Printer Friendly

Quantification and characterization of the production of biogas from blends of agro-industrial wastes in a large-scale demonstration plant/Quantificacao e caracterizacao da producao de biogas a partir de misturas de residuos agroindustriais em uma planta de demonstracao em larga escala.

Introduction

Until recently, biogas was considered simply as a by-product obtained from the anaerobic decomposition of animal waste and sludge from treatment plants of domestic wastewater. However, the accelerated economic development in recent years and the increase in prices of conventional fuels have encouraged researches into the energy production from alternative and economically attractive sources (Goldemberg & Paletta, 2012).

The sources for the biogas generation cover various raw materials types, such as wastes from households and agriculture, sewage sludge and wastewater (Kapdi, Vjay, Rajesh, & Prasad, 2005). In the composition of biogas, methane (C[H.sub.4]) has an aggression potential to the environment around 20 times that of carbon dioxide (C[O.sub.2]), being then characterized as the main responsible for the increase in the concentration of greenhouse gases (Sanquetta, Balbinot, & Ziliotto, 2004).

The C[H.sub.4] produced by degradation of organic matter could be channeled and burned in power generators engines, in order to minimize environmental impacts, and enhance the biogas. The advantages of the use of biogas can be considered in the electric power generation as well as being a possible solution in the treatment of waste.

Biogas is a colorless, odorless and highly flammable gas that produces no soot and, therefore, has atmospheric pollution potential lower than that of the butane present in the cooking gas (Oliveira & Higarashi, 2006). Biogas is composed by different gases such as C[H.sub.4] (60-70%), C[O.sub.2] (30-40%), [N.sub.2] (< 1%) and [H.sub.2] (10-2000 ppm). C[H.sub.4] represents the calorific power value contained in the gas equal to 37781.6 kJ [m.sup.-3] and power generation capacity of 5 kW hour [m.sup.-3] (Torres & Osorio, 2009).

Biogas can be used in its original composition, but depending on the application, it is necessary to remove C[O.sub.2] and sulphidric acid ([H.sub.2]S), as humidity and high pressure (Diaz, Ramos and Polanco, 2015). [H.sub.2]S is responsible for toxicity and corrosion in most devices, when concentrations exceed 50 ppm. The toxicity affects human health, causing headaches, nausea and eye irritation, and, in addition, the combustion of this gas generates emissions of sulfur dioxide (S[O.sub.2]), with negative environmental effects (Busca & Pistarino, 2003; Greenpro, 2004). Currently, there are various methods of treating for effluent gases, which may be used to minimize these emissions (Pagliuoso & Regattieri, 2008).

All production of biogas from the anaerobic degradation using the upflow anaerobic sludge blanket (UASB) technology is enough to sanitize the entire sludge production from a wastewater treatment plant (WWTP). The pathogenic microorganisms found in the sludge, when not disposed of properly, can be harmful to public health (Borges & Chernicharo, 2009). In this context, it was considered the use of the energy contained in biogas as an interesting alternative to reconcile renewable electricity generation to environmental sanitation.

Regarding the egg poultry manure, these materials are constituted by complex substrates containing particulate and dissolved organic matter as, for example, polysaccharides, lipids, proteins, volatile fatty acids, a high number of inorganic components and high concentrations of pathogenic organisms (Steil, Lucas Junior, & Oliveira, 2012). In a study performed by Minho et al. (2012), the authors evaluated the potential of biogas generation of this slurry mixed with sludge from wastewater treatment (WWTP) and obtained, at the end of 28 days, about 60% of C[H.sub.4]. Atuanya and Aigbirior (2002) evaluated the feasibility of the UASB reactor for wastewater treatment from poultry and obtained an average content of C[H.sub.4] of 57%, whereas in the study of Kalyuzhnyi, Fedorovich, and Nozhevnikova (1998) the CH 4 concentration was about 80%.

Among the technologies used for energy recovery from biomass, anaerobic digestion has been used in many applications, demonstrating ability to treat solid waste and effluents, also allowing nutrient recycling and energy recovery (Metcalf & Eddy Inc., 2003; Alvarez & Liden, 2008). This process occurs through distinct stages, and the initial stage of the degradation is the hydrolysis. During the hydrolysis, there is the transformation of polymers (starch, proteins, and carbohydrates) into monomers, such as amino acids and sugars, by enzymes produced by bacteria. These monomers, in the acidogenic phase, are transformed into volatile fatty acids (VFA) such as butyric, valeric and propionic acids. In the acetogenic stage, these volatile fatty acids are converted into acetic acid, carbon dioxide and gaseous hydrogen, which produce methane by cleavage of acetic acid (acetoclastic methanogenic) and from the reduction of carbon dioxide to molecular hydrogen (hydrogenotrophic methanogens) (Parker, 2005).

It is important to learn about the characteristics and the quantity of biogas produced, since this allows the identification of the constituent gases of biogas in order to optimize the further use of biogas for energy purposes.

The aim of this study was to analyze the physical and chemical factors on the performance of anaerobic digestion of the 'blend', a mix between WWTP sludge and poultry manure, and, further, to perform the characterization of the biogas in order to evaluate its quality.

Material and methods

The reading of gases and collection of material were performed in a biogas plant located in the metropolitan area of Porto Alegre, State of Rio Grande do Sul, Brazil. The blend samples were sent to the Laboratory of Bioreactors at the University Center Univates for physical and chemical analysis.

Initially the blend is produced, a mixture of liquid waste arising from various industrial processes and wastes from poultry manure. The blend is conducted to a container in order to achieve a minimum of 8% of total solids (TS). It is subsequently sieved to eliminate materials that may compromise the subsequent stages of the process, and then led through a pipe to three storage tanks, with capacity of 15 [m.sup.3] each.

At the considered biogas plant, the feeding is performed through a continuous stream comprising a storage tank, a piston flow type reactor (R1) with 450, and a vertical upflow reactor (R2) with 900 [m.sup.3] (Figure 1), plus two gasometers with 1,000 and 1,200 [m.sup.3] and a reservoir at the end of the process which is intended to the biofertilizer. For the pumping of the input material to the first reactor (R1) there is a timer system that sends blend parcels every 10 min, operating a total of 40 [m.sup.3] [day.sup.-1] in both R1 and R2 reactors.

[FIGURE 1 OMITTED]

The total hydraulic retention time is 30 days (R1: 10 days and R2: 20 days). R1 has agitation system divided into three zones (surface, middle and bottom) and R2 suffers agitation only when matter is supplied to it. Both are kept at 36 [degrees]C through a piping system with heat generated from the combustion of surplus biogas.

The characterization of gases was performed daily in both reactors (R1 and R2) for a period of three months, using a gas analyzer Oriun Plus[R], manufactured by MSA AER GmBH Company, which determined the percentage of C[H.sub.4], C[O.sub.2], [H.sub.2]S and O2 present in the biogas.

The collection points in the biogas plant are outlined in Figure 2, where R1 is the Reactor 1 and R2 is the Reactor 2. The sampling points are 1 (at the input of R1), 2 (between the output of R1 and the input of R2) and 3 (at the output of R2). The symbols: a *, b * and c * indicate the effectiveness of treatment demonstrated by the removal of the organic load, wherein: a* is the value for the analysis of the sample at the R1 input (1) in relation to the R2 input (2), b* is this value for analysis at the R2 output (3) in relation to the input (2), and c* is the value for the analysis of the sample at the R1 input (1) in relation to R2 output (3).

[FIGURE 2 OMITTED]

The physical-chemical parameters analyzed were: carbon (C), nitrogen (N), biochemical oxygen demand (BOD), pH, total (TS), volatile (VS) and fixed solids (FS). Samples were collected biweekly at three points: the input of material (point 1) and the outputs of the reactors R1 (point 2) and R2 (point 3). The equipment and method used for each parameter is presented in Table 1.

Results and discussion

Physical and chemical analyses

Table 2 presents the values given as average and standard deviation (SD) of BOD, C, N, C:N, FS, TS, VS and pH values of the sample points: 1 , 2, 3. The values of the removal for BOD and reductions of C, N, C:N, FS, TS, VS in a*, b* and c* are also shown in this table.

The average removal of samples [BOD.sup.a*], [BOD.sup.b*] and [BOD.sup.c*] were 69.34, 71.03 and 88.01% respectively. It was also obtained a [BOD.sup.c*] removal with efficiency equal to 98% at the end of the process (point 3) in a punctual analysis. The favorable removal obtained from sludge purification is due to R2, which is a reactor of upward flow type. However, it can be seen that R1 has achieved a considerable percentage of removal too. Analyzing the complete system, it was visualized a BOD removal efficiency that was even more satisfactory. In the study performed by Campos, Mochizuki, Damasceno, and Botelho (2005) about the treatment of wastewater from pig manure using the same type of reactor, the efficiency of this parameter was of 75%.

The effluent from the input (point 1) presented a concentration of 26,089.39 [+ or -] 10,436.18 mg L-1 of C and 1,780.91 [+ or -] 1,561.31 mg L-1 of N. The reduction obtained in [C.sup.a*] was of 23.19 [+ or -] 25.60%, showing that in some analyzes it was obtained an increase of carbon, as well as in [C.sup.c*], which presented 18.28 [+ or -] 36.74% of reduction. The best carbon reduction was obtained at the end of the process [C.sup.b*] (44.30 [+ or -] 26.19%). Concerning nitrogen, there was a better reduction in the second sampling point, after treatment in R1, with value of 24.69 [+ or -] 20.79. Subsequently there was an increase for this parameter in the middle.

The concentrations of carbon and nitrogen determine the performance of the anaerobic digestion process. The carbon is the source of energy for microorganisms and nitrogen stimulates microbial growth; therefore, so the process has optimum operation, the C: N should be 30: 1 (Igoni, Ayotamuno, Eze, Ogaji, & Probert, 2008). The C: N ratio of the sampling points 1, 2 and 3 were 22.88:1 [+ or -] 21.01:1; 7.62:1 [+ or -] 3,48:1 and 8.86: 1 [+ or -] 6.05:1; respectively. There was a normal process of anaerobic degradation, with initial and final values for C: N ratio close to optimum value. The C: N ratio was higher at point 3; we infer that the increase of carbon in the medium may have favored the microbial inhibition, reducing the ability of degradation of organic matter (Sgorlon, Rizk, Bergamasco, & Tavares, 2011). The input material presented C:N ratio in the range recommended Luna, Leite, Lopes, Silva, and Silva (2008), between 20: 1 and 30: 1, which is favorable to the biostabilization process. A satisfactory C: N ratio was also obtained at the end of the process, in accordance with Rao and Singh (2004), who explain that the C: N ratio of the stabilized waste varies between 10: 1 and 13: 1.

The average values of TS in the samples 2 and 3 were 7.14 and 7.65%, respectively. The input material contained about 7.72% of TS, which exceeded the level of 5% obtained by Felizola, Leite, and Prasad (2006) in the anaerobic treatment of organic waste.

The content of the VS of the sample points 1, 2 and 3 were 58.97, 55.53 and 52.22%, respectively. The higher the concentration of volatile solids in the daily diet of the digester ([m.sup.3] [kg.sup.-1]), the higher will be the biogas generation (Oliveira & Otsubo, 2002).

The FS at the sampling points 1, 2 and 3 were equal to 41.03, 44.47 and 47.78%, respectively. These values were consistent with a process of anaerobic degradation where an increasing trend of FS occurs over the time by volatilization of a portion of the total solids, which is in agreement with Nielsen (2011), who describes the increase that occurs on the fixed solids concentration with the passage of time due to the buildup of deposits and recalcitrant compounds in the system.

The average pH of the sample point 1 was 6.87 [+ or -] 0.63, whereas for the sample point 2 it was 7.85 [+ or -] 0.13 and, for the sample point 3, 7.88 [+ or -] 0.22. Even though there have been no significant changes in pH, this increase is associated with the buffering effect provided by biostabilization process of organic solid waste (Bouallagui, Cheikh, Marouani, & Hamdi, 2003). According to Gerardi (2003), at pH values between 6.8 and 7.2, methanogenic bacteria present a better performance, occurring the converting from volatile acids into C[H.sub.4] and C[O.sub.2]. The autor Gerardi (2003) explains that the pH of an anaerobic system is significantly affected by the presence of C[O.sub.2] in the biogas and pH values from below 6 to above 8 limit the methanogenic activity by presenting a toxic environment.

Characterization of the biogas

The average values and standard deviation of C[H.sub.4], C[O.sub.2], [H.sub.2]S and O2 present in R1 and R2 are shown in Table 3.

During the three months of monitoring, it was observed that the percentage of C[H.sub.4] in R1 was higher than the percentage of this gas in R2, which may be explained by a higher concentration of volatile fatty acids in R1, also confirmed by Felizola et al. (2006).

The percentage of C[H.sub.4] and C[O.sub.2] in R1 was of 75.76 and 24%; in R2 this percentage was of 74.64 and 25.07%, respectively. These values are similar to those obtained by Balde et al. (2016) the balance of C[H.sub.4]:C[O.sub.2] in the digestate storage was 74:26% by volume, which is similar to the 66% C[H.sub.4] content in the biogas produced in the digester.

The energy potential of biogas varies depending on the presence of C[H.sub.4] in its composition. Its quality for energy uses is directly proportional to the amount of methane it has. Regarding the inferior calorific power value (ICP) of the biogas, this depends on the ratio between C[O.sub.2] and C[H.sub.4] and, when the C[H.sub.4] concentration is high, the calorific power will have a high value too (Lima, 2005). According to Lima (2005), biogas with an ICP between 4,300 and 6,850 kcal [kg.sup.-1] is a very good primary source of energy. As mentioned by Leonzio (2016), biogas is composed approximately of 55-70% of C[H.sub.4] and 30-45% of C[O.sub.2], has the ICP equal to 6,253 kcal [kg.sup.-1]. Based on this, the biogas generated in this study fits in these recommended values, showing that the considered biogas plant has satisfactory energy potential and renewable purposes.

The average values of [H.sub.2]S ranged from 156.01 in R1 to 91.64 ppmv in R2. Considering the minimum and maximum values obtained in the present study, it can be stressed that they are in accordance with Nghiem, Manassa, Dawson and Fitzgerald (2014).

[FIGURE 3 OMITTED]

The amounts of [O.sub.2] in both reactors were very similar, resulting in an average of 0.23 in R1 and 0.25% in R2. It is important to note that the [O.sub.2] concentration was above 1% in both readings in R1 and in one reading in R2 during the first month of monitoring. High levels of [O.sub.2] in the biogas present risk of explosion inside the digester. Such situation can arise at the beginning of the operation, due to the input of the first charge of organic matter (Prati, 2010).

Table 4 depicts the Pearson correlation for the values of the main gases that constitute the biogas. In R1 there was only a significant positive correlation between the production C[H.sub.4] and [H.sub.2]S ([r.sup.2] = 44.98%; p = 0.0004 ). C[O.sub.2] presented a significant negative correlation with [H.sub.2]S ([r.sup.2] = -43.50%; p = 0.0006) and C[H.sub.4] ([r.sup.2] = -99.67%; p = 0.0001 ). In R2, the percentage of C[H.sub.4] was inversely proportional to the volume of C[O.sub.2], presenting a significant negative correlation ([r.sup.2] = -99.21%; p = 0.0001 ) between both.

C[H.sub.4] and C[O.sub.2] generation data can be observed in the graphical representation of Figure 3, which shows the percentage of C[H.sub.4] and its inverse proportion to C[O.sub.2] production in both reactors. The relative proportions in which C[O.sub.2] and C[H.sub.4] are produced from the original organic matter depend on the presence of sufficient inorganic oxidants, as nitrate, Mn, Fe or sulfate, which generate competition for organic matter to produce C[O.sub.2] or C[H.sub.4] (Yao & Conrad, 2000; Kruger, Frenzel, & Conrad, 2001).

Luque and Balu (2013), when the ratio between C[H.sub.4] and C[O.sub.2] reaches an average value of 1.5, the anaerobic treatment process reaches a steady state, that is, conditions under which the biogas produced by the process of anaerobic biostabilization of the organic matter contains, in average, 60 of C[H.sub.4] and 40% of C[O.sub.2]. In this study, the biogas produced in R1 provided a C[H.sub.4]:C[O.sub.2] ratio equal to 3.15, and equal to 2.98 in R2. The biogas obtained was mainly formed by two gases, C[H.sub.4] and C[O.sub.2], presenting an inversely proportional concentration of one over the other and still leaving traces of other gases characterized in this study ([H.sub.2]S and [O.sub.2]).

Conclusion

This research demonstrated that the blends of agro-industrial wastes treated in the studied biogas plant has a significant energy potential, presenting average values for the concentration of methane in the generated biogas of about 75%. The flow of waste from agro-industrial activities can present environmental and health hazard; however, by converting this waste into energy, the health and environment problems are solved, while the energy generated contributes to the sustainable development of society.

The generation of C[H.sub.4] is inversely proportional to C[O.sub.2] generation. During the monitoring period, the C[H.sub.4]: C[O.sub.2] ratio was of 3.15 for R1 and 2.98 for R2. Other parameters were assessed from the generated biogas. Concentration of [O.sub.2] presented values of 0.23 for R1 and 0.25 for R2, while for [H.sub.2]S, the values were equal to 156.01 in R1 and 91.64 ppmv in R2.

Concerning the evaluations of physical and chemical parameters, results obtained for the removal of BOD were satisfactory, presenting values of 69.34, 71.03 and 88.01% of removal in the analyzed sample points, whereas for the other parameters (C, N, pH, TS, FS and VS), the obtained values were consistent with the anaerobic degradation. The C: N ratio in the sampling points was equal to 22.88:1, 7.62:1 and 8.86:1, while the best reductions of C and N were found in the sampling points 2 and 3, with a reduction of 44.30 and 24.69%, respectively. The values of pH varied between 6.87 and 7.88, and the content of TS, VS and FS ranged from 7.14 to 7.72%, 52.22 to 58.97% and 41.03 to 47.78%, respectively.

Doi: 10.4025/actascitechnol.v38i4.28649

Acknowledgements

The authors thank the University Center Univates, CNPq (National Council for Scientific and Technological Development of Brazil), Fapergs (Foundation for Support to Research of the State of Rio Grande do Sul), and the companies Naturovos and Ecocitrus for supporting the implementation of this research work.

References

Alvarez, R., & Liden, G. (2008). Semi-continuos co-digestion of solid slaughterhouse waste manure, and fruit and vegetable waste. Renewable Energy, 33(4), 726-734.

AOAC International. (1995). Official methods of analysis of AOAC International (16th ed., 2 vols). Arlington, VA: Association of Analytical Communities.

Atuanya, E. I., & Aigbirior, M. (2002). Mesophilic biomethanation and treatment of poultry wastewater using pilot scale UASB reactor. Environmental Monitoring and Assessment, 77(2), 139-147.

Balde, H., Vanderzaag, A. C., Burtt, S. D., Wagner-riddle, C., Crolla, A., Desjardins, R. L., & Macdonald, D. J. (2016). Methane emissions from digestate at an agricultural biogas plant. Bioresource Technology, 216(9), 914-922.

Borges, E. S. M., & Chernicharo, C. A. L. (2009). Efeito do tratamento termico de lodo anaerobio sobre as caracteristicas de biodegradabilidade da fracao organica. Engenharia Sanitaria e Ambiental, 14(4), 489-498.

Bouallagui, H., Ben Cheikh, R., Marouani, L. E., & Hamdi, M. (2003). Mesophilic biogas production from fruit and vegetable waste in a tubular digester. Bioresource Technology, 86(1), 85-89.

Busca, G., & Pistarino, C. (2003). Technologies for the abatement of sulphide compounds from gaseous streams: a comparative overview. Journal of Loss Prevention in the Process Industries, 16(5), 363-371.

Campos, C. M. M., Mochizuki, E. T., Damasceno, L. H. S., & Botelho, C. G. (2005). Avaliacao do potencial de producao de biogas e da eficiencia de tratamento do reator anaerobio de manta de lodo (UASB) alimentado com dejetos de suinos. Ciencia e Agrotecnologia, 29(4), 848-856.

Diaz, I., Ramos, I., & Polanco, M. (2015). Economic analysis of microaerobic removal of [H.sub.2]S from biogas in full-scale sludge digesters. Bioresource Technology, 192, 280-286.

Felizola, C. S., Leite, V. D., & Prasad, S. (2006). Estudo do processo de digestao anaerobia de residuos. Agropecuaria Tecnica, 27(1), 132-187.

Gerardi, M. H. (2003). The microbiology of anaerobic digesters. New Jersey, NJ: John Wiley & Sons.

Goldemberg, J., & Paletta, F. C. (2012). Energias renovaveis. Sao Paulo, SP: Edgar Blucher.

Greenpro. (2004). Manual sobre tecnologias, projeto e instalacao. Retrieved from http://www.greenpro.de/po/bioenergia.pdf

Igoni, A. H., Ayotamuno, M. J., Eze, C. L., Ogaji, S., & Probert, S. D. (2008). Designs of anaerobic digesters for producing biogas from municipal solid-waste. Applied Energy, 85(6), 430-438.

Kalyuzhnyi, S., Fedorovich, V., & Nozhevnikova, A. (1998). Anaerobic treatment of liquid fraction of hen manure in UASB reactors. Bioresource Technology, 65(3), 221-225.

Kapdi, S. S., Vijay, V. K., Rajesh, S. K., & Prasad, R. (2005). Biogas scrubbing, compression and storage: perspective and prospectus in Indian context. Renewable Energy, 30(8), 1195-1202.

Kruger, M., Frenzel, P., & Conrad, R. (2001). Microbial processes influencing methane emission from rice fields. Global Change Biology, 7(1), 49-63.

Leonzio, G. (2016). Upgrading of biogas to bio-methane with chemical absorption process: simulation and environmental impact. Journal of Cleaner Production, 131(10 ), 364-375

Luque, R., & Balu, A. M. (Ed.). (2013). Producing fuels and fine chemicals from biomass using nanomaterials. Boca Raton, FL: CRC Press.

Lima, F. P. (2005). Energia no tratamento de esgoto: analise tecnologica e institucional para conservacao de energia e uso do biogas. Sao Paulo, SP: USP.

Luna, M. L. D., Leite, V. D. L., Lopes, W. S., Silva, A. S., & Silva, J. V. N. (2008). Tratamento anaerobio de residuos solidos organicos para pequenas comunidades. Agropecuaria Tecnica, 29(1-2), 21-34.

Metcalf & Eddy Inc. (2003). Wastewater engineering treatment disposal reuse (4th ed.). New York City, NK: McGraw Hill Book.

Minho, C. V., Konrad, O., Koch, F. F., Kleinschmitt, A. B., Casaril, C., & Lumi, M. (2012). Uso da glicerina residual na geracao de biogas a partir do lodo de estacao de tratamento de efluentes e dejetos de aves poedeiras. Engenharia Ambiental - Espirito Santo do Pinhal, 9(3), 41-50.

Nghiem, L., Manassa, P., Dawson, M., & Fitzgerald, S. K. (2014). Oxidation reduction potential as a parameter to regulate micro-oxygen injection into anaerobic digester for reducing hydrogen sulphide concentration in biogas. Bioresource Technology, 173, 443-447.

Nielsen, S. (2011). Sludge treatment reed bed facilities--organic load and operation problems. Water Science Technology, 63(5), 942-948.

Oliveira, P. A. V., & Higarashi, M. M. (2006). Geracao e utilizacao de biogas em unidades de producao de suinos. Concordia, SC: Embrapa Suinos e Aves.

Oliveira, P. A. V., & Otsubo, C. S. (2002). Sistema simples para a producao de biogas com o uso de residuos de suinos e aves. Gerenciamento Ambiental, 4(19), 12-15.

Pagliuso, J. D., & Regattieri, R. C. (2008). Estudo do aproveitamento da energia do biogas proveniente da incineracao do chorume para a geracao de eletricidade. Revista Brasileira de Ciencias Ambientais, 16, 32-38.

Parker, W. J. (2005). Application of the ADM1 model to advanced anaerobic digestion. Bioresource Technology, 96(16), 1832-1842.

Prati, L. (2010). Geracao de energia eletrica a partir de biogas gerado por biodigestores (TCC). Universidade Federal do Parana, Curitiba.

Rao, M. S., & Singh, S. P. (2004). Bioenergy conversion studies of organic fraction of MSW: kinetic studies and gas yield-organic loading relationships for process optimization. Bioresource Technology, 95(2), 173-185.

Sanquetta, C. R., Balbinot, R., & Ziliotto, M. A. B. (2004). Fixacao de carbono: atualidades, projetos e pesquisas. Curitiba, PR: AM Impressos.

Sgorlon, J. G., Rizk, M. C., Bergamasco, R., & Tavares, C. R. G. (2011). Avaliacao da DQO e da relacao C/N obtidas no tratamento anaerobio de residuos fruti-horticulas. Acta Scientiarum Technology, 33(4), 421-424.

Steil, L., Lucas Junior, J., & Oliveira, R. A. (2002). Avaliacao do uso de inoculo na digestao anaerobia de residuos de aves de postura, frangos de corte e suinos. Engenharia Agricola, 22(2), 146-149.

Torres, J. C., & Osorio, F. (2009). Biogas purification from anaerobic digestion in a wastewater treatment plant for biofuel production. Renewable Energy, 34 (10), 2164-2171.

Yao, H., & Conrad, R. (2000). Electron balance during steady-state production de C[H.sub.4] and C[O.sub.2] in anoxic rice soil. European Journal Soil Science, 51(3), 369-378.

Received on July 27, 2015.

Accepted on February 5, 2016.

Odorico Konrad *, Joao Vicente Akwa, Fabio Fernandes Koch, Marluce Lumi and Jaqueline Tonetto

Centro de Ciencias Exatas e Tecnologicas, Unidade Integrada Vale do Taquari de Ensino Superior, Avenida Avelino Talini, 171, 95900-000, Lajeado, Rio Grande do Sul, Brazil. * Author for correspondence. E-mail: okonrad@univates.br
Table 1. List of parameters and their methods or models of
equipment.

Parameter                      Equipment              Method or
                                                   equipment model

BOD                             Oxitop                IS 6, TWT

Nitrogen               Digester and distillation      PHA/AWWA

Carbon                       Heating plate            PHA/AWWA

pH                             pH meter            DM-2P, Digimed

Volatile solids (VS)      Muffle and hothouse      Association of
                                                      Official
                                                     Analytical
                                                   Chemists (AOAC,
                                                        1995)

Total solids (TS)              Hothouse              AOAC (1995)

Table 2. Average and standard deviation for the analyzed physical
and chemical parameters.

Parameter         (1) R1 input      (2) between R1    (3) output R2
                                    output  and
                                    input R2

                               (average [+ or -] SD)

C (mg [L.sup.-    26,089.39 [+ or   18,474.07 [+ or   18,259.60 [+ or
1])                -] 10,436.18       -] 6,100.12       -] 9,468.10

N (mg [L.sup.-    1,780.914 [+ or   2,750.59 [+ or    2,241.19 [+ or
1])                 -] 1,561.31        -] 465.21         -] 910.53

C: N              22.88 [+ or -]     7.62 [+ or -]     8.86 [+ or -]
                       21.02             3.48              6.05

BOD (mg           38,000.00 [+ or   10,166.70 [+ or   5,250.00 [+ or
[L.sup.-1])        -] 17,193.02       -] 3,970.73       -] 4,645.79

pH                 6.87 [+ or -]     7.85 [+ or -]     7.88 [+ or -]
                       0.63              0.13              0.22

FS (%)            41.03 [+ or -]    44.47 [+ or -]    47.78 [+ or -]
                       12.98             9.18              7.19

TS (%)             7.72 [+ or -]     7.14 [+ or -]     7.65 [+ or -]
                       1.69              1.37              2.30

VS (%)            58.97 [+ or -]    55.53 [+ or -]    52.22 [+ or -]
                       12.98             9.18              7.19

Parameter         a *               b *               c *

                                 (average [+ or -] SD)

C (mg [L.sup.-    23.19 [+ or -]    18.28 [+ or -]    44.30 [+ or -]
1])                    25.60             36.74             26.19

N (mg [L.sup.-    -116.8 [+ or -    24.69 [+ or -]    -41.41 [+ or -
1])                  ] 102.34            20.79            ] 73.31

C: N              51.08 [+ or -]    1.730 [+ or -]    52.60 [+ or -]
                       28.85             45.00             38.35

BOD (mg           69.33 [+ or -]    71.03 [+ or -]    88.01 [+ or -]
[L.sup.-1])            16.47             32.36             18.25

pH                      --                --                --

FS (%)                  --                --                --

TS (%)                  --                --                --

VS (%)                  --                --                --

Table 3. Average values and standard deviations for the
parameters of the gases present in reactors 1 and 2.

Parameters   C[H.sub.4]   C[O.sub.2]   [H.sub.2]S     [O.sub.2]
                %-SD         %-SD        ppmv-DP         %-SD

Reactor 1    75.76-3.09   24.00-3.02   156.01-53.64   0.23-0.26
Reactor 2    74.64-2.33   25.07-2.28   91.640-49.69   0.25-0.26

Table 4. Indexes of the Pearson correlation ([r.sup.2]%) and the
difference (p < 0.05) of the constituent parameters of biogas
between them even in reactors 1 and 2 (R1 and R2).

Parameters              C[O.sub.2] (%)          [H.sub.2]S (ppmv)

                                           [r.sup.2]%-p

C[O.sub.2] (%)                --              [-43.6%-0.0006.sup.R1]
[H.sub.2]S (ppmv)   [-8.630%-0.5155.sup.R2]             --
C[H.sub.4] (%)      [-99.21%-0.0010.sup.R2]   [8.14%-0.5397.sup.R2]
[O.sub.2] (%)       [17.24%-0.1916.sup.R2]    [-9.11%-0.4924.sup.R2]

Parameters              C[H.sub.4] (%)             [O.sub.2] (%)

                                           [r.sup.2]%-p

C[O.sub.2] (%)      [-99.67%-0.0010.sup.R1]   [23.53%-0.0720.sup.R1]
[H.sub.2]S (ppmv)   [44.98%-0.0004.sup.R1]    [-28.47%-0.2880.sup.R1]
C[H.sub.4] (%)                --              [-31.38%-0.0155.sup.R1]
[O.sub.2] (%)       [-7.86%-0.0326.sup.R2]              --
COPYRIGHT 2016 Universidade Estadual de Maringa
No portion of this article can be reproduced without the express written permission from the copyright holder.
Copyright 2016 Gale, Cengage Learning. All rights reserved.

Article Details
Printer friendly Cite/link Email Feedback
Author:Konrad, Odorico; Akwa, Joao Vicente; Koch, Fabio Fernandes; Lumi, Marluce; Tonetto, Jaqueline
Publication:Acta Scientiarum. Technology (UEM)
Date:Oct 1, 2016
Words:5012
Previous Article:Cost-benefit analysis of the construction of different flexible pavement structures considering the axle load and type of binder/Analise...
Next Article:Utilization of low-cost substrates for the production of nystose by Bacillus subtilis natto cct 7712/Utilizacao de substratos de baixo custo para...
Topics:

Terms of use | Privacy policy | Copyright © 2021 Farlex, Inc. | Feedback | For webmasters |