. Suction created by the permeate pump 23 creates a transmembrane pressure across the walls of the membranes 22.
  • the membranes 22 reject bacteria or suspended solids but allow filtered permeate 26 to permeate through the walls of the membranes 22 from a first side, the outsides, to a second side, the lumens 20.
  • the filtered permeate 26 is stored in a permeate tank 28 and later released through a permeate outlet 27.
  • a backwash pump 29 is used to periodically pump permeate 26 back through the membranes 22 in a reverse direction for additional cleaning but the time required for such backwashing is minimal and the process is still considered to be continuous.
  • a scouring bubble supply 30 has a membrane aerator 31, a membrane air pump 34 and a membrane air line 36.
  • the membrane aerator 31 is located below and in close proximity to the membrane module 16 and delivers scouring bubbles 32 to the membrane module 16.
  • the scouring bubbles 32 are preferably made of air and more preferably of oxygen depleted air supplied from the membrane air pump 34 through the membrane air line 36.
  • the scouring bubbles 32 rise upwards through the membrane module 16 and inhibit fouling of the membranes 22.
  • the scouring bubbles 32 also create an air lift which mixes and recirculates the mixed liquor 15.
  • the scouring bubbles 32 have an average diameter preferably between 5 mm and 20 mm. At this size, the scouring bubbles 32 flow rapidly through the membranes 22 to provide effective cleaning but little time for oxygen to be transferred to the mixed liquor 15. Large scouring bubbles 32 have a reduced ratio of surface area to volume compared to small bubbles which further inhibits oxygen transfer. In addition, large scouring bubbles 32 tend to reach the surface of the mixed liquor 15 and burst whereas smaller bubbles more often become entrained in the recirculating mixed liquor 15.
  • a bubble collector 37 located above the membrane module 16 and connected to the membrane air pump 34 through a gas line 38 collects scouring bubbles 32 for reuse.
  • the re-used scouring bubbles 32 have reduced oxygen content. Under the influence of the scouring bubbles alone, the mixed liquor 15 is maintained under anoxic conditions throughout most of the tank 12, which enables appropriate bacteria to grow to cause denitrification of the mixed liquor 15. It is not necessary that all parts of the tank 12 be anoxic for sufficient denitrification to occur.
  • the scouring bubbles 32 create an airlift effect which causes the mixed liquor to move in a recirculation pattern 100 in the tank 12. As the mixed liquor 15 moves away from the membrane module 16, dissolved oxygen is depleted and diluted so that the concentration of dissolved oxygen in the mixed liquor 15 is reduced.
  • the mixed liquor 15 is anoxic when air is supplied by the scouring bubbles alone.
  • This anoxic region typically occurs below or adjacent to the bottom of the membrane module 16, but may also extend upwards to an area beside the membrane module 16.
  • the area immediately surrounding the membrane module 16 is less likely to be anoxic than other parts of the tank 12 but is sufficiently small that the supply of scouring bubbles 32 need not be compromised to produce anoxic conditions there.
  • a typical flux of air for scouring bubbles may be between 0.8 and 2.1 m 3 /h (at standard temperature and pressure) per square metre of membrane surface area. Using the techniques described below if necessary, it is not typically necessary to depart significantly from typical ranges of scouring air flux.
  • Anoxic conditions occur when there is less than 0.5 mg/L of dissolved oxygen (DO) in the mixed liquor 15.
  • DO dissolved oxygen
  • the calculation of the amount of oxygen that can be added by the scouring bubbles 32 to maintain the desired level of DO concentration will be apparent to those skilled in the art and may vary for different installations.
  • the calculation involves multiplying the volume of the mixed liquor 15 by the desired concentration of DO to get a total permissable amount of oxygen and then comparing oxygen sources, such as oxygen introduced by the feed water 13 or dissolving into the mixed liquor 15 at the top of the tank 12, with oxygen losses such as use by the organisms in the mixed liquor 15 during the anoxic phase.
  • oxygen sources such as oxygen introduced by the feed water 13 or dissolving into the mixed liquor 15 at the top of the tank 12, with oxygen losses such as use by the organisms in the mixed liquor 15 during the anoxic phase.
  • the size and configuration of the tank is effectively used to achieve anoxic conditions despite the scouring bubbles 32.
  • Increasing the total size of the tank 12 provides a greater volume of mixed liquor 15 and thus reduces the increase in concentration of DO which results from oxygen transferred from the scouring bubbles 32.
  • a large tank is more expensive and merely increasing the size of the tank is not preferred.
  • the tank 12 remains within the size range of ordinary membrane bioreactor tanks but the membrane module 16 is placed near the top of the tank 12. Scouring air bubbles 32 largely burst at the surface and infrequently travel to the area beneath the membrane module 16. A deep tank, relative to the height of the membrane module 16, is preferable to maximize this effect.
  • baffles can be provided below the membrane module 16 to partially isolate an area near the bottom of the tank which is minimally effected by the recirculation of mixed liquor in the tank 12 until aerated as will be described further below.
  • the inlet 42 directs the feed water 13 to enter the tank 12 directly over the membrane module 16. Although the inlet 42 may satisfactorily direct the feed water 13 to any other part of the tank 12, by dumping it over the membrane module 16, oxygen is removed from the scouring bubbles 32 and the feed water 13 is partially nitrified even if the mixed liquor 15 is in a substantially anoxic condition.
  • anoxic conditions and denitrification occur in a substantial portion of the mixed liquor 15 when under the influence of scouring bubbles 32 alone.
  • at least a significant part of the mixed liquor 15 must cycle back and forth between anoxic and aerobic conditions so that nitrification can also occur.
  • BOD is partially removed under anoxic conditions but is more quickly removed under aerobic conditions.
  • the reactor 10 has an independent oxygenating bubble supply 47 which can be controlled to produce alternating aerobic and anoxic conditions in at least a significant part of the mixed liquor 15.
  • the oxygenating bubble supply 47 has a process aerator 48 which produces oxygenating bubbles 50 with air or oxygen supplied from a process air pump 52 through a process air line 54.
  • the process aerator 48 is preferably located at the bottom of the tank 12 on the opposite side from the membrane module 16. If the membrane module 16 is located in the centre of the tank 12, then the process aerator 48 is preferably located at the centre of the bottom of the tank 12.
  • Aerobic conditions suitable for nitrification and rapid BOD digestion are achieved in a significant portion of the mixed liquor 15 by turning on the oxygenating bubble supply 47.
  • the mixed liquor is considered to be aerobic when the concentration of DO is greater than 0.5 mg/L although the concentration of DO in an aerobic zone is preferably between 0.5 mg/L and 5.0 mg/L for aerobic digestion and nitrification and more preferably between 0.5 mg/L and 2.5 mg/L.
  • the oxygenating bubbles 50 are preferably small, with an average diameter between 0.5 mm and 5.0 mm, to provide an efficient transfer of oxygen to the mixed liquor 15.
  • the oxygenating bubbles 50 are sufficient in combination with the scouring bubbles 32 (whose supply may be increased in the aerobic phase) to produce aerobic conditions near the membrane module 16 and bottom of the tank 12 but are insufficient to make all regions of the tank 12 become aerobic.
  • the reactor 10 does not cycle completely between aerobic and anoxic conditions, but has an area in or near the centre of the membrane module 16 which is always aerobic and an area near the bottom of the tank 12 which is always anoxic.
  • aerobic and anoxic thus indicate times or places in which the mixed liquor 15 is on average aerobic or anoxic.
  • the average size of the anoxic zone in time and space is preferably larger than the average size of the aerobic zone over the same time and space.
  • At least one sensor 60 is located in the tank 12 and connected to a microprocessor 62 which controls the process air pump 52.
  • a microprocessor 62 which controls the process air pump 52.
  • at least two sensors 60 are used, one above and one below the membrane module 16 so that the change in size of the aerobic and anoxic zones as well as the change in their respective concentration of DO can be monitored.
  • the sensors 60 record the concentration of DO in the mixed liquor 15 directly or, preferably, measure the oxygen reduction potential (ORP) of the mixed liquor 15. ORP is related to the concentration of DO but ORP sensors are more sensitive.
  • a control flow chart is shown which illustrates the process steps accomplished by the microprocessor 62 reading a sensor 60 near the top of the tank 12 in controlling the process air pump 52.
  • the time between the beginning and end of aeration is set between Tlmin and Tlmax.
  • Tlmin is chosen to reflect the minimum amount of time needed to achieve organic carbon and ammonia conversion should the organic load to the bioreactor increase excessively during the present step and is preferably between five minutes and two hours.
  • Tlmax is chosen to limit the maximum aerobic time during low load periods so that adequate anaerobic time occurs and is preferably between ten minutes and eight hours.
  • the microprocessor 62 sets a timer and begins to periodically check the level of ORP in the mixed liquor 15. If at any time greater than Tlmin the microprocessor 62 detects a level of ORP of greater than ORPmax, then the microprocessor ends aeration.
  • ORPmax is between 200 an 250 mV. If Tlmax is reached, the microprocessor also ends aeration. The time between the beginning and end of non-aeration is set between T2min and T2max. T2min is chosen to provide a minimum anoxic time during low load periods and is preferably between five minutes and two hours.
  • T2max is chosen to provide a maximum anoxic time during high load periods and is preferably between ten minutes and eight hours.
  • the microprocessor 62 sets a timer and begins to periodically check the level of ORP in the mixed liquor 15. If at any time greater than T2min the microprocessor 62 detects a level of ORP less than ORPmin, then the microprocessor ends starts aeration.
  • ORPmin is between -50 mV and 50 mV. If T2max is reached, the microprocessor also starts aeration and the cycle is repeated.
  • Tlmin, Tlmax, T2min and T2max obviously relate to each other and so the time given to any one parameter must be reasonable compared to the other parameters. For example, if times at the high end of the acceptable ranges are chosen for Tlmin and Tlmax, then times at the low end of the acceptable ranges should not be chosen for T2min and T2max or the system may be aerobic for too much time in any given period of time. Generally, higher time periods are preferable for systems with a high sludge age or hydraulic retention time and lower time periods are preferable for systems with lower sludge age or hydraulic retention times. Further, in many jurisdictions, limits on ammonia in the permeate are stricter than limits on total nitrogen since ammonia is a toxin.
  • the parameters may be chosen to favour the aerobic part of the cycle as necessary.
  • the minimum and maximum times may be chosen to reflect constraints imposed by system components. For example, Tlmin and T2min may be chosen to be greater than 15 minutes to reduce wear on the process air pump 52 from being switched on and off frequently.
  • the oxygenating bubble supply 47 is preferably controlled so that mixed liquor 15 does not instantaneously change from aerobic to anoxic. The change in concentration of DO in the mixed liquor 15 will naturally lag behind a change in the supply of oxygenating bubbles 50 since it takes time for oxygen to be transferred from bubbles to the mixed liquor 15 and time for the mixed liquor 15 to release or metabolize oxygen when aeration stops.
  • an oxygen uptake rate or outlet rate can be determined. If these rates are insufficient to get the desired time between anoxic and aerobic conditions in the mixed liquor 15, the microprocessor 62 can gradually decrease power to the process air pump 52 at the end of aeration or gradually increase power to the process air pump 52 at the start of aeration as needed. Ideally, there is a sinusoidal variation between anoxic and aerobic conditions, but it is sufficient if the change in concentration of DO occurs smoothly and over the minimum time period described above.
  • an alternate control strategy may be required.
  • highly loaded systems ie. systems with an organic loading greater than 3 kilograms of 5 day BOD per cubic meter per day of feed, may require continuous aeration through the process aerator 48 to avoid anaerobic conditions at the bottom of the tank 12 or may require that the supply of scouring air bubbles 32 be increased during the aerobic phase to provide additional oxygen transfer.
  • the supply of scouring air bubbles 32 may be reduced during the anoxic phase.
  • the bioreactor is operated at a high concentration of MLVSS because it provides a high level of oxygen demand in the anoxic phase and assists in maintaining anoxic conditions despite the presence of scouring bubbles 32.
  • a high concentration of MLVSS also allows a high organic loading capacity of feed and small bioreactor size. Further, a high concentration of MLVSS allows a high population of nitrifying bacteria to be present whereas, in less highly loaded systems, the population of nitrifying bacteria may be unacceptably low at some times.
  • the average concentration of MLVSS ranges from 10 g/1 to 30 g/1 and more preferably from 12 g/1 to 25 g/1.
  • a drain pump 44 connected to a sludge outlet 45 and a drain 46 allows a portion of the mixed liquor 15 to be continuously or intermittently discharged to maintain a desired and substantially constant suspended solids concentration in the mixed liquor 15.
  • the reactor 10 has a minimum hydraulic retention time of 1.5 hours and, more preferably, the hydraulic retention time is between 1.5 hours and 6 hours.
  • the reactor 10 preferably has a minimum mean cell residence time of 7 days and maximum mean cell residence time of 100 days and is preferably operated with a mean cell residence time between 10 days and 30 days for good growth of nitrifiers.
  • the embodiment shown in Figure 1 has two sensors 60, a large tank might have many sensors 60, many process aerators 48 and many membrane aerators 31.
  • the microprocessor would then be used to monitor the concentration of DO or ORP throughout the tank 12 and control each process aerator 48 or membrane aerator 31 to prevent any area of the tank 12 from exceeding the minimum concentration of DO for an anoxic zone or the maximum concentration of DO for an aerobic zone.
  • the microprocessor 62 could create controlled aerobic areas and anoxic areas simultaneously in the mixed liquor 15.
  • Additional inputs to the microprocessor 62 come from an ammonia sensor 70 and a total nitrate sensor 72 in the permeate line 24.
  • the ammonia sensor 70 and total nitrate sensor 72 send signals to the microprocessor 62 indicating the concentration of ammonia and total nitrates in the permeate 26. This information is used to determine when the relative lengths of time for the aerobic or anoxic cycles must be adjusted or when the minimum and maximum oxygen concentration limits at any point in the tank 12 should be adjusted.
  • the maximum DO in the aerobic stage may be reduced or the rate of change between the anoxic and aerobic cycles may be decreased so that the concentration of DO stays closer to a lower, but still aerobic, value for a longer time period.
  • the reverse adjustments may be made.
  • experience in using the reactor will suggest how the microprocessor 62 is best used to control the reactor 10 under varying conditions of feed water 13.
  • a waste feed water treating reactor was constructed and operated according to the description above.
  • the apparatus was operated for 16 hours manually controlling the supply of fine bubbles from a process aerator to achieve average DO concentrations in the mixed liquor ranging from 0.05 mg/L to 0.55 mg/L in the anoxic phase (in various parts of the tank) and between 0.1 mg/L and 1.2 mg/L in the aerobic phase (in various parts of the tank).
  • the tank had a volume of 11,000 L and was outfitted with a module of hollow fiber membranes having 13.9 m 2 of surface area.
  • the reactor had a hydraulic retention time of 3 hours.
  • the average concentration of MLVSS was approximately 20 g/1.
  • the average organic loading of the feed was 1.3 kg of 5 day BOD per cubic metre per day.
  • Figures 3 shows the ammonia levels in the feed and permeate during the experiment and indicates that the reactor was very effective in removing ammonia, particularly when average concentrations are considered as would emerge from a significantly large permeate tank.
  • Figure 4 shows the total nitrogen levels in the feed and permeate during the experiment. The average concentration of total nitrogen remained below 10 mg/L which is the maximum concentration allowed in many jurisdictions.
  • Figure 5 shows the concentration of dissolved oxygen during the experiment and shows that one area of the tank was continuously maintained in an anoxic state while another area of the tank cycled back and forth between anoxic and aerobic states.
  • a second waste feed water treating reactor was constructed and operated according to the description above including a microprocessor used to control the flow of fine air bubbles at the bottom of the tank based on signals received from an ORP sensor at the top of the tank.
  • the tank had a volume of 2.0 m 3 and was outfitted with a module of hollow fiber membranes having 13.9 m 2 of surface area.
  • Figure 6 shows the variation of ORP, concentration of DO and flow rate of aeration to a process aerator in a first trial.
  • ORPmax was 200 mV and ORPmin was near 0 mV.
  • Figure 7 shows the variation of ORP, concentration of DO and flow rate of aeration to a process aerator in a second trial.
  • ORPmax was 250 mV and ORPmin was 50 mV.
  • the concentration of DO at the top of the tank was effectively cycled between a value less than 0.5 mg/L and a value above 0.5 mg/L.
  • the concentration of MLVSS during the trials ranged from 15 g/1 to 20 g/1 and averaged about 18 g/1.
  • the organic loading in the feed varied from about 0.5 kg of 5 day BOD per cubic metre per day to 1.0 kg of 5 day BOD per cubic metre per day.
  • the average concentration of total nitrogen in the permeate was again less than 10 mg/L and both total nitrogen and ammonia removal rates were at least 60%.
  • a third waste water treating reactor was constructed and operated according to the description above, also including a microprocessor used to control the flow of fine air bubbles at the bottom of the tank based on signals received from an ORP sensor at the top of the tank. Except for a brief period noted on the Figures, the feed water had the following characteristics:
  • a module of hollow fibre membranes having 13.9 m 2 of surface area was used with outside/in permeation driven by a vacuum pump.
  • the tank had a volume of 2.0 m3. Permeation was substantially continuous, stopping only for periodic membrane backwashing. Scouring aeration was provided at all times with course bubbles at a rate of 12 m3/h. After a start up period of about one month, mixed liquor was discharged continuously from a drain to produce a sludge age (reactor volume /flux of waste sludge) of 25 days. Feed water was provided as required to keep the membranes immersed. A stirrer at the bottom of the tank was also operated at all times to provide more nearly homogeneous conditions in the tank. Operating conditions in the tank were as follows:

Landscapes

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

Abstract

Un bioréacteur à membrane immergé dans un seul réservoir destiné au traitement d'une eau d'alimentation présentant des niveaux inacceptables d'ammoniaque ou d'azote total présente à la fois une alimentation en bulles de lavage à membrane et une alimentation en bulles d'oxygénation. L'alimentation en bulles de lavage à membrane produit en continu de grosses bulles de lavage afin de nettoyer les membranes. Le perméat est retiré de façon continue des membranes à haut débit mais les grosses bulles de lavage ne transfèrent pas suffisamment d'oxygène dans la liqueur mélangée pour créer des conditions aérobies dans le réacteur. L'alimentation en bulles d'oxygénation est exploitée pour produire des petites bulles d'air ou d'oxygène produisant, de façon intermittente, des conditions aérobies dans une partie significative de la liqueur mélangée. Des conditions aérobies et anoxiques alternées se produisent dans une partie importante du réservoir apte à la nitrification et la dénitrification. Le niveau d'oxygène dissous (OD) ou de potentiel de réduction d'oxygène (PRO) dans le réservoir est mesuré par des détecteurs et il détermine quand l'alimentation en bulles d'oxygénation doit être mise en marche ou coupée entre des limites définies de temps minimum et maximum.
PCT/CA1999/001205 1998-12-18 1999-12-17 Bioreacteur a membrane immerge destine au traitement d'eau contenant de l'azote WO2000037369A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
AU17639/00A AU766535B2 (en) 1998-12-18 1999-12-17 Submerged membrane bioreactor for treatment of nitrogen containing water
CA 2355087 CA2355087A1 (fr) 1998-12-18 1999-12-17 Bioreacteur a membrane immerge destine au traitement d'eau contenant de l'azote
US09/856,504 US6616843B1 (en) 1998-12-18 1999-12-17 Submerged membrane bioreactor for treatment of nitrogen containing water
EP19990960738 EP1140706A1 (fr) 1998-12-18 1999-12-17 Bioreacteur a membrane immerge destine au traitement d'eau contenant de l'azote

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CA2256989 1998-12-18
CA2,256,989 1998-12-18
US11324998P 1998-12-21 1998-12-21
US60/113,249 1998-12-21

Publications (1)

Publication Number Publication Date
WO2000037369A1 true WO2000037369A1 (fr) 2000-06-29

Family

ID=25680681

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CA1999/001205 WO2000037369A1 (fr) 1998-12-18 1999-12-17 Bioreacteur a membrane immerge destine au traitement d'eau contenant de l'azote

Country Status (3)

Country Link
EP (1) EP1140706A1 (fr)
AU (1) AU766535B2 (fr)
WO (1) WO2000037369A1 (fr)

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2822150A1 (fr) * 2001-03-15 2002-09-20 Vivendi Water Systems Procede et installation pour le traitement des eaux mettant en oeuvre au moins un bio-reacteur a membrane immergee
NL1020091C2 (nl) * 2002-02-28 2003-08-29 Tno Nieuwe membraanbioreactor.
EP1346956A1 (fr) * 2002-03-15 2003-09-24 Genix Engineering, Inc. Procédé de traitement des boues en utilisant prétraitement des boues et bioréacteur à membrane immergée
DE10310097A1 (de) * 2003-03-06 2004-09-23 Volker Lenski Vorrichtung und Verfahren zum Aufbereiten von Schmutzwasser
EP1369386A3 (fr) * 2002-05-31 2005-01-26 RHEBAU Rheinische Beton- und Bauindustrie GmbH & Co. Dispositif d'aération d'eaux usées et de nettoyage d'une installation à membranes et microstation d'épuration d'eau contenant ce dispositif
FR2858609A1 (fr) * 2003-08-04 2005-02-11 Otv Sa Procede et installation de traitement biologique des eaux par boues activees avec regulation de l'aeration
US6863817B2 (en) 2002-12-05 2005-03-08 Zenon Environmental Inc. Membrane bioreactor, process and aerator
AT503422B1 (de) * 2006-08-11 2007-10-15 Hans-Peter Dr Bierbaumer Vorrichtung zur trinkwassererzeugung
WO2008035710A1 (fr) 2006-09-21 2008-03-27 Asahi Kasei Chemicals Corporation Procédé d'élimination d'eaux usées
JP2010207799A (ja) * 2009-03-09 2010-09-24 Shenzhen Jdl Environmental Protection Ltd ジェット・曝気装置と装置使用方法
EP2251309A1 (fr) * 2009-05-15 2010-11-17 Shenzen JDL Environmental Protection Ltd. Procédé de formation du bioréacteur à membrane adaptée pour les organismes facultatifs
EP2253596A1 (fr) * 2009-05-15 2010-11-24 Jiangxi JDL Environmental Protection Research Ltd. Procédé pour retirer le phosphore en utilisant un bioréacteur à membrane
CN102701434A (zh) * 2012-07-10 2012-10-03 哈尔滨工业大学 一种复合式自控膜生物反应器及其处理低温低浊高色高氨氮水源水的方法
CN107117703A (zh) * 2017-05-12 2017-09-01 北京建筑大学 一种实时控制序批式膜生物反应器
EP3344584A4 (fr) * 2015-09-01 2018-07-11 Jiangxi JDL Environmental Protection Co., Ltd. Procédé et système de traitement des eaux usées avec zéro décharge de boues
CN108911135A (zh) * 2018-07-17 2018-11-30 厦门理工学院 一种畜禽废水的处理方法
CN108911136A (zh) * 2018-07-17 2018-11-30 厦门理工学院 一种重金属废水的处理方法
CN110078175A (zh) * 2019-05-22 2019-08-02 江苏南大环保科技有限公司 一种超滤和气浮一体化装置及应用
WO2020017956A1 (fr) 2018-07-16 2020-01-23 Haskoningdhv Nederland B.V. Granulation rapide lors du démarrage d'un système de traitement des eaux usées et système de commande associé
US11092977B1 (en) 2017-10-30 2021-08-17 Zane Coleman Fluid transfer component comprising a film with fluid channels
WO2024015799A1 (fr) * 2022-07-14 2024-01-18 Bl Technologies, Inc. Bioréacteur avec filtration sur membrane et procédés de traitement des eaux usées

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3028998B1 (fr) * 2014-12-03 2019-03-06 Institut National des Sciences Appliquées de Toulouse Procédé de traitement d'un effluent par nitrification-denitrification
DE102019003346B3 (de) * 2019-05-11 2020-07-02 Messer Bulgaria EOOD Verfahren und Vorrichtung zur Sauerstoffanreicherung von Wasser in einer Fischzuchtanlage

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS62181772A (ja) * 1986-02-05 1987-08-10 Kurita Water Ind Ltd 生物反応装置
US5266200A (en) * 1991-04-17 1993-11-30 Reid John H Sequence continuous reaction in complete mix activated sludge systems
EP0695722A1 (fr) * 1994-08-03 1996-02-07 Sharp Kabushiki Kaisha Appareil et procédé pour le traitement d'eau usée à l'aide de microorganismes aérobies et anaérobies
JPH08187494A (ja) * 1995-01-09 1996-07-23 Kubota Corp 浄化槽
FR2737202A1 (fr) * 1995-07-25 1997-01-31 Omnium Traitement Valorisa Installation pour le traitement biologique des eaux en vue de leur potabilisation
JPH11314025A (ja) * 1998-03-03 1999-11-16 Inax Corp 膜の洗浄方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS62181772A (ja) * 1986-02-05 1987-08-10 Kurita Water Ind Ltd 生物反応装置
US5266200A (en) * 1991-04-17 1993-11-30 Reid John H Sequence continuous reaction in complete mix activated sludge systems
EP0695722A1 (fr) * 1994-08-03 1996-02-07 Sharp Kabushiki Kaisha Appareil et procédé pour le traitement d'eau usée à l'aide de microorganismes aérobies et anaérobies
JPH08187494A (ja) * 1995-01-09 1996-07-23 Kubota Corp 浄化槽
FR2737202A1 (fr) * 1995-07-25 1997-01-31 Omnium Traitement Valorisa Installation pour le traitement biologique des eaux en vue de leur potabilisation
JPH11314025A (ja) * 1998-03-03 1999-11-16 Inax Corp 膜の洗浄方法

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
DATABASE WPI Section Ch Week 200007, Derwent World Patents Index; Class D15, AN 2000-075410, XP002132967 *
PATENT ABSTRACTS OF JAPAN vol. 012, no. 033 (C - 472) 30 January 1988 (1988-01-30) *
PATENT ABSTRACTS OF JAPAN vol. 1996, no. 11 29 November 1996 (1996-11-29) *

Cited By (33)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2822150A1 (fr) * 2001-03-15 2002-09-20 Vivendi Water Systems Procede et installation pour le traitement des eaux mettant en oeuvre au moins un bio-reacteur a membrane immergee
NL1020091C2 (nl) * 2002-02-28 2003-08-29 Tno Nieuwe membraanbioreactor.
WO2003072513A1 (fr) * 2002-02-28 2003-09-04 Nederlandse Organisatie Voor Toegepast- Natuurwetenschappelijk Onderzoek Tno Bioreacteur a membranes
EP1346956A1 (fr) * 2002-03-15 2003-09-24 Genix Engineering, Inc. Procédé de traitement des boues en utilisant prétraitement des boues et bioréacteur à membrane immergée
EP1369386A3 (fr) * 2002-05-31 2005-01-26 RHEBAU Rheinische Beton- und Bauindustrie GmbH & Co. Dispositif d'aération d'eaux usées et de nettoyage d'une installation à membranes et microstation d'épuration d'eau contenant ce dispositif
US6863817B2 (en) 2002-12-05 2005-03-08 Zenon Environmental Inc. Membrane bioreactor, process and aerator
DE10310097A1 (de) * 2003-03-06 2004-09-23 Volker Lenski Vorrichtung und Verfahren zum Aufbereiten von Schmutzwasser
CN100360438C (zh) * 2003-08-04 2008-01-09 Otv股份有限公司 使用曝气调节并通过活性污泥进行水的生物处理的方法和装置
WO2005021446A1 (fr) * 2003-08-04 2005-03-10 Otv Sa Procede et installation de traitement biologique des eaux par boues activees avec egulation de l’aeration
US7473365B2 (en) 2003-08-04 2009-01-06 Otv Sa S.A. Method and installation for the biological treatment of water using activated sludge and comprising aeration regulation
AU2004268806B2 (en) * 2003-08-04 2009-08-27 Veolia Water Solutions & Technologies Support Method and installation for the biological treatment of water using activated sludge and comprising aeration regulation
FR2858609A1 (fr) * 2003-08-04 2005-02-11 Otv Sa Procede et installation de traitement biologique des eaux par boues activees avec regulation de l'aeration
KR101125165B1 (ko) 2003-08-04 2012-04-18 베올리아 워터 솔루션즈 앤드 테크놀러지스 써포트 활성 슬러지를 사용하고 폭기(曝氣) 조절을 포함하는생물학적 수처리 방법 및 장치
AT503422B1 (de) * 2006-08-11 2007-10-15 Hans-Peter Dr Bierbaumer Vorrichtung zur trinkwassererzeugung
US8097161B2 (en) 2006-09-21 2012-01-17 Asahi Kasei Chemicals Corporation Wastewater treatment method
WO2008035710A1 (fr) 2006-09-21 2008-03-27 Asahi Kasei Chemicals Corporation Procédé d'élimination d'eaux usées
EP2065343A1 (fr) * 2006-09-21 2009-06-03 Asahi Kasei Chemicals Corporation Procédé d'élimination d'eaux usées
KR101158964B1 (ko) 2006-09-21 2012-06-28 아사히 가세이 케미칼즈 가부시키가이샤 폐수의 처리 방법
EP2065343A4 (fr) * 2006-09-21 2010-12-22 Asahi Kasei Chemicals Corp Procédé d'élimination d'eaux usées
JP2010207799A (ja) * 2009-03-09 2010-09-24 Shenzhen Jdl Environmental Protection Ltd ジェット・曝気装置と装置使用方法
EP2251309A1 (fr) * 2009-05-15 2010-11-17 Shenzen JDL Environmental Protection Ltd. Procédé de formation du bioréacteur à membrane adaptée pour les organismes facultatifs
JP2010264435A (ja) * 2009-05-15 2010-11-25 Shenzhen Jdl Environmental Protection Ltd 通性生物適応膜バイオリアクター形成の方法
EP2253596A1 (fr) * 2009-05-15 2010-11-24 Jiangxi JDL Environmental Protection Research Ltd. Procédé pour retirer le phosphore en utilisant un bioréacteur à membrane
CN102701434A (zh) * 2012-07-10 2012-10-03 哈尔滨工业大学 一种复合式自控膜生物反应器及其处理低温低浊高色高氨氮水源水的方法
EP3344584A4 (fr) * 2015-09-01 2018-07-11 Jiangxi JDL Environmental Protection Co., Ltd. Procédé et système de traitement des eaux usées avec zéro décharge de boues
CN107117703A (zh) * 2017-05-12 2017-09-01 北京建筑大学 一种实时控制序批式膜生物反应器
US11092977B1 (en) 2017-10-30 2021-08-17 Zane Coleman Fluid transfer component comprising a film with fluid channels
WO2020017956A1 (fr) 2018-07-16 2020-01-23 Haskoningdhv Nederland B.V. Granulation rapide lors du démarrage d'un système de traitement des eaux usées et système de commande associé
NL2021313B1 (en) * 2018-07-16 2020-01-24 Haskoningdhv Nederland Bv Rapid granulation for the start-up of a wastewater treatment system and associated control system
CN108911135A (zh) * 2018-07-17 2018-11-30 厦门理工学院 一种畜禽废水的处理方法
CN108911136A (zh) * 2018-07-17 2018-11-30 厦门理工学院 一种重金属废水的处理方法
CN110078175A (zh) * 2019-05-22 2019-08-02 江苏南大环保科技有限公司 一种超滤和气浮一体化装置及应用
WO2024015799A1 (fr) * 2022-07-14 2024-01-18 Bl Technologies, Inc. Bioréacteur avec filtration sur membrane et procédés de traitement des eaux usées

Also Published As

Publication number Publication date
EP1140706A1 (fr) 2001-10-10
AU1763900A (en) 2000-07-12
AU766535B2 (en) 2003-10-16

Similar Documents

Publication Publication Date Title
US6616843B1 (en) Submerged membrane bioreactor for treatment of nitrogen containing water
AU766535B2 (en) Submerged membrane bioreactor for treatment of nitrogen containing water
JP4508694B2 (ja) 水処理方法および装置
AU2001280766B2 (en) Method and apparatus for treating wastewater using membrane filters
KR100441208B1 (ko) 생물 여과 기술을 이용하는 회분식 폐수처리장치 및 이를이용한 폐수처리방법
AU2007238520B2 (en) Method and system for nitrifying and denitrifying wastewater
US6555002B2 (en) Apparatus and method for wastewater treatment with enhanced solids reduction (ESR)
EP0618885B1 (fr) Procede biologique pour eliminer la d.b.o. et l'azote d'eaux residuaires
AU2001280766A1 (en) Method and apparatus for treating wastewater using membrane filters
JP4059790B2 (ja) 膜分離活性汚泥処理装置及び膜分離活性汚泥処理方法
US8273247B2 (en) Water reclamation without biosludge reproduction
US5776344A (en) Method for removing nitrogen from wastewater
JP2008264772A (ja) 膜分離活性汚泥装置及び有機物含有水の処理方法
US20070017867A1 (en) Submerged attached growth bioreactor
US20040238441A1 (en) Apparatus and method for treating organic waste water
Wang et al. Simultaneous nitrification and de-nitrification in MBR
CA2355087A1 (fr) Bioreacteur a membrane immerge destine au traitement d'eau contenant de l'azote
KR20060085770A (ko) 미생물과 분리막을 이용한 오폐수 고도처리 시스템 및 방법
IL155193A (en) A device and method for treating wastewater with improved solids reduction
US7976703B2 (en) Treating unit for simultaneous removal of carbon and nitrogen from wastewater and treating apparatus having the same
KR101032068B1 (ko) 고효율 회분식 공정을 이용한 하.폐수 처리 장치 및 방법
JPH09253687A (ja) 排水の嫌気・好気処理装置
JP3807945B2 (ja) 有機性廃水の処理方法及び装置
JP3819457B2 (ja) 排水の生物学的脱窒法
JP2673488B2 (ja) 有機性廃水の処理方法及びその装置

Legal Events

Date Code Title Description
ENP Entry into the national phase

Ref document number: 2000 17639

Country of ref document: AU

Kind code of ref document: A

AK Designated states

Kind code of ref document: A1

Designated state(s): AE AL AM AT AU AZ BA BB BG BR BY CA CH CN CR CU CZ DE DK DM EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT TZ UA UG US UZ VN YU ZA ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW SD SL SZ TZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
ENP Entry into the national phase

Ref document number: 2355087

Country of ref document: CA

Kind code of ref document: A

Ref document number: 2355087

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 1999960738

Country of ref document: EP

Ref document number: 17639/00

Country of ref document: AU

WWE Wipo information: entry into national phase

Ref document number: 09856504

Country of ref document: US

WWP Wipo information: published in national office

Ref document number: 1999960738

Country of ref document: EP

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

WWG Wipo information: grant in national office

Ref document number: 17639/00

Country of ref document: AU