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Effect of Organic Loading Rate and Fill Time on the Biohydrogen Production in a Mechanically Stirred AnSBBR Treating Synthetic Sucrose-Based Wastewater

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Abstract

This study investigated the feasibility to produce biohydrogen of a mechanically stirred anaerobic sequencing batch biofilm reactor (AnSBBR) treating sucrose-based synthetic wastewater. The bioreactor performance (30 °C) was evaluated as to the combined effect of fill time (2, 1.5, and 1 h), cycle length (4, 3, and 2 h), influent concentration (3,500 and 5,250 mg chemical oxygen demand (COD) L−1) and applied volumetric organic load (AVOLCT from 9.0 to 27.0 g COD L−1 d−1). AVOLs were varied according to influent concentration and cycle length (t C). The results showed that increasing AVOLCT resulted in a decrease in sucrose removal from 99 to 86 % and in improvement of molar yield per removed load (MYRLS.n) from 1.02 mol H2 mol carbohydrate−1 at AVOLCT of 9.0 g COD L−1 d−1 to maximum value of 1.48 mol H2 mol carbohydrate−1, at AVOLCT of 18.0 g COD L−1 d−1, with subsequent decrease. Increasing AVOLCT improved the daily molar productivity of hydrogen (MPr) from 15.28 to 49.22 mol H2 m−3 d−1. The highest daily specific molar productivity of hydrogen (SMPr) obtained was 8.71 mol H2 kg TVS−1 d−1 at an AVOLCT of 18.0 g COD L−1 d−1. Decreasing t C from 4 to 3 h decreased sucrose removal, increased MPr, and improved SMPr. Increasing influent concentration decreased sucrose removal only at t C of 2 h, improved MYRLS,n and MPr at all t C, and also improved SMPr at t C of 4 and 3 h. Feeding strategy had a significant effect on biohydrogen production; increasing fill time improved sucrose removal, MPr, SMPr, and MYRLS,n for all investigated AVOLCT. At all operational conditions, the main intermediate metabolic was acetic acid followed by ethanol, butyric, and propionic acids. Increasing fill time resulted in a decrease in ethanol concentration.

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Abbreviations

PA:

Partial alkalinity (mg CaCO3 L−1)

IA:

Intermediate alkalinity (mg CaCO3 L−1)

TA:

Total alkalinity (mg CaCO3 L−1)

BA:

Bicarbonate alkalinity (mg CaCO3 L−1)

TVA:

Total volatile acids (mg HAc L−1)

TS:

Total solids concentration (mg TS L−1)

TVS:

Total volatile solids concentration (mg TVS L−1)

TSS:

Total suspended solids concentration (mg TSS L−1)

VSS:

Volatile suspended solids concentration (mg VSS L−1)

pH:

Hydrogen ion potential (μ)

C CT :

Concentration based on organic matter for unfiltered samples in the influent (mg DQO L−1)

C ST :

Concentration based on carbohydrates (sucrose) for unfiltered samples in the influent (mg carbohydrate L−1)

C CT,E :

Concentration based on organic matter for unfiltered samples in the effluent (mg DQO L−1)

C CF,E :

Concentration based on organic matter for filtered samples in the effluent (mg DQO L−1)

C ST,E :

Concentration based carbohydrates (sucrose) in the influent for unfiltered samples (mg carbohydrate L−1)

C SF,E :

Concentration based on carbohydrates (sucrose) for filtered samples in the effluent (mg carbohydrate L−1)

AVOLCT :

AVOL based on organic matter (g COD L−1 d−1)

AVOLST :

AVOL based on carbohydrate (sucrose) (g carbohydrate L−1 d−1)

ASOLCT :

Applied specific organic load based on organic matter (g DQO g SVT−1 d−1)

ASOLST :

Applied specific organic load based on carbohydrate (sucrose) (g SAC g SVT−1 d−1)

C′X − TVS :

Concentration of biomass in the reactor in total volatile solids per mass of support (g TVS g support−1)

ε CT :

Removal efficiency based on organic matter (COD) for unfiltered samples (%)

ε CF :

Removal efficiency based on organic matter (COD) for filtered samples (%)

ε ST :

Removal efficiency based on carbohydrates (sucrose) for unfiltered samples (%)

ε SF :

Removal efficiency based on carbohydrates (sucrose) for filtered samples (%)

M T − IS + B :

Total mass of the inert support and the biomass in the reactor (g)

M S − IS + B :

Sample mass of the inert support and the biomass in the reactor (g)

M S − TS :

Total solids mass (TS) of the biomass sample (g)

M S − TVS :

Total volatile solids mass (TVS) of the biomass sample (g)

M TVS :

Total biomass in the reactor in total volatile solids (g TVS)

N :

Number of cycles in a day

n CH4 :

Daily molar production of methane (mol H2 d−1)

n CO2 :

Daily molar production of carbon dioxide (mol H2 d−1)

n H2 :

Daily molar production of hydrogen (mol H2 d−1)

MPr:

Daily molar productivity of hydrogen (mol H2 m−3 d−1)

SMPr:

Daily specific molar productivity of hydrogen (mol H2 kg TVS−1 d−1)

MYALS,n :

Molar yield per applied load based on carbohydrates (sucrose) expressed as mole (mol H2 mol carbohydrate−1)

MYRLS,n :

Molar yield per removed load based on carbohydrates (sucrose) expressed as mole (mol H2 mol carbohydrate−1)

MYALS,n :

Molar yield per applied load based on organic matter expressed as mole (mol H2 mol DQO−1)

MYRLS,n :

Molar yield per removed load based on organic matter expressed as mole (mol H2 mol DQO−1)

MYALC,m :

Molar yield per applied load based on organic matter expressed as kg (mol H2 kg DQO−1)

MYRLC,m :

Molar yield per removed load based on organic matter expressed as kilograms (mol H2 kg DQO−1)

t C :

Cycle length (h cycle−1)

t F :

Fill time (h cycle−1)

V F :

Volume of wastewater fed during the cycle (L cycle−1)

V R :

Volume of liquid medium in the reactor (L)

V G :

Volume of total biogas produced in the STP per cycle (mL STP d−1)

EtOH:

Ethanol

HAC:

Acetic acid

HPr:

Propionic acid

HBut:

Butyric acid

N SF :

Molar concentration of sucrose for filtered samples (mmol carbohydrate L−1)

N G :

Molar quantity of biogas (H2, CO2, and CH4) produced along a cycle (mmol)

F F :

Feeding flow of the period in fed batch (L h−1)

v SF :

Carbohydrate consumption rate for filtered samples (mmol L−1 h−1)

v H2 :

Hydrogen formation rate (mmol L−1 h−1)

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Acknowledgments

This work was funded by Fundação de Amparo a Pesquisa do Estado de São Paulo—FAPESP (Process 09/15.984-0, 10/19.315-3, and 11/13.750-2). The authors gratefully acknowledge Dr. Baltus C. Bonse for the revision of this paper.

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Authors and Affiliations

  1. Escola de Engenharia de São Carlos, Universidade de São Paulo (USP), Av. Trabalhador São-Carlense 400, 13.566-590, São Carlos, SP, Brazil

    R. K. Inoue, D. M. F. Lima & M. Zaiat

  2. Escola de Engenharia Mauá, Instituto Mauá de Tecnologia (IMT), Praça Mauá 1, 09.580-900, São Caetano do Sul, SP, Brazil

    J. A. D. Rodrigues & S. M. Ratusznei

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  1. R. K. Inoue
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  2. D. M. F. Lima
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  3. J. A. D. Rodrigues
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  4. S. M. Ratusznei
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  5. M. Zaiat
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Correspondence to J. A. D. Rodrigues.

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Inoue, R.K., Lima, D.M.F., Rodrigues, J.A.D. et al. Effect of Organic Loading Rate and Fill Time on the Biohydrogen Production in a Mechanically Stirred AnSBBR Treating Synthetic Sucrose-Based Wastewater. Appl Biochem Biotechnol 174, 2326–2349 (2014). https://doi.org/10.1007/s12010-014-1205-7

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