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Water SA

versión On-line ISSN 1816-7950
versión impresa ISSN 0378-4738

Water SA vol.37 no.1 Pretoria ene. 2011


Comparison between a two-stage and single-stage digesters when treating a synthetic wastewater contaminated with phenol



JE HernandezI,II,*; RGJ EdyveanII

IInstitute for Biotechnology and Bioengineering, Centre for Biological Engineering, UMINHO, Campus Gualtar, 4710-057 Braga, Portugal
IIDepartment of Chemical and Process Engineering, University of Sheffield, Broad Lane, Sheffield, S3 7HQ, United Kingdom




Phenol is a pollutant found in many industrial wastewaters, which diminishes biogas formation in anaerobic digesters. In this study, a two-stage (acidogenic and methanogenic) anaerobic digester (TSAD) was compared to a single stage digester (SSD), in treating a synthetic wastewater contaminated with phenol. Both systems were operated in batch-dilution and semi-continuously at 35ºC, and were loaded with a synthetic wastewater containing a constant concentration of readily biodegradable organic matter and an increasing concentration of phenol. The TSAD had greater biogas production, and its acidogenic reactor fermented the readily biodegradable matter without inhibition by accumulation of phenol (up to 1 450 mg·ℓ-1). The acidogenic reactor also prevented inhibition of biogas formation in the second phase (methanogenic), by holding phenol and fast produced organic acids. Batch TSAD is a potential wastewater treatment option to decontaminate streams containing readily biodegradable matter contaminated with phenol. This system enhances biogas production and allows better control of the acidogenic and methanogenic phases.

Keywords: Acidogenic, biodegradation, biogas, industrial waste, methanogenic, phenol, two-phase anaerobic digestion




Phenol is mainly derived from oil and coal and is used in the production of fertilisers, fungicides, dyes, plastics, solvents and fibre board (Veeresh et al., 2005). The global production of phenol surpassed 6.6 x 106 t in 2000; it is mainly manufactured in Europe and the USA (Niwa et al., 2002; Panov, 2000). Phenol is a priority pollutant and the latest figure shows that 3 480 t were released into the USA environment in 2005 (USEPA, 2008). A maximum concentration of 17 000 mg·ℓ-1 in wastewater has been reported (Veeresh et al., 2005).

The elimination of phenol in wastewater has been studied by applying several physicochemical and biological technologies, with a variety of operational designs and combinations. However, anaerobic digestion still remains the most attractive option (Veeresh et al., 2005). A major drawback is that at certain concentrations phenol can disturb the trophic chain established between microorganisms, by affecting the production of fatty acids, hydrogen and thus methane (Fedorak and Hrudey, 1984; Wang et al., 1989; Hernandez and Edyvean, 2008). Phenol biomethanisation has been studied in a variety of single-phase anaerobic digesters (Veeresh et al., 2005). Nevertheless, the application of two-phase anaerobic digestion (TSAD), consisting of acidogenic and subsequent methanogenic steps, is largely unexplored. In addition, the inhibitory effects of phenol on the TSAD are not known.

The advantages of TSAD over a single-stage digester (SSD) are well recognised. TSAD reduces toxicity to methanogenesis by hosting fast growing acidogens in a separate reactor, thus preventing trophic-chain imbalances due to both the high rate of production of volatile fatty acids (VFAs), and their low rate conversion by methanogens (Tchobanoglous et al., 2003). In addition, TSAD allows the dilution of the VFAs produced in the acidogenic phase before being loaded into the methanogenic reactor, avoiding the utilisation of sources of freshwater for dilution. Some findings show that the acidogenic phase enhanced the biodegradability of aromatic ring molecules such as nitrobenzene and flavonoids (Herrmann and Janke, 2001; Ng et al., 1999).

In this study, the aim was to compare the treatment of a synthetic wastewater containing a readily biodegradable matter and phenol, when performed in a TSAD and SSD. Performance of both TSAD and SSD was studied at dilution-batch and semicontinuous operation. The results of this study address the question as to whether continuous or batch TSAD is the best option for treating a wastewater contaminated with phenol.


Materials and methods


Anaerobic reactors were constructed with glass 'quick fit' vessels fitted with a multi-socket top (Fig. 1). The TPAD was composed of an acidogenic (R1) and a methanogenic reactor (R2). The SSD was a methanogenic reactor similar to R2. All reactors had 4 ℓ of reaction volume and were magnetically stirred and submerged in water baths at 35ºC. R2 and SSD were filled with a commercial rigid packing design (Flocor, UK) to support the growth of fermenting methanogenic consortia. The produced biogas was collected and measured in graduated cylinders (approx. 101.325 kPa and 25ºC), whose tops were submerged downwards into a barrier solution to avoid the loss of CO2 (DIN, 1985); the prototype is shown in Fig. 4. pH was recorded by a portable temperature compensated pH meter. A buffer solution made of 7.5 g NaOH/10 g NaHCO3 was used to control pH.





A commercial nutritional supplement (NS), containing readily biodegradable matter, was obtained from Boots, Co. (Table 1), while phenol and other chemicals were obtained from Sigma-Aldrich, Co. Synthetic Wastewater 1 (SWW1) was a mixture of phenol (50 to 250 mg·ℓ -1) and the medium given in ISO 11734 (CEN, 1999). Synthetic Wastewater 2 (SWW2) was prepared by mixing phenol and NS (Table 1).



Digesting sludge was obtained from an anaerobic digester treating yeast and industrial wastewater. It was mesh sieved (1 mm2) and utilised to produce acidogenic and methanogenic sludge.


Liquid samples were taken and stored following standard methods (APHA, 1998). Chemical analyses to the liquid fraction were carried out with the following Dr Lange® cuvette test kits: LCK 384 Total organic carbon (TOC), LCK 114 chemical oxygen demand (COD), LYW 365 organic acids (VFAs) and LCK 346 phenols. Volatile suspended solids (VSS) were determined by standard methods (APHA, 1998). The suspended fraction of COD and TOC (i.e. SCOD and SOC) were calculated after separating the dissolved fraction through a 0.45 µm pore diameter fibreglass filter. CH4 and CO2 in the biogas were analysed using a gas chromatograph (GC, Varian 3400) fitted with a methaniser. The capillary column (30 m x 0.530 mm GS-Q) was packed with 10% nickel nitrate on Chromosorb GAW 100/120. It operated at 60ºC and inlet pressure of 39.3 kPa. The injector and flame ionisation detector operated at 350ºC and 280ºC, respectively. Nitrogen gas was used as a carrier gas (19.0 cm·s-1). Gas concentrations, including CO2 and CH4 dissolved in aqueous phase, were corrected by applying Henry's Law as reported (Hernandez and Edyvean, 2008). Methane-rich gas in R2 and SSD is referred as biogas throughout the text.

Acclimation of methanogenic sludge to phenol

Three reactors were separately inoculated with sludge (3.6 ℓ, VSS = 18.9 g·ℓ-1) and loaded with 0.4 ℓ of SWW1, which contained only phenol as a carbon source. Initially, the reactors contained 50 mg phenol·ℓ-1. After complete elimination of phenol (6 d), a settling period of 3 h was allowed; subsequently the supernatant was drawn off. The whole cycle was repeated at 100 and then at 250 mg phenol·ℓ-1, respectively, with the aim of gradually increasing the number of phenol degraders. Two final cycles at 250 mg phenol·ℓ-1 were run to stabilise conditions. In these final cycles, the average biogas produced in each reactor was 369 ± 4 mℓ (65 ± 2.8% CH4). Methanogenesis was not observed in autoclaved inactivated sludge with (i.e. controls) and without (i.e. blanks) phenol. Methanogenesis was insignificant in controls containing medium and active sludge, and inexistent in blanks containing medium and phenol.

Production of acidogenic sludge

R1 was inoculated with acclimatised methanogenic sludge (VSS = 18.9, g·ℓ -1) and loaded with SWW2, which contains readily biodegradable matter and phenol. Initially, R1 contained 25 mg phenol·ℓ -1 and 1.83 g DCOD·ℓ -1 (DCOD is dissolved chemical oxygen demand). This DCOD load was in the range of previously reviewed values for TPAD (Demirel and Yenigun, 2002). After 24 h, the pH dropped due to fast production of organic acids, which were partially removed by settling the sludge down for 3 h and removing the supernatant. R1 was reloaded with SWW2 and adjusted with buffer to pH 5.5 twice a day. The batch cycle was serially repeated until the sludge became yellowish-brown in colour, this being an indication of disrupted methanogenesis (Demirel and Yenigun, 2002). The lack of methane formation was also confirmed by GC analysis.

Batch-dilution elimination of phenol

Two separated reactors formed the TSAD (R1 and R2). The SSD was similar to R2. In total, 4 consecutive batches were double run, and the concentration of phenol (25 to 250 mg·ℓ -1) was increased between batches while keeping constant the complementary DCOD within SWW2. On the first run of Batch 1, both R1 and the SSD were loaded with SSW2, and operated at initial concentration of 25 mg phenol·ℓ -1 and 1.83 g DCOD·ℓR-1.

R2 is fed with R1 effluent and, therefore, after 1 d (approximate time to eliminate phenol in R2) 400 mℓ of liquor was pumped out from R1, pH adjusted and then fed into R2. The missing volume in R1 was replenished with acidogenic sludge. To allow for comparison, the same volume was drawn from the SSD and replenished with methanogenic sludge (prepared as described earlier). Adjustment of pH was done twice a day at 5.5 in R1 and 8.5 in both R2 and SSD, aiming at promoting acidogenic and methanogenic conditions, respectively.

The whole procedure was repeated daily until the concentration of phenol was undetectable in R1 and SSD. Afterwards, the sludge was settled for 3 h and the supernatant drawnoff, this was the end of a single run and the whole cycle was repeated at the same conditions for a second run. At the end of Batch 4, the reactors were left standing for 1 d and then were semi-continuously operated.

Semi-continuous elimination of phenol

This experiment was carried out semi-continuously for 15 d. R1 and SSR were daily refilled with substrate SWW2 (9.7 g COD; Table 1). Every day, 400 mℓ of liquid was pumped out of each reactor. The effluent of R1 was pH-adjusted and fed into R2, whereas the effluent from the SSR was discarded. pH was controlled as described above. In this operational mode, the remaining volume in R1 and SSR was increased up to 4 ℓ with the daily feed of substrate and buffer.


Results and discussion

Batch-dilution elimination of phenol

In R1, fast fermentation of the readily organic fraction in SWW2 was observed, as will normally occur in acidogenic reactors where methanogens have been largely eliminated. Part of the phenol in SWW2 was lost, probably due to adsorption onto sludge, as evaluated in blanks and controls, and not converted to gas products. It can be seen that the experimental values of phenol concentration describe a curve that closely approximates calculated concentrations due to daily dilution (Fig. 2). On this basis, the difference between both experimental and calculated concentration plots cannot be linked to biodegradation, but can be attributed either to experimental errors or to adsorption of phenol onto the sludge. In some cases, up to 40% adsorption has been reported (Healy and Young, 1979; Hernandez and Edyvean, 2008). Therefore, phenol was not biodegraded in R1 but diluted and disposed of due to filling and draw.

Phenol biodegradation occurred in the acclimatised digesting sludge used as initial inoculum. However, in R1, phenol mineralisation is thermodynamically limited due to lack of syntrophism between fast-fermenting microorganisms and the deliberately disturbed methanogens. Thermodynamically, this association is necessary to favour aromatic ring fission to produce acetate and hydrogen, which are subsequently utilised by methanogens to produce biogas (Thauer et al., 1977; Winter and Knoll, 1989). Phenol fermentation can also be impeded due to its highly effective inhibition effects on the electron transport and energy production of phenol degraders (Escher et al., 1996; Fedorak and Hrudey, 1984; Wang et al., 1989). R1 is therefore not effective in breaking the aromatic ring but it may enhance the biodegradability of phenol by modifying the molecule, as occurred in similar experiments with acidogenic reactors (Herrmann and Janke, 2001; Karlsson et al., 2000; Ng et al., 1999).

The gas produced in R1 (1.1 ± 0.07 ℓ, 99.98% CO2, not considering H2 and VFAs) is likely to come from the fermentation of readily biodegradable matter into VFAs (Fig. 2). In this reactor, increasing the concentration of phenol did not affect the production of gas, meaning that the fermentation of organic matter in SSW2 is not inhibited. This advantageous feature could be useful for the pre-treatment of waste streams containing a readily biodegradable matter mixed with phenol.

Biogas production (ℓ) and biogas productivity (ℓ (ℓ Rd)-1) were always higher in the TSAD at the end of each batch cycle (Table 2). Increasing phenol concentration increased both the time required for phenol elimination and the biogas production in both TPAD and SSD. Therefore, this operation affected biogas productivity differently. For instance, productivity decreased in the TPAD (longer time batch cycles) but increased in the SSR (shorter time batch cycles).

The methane composition in the biogas produced by the SSD was initially 59 ± 2% when SSW1 was fed. In this reactor, swapping to SSW2 caused a delay in phenol elimination (5 d) when compared to the TSAD (Table 2). This probably occurred because the bulk matter in SSW2 was easily fermented by fastgrowing acidogenic bacteria into organic acids, consequently causing an imbalance with slow-growing methanogens. As the operation continues, SSD overcame the imbalances and biologically eliminated higher loads of phenol faster than the TSAD. Such recovery of methanogenic activity might be due to repeated replenishment with fresh methanogenic sludge already adapted to phenol.

In the TSAD, a fraction of phenol and organic acids from R1 was biomethanised in R2 (67% CH4 and 33% CO2), as would normally occur in anaerobic digesters. Such fraction of phenol was completely eliminated every day, in R2, by the parallel participation of biomethanisation, adsorption onto the sludge and cell mass assimilation (Healy and Young, 1979; Hernandez and Edyvean, 2008). Methanogenic conditions in R2 were superior because the effluent (400 mℓ) taken from R1 (containing phenol, organic acids and acidogens) was diluted within the total R2 volume, and shock due to overloading or inhibition was therefore avoided. The longer times required to eliminate phenol by dilution in R1 allowed more loadings into R2. Logically, more biogas was produced at the expense of longer periods of time, causing a reduction in biogas productivity (ℓ (ℓR d)-1).

Semi-continuous elimination of phenol

The lack of phenol biodegradability and its daily feeding into R1 caused accumulation (Fig. 3). As explained before, the biodegradation of phenol was hampered due to the thermodynamic and ecotoxicological limitations established in R1, so the losses of phenol might be attributed to physical interactions, e.g. adsorption onto sludge as evaluated in blanks and controls (Hernandez and Edyvean, 2008).

The maximum concentration of phenol reached in R1 was 1 450 mg·ℓ-1, from which 400 mℓ was transferred for subsequent treatment in R2. Since phenol was diluted within the whole R2 working volume, its concentration was far below 1 250 mg·ℓ -1, which may promote 50% inhibition of acetate methanogenesis (Wang et al., 1991). This capacity of preventing shock loading to the methanogenic reactor can reduce the vulnerability against unexpected increments of phenol and other organic matter in wastewater streams. However, accumulation is not desirable in a process receiving regular inputs of wastewater. Therefore, the continuous operation of a TSAD treating a wastewater containing phenol may not be acceptable.

Gas production was stable in R1 and R2 over the experiment. The gas produced in R1 (99% CO2, disregarding H2 and volatile organics) was derived from the fermentation of readily biodegradable matter in SSW2 and not from phenol. On the other hand, R2, which is the TSAD second stage, produced 3 times more biogas with a richer CH4 content than the SSD (Table 3). The biogas production capacity in the SSD was disturbed after 24 h of starting the operation. Probably, the daily feeding of SSW2 led to fast growth of acidogens, as commonly happens in acidogenic reactors fed with readily biodegradable matter (Demirel and Yenigun, 2002). Consequently, the SSD failed to produce methane and eliminate phenol. Therefore, further analysis of the SSD was stopped at this stage of the experiment.



Stable control of pH was achieved in R1 by feeding a variable volume of buffer solution over the period of the experiment (Table 3). The pH was acid due to VFA formation from SWW2, since VFAs are stronger acids (Ka in the order of 10-5) than phenol (Ka = 1.1 x 10-10). In the case of R2, pH was stable. In contrast, stable pH conditions were not achieved in the SSD (Table 3). This reactor started as methanogenic and became acidogenic after 24 h due to fast growth of acidogens and flushing out of methanogens (sludge replenishing was not allowed in both TSAD and SSR). Better pH control was therefore achieved in the TSAD.

The 400 mℓ daily loading (9.7 g DCOD) led to an increment in the DCOD in R1 and SSD, resulting in negative conversion values (Table 3), which are merely mathematical artefacts.

Similar findings have been reported by Ghosh et al. (1975) and are caused by accumulation of VFAs due to overloading. Contrary to this, in R2 nearly 77% of the initial DCOD was degraded after 1 day of operation. In this reactor, there was not accumulation of the un-degraded DCOD fraction, which was most probably co-degraded with the diluted load coming from R1 and adsorbed onto the sludge in R2. Under these conditions, both R1 and SSD were inefficient for DCOD removal.

Hydrolysis of readily biodegradable matter in SSW2 and subsequent formation of organic acids in R1 occurred without inhibition by phenol accumulation (Table 3). In R2, 95% of organic acids contained in the effluent of R1 were easily reduced within 24 h and such reduction was linked to an increase in CH4 and CO2 production. The concentration of organic acids in R2 was below 500 mg acetic acid·ℓ-1, which is a recommended value for stable methanogenic reactors (Dries, 2002). Again, in the case of the SSD, the accumulation of organic acids produced by fast-growing acidogens promoted the disruption of methanogenesis. A low pH and the yellowishbrown colour were observed (Table 3). This reactor was not further analysed due to its failure to biomineralise phenol and readily biodegradable matter in SSW2.

Biomass concentration (SOC) in R1 was not affected by the accumulation of phenol. In R2, there was variability in biomass concentration, probably caused by the detachment of biomass from the packing material due to stirring. In the case of the SSD, biomass concentration was approximately that of R1, indicating that the same operational conditions in both reactors led to similar growth rates of acidogens (Table 3).



A synthetic wastewater containing a readily biodegradable matter and phenol was treated in a two-stage anaerobic digester (TSAD: acidogenic and methanogenic) and a single-stage digester (SSD). The TSAD produced more biogas; fermented a readily biodegradable organic matter without inhibition by phenol; facilitated the control of acidogenic and methanogenic stages and allowed the dilution of both VFAs and aromatic compounds to avoid methanogenesis inhibition. Batch TSAD is a potential wastewater treatment option to decontaminate streams containing phenol and readily biodegradable organic matter.



We would like to express gratitude to CONACYT for the sponsorship given (Grant 167740).



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Received 1 August 2008; accepted in revised form 5 November 2010.



* To whom all correspondence should be addressed. New address: School of Chemical Engineering and Analytical Science, University of Manchester, Oxford Road, Manchester, M13 9PL, United Kingdom. +44(0)1613064418; fax: +44 (0) 161 306 9321; e-mail:

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