Received 10 July 2015; accepted 19 September 2015; published 22 September 2015

ABSTRACT

The objective of this study was to evaluate the performance of anaerobic digestion (AD) within the intermediate zone, specifically at 45˚C. Single-stage batch anaerobic digestion system was developed in the lab and performance was monitored for more than 2 years. The AD system was able to achieve high biogas production with about 62% - 67% methane content. The digester exhibited high acetate accumulation, but sufficient buffering capacity was observed as the pH, alkalinity and volatile fatty acids-to-alkalinity ratio were within recommended values. The system achieved 36.5% reduction of total solids (TS) and 47.8% reduction of volatile solids (VS), which exceeded the required VS destruction efficiency for Class A biosolids. The pathogen counts were less than 1000 MPN/g total solids in the effluent, which also satisfied Class A biosolids requirements. The accumulation of acetate was presumably due to the high temperature which contributed to high hydrolysis rate. Consequently, it produced large amount of toxic salts that combined with the acetate, making them not readily available to be consumed by methanogens. The slower degradation of acetate was observed by the kinetic parameters. Accumulation of acetate contributed to 52% to 71% reduction in acetate degradation process, but was not completely inhibitory. The methanogens existing in the system were mostly thermo-tolerant acetate-utilizing methanogens, and specifically from Methanosarcinaceae species.

Keywords:

Anaerobic Digestion, Acetate Accumulation, Salt Toxicity, Inhibition Kinetics

1. Introduction

Anaerobic digestion has been the most widely used method for the degradation and stabilization of domestic and industrial wastes for many years. This process has received increased attention in the recent years due to global energy crisis, as anaerobic digestion has great potential for producing energy-rich biogas and nutrient-rich biosolids. Strict environmental regulations for pollutant minimization also demonstrated the need of anaerobic digestion for safe and effective method of organic waste disposal.

Anaerobic digestion (AD) is a biological process that converts complex substrates into biogas and digestate by microbial action in the absence of oxygen through four main steps, namely hydrolysis, acidogenesis, acetogenesis and methanogenesis [1] . Anaerobic digestion of wastewater sludge has generally been conducted within the mesophilic temperature range of 30˚ - 40˚C or thermophilic temperature range of 55˚ - 60˚C. The mesophilic system is often preferred due to its good operational performances, good effluent quality, higher degree of stability and comparatively low energy requirement. Despite that, mesophilic anaerobic digestion usually requires long retention time, produces insufficient reduction of volatile solids and deactivates insufficient amount of pathogens [2] - [4] . To overcome the limitations, thermophilic anaerobic digestion has been the technology of choice due to enhanced hydrolysis of complex organic materials, higher solids destruction efficiency, better dewatering capability, ability to sustain higher loading of waste, reduction in foaming and most importantly the production of biosolids that meets United States Environmental Protection Agency (U.S. EPA) Class A biosolids specifications [5] - [7] . However, several studies have reported that the slightly higher rates of hydrolysis and fermentation in thermophilic digesters have not necessarily led to a higher methane yield and can be disadvantageous due to large amount of energy required for heating, the increased sensitivity to environmental factors and poor effluent quality with high volatile fatty acids (VFA) content [2] [6] [7] .

Although a large number of researchers have addressed the performance of mesophilic and thermophilic anae- robic digestion, very few studies have investigated the possibility of operating anaerobic digestion in the intermediate zone between mesophilic and thermophilic range. This is based on the assumption that limited microbial activity occurs within the intermediate zone of 40˚ - 50˚C due to the fact that neither mesophilic nor thermophilic microorganisms would flourish in the intermediate zone, as the microorganisms are trying to cope with the changing environment, hence causing the digestion to slow down [8] . However, few recent studies have triggered questions regarding its validity as 45˚C anaerobic digestion system was still producing gas and was significantly similar, or even higherthan the mesophilic system [4] [9] . Good effluent quality in terms of COD removal efficiency, ranging from 81.5% to 91.2%, was observed using 45˚C digester [10] and there was no great variation between anaerobic digestion systems operating at 37˚C and 45˚C in terms of methane production, volatile solids (VS) content and pH, except for VFA concentration that increased significantly with increasing temperature [11] . Ref. [12] exhibited a significant increase in VS removal with the rise in temperature and approaches a plateau at 45˚C. The degree of acidification (VFA/tCOD) was highest at 45˚C and was chosen as optimum temperature for acidogenic phase [13] . However, none of these studies have done any further investigation in finding the reasons behind the accumulation of VFAs observed in their digestion system, as well as the capability of the system to produce Class A biosolids. The above findings imply that microbial activities are still occurring within the intermediate zone, and thus it is necessary to further investigate whether they are mesophilic activities, or thermophilic activities, or possibly activities involving both types of microorganisms.

According to U.S. EPA, Class A biosolids can only be produced through treatment processes involving high temperatures such as thermophilic anaerobic digestion [14] . The motivations for this research were, if the 45˚C anaerobic digestion system could produce comparable amount of methane as the mesophilic digester, and could generate same quality of biosolids as thermophilic digester, there could be significant economic benefits by operating the digester at 45˚C, in comparison to the conventional thermophilic digester. This study investigated the performance of anaerobic digestion within the intermediate zone, specifically at 45˚C, and the potential for generating Class A biosolids. In addition, the possible inhibition kinetics for the accumulation of VFAs at higher temperature was also analyzed.

2. Materials and Methods

2.1. Anaerobic Digester Setup

Two single-stage batch anaerobic digestion systems were constructed and operated in parallel, where the second system served as a duplicate. The digester was made of high density polyethylene (HDPE) 25 L brewery tanks of Hobby Beverage Equipment Company (Temecula, California). The temperature of the digester was maintained at 45˚C with a heating system controlled by a thermostat connected to a temperature sensor inserted into the digester. The digester was covered with aluminum foil and temperature adjustable heating tape was placed on top of the foil to ensure even heat distribution to the digester and to provide protection from the heating tape so that physical failure of the polyethylene would not occur. Gas mixing was applied by circulating the headspace gas to the bottom of the digester by using a peristaltic pump (Cole-Parmer, Vernon Hills, IL). The digester was equipped with a gas collection flask and Wet Tip gas meter (Nashville, TN) to measure volume of gas production. Figure 1 shows the schematic diagram of the anaerobic digestion system.

2.2. Digester Start-Up and Operations

The anaerobic digester system was initiated by inoculating with seed sludge from well operating mesophilic anaerobic digester in Alexandria Wastewater Treatment Plant, AlexRenew (Alexandria, VA). This was done to benefit from the seed sludge that usually contains abundant amounts of microorganisms such as methane formers and acid forming bacteria. After approximately 3 days of seed feeding, the digester system was fed with raw municipal sludge obtained from Blue Plains Advanced Wastewater Treatment Plant (Washington, DC). The raw sludge was the effluent after the thickening process. During this initial phase, no effluents were taken out as the microorganisms need to have ample time to establish themselves within the new environment. After approximately two weeks, duration that was considered sufficient for microorganisms’ adaptation, the feeding and effluent withdrawing schedules were started. The digester was fed once a day and an equal amount of digested sludge or effluent was withdrawn directly before feeding.

The operational volume of the anaerobic digester was 15 L. The total solids (TS) content of the feed sludge (influent) was 6.5% with an average organic loading rate (OLR) of 5.22 kgVS/m³・d. The feed sludge was acclimated to the desired temperature of 45˚C by incubating for approximately 2 h before feeding. The solid retention time (SRT) of 10 d was selected for the digester, which is regarded as optimum time for the methanogens to complete the digestion process. Because the digester was kept completely mixed throughout the study, and

feeding and wasting were done in equal amounts, solids retention time (SRT) of the reactor was equal to hydraulic retention time (HRT).

Inorganic nutrients in the form of chloride salts were added into the anaerobic digester systems, as an initiative to increase the rate of anaerobic metabolism in term of methane gas production and low VFA accumulation [6] [15] . Typically, the feed may contain more than ample nutrients, but its bioavailability can be limiting due to precipitation reactions occurring during the digestion process. Table 1 lists the inorganic nutrients prepared from the chloride salts (Acros Organics, NJ). 2 mL of each nutrient was added to the feed sludge before the feeding process.

2.3. Experimental Methods

The operating parameters of the feed and digested sludge were analyzed regularly for more than 2 years of operations. The pH was measured daily, while the alkalinity, total solids (TS), volatile solids (VS), soluble COD (sCOD), total COD (tCOD), total ammonia nitrogen (TAN) and volatile fatty acids (VFA) were analyzed weekly. Alkalinity, TS, VS, COD and TAN tests were conducted in accordance to Standard Methods 2320 B, 2540 B, 2540 E, 5220 D and 4500-NH₃ B & C, respectively [16] . VFA was analyzed using a Shimadzu Gas Chromatograph Model GC-2010 (Shimadzu, Columbia, MD) with flame ionization detector (FID) and equipped with a RestekStabilwaxfi-DA capillary column. The column temperature was 145˚C, and the injector and flame ionization detector temperature was 250˚C. The calibration curves were obtained using five aqueous solutions of organic acids: acetic, propionic, butyric, valeric and caproic, in the concentration range of 25 to 1000 𝜇L/L. The feed and digested sludge was analyzed for pathogens using MPN Method as described in EPA Method 1680 [17] . The total biogas production was monitored daily using a Wet Tip gas meter (Nashville, TN) and gas composition was analyzed using SRI 8610 C Gas Chromatograph (SRI Instruments, Torrance, CA) equipped with a flame ionization detector (FID) with Helium as the carrier gas. Sludge samples from the digesters were sent to MRDNA laboratory (Shallowater, TX) for methanogen Illumina Assays, to obtain the methanogen species and counts.

2.4. Batch Kinetic Tests

The effluent from the digester was collected and used as a sample for batch kinetic tests. The effluent was first diluted to eliminate the possible inhibition effects of existing soluble compounds such as ammonia and acetate. Subsequently, the samples were mixed and placed in 500 mL glass bottles. The temperature was controlled and the headspace was flushed with nitrogen gas to create anaerobic condition within the vessel. The substrate (acetic acid) was added in a diluted form of synthetic acetic acid 2.0 N (Fisher Chemical, Pittsburgh, PA) to the samples. The tests were conducted using 400 mL of digester effluent, mixed at least once a day using a magnetic stirrer and incubated at 45˚C. The concentrations of the remaining acetate were observed for every 30 min to 1 h intervals and the tests were conducted until all acetate has been harvested or when there is no further destruction of the remaining acetate.

During the kinetic tests, the concentrations of remaining unionized acetate, S at different sampling time, t was collected. Unionized acetate progress curve was plotted and the model was developed to fit these curves. The kinetic coefficients were determined using a Monod-based model [18] .

The Monod model is shown in Equation (1), and the model proposed by Ref. [18] is presented in Equation (2).

(1)

where µ, µ_max and S are specific growth rate (t⁻¹), maximum specific growth rate (t⁻¹) and concentration of growth-limiting substrate (mg/L), respectively. K_s is half saturation constant, substrate concentration at one-half the maximum growth rate. In the model, the best estimates of the kinetic coefficients and constant can be determined by minimizing differences between model predictions to observed experimental values of sampling time t using Equation (2).

(2)

where Y is the yield coefficient (mg/mg), and r_max is the maximum bacterial growth rate (mg/L・d). The model predictions of t were calculated by using the known value of Y together with initial estimates of the parameters that are sought (i.e. K_s, r_max and S₀). In this model, S₀ was also used as a fitting parameter because it was not known with greater certainty than the other data points, thus, it would not be appropriate to force the best-fit curve through the measured value of S₀ [18] . The best fit was obtained with Solver function in Microsoft Excel, which used an iterative search for the parameter values that yielded the minimum square errors, and the initial estimates of the parameters were automatically replaced by the parameters best estimates.

The inhibition kinetic coefficient, K_I and dimensionless inhibition concentration, I_HAc, were determined using a Michaelis-Menten model [19] . Equation (3) shows the basis of the model.

(3)

where v is the rate of substrate utilization (substrate/unit volume・time), V_m is the maximum specific rate (t⁻¹) and K_m is the substrate utilization constant or saturation constant (mg/L). Detail parameter estimation process using the extended version of the model, depending on the type of inhibition, are available in [19] .

3. Results and Discussions

3.1. Performance of Anaerobic Digestion at 45˚C

The performance of the anaerobic digestion (AD) at 45˚C was assessed based on methane gas production, methane yield, biogas composition, ammonia content, VFA content, buffering capacity, TS and VS reductions, soluble and total COD reductions as well as pathogen destruction. Daily methane production of the anaerobic digester is illustrated in Figure 2. In general, increasing trends of methane gas over time was observed in the system indicating

that as the days progressed, the microbes had established, flourished and expanded their colonies, hence, contributed to the gradual increase of methane production.

The specific methane yield for the AD system was 0.56 ± 0.04 m³・CH₄/kgVS removed, which is within the lower end of the recommended range of 0.60 to 1.60 m³・CH₄/kgVS removed [20] . The composition of methane in the headspace gas was 66.08 percent which is comparable to the values for mesophilic digesters found in the literatures. The absence of any clear and sharp decline of gas production at 45˚C implies that there may not be a transition zone between mesophilic and thermophilic zones that inhibit the methane forming activity. Instead, as mesophilic methane formers exist in mesophilic zone, and thermophilic methane formers exist in thermophilic zone, there might be an overlap between these two zones that still allow methane formation by both types of microorganisms. The lower methane yield of the 45˚C AD system can be associated to its operation within the intermediate zone of mesophilic and thermophilic, therefore not providing an optimum growth environment for either type of methane formers, and subsequently affecting the amount of methane produced.

Since inhibition of the anaerobic digestion system is primarily indicated by the levels of total ammonia (TAN) and free ammonia generated within the system, therefore both were measured in the study. The average TAN and free ammonia concentrations were found to be 1735 mg/L and 83 mg/L, respectively. The TAN concentrations were slightly higher than the lower limit of the inhibitory region of 1500 and 3000 mg/L [21] , whereas the level of free ammonia was lower than the inhibitory level of 100 to 150 mg/L [22] . The higher TAN concentrations may have exerted a detrimental effect on the methanogens, particularly on the acetate-utilizing methane formers. However, inhibition was not observed, as the 45˚C digesters have been operated for more than 2 years with sufficient VS destruction and methane production, as well as stable pH levels. A gas chromatographic analysis of the VFA in AD system showed that they consisted of acetate, propionate, butyrate and valerate, with the first two being the predominant components. As acetate accounted for a significant majority of the total VFA concentration, it was thus the most sensitive VFA indicator of digester operation. The average concentrations of all types of VFAs for the feed and digester effluent are presented in Figure 3.

Buffering capacity is also a crucial indicator of the well-being of anaerobic digester. The average pH and alkalinity of the digester were 7.41 and 10,082 mg/L, respectively. pH value was within high end of the operable pH range value of 6.6 - 7.6 [23] . The increased pH value in 45˚C AD was due to reduced solubility of carbon dioxide at higher temperature. With regard to alkalinity, an anaerobic digestion system requires an alkalinity of at least 1500 mg/L in the presence of biogas containing about 30 percent carbon dioxide [24] . Within the AD system, the alkalinity was observed to be as high as 10,000 mg/L and apparently, high alkalinity was favorable as it provided effective buffering against a pH drop due to the accumulation of VFAs. Higher alkalinity usually indicates a greater amount of protein conversion resulting in high ammonia content as well as salts. In a digester, these salts produce natural buffers, which normally remain fairly constant at about 3000 to 4000 mg/L [25] .

Additionally, other than ammonia and salts, the increase in alkalinity was also attributed to its high

concentration of VFA observed in 45˚C systems. As VFA concentrations began to increase, they are neutralized by the bicarbonate alkalinity, thus, forming volatile acid alkalinity [23] . Therefore, instead of only having bicarbonate alkalinity, which is normally observed in mesophilic systems, the 45˚C systems now had total alkalinity composed of bicarbonate alkalinity and volatile acid alkalinity. As a result, the VFA-to-alkalinity ratio, an estimate to enumerate the ability of the system’s capacity to cope with rapid change in pH, was 0.16 which is well below the suggested inhibition value of 0.4 [26] .

With regard to the ability of the digester for reducing TS and VS content, the system was able to achieve 36.5% reduction of TS and 47.8% reduction of VS, which exceed the required average VS destruction efficiency of 45% for Class A biosolids criterion for vector attraction reduction [27] . High TS and VS reductions in 45˚C system implied an increase in dewatering capabilities of the digested effluent due to its reduced viscosity and a better separation of solids. In addition to that, it also suggested an increase in sludge reduction as well as sufficient sludge stabilization.

The system was able to achieve significantly high reduction of soluble COD (sCOD), total COD (tCOD) and pathogen from the feed, as presented in Table 2. Pathogenic bacteria are an important factor to consider, if the sludge is to be used as a fertilizer or soil amendment. The AD system at 45˚C had successfully achieved 3-log reduction of fecal coliforms, which is very difficult to achieve by the traditional mesophilic digester at 35˚C. The concentration of fecal coliforms in the digested sludge never exceeded 1000 MPN/g total solids, thus met the U.S. federal fecal coliform requirements for Class A biosolids [27] . The higher deactivation of pathogens was probably a result of the combined effects of high temperature, VFA, TAN, free ammonia and long retention time.

3.2. Acetate Accumulation in Anaerobic Digestion at 45˚C

Anaerobic digester at 45˚C produced significantly high acetate accumulation, as shown in Figure 3, due to high hydrolysis rate at higher temperature. In some cases, they were even higher than the feed itself, even though methane was continuously produced throughout the process. They were four reasons that possibly contributed to this situation. First, at higher temperature, more proteinaceous materials were degraded and created ammonia-stress condition which had a negative influence on acetate-utilizing methanogens in comparison to the other microbes (i.e. acetate-producing acidogens). As a result, acetate was produced faster than they could be utilized, hence allowing them to accumulate within the system. Second, the abundance of acetate in the effluent suggested that instead of functioning as a fully methanogenic digester, it was serving more as an acid-phase digester. In other words, the methanogenesis process had not reached a complete steady state yet. If more time were to be given to the methanogens, more appreciable acetate reduction would be expected. Third, at 45˚C, instead of acting as a transition zone that inhibits microbial activity, there might be an overlap between these two zones that allow the methane to be formed despite the accumulation of VFA. The said methane formers might be the hydrogen-utilizing thermophilic methanogens instead of acetate-utilizing mesophilic methanogens. Presumably, the colonies of hydrogen-utilizing thermophilic methanogens which was at its optimum at higher temperature, were more abundant in number, hence leaving the other methanogens’ substrate, acetate, not fully utilized. Lastly, it might also be caused by the way the digester was started up. The 45˚C digester was started up by increasing the temperatures slowly from the mesophilic operating temperature. This technique was likely to lead to the development of a population that was different from a population obtained through a true thermophilic digester.

The population was most probably a thermo-tolerant acetate-utilizing mesophilic methanogens, a mesophile that can survive at high temperature but whose optimum growth rate occurs at mesophilic temperatures [28] . Thus, the operating temperature of 45˚C might not be the optimum temperature for the microbes, hence affecting

their methanogenic activity. At 45˚C AD system, the population of true acetate-utilizing mesophilic methanogens or thermo-tolerant acetate-utilizing mesophilic methanogens were gradually diminishing, due to the high ammonia content and high temperature, hence, leaving more acetate unutilized.

As for the presence of propionate, though was commonly believed to also inhibit methanogenesis, the concentrations were well below the tolerable range of 800 mg/L to 3000 mg/L [15] [29] , whereas the presence of butyrate and valerate were remained minimal in the digester.

3.3. Kinetics of Acetate Accumulation

A series of kinetic tests were performed in order to investigate the accumulation and inhibitory effect of acetate despite the abundant generation of methane in 45˚C anaerobic digestion system. The comparisons were made between systems containing different sources of acetate, one was found naturally in the system, while the other one, was added in a form of acetic acid to the system. In this study, the former was termed as background acetate (B/g HAc) or salt-originated-acetate and the later was termed as added acetate (HAc) or acetic acid-origi- nated-acetate. Four sets of experiments were conducted varying the concentration of background acetate and added acetate, and corresponding kinetic parameters are summarized in Table 3.

Figure 4 presents the progress curve of acetate degradation at different background acetate (B/g HAc) concentration of 500, 1000 and 1500 mg/L. All the kinetic parameter values in the system were decreasing as the background acetate concentration increased, as shown in Table 3, indicating slower acetate degradation at higher concentration. Figure 5 shows the progress curve of acetate degradation with and without the added acetate (HAc). Observing Figure 4 and Figure 5, it was clear that the system with added acetate degraded faster than the system with background acetate source. This observation was evidenced by its K_s, r_max and I_HAc values which were higher in the system with added acetate in comparison to the system with background acetate.

Figure 6 compares the acetate degradation by individually considering the background acetate (B/g HAc) and added acetate (HAc), and showed that almost negligible acetate left in the case with added acetate in comparison to more than 400 mg/L acetate left in the case with background acetate. Such distinct differences in the degradation pattern with different sources of acetate are explained below.

In anaerobic digestion process, hydrolysis is always rate limiting [30] , i.e. organic materials in solid portion of the sludge are slowly hydrolyzed and brought into solution by the microorganisms present in the digester. Under optimal operating conditions, the organic matter is broken down into VFAs by acid formers, and decomposed rapidly into carbon dioxide and methane by methane formers. During the process, there is a buildup of certain salts in solution such as ammonium, calcium, magnesium, potassium and sodium resulting from the break-up of proteins. As the cations of salts in solution must always be associated with the anions, it might possibly be bonded with the acetate produced from acidogenesis, hence contribute significantly in the generation of acetate

salts [31] . Acetate that was naturally found in the system was the accumulation of acetate from acetic acid produced through acidogenesis, as well as the anion parts of the acetate salts. Acetate that was added into the system was solely from the dissociation product of added acetic acid. Thus, with regard to lower degradation rate indicated by the r_max and K_s values with the presence of background acetate, it can be postulated that the system suffered from salt toxicity caused by acetate salts. As the background acetate concentration increased, more acetate salts were formed, and contributed to the slowing down of the degradation process. However, the toxicity effect was not detrimental as the system was still able to degrade the acetate, though not as fast as the system without acetate salts.

Another observation from Figure 6 was the inability of the system with salt-originated-acetate or background acetate (B/g HAc) to utilize the acetate to a very minimal or almost negligible content, in comparison to almost complete acetate utilization found in the system with acetic acid-originated-acetate (HAc). This is due to the inability of the salt-originated-acetate to completely dissociate itself at the experimental conditions thus making the acetate anion not readily available for consumption by the methanogens, as opposed to acetic acid-origi- nated-acetate that dissociated more readily at the experimental conditions hence explaining the almost complete utilization of acetate. In terms of inhibitory condition, it was observed that the presence of salt-originated acetate,

which contributed to 52% to 71% reduction in acetate degradation process, could not be considered as completely inhibitory as there was still utilization of acetate at a lower rate.

3.4. Methanogen Count of Anaerobic Digester at 45˚C

Methanogen Illumina Assay of the sludge from the 45˚C anaerobic digester verified the presence of the presumptive methanogens. Methanosarcinaceae, a methanogen from mesophilic group was the dominant methanogen found in the system. Comparing the K_s value of the kinetic experiment (Run 4: B/g HAc + HAc = 0 + 1000 mg/L) with K_s values of two dominant mesophilic methanogens, Methanosarcinaceae with K_s of approximately 200 mg/L as HAc and Methanosaetaceae with K_s of approximately 30 mg/L as HAc [15] , revealed that the methanogens of the 45˚C AD system belong to Methanosarcinaceae type. Since the methanogens were able to survive high temperature condition, the said methanogens were probably the thermo-tolerant Methanosarcinaceae. Further assay, which demonstrated that Methanosarcinaceae existed in significant numbers of 82.47% in the digester, confirmed the findings.

4. Conclusion

Anaerobic digesters operated at 45˚C for more than 2 years demonstrated high biogas production with methane content of 62% - 67%. The system was able to achieve 47.8% reduction of volatile solids and pathogen count of less than 1000 MPN/g total solids in the digester effluent, satisfying U.S. EPA Class A biosolids requirements. Although the digester showed high acetate accumulation, it was not detrimental as evidenced by adequate buffering capacity and abundant production of methane. The accumulation of acetate produced large amount of toxic salts that combined with the acetate, making them not readily available to be consumed by methanogens, and resulted in 52% to 71% reduction in the acetate degradation process. The methanogens existing in the system were mostly thermo-tolerant acetate-utilizing methanogens with 82.47% Methanosarcinaceae species.

Acknowledgements

This study was supported by a grant from the United States Department of State under the Pakistan-US Science and Technology Cooperation Program. The authors gratefully acknowledge the assistance of the staff of Blue Plains Advanced Wastewater Treatment Plant in Washington, DC, for providing the feed sludge for the digesters.

Cite this paper

Nuruol SyuhadaaMohd,TaqsimHusnain,BaoqiangLi,BaoqiangLi,ArifurRahman,RumanaRiffat, (2015) Investigation of the Performance and Kinetics of Anaerobic Digestion at 45°C. Journal of Water Resource and Protection,07,1099-1100. doi: 10.4236/jwarp.2015.714090

References