WO2016027223A1 - Système de bioréacteur à membrane anaérobie - Google Patents

Système de bioréacteur à membrane anaérobie Download PDF

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Publication number
WO2016027223A1
WO2016027223A1 PCT/IB2015/056262 IB2015056262W WO2016027223A1 WO 2016027223 A1 WO2016027223 A1 WO 2016027223A1 IB 2015056262 W IB2015056262 W IB 2015056262W WO 2016027223 A1 WO2016027223 A1 WO 2016027223A1
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Prior art keywords
bioreactor
anaerobic
membrane
line
effluent
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Application number
PCT/IB2015/056262
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English (en)
Inventor
Ramakrishna Ramanath SONDE
Raman Venkatraman KALYAN
Janardhan Bhikaji BORNARE
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Thermax Limited
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Application filed by Thermax Limited filed Critical Thermax Limited
Priority to MYPI2017000251A priority Critical patent/MY184894A/en
Publication of WO2016027223A1 publication Critical patent/WO2016027223A1/fr
Priority to PH12017500312A priority patent/PH12017500312A1/en

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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
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2853—Anaerobic digestion processes using anaerobic 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
    • 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
    • C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
    • C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
    • 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
    • C02F2209/001—Upstream control, i.e. monitoring for predictive control
    • 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
    • C02F2209/003—Downstream control, i.e. outlet monitoring, e.g. to check the treating agents, such as halogens or ozone, leaving the process
    • 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
    • C02F2209/03—Pressure
    • 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
    • C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/20—Prevention of biofouling
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present disclosure relates to a system and method for treating wastewater.
  • the present disclosure relates to a bioreactor system for treating wastewater and generating biogas.
  • Anaerobic wastewater treatment processes such as upflow anaerobic sludge blanket (UASB), upflow anaerobic filter process (UAFP), anaerobic fluidized bed bioreactor (AFBR) have several advantages as compared to aerobic processes. These advantages include low energy consumption, low sludge production, and significant energy recovery in terms of biogas. However, these anaerobic processes have a few limitations/challenges, including high hydraulic retention time in the bioreactor, and hence larger footprint, frequent washing out of the culture from the bioreactor, i.e.
  • an anaerobic membrane bioreactor system including:
  • an anaerobic bioreactor in fluid communication with a membrane separation unit
  • said system comprises a feed line connecting at a location proximal to the operative bottom of said bioreactor for conveying an influent; a bioreactor effluent line connecting a location proximal to the operative top of said bioreactor and an inlet to said membrane separation unit for conveying the bioreactor effluent; and a membrane retentate line connecting retentate outlet of said membrane separation unit to at least one functional element of said system selected from said feed line, said bioreactor effluent line, and operative top of said bioreactor, for conveying at least a portion of a retentate stream.
  • the anaerobic bioreactor comprises a feed distribution pipe having a plurality of openings preferably facing the operative bottom of said bioreactor, said feed distribution pipe receiving the influent through said feed line and said feed distribution pipe being adapted for obtaining a fluid upflow in said bioreactor.
  • the operative bottom of said anaerobic bioreactor is conical.
  • said membrane separation unit is a cross-flow membrane unit.
  • said method comprises maintaining the fluid upflow velocity in said bioreactor in the range of 5 - 10 m/hr and maintaining the fluid exit velocity from said plurality of openings of said feed distribution pipe in the range of 1 - 2 m/s.
  • said method comprises discharging a biogas stream from a location near the operative top of said anaerobic bioreactor above the fluid surface.
  • said method comprises spraying at least a portion of said retentate stream through the operative top of said bioreactor to contact said retentate stream with biogas generated in the headspace of said bioreactor.
  • said method comprises feeding at least a portion of said retentate stream through said feed line at the operative bottom of said bioreactor.
  • said method comprises recirculating at least a portion of said retentate stream to said membrane separation unit through said bioreactor effluent line.
  • FIGURE 1 illustrates a schematic of a preferred embodiment of the anaerobic membrane bioreactor system
  • FIGURE 2 illustrates a graphical representation showing the Chemical Oxygen Demand (COD) concentration in the feed and the permeate during performance evaluation of the anaerobic membrane bioreactor system;
  • COD Chemical Oxygen Demand
  • FIGURE 3 illustrates a graphical representation showing the biogas generation and the biogas yield as a function of time during performance evaluation of the anaerobic membrane bioreactor system
  • FIGURE 4 illustrates a graphical representation showing the methane generation and the calculated methane yield as a function of time during performance evaluation of the anaerobic membrane bioreactor system
  • FIGURE 5 illustrates a graphical representation showing the Mixed Liquor Suspended Solids (MLSS) and the Mixed Liquor Volatile Suspended Solids (MLVSS) concentration in the bioreactor as a function of time during performance evaluation of the anaerobic membrane bioreactor system
  • MMS Mixed Liquor Suspended Solids
  • MLVSS Mixed Liquor Volatile Suspended Solids
  • FIGURE 6 illustrates a graphical representation showing the membrane permeate flux as a function of time during performance evaluation of the anaerobic membrane bioreactor system.
  • An anaerobic Membrane Bioreactor can be an effective solution to face the challenge of conventional devices.
  • a membrane coupled system can facilitate independent control of the hydraulic and solid retention within the reactor.
  • AnMBR can facilitate retention of microorganisms and allow operations with high biomass concentrations.
  • an AnMBR is expected to provide more efficient digestion, higher methane production, better effluent quality, and can be smaller in size than conventional anaerobic digesters.
  • the integration of a membrane separation unit with an anaerobic bioreactor can have several advantages, however, the system has a few limitations as listed here below:
  • the biogas produced in the anaerobic membrane bioreactor has low methane content and must be purified separately to enhance the methane content and thereby the calorific value of the fuel gas;
  • the suspended microorganisms in the bioreactor are more useful than the settled bed, and therefore a mixing arrangement is required to keep all biomass in suspension.
  • an agitation system in the anaerobic bioreactor will increase the capital and operational costs of the system; higher concentration of anaerobic microorganisms is required in the mixed liquor of the bioreactor for efficient functioning and conversion of the biodegradable organics into biogas, however the higher concentration of microorganisms in the mixed liquor increases the total suspended solids load for filtration in the membrane separation process, causing membrane fouling.
  • the present disclosure envisages an anaerobic membrane bioreactor system for treating wastewater and generating biogas.
  • the anaerobic membrane bioreactor system of the present disclosure typically includes a cross-flow membrane unit for the solid-liquid separation of the bioreactor effluent, and therefore recyclable quality, suspended solid free treated water is produced.
  • the cross-flow membrane unit is preferably a cross-flow microfiltration or ultrafiltration unit. A portion of the retentate stream from the membrane separation unit with relatively higher concentration of anaerobic microorganisms is recycled back to the anaerobic bioreactor, thus making it possible to carry out the operation at higher biomass concentrations as compared to the conventional aerobic and anaerobic systems.
  • This higher concentration of anaerobic microorganisms in the bioreactor reduces the hydraulic retention time, and enhances the treatment efficiency and quality of the treated effluent. Also, the system has a smaller footprint. Since the membrane is acting as a physical barrier for retention of microorganisms in the bioreactor, the system can be used for the treatment of tough to degrade effluent without washing out of the anaerobic microorganisms. A lower food to microbe ratio in the system increases efficiency of the system leading to higher biogas generation and biogas yield. Since the biological growth and yield of anaerobic microorganisms is relatively lower than the aerobic microorganisms, sludge generation is much lower in the anaerobic membrane bioreactor system.
  • the biological sludge has a tendency to settle down in the bioreactor if mixing is not provided.
  • a higher concentration of biomass can be achieved at the bottom of the bioreactor whereas medium concentration of microorganisms can be obtained in the middle zone.
  • the bioreactor has minimal concentration of microorganisms in the top most zone of the bioreactor with surface floating scum containing solids.
  • the bioreactor effluent discharge is taken from a location proximal to the operative top of the bioreactor below the fluid surface to avoid scum entry in the bioreactor effluent.
  • This elevated discharge of the bioreactor effluent avoids extra loading of biological solids for membrane filtration. This helps in reducing membrane fouling and improving the membrane filtration performance. This not only helps in reducing fouling but also reduces the requirement of chemicals, the chemical cleaning frequency, enhances life of the membrane, and thereby reduces the operating cost of the membrane.
  • a minimum fluid cross-flow velocity for the fluid to avoid membrane fouling governs the recirculation flow. Thus, a portion of the membrane retentate stream is recycled to the bioreactor and allowed to enter at the operative bottom.
  • the liquid upflow velocity in the bioreactor (in the range of 5-10 m/hr) helps in keeping all the biomass in suspension and avoid the mechanical mixer/agitator. The biomass settling in the bioreactor is not preferable since organic substrate and microorganism contact is necessary for efficient operation of the bioreactor.
  • FIGURE 1 of the accompanying drawings A preferred embodiment of the anaerobic membrane bioreactor system of the present disclosure is illustrated in the FIGURE 1 of the accompanying drawings; the system is generally referenced by numeral 100 in the FIGURE 1.
  • the system 100 includes the anaerobic bioreactor 106 provided in fluid communication with the membrane separation unit 116.
  • the membrane separation unit 116 can be a cross-flow microfiltration or ultrafiltration membrane unit.
  • the system comprises a feed line 124 connecting to a location proximal to the operative bottom of the bioreactor 106 for conveying an influent flow, a bioreactor effluent line 126 connecting a location proximal to the operative top of the bioreactor 106 to an inlet of the membrane separation unit 116 for conveying the bioreactor effluent, and a membrane retentate line 128 connecting a retentate outlet of the membrane separation unit 116 to the feed line 124, the bioreactor effluent line 126, and the operative top of the anaerobic bioreactor 106.
  • the influent flow is sprayed in the anaerobic bioreactor 106 through a feed distribution pipe 122.
  • the feed distribution pipe 122 contains a plurality of openings, preferably facing the operative bottom of the bioreactor 106, such that fluid discharged through the feed distribution pipe 122 gains an upward flow. This upward fluid flow helps in maintaining the biomass in suspension.
  • the bioreactor 106 may preferably have a cylindrical shell.
  • the bioreactor 106 may also suitably have a square or rectangular shell.
  • the operative bottom of the bioreactor 106 is preferably conical to maintain the biomass in suspension.
  • the influent is purged in the conical zone of the bioreactor 106. This arrangement does not demand agitation system for the bioreactor.
  • a sludge drain 130 is provided at the operative bottom of the bioreactor 106 for draining sludge from the bioreactor 106.
  • the sludge drain 130 includes a drain valve for controllably draining the excess sludge produced in the bioreactor 106.
  • the raw wastewater is pumped as influent by a feed pump 104 from a feed tank 102 through the feed line 124 at the operative bottom of the anaerobic bioreactor 106 containing anaerobic microorganisms in suspension.
  • the influent is sprayed in the bioreactor 106 through the feed distribution pipe 122 which produces a fluid upflow velocity in the range of 5 - 10 m/hr, which is sufficient to maintain the biomass in suspension during the process.
  • the fluid exit velocity from the plurality of openings of the feed distribution pipe 122 is maintained in the range of 1 - 2 m/s.
  • the anaerobic microorganisms degrade the organic matter in the wastewater to produce a bioreactor effluent.
  • the biomass is stratified in a bottom zone of the bioreactor 106 and the bioreactor effluent with fewer solids can be discharged from a location near the operative top of the bioreactor 106 and below the fluid surface to prevent scum being carried with the effluent.
  • the bioreactor effluent is discharged at 108 through the bioreactor effluent line 126.
  • Biogas produced during the process may be intermittently discharged at a location near the operative top of the bioreactor 106 above the fluid surface at point 110.
  • the biogas may be collected in a biogas collection tank (not shown).
  • the bioreactor effluent carried through the bioreactor effluent line 126 is pumped by membrane feed pump 112 to the membrane separation unit 116.
  • Excess sludge in the bioreactor 106 may be drained through the sludge drain 130 to maintain the designed concentration of biosolids in the bioreactor 106.
  • the quantum of sludge drain from the reactor depends on solid load in the influent and solid properties. Solid retention time for the bioreactor is in the range from 200 - 300 days.
  • the drained sludge may be further treated separately or disposed directly as per the discharge guidelines.
  • the bioreactor effluent is filtered in the membrane separation unit 116 to remove solids and produce a treated permeate stream 120 and a retentate stream 118.
  • a first portion 118a of the retentate stream is recirculated to the membrane separation unit 116 by membrane recirculation pump 114.
  • a second portion 118b of the retentate stream is circulated to the bioreactor 106 as influent with the wastewater to maintain the concentration of microorganisms in the bioreactor 106 during the process.
  • a third portion 118c of the retentate stream is sprayed at the operative top of the bioreactor 106 to contact with the biogas in the headspace of the bioreactor 106.
  • the anaerobic membrane bioreactor system of the present disclosure was tested for treatment of synthetic wastewater.
  • a cylindrical configuration of bioreactor was designed and fabricated in stainless steel.
  • the bioreactor was fully automatic, equipped with necessary instrumentation and controls to operate the system at optimum process parameters.
  • a skid mounted membrane separation unit consisting of membranes, pumps, flow meters, pressure gauges and piping, was designed. Microfiltration / ultrafiltration membrane modules were used for solid-liquid separation.
  • treated water flow rate (permeate flow rate): X liters/hr;
  • feed flow rate to the bioreactor X lit/hr
  • bioreactor head space height 10 - 20 % of total reactor height
  • liquid depth in the bioreactor 80 - 90 % of total reactor height
  • discharge connection (outlet) of the bioreactor at a distance of 10 % liquid depth from the liquid surface in the bioreactor.
  • a low strength synthetic wastewater representing domestic sewage, consisting of glucose and other nutrients was used for the study.
  • the synthetic substrate was prepared to provide necessary inorganics and micronutrients, as well as nitrogen, phosphorus for the development of the biomass.
  • the initial seeding of the bioreactor was carried out by inoculating the bioreactor with anaerobic sieved sludge collected from an anaerobic wastewater treatment plant. Sufficient nitrogen gas was purged in the bioreactor for creating anaerobicity in the reactor after seeding the sludge. Initially the biomass was allowed to acclimatize with fed synthetic wastewater in the bioreactor.
  • Synthetic feed solution was prepared in the feed tank and continuously fed to the bioreactor during the performance evaluation period.
  • the bioreactor effluent was pumped through membrane modules arranged outside the bioreactor. A portion of the reject (retentate) from the membrane module was recycled to the bioreactor.
  • the bioreactor effluent was recirculated through the membrane modules at a constant flow rate to maintain sufficient cross-flow velocity on membrane surface.
  • the permeate flow rate from the external membrane was set a little higher than the influent flow rate with recycling the excess permeate because it was practically difficult to precisely keep a constant flux during continuous operation.
  • the excess biomass produced in the bioreactor during operation was drained periodically to maintain the designed concentration of biomass in the reactor.
  • the solid retention time in the bioreactor was in the range from 200-300 days.
  • Feed and permeate samples were tested on a daily basis for pH and chemical oxygen demand (COD). Periodic sampling was also carried out from the bioreactor for the analysis of mixed liquor suspended solids (MLSS) and mixed liquor volatile suspended solids (MLVSS). The generated biogas was measured on daily basis during the study. All analyses were performed according to standard methods for the examination of water and wastewater. A standard practice of membrane cleaning was adopted for chemical cleaning.
  • COD chemical oxygen demand
  • FIGURE 2 illustrates a graphical representation showing the COD concentration in the feed and the permeate during the performance evaluation of the anaerobic membrane bioreactor system. After stabilization of the biological performance, the total suspended solids (TSS) and the COD average removals were 100% and greater than 94%, respectively.
  • TSS total suspended solids
  • FIGURE 3 illustrates a graphical representation showing the biogas generation and the biogas yield as a function of time during the performance evaluation of the anaerobic membrane bioreactor system. Average Biogas generation was 250 liters/day. The generated biogas was analyzed for methane composition on periodic basis and found varying from 69 % to 86 %.
  • FIGURE 4 illustrates a graphical representation showing the methane generation and the calculated methane yield as a function of time during the performance evaluation of the anaerobic membrane bioreactor system. The average biogas and methane yields were 0.44 and 0.35 m /kg COD removed. As indicated in the FIGS. 3 & 4, it was observed that the biogas and methane generation were stable after stabilization of the biological process.
  • biomass concentration in the bioreactor was reduced slightly and then stabilized in the later phase.
  • sampling was carried out from the bottom and top zone of the bioreactor for analyzing the concentration of biosolids in the bioreactor.
  • the mixed liquor suspended solids (MLSS) concentration in the bottom zone of the bioreactor was found higher than the top zone.
  • the MLSS in the bottom zone of the bioreactor was in the range from 10852 mg/1 to 13369 mg/1.
  • concentration of MLSS in the top zone of the bioreactor was varied in the range from 8195 mg/1 to 9849 mg/1.
  • the mixed liquor volatile suspended solid (MLVSS) concentration in the samples collected from the top zone of the bioreactor was in the range from 5327 mg/1 to 6943 mg/1.
  • the average MLSS in the bottom and top zone of the bioreactor were 12042 and 9040 mg/1, respectively.
  • the average MLVSS in the samples collected from the top zone of the bioreactor was 6184 mg/1.
  • FIGURE 5 illustrates a graphical representation showing the MLSS and the MLVSS concentration in the bioreactor as a function of time during the performance evaluation of the anaerobic membrane bioreactor system.
  • the conversion of complex organic matter to methane and carbon dioxide is possible only by the common action of at least four different groups of microorganisms.
  • the essential microbial complex comprises hydrolytic bacteria, fermenting bacteria, acetogenic bacteria and methanogenic Archaea.
  • a mixed microflora of different species was isolated for pure species and identified as Clostridium sp., Ruminococcus sp., Smithella sp., Slelnomonas sp., Bacteriodes sp., Succinomonas sp., Pelotomaculum sp., Desuljotomaculum sp., Methanobacterium sp., Methanothermobacter sp., Methanobrevibacter sp., Methanosarcina sp., Methanosaeta sp.
  • FIGURE 6 illustrates a graphical representation showing the membrane permeate flux as a function of time during performance evaluation of the anaerobic membrane bioreactor system at transmembrane pressure below 1 bar.
  • the membrane flux decline was relatively higher in the initial phase of filtration; however it was stabilized in the later phase of operation.
  • the filtration flux was found in the range from 110 LMH to 70 LMH during the period of two months before chemical cleaning of the membrane.
  • the obtained flux was found 50 % higher than reported in the literature for the conventional system, which is typically in the range of 45 - 60 LMH.
  • the obtained higher flux could be due to the lesser MLSS observed in the top portion of the bioreactor.
  • the lesser concentration of biosolids in the treated effluent might have improved filtration performance of the membrane. This not only reduced fouling but also reduced frequency of chemical cleaning of the membrane.
  • the anaerobic membrane bioreactor system and method thereof, as described in the present disclosure, has several technical advantages including, but not limited to, the realization of: requires a low hydraulic retention time, provides high treatment efficiency, and produces reusable quality treated effluent and biogas having high calorific value; controls membrane fouling, thereby reducing the use of chemicals, the chemical cleaning frequency, increasing the life of the membrane, and thus reducing the operating costs of the membrane;

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  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Molecular Biology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un système de bioréacteur à membrane anaérobie (100) et un procédé associé. Le système (100) comprend un bioréacteur anaérobie (106) en communication fluidique avec une unité de séparation à membrane (116). Le système (100) comprend une conduite d'alimentation (124) se raccordant au niveau d'un emplacement proximal à la partie inférieure opérationnelle du bioréacteur (106) pour transporter un influent, une conduite d'effluent de bioréacteur (126) se raccordant au niveau d'un emplacement proximal à la partie supérieure opérationnelle du bioréacteur (106) et une admission dans l'unité de séparation à membrane (116) pour transporter l'effluent de bioréacteur, et une conduite de concentré de membrane (128) raccordant l'évacuation de concentré de l'unité de séparation à membrane (116) à au moins un élément fonctionnel sélectionné parmi la conduite d'alimentation (124), la conduite d'effluent de bioréacteur (126) et la partie supérieure opérationnelle du bioréacteur (106) permettant de transporter au moins une partie d'un flux de concentré. Fig. 1
PCT/IB2015/056262 2014-08-19 2015-08-18 Système de bioréacteur à membrane anaérobie WO2016027223A1 (fr)

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MYPI2017000251A MY184894A (en) 2014-08-19 2015-08-18 Anaerobic membrane bioreactor system
PH12017500312A PH12017500312A1 (en) 2014-08-19 2017-02-20 Anaerobic membrane bioreactor system

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Cited By (5)

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CN108328869A (zh) * 2018-03-07 2018-07-27 中科瑞阳膜技术（北京）有限公司 厌氧膜生物反应器及废水处理系统
CN110214128A (zh) * 2016-12-21 2019-09-06 维利亚水务解决方案及技术支持公司 使用反渗透或纳滤处理来自anmbr的滤液
CN111892159A (zh) * 2020-06-24 2020-11-06 清华大学 厌氧膜生物反应器及膜污染控制方法
WO2021206550A1 (fr) * 2020-04-07 2021-10-14 Christiaan Emanuel Zagt Bioréacteur à membrane anaérobie de construction à pression générative améliorée et procédé de travail amélioré pour la production de gaz vert
CN114195262A (zh) * 2021-10-29 2022-03-18 清华大学 厌氧摆动膜生物反应器

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EP2641877A1 (fr) * 2012-03-20 2013-09-25 Veolia Water Solutions & Technologies Support Procédé de traitement d'un flux de déchets à l'aide d'un bioréacteur et d'un filtre à membrane

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US7648634B2 (en) * 2005-04-19 2010-01-19 Procorp Enterprises, Llc Method for wastewater treatment
EP2641877A1 (fr) * 2012-03-20 2013-09-25 Veolia Water Solutions & Technologies Support Procédé de traitement d'un flux de déchets à l'aide d'un bioréacteur et d'un filtre à membrane

Cited By (7)

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CN108328869A (zh) * 2018-03-07 2018-07-27 中科瑞阳膜技术（北京）有限公司 厌氧膜生物反应器及废水处理系统
CN108328869B (zh) * 2018-03-07 2023-07-18 中科瑞阳膜技术（北京）有限公司 厌氧膜生物反应器及废水处理系统
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CN111892159A (zh) * 2020-06-24 2020-11-06 清华大学 厌氧膜生物反应器及膜污染控制方法
CN114195262A (zh) * 2021-10-29 2022-03-18 清华大学 厌氧摆动膜生物反应器

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