S.C.E.N.A. presentation @ECOMONDO2015 by Daniele Renzi - Alto Trevigiano Servizi srl
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Presentazione del primo impianto SCENA in piena scala, brevetto n. 0001417827 concesso il 4 Settembre 2015
S.C.E.N.A. presentation @ECOMONDO2015 by Daniele Renzi - Alto Trevigiano Servizi srl
- 1. 属 AltoTrevigianoServiziS.r.l.,Montebelluna (TV),Veneto,Italy *DepartmentofBiotechnology,UniversityofVerona,Italy **GroupofEnvironmental EngineeringandBioprocesses,Universidade deSantiagodeCompostela ,Spain DanieleRenzi属,NicolaFrison*,SteganoLongo**,AlbertoPiasentin属,FrancescoFatone* THEFIRSTFULLSCALEAPPLICATIONOFTHE SHORTCUTENHANCEDNUTRIENTSABATEMENT (S.C.E.N.A.)SYSTEM ATTHECARBONERAWWTP(VenetoRegion,Italy) Europe,environment andurban wastewater treatment:thepolicy,theeconomyandthe readytomarketinnovations 5novembre2015 Rimini,Italy
- 2. * M. Cermer坦n et al (2013) Ecosistema de innovaci坦n sostenible. El conocimiento circular. La Transferencia de Tecnolog鱈a Universidad - Empresa. Nuevos instrumentos y horizontes. Fundaci坦n CYD. 2011 2012 2013 2014 2015S.C.E.N.A. CourtesyProf.JuanM.LemaRodicio USC
- 3. ALTOTREVIGIANOSERVIZI Publicowned WaterUtility Municipalities 53 Area1375km2 Population 500000 ALTOTREVIGIANOSERVIZI Publicowned WaterUtility Municipalities 53 Area1375km2 Population 500000
- 4. O&M OPTIMIZATION &INNOVATION UPGRADING PLANTS DESIGN 80WWTPS (5070.000P.E.) 150SEWAGE PUMPS SYSTEMS 1.300KMSEWAGE NETWORK
- 7. BOD 100% TN 100% TP 100% BOD <5% TN 15-30% TP 10-30% To discharge BOD 50% TN 40% TP 70-90% TN 50-65% BNR Sludge digester Primary settling tank Secondary settling tank BOD 30% TN 40% TP 70-85% BOD 0% TN 20% TP 20-30% BOD 30% TN 20% TP 40-55% Centrifuge To composting and land application !
- 9. BIOLOGICALREACTOR (SCHREIBERPROCESS) +chemicalPremoval FINALFILTRATION&DISINFECTION PUMPING&PRETREATMENTS PRIMARYSETTLING SECONDARYSETTLING WATERLINE N.LINES TREATMENT DIMENSIONAL DATA CHARACTERISTICSAND FLOWS 1 PUMPINGSTATION 131m続 WASTEWATER INFLOW15.000mc/d 2 SCREENINGSTATION FREEPASSAGE OF5mm 1 SAND/OILSEPARATOR 120m続 40m族 1 PRIMARYSETTLER 1.600m続 452m族 225mc/dOFI属 +II属 SLUDGEOUTFLOW 1 BIOREACTOR Schreibersystem 4.571m続 207m族 400mc/dOFII属 SLUDGE PRODUCTION 2 SECONDARYSETTLERS 2.260m続 904m族 600mc/hOFSECONDARY SLUDGERICIRCULATION 1 DISINFECTION 180m続 114m族 2 FINALFILTRATION
- 10. ANAEROBICDIGESTION DEWATERING PRE&POSTSTATIC THICKENING SLUDGELINE N. LINES TREATMENT DIMENSIONAL DATA CHARACTERISTICSAND FLOWS 1 I属 +II属 SLUDGE STATICTHICKNER 395m続 113m族 225mc/dOFI属 +II属 SLUDGEINFLOW 1 ANAEROBIC MESOPHILIC REACTOR 1.800m続 75m族 70mc/dOFTHICKENED SLUDGE 25mc/hOFBIOGAS AT 65% CH4 1 DIGESTATESTATIC THICKNER 175m続 50m族 63mc/dOFDIGESTED THICKENEDSLUDGE INFLOW 1 DEWATEREING SEWAGESLUDGE CENTRIFUGE 55mc/dOFDIGESTATE GASLINE N. LINES TREATMENT DIMENSIONAL DATA CHARACTERISTICSAND FLOWS 2 BIOGAS COMPRESSORS 233mc/hOFBIOGAS RICIRCOLATION 1 BOILER 180kW 1 GASOMETER 362m続 75,4m族 PRIMARYSETTLING SECONDARY SETTLING
- 11. 0 10.000 20.000 30.000 40.000 50.000 60.000 70.000 80.000 1 3 5 7 9 11 13 15 17 19 21 23 PE h TotalP Influent 0 10.000 20.000 30.000 40.000 50.000 60.000 70.000 80.000 1 3 5 7 9 11 13 15 17 19 21 23 PE h TotalN SEWERINFLUENT Parameter Average Conc. mg/l Load kg/d Flow 16.972 TN 16 270 NH4N 12 202 NO2N <0.5 NO3N <0.5 PO4P 1,5 25 TP 2 34
- 12. 0 10 20 30 40 50 0 10.000 20.000 30.000 40.000 50.000 60.000 70.000 80.000 1 3 5 7 9 11 13 15 17 19 21 23 25 FLOW PE h TotalP Influent Supernantant Flowsupernatant(m続/h) 0 10 20 30 40 50 0 10.000 20.000 30.000 40.000 50.000 60.000 70.000 80.000 1 3 5 7 9 11 13 15 17 19 21 23 FLOW PE h TotalN SEWERINFLUENT Parameter Average Conc. mg/l Load kg/d Flow 16.972 TN 16 270 NH4N 12 202 NO2N <0.5 NO3N <0.5 PO4P 1,5 25 TP 2 34 SUPERNATANTFLOW Parameter Average Conc.mg/l Load kg/d Flow 134 TN 521 70 NH4N 511 68 NO2N <0.5 NO3N <0.5 PO4P 63 8 TP 89 12 FINAL INFLUENT Parameter Average Conc.mg/l Load kg/d Flow 17.106 TN 20 340 NH4N 16 270 NO2N <0.5 NO3N <0.5 PO4P 2,7 33 TP 3 46 21%ofTN 23%ofTP from Supernatants
- 15. Investmentcosts(volume,materials) Energydemand(aeration,mixing,pumping) Chemicals(NaOH,Csource) Sludgedisposal(treatment,transport) Startup(duration,effort) Controlsystem(complexity,degreeofautomation) Experience(pilot&fullscaleplantsinoperation) Stability(endurance,resistanceagainstpeakloads, inhibition) EasyO&M Guaranteeofthedischarge Carbonfootprint Costoptimization
- 16. The IDEA: a pilot scale experimantation and prompt fullscale validation to test innovative technologies for Vianitrite removal of nutrients nitrogen and phosphorus from AD supernatants at Carbonera WWTP AUTHORIZATION :DecreeoftheVenetoRegionn.754of21.05.2013 PHASEI(PILOTSCALE)+PHASEII(FULLSCALE) ACOLLABORATIONBETWEENUNIVERSITYANDWATER UTILITIES>>AREWEWITHINCONCEPT? TheNAME:S.C.E.N.A.ShortCutEnhancedNutrientsAbatement ThePREVIOUSEXPERIENCE:testonpilotplantwithinaco digestionWAS+OFMSWtreatmentplant TheINNOVATION:BACS(BESTAVALAIBLECARBONSOURCE)from sewagesludgefermentationandvianitritephosphorusenhanced bioaccumulation
- 17. AdvantagesFA>1 mgNH3NL1 FNA>0.02 mgHNO2NL1 DO:0.51.5 mgL1 T:3040oC pH>7.5 Up to 25% lower oxygen demand Up to 40% less external carbon source 30 40% less sludge production Shortcut nitrification/denitrification (SCDN) TheapplicationoftheprocessinSBRensures: Higherkinetics Lessworkingvolume Higherflexibility NH4 +NO2 NO3 NO2 NON2ON2 AOB NOB Autotrophicbacteria Heterotrophicbacteria DenitritationNitritation Pathway AOBgrowth NOBwashout Possible enhanced P bioremoval NOexternalCarbonsourceusingBACS S.C.E.NA.
- 19. 1 Filling(1015min) 2 Anaerobic(60min) 3 Aerobic(180 300min) 4 Anoxic(5060min) 5 Settling(3040min) 6 Discharge(1015min) VFAs VFAs BACSCarbonsourceaddition BACSCarbonsourceaddition Nitrogen & Phosphorus Biological removal
- 20. DATACYCLE IDENTIFICATIONOFFAULTS PROFILESSIGNALPROCESSED INTELLIGENTCONTROLSYSTEM DISSOLVEDOXYGEN pH RESULTS:CONTROLPOINTSOFIDENTIFICATION MOVETOTHENEXTSTEP %Ntot removal DosageBACS forN&Pbiological removal NN02 production ELECTRICALCONDUCTIVITY
- 25. STARTUP NOVEMBER2013 Alkaline Fermentation Solid/Liquid Separation short-cut SBR BACS tank 0,5m3 formixedsludge (primaryandsecondary) UFmembranefiltrationskid 3m3 SBRreactortotreatsupernatant usingvianitriteprocess
- 26. 86,6 84,1 72,6 206,8 171,7 154,3 0 50 100 150 200 250 300 350 Scenario1(current situation) Scenario2 (supernatant equalization) Scenario3(with SCENA) MaximumOxygenconsumption(kg/h) AverageOxygenconsumption(kg/h) IMPACTONSECONDARYEFFLUENT IMPACTONAERATION 0 1 2 3 4 5 6 7 8 9 10 TotalCOD (mg/l) Ammonia (mg/l) Nitrate(mg/l) TotalP(mg/l) TotalN(mg/l) Scenario1(currentsituation) Scenario2(supernatantequalization) Scenario3(withSCENA) ABOUT 16%OFAVERAGE OXYGEN CONSUMPTION INTHE MAIN BIOLOGICAL REACTOR AND 25%OFTHEMAXIMUMOXYGEN CONSUMPTION ABOUT 50%OFTN AND 20%OFTP INDISCHARGE OFMAIN LINE
- 27. ULTRAFILTRATIONMEMBRANE CENTRIFUGALSLUDGE EXTRACTOR SCREW PRESS 15 20kWh/mc 1,5 2,0kWh/mc 0,12 0,20kWh/mc WHICHS/LSEPARATORCOULDBEBETTER? About Energydemand Maintenancecosts EasyO&M
- 29. VOLUME TANK STORAGE/EQUALIZATION SUPERNATANT 40m3 ExStorageofLiquidWaste scSBR BIOLOGICALPROCESS 70m3 ExStorageofLiquidWaste FERMENTATORFOR BACS PRODUCTION 50m3 ExStorageofLiquidWaste BACSSTORAGE 10m3 External tank PILOTSCALE SUPERNATANT TREATINGON S.C.E.N.A.FULL SCALE mc/d 65 kgN /d 35 50 KgP /d 3 5 FULLSCALE
- 36. S/LSEPARATOROFFERMENTEDSLUDGE VolumeTank=10mc ScrewPressworkingflow=2mc/h FERMENTER VolumeTank=50mc
- 38. 0 10 20 30 40 50 60 70 80 90 100 0 100 200 300 400 500 600 700 800 0 5 10 15 20 25 30 35 40 45 50 %NO2-N/NOx-N Nitrogen(mgN/L) Tempo (d) NH4-N influent NH4-N effluent Nox-N effluent %NO2-N/NOX-N After10days CompleteViaNitritepathway(NOBinhibition) After15days StartwithBACSdosage After18days NoNNO3 indischarge Now weareoptimizingBACSquality
- 39. BACSdosageisautomaticallydosedinthedenitritation phaseofthe scSBR operationtoremovenitriteandinthesametimephosphorus. CARBONERAWWTPMAINLINE SPECIFICNUTRIENTSREMOVALRATES (T=20属C) sAUR(mgN/gVSS*h) 1.5 2.5 sNUR(mgN/gVSS*h) 5 6 0 0,1 0,2 0,3 0,4 0,5 0,6 0 5 10 15 20 25 30 35 40 45 0 5 10 15 20 25 30 35 40 45 50 vNLR(kgN/m3d) kn20属C(mgN/gVSSh) Tempo (d) kn (20属C) kd (20属C) vNLR CARBONERAS.C.E.N.A.SBR SPECIFICNUTRIENTSREMOVALRATES (T=20属C) sAUR(mgN/gVSS*h) 12 15 sNURBACS (mgN/gVSS*h) 35 40
- 40. ltReactor/P.E. OTHERS/S.C.E.N.A. VOLUME(mc) Conventional MLE 180 12 840 Intermitted Aeration 150 10 700 CarboneraWWTPMain line 114 7,6 533 Carbonera S.C.E.N.A.SBR 15 1 70 HowmuchVOLUMEofBiologicalReactortotreatthesameLoad? IntermittedAeration ConventionalMLE Carbonera WWTP S.C.E.N.A.SBR Lessimpactonthelandscape Lowercostsofcostruction
- 41. 0 1 2 3 4 5 6 7 8 9 10 11 12 13 0 200 400 600 800 1000 1200 1400 1600 1800 2000 03/09/2015 13/09/2015 23/09/2015 03/10/2015 13/10/2015 23/10/2015 02/11/2015 12/11/2015 kWh BIO N-NH4 out N-NO2 out N-NO3 out Startup StartBACS
- 42. CarboneraWWTP 3,4 /kgN rem reduction ofsupernatants OPEX 53% 1,61/kgN rem...+Prem Optimizingat 50kgN/d 1,1 1,3/kgN rem...+Prem Load=35kgN/d 9 7% Storagemixer kW 1,5 h/d 6 kwh/d 9 7% 56 43% Fillingpump kW 1,3 h/d 0,6 kwh/d 0,78 0,6% Dischargepump kW 1,3 h/d 0,6 kwh/d 0,78 0,6% MixerSBR kW 1,5 h/d 6,3 kwh/d 9,4 7,2% AirBlower kW 3,0 h/d 15,1 kwh/d 45,4 34,8% 48 37% FermenterMixer kW 2,5 h 6 kwh/d 15 11,5% HeatingSystem kW 5,5 h 24 kwh/d 33 25,3% 17 13% Sludgeloadpump kW 0,4 h/d 6 kwh/d 2,4 1,8% ScrewPress kW 0,37 h/d 6 kwh/d 2,22 1,7% Bacspumptostorage kW 4 h/d 2 kwh/d 8 6,1% Polypump kW 0,4 h/d 6 kwh/d 2,4 1,8% BACSdosagepump kW 1,5 h/d 1,3 kwh/d 2 1,5% Dosagesolutionpolywater lt/h 270 h/d 6 lt/d 1620 Dosagepoly %vol 0,5% kg/l 1,05 kg/d 8,51 0,10 PERSONELLE MAINTENANCE 0,01 0,01 /kgNrem...+Prem 0,21 0,18 0,09 0,01 0,01 0,04 SLUDGEPRODUCTIONtonn/d 0,07 0,17 POLYELECTROLYTEDOSAGEkg/d 130 8,5 0,72 0,4 0,05 0,05 0,31 0,00 0,00 0,05 0,25 0,26 0,08 S/LSEPARATORkWh/d FERMENTERkWh/d STORAGESUPERNATANTkWh/d SBRkWh/d ENERGYCONSUMPTIONkWh/d Investment PBP4,5years
- 43. BestAvalaible CarbonSource BACS ExternalCarbonSource (eg.AceticAcid) StableNremovalindenitrification InstableBIOPremoval HigherCarbonFootprint Commercialproduct Cost1,58/kgNrem StableNremovalindenitrification StableandlinearBIOPremoval LowerCarbonFootprint HomemadeProduct Cost0,92/kgNrem+Prem Howshouldweimagine/designthe2020WWTPs? SystemsforPRIMARYSETTLEMENT+FERMENTER+S/LSEPARATOR BACS...ineachplant.... toenhanceNitrogen&PhosphourBIOremoval moreBIOREMOVAL,lessCHEMICALADDITION
- 45. EXTRACTION OF PHA BIOPOLYMERS FROM WWTPS SLUDGE FOR THE PRODUCTION OF BIOPLASTICS IMAGE OF THE FIRST BIOPOLYMER PRODUCT AT UNIVERSITY OF VERONA LABORATORY FROM CARBONERA WWTPS SLUDGE (SPRING 2014)
- 47. SHORTCUT NITRITATION AND DENITRITATION (SCND) WITH BACS IS SOLID AND RELIABLE PROCESS TO TREAT LIQUID EFFLUENTS ORIGINATED FROM ANAEROBIC DIGESTION >> STATEOFTHEART STABLE AND ROBUST WASHOUT OF NITRITE OXIDIZING BACTERIA CAN BE ACHIEVED WITHIN 1015 DAYS TREATING ANAEROBIC SUPERNATANTS OF DIGESTATE SLUDGE, WITHOUT INFLUENCE OF ORGANIC OVERLOADS THE APPLICATION OF S.C.E.N.A. PROCESS IN FULL SCALE WWTP LETS ACHIEVE A BETTER QUALITY OF DISCHARGE (TN, TP), REDUCING ENERGY CONSUMPTION AND FLUCTUATIONS THE TREATMENT OF ANAEROBIC SUPERNATANTS USING S.C.E.N.A. PROCESS CAN REACH OPERATIONAL COST OF ABOUT 1.2 1.5 /KG VS. 3 5 /KG OF NITROGEN TREATING THE SAME FLOW IN FULLSCALE PLANT, CONSIDERING THE REMOVAL OF BOTH TN AND TP. THE SHORTCHAIN FATTY ACIDS PRODUCED BY THE ALKALINE FERMENTATION OF SEWAGE SLUDGE AVAILABLE IN WWTPS MAY ENHANCE THE SIMULTANEOUS BIOLOGICAL REMOVAL OF NITROGEN AND PHOSPHORUS VIANITRITE PATHWAY. This is aREADYtoMARKET Technologyfor2020WWTPs LOWNOVELTYHIGHNOVELTYAPPLICATION
- 48. Europe,environment andurban wastewater treatment:thepolicy,theeconomyandthe readytomarketinnovations 5novembre2015 Rimini,Italy THANKSFORYOURATTENTION Info&visitstoS.C.E.N.A.plant drenzi@altotrevigianoservizi.it