WO1995019322A1 - Traitements microbiologiques a contre-courant - Google Patents

Traitements microbiologiques a contre-courant Download PDF

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Publication number
WO1995019322A1
WO1995019322A1 PCT/US1995/000317 US9500317W WO9519322A1 WO 1995019322 A1 WO1995019322 A1 WO 1995019322A1 US 9500317 W US9500317 W US 9500317W WO 9519322 A1 WO9519322 A1 WO 9519322A1
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anaerobic
aerobic
sludge
εaid
meanε
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PCT/US1995/000317
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English (en)
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Boris M. Khudenko
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Khudenko Boris M
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Priority claimed from US08/181,387 external-priority patent/US5514278A/en
Application filed by Khudenko Boris M filed Critical Khudenko Boris M
Priority to AU15623/95A priority Critical patent/AU1562395A/en
Priority to BR9505641A priority patent/BR9505641A/pt
Publication of WO1995019322A1 publication Critical patent/WO1995019322A1/fr

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    • 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
    • C02F3/1221—Particular type of activated sludge processes comprising treatment of the recirculated sludge
    • 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
    • C02F3/28—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
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2806—Anaerobic processes using solid supports for microorganisms
    • 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
    • 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
    • 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
    • C02F2209/02—Temperature
    • 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
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • 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
    • C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
    • 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
    • C02F2209/20—Total organic carbon [TOC]
    • 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
    • C02F2209/24—CO2
    • C02F2209/245—CO2 in the gas phase
    • 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
    • C02F2209/28—CH4
    • 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
    • C02F2209/38—Gas flow rate
    • 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
    • C02F2209/40—Liquid flow rate
    • 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 generally to industrial biological methods and processes for treatment of wastewater, wastewater sludges, and solid, liquid and gaseous organic materials, and is more particularly related to a counterflow system wherein the influent flows generally in a first direction and the sludge flows generally in the opposite direction.
  • Modern activated sludge systems are used for removal of organics and suspended solids, and for control of nutrients.
  • sludge recycle from the final sludge separator to the head of the treatment process is provided.
  • These systems often incorporate several functional zones, usually called anaerobic (nonaerated, preferably, with low nitrate and nitrite in the feed) , anoxic (nonaerated, nitrite and nitrate present in the feed water) and aerobic (aerated, dissolved oxygen present in the water, nitrification occurs).
  • Mixed liquor is recycled from downstream zones to upstream zones and the separated activated sludge is recycled from the final clarifier to the head of the process.
  • a so-called single sludge is cultivated in all these zones.
  • the sludge recycle from the final clarifier is intended mainly for controlling the average sludge age, or average for the system food to microorganism (F/M) ratio.
  • the upstream facultative zone serves to control the filamentous growth (selector zone) and to release phosphorous for its improved uptake in the aerobic zone.
  • the facultatively anaerobic organisms are circulated with the sludge throughout the system.
  • Anoxic zones are used for denitrification: the biological reduction of nitrites and nitrates formed in the aerobic zone and directed to the anoxic zone with the mixed liquor. These systems are used for treatment of municipal and low to moderately strong industrial wastewater. Examples of these systems are described in U. S. Patents No. 3,964,998 and No. 4,867,883.
  • the disadvantages of such systems include the following: —single predominantly aerobic sludge is formed in the system, such sludge having a poor diversity of species and a narrow range of oxidation-reduction and biodegradation abi l ity ;
  • process can be used only for dilute to moderately strong wastewater
  • the wastewater concentrations are low, while the sludge concentration is about the same as upstream; accordingly, sludge dies off from lack of food, releasing nitrogen, phosphorus, and organics back into the water;
  • OCR oxidation-reduction potential
  • -volatile organics may be emitted to the air in facultative, anoxic and aeration sections.
  • the combined anaerobic-aerobic systems have been developed and used during the past fifty years for treatment of concentrated industrial wastewater. These systems incorporate a separate anaerobic subsystem (functional section) with the final anaerobic clarifier and sludge recycle, and aerobic subsystem (functional section) with the final clarifier as a sludge separation and sludge recycle step. Only excess aerobic sludge may sometimes be transferred to the anaerobic subsystem.
  • This system has important advantages as compared to aerobic systems: high concentration waste can be treated, lesser quantities of sludge are produced, better removal of soluble and suspended solid organics can be achieved.
  • anaerobic and aerobic functional sections in the anaerobic-aerobic systems are only mechanistically coupled. Sludges in these sections do not interact: their make-up and properties abruptly change from anaerobic to aerobic stage.
  • the major disadvantages of anaerobic-aerobic systems are as follows:
  • Hydraulic retention time in lagoons is very long and sludge recycle is not practiced.
  • Processes in lagoons are usually similar to those in ASP, but not intensive and less controlled. Some lagoons may have an anaerobic section, often followed with aerobic sections. Such lagoons are similar to the anaerobic-aerobic systems. Large water volume in the systems insures equalization of wastewater and sludge concentrations and provides a substantial process stability. These systems are mechanically simple and require low maintenance. Many disadvantages of ASP and anaerobic-aerobic processes listed above are also typical for biofilter ⁇ , lagoon systems and various other modifications of biological wastewater treatment.
  • the main objective of the present invention is to improve biological treatment methods by providing novel flow patterns of wastewater and sludges, and by cultivating sludges most appropriate for the concentration and composition of wastewater in a given process section, by providing a broad range of sludge compositions and properties.
  • the objectives of the present invention are achieved by using a treatment system with (1) a general counterflow of the biological sludges and wastewater being treated, (2) a high sludge concentration at the head of the system where the organics concentration is also high, (3) a great diversity of sludge organisms in the systems and gradual change in the biocenoses along the system, and (4) an alternating exposure of wastewater constituents and metabolic products to various functional groups of biological sludges.
  • the wastewater constituents are exposed to a broad range of environmental conditions: physical, chemical, and biochemical and physical-chemical actions due to the availability of many organism types, enzymes, co-metabolizing species (vitamins, growth substances, steroids, nucleic acids, etc.), a broad ORP range, and favorable chemical make up.
  • a novel type of functional zone with simultaneous anaerobic, anoxic and aerobic activities is developed for the removal of various classes of organics, including biodegradable and recalcitrant and toxic, through oxidations and reductions in a wide ORP range. Biological and chemical pathways of nitrogen removal are employed in such functional zones.
  • Additional improvement is in applying to the treatment systems physical actions, such as magnetic, ultrasonic, or radio frequency electromagnetic fields, physical-chemical actions, such as electrolytic action, adsorption, coagulations-flocculation (including electrocoagulation) , and chemical actions, such as addition of strong oxidants (H 2 0 2 , ozone, Fe , nitrates, nitrites, and other oxyion ⁇ ) or their internal beneficial reuse. Addition of nutrients, ⁇ uch as nitrogen and phosphorous, and micronutrients, such a ⁇ microelements and, if needed, biostimulators, ⁇ uch a ⁇ vitamins, steroids, folic acid, metal naftenates and nucleic acid ⁇ .
  • physical actions such as magnetic, ultrasonic, or radio frequency electromagnetic fields
  • physical-chemical actions such as electrolytic action, adsorption, coagulations-flocculation (including electrocoagulation)
  • chemical actions such as addition of strong oxidants (H 2 0 2 , ozone, Fe
  • Provisions for reducing air emis ⁇ ion ⁇ of volatile organic and inorganic con ⁇ tituents from the wastewater treatment processes further improve the system.
  • a variable flow effluent recycling for stabilizing the flow rate acros ⁇ the treatment train may be provided; and, a provi ⁇ ion for managing increased flow of more dilute water during a storm event is a further process improvement.
  • FIG. 1 i ⁇ a schematic diagram showing the basic counter flow arrangement of the present invention
  • Fig. 2 is a ⁇ chematic diagram showing a modified form of the proces ⁇ of Fig. 1, the reactors of Fig. 1 being split into a plurality of reactors;
  • Fig. 4 is a view similar to Fig. 2 and showing treatment by electric potential and by magnetism;
  • Fig. 5 i ⁇ a view ⁇ imilar to Fig. 2 but showing a con ⁇ tant flow system
  • FIG. 7 is a rather schematic illustration showing an apparatus for carrying out the process illustrated in Fig. 1 of the drawings;
  • Fig. 9 is a view ⁇ imilar to Fig. 8 but ⁇ howing a modified form of apparatus;
  • Fig. 11 is a rather ⁇ chematic view ⁇ howing another form of apparatu ⁇ for carrying out the proce ⁇ of the pre ⁇ ent invention.
  • the basic counterflow ⁇ ystem as shown in Fig. 1 comprises multiple parallel consecutive ⁇ tages of biological reaction and sludge separation step ⁇ , with a fraction of the mixed liquor being fed directly to the down ⁇ tream stage and the balance of the liquor being fed to the sludge ⁇ eparator.
  • the final sludge discharge is preferably provided at the inlet stage of the counterflow process.
  • ⁇ ludge may be di ⁇ charged from an intermediate proce ⁇ stage.
  • the largest sludge concentration will occur in the upper stage ⁇ where the food concentration is also the highe ⁇ t; and, the lowe ⁇ t sludge concentration will be found in the last stage ⁇ of the ⁇ y ⁇ tem where the food concentration i ⁇ low. Therefore, the F/M ratio along the entire process train can be close to the optimum.
  • Thi ⁇ will in ⁇ ure more optimal F/M ratio ⁇ , the condition along the process train in which the available substrate can best support the bioceno ⁇ es in a given proces ⁇ ⁇ tage.
  • the relea ⁇ e of nutrient ⁇ (nitrogen and pho ⁇ phoru ⁇ ) and intracellular organic ⁇ in the water at the end of the biological treatment ⁇ tep (due to the microbes' dying from lack of food) will be largely eliminated. Accordingly, the control of organic ⁇ and nutrients i ⁇ improved.
  • the ⁇ e sludges have a gradually changing make-up because the biomass is not only retained within a stage, but i ⁇ also tran ⁇ ferred up ⁇ tream and down ⁇ tream.
  • a gradual change from a very high to low sludge concentration, and a gradual change in the microbial and enzymatic make-up from the upstream to the down ⁇ tream, provide greater diversity of actions applied to the original constituents and intermediate metabolic products in wastewater.
  • the recycle rate in the new system may be determined not only by the need to transfer the sludge upstream, but also by the requirement to recycle wastewater and metabolic products in it to the upstream zone.
  • anaerobic, facultatively anaerobic, anoxic, aerobic, and polishing zones can be establi ⁇ hed in the proce ⁇ train.
  • Each zone may be repre ⁇ ented by one or multiple proce ⁇ s stages.
  • Multiple, but interacting and progressively changing, sludges are formed in each ⁇ tage in each zone: from the true anaerobic ⁇ ludge that predominate ⁇ at the up ⁇ tream of the ⁇ y ⁇ tem, through facultative anaerobic and anoxic, to the aerobic being dominant at the effluent end.
  • the sequence of sludges may change, or certain sludge zones, (e.g. anaerobic) may be repeated.
  • specific sludge ⁇ (e.g. anaerobic) may be tran ⁇ ferred down ⁇ tream; however, the predominant flow of the ⁇ ludge ⁇ will remain from the down ⁇ tream to the up ⁇ tream, in counterflow to the wa ⁇ tewater.
  • parallel proce ⁇ s stage ⁇ may be used.
  • an aerobic process stage conducted in a biofilter may be established in parallel to the anoxic process stage.
  • Mixed liquor from the anoxic ⁇ tage i ⁇ pumped to the biofiltration ⁇ tage wherein further organic ⁇ ' oxidation and nitrification occur.
  • the nitrified effluent from the biofiltration ⁇ tage i ⁇ returned to the anoxic stage for the denitrification.
  • Air fed in the parallel biofiltration step may vent the anaerobic and other ⁇ tage ⁇ and pick up the organic and inorganic volatile materials emitted from these ⁇ tages. These volatile materials will be biologically treated in the biofiltration step, thereby preventing their e ⁇ cape to the air.
  • Variou ⁇ ⁇ ludge ⁇ cultivated in the functional proces ⁇ zone ⁇ will ⁇ ubject the wa ⁇ tewater con ⁇ tituents to the widest range of enzymes, Oxidation-Reduction Potential ⁇ (ORP), and other biological, biochemical, chemical, and phy ⁇ ical- chemical actions which can be established with the given wastewater. This provide ⁇ the best conditions for transformation and removal of waste constituents.
  • certain metabolic product ⁇ formed in the down ⁇ tream ⁇ tage ⁇ e.g.
  • nitrates and nitrites are recycled up ⁇ tream with the ⁇ eparated ⁇ ludge and undergo a ⁇ econd round of treatment by a ⁇ et of microorganisms available upstream in the ORP domain, that would not be available in the down ⁇ tream proce ⁇ s zones.
  • Certain constituents, for example, nitrates and nitrites, recycled from the down ⁇ tream to the upstream sections will serve as u ⁇ eful reactant ⁇ .
  • nitrite ⁇ and nitrate ⁇ strong oxidizers
  • Pas ⁇ ing down the mixed liquor and the ⁇ ludge ⁇ , and returning up ⁇ tream material from the downstream proces ⁇ zone ⁇ will subject the original constituent ⁇ and metabolic product ⁇ to the alternating treatment condition ⁇ , particularly very wide ORP range ⁇ .
  • sludges may also be transferred down ⁇ tream, bypassing one or several process stages.
  • the excess sludge from the upstream separator is discharged from the sy ⁇ tem directly, or after dige ⁇ tion and conditioning.
  • Anaerobic zone ⁇ may be further divided into acidification and hydrolyzing zone ⁇ , and into methanogenic zone ⁇ and ⁇ ludge conditioning zone ⁇ a ⁇ defined in the co ⁇ pending application No. 08/046,788.
  • the ⁇ ludge separation device ⁇ can combine function ⁇ of anaerobic, facultative, anoxic, or aerobic zone ⁇ .
  • the wa ⁇ tewater influent may be di ⁇ tributed over multiple proce ⁇ ⁇ tage ⁇ along the flow. Such distribution may be needed to support generation and accumulation of the sludge mas ⁇ when treating dilute wa ⁇ tewater, for example, municipal ⁇ ewage.
  • ⁇ pecific ⁇ ludge zone ⁇ can be established.
  • most upstream zones can be true anaerobic zone, followed by a facultative zone, an anoxic zone, and an aerobic zone.
  • a polishing zone for example, with activated carbon adsorption and coagulation-flocculation zone can be establi ⁇ hed after the aerobic zone.
  • the ⁇ e zone ⁇ may partially overlap. They also may shift during operation of the system. Zones combining ⁇ everal functions, for example, anaerobic with facultative anaerobic, anoxic and aerobic can al ⁇ o be e ⁇ tabli ⁇ hed.
  • Such zone ⁇ involve either feeding various sludges to the zone, or include means for retaining at least one sludge in thi ⁇ zone, for example, anaerobic, and feeding through other ⁇ ludge ⁇ cultivated in other zone ⁇ , for example, aerobic.
  • a sludge retaining means a fixed or fluidized bed can be u ⁇ ed. Wa ⁇ tewater Recycle
  • fatty acids and other degradable compounds In the upstream anaerobic functional zone, a significant fraction of organics is hydrolyzed, and a fraction of it is converted into fatty acids and other degradable compounds. Such tran ⁇ formation ⁇ are mo ⁇ t applicable to the organic ⁇ that can be ea ⁇ ily reduced, or transformed in the reducing anaerobic media. Some fatty acids will be further converted into methane and carbon dioxide. The remaining fatty acid ⁇ , and the con ⁇ tituent ⁇ not ea ⁇ ily degradable in the anaerobic environment, are transferred to the downstream aerobic zone(s) with the mixed liquor and sludge-free separated water. Most of these constituents have been brought to a reduced state in the anaerobic zone and are readily oxidizable.
  • the remaining original wastewater constituents are mixed with anaerobic metabolic product ⁇ .
  • anaerobic metabolic product ⁇ Such a mixture i ⁇ nutritionally richer and can ⁇ upport the growth of a more diver ⁇ e aerobic biocenoses.
  • the biodegradation efficiency (percent degraded) and rate increase.
  • the biodegradation of many single fatty acid ⁇ range ⁇ from 60 to 80 percent, wherea ⁇ their mixtures may be 100% degraded.
  • aerobic ⁇ ection aerobic degradation re ⁇ ult ⁇ in the production of water, carbon dioxide, incompletely degraded product ⁇ (a ⁇ expected, in an "oxidized” ⁇ tate) , ⁇ oluble metabolic product ⁇ , and biomass.
  • Nitrification will occur in the aerobic and aerated polishing zone ⁇ . Recycling of the nitrified liquid up ⁇ tream to the anaerobic or anoxic zone ⁇ will result in reduction of nitrate ⁇ and nitrite ⁇ to nitrogen. Additional denitrification may be provided by u ⁇ ing intermittent aeration in the aerobic zone. The nitrification can be further improved by u ⁇ ing powdered activated carbon (PAC) a ⁇ a ⁇ upport medium for the nitrifying bacteria. Alternatively, a ⁇ ubmerged ⁇ upport medium, floating or fixed, can be provided in the aerobic zone, or a biofiltration may be u ⁇ ed.
  • PAC powdered activated carbon
  • a di ⁇ tributed influent feed can be provided.
  • Line ⁇ for feeding part of the influent may be u ⁇ ed in each reaction stage, or certain ⁇ tage ⁇ can be selected during design and operation.
  • a clarified flow of partially treated wa ⁇ tewater for example after the anaerobic functional zone, can also be di ⁇ tributed over several downstream functional zone ⁇ similarly to the described distributed influent feed.
  • This option provide ⁇ ⁇ equential anaerobic-aerobic treatment for the entire wa ⁇ tewater flow. Accordingly, a broader range of biochemical, phy ⁇ ical-chemical, and chemical tran ⁇ formations will be applied to the entire quantity of pollutant ⁇ fed into the system.
  • the ⁇ eparated PAC i ⁇ recycled upstream and passes with the sludge, in counterflow to the water.
  • the PAC function ⁇ mostly as an adsorbent; however, a slow biological proces ⁇ on the active ⁇ urface al ⁇ o occur ⁇ , similar to proces ⁇ e ⁇ in water purification for water ⁇ upplie ⁇ .
  • the PAC ⁇ pent in the polishing stage and tran ⁇ ferred up ⁇ tream act ⁇ al ⁇ o a ⁇ an ad ⁇ orbent with the increasing role of the biological activity. Subjecting PAC to the alternate aerobic-anaerobic environments i ⁇ helpful for its bioregeneration.
  • coagulants for example, aluminum and iron ions or their combinations
  • coagulation and flocculation aids for example, polymer ⁇ , silica based aids, etc.
  • Aluminum and iron ion ⁇ are used in the upstream sections for phosphoru ⁇ removal.
  • Iron ions are also es ⁇ ential for microorgani ⁇ m ⁇ a ⁇ a icronutrient. Iron ions are oxidized to the trivalent state in the aerobic stages and reduced to the divalent state in the anaerobic and anoxic stage ⁇ . Such cycling of iron ⁇ pecies is useful for chemical conversions of organic and inorganic constituents.
  • Biochemical, physico-chemical, and chemical conver ⁇ ion ⁇ of con ⁇ tituent ⁇ in wastewater can be additionally improved by imposing electrical and electromagnetic fields on the liquid in the biological reactors in all, or selected ones, of the functional zone ⁇ .
  • the ⁇ e field ⁇ can increa ⁇ e the proce ⁇ rate and shift equilibrium in many reactions, especially, oxidation-reduction and precipitation equilibria, and al ⁇ o pH dependent processe ⁇ .
  • Electrochemical action can be produced by applying a direct current, an alternating current, or an a ⁇ ymmetric current (for example, a combination of direct and alternating current ⁇ ).
  • a partially rectified direct current, and direct current with a back pul ⁇ e can al ⁇ o be u ⁇ ed.
  • Magnetic field ⁇ can be applied with the u ⁇ e of permanent magnet ⁇ and electromagnet ⁇ .
  • the ⁇ e action ⁇ can be applied to the mixed liquor, mixed liquor with PAC and /or GAC (granular activated carbon), and with coagulants.
  • PAC, GAC, flocculent and bioflock particles and their combinations will serve as fluidized electrode ⁇ and micromagnet ⁇ (particles loaded with iron) .
  • Electric current can be applied to the mixed liquor or sludge ⁇ at variou ⁇ proces ⁇ step ⁇ ⁇ imultaneously with other action ⁇ , for example with addition of the powdered and granular activated carbons.
  • Carbon particles will serve a ⁇ multiple intermediate electrode ⁇ or fluidized electrode ⁇ .
  • the electric forces will a ⁇ i ⁇ t in transforming the materials ad ⁇ orbed on the carbon.
  • the ⁇ e tran ⁇ formation ⁇ may include coagulation-flocculation, polymerization, and oxidation-reduction.
  • Electric current may also as ⁇ ist nitrification and denitrification, reduction and oxidation of ⁇ ulfur ⁇ pecie ⁇ , precipitation of heavy metal ⁇ , aluminum and iron ⁇ alts coagulation, and oxidation-reduction involving hydrogen peroxide.
  • the aerobic and polishing proces ⁇ ⁇ tep ⁇ may be enhanced by the addition of hydrogen peroxide, ozone, ultraviolet
  • UV radiation or various combinations of these three.
  • Such provision ⁇ are not possible in the prior art sy ⁇ tem ⁇ becau ⁇ e of the high biomass concentration which makes the mixed liquor nontran ⁇ parent and rapidly con ⁇ ume ⁇ hydrogen peroxide and ozone for nontarget reactions.
  • wastewater and sludge concentrations are low and the mixed liquor i ⁇ tran ⁇ parent for the UV light. Accordingly, UV light can be u ⁇ ed, and hydrogen peroxide can be introduced to react with residual organics in the water being polished.
  • ⁇ ome inorganic ⁇ can be achieved in the new ⁇ y ⁇ tem.
  • ⁇ ulfur specie ⁇ for example ⁇ ulfate ⁇
  • ⁇ ulfate ⁇ can be converted into elemental ⁇ ulfur via biological conver ⁇ ion to ⁇ ulfite ⁇ and sulfides in anaerobic step ⁇ , and chemical reaction ⁇ between sulfides and ⁇ ulfites and sulfates to form sulfur, and sulfides and nitrites and nitrates to form sulfur and nitrogen.
  • Calcium and carbonates can be removed as calcium carbonate ⁇ .
  • Pho ⁇ phoru ⁇ can be removed with calcium, iron, and aluminum.
  • Heavy metals can be largely precipitated with sulfides formed in anaerobic steps. Stabilized Flow Rate
  • a time variable recycle of the effluent to the head of the system i ⁇ provided at the flow rate nece ⁇ ary to complement the influent flow to make up a con ⁇ tant combined flow equal to the maximum influent flow rate.
  • a flow equalization tank i ⁇ provided to reduce the maximum flow rate.
  • the complementary effluent recycle rate i ⁇ reduced to make up for the equalized maximum flow rate.
  • the influent flow rate increase ⁇ , while the pollution loading may remain the same or change only slightly.
  • the influent will be distributed into several zone ⁇ along the flow and the effluent will be di ⁇ charged from the final ⁇ ludge ⁇ eparator ⁇ and from one or several preceding ⁇ ludge separators.
  • Fractions of ⁇ eparated wa ⁇ tewater from the ⁇ e preceding clarifier ⁇ may not undergo the whole ⁇ equence of treatment; however, the wa ⁇ tewater during storm events i ⁇ more dilute and needs les ⁇ treatment.
  • Such an arrangement permits the use of smaller final ⁇ ludge ⁇ eparator ⁇ during rain event ⁇ a ⁇ compared to conventional ⁇ y ⁇ tems designed to meet the storm conditions.
  • increa ⁇ ed (decrea ⁇ ed) incoming loading rate ⁇ will cau ⁇ e the ⁇ pecific treatment zone ⁇ to increa ⁇ e (decrea ⁇ e) in ⁇ ize by stretching (shrinking) downstream. This will control and insure stability and high performance under variable input conditions.
  • the escape of volatile organics and other obnoxious gase ⁇ , for example, hydrogen ⁇ ulfide, to the air from an open anaerobic, facultative, anoxic, and aerobic sections can be reduced by collecting the said ga ⁇ e ⁇ and ⁇ crubbing them with the water undergoing the final ⁇ tage ⁇ of the aerobic or poli ⁇ hing treatment. This can be done in a separate biofilter, or a biofilter stacked above the other proce ⁇ s sections. Alternatively, a double-deck biofiltration can be used with the upper deck irrigated by the wastewater treated in the lower deck, and the lower deck fed with the water from the preceding proces ⁇ steps, for example, the anoxic step.
  • obnoxious gase ⁇ for example, hydrogen ⁇ ulfide
  • ⁇ crubbing proce ⁇ Further improvement of the ⁇ crubbing proce ⁇ can be provided by adding PAC to the top deck water in the biofilter. The PAC will then be retained in a ⁇ ludge ⁇ eparation device and recycled to the preceding proces ⁇ ⁇ teps as previously described.
  • Methane gas can be introduced in aerobic ⁇ tage ⁇ , for example, by sparging in the aerated chambers, or a ⁇ admixture to the air in biofilter ⁇ .
  • Methanotrophic organi ⁇ m ⁇ will develop and co-metabolize chlorinated and other poorly degradable organic ⁇ .
  • the off gas from the anaerobic proce ⁇ ⁇ tage can be u ⁇ ed for this purpose. In case of an open anaerobic stage, this gas can be collected under a hood and picked up by a blower or a fan delivering air in either an aeration basin or in a biofilter. In such a case, the anaerobic off gas will also be treated for hydrogen sulfide and volatile organics.
  • the present biological method may also be applied to the treatment of indu ⁇ trial ga ⁇ eou ⁇ emissions such as venting and breathing devices in chemical, biochemical (fermentation), painting and coating, and other processes emitting organic gasses, organic particulates, and inorganic gases treatable biologically (for example, hydrogen sulfide).
  • the treatment of these emission ⁇ may be the same as described for the fugitive gase ⁇ emitted from the wastewater treatment operations, or it may involve a multistage system similar to the present method of wastewater treatment.
  • the gaseous emission can be fed into an anaerobic reaction ⁇ tage and then tran ⁇ ferred in an aerobic reaction stage.
  • the constituent ⁇ of pollution, gaseous or particulate, will be scrubbed and adsorbed by the water carrying anaerobic and then aerobic biomas ⁇ respectively.
  • These two types of biomass (sludges) in two proces ⁇ ⁇ tage ⁇ will degrade the ⁇ aid organic ⁇ , while multiplying the bioma ⁇ .
  • sludges Similar to the previously described novel method of wa ⁇ tewater treatment, a portion of anaerobic bioma ⁇ i ⁇ tran ⁇ ferred to the aerobic ⁇ tage, and a substantial portion of the aerobic bioma ⁇ s i ⁇ tran ⁇ ferred to the anaerobic stage.
  • a sludge conditioner as ⁇ ociated with the anaerobic ⁇ tage may be provided.
  • PAC can be added to the aerobic process ⁇ tage.
  • a wastewater may be u ⁇ ed as a source of organic substrate.
  • Fig. 1 illustrate ⁇ a ba ⁇ ic ⁇ y ⁇ tem with counterflow of the activated biological ⁇ ludge and wa ⁇ tewater.
  • the system consists of consecutive reaction ⁇ tage ⁇ 111, 2010, 301, 401 and 501 connected to each other by line ⁇ 131, 231, 331 and 431.
  • Lines 110, 210, 310, 410 and 510 connect treatment stages 101, 201, 301, 401 and 501 to sludge separators 100, 200, 300, 400 and 500 respectively.
  • Lines 111, 212, 311 and 411 are provided for transferring the separated sludge-free water to the downstream reactions stages 201, 301, 401 and 501.
  • Line 512 is the effluent discharge line.
  • Lines 221, 321, 421 and 521 are line ⁇ for counterflow feeding of the separated concentrated sludge from sludge separators 200, 300, 400 and 500 to reactions stage ⁇ 101, 201, 301 and 401 respectively.
  • Line 13 is the sludge discharge line connected to the sludge separator 100.
  • Line 121 is an optional sludge recycle in the section compri ⁇ ing the reaction stage 101 and ⁇ ludge separator 100.
  • the biological ⁇ ludge is grown.
  • the mixture of wastewater and the sludge form the mixed liquor.
  • Wastewater is continuously fed into the reaction stage 101 and the mixed liquor is continuously displaced from this stage. Part of the mixed liquor is tran ⁇ ferred in the next reaction ⁇ tage 201.
  • the balance of the mixed liquor i ⁇ fed into the sludge ⁇ eparator 100 The water fraction (sludge-free water) from the sludge separator is also fed into the next reaction stage 201, while the separated sludge (concentrated sludge) i ⁇ di ⁇ charged via line 13.
  • part of the ⁇ ludge separated in the sludge separator 100 may be recycled via line 121 back into the reaction stage 101.
  • the second reaction stage is fed via line 131 with mixed liquor from the reaction stage 101, clarified sludge-free water via line 111 from the sludge separator 100, and with the backfed concentrated sludge via line 321 from the sludge ⁇ eparator 300.
  • reaction ⁇ stage 301 with associated sludge separator 300, reaction stage 401 with sludge separator 400, and reaction stage 501 with sludge separator 500 are operated the same way as the preceding stage except that the last stage where the entire amount of the mixed liquor is directed to the ⁇ ludge separator 500 and the clarified water is discharged from the ⁇ ystem via line 512.
  • Means for aeration, mixing, pH control, nutrients addition, and other well known means can be used, but these means are not ⁇ hown in Fig. 1.
  • the wastewater and the biological sludge in the pre ⁇ ent ⁇ ystem are going in generally counterflow direction . Due to the backfeed of a fraction of the ⁇ ludge in ⁇ tage ⁇ 201, 301 and 401, and all ⁇ ludge in ⁇ tage 501, the ⁇ ludge concentration in the head ⁇ ection ⁇ of the ⁇ ystem i ⁇ the greate ⁇ t, and it decline ⁇ toward ⁇ the down ⁇ tream ⁇ ections. The wastewater concentration in the system declines from the upstream to the downstream. Accordingly, the F/M ratios vary less along the process train in the pre ⁇ ent system than in the prior art methods. The highest organic ⁇ (food) supply corresponds to the greatest concentration of the biological sludge.
  • the biological ⁇ ludge concentration i ⁇ at a minimum. Accordingly, the food deficiency will not cau ⁇ e a ma ⁇ ive die off and relea ⁇ e the ⁇ econdary substrate (a pollutant) and nutrients (also pollutant ⁇ ).
  • the ⁇ ludges in each stage are largely adapted to the environment in the stage, sub ⁇ trate concentration and compo ⁇ ition, F/M ratio, pH, nutrient ⁇ concentration ⁇ , etc.
  • the flow pattern of wastewater i ⁇ generally down ⁇ tream.
  • water flow ⁇ with backfeed of sludges provides some backfeed of water.
  • variable influent condition ⁇ variable flow, concentration and compo ⁇ ition of ⁇ ubstrate
  • the present sy ⁇ tem will be operated a ⁇ follow ⁇ : ⁇ hort time (high frequency) variation ⁇ in concentrations will be very effectively equalized due to the dilution in the reaction volumes, due to the split parallel flows in the reaction stages and sludge separator ⁇ with time delay, and due to the backfeed of ⁇ ludges.
  • the treatment proces ⁇ may be virtually completed, for example at a prolonged low loading rate, in the reaction stage 301. Very little treatment, if any, will occur in stage ⁇ 401 and 501. Accordingly, ⁇ ludge concentration ⁇ in ⁇ tage ⁇ 401 and 501 will al ⁇ o decline.
  • Fig. 2 illu ⁇ trate ⁇ a novel system with multiple-chamber functional zones. It comprises reaction stage ⁇ 101,
  • 302 ... and so on represent multiple chambers in functional zone ⁇ .
  • 101, 102 ... ⁇ tage ⁇ may form an anaerobic functional zone
  • 201 ... chamber ⁇ form facultative zone
  • 301... stages an anoxic zone. All reaction stages in all zones are connected by lines 131, 132 ..., 231 ..., 331, 332 ..., 431 ..., 531.
  • Each zone ha ⁇ at least one sludge separation device 100, 200, 300, 400 and 500 connected to the last chamber in a particular zone by line ⁇ 110, 210, 310, 410 and 510.
  • more than one sludge separation device can be used in a functional zone.
  • the ⁇ ludge separation device i ⁇ connected to one of stages within the zone preceding the last stage.
  • it can be connected to stage 301, or ⁇ tage 302, or to both.
  • the separated water i ⁇ pas ⁇ ed downstream via lines 111, 211, 311 and 411.
  • the separated sludge is fed back to one or ⁇ everal preceding stages within the same functional zone, or in the preceding functional zone.
  • Lines 221, 222 ..., 321, 322 ..., 421, 422 ..., 521, 522 ... are provided for the ⁇ ludge feed back.
  • the influent is conveyed by a line 1, and the effluent is di ⁇ charged via line 512.
  • the sludge discharge line 121 is provided.
  • line 121 is used for transferring the anaerobic ⁇ ludge to a sludge conditioner 10, which has a line 12 and a pump or other conveying mean ⁇ 11 for tran ⁇ ferring part of the conditioned sludge to the anaerobic functional zone, for example, to a stage 101, and a line 13 for sludge discharge.
  • the system is equipped with appropriate auxiliary mixing and aeration devices and other conventional mean ⁇ commonly found in anaerobic, facultative, anoxic, aerobic, and polishing zones.
  • the auxiliary means are not shown in Fig. 2.
  • Functional zone ⁇ provide a greater variety of microorgani ⁇ ms and a broader range of environmental conditions.
  • the strongly anaerobic functional zone provide ⁇ strongly reducing conditions helpful for reductive dehalogenation of organics, reduction of toxic and poorly degradable organics containing oxygen, sulfur, nitrogen, phosphorous, and others not degradable aerobically.
  • Metabolic products of the anaerobic zone mainly fatty acids, and some original readily oxidizable organic ⁇ are transferred to the subsequent zone ⁇ where they are ea ⁇ ily oxidized.
  • alternating functional zone ⁇ (anaerobic-aerobic- anaerobic-aerobic ...) may be u ⁇ ed. Facultative and anoxic zone ⁇ can al ⁇ o be included in the alternation ⁇ .
  • ⁇ ludge ⁇ are compo ⁇ ed of p ⁇ ychrophilic, e ⁇ ophilic, and thermophilic microorgani ⁇ m ⁇ .
  • the proportion of such organi ⁇ m ⁇ depends on temperature and other environmental conditions. Particularly, in media with easily degradable organic ⁇ percentage of the thermophiles i ⁇ high even at moderate temperature ⁇ .
  • Thi ⁇ increases the diversity of biopopulation in the sy ⁇ tem and improve ⁇ the process. Alternate exposure of the original organic ⁇ and the metabolic product ⁇ to the anaerobic and aerobic environment ⁇ produces easily degradable constituent ⁇ for both anaerobic and aerobic zone ⁇ .
  • Fig. 3 i ⁇ a flow chart ⁇ imilar to that of Fig. 2 with the additional line ⁇ 2 and 242, 341, 343, 441 ... for di ⁇ tributed feed of influent in various functional zone ⁇ in the sy ⁇ tem.
  • Distributed feed of the influent may be helpful for increasing the sludge mas ⁇ in the system by providing more food in aerobic functional zones where sludge yield is greater than in anaerobic zones.
  • Distributed feed may also be helpful in system ⁇ with alternating aerobic-anaerobic zone ⁇ to provide ⁇ ufficient organic ⁇ ⁇ upply for maintaining anaerobio ⁇ i ⁇ in the down ⁇ tream anaerobic zone ⁇ . It can al ⁇ o be u ⁇ ed a ⁇ a ⁇ ource of organic ⁇ in the anoxic zone for the reduction of nitrate ⁇ and nitrite ⁇ .
  • additional optimization of F/M ratios and improved biodegradability of organic ⁇ are provided.
  • partially treated wa ⁇ tewater for example from the anaerobic functional zone, can be di ⁇ tributed over ⁇ everal downstream functional zones.
  • thi ⁇ purpose line 111 would be extended and provided with branches leading to the reaction ⁇ tage ⁇ 301, 401 and 501 or other intermediate stages.
  • Fig. 4 is a flow chart ⁇ imilar to that shown in Fig. 2 with additional means for phy ⁇ ical, chemical and phy ⁇ ico- chemical treatment combined with the previou ⁇ ly de ⁇ cribed biological treatment.
  • Phy ⁇ ical means include an electrolyzing means comprising electric current ⁇ ource ⁇ 172 ... , 373 ... , 472 ... 572 and electrode ⁇ 182 ..., 383 . . . , 482 ..., 582. Electrode ⁇ are submerged in the reaction stages.
  • Alternating including industrial frequencies (50—60 Hz), or direct, or asymmetric alternating, or rever ⁇ ing currents, and currents with backpulses, can be applied.
  • the sludge flocks and particles of the powdered activated carbon can be used a ⁇ fluidized electrode ⁇ .
  • Application of the electric current to the biological ⁇ y ⁇ tem greatly expand ⁇ the range of ORP in the reaction zone ⁇ .
  • microzone ⁇ with a wide pH range are formed in the liquid. Accordingly, many chemical, electrochemical and biochemical reaction ⁇ will be effected, and/or accelerated.
  • nitrification-denitrification may be greatly improved, including the accelerated biological pathway and the chemical pathway when ammonia and nitrogen oxide ⁇ react to form nitrogen and water.
  • Sulfur formation from hydrogen sulfides and oxyions of sulfur can be accelerated. Many oxidation-reduction reactions involving toxic, poorly degradable, and recalcitrant organic ⁇ can be effected.
  • Magnetic devices 261 ..., 361, 362 ..., 562 can be submerged in the reaction stages. Permanent magnets or electromagnets can be used. Magnetic action will accelerate biochemical reactions and promote some chemical reactions, primarily formation of the insoluble calcium carbonate. The latter are helpful for reducing the TDS of the effluent. Magnetization of mixed liquor can also reduce heavy metals in the effluent due to formation of the metal carbonate ⁇ and other poorly ⁇ oluble ⁇ alt ⁇ .
  • Mean ⁇ 541, 542, 543 ... for addition of the powdered activated carbon (PAC), coagulants, hydrogen peroxide, and other reagents can be provided.
  • the ⁇ e reagent ⁇ are fed into the poli ⁇ hing ⁇ tage or one of preceding treatment ⁇ tage ⁇ .
  • PAC in the polishing step can adsorb residual organics including toxic, poorly and slowly degradable.
  • PAC will be ⁇ eparated from the liquid in the ⁇ ludge separator 500 and back fed in the previous reaction stages. Gradually, PAC will be transported with the sludge in the counterflow direction to the water flow. In each reaction stage, PAC will be used a ⁇ an ad ⁇ orbent of organic ⁇ . Adsorbed organics will be largely biologically degraded, including a substantial fraction of toxic, poorly and slowly degradable organics. Alternating anaerobic-aerobic condition ⁇ improve biological regeneration of PAC by ⁇ upporting the de ⁇ truction of organic ⁇ that otherwi ⁇ e would be not degraded.
  • Electrocoagulation does not increase the effluent TDS.
  • Coagulants help to remove ⁇ uspended solid ⁇ , di ⁇ solved organic ⁇ and pho ⁇ phoru ⁇ .
  • Coagulation material ⁇ are ⁇ eparated with the ⁇ ludge in the ⁇ ludge ⁇ eparator 500 and are back-fed in the counterflow to the water flow. Iron ion ⁇ are helpful in chemical, biological and electrochemical conver ⁇ ion ⁇ involving ⁇ ludge ⁇ .
  • iron can be oxidized to it ⁇ trivalent state in aerobic proces ⁇ zone ⁇ and reduced to it divalent ⁇ tate in the anaerobic and facultative zone ⁇ .
  • Such cycling of iron i ⁇ very supportive for biological and chemical oxidation-reduction reactions in the reaction stages.
  • iron will largely be consumed for sulfide precipitation. This will reduce the sulfide content and TDS of the liquid in the system.
  • Both, iron and aluminum will be used in phosphorus precipitation.
  • Hydrogen peroxide, or ozone, or both, can be added to the polishing reaction stage for oxidation of re ⁇ idual organics. In the presence of the iron coagulant, hydrogen peroxide would become the Fenton reagent, a more capable oxidizer than the hydrogen peroxide itself.
  • Fig. 5 i ⁇ a flow chart similar to that shown in Fig. 2 with the addition of an effluent recycle line 511 and a conveying means 513 for tran ⁇ ferring part of the effluent to the influent line 1.
  • line 511 is connected to a flow control box 514 on the line 1 for producing a constant flow rate of liquid through the sy ⁇ tem a ⁇ de ⁇ cribed in the co-pending application Serial No. 08/046,788 filed 04/12/93.
  • Thi ⁇ ⁇ y ⁇ tem modification i ⁇ operated ⁇ imilarly to those previously described.
  • the effluent recycle serves to dilute the excessively concentrated influent.
  • the recycle of metabolic products expo ⁇ e ⁇ them to a wide range of enzymes and ORP condition ⁇ .
  • a ⁇ y ⁇ tem with a flow control box 514 the liquid flow rate acro ⁇ the ⁇ ystem is ⁇ tabilized. Accordingly, operations of ⁇ ludge separation means and other portions of the ⁇ y ⁇ tem become ⁇ impler and more reliable.
  • Fig. 6 i ⁇ a flow chart ⁇ imilar to that depicted in Fig. 2, with the addition of the ⁇ tormwater overflow chamber 16 and additional di ⁇ tributed ⁇ torm flow input line ⁇ 3 and 351, 352, 353, 451, 452.
  • di ⁇ tribution line ⁇ can also be provided to other reaction stages.
  • Overflow clarified water lines 312 ... , 412 from several ⁇ ludge ⁇ eparator ⁇ in the mid-to-downstream sections of the system are also provided for the ⁇ torm event flows.
  • the system In dry weather, the system is operated the same way as described for the system shown in Fig. 2.
  • the exce ⁇ influent above the maximum dry weather flow, i ⁇ split in the chamber 16 and stage ⁇ 301 ..., 402. Therefore, portion ⁇ of the influent are bypa ⁇ ing ⁇ everal up ⁇ tream reaction stages.
  • the influent during the storm event i ⁇ diluted by the ⁇ torm water, i ⁇ u ⁇ ually le ⁇ polluted, and need ⁇ less treatment. Accordingly, bypa ⁇ ed portion ⁇ will get sufficient treatment.
  • Fig. 7 depicts a possible layout of the novel system with counterflow of wastewater and sludge ⁇ and with multiple functional zone ⁇ along the proce ⁇ train.
  • the system may include anaerobic, an intermittent aerobic-facultative, anoxic, aerobic and polishing zones.
  • An anaerobic functional zone comprise ⁇ the reaction stage 101, sludge separator 100, and the sludge conditioner 10 with a ⁇ upernatant ⁇ eparator 14 and a mixing mean ⁇ 15.
  • the reaction ⁇ tage may be any apparatu ⁇ ⁇ elected from an empty tank type, a fluidized bed reactor, a packed bed fixed or floating media reactor, or a biofiltration type reactor. Wa ⁇ tewater influent line 1 i ⁇ connected to the reaction zone 101 equipped with a mixing mean ⁇ 115.
  • a pa ⁇ ageway 131 for anaerobic mixed liquor connect ⁇ the anaerobic reaction ⁇ tage to the down ⁇ tream ⁇ ection of the proce ⁇ train.
  • the ⁇ ludge separator 100 may be any suitable mean ⁇ u ⁇ ed for ⁇ ludge separation: a gravity settling tank, a suspended sludge blanket clarifier (for example, such as shown in Fig. 7, see also the U.S. Patent No. 4,472,358), a flotator, a centrifuge, or a filter.
  • Intake pas ⁇ ages 110 for the anaerobic mixed liquor connect the reaction stage 101 to the suspended sludge blanket clarifier 100.
  • Conveying mean ⁇ 125 are provided for ⁇ ettled and, po ⁇ ibly, partially compacted sludge, thi ⁇ mean ⁇ being connected to the ⁇ ludge line ⁇ 121 and 122 going to the reaction ⁇ tage 101 and the ⁇ ludge conditioner 10.
  • Line 12 and conveying means 11 are provided for transferring the conditioned sludge from the sludge conditioner 10 to the reaction stage 101.
  • Line 13 i ⁇ provided for the discharge of the conditioned sludge.
  • the supernatant separator may also be any means for ⁇ olid-liquid separation.
  • An Imhoff settling trough is shown in Fig. 7.
  • a pas ⁇ ageway 31 for the supernatant connects the means 14 to the reaction stage 101.
  • the intermittent aerobic-facultative zone comprise ⁇ a reaction ⁇ tage 201 equipped with aeration mean ⁇ 216, mixing mean ⁇ 215, and a ⁇ ludge ⁇ eparation mean ⁇ 200 similar to that as ⁇ ociated with the anaerobic reaction zone.
  • a passage 131 for the mixed liquor from the previous stage, a passage 111 for the clarified water from the previous stage, and optional raw influent feed lines 2 and 3 are connected to the reaction stage 201.
  • Mean ⁇ 225 for conveying sludge and lines 221 and 222 are provided with the sludge separator 200.
  • Passage ⁇ 231 and 211 for transferring the mixed liquor and the clarified water to the down ⁇ tream proce ⁇ s ⁇ tage are provided.
  • the anoxic zone i ⁇ ⁇ imilar to the intermittent aerobic- facultative zone.
  • Major elements of this zone are the reaction ⁇ tage 301 and the associated ⁇ ludge separator.
  • This zone is equipped similarly to the previou ⁇
  • the la ⁇ t proce ⁇ zone is also similar to the preceding zones. It also includes two major elements: the reaction stage 501 and the sludge separation stage 500. Similar equipment is al ⁇ o shown in the drawing.
  • An optional mixer may be provided in the reaction zone 501.
  • the reagent feed line ⁇ 541, 542, 543 ... are provided for pH control, for coagulant ⁇ , polymers, PAC, hydrogen peroxide, etc.
  • the line 512 for the effluent from the sludge separator in this zone i ⁇ provided.
  • An optional line 511 with conveying means 513 connects the effluent line 512 to the influent line 1.
  • An optional flow control mean ⁇ 514 a ⁇ shown in Fig. 5 may also be provided.
  • the sy ⁇ tem of Fig. 7 i ⁇ operated a ⁇ follow ⁇ The influent is fed via line 1 into the reaction stage 101 of the anaerobic functional zone.
  • organic particles in the influent are partially solubilized by the hydrolyzing microorgani ⁇ ms, the ⁇ oluble organic ⁇ thus formed and those originally present in the influent are at least partially converted into fatty acids by the acidogenic organisms, and the fatty acids are at least in part converted into methane by the methanogenic organisms.
  • the mixed liquor containing particles of biological sludge formed by these organism ⁇ i ⁇ transferred into the suspended sludge blanket clarifier 100 through pas ⁇ ages 110.
  • Some nonconditioned sludge may be recycled to the reaction stage 101 via line 121.
  • the effects produced by the sludge conditioner are described in the co-pending patent application No. 08/046,788 dated 04/12/93.
  • Supernatant may be separated in unit 14 from the sludge being conditioned and transferred to the reaction ⁇ tage 101 via pa ⁇ age 31.
  • the conditioned sludge is recycled to the reaction stage 101 via line 12 by means 11.
  • the contents of the reaction stage 101 and the sludge conditioner 10 are mixed by the mixers 115 and 15.
  • Nitrates and nitrites fed with the recycled effluent, if any, are reduced to nitrogen and water.
  • Sulfur in sulfur-containing compounds, organic or mineral is reduced to hydrogen ⁇ ulfide.
  • a fraction of hydrogen sulfide is u ⁇ ed to precipitate heavy metal ⁇ , ⁇ ome sulfides react with nonreduced sulfate and incompletely reduced sulfite to form elemental sulfur, and some sulfides are ⁇ pent to reduce the nitrate ⁇ and nitrite ⁇ to nitrogen and ⁇ ulfur.
  • the mixed liquor from the anaerobic functional zone, the clarified effluent from the clarifier a ⁇ ociated with the anaerobic functional zone, and, optionally, part of the influent, are fed into the intermittent aerobic-facultative zone through line ⁇ and pa ⁇ sage ⁇ 131, 111, and 2 and 3.
  • the sludge separated in the anoxic functional zone is also fed into thi ⁇ zone.
  • the content ⁇ of the zone are periodically aerated by mean ⁇ 216 and mixed by mean ⁇ 215 during the balance of the time.
  • Part of the aerobic-facultative sludge is recirculated from the sludge separator 200 with the help of means 225 via line 221.
  • the wa ⁇ tewater constituents are subjected to the action of aerobic and facultative organism ⁇ .
  • facultative period biological processes involve destruction of organics, growth of facultative anaerobes, suppre ⁇ ion of the filamentous growth, and phosphorus release from the sludge.
  • aerobic period the biological proces ⁇ e ⁇ involve microbial growth, de ⁇ truction of organic ⁇ , and pho ⁇ phoru ⁇ uptake.
  • nitrification may occur during the aerobic period. In such a case, denitrification will occur during the facultative period.
  • the mixed liquor and the clarified water from the intermittent aerobic-facultative zone are fed to the anoxic zone via passage ⁇ 231 and 211, and ⁇ eparated ⁇ ludge from the aerobic functional zone i ⁇ fed via line 422.
  • the content of the zone is mixed by mean ⁇ 315.
  • Nitrate ⁇ and nitrite ⁇ generated in the aerobic functional zone and transferred with the ⁇ eparated ⁇ ludge to the anoxic zone are reduced with the simultaneous oxidation of organics.
  • the mixed liquor and the clarified water from the anoxic functional zone are fed into the aerobic functional zone (reaction stage 401), via passages 331 and 311, and separated sludge from the polishing zone (reaction ⁇ tage 501), is backfed into the aerobic functional zone through the line 422.
  • the mixed liquor and the clarified water from the aerobic functional zone are fed into the polishing functional zone (reaction stage 501), via passages 431 and 411.
  • the volume of the reaction stage 501 i ⁇ aerated and mixed by mean ⁇ 516 and 515 (not ⁇ hown).
  • the effluent is polished: BOD and COD, and specific organic ⁇ are additionally removed and residual nitrogen is oxidized. Because concentration ⁇ of organics and ⁇ ludge are low, the ⁇ econdary pollution of the effluent by the product ⁇ of die-off and ly ⁇ is is minimized.
  • organic ⁇ of the "internal bacterial juice ⁇ ", pho ⁇ phoru ⁇ , nitrogen and heavy metal ⁇ are not emitted in the water in noticeable quantities.
  • Fig. 8 illustrate ⁇ another po ⁇ ible layout of the pre ⁇ ent ⁇ ystem.
  • the ⁇ y ⁇ tem comprises the anaerobic reaction stage 101 dispo ⁇ ed above multiple sludge conditioning ⁇ ection ⁇ , or compartments, 10a, 10b, etc.
  • the anaerobic reaction stage and sludge conditioning sections are equipped with a sludge ⁇ eparation device 100, such as an Imhoff trough, having an outlet 111, a mixing means 115, mean ⁇ 131 for tran ⁇ ferring the mixed liquor, influent feed pipe 1, and line 12 for ⁇ ludge recycle from the sludge conditioners to the anaerobic reaction stage 101 with a pump 11, and a line 13 for ⁇ ludge discharge.
  • Line 12 is conditionally shown only in compartment 10a, however, it i ⁇ provided in all ⁇ ludge conditioning compartment ⁇ .
  • the combined reaction- ⁇ ludge-separation stage 201 consists of two sections: a downflow section 201a and an upflow section 201b. These sections are hydraulically connected via opening 290.
  • Section 201b i ⁇ a fixed bed upflow filter with a ⁇ tone, plastic or other medium.
  • section 201b may be partially filled with a fluidizable media, such as sand, granular activated carbon, crushed porous baked clay (ceramsite) or other suitable medium.
  • the fluidizable medium is preferred in case ⁇ when a risk of plugging the fixed medium exists.
  • Adsorption media such as carbon, or attached bioma ⁇ , con ⁇ titute an active material in the bed.
  • Pipe 310 connect ⁇ the reaction stage 301 to the sludge ⁇ eparator 300.
  • the clarified water from the separator is removed via line 311, and the separated sludge i ⁇ withdrawn from the separator's bottom via pipe 324 with a pump 325, and transferred to the reaction ⁇ tage ⁇ 301, 201a and 101 through line ⁇ 321, 323 and 322 re ⁇ pectively.
  • Wastewater is fed into the anaerobic reaction stage 101 and i ⁇ mixed by the mixing device 115 with the anaerobic sludge grown in this stage and conditioned in the ⁇ ludge conditioner 10. Some conditioned sludge i ⁇ recycled via line 12 by a pump 11.
  • the clarified water and mixed liquor from the anaerobic stage and the mixed liquor from the aerobic ⁇ tage 301, and optionally, ⁇ eparated sludge from the separator 300, are fed to the downflow section 201a of the reaction stage 201.
  • the flows from the stage 301 via pipe 365 and from ⁇ ludge separator 300 via lines 321, 322 and 323 may carry substantial quantities of nitrates and nitrites.
  • the mixture of waters and aerobic and anaerobic sludges is directed through opening 290 into the upflow section 201b.
  • nitrate ⁇ and nitrite ⁇ are reduced by denitrifying organisms to nitrogen and water. Some nitrites and nitrates will be reacting with poorly degradable, recalcitrant and toxic organic ⁇ .
  • nitrate ⁇ and nitrites may be added in the section 201a or at the bottom of the ⁇ ection 201b to increa ⁇ e the effect of oxidation of such organics.
  • the stage 201 described in thi ⁇ embodiment i ⁇ a novel reaction- ⁇ eparation method and device in which part of the ⁇ ludge is retained (grown and immobilized) on the GAC, and another portion is pa ⁇ ed through with the PAC (or in form of biological flock found in u ⁇ ual sludge).
  • the fluidized bed may be formed by a granular anaerobic sludge grown with PAC.
  • the adsorption capacity of either GAC, or granular sludge with PAC i ⁇ regenerated biologically using active agents associated with aerobic and anaerobic sludges simultaneously present in the sy ⁇ tem.
  • Aerobic biochemical proce ⁇ e ⁇ occur in the reaction ⁇ tage 301, po ⁇ sibly with the nitrification.
  • the nitrogen control in the effluent i ⁇ provided by chemically reacting ammonia and nitrite ⁇ and nitrate ⁇ and biological reduction of nitrate ⁇ and nitrite ⁇ in the reaction- ⁇ eparation ⁇ tage 201.
  • Pho ⁇ phoru ⁇ control i ⁇ provided by partial biological uptake and by addition of iron and aluminum coagulants to the reaction stage 301.
  • FIGs. 9 and 10 there i ⁇ ⁇ hown an alternative apparatu ⁇ for practicing the method of this invention.
  • the apparatus con ⁇ i ⁇ t ⁇ of an anaerobic reaction stage 101 made of several compartments 101a, 101b, etc., an anaerobic sludge conditioner 10 located centrally relative the said anaerobic compartment ⁇ 101, an aerobic reaction stage 201 dispo ⁇ ed above the anaerobic compartment ⁇ 101 and the sludge conditioner 10, and a sludge separator 200 located in the upper section of the aerobic reaction stage 201.
  • the anaerobic compartment ⁇ 101a, 101b, 101c, etc. can be a free volume ⁇ ection with a fluidized granular anaerobic ⁇ ludge, or, optionally, be loaded with fluidizable coarse bed media ⁇ uch a ⁇ ⁇ and, granular activated carbon, or cru ⁇ hed packed porou ⁇ clay (ceram ⁇ ite) or they may have a fixed bed of ⁇ tone or pla ⁇ tic contact medium or other packing type. Granular anaerobic sludge with or without PAC can also be used as a fluidizable material.
  • the aerobic reaction zone 201 can optionally be packed with a support material providing the attached growth as in submerged biofilters.
  • the aerobic ⁇ tage i ⁇ equipped with aerator ⁇ 216 Feed line 1 for the influent i ⁇ connected to a constant flow box 514, this line continue ⁇ downward and i ⁇ connected to a ring pipe 1R having branche ⁇ la, lb, lc, etc. with valve ⁇ for each anaerobic compartment 101a, 101b, 101c, etc.
  • a line 265 with a pump 264 connect ⁇ aerobic ⁇ tage 201 to the anaerobic compartment ⁇ 101 via line ⁇ 1, 1R and branche ⁇ la, lb, lc, etc.
  • Line 12 and pump 11 connect the bottom part of the ⁇ ludge conditioner via the ring pipe 1R and branche ⁇ la, lb, lc, etc.
  • Pipe 13 i ⁇ the ⁇ ludge di ⁇ charge.
  • Pipe 210 connect ⁇ the volume of the aerobic ⁇ tage 201 to the ⁇ eparator 200, which i ⁇ ⁇ hown here a ⁇ a vertical flow clarifier.
  • An airlift 225 is installed in the clarifier 200 and i ⁇ connected to a pipe 221 for tran ⁇ ferring the ⁇ eparated ⁇ ludge to the aerobic reaction stage 201.
  • Pipe 211 further connected to pipe 512 i ⁇ provided at the clarifier 200 of the effluent di ⁇ charge.
  • the effluent recycle pipe 211 with a pump 213 connect ⁇ the effluent pipe 211 to the con ⁇ tant flow box 514.
  • An overflow pipe 570 connect ⁇ the said box 514 to the effluent line 512.
  • Means 541, 542, 543, etc. for feeding various reagent ⁇ a ⁇ previou ⁇ ly de ⁇ cribed are also provided. These mean ⁇ may be attached to feed ⁇ aid reagent ⁇ to either aerobic reaction stage 201 or anaerobic compartment ⁇ 101.
  • the ⁇ y ⁇ tem is operated as follows. The wastewater influent and the recycled effluent are fed via line ⁇ 1 and 211 into the constant flow box 514. The con ⁇ tant flow of the influent and recycled effluent mixture produced by the box 514 i ⁇ fed via line ⁇ 1, 1R, and la, lb, lc, etc. into the selected compartments 101a, 101b, 101c, etc.
  • a recycled flow of the mixed liquor from the aerobic reaction compartment 201 is fed into the anaerobic compartments 101a, 101b, 101c, etc. by the pump 264 via line 265.
  • One or several compartments can be ⁇ elected by opening or closing valves on branches la, lb, lc, etc.
  • the upflow ⁇ tream ⁇ fed into the selected anaerobic compartments fluidize the bed of biological sludge, or the bed of the coarse material supporting the sludge ( ⁇ and, GAC, ceram ⁇ ite).
  • the original organic material ⁇ and metabolic product ⁇ from the aerobic reaction stage 201 are anaerobically converted in the compartment ⁇ 101 forming anaerobic bioma ⁇ , methane, carbon dioxide, hydrogen, sulfide ⁇ , nitrogen, and residual fatty acids and other organic ⁇ , including residual poorly degradable and toxic con ⁇ tituent ⁇ .
  • GAC is packed in compartments 101 and PAC i ⁇ added to the mixed liquor, preferably in the aerobic reaction ⁇ tage 201, the proce ⁇ se ⁇ occur in the manner as described above.
  • Thi ⁇ anaerobic stage converts organics and inorganics, including nitrogen removal.
  • Recycle via line 265 provide ⁇ a repeated (alternating) anaerobic-aerobic treatment of organic ⁇ and metabolic products.
  • the suspended solid ⁇ and ⁇ ome organic ⁇ are coagulated and flocculated by both the aerobic ⁇ ludge brought in via recycle pipe 265, and the conditioned anaerobic sludge fed via lines 12 and la, lb, lc, etc. and the anaerobic sludge cultivated in the compartment ⁇ 101.
  • the process can further be improved by applying previously described phy ⁇ ical, physical-chemical and chemical action ⁇ to the anaerobic system in compartments 101.
  • the mixed liquor leaving the selected compartments 101 enters an area below the aerators 216 and above the top of compartments 101.
  • part of the sludge settle ⁇ down by gravity into the ⁇ ludge conditioner 10, and onto the top of compartments 101 that are not selected at the time.
  • Anaerobic sludge i ⁇ conditioned in the ⁇ ludge conditioner a ⁇ previou ⁇ ly described.
  • Part of thi ⁇ sludge is recycled to the anaerobic reaction compartment ⁇ 101, and the balance i ⁇ di ⁇ charged through the line 13.
  • Coagulant ⁇ and flocculant ⁇ can be added to improve the sludge settlability and for removal of pho ⁇ phoru ⁇ .
  • PAC and other reagent ⁇ can also be u ⁇ ed with the benefit ⁇ previou ⁇ ly described. If the optional support medium is provided, an attached growth of aerobic biomas ⁇ will occur.
  • the aerobic sludge i ⁇ partially circulating in the aerobic reaction ⁇ tage 201, i ⁇ partially pumped through the anaerobic compartment ⁇ 101 by line 265 and pump 264, and partially precipitates to the anaerobic sludge conditioner 10. Regardless of the pathway, all aerobic sludge is tran ⁇ ferred to the previou ⁇ , anaerobic stage.
  • Modifications to the system presented by Figs. 9 and 10 may include multiple sludge conditioning zones, a single upflow reaction zone, the use of a downflow fixed bed reaction zone in ⁇ tead of the upflow reaction zone, additional poli ⁇ hing zone, for example, a chemical- biological treatment in a biofilter with the addition of PAC and coagulant ⁇ for the purpo ⁇ e ⁇ a ⁇ previously described.
  • the sy ⁇ tem depicted in Fig ⁇ . 9 and 10 can al ⁇ o be u ⁇ ed a ⁇ a sequencing batch reactor with anaerobic-aerobic cycles.
  • the sludge separation means 200 is not required, and an alternative discharge line 512a for the effluent i ⁇ provided.
  • the treated wa ⁇ tewater i ⁇ allowed to ⁇ eparate from the settling sludge. Separated water is decanted. The aerobic sludge remain ⁇ on top of anaerobic compartment ⁇ . A portion of anaerobic and aerobic sludges is conditioned in sludge conditioner 10. Conditioned ⁇ ludge is recycled and periodically discharged from the ⁇ y ⁇ tem.
  • a portion of the reaction compartment ⁇ 101 may be aerobic. In such a ca ⁇ e, aeration mean ⁇ can be provided in the ⁇ e section ⁇ .
  • ⁇ y ⁇ tem given in Fig ⁇ . 9 and 10, either flow-through or batching, can al ⁇ o be used for sludge digestion.
  • a ⁇ y ⁇ tem for treatment of ga ⁇ e ⁇ bearing biodegradable constituents either in gaseou ⁇ or particulate form, or both.
  • a bottom section of the apparatus may be as ⁇ igned for an optional ⁇ ludge conditioner 10.
  • Line 221 with a pump 291 connect ⁇ the ⁇ ludge ⁇ eparator 200 to the top of the reaction ⁇ tage 201.
  • a mean ⁇ 207 for example a ⁇ praying device, is attached to the end of pipe 221 at the top of the reactor stage 201.
  • Lines 111 and 12a with a pump 191 connect a sludge separator 100 to the top of the reaction ⁇ tage 101.
  • Line ⁇ 12 and 12a connect the ⁇ ludge conditioner 10 to the ⁇ praying device 107.
  • a branch 131 connect ⁇ the pipe 12a to the sludge separator 200.
  • Line 13 for sludge discharge is attached to line 12.
  • Line 603 i ⁇ connected to the ⁇ ludge ⁇ eparator at it ⁇ top.
  • Thi ⁇ pipe with a pump 605 and the fresh water feed pipe are connected to a tank 600 (or several tanks) for reagents.
  • Tank 600 i ⁇ connected to the line 221 by a pipe 601 with a metering pump 602.
  • a line 133 for oxygen-containing ga ⁇ (air, or oxygen, or both) i ⁇ connected to the bottom of the reaction ⁇ tage 201.
  • Pipe 512g for discharging the treated gas i ⁇ attached to the top of the reaction ⁇ tage 201.
  • This ⁇ y ⁇ tem is operated as follows;
  • the polluted gas is fed at the bottom of the reaction stage 101 via line lg and flows upward acros ⁇ the packing.
  • Conditioned anaerobic sludge from the sludge conditioner 10 and a clarified, or partially clarified anaerobic supernatant from the top of the sludge separator are fed by pumps 11 and 191 via lines 12, 111, and 12a to the top of the reaction stage 101 and sprayed over the reactor packing by a spraying device 107.
  • the ⁇ prayed mixture of anaerobic ⁇ ludge and ⁇ upernatant come into contact with the ga ⁇ fed into the reaction ⁇ tage 101 and ⁇ crub and ab ⁇ orb a fraction of the pollutants from the gas.
  • Biological growth in the reaction ⁇ tage 101 occurs on the packing (attached growth) and in the ⁇ u ⁇ pen ⁇ ion.
  • Hydrolyzing, acidogenic and ethanogenic microorgani ⁇ m ⁇ are grown in the reactor ⁇ tage 101.
  • Other ⁇ pecialized group ⁇ of organi ⁇ m ⁇ are al ⁇ o pre ⁇ ent, particularly ⁇ ulfate reducer ⁇ .
  • Organic particulate ⁇ ⁇ crubbed in thi ⁇ reactor are at lea ⁇ t partially ⁇ olubilized by the hydrolyzing organi ⁇ m ⁇
  • ⁇ oluble material ⁇ are at lea ⁇ t partially converted into fatty acid ⁇ and carbon dioxide
  • methane, hydrogen, ammonia, and hydrogen ⁇ ulfide by the acidogenic and other organi ⁇ m ⁇
  • fatty acid ⁇ are at lea ⁇ t partially converted into methane and carbon dioxide by the methanogen ⁇ .
  • the mixed liquor is collected on the tray 193 and flow ⁇ into the ⁇ ludge ⁇ eparator 100.
  • the clarified water in the separator is collected at the top and is partially recycled by pump 191 via lines 111 and 12a to the top of the reaction stage 101, and to the reaction stage 201.
  • a fraction of thi ⁇ stream may be periodically or continuou ⁇ ly di ⁇ carded via line 604.
  • the settled sludge goes to the sludge conditioner 10 by gravity.
  • Scrubbed particulates and incompletely digested ⁇ oluble organic ⁇ are additionally digested and converted to the final products of anaerobic processe ⁇ .
  • the ga ⁇ e ⁇ generated in the ⁇ ludge conditioner pa ⁇ through the ⁇ ludge separator 100 become collected under the tray 193 and released to the reaction stage 101 via pipe 171.
  • the conditioned sludge is recycled by pump 11 through lines 12 and 12a to the top of the reaction stage separator 200.
  • a portion of the conditioned ⁇ ludge i ⁇ di ⁇ charged continuou ⁇ ly or periodically through line 13.
  • the feed ga ⁇ is transferred through opening 222 to the reaction ⁇ tage 201 ( ⁇ econd treatment ⁇ tage).
  • the feed ga ⁇ is mixed with oxygen-containing gas fed via line 133.
  • the gas mixture flows upward acro ⁇ the packing in the reaction stage 201 and contacts the downflowing aerobic mixed liquor. This mixed liquor is recycled by the pump 291 via lines 221, and distributed over the packing means 207.
  • Attached and suspended aerobic microorganisms are growing in the reactions stage 201. Residual organic ⁇ , volatile metabolic product ⁇ from the previou ⁇ ⁇ tage, and ammonia and hydrogen ⁇ ulfide are additionally ab ⁇ orbed, and removed from the gas by the biomas ⁇ and water.
  • the bulk of the biodegradable material ⁇ are oxidized to carbon dioxide and water, ammonia i ⁇ partially converted to nitrate ⁇ and nitrite ⁇ , ⁇ ulfide ⁇ are partially oxidized to ⁇ ulfite ⁇ and sulfates. Nitrogen and ⁇ ulfur are partially formed through the chemical reaction ⁇ between ammonia, sulfides, and nitrates and nitrite ⁇ , and sulfites and ⁇ ulfate ⁇ .
  • Additional reagents may be placed into the ⁇ y ⁇ tem by the u ⁇ e of tank ⁇ such as tank 600 with the metering pump 602 and line ⁇ 601 and 221. Addition of PAC re ⁇ ult ⁇ in ad ⁇ orption of pollutants from the gas, thus increa ⁇ ing the proce ⁇ s rate and efficiency.
  • the PAC will take part in the sludge counterflow and will be used in aerobic and anaerobic reaction steps as previously de ⁇ cribed.
  • Other reagent ⁇ can al ⁇ o be u ⁇ ed a ⁇ previou ⁇ ly de ⁇ cribed for the wa ⁇ tewater treatment application ⁇ .
  • a ⁇ pecific reagent, ⁇ ource of carbon, or organics may be needed in the gas treatment ⁇ y ⁇ tems to improve the process ⁇ tability at highly variable, and periodic ga ⁇ loading condition ⁇ , or for ga ⁇ e ⁇ carrying poorly degradable organic ⁇ .
  • nonvolatile organic ⁇ ⁇ hould be u ⁇ ed.
  • Wa ⁇ tewater may al ⁇ o be u ⁇ ed as a source of organic ⁇ .
  • electromagnetic field ⁇ can be applied to reaction ⁇ tage ⁇ in the ga ⁇ treatment ⁇ y ⁇ tem ⁇ imilar to the described wastewater treatment sy ⁇ tem.
  • the embodiment ⁇ illu ⁇ trated in Fig ⁇ . 1 through 11 ⁇ how that various arrangements, including novel apparatuses, for producing unexpected useful effects in the biological treatment of streams loaded with organics can be u ⁇ ed.
  • the novel ⁇ ystem may be used for treatment of wa ⁇ tewater, wa ⁇ te and other gaseous steams, solid waste, such a ⁇ municipal garbage, commercial, indu ⁇ trial and agricultural wa ⁇ te, fossil fuels, and pos ⁇ ible other materials. These material can be treated the same way as wastewater in a slurried form, or in contactors such as de ⁇ cribed for gas treatment, or in apparatuse ⁇ a ⁇ de ⁇ cribed or in apparatu ⁇ es for handling dry (moistened) materials.

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  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
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Abstract

La présente invention concerne un procédé et un dispositif de traitement microbiologique multiphase recevant la matière à traiter (1), et faisant passer cette matière au travers d'un certain nombre de réacteurs (101, 201, 301, 401, 501). Une partie du contenu de chacun des réacteurs est prélevée et soumise à séparation (100, 200, 300, 400, 500), et la biomasse est transférée vers la phase précédente (121, 221, 321, 421, 521) alors que la matière à traiter et les produits métaboliques progressent vers la phase suivante (111, 211, 311, 411). Selon ce procédé, la biomasse s'écoule principalement vers l'amont, alors que la matière à traiter progresse principalement vers l'aval. De préférence, la séquence de réacteurs respecte l'alternance entre réacteur anaérobie et réacteur aérobie, ce qui fait que la matière est soumise à un environnement alternativement anaérobie et aérobie. On peut perfectionner ce traitement en intégrant dans le système des opérations physiques, physico-chimiques, chimiques et biochimiques.
PCT/US1995/000317 1994-01-13 1995-01-09 Traitements microbiologiques a contre-courant WO1995019322A1 (fr)

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AU15623/95A AU1562395A (en) 1994-01-13 1995-01-09 Counterflow microbiological processes
BR9505641A BR9505641A (pt) 1994-01-13 1995-01-09 Processos para o tratamento biológico em multiplos estagios de um material influentes para sequenciar processamento em batelada de refugo liquido em um reator de pelo menos um estágio anearóbico e um aeróbico e para tratar mateirais fluidos e aparelho de tratamento de água de refugo e de gás

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US08/181,387 US5514278A (en) 1993-04-12 1994-01-13 Counterflow microbiological processes
US08/181,387 1994-01-13

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EP2158165A1 (fr) * 2007-05-10 2010-03-03 O'Regan, Patrick T., Jr. Systemes, procedes et composants de traitement des eaux et d'action corrective
US7972512B2 (en) 2007-12-19 2011-07-05 Saudi Arabian Oil Company Suspended media granular activated carbon membrane biological reactor system and process
US8440074B2 (en) 2009-07-08 2013-05-14 Saudi Arabian Oil Company Wastewater treatment system including irradiation of primary solids
US8551341B2 (en) 2009-06-15 2013-10-08 Saudi Arabian Oil Company Suspended media membrane biological reactor system including suspension system and multiple biological reactor zones
US8557111B2 (en) 2009-07-08 2013-10-15 Saudi Arabian Oil Company Low concentration wastewater treatment system
WO2015002552A1 (fr) * 2013-07-04 2015-01-08 Lanzatech New Zealand Limited Système de multiples réacteurs et processus pour fermentation gazeuse continue
CN113248005A (zh) * 2021-04-25 2021-08-13 河海大学 一种利用交替微电场增强反硝化菌活性池及方法
CN113603312A (zh) * 2021-09-13 2021-11-05 北京博汇特环保科技股份有限公司 一种难生物降解的高氨氮废水的综合处理系统及处理方法

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US4200524A (en) * 1978-10-25 1980-04-29 Biospherics Incorporated Bio-surface separation process
US4919815A (en) * 1989-02-06 1990-04-24 Zimpro/Passavant Inc. Two-stage anaerobic/aerobic treatment process

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2158165A4 (fr) * 2007-05-10 2012-04-18 Patrick T O'regan Jr Systemes, procedes et composants de traitement des eaux et d'action corrective
EP2158165A1 (fr) * 2007-05-10 2010-03-03 O'Regan, Patrick T., Jr. Systemes, procedes et composants de traitement des eaux et d'action corrective
US7972512B2 (en) 2007-12-19 2011-07-05 Saudi Arabian Oil Company Suspended media granular activated carbon membrane biological reactor system and process
US8329035B2 (en) 2007-12-19 2012-12-11 Saudi Arabian Oil Company Suspended media granular activated carbon membrane biological reactor system and process
US8551341B2 (en) 2009-06-15 2013-10-08 Saudi Arabian Oil Company Suspended media membrane biological reactor system including suspension system and multiple biological reactor zones
US9340441B2 (en) 2009-07-08 2016-05-17 Saudi Arabian Oil Company Wastewater treatment system including irradiation of primary solids
US8440074B2 (en) 2009-07-08 2013-05-14 Saudi Arabian Oil Company Wastewater treatment system including irradiation of primary solids
US8557111B2 (en) 2009-07-08 2013-10-15 Saudi Arabian Oil Company Low concentration wastewater treatment system
US8721889B2 (en) 2009-07-08 2014-05-13 Saudi Arabian Oil Company Wastewater treatment process including irradiation of primary solids
US9073764B2 (en) 2009-07-08 2015-07-07 Saudi Arabian Oil Company Low concentration wastewater treatment system and process
US9290399B2 (en) 2009-07-08 2016-03-22 Saudi Arabian Oil Company Wastewater treatment process including irradiation of primary solids
WO2015002552A1 (fr) * 2013-07-04 2015-01-08 Lanzatech New Zealand Limited Système de multiples réacteurs et processus pour fermentation gazeuse continue
JP2016523544A (ja) * 2013-07-04 2016-08-12 ランザテク・ニュージーランド・リミテッド 連続ガス発酵のための多段リアクタシステム及びプロセス
US9988598B2 (en) 2013-07-04 2018-06-05 Lanzatech New Zealand Limited Multiple reactor system for continuous gas fermentation
EA031512B1 (ru) * 2013-07-04 2019-01-31 Ланцатек Нью Зилэнд Лимитед Многореакторная система и способ непрерывной ферментации газов
CN113248005A (zh) * 2021-04-25 2021-08-13 河海大学 一种利用交替微电场增强反硝化菌活性池及方法
CN113248005B (zh) * 2021-04-25 2022-09-06 河海大学 一种利用交替微电场增强反硝化菌活性池及方法
CN113603312A (zh) * 2021-09-13 2021-11-05 北京博汇特环保科技股份有限公司 一种难生物降解的高氨氮废水的综合处理系统及处理方法

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AU1562395A (en) 1995-08-01

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