Berruti, Franco

Briens, Cedric

Della Volpe, Mirco

Greenhalf, Charles

English

Engineering Conferences International

Engineering Conferences InternationalECI Digital ArchivesWastewater and Biosolids Treatment and Reuse:Bridging Modeling and Experimental Studies ProceedingsSpring 6-10-2014Sewage sludge valorization by pyrolysis using amechanically fluidized reactorFranco BerrutiWestern UniversityMirco Della VolpeWestern UniversityCharles GreenhalfWestern UniversityCedric BriensWestern UniversityFollow this and additional works at: http://dc.engconfintl.org/wbtr_iPart of the Environmental Engineering CommonsThis Conference Proceeding is brought to you for free and open access by the Proceedings at ECI Digital Archives. It has been accepted for inclusion inWastewater and Biosolids Treatment and Reuse: Bridging Modeling and Experimental Studies by an authorized administrator of ECI Digital Archives.For more information, please contact franco@bepress.com.Recommended CitationFranco Berruti, Mirco Della Volpe, Charles Greenhalf, and Cedric Briens, "Sewage sludge valorization by pyrolysis using amechanically fluidized reactor" in "Wastewater and Biosolids Treatment and Reuse: Bridging Modeling and Experimental Studies", Dr.Domenico Santoro, Trojan Technologies and Western University Eds, ECI Symposium Series, (2014). http://dc.engconfintl.org/wbtr_i/17Sewage Sludge Valorization by Pyrolysis using a Mechanically Fluidized Reactor Mirco Della Volpe, Franco Berruti, Charles Greenhalf & Cedric Briens Institute for Chemicals and Fuels from Alternative Resources (ICFAR), Western University, London, Ontario, Canada  MOTIVATION AND BACKGROUND   Municipal sewer sludge (bio-solids) disposal:  Incineration  Landfilling  Agricultural applications   No general agreement on most appropriate method   Our research: utilisation of bio-solids as a “resource” for:  Energy  Chemicals  Fertilizers  Materials and catalysts  Activated carbon   Wastewater Treatment in London, Ontario Source: City of London, Environmental & Engineering Services, Wastewater Treatment Operations Division, March 2013 PYROLYSIS Thermal decomposition (thermal cracking) of organics in inert atmosphere, producing:   Char Bio-Oil Gas PYROLYSIS Feedstocks: any organic material  Temperature: 450 to 550 ˚C  Processing time: seconds to minutes  Vapor residence times at temperature: ~ 2 seconds  Thermal or Catalytic  Reactors: need to provide good heat and mass transfer (i.e. good mixing)  •  Gas-solid fluidized beds  •  Auger-type of reactors  •  Mechanically mixed vessels  •  Rotating kilns  PYROLYSIS OBJECTIVES  Reduction in waste volume   Destruction of pathogens   Production of energy   Production of liquid fuels   Production of value-added chemicals   Stabilization of metals in solid matrix   Production of value-added solid char:  fuel  reducer for metallurgical processes  catalyst  adsorbent (activated)  PYROLYSIS YIELDS Char Bio-Oil Gas ~ 35% on a db ~ 50% on a db ~ 15% on a db PYROLYSIS PRODUCTS Bio-oil:  Dark, brown, low viscosity aqueous and high viscosity organic fractions, basic pH  Aqueous fraction could become a fertilizer  Organic fraction could become a fuel oil (HHV > 30 MJ/kg)  Low metals content  Alkanes, alkenes, aromatics, carboxylic acids, fatty acids, aldehydes, ketones, phenols, nitriles, amides…..  Source of pesticides, anti-oxidants.. Gas: CO, CO2, CH4, H2,… some N2O  High ash content in a porous carbon matrix  Metals strongly incorporated as oxides, sulfides, carbonates, alumino-silicates  Adsorbent with porosity of 5 – 150 m2/g (can be activated to > 1,500 m2/g)  HHV ~ 5 to 20 MJ/kg  Catalytic properties for H2S and NOx removal  Char: PLANT INTEGRATION OBJECTIVES  Investigate fractional separation and condensation of pyrolysis vapors produced from bio-solids, using a bench-scale batch mechanically fluidized reactor (MFR) to achieve products of potential value Reactor LegsMechanically FluidizedReactor Gas/Vapors OutletReactor OutletPipeRotatingBlades2 L batch MFR 1 t/day continuous MFR 2 Pyrolysis and Condensation Strategies EGTEl.Reactor(12.7cm height; 9.1cm id)10 PSI Pressure Release ValveElectric Motor 1/4hpEl.Mixer/stirrerEGCotton Filter & Gas Exit1. Physical          Separation2. Fractional CondensationCondensers75˚C 35˚C 0˚C @ 500˚C 3 cuts:  Room to 175˚C 175 to 250˚C 250 to 550˚C  during progressive cracking in series Condensers in parallel 2 Pyrolysis and Condensation Strategies EGTEl.Reactor(12.7cm height; 9.1cm id)10 PSI Pressure Release ValveElectric Motor 1/4hpEl.Mixer/stirrerEGCotton Filter & Gas Exit1. Physical          Separation2. Fractional CondensationCondensers75˚C 35˚C 0˚C @ 500˚C 3 cuts:  Room to 175˚C 175 to 250˚C 250 to 550˚C  during progressive cracking in series Condensers in parallel 34.87 34.87 34.34 38.74 35.34 36.42 34.56 12.68 12.42 14.00 14.40 12.85 12.05 12.04 52.45 52.71 51.66 46.86 51.80 51.54 53.40 0% 10% 20% 30% 40% 50% 60% 70% 80% 90% 100% Weight % Reaction Temperature ºC; Condenser Collection 1-2-3 at a Condenser Temperature of 0ºC Char yield Gas yield  Liquid yield Parallel Scheme: Pyrolysis Yields  EGTEl.Reactor(12.7cm height; 9.1cm id)10 PSI Pressure Release ValveElectric Motor 1/4hpEl.Mixer/stirrerEGCotton Filter & Gas Exit1. Physical          Separation2. Fractional CondensationCondensers0% 10% 20% 30% 40% 50% 60% 70% 80% 90% 100% Weight % of Bio-oil Yield Reaction Temperature ºC; Condenser Collection 1-2-3 at a Condenser Temperature of 0ºC 1st Condenser 2nd Condenser 3rd Condenser Parallel Scheme - Ratio of Collected Bio-oil in Condensers 1,2 & 3 EGTEl.Reactor(12.7cm height; 9.1cm id)10 PSI Pressure Release ValveElectric Motor 1/4hpEl.Mixer/stirrerEGCotton Filter & Gas Exit1. Physical          Separation2. Fractional CondensationCondensers0 5000 10000 15000 20000 25000 30000 20 30 40 50 60 70 80 Calorific Value J/g  Water Content wt.% 160-350-500 160-350-550 160-350-500 175-250-450 175-250-500 175-250-500 175-250-550 Condenser 1 Condenser 3 Condenser 2 Parallel Scheme - Calorific Value vs. Water Content for Condensers 1,2 & 3  EGTEl.Reactor(12.7cm height; 9.1cm id)10 PSI Pressure Release ValveElectric Motor 1/4hpEl.Mixer/stirrerEGCotton Filter & Gas Exit1. Physical          Separation2. Fractional CondensationCondensers35.13 35.13 35.11 35.11 13.84 13.57 14.10 13.30 51.03 51.30 50.80 51.59 0% 10% 20% 30% 40% 50% 60% 70% 80% 90% 100% 60-20-0 60-20-0 75-50-0 75-35-0 Weight % Condenser Temperature ºC; Condenser Collection 1-2-3 at a Reaction Temperature of 500ºC Char yield Gas yield  Liquid yield Series Scheme – Pyrolysis Yields EGTEl.Reactor(12.7cm height; 9.1cm id)10 PSI Pressure Release ValveElectric Motor 1/4hpEl.Mixer/stirrerEGCotton Filter & Gas Exit1. Physical          Separation2. Fractional CondensationCondensers0% 10% 20% 30% 40% 50% 60% 70% 80% 90% 100% 60-20-0 60-20-0 75-50-0 75-35-0 Weight % of Bio-oil Yield Condenser Temperature ºC; Condenser Collection 1-2-3 at a Reaction Temperature of 500ºC 1st Condenser 2nd Condenser 3rd Condenser Series Scheme - Ratio of Collected Bio-oil in Condensers 1, 2 & 3 EGTEl.Reactor(12.7cm height; 9.1cm id)10 PSI Pressure Release ValveElectric Motor 1/4hpEl.Mixer/stirrerEGCotton Filter & Gas Exit1. Physical          Separation2. Fractional CondensationCondensers0 5000 10000 15000 20000 25000 30000 35000 40000 0 20 40 60 Calorific Value J/g  Water Content wt.% 60-20-0 60-20-0 75-50-0 75-35-0 Condenser 1 Condenser 2 Condenser 3 Series Scheme - Calorific Value vs. Water Content for Condensers 1,2 & 3  EGTEl.Reactor(12.7cm height; 9.1cm id)10 PSI Pressure Release ValveElectric Motor 1/4hpEl.Mixer/stirrerEGCotton Filter & Gas Exit1. Physical          Separation2. Fractional CondensationCondensersBio-oil Analysis Series Scheme 75-35-0ºC EG TEl.Reactor(12.7cm height; 9.1cm id)10 PSI Pressure Release ValveElectric Motor 1/4hpEl.Mixer/stirrerEGCotton Filter & Gas Exit1. Physical          Separation2. Fractional CondensationCondensers0 10 20 30 40 50 60 70 80 90 100 5 10 15 20 25 30 Relative Abundance (%) Retention Time (min.) Condenser 1, Water Content of 1.40 wt.% n-Hexadecanoic Acid – C16 Tetradecanoic Acid – C14 Oleic Acid – C18 11-Methylnonacosane – C30 CH3OOHCH3OOHCH3ONH2CH3 CH3CH3CH3CH3CH3CH3CH3CH3OOH9-Octadecenamide, (Z) – C18 Cholest-3-ene, (5β)- Heat and Mass Balance (optimal conditions for Series Scheme) 0 1000 2000 3000 4000 5000 6000 Dried Solid Sludge Bio-oil 3rd Condenser  Char mg 200g dried solid sludge = Yield (31% Bio-oil 3rd Condenser & 36% Char ) Aluminum Calcium Copper Iron Magnesium Phosphorus Potassium Sodium Sulphur 94 86 84 96 87 97 88 96 34 0 10 20 30 40 50 60 70 80 90 100 Percentage % Aluminum Calcium Copper Iron Magnesium Phosphorus Potassium Sodium Sulphur Inorganic Transfer and Recovery  Parallel Scheme 175-250-500 EGTEl.Reactor(12.7cm height; 9.1cm id)10 PSI Pressure Release ValveElectric Motor 1/4hpEl.Mixer/stirrerEGCotton Filter & Gas Exit1. Physical          Separation2. Fractional CondensationCondensersConclusions   Bio-oil yield, calorific value and water content are functions of pyrolysis process and fractionation scheme.   Both fractionation schemes are effective de-watering techniques.   Through optimisation of the fractional condensation scheme (series), a bio-oil with a calorific value of ~35 MJ/kg and water content of ~1.5 % is achievable.   Good recovery for most inorganics in char, except for sulphur.    Acknowledgements   BioFuelNet  City of London’s Greenway Wastewater Treatment Plant   Mirco Della Volpe has been funded by the program “Messaggeri della Conoscenza” of the Italian Government (Ministro per la Coesione Territoriale). 

Sewage sludge valorization by pyrolysis using a mechanically fluidized reactor

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Sewage sludge valorization by pyrolysis using a mechanically fluidized reactor

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