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Treatment of Sago Wastewater Using Hybrid Anaerobic Reactor

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Treatment of Sago Wastewater Using Hybrid Anaerobic Reactor Water Qual. Res. J. Canada, 2006 • Volume 41, No. 1, 56–62 Copyright © 2006, CAWQ Treatment of Sago Wastewater Using Hybrid Anaerobic Reactor J. Rajesh Banu,1 Sudalyandi Kaliappan1* and Dieter Beck2 1Centre for Environmental Studies (CES), Anna University, Chennai – 600025, Tamilnadu State, India 2Indo-German Project, Centre for Environmental Studies, Freiheits Str. 195, 42853 Remscheid, Germany Sago, tapioca starch, is manufactured by over 800 small-scale units located in the Salem district of the State of Tamilnadu, South India. These units generate large quantities of high-strength wastewater requiring elaborate treatment prior to dis- posal. The present study is an attempt to treat the sago wastewater using a hybrid reactor, which combines the advantages of both fixed-film and up-flow anaerobic sludge blanket systems. A hybrid reactor with a volume of 5.9 L was operated at organic loading rates varying from 10.4 to 24.6 kg COD/m3d. After 120 d of start-up, an appreciable decrease in COD and efficient removal of solids were evident. The COD removal varied from 91 to 83%. While the removal of total solids was in the range of 56 to 63%, that of volatile solids varied from 67 to 72%. The methane production during the study period was in the range of 0.11 to 0.14 L CH4/g COD-d and the percentage was from 55 to 67%. The ideal organic loading rate (OLR) was determined on the basis of tolerance of the reactor towards higher organic loading rate and it was found to be 23.4 kg COD/m3d. The findings of the study open new possibilities for the design of low-cost and compact on-site treatment systems with very short retention periods. Key words: sago effluent, tapioca starch, hybrid anaerobic reactor, biogas Introduction wastewaters (Tilche and Vieira 1991). Over the years, hybrid reactors have been used to treat wastewaters Sago, the edible starch globules processed from the from the sugar industry (Coates and Colleran 1990), tubers of tapioca (Mannihot utillisema), is the staple diet pharmaceutical units (Hentry et al. 1996), distilleries of middle income populations in India. Processing of (Shivayogimath and Ramanujam 1999) and domestic tapioca requires 20,000 to 30,000 L of water per tonne sectors (Elmitwalli et al. 2002a,b). Studies on the treat- of sago. In addition, it produces an equal quantity of ment of sago wastewater using hybrid reactors are scarce highly organic, foul-smelling, acidic wastewater (Murthy and hence the present study was undertaken. and Patel 1961; Sastry and Mohan 1963). Various anaerobic technologies including conventional anaerobic Materials and Methods treatment (Pescod and Thanh 1977; Pugalendhi 1996; Saroja and Sastry 1972; Sastry et al. 1964; Tongkasane The schematic diagram of the hybrid reactor is illus- 1970), high-rate anaerobic treatment such as anaerobic trated in Fig. 1. The laboratory-scale hybrid reactor was filters (Khageshan 1998) and fluidized beds (Saravanane fabricated using PVC tube with an internal diameter of et al. 2001) have been used to treat sago wastewater. 11 cm and an overall height of 88 cm. The working vol- The conventional treatment options are not very efficient ume of the reactor was 5.9 L. A gas headspace of 1.5 L owing to high concentrations of solids present in the was maintained above the effluent line. A screen was wastewater. Possibilities of overcoming many of the placed at a height of 60 cm to restrict the floating pack- functional drawbacks of high-rate anaerobic reactors ing material. Two hundred plastic cut rings measuring through modified designs have been discussed by many 1 cm in diameter and 2 cm in height were used as carrier authors. For instance, restricting the supporting material material. A peristaltic pump (Miclins, Mode PP 20) was to the top 25 to 30% of the reactor volume has used for feeding wastewater into the reactor. The efflu- increased the efficiency of reactors (Guiot and Van den ent pipeline in turn was connected to a water seal to pre- Berg 1984, 1985). This would help further realize the vent the escape of gas. The gas outlet was connected to a advantages of both fixed-film and up-flow sludge blan- wet gas meter (Ritter, Model TG 05). ket treatment. This type of reactor is often called a hybrid reactor and is considered more stable for the Seed and Inoculation treatment of a series of soluble or partially soluble Contents of the rumen of a cow immediately after * Corresponding author; [email protected] slaughter were collected from a slaughterhouse in 56 Downloaded from http://iwaponline.com/wqrj/article-pdf/41/1/56/230287/wqrjc0410056.pdf by guest on 28 September 2021 High-Rate Anaerobic Treatment of Sago Wastewater 57 increased from 1000 to 1050 mL/h (24.6 kg COD/m3d). The efficiency of the treatment was evaluated in terms of removal of total solids (TS), volatile solids (VS), COD and generation of biogas. Chemical Analysis Chemical oxygen demand (COD), volatile fatty acids as acetate (VFA), total alkalinity, total solids (TS), volatile solids (VS) and total Kjeldhal nitrogen (TKN) of the raw and treated wastewater were analyzed following APHA 3- (1998). Anions such as phosphate (PO4 ), sulphate 2- - (SO4 ) and chloride (Cl ) were analyzed employing ion exchange chromatography (Dionex, model DX-120) after filtering the samples through a 0.45-µm filter. The eluent was a combination of 3.5 mM bicarbonate and 1 mM carbonate, and the flow rate was 1.2 mL/min with an injection volume of 25 µL. Methane content in the biogas was measured by gas chromatography (Chemito, GC 1000) equipped with flame ionization detector (FID). The column used was Proapak Q. Results and Discussion Start-up Phase The sago wastewater was analyzed for various physico- Fig. 1. Schematic diagram of the anaerobic hybrid reactor. chemical characteristics and the results are furnished in Table 1. To obtain lower organic load, the sago waste- Aduthotti, Chennai, India, and were transported to the water was appropriately diluted with distilled water. Fig- laboratory in an oxygen-free container. The contents ure 2 presents the loading pattern and performance of were strained using cheesecloth and the liquor was used the reactor during the start-up phase. The initial organic as the digester inoculum (Ezeonu and Okaka 1996). To loading rate (OLR) applied during start-up was 0.81 kg accelerate the start-up, 40% (v/v) slurry was mixed with COD/m3d at a HRT of 59 h. This HRT was preferred to the feed as recommended in earlier studies (Hickey et al. prevent the washout of inoculated biomass (Hickley et 1991; Shapiro and Switzenbanum 1984). al. 1991). When the OLR was increased in a stepped manner to 8.3 kg COD/m3d, over a period of 120 d, the Sago Effluent biogas generation also increased and reached a maxi- mum of 9.7 L/d at an OLR of 8.3 kg COD/m3d. Synthetic sago wastewater was prepared following Khageshan (1998). TABLE 1. Physicochemical characteristics of sago Start-up Phase wastewater a During the start-up, the reactor was operated with the Parameter Values wastewater having a chemical oxygen demand (COD) of pH 7.2 2000 mg/L. The initial hydraulic retention time (HRT) was Total solids 7645 59 h. It was gradually decreased to 5.9 h by increasing the Suspended solids 1405 Volatile solids 1834 flow rate from 100 to 1000 mL/h over a period of 120 d. COD 5750 BOD 4400 Treatment Phase TKN 180 Chloride 231 After the start-up, the reactor was operated by varying Sulphate 87 Phosphate 60 the influent COD at a constant flow rate of 1000 mL up Potassium 15 to its maximum value of 5750 mg/L (23.4 kg COD/m3d). After attaining the maximum COD, flow rate was aAverage of triplicate. All values except pH are in mg/L. Downloaded from http://iwaponline.com/wqrj/article-pdf/41/1/56/230287/wqrjc0410056.pdf by guest on 28 September 2021 58 Banu et al. Fig. 2. Loading pattern and biogas production during the treatment of sago wastewater. The removal of COD from the medium increased and Lettinga 1994). VFA as acetate in the wastewater with OLR (Fig. 3), a finding which is in conformity with decreased further and was in the range of 540 to an earlier report on the treatment of sago wastewater 345 mg/L, indicating a healthy anaerobic environment (Saravanane et al. 2001). The VFA as acetate in the and marked methanogenic activity. Overall, the reactor wastewater on day 1 was 758 mg/L and it fell to 578 performed very satisfactorily due to a rich consortium of mg/L on day 18. Higher levels of VFA as acetate in the physiologically active microorganisms in the seed slurry wastewaters during the initial phases are known to indi- during the start-up. It is known that the selection of seed cate the prevalence of acid fermentation (van Hanndel material plays a crucial role in minimizing time required Fig. 3. Influence of OLR on COD removal and VFA accumulation during the treatment of sago waste- water. Downloaded from http://iwaponline.com/wqrj/article-pdf/41/1/56/230287/wqrjc0410056.pdf by guest on 28 September 2021 High-Rate Anaerobic Treatment of Sago Wastewater 59 for initial biofilm establishment (Bull et al. 1983; Salki- 590 mg/L. Buildup of VFA was found to be influenced noja-Salonen et al. 1983). by the digestion period and the OLR. The maximum concentration of 2900 mg/L was recorded at an OLR of Treatment Phase 24.6 kg COD/m3d. VFA, a recognized intermediate dur- ing the anaerobic digestion (Wang et al.
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