Gotowa bibliografia na temat „MBBR TECHNOLOGY”

A hybrid moving bed biofilm reactor–membrane bioreactor (hybrid MBBR-MBR) system was studied as an alternative solution to conventional activated sludge processes and membrane bioreactors. This paper shows the results obtained from three laboratory-scale wastewater treatment plants working in parallel in the start-up and steady states. The first wastewater treatment plant was a MBR, the second one was a hybrid MBBR-MBR system containing carriers both in anoxic and aerobic zones of the bioreactor (hybrid MBBR-MBRa), and the last one was a hybrid MBBR-MBR system which contained carriers only in the aerobic zone (hybrid MBBR-MBRb). The reactors operated with a hydraulic retention time of 30.40 h. A kinetic study for characterizing heterotrophic biomass was carried out and organic matter and nutrients removals were evaluated. The heterotrophic biomass of the hybrid MBBR-MBRb showed the best kinetic performance in the steady state, with yield coefficient for heterotrophic biomass = 0.30246 mg volatile suspended solids per mg chemical oxygen demand, maximum specific growth rate for heterotrophic biomass = 0.00308 h−1 and half-saturation coefficient for organic matter = 3.54908 mg O2 L−1. The removal of organic matter was supported by the kinetic study of heterotrophic biomass.

A combined process consisted of a Moving-Bed Biofilm Reactor (MBBR) and chemical coagulation was investigated for textile wastewater treatment. The pilot scale MBBR system is composed of three MBBRs (anaerobic, aerobic-1 and aerobic-2 in series), each reactor was filled with 20% (v/v) of polyurethane-activated carbon (PU-AC) carrier for biological treatment followed by chemical coagulation with FeCl2.In the MBBR process, 85% of COD and 70% of color (influent COD=807.5 mg/L and color=3,400 PtCo unit) were removed using relatively low MLSS concentration and short hydraulic retention time (HRT=44 hr). The biologically treated dyeing wastewater was subjected to chemical coagulation. After coagulation with FeCl2, 95% of COD and 97% of color were removed overall. The combined process of MBBR and chemical coagulation has promising potential for dyeing wastewater treatment.

The moving bed biofilm reactor (MBBR) wastewater treatment process is usually designed based on the assumption that all activity in the process occurs in the biofilm on the MBBR carriers, although there is always some active biomass in the bulk liquid due to biofilm sloughing and, sometimes, free-growing bacteria. In this study the removal of organic matter is evaluated in laboratory-scale MBBR reactors under varying load, hydraulic retention time (HRT), oxygen concentration and volumetric filling degree of carriers in order to determine the heterotrophic activity in the different fractions of the MBBR biomass. The results showed that the heterotrophic conversions in an MBBR can show the same type of diffusion limited dependency on oxygen as nitrification, even for easily degradable substrates such as acetate. The contribution to the removal from the suspended biomass is shown to vary depending on HRT, as the amount of suspended solids changes. The developed method in this report is a useful tool for determining heterotrophic activity in the separate fractions of biomass in MBBRs.

The effect of moving bed biofilm reactor (MBBR) loading rate on membrane fouling rate was studied in two parallel units combining MBBR and membrane reactor. Hollow fiber membranes with molecular weight cut-off of 30 kD were used. The HRTs of the MBBRs varied from 45 min to 4 h and the COD loading rates ranged from 4.1 to 26.6 g COD m−2 d−1. The trans-membrane pressure (TMP) was very sensitive to fluxes for the used membranes and the experiments were carried out at relatively low fluxes (3.3–5.6 l m−2 h−1). Beside the test with the highest flux, there were no consistent differences in fouling rate between the low- and high-rate reactors. Also, the removal efficiencies were quite similar in both systems. The average COD removal efficiencies in the total process were 87% at 3–4 h HRT and 83% at 0.75–1 h HRT. At high loading rates, there was a shift in particle size distribution towards smaller particles in the MBBR effluents. However, 79–81% of the COD was in particles that were separated by membranes, explaining the relatively small differences in the removal efficiencies at different loading rates. The COD fractionation also indicated that the choice of membrane pore size within the range of 30 kD to 0.1 μm has very small effect on the COD removal in the MBBR/membrane process, especially with low-rate MBBRs.

Abstract The suspended solids (SS) concentrations in effluent from moving bed biofilm reactors (MBBRs) used for secondary biological treatment can be up to 500 mg/L. Microscreens (Drumfilters or Discfilters) can be used as alternatives to traditional clarification or dissolved air flotation to remove SS and total phosphorus (TP). This study shows how a small-scale municipal WWTP for 5,700 population equivalent (PE) can be upgraded to 12,000 PE by combining MBBR with coagulation-flocculation tanks and a Discfilter with a total footprint of 160 m2. This long-term investigation demonstrated that even though influent turbidity (range 146–431 NTU) and flow (25–125 m3/h) varied considerably, very low effluent turbidities (below 10 NTU) could be achieved continuously. Furthermore, this compact treatment system can provide average reductions of ammonium (NH4-N) from 19 to 0.04 mg/L, COD from 290 to 10 mg/L, and TP from 4.5 to 0.3 mg/L. The results show that effluent requirements can be reached by combining MBBR, coagulation-flocculation and disc filtration at full scale, without a primary clarifier upstream of MBBR.

A moving bed biofilm reactor (MBBR) pilot plant, using Kaldnes type K1 biofilm carriers, was tested for nitrogen removal at the FREVAR wastewater treatment plant. The pilot plant was fed primary treated municipal wastewater, at temperatures from 4.8 to about 20°C. The results showed that a reasonable design nitrification rate will be 190 g TKN/m3d, at 10°C and a reactor pH≥7.0. Pre-denitrification was very dependent on the concentration of readily biodegradable organic matter and the amount of oxygen in the influent to the first anoxic MBBR. It was found that a MBBR process for nitrogen removal at FREVAR will require a total reactor volume corresponding to an empty bed hydraulic retention time of 4–5 hours at average design influent flow. This was based on an influent concentration of 25 mg total N/l, 70% annual average removal of total N and a treatment process consisting of primary treatment, MBBRs with combined pre- and post-denitrification, and followed by coagulation/flocculation and a final solids separation stage.

Abstract Fluidization of carrier media for biofilm support and growth defines the moving bed biofilm reactor (MBBR) process. Major MBBR facilities apply virgin polyethylene (PE)-based circular plastic carrier media. Various carriers were studied to replace these conventional carriers, but polyurethane (PU) foam-based carrier media has not been much explored. This study evaluates the potential of PU foam carrier media in aerobic MBBR process for simultaneous nitri-denitrification (SND). Two parallel reactors loaded with conventional PE plastic (circular) and PU foam (cubical) carriers compared for their removal efficiencies of chemical oxygen demand (COD) and nitrogen contaminants from wastewater. Results indicate that average COD removal in MBBR containing PE plastic carrier media was 81%, compared to 83% in MBBR containing PU foam. Average ammonical and total nitrogen reduction was 71% and 59% for PU foam-based MBBR, compared to 60% and 42% for PE plastic-based MBBR. SND-based nitrogen removal capacity was doubled in aerobic MBBR filled with PU foam carrier media (27%), than MBBR containing PE plastic carrier media (13%). Cost economics also governs the commercial advantage for the application of PU foam-based carrier media in the MBBR process.

Moving bed biofilm reactor combined with membrane bioreactor (MBBR-MBR) constitute a highly effective wastewater treatment technology. The aim of this research work was to study the effect of commercial K1 biocarriers (MBBR-MBR K1 unit) and 3D-printed biocarriers fabricated from 13X and Halloysite (MBBR-MBR 13X-H unit), on the efficiency and the fouling rate of an MBBR-MBR unit during wastewater treatment. Various physicochemical parameters and trans-membrane pressure were measured. It was observed that in the MBBR-MBR K1 unit, membrane filtration improved reaching total membrane fouling at 43d, while in the MBBR-MBR 13X-H and in the control MBBR-MBR total fouling took place at about 32d. This is attributed to the large production of soluble microbial products (SMP) in the MBBR-MBR 13X-H, which resulted from a large amount of biofilm created in the 13X-H biocarriers. An optimal biodegradation of the organic load was concluded, and nitrification and denitrification processes were improved at the MBBR-MBR K1 and MBBR-MBR 13X-H units. The dry mass produced on the 13X-H biocarriers ranged at 4980–5711 mg, three orders of magnitude larger than that produced on the K1, which ranged at 2.9–4.6 mg. Finally, it was observed that mostly extracellular polymeric substances were produced in the biofilm of K1 biocarriers while in 13X-H mostly SMP.

Moving Bed Biofilm Reactor (MBBR) systems have been proven as an effective technology for water treatment and have been used for Biochemical Oxygen Demand/Chemical Oxygen Demand (BOD/COD-removal), as well as for nitrification and denitrification in municipal and industrial wastewater treatment. Conventional Activated Sludge (CAS), in particular, has been extensively used in wastewater treatment since decades ago. In this study, physical performance results for both MBBR and CAS were compared and evaluated on laboratory scale basis. The study aims to identify the best system performance in terms of constituent removal efficiency for effective management of the river purification plant. A novel parallel MBBR and CAS pilot plant were fabricated and operated to compare the physical performance of MBBR and CAS. Analysis of the performances for MBBR and CAS show, MBBR has higher COD (85%), AN (75%) and TSS (80%) removal rate compared to CAS COD (53%), AN (53%) and TSS (69%). For BOD removal rate, CAS shows 68% removal rate whereas MBBR shows only 65%. Thus CAS has shown slightly higher removal rate than MBBR. In terms of sludge production, MBBR sludge is less than CAS. Overall performance proves that MBBR has better rate of constituent removal efficiency compared to CAS in the laboratory basis study.

The aim of the described experimentation was the comparison of a low cost MBBR and an activated sludge system (AS). The MBBR applied system consists of the FLOCOR-RMP® plastic media with a specific surface area of about 160 m2/m3 (internal surface only). The comparison with activated sludge (AS) was performed by two parallel treatment lines. Organic substance removal and nitrification were investigated over a 1-year period. Comparing the results obtained with the two lines, it can be observed AS totCOD removal efficiencies were higher than MBBR ones; the average efficiencies for totCOD removal were 76% for MBBR and 84% for AS. On the contrary, the solCOD removals resulted alike (71% for both systems). In spite of the remarkable variations of wastewater temperature, mainly in winter (range of 5–21°C), the average ammonium removal efficiency resulted 92% for MBBR and 98% for AS. With an ammonium loads up to 1.0 g m2 d−1 (up to 0.12 kg m−3 d−1), nitrification efficiencies in MBBR were more than 98%. At higher loads decrease in the MBBR efficiency was registered; that is related to the increase in the applied COD load.

By rethinking wastewater treatment plants (WWTPs) as resource recovery facilities, it is possible to de- velop the next generation of WWTPs. Moreover, it allows to accomplish environmental goals, such as reducing the CO2 footprint, and comply with increasing effluent standards regarding the concentration of nitrogen in a more sustainable way. This research study aims to analyse the possibility of recirculating carbon within WWTPs in form of volatile fatty acids (VFAs) produced by co-fermentation of primary sludge and food waste. The obtained fermentation liquid is utilised as carbon source to enhance the denitrification process in a post-anoxic denitrification plant setup. Two pilot scale fermentation reactors were semi-continuously operated, systematically varying only in pH. By controlling one reactor to pH 10, while the second reactor was operated without pH control, it was possible to assess the influence of the pH on the carbon recovery process. Despite the pH not being controlled in the second fermentation reactor, it adjusted itself to a stable pH around 5.4. The co-fer- mentation process was monitored by weekly analysis of the SCOD and total amount of VFAs (TVFA). While the alkaline conditions in the reactor operated at pH 10 allowed a higher hydrolysis of the sub- strate, the second reactor, operated without pH control, achieved a more distinct acidification, due to the lower pH. Consequently, the SCOD in the reactor operated without pH control contains a higher percentage of TVFA amounting to 64 % in comparison to the reactor operated at pH 10 with 40 % TVFA. Furthermore, the achieved degree of fermentation was assessed by calculating the net increase of TVFA per gram of VS, respectively VSS. A higher degree of fermentation was achieved without pH control, resulting in a higher VFA yield compared to the fermentation reactor operated at pH 10. Moreover, anal- ysis of the individual VFAs by gas chromatography showed distinct differences in the composition of the fermentation liquids. According to the findings, the reactor operated at pH 10 produced mainly acetic acid (61 %), followed by propionic acid (18 %) and n-butyric acid (14 %). In contrast, the fermentation reactor operated without pH control produced mainly n-caproic acid (47 %), followed by acetic acid (25 %) and n-butyric acid (16 %). Despite the similar fermentation substrate supplied to both reactors, the acidic conditions in the reactor operated without pH control allowed carboxylic acid chain elongation from acetic acid to n-caproic acid, resulting in the main difference of the fermentation liquids. The fermentation liquid of the two reactors was filtered, diluted to a concentration of 5 g COD/L and supplied as additional carbon source to enhance denitrification in two continuously operated pilot scale moving bed biofilm reactors (MBBR), applying a carbon-to-nitrogen ratio of 4.5. One of the denitrifica- tion MBBRs received the carbon recovered by fermentation at pH 10 as external carbon source, whereby the carbon source produced by fermentation without pH control was supplied to the other MBBR. The maximal achieved denitrification rate was quite similar for both MBBRs amounting to 3.25 g NO3- Neq/(m2·d) for the MBBR receiving the carbon source recovered by co-fermentation at pH 10 and 3.38 g NO3-Neq/(m2·d) for the MBBR receiving the VFA-mix obtained by co-fermentation without pH control. However, the MBBR provided with the carbon source recovered by co-fermentation under acidic conditions achieved a higher average denitrification rate of 2.5 g NO3-Neq/(m2·d), compared with the MBBR receiving carbon produced by co-fermentation at pH 10 (1.8 g NO3-Neq/(m2·d)). The lower efficiency of the MBBR supplied with additional carbon recovered by fermentation at pH 10 is caused by an accumulation of NO2-N during the denitrification process. This accumulation of NO2-N indicates suboptimal conditions, both due to the composition of the supplied carbon source and an overall higher pH during the denitrification process, which might supress facultative anaerobes, such as denitrifiers. Nevertheless, this study shows that both VFA-rich carbon sources obtained by co-fermentation of pri- mary sludge and food waste are suitable to enhance denitrification of municipal wastewater, with the carbon source recovered by fermentation without pH control achieving a higher denitrification effi- ciency.
Eine Neuinterpretation kommunaler Klärwerke als Rohstoff-Rückgewinnungsanlagen ermöglicht die Entwicklung der Kläranlagen der Zukunft. Umweltziele, wie die Reduktion des CO2-Fußabdrucks und die Einhaltung steigender Abwasserstandards im Hinblick auf die Stickstoffkonzentration können somit nachhaltiger erreicht werden. Diese Forschungsstudie zielt darauf ab, die Möglichkeit der Rückführung von Kohlenstoff in Kläranlagen in Form leichtflüchtiger Fettsäuren (engl. volatile fatty acids, VFAs) zu untersuchen. Diese VFAs werden durch Co-Fermentation von Primärschlamm und Lebensmittelabfäl- len erzeugt und als zusätzliche Kohlenstoffquelle einer nachgeschalteten Denitrifikation zugeführt, um die Prozesseffizienz zu steigern. Zur Erzeugung der VFAs wurden zwei Fermentationsreaktoren halbkontinuierlich im Pilotmaßstab be- trieben, welche systematisch im pH-Wert variierten. Der Einfluss des pH-Wertes auf den Kohlenstoff- rückgewinnungsprozess konnte beurteilt werden, indem ein Reaktor auf pH 10 geregelt wurde, während dieser im zweiten Reaktor nicht beeinflusst wurde. In diesem stellte sich aufgrund ablaufender Reakti- onen ein stabiler pH-Wert um 5,4 ein. Der Co-Fermentationsprozess wurde durch wöchentliche Analyse des gelösten chemischen Sauerstoffbedarfs (engl. soluble chemical oxygen demand, SCOD) und der Ge- samtmenge an VFAs (TVFA) überwacht. Während die alkalischen Bedingungen in dem bei pH 10 be- triebenen Reaktor eine höhere Hydrolyse des Substrats ermöglichten, erreichte der zweite Reaktor auf- grund des niedrigeren pH-Werts eine stärkere Versäuerung. Folglich enthält der SCOD in dem Reaktor, der ohne pH-Regelung betrieben wurde, mit 64 % einen höheren Anteil an TVFA im Vergleich zu dem bei pH 10 betriebenen Reaktor mit 40 % TVFA. Außerdem wurde der erreichte Fermentationsgrad durch Berechnung der Nettozunahme der TVFA pro Gramm flüchtige Feststoffe (VS) bzw. flüchtige suspendierte Feststoffe (VSS) erfasst. Ein höherer Fer- mentationsgrad konnte ohne pH-Regelung erzielt werden, welche eine höhere VFA-Ausbeute im Ver- gleich zur Fermentation bei pH 10 zeigt. Deutliche Unterschiede in der Zusammensetzung der gewon- nenen VFAs konnten durch Analyse mittels Gaschromatographie erfasst werden. Demzufolge entstand bei der Fermentation bei pH 10 hauptsächlich Essigsäure (61 %), gefolgt von Propionsäure (18 %) und n-Buttersäure (14 %). Im Gegensatz dazu, produzierte der Fermentationsreaktor ohne pH-Regelung überwiegend n-Capronsäure (47 %), gefolgt von Essigsäure (25 %) und n-Buttersäure (16 %). Trotz des gleichen Fermentationssubstrates, welches beiden Reaktoren zugeführt wurde, ermöglichen die sauren Bedingungen in dem Fermentationsreaktor ohne pH-Regelung, eine Verlängerung der Carbonsäureket- ten von Essigsäure zu n-Capronsäure. Nach Filtration der in verschiedenen Milieus gewonnenen Fermentationssubstrate und Verdünnung auf eine Konzentration von 5 g COD/L, wurden diese zwei im Pilotmaßstab kontinuierlich betriebenen Fließbett-Biofilmreaktoren (engl. Moving bed biofilm reactor, MBBR) als zusätzliche Kohlenstoffquelle zur Denitrifikation zugeführt. Über die gesamte Versuchsdauer wurden ein MBBR mit dem alkalisch gewonnenen und der Andere mit dem im sauren Milieu erzeugten VFA-Mix betrieben. Das Kohlenstoff- Stickstoff-Verhältnis (C/N Ratio) lag dabei bei 4,5. Beide MBBRs wiesen eine vergleichbare maximale Denitrifikationsrate von 3,25 g NO3-Neq/(m2·d) (VFAs pH 10) und 3,38 g NO3-Neq/(m2·d) (VFAs pH un- geregelt) auf. Der MBBR, welcher die im sauren Milieu rückgewonnene Kohlenstoffquelle erhielt, er- reichte im Durchschnitt eine höhere Denitrifikationsrate von 2,5 g NO3-Neq/(m2·d) als der MBBR, der den bei pH 10 gewonnenen VFA-Mix erhielt (1,8 g NO3-Neq/(m2·d)). Die im Vergleich geringere Effizi- enz der alkalisch rückgewonnenen Kohlenstoffquelle wird durch eine NO2-N-Anreicherung während der Denitrifikation verursacht, welche suboptimale Bedingungen während des Prozesses indiziert. Dies ist sowohl auf die Zusammensetzung der zugeführten Kohlenstoffquelle, als auch auf einen insgesamt hö- heren pH-Wert während des Reduktionsprozesses zurückzuführen, der fakultative Anaerobier, wie bspw. Denitrifikanten, unterdrücken kann. Dessen ungeachtet zeigt diese Studie, dass beide durch Co- Fermentation von Primärschlamm und Lebensmittelabfällen gewonnenen VFA-reichen Kohlenstoff- quellen zur Verbesserung der Denitrifikation kommunalen Abwassers geeignet sind, wobei die durch Fermentation ohne pH-Regelung erzeugte Kohlenstoffquelle eine höhere Effizienz aufweist.
Det är möjligt att utveckla den nya generationen av avloppsreningsverk genom att ompröva avloppsreningsverk som resursanläggning. Därtill möjliggör det att uppnå miljömål som att minska koldioxidavtrycket och följa ökande utsläppskrav, t.ex. för kvävekoncentration, på ett mer hållbart sätt. Denna forskningsstudie syftar till att analysera möjligheten att återcirkulera kol inom reningsverket i form av lättflyktiga fettsyror (engl. volatile fatty acids, VFAs), producerades genom samfermentering av primärslam och matavfall. Det erhållna fermenteringssubstratet används som extern kolkälla för att förbättra processeffektiviteten i en efterdenitrifikationsanläggning. Två pilotskaliga fermenteringsreaktorer drevs i semikontinuerligt driftläge med endast en skillnad i pH. Det var möjligt att utvärdera pH-påverkan på kolåtervinningsprocessen genom att kontrollera pH- värdet i en reaktor till pH 10, medan den andra reaktorn drevs utan pH-kontroll. På grund av reaktionerna som fortlöpte, justerade sig den icke-kontrollerade reaktorn själv till ett stabilt pH runt 5,4. Samfermenteringsprocessen övervakades genom veckoanalys av kemisk syreförbrukning i filtrerade prover (engl. soluble chemical oxygen demand, SCOD) och total mängd av VFAs (TVFA). Medan den alkaliska miljö i den första reaktorn gynnade en högre hydrolys av substratet, uppnådde den andra reaktorn en mer tydlig surgöring på grund av det lägre pH-värdet. Följaktligen innehåller SCOD i reaktorn som drivs utan pH-kontroll en större andel TVFA – 64 % av SCOD - jämfört med reaktorn som drivs vid pH 10, där TVFA utgör 40 % av SCOD. Vidare analyserades den uppnådda fermenteringsgraden genom att beräkna nettoökningen av TVFA per gram VS, respektive VSS. En högre jäsningsgrad uppnåddes i sur miljö, vilket resulterade i en högre VFA-produktion jämfört med fermenteringsreaktorn som drevs vid pH 10. Därtill visade analys med gaskromtografi av de individuella VFA tydliga skillnader i sammansättning av substraten. Enligt rönen producerade reaktorn vid pH 10 mestadels ättiksyra (61 %) följt av propionsyra (18 %) och n-smörsyra (14 %). Däremot producerade fermenteringsreaktorn utan pH-kontroll mestadels n-kapronsyra (47 %) följt av ättiksyra (25 %) och n-smörsyra (16 %). Detta visar att trots att samma fermentationssubstrat användes för båda reaktorerna möjliggör den sura miljön i reaktorn utan pH-kontroll karboxylkedjeförlängningen från ättiksyra till n-kapronsyra. Fermentationssubstraten av de två reaktorerna filtrerades, utspäddes till en koncentration av 5 g COD/L och tillfördes som extern kolkälla, med ett kol/kväve-förhållande på 4,5, för att förbättra denitrifikationen i två kontinuerliga drivna biofilmreaktorer med rörliga bärare (engl. moving bed biofilm reactor, MBBR). En MBBR erhöll under hela experimentets gång den kolkälla som bildats under alkaliska förhållanden och den andra MBBR:en erhöll motsvarande kolkälla som bildats i den sura miljön i fermenteringsreaktorn utan pH-kontroll. Den maximala uppnådda denitrifikationskapaciteten var ganska likartad för båda MBBR: 3,25 g NO3-Neq/(m2·d) för den MBBR som opererades med den alkaliska erhållen kolkällan och 3,38 g NO3-Neq/(m2·d) för MBBR som erhöll den utspädda fermenteringsvätskan bildad utan pH-kontroll. Emellertid uppnådde den MBBR som erhöll kolkällan bildad i sura miljön en högre genomsnittlig denitrifikationskapacitet på 2.5 g NO3-Neq/(m2·d) jämfört med MBBR som fick kolkällan producerad genom fermentering vid pH 10 (1.8 g NO3-Neq/(m2·d)). Den lägre effektiviteten i den MBBR som fick den alkaliskt erhållna kolkällan orsakas av en ansamling av NO2-N under denitrifikationsprocessen, vilket indikerar suboptimala förhållanden. Detta beror både på sammansättningen av den tillförda kolkällan och ett högre totalt pH-värde under reduktionsprocessen, vilket kan hämma fakultativa anaerober såsom denitrifierare. Trots det visar denna forskningsstudie att båda de VFA-rika kolkällorna erhållna genom samfermentering av primärslam och matavfall är lämpliga för att förbättra denitrifikationen av kommunalt avloppsvatten, varvid kolkällan som produceras genom fermentering utan pH-kontroll uppnår en högre denitrifikationseffektivitet.

This diploma thesis is focused on the topic of membrane technologies used in wastewater treatment. The research part of the thesis deals with membrane separation of activated sludge, and the focus is on the submerged membrane modules. The thesis contains basic principles of MBR systems, an overview of used membrane modules, modes of operation, advantages and disadvantages of using this process. The practical part of the thesis proposes the intensification of WWTP Perná with using MBR technology. This part includes the technical-economic assessment of the activation WWTP with the third stage of treatment and activation WWTP with MBR.

This membrane aerated biofilm reactor (MABR) pilot project was performed at Ekeby wastewater treatment plant (WWTP) in Eskilstuna, Sweden. This plant is facing a future challenge of effluent TN < 10mg/L according to the new standard and the growing population, where higher treatment capacity is needed. The MABR as a newly invented technology, is chosen as a promising countermeasure towards the challenge, because of the simultaneous nitrification and denitrification of this technology. By the time of reporting, this project is still on-going, and more information will be reported later in separate report. The feed water comes from the secondary clarifier of full-scale plant. Dissolved oxygen (DO), processing air and flow rate was manually controlled to test different operational settings. However, there were a lot challenges during the testing period which makes it hard to evaluate the performance of this pilot. The ammonium removal efficiency is satisfying when the pilot was running smoothly. However, the TN removal efficiency did not comply with the expectation, achieved in average of 39,01%, due to the limitation of readily bio-degradable COD (rbCOD), which is a limitation of the biological process in general and is not specific to MABR. This technology is considered as promising by the end of the current testing period, since it can oxidize the ammonium effectively with smaller volume.
Detta pilotprojekt med membranluftad biofilmreaktor (MABR) utfördes på Ekeby avloppsreningsverk i Eskilstuna, Sverige. Denna anläggning står inför en framtida utmaning med utflöde-TN <10 mg / L enligt den nya standarden och den växande befolkningen, där högre behandlingskapacitet behövs. MABR som nyutvecklad teknik, väljs som en lovande motåtgärd för utmaningen på grund av den samtidiga nitrifikationen och denitrifikationen med denna teknik. Vid rapporteringstillfället är projektet fortfarande pågående och mer information kommer att rapporteras senare i separat rapport. Matarvattnet kommer från den sekundärfällningen i fullskaleanläggningen. Löst syre (DO), bearbetningsluft och flödeshastighet kontrollerades manuellt för att testa olika driftsinställningar. Det fanns emellertid många utmaningar under testperioden vilket gör det svårt att utvärdera prestanda för denna pilot. Ammoniumavlägsningsgraden var tillfredsställande när piloten körde smidigt. TN-avlägsningseffektiviteten som i genomsnitt uppnådde 39,01% TN-avlägsning motsvarade emellertid inte förväntan, på grund av begränsningen av lätt biologisk nedbrytbar COD (rbCOD), vilken är en begränsning av den biologiska processen i allmänhet och inte specifik för MABR. Denna teknik anses vara lovande vid slutet av den aktuella testperioden, eftersom den kan oxidera ammoniumen effektivt med en mindre volym.

Vid Hammarby Sjöstadsverk drivs en pilotanläggning som är en mindre skala av det framtida avloppsreningsverket i Henriksdal. Delar av reningsprocessen består av membranbioreaktorer. I pilotanläggningen finns en zon kallad RAS-DeOx dit returslammet från membrantankarna och rejektvattnet från slambehandlingen leds. Luftning av membrantankarna gör att returslammet är syrerikt och rejektvattnet innehåller mycket ammonium.Zonen fungerar som ett nitrifikationssteg då syret i returslammet kan oxidera ammoniumet från rejektvattnet. Dessutom kan zonen minska syrehalterna i returslammet för att undvika att det hamnar i pilotanläggningens fördenitrifikation. För att få bättre uppfattning om vad som sker i zonen och hur denna fungerar som ett nitrifikationssteg studerades nitrifikation, denitrifikation och syreförbrukningen i zonen. För att utvärdera RAS-DeOx-zonen belastades den med olika nivåer av ammonium från rejektvattnet vid olika hög luftning i membrantankarna. Detta utfördes både experimentellt direkt på pilotanläggningen och i en simuleringsstudie där processimuleringar genomfördes i en simuleringsmodell. I modellen utvärderades även två styrstrategier för zonen.Resultaten från studierna visade att både nitrifikation och denitrifikation förekom i zonen. Jämfört med simuleringsstudien varierade omfattningen av nitrifikation och denitrifikation mer i den experimentella studien. Båda studierna visade att det fanns risk att syre hamnande i pilotanläggningens fördenitrifikation. Styrstrategierna visade att det inte var fördelaktigt för pilotanläggningens resurseffektivitet att zonen luftades vid hög ammoniumbelastning från rejektvattnet. Det visade sig också att det var ingen större skillnad när det gällde pilotanläggningens prestation vid högt, lågt eller styrt returflöde för zonen. Däremot skiljde sig prestationen mer avseende luftning och koldosering.Utöver att det förekom nitrifikation och denitrifikation i zonen bedömdes den även fungera som ett nitrifikationssteg för ammoniumet i rejektvattnet. Dessutom minskade den syrehalterna i returslammet. Hur väl ammonium nitrifierades och syre förbrukades i zonen berodde på förhållandena i pilotanläggningen och förhållandet mellan mängden ammonium och syre i zonen.
At Hammarby Sjöstadsverk there is a pilot plant which is a smaller version of the future wastewater treatment plant at Henriksdal. Parts of the treatment process steps are membrane bioreactors. There is a zone in the pilot plant which is called RAS-DeOx to where the return activated sludge from the membrane tanks and the reject water from the sludge treatment are pumped. The return activated sludge contains oxygen since the membranetanks are aerated and the reject water has high contents of ammonium.The zone works as a nitrification step for the ammonium in the reject water, and also reduces the oxygen levels in the return sludge to avoid oxygen in the pilot plant's pre-denitrification step. To aquire a better understanding of what occurs in the zone and how it functions as a nitrification step; nitrification, denitrification and oxygen consumption was studied in the zone. To evaluate the RAS-DeOx-zone it was loaded with different loads of ammonium from the reject water at different levels of aeration in the membrane tanks. This was evaluated both experimentally at the pilot and in a simulation model of the pilot. In the simulation model two control strategies for the zone were also evaluated.It was shown that both nitrification and denitrification occurred in the zone. Furthermore, both studies showed that there is a risk that oxygen occurs in pilot's pre-denitrification step if the ammonium load in zone was low. Then, all of oxygen in the zone was not consumed. As for the control strategies, it was shown that the benefits were low for the resource efficiency of the pilot when the zone was aerated during high loads of ammonium. The performance of the pilot was similiar for high, low and regulated return flows for the zone, but the aeration and carbon dosage in the pilot differed.Besides that both nitrification and denitrification occurred in the zone, it was also functioning as a nitrification step for the ammonium from the reject water. The oxygen from the return sludge was reduced as well. The extent of nitrification and consumption of oxygen in the zone depended on the circumstances in the pilot and the relationship between the amount of oxygen and ammonium.

The Yamuna River runs through Noida on the west and southwest, while the Hindon River runs through it on the east and south. Noida is a part of the Yamuna River's catchment area. In the last 10 years, Noida has become a center for the real estate, electronics, and software development sectors. As a result, an beneath land network of conduits for the discharge of wastewater generates in the complex area is necessary to relieve pressure on existing municipal sewage treatment facilities. The sewage system for the complex was designed to take into account the natural slope. Three STPs for large group housings are being proposed in Noida: STP Group Housing 1 in sector 71 uses MBBR (Moving Bed Biofilm Reactor) technology, STP Group Housing 2 in sector 136 uses MBR (Membrane Bioreactor) technology, and STP Group Housing 3 in Greater Noida West Sector 1 uses SBR (Sequential Batch Reactor) technology. These facilities are designed and constructed with the purpose of eliminating organic material, sediments, and other pollutants from waste water before it reaches a water source. The effluent from these STPs is used for flushing water, irrigation, and the rest of the discharge into Municipal Drains. Many Physio-Chemical and Biological parameters are evaluated and compared in this study to the Central Pollution Control Board (CPCB) General Standards for the Discharge of Environmental Pollutants Part–A: Effluents into Inland Surface Water, as set forth in The Environment (Protection) Rules, 1986 Schedule–VI. Each STP's performance was also assessed in terms of Removal/Reduction Efficiency. Because Group Housing 1, uses 390 KLD of STP treated waste water for irrigation, the average effluent of this STP is compared to the CPCB Effluent Discharge Standards into Land for Irrigation. According to the findings, the BOD value of STP 2 and STP 3 effluent was not under the permissible level for the period of the research, and the Average Phosphate value of STP 3 was exactly up to the limit, as directed by the Central Pollution Control Board. General Standards for the Discharge of Environmental Pollutants Part –A: Effluents into Inland Surface Water is established by the Environment (Protection) Rules, 1986 Schedule-VI. According to the findings, according to CPCB Effluent Discharge Standards into Land for Irrigation and Inland Surface Water, all of the Physio-Chemical and Biological parameters examined for STP 1 were within limits.

碩士
國立交通大學
環境工程系所
100
Along with the technical progress, the people live are getting more and more convenient, however, behind the gorgeous high tech product there is depletion of resources and huge waste. The water resource, which people are closely linked, is indispensable for the producing processes of high-technology industry. The high-technology industry not only has the huge requirement to the water resources, the wastewater produced from producing processes is an important topic. In recent years, with the environmental consciousness upward in Taiwan, the wastewater emission standard of high-technology industry is sterner, and the ammonia nitrogen in the wastewater will be limited in the future. The effect of supplementary carbon addition for the treatment of high-technology industrial wastewater in a membrane bioreactor (MBR) was investigated. The MBR was operated for 346 days under different C/N (BODL/ NH4- -N) ratios, i.e. 0.9, ~ 1 to 20 days; 1.6, ~ 21 to 42 days; 2.8, ~ 43 to 82 days; 3.6, ~ 83 to 141 days; 4.9, ~ 165 to 233 days and 9.6, ~ 240 to 346 days. Irrespective of the C/N ratios investigated, SS and BOD5 removal efficiencies were above 95%. Also, above 80% COD removal efficiency was observed in the entire C/N ratio investigated. In addition, complete nitrification was observed throughout the investigation. However, denitrification and total nitrogen removal efficiencies reached their maximum values at the highest C/N ratio i.e. 9.6 investigated. Real-time PCR analysis revealed 10 times higher ammonia oxidizing bacteria to total bacteria ratio under the highest C/N ratio condition (9.6) compared to the low C/N ratio condition (0.9). In addition, Nitrospira is the main nitrite oxidizing bacteria (NOB).

Transitional and marine coastal discharges are gaining more attention due to the increase of human pressures on coastal areas. The proposal for wastewater biomonitoring via brackish and salt water toxicity testing organisms on an end-of-pipe basis can provide information about wastewater treatment plants management, wastewater treatment technologies efficiency in toxicity reduction/removal and final discharge potential hazard. Activated sludge sequencing batch reactor, ultra-filtration membrane biological reactors, activated carbon and reverse osmosis were checked in small and medium sized configurations for their discharge quality. Domestic/hotel, mixed domestic, septic tank and industrial (glass factory), TNT, table olive brine and aircraft washing wastewaters were assessed before and after their relative treatment process via Artemia franciscana, Vibrio fischeri, Crassostrea gigas and Mytilus galloprovincialis toxicity tests. All the main physico-chemical parameters were also provided. The ultra-filtration membrane biological reactors showed to improve more efficiently the quality of the discharge from both the physico-chemical and the ecotoxicological point of view, suggesting more support by regulatory authorities on their implementation. Moreover, it was evidenced that A. franciscana is not suitable for wastewater toxicity testing, whereas all other bioassays are relatively sensitive and reliable.

AbstractLiquid water, with a vapor pressure of 6.1 mbar at freezing point, is rapidly evaporating in high vacuum, rapidly cooling off by the evaporative cooling, and is freezing to ice almost instantly. Nevertheless, liquid water free vacuum surfaces can be prepared for short instances when injecting very small, fast flowing, liquid jets into high vacuum. They provide perfectly suited targets for molecular beams analysis of molecular evaporation of monomers and dimers from liquids. Also, the microjet technology allows ultrahigh vacuum studies of atomic scale liquid surface composition and electronic structures, as will be demonstrated by using highly focused Synchrotron radiation for EUV/XUV-photoelectron spectrocopy on a wide range of chemical solutions.

We describe a wafer level fabrication process for evacuated Rb vapor cells. By etching channels on the wafer surface around the cell positions, we demonstrate wafers of cells with residual gas pressures below 5 mbar.

With improving optical device technology it is now possible to consider constructing very large optoelectronic neural networks containing of the order of 1000 fully interconnected neurons. Whether such systems will work, though, depends on the quality of the optical devices and the network architecture. A recent study has indicated that a 200 neuron single layer polarization logic network can operate under the constraints of presently available spatial light modulators.1 In this paper we will extend this study to examine the effect of device limitations on the performance of single- and multilayer networks containing up to 1000 fully interconnected neurons. We consider the effect of nonlinearities, contrast ratio, and quantization noise in the weight matrix and the effect of noise at the inputs and outputs on the convergence rate and number of patterns that can be classified.

The integrated-optic technology can provide rugged and compact devices/circuits for fiber sensors such as gyro [1,2] and LDV (laser Doppler velocimeter) [3,4]. In particular, the integrated-optic LDV seems to be promising for the practical use, because the Doppler-shifted signal light can be steadily heterodyne-detected via waveguides and fibers without influence of phase fluctuation caused by ambient temperature change. Very recently, we demonstrated the integrated-optic LDV pigtailed with a polarization-maintaining fiber, in which the whole heterodyne optics was integrated on a LiNbO3 [3,4]. This is called the reference-beam (one-beam) type of LDV. On the other hand, the relatively higher signal-to-noise ratio is in general obtained in the differential (two-beam) type of LDV [5]. The latter type has more often been used in practice for velocity measurement. In this paper, we propose and demonstrate a novel integrated-optic differential LDV consisting of a LiNbO3 waveguide device and a micro Fresnel lens (MFL) array.

In coherent atomic and molecular laser spectroscopy, the capability to synthesize a temporally shaped laser pulse is a valuable asset. Experimental and theoretical work on pulse shaping in coherent spectroscopy has shown that precise control over the radiation field can enhance direct and multiphoton excitation or selectively excite an electronic or high vibrational state in a molecular system[1]. Complicated phase and amplitude modulated pulse shapes, such as [sech(at) ](1+3i), have been shown to be insensitive to inhomogeneous broadening, and do not undergo severe distortion due to optical density[2]. In addition to nonlinear laser spectroscopy, pulse shaping technology has been applied to several problems in nonlinear optics. In particular, it has been applied to soliton propagation in fibers where pulse shaping techniques have been used to observe new aspects of optical soliton propagation. Synthesis of tailored pulses with complicated amplitude and phase envelopes has enabled direct observations of complex solitons[3], and of "dark solitons"[4]. Both soliton families have detailed temporal and phase envelopes which can only be generated using pulse shaping techniques. Application of pulse shaping in other nonlinear propagation studies allow one to measure the sensitivity of the nonlinear interaction to phase and amplitude characteristics of the pulse.