Environmental parameters affecting xylitol production from sugar cane bagasse hemicellulosic hydrolyzate by Candida guilliermondii

The bioconversion of xylose to xylitol by Candida guilliermondii FTI 20037 cultivated in sugar cane bagasse hemicellulosic hydrolyzate was influenced by cell inoculum level, age of inoculum and hydrolyzate concentration. The maximum xylitol productivity (0.75 g L⁻¹ h⁻¹) occurred in tests carried out with hydrolyzate containing 54.5 g L⁻¹ of xylose, using 3.0 g L⁻¹ of a 24-h-old inoculum. Xylitol productivity and cell concentration decreased with hydrolyzate containing 74.2 g L⁻¹ of xylose. Received 02 February 1996/ Accepted in revised form 15 November 1996     

Mineralization of pentachlorophenol in a contaminated soil by Pseudomonas sp UG30 cells encapsulated in κ-carrageenan

A fermentation process in Escherichia coli for production of supercoiled plasmid DNA for use as a DNA vaccine was developed using an automated feed-back control nutrient feeding strategy based on dissolved oxygen (DO) and pH. The process was further automated through a computer-aided data processing system to regulate the cell growth rate by controlling interactively both the nutrient feed rate and agitation speed based on DO. The process increased the total yield of the plasmid DNA by approximately 10-fold as compared to a manual fed-batch culture. The final cell yield from the automated process reached 60 g L⁻¹ of dry cell weight (OD₆₀₀ = 120) within 24 h. A plasmid DNA yield of 100 mg L⁻¹ (1.7 mg g⁻¹ cell weight) was achieved by using an alkaline cell lysis method. Plasmid yield was confirmed using High Performance Liquid Chromatography (HPLC) analysis. Because cells had been grown under carbon-limiting conditions in the automated process, acetic acid production was minimal (below 0.01 g L⁻¹) throughout the fed-batch stage. In contrast, in the manual process, an acid accumulation rate as high as 0.36 g L⁻¹ was observed, presumably due to the high nutrient feed rates used to maintain a maximum growth rate. The manual fed-batch process produced a low cell density averaging 10–12 g L⁻¹ (OD₆₀₀ = 25–30) and plasmid yields of 5–8 mg L⁻¹ (approximately 0.7 mg g⁻¹ cells). The improved plasmid DNA yields in the DO- and pH-based feed-back controlled process were assumed to be a result of a combination of increased cell density, reduced growth rate (μ) from 0.69 h⁻¹ to 0.13 h⁻¹ and the carbon/nitrogen limitation in the fed-batch stage. The DO- and pH-based feed-back control, fed-batch process has proven itself to be advantageous in regulating cell growth rate to achieve both high cell density and plasmid yield without having to use pure oxygen. The process was reproducible in triplicate fermentations at both 7-L and 80-L scales. Received 22 March 1996/ Accepted in revised form 20 September 1996     

Production of xylitol by Candida peltata

Candida peltata NRRL Y-6888 to ferment xylose to xylitol was evaluated under different fermentation conditions such as pH, temperature, aeration, substrate concentration and in the presence of glucose, arabinose, ethanol, methanol and organic acids. Maximum xylitol yield of 0.56 g g⁻¹ xylose was obtained when the yeast was cultivated at pH 6.0, 28°C and 200 rpm on 50 g L⁻¹ xylose. The yeast produced ethanol (0.41 g g⁻¹ in 40 h) from glucose (50 g L⁻¹) and arabitol (0.55 g g⁻¹ in 87 h) from arabinose (50 g L⁻¹). It preferentially utilized glucose > xylose > arabinose from mixed substrates. Glucose (10 g L⁻¹), ethanol (7.5 g L⁻¹) and acetate (5 g L⁻¹) inhibited xylitol production by 61, 84 and 68%, respectively. Arabinose (10 g L⁻¹) had no inhibitory effect on xylitol production. Received 24 December 1998/ Accepted in revised form 18 March 1999     

Pullulan production from deproteinized whey by Aureobasidium pullulans

Aureobasidium pullulans P56 was investigated using an adaptation technique and a mixed culture system. The adaptation of A. pullulans and the mixed cultures of A. pullulans and/or Lactobacillus brevisX20, Debaryomyces hansenii 194 and Aspergillus niger did not increase the production of polysaccharide. Enzymic hydrolysis of lactose in deproteinized whey gave a higher polysaccharide concentration and polysaccharide yield than acidic hydrolysed lactose. Maximum polysaccharide concentration (11.0 ± 0.5 g L⁻¹), biomass dry weight (10.5 ± 0.4 g L⁻¹), polysaccharide yield (47.2 ± 1.8%) and sugar utilization (93.2 ± 2.8%) were achieved using enzyme-hydrolysed whey (pH 6.5) containing 25 g L⁻¹ lactose and supplemented with K₂HPO₄ 0.5%, L-glutamic acid 1%, olive oil 2.5%, and Tween 80 0.5%. In this case the pullulan content of the crude polysaccharide was 40%. Received 16 December 1997/ Accepted in revised form 12 March 1999     

Docosapentaenoic acid (C22:5, ω-3) production by Pythium acanthicum

The physiological roles of omega-3 fatty acids, eicosapentaenoic acid and docosahexaenoic acid have been investigated in detail and microbial strains producing these polyunsaturated fatty acids have been characterised. It has recently been suggested that docosapentaenoic acid may have an important role, especially in infant nutrition, and that its positive health effects have been overlooked. Docosapentaenoic acid (C22:5, ω-3) production by a strain of Pythium acanthicum ATCC 18660 was thus investigated. Optimum conditions for growth of P. acanthicum ATCC 18660 and docosapentaenoic acid production were: pH 6.0, temperature 20°C and incubation time, 10 days. Among different saccharides and complex nitrogen sources tested, glucose and sodium glutamate were preferred carbon and nitrogen sources, respectively. Maximum biomass content (10.4 g L⁻¹) and docosapentaenoic acid yield (49.9 mg L⁻¹) were obtained in 10 days. An increase in docosapentaenoic acid volumetric yields to 108–110 mg L⁻¹ was obtained when linseed oil was used to supplement glucose or soy flour-containing medium. Batch feeding of additional glucose or linseed oil further enhanced the docosapentaenoic acid volumetric yield to 132 mg L⁻¹ and 125 mg L⁻¹, respectively, in 14 days. The specific production of docosapentaenoic acid in preliminary experiments ranged from 1.0–5.0 mg g⁻¹ biomass. As conditions were optimised, docosapentaenoic acid specific production titers were generally in the range of 4.0–5.5 mg g⁻¹ and increases in docosapentaenoic acid volumetric production could be attributed to increased biomass production. The limited improvement obtained by modifying culture conditions indicates that increasing volumetric yields of docosapentaenoic acid by modifying culture conditions appears to represent a significant barrier to commercialisation of such a process and suggests a more fundamental manipulation of metabolism and physiology is required. Received 06 November 1997/ Accepted in revised form 10 January 1998     

Continuous production of l(+)-lactic acid by Lactobacillus casei in two-stage systems

A two-stage two-stream chemostat system and a two-stage two-stream immobilized upflow packed-bed reactor system were used for the study of lactic acid production by Lactobacillus casei subsp casei. A mixing ratio of D ₁₂/D ₂= 0.5 (D = dilution rate) resulted in optimum production, making it possible to generate continuously a broth with high lactic acid concentration (48 g l⁻¹) and with a lowered overall content of initial yeast extract (5  g l⁻¹), half the concentration supplied in the one-step process. In the two-stage chemostat system, with the first stage at pH 5.5 and 37 °C and a second stage at pH 6.0, a temperature change from 40 °C to 45 °C in the second stage resulted in a 100% substrate consumption at an overall dilution rate of 0.05 h⁻¹. To increase the cell mass in the system, an adhesive strain of L. casei was used to inoculate two packed-bed reactors, which operated with two mixed feedstock streams at the optimal conditions found above. Lactic acid fermentation started after a lag period of cell growth over foam glass particles. No significant amount of free cells, compared with those adhering to the glass foam, was observed during continuous lactic acid production. The extreme values, 57.5 g l⁻¹ for lactic acid concentration and 9.72 g l⁻¹ h⁻¹ for the volumetric productivity, in upflow packed-bed reactors were higher than those obtained for free cells (48 g l⁻¹  and 2.42 g l⁻¹ h⁻¹) respectively and the highest overall l(+)-lactic acid purity (96.8%) was obtained in the two-chemostat system as compared with the immobilized-cell reactors (93%). Received: 4 December 1997 / Received revision: 23 February 1998 / Accepted: 14 March 1998     

Production of Cold-Adapted Amylase by Marine Bacterium <Emphasis Type="Italic">Wangia</Emphasis> sp. C52: Optimization,Modeling, and Partial Characterization

The aim of this work was to optimize the fermentation parameters in the shake-flask culture of marine bacterium Wangia sp. C52 to increase cold-adapted amylase production using two statistical experimental methods including Plackett–Burman design, which was applied to find the key ingredients for the best medium composition, and response surface methodology, which was used to determine the optimal concentrations of these components. The results showed starch, tryptone, and initial pH had significant effects on the cold-adapted amylase production. A central composite design was then employed to further optimize these three factors. The experimental results indicated that the optimized composition of medium was 6.38 g L⁻¹ starch, 33.84 g L⁻¹ tryptone, 3.00 g L⁻¹ yeast extract, 30 g L⁻¹ NaCl, 0.60 g L⁻¹ MgSO₄ and 0.56 g L⁻¹ CaCl₂. The optimized cultivation conditions for amylase production were pH 7.18, a temperature of 20°C, and a shaking speed of 180 rpm. Under the proposed optimized conditions, the amylase experimental yield (676.63 U mL⁻¹) closely matched the yield (685.60 U mL⁻¹) predicted by the statistical model. The optimization of the medium contributed to tenfold higher amylase production than that of the control in shake-flask experiments.     

Increased astaxanthin production by a Phaffia rhodozyma mutant grown on date juice from Yucca fillifera

The wild strain and the astaxanthin-overproducing mutant strain 25–2 of Phaffia rhodozyma were analyzed in order to assess their ability to grow and synthesize astaxanthin in a minimal medium composed of g L⁻¹: KH₂PO₄ 2.0; MgSO₄ 0.5; CaCl₂ 0.1; urea 1.0 and supplemented with date juice of Yucca fillifera as a carbon source (yuca medium). The highest astaxanthin production (6170 μg L⁻¹) was obtained at 22.5 g L⁻¹ of reducing sugars. The addition of yeast extract to the yuca medium at concentrations of 0.5–3.0 g L⁻¹ inhibited astaxanthin synthesis. The yuca medium supported a higher production of astaxanthin, 2.5-fold more than that observed in the YM medium. Journal of Industrial Microbiology & Biotechnology (2000) 24, 187–190. Received 14 July 1999/ Accepted in revised form 02 December 1999     

High alcohol production by repeated batch fermentation using an immobilized osmotolerant Saccharomyces cerevisiae

A repeated batch fermentation system was used to produce ethanol using an osmotolerant Saccharomyces cerevisiae (VS₃) immobilized in calcium alginate beads. For comparison free cells were also used to produce ethanol by repeated batch fermentation. Fermentation was carried for six cycles with 125, 250 or 500 beads using 150, 200 or 250 g glucose L⁻¹ at 30°C. The maximum amount of ethanol produced by immobilized VS₃ using 150 g L⁻¹ glucose was only 44 g L⁻¹ after 48 h, while the amount of ethanol produced by free cells in the first cycle was 72 g L⁻¹. However in subsequent fed batch cultures more ethanol was produced by immobilized cells compared to free cells. The amount of ethanol produced by free cells decreased from 72 g L⁻¹ to 25 g L⁻¹ after the fourth cycle, while that of immobilized cells increased from 44 to 72 g L⁻¹. The maximum amount of ethanol produced by immobilized VS₃ cells using 150, 200 and 250 g glucose L⁻¹ was 72.5, 93 and 87 g ethanol L⁻¹ at 30°C. Journal of Industrial Microbiology & Biotechnology (2000) 24, 222–226. Received 16 September 1999/ Accepted in revised form 22 December 1999     

Phenol inhibition kinetics for growth of Acetobacter aceti on ethanol

Acetobacter aceti have been grown on ethanol under inhibitory conditions created by high concentrations of phenol. A defined medium with no vitamin or amino acid supplements has been used such that ethanol was the sole carbon substrate. The culture temperature was maintained at 30 °C while the pH was manually controlled to fall within the range 4.5–6.0 during ethanol consumption. Growth on ethanol at a few thousand milligrams per litre (below the known inhibitory level) resulted in a maximum specific growth rate of 0.16 h⁻¹ with a 95% yield of acetic acid, followed immediately by acetic acid consumption at a growth rate of 0.037 h⁻¹. Phenol was found to inhibit growth by decreasing both the specific growth rate and the biomass yield during ethanol consumption. On the other hand, the yield of acetic acid during ethanol consumption and the yield of biomass during acetic acid consumption remained constant, independent of phenol inhibition. A model is presented and is shown to represent the phenol-inhibited growth behaviour of A. aceti during both ethanol and acetic acid consumption. Received: 6 November 1998 / Received revision: 8 February 1999 / Accepted: 12 February 1999     

Production of curdlan using sucrose or sugar cane molasses by two-step fed-batch cultivation of Agrobacterium species

Maltose and sucrose were efficient carbon sources for the production of curdlan by a strain of Agrobacterium sp. A two-step, fed-batch operation was designed in which biomass was first produced, followed by curdlan production which was stimulated by nitrogen limitation. There exists an optimal timing for nitrogen limitation for curdlan production in the two-step, fed-batch operation. Maximum curdlan production (60 g L⁻¹) was obtained from sucrose with a productivity of 0.2 g L⁻¹ h⁻¹ when nitrogen was limited at a cell concentration of 16.0 g L⁻¹. It was also noted that the curdlan yield from sucrose was as high as 0.45 g curdlan g⁻¹ sucrose, and the highest specific production rate was 1.0 g curdlan g⁻¹ cells h⁻¹ right after nitrogen limitation. Of particular importance was the use of molasses as a cheap carbon source to produce curdlan in the two-step, fed-batch cultivation. As high as 42 g L⁻¹ of curdlan with a yield of 0.35 g curdlan g⁻¹ total sugar was obtained after 120 h of fed-batch cultivation. Received 20 August 1996/ Accepted in revised form 26 November 1996     

Ethanol fermentation of mixed-sugars using a two-phase, fed-batch process: method to minimize D-glucose repression of Candida shehatae D-xylose fermentations

Candida shehatae cells pre-grown on D-xylose simultaneously consumed mixtures of D-xylose and D-glucose, under both non-growing (anoxic) and actively growing conditions (aerobic), to produce ethanol. The rate of D-glucose consumption was independent of the D-xylose concentration for cells induced on D-xylose. However, the D-xylose consumption rate was approximately three times lower than the D-glucose consumption rate at a 50% D-glucose: 50% D-xylose mixture. Repression was not observed (substrate utilization rates were approximately equal) when the percentage of D-glucose and D-xylose was changed to 22% and 78%, respectively. In fermentations with actively growing cells (50% glucose and D-xylose), ethanol yields from D-xylose increased, the % D-xylose utilized increased, and the xylitol yield was significantly reduced in the presence of D-glucose, compared to anoxic fermentations (Y_ETOH,xylose = 0.2–0.40 g g⁻¹, 75–100%, and Y_xylitol = 0–0.2 g g⁻¹ compared to Y_ETOH,xylose = 0.15 g g⁻¹, 56%, Y_xylitol = 0.51 g g⁻¹, respectively). To increase ethanol levels and reduce process time, fed-batch fermentations were performed in a single stage reactor employing two phases: (1) rapid aerobic growth on D-xylose (μ = 0.32 h⁻¹) to high cell densities; (2) D-glucose addition and anaerobic conditions to produce ethanol (Y_ETOH,xylose = 0.23 g g⁻¹). The process generated high cell densities, 2 × 10⁹ cells ml⁻¹, and produced 45–50 g L⁻¹ ethanol within 50 h from a mixture of D-glucose and D-xylose (compared to 30 g L⁻¹ in 80 h in the best batch process). The two-phase process minimized loss of cell viability, increased D-xylose utilization, reduced process time, and increased final ethanol levels compared to the batch process. Received 23 February 1998/ Accepted in revised form 15 July 1998     

Influence of linearly decreasing feeding rates on fed-batch ethanol fermentation of sugar-cane blackstrap molasses

Summary The ethanol yield was not affected and the ethanol productivity increased (10%) when linearly decreasing feeding rates were used instead of constant feeding rates in fed-batch ethanol fermentations.Nomenclature F reactor feeding rate (L.h^–1) - M_E mass of ethanol in the fermentor (g) - M_s mass of TRS in the fermentor (g) - M_x mass of yeast cells (dry matter) in the fermentor (g) - P ethanol productivity (g.L^–1.h^–1) - s standard deviation - S_o TRS concentration in the feeding mash (g.L^–1) - t time (h) - T fermentor filling-up time (h) - TRS total reducing sugars calculated as glucose (g.L^–1) - X_o yeast cells concentration (dry matter) in the inoculum (g.L^–1) - average ethanol yield (% of the theoretical value)     

Production of hexanoic acid from d-galactitol by a newly isolated Clostridium sp. BS-1

In a study screening anaerobic microbes utilizing d-galactitol as a fermentable carbon source, four bacterial strains were isolated from an enrichment culture producing H₂, ethanol, butanol, acetic acid, butyric acid, and hexanoic acid. Among these isolates, strain BS-1 produced hexanoic acid as a major metabolic product of anaerobic fermentation with d-galactitol. Strain BS-1 belonged to the genus Clostridium based on phylogenetic analysis using 16S rRNA gene sequences, and the most closely related strain was Clostridium sporosphaeroides DSM 1294^T, with 94.4% 16S rRNA gene similarity. In batch cultures, Clostridium sp. BS-1 produced 550 ± 31 mL L⁻¹ of H₂, 0.36 ± 0.01 g L⁻¹ of acetic acid, 0.44 ± 0.01 g L⁻¹ of butyric acid, and 0.98 ± 0.03 g L⁻¹ of hexanoic acid in a 4-day cultivation. The production of hexanoic acid increased to 1.22 and 1.73 g L⁻¹ with the addition of 1.5 g L⁻¹ of sodium acetate and 100 mM 2-(N-morpholino)ethanesulfonic acid (MES), respectively. Especially when 1.5 g L⁻¹ of sodium acetate and 100 mM MES were added simultaneously, the production of hexanoic acid increased up to 2.99 g L⁻¹. Without adding sodium acetate, 2.75 g L⁻¹ of hexanoic acid production from d-galactitol was achieved using a coculture of Clostridium sp. BS-1 and one of the isolates, Clostridium sp. BS-7, in the presence of 100 mM MES. In addition, volatile fatty acid (VFA) production by Clostridium sp. BS-1 from d-galactitol and d-glucose was enhanced when a more reduced culture redox potential (CRP) was applied via addition of Na₂S·9H₂O.     

Influence of initial cellulose concentration on the carbon flow distribution during batch fermentation by Clostridium thermocellum ATCC 27405

The objective of this research was to understand how carbon loading influences hydrogen (H₂) synthesis and metabolic flow patterns in the thermophilic, cellulolytic bacterium, Clostridium thermocellum. C. thermocellum was cultivated in batch cultures with high (5 g L⁻¹) and low (1 g L⁻¹) initial concentrations of α-cellulose at 60°C. The growth rate of C. thermocellum was 22% lower (0.15 h⁻¹) in cultures with low-cellulose concentration compared with cultures with high-cellulose concentrations. Although substrate depletion coincided with the end of log-growth in low-cellulose cultures, the prime reason for growth arrest in high-cellulose cultures was not identified. Ethanol, acetate, and formate were the major soluble end-products with concomitant release of H₂ and CO₂ under both conditions. Lactate appeared during the late log phase in high-carbon cultures when pH dropped below 6.4 and became the major end-product in stationary phase. During the exponential phase of cell growth, significantly higher yields for H₂ and acetate (1.90 ± 0.14 and 1.11 ± 0.04 mol/mol glucose equivalent, respectively) were obtained from low-cellulose cultures compared to those from high-cellulose cultures. The maximum specific rate of H₂ production, 6.41 ± 0.13 mmol H₂/g dry cell/h, obtained during the exponential phase from low-carbon cultures was about 37% higher than that obtained from high-carbon cultures.     

Analysis and optimization of a two-substrate fermentation for xylitol production using Candida tropicalis

Xylitol, a functional sweetener, was produced from xylose using Candida tropicalisATCC 13803. A two-substrate fermentation was designed in order to increase xylitol yield and volumetric productivity. Glucose was used initially for cell growth followed by conversion of xylose to xylitol without cell growth and by-product formation after complete depletion of glucose. High glucose concentrations increased volumetric productivity by reducing conversion time due to high cell mass, but also led to production of ethanol, which, in turn, inhibited cell growth and xylitol production. Computer simulation was undertaken to optimize an initial glucose concentration using kinetic equations describing rates of cell growth and xylose bioconversion as a function of ethanol concentration. Kinetic constants involved in the equations were estimated from the experimental results. Glucose at 32 g L⁻¹ was estimated to be an optimum initial glucose concentration with a final xylose concentration of 86 g L⁻¹ and a volumetric productivity of 5.15 g-xylitol L⁻¹ h⁻¹. The two-substrate fermentation was performed under optimum conditions to verify the computer simulation results. The experimental results were in good agreement with the predicted values of simulation with a xylitol yield of 0.81 g-xylitol g-xylose⁻¹ and a volumetric productivity of 5.06 g-xylitol L⁻¹ h⁻¹. Received 16 June 1998/ Accepted in revised form 28 February 1999     

Simultaneous utilization of glucose and D-xylose by Candida shehatae in a chemostat

The kinetics of biomass formation, D-xylose utilization, and mixed substrate utilization were determined in a chemostat using the yeast Candida shehatae. The maximum growth rate of C. shehatae grown aerobically on D-xylose was 0.42 h⁻¹ and the Monod constant, K _s, was 0.06 g L⁻¹. The biomass yield, Y _{X/S}, ranged from 0.40 to 0.50 g g⁻¹ over a dilution rate range of 0.2–0.3 h⁻¹, when C. shehatae was grown on pure D-xylose. Mixtures of D-xylose and glucose (∼1 : 1) were simultaneously utilized over a dilution rate from 0.15 to 0.35 h⁻¹ at pH 3.5 and 4.5, but pH 3.5 reduced μ_max and reduced the dilution rate range over which D-xylose was utilized in the presence of glucose. At pH 4.5, μ_max was not reduced with the mixed sugar feed and the overall or lumped K _s value was not significantly increased (0.058 g L⁻¹ vs 0.06 g L⁻¹), when compared to a pure D-xylose feed. Kinetic data indicate that C. shehatae is an excellent candidate for chemostat production of value added products from renewable carbon sources, since simultaneous mixed substrate utilization was observed over a wide range of growth rates on a 1 : 1 mixture of glucose and D-xylose. Received 21 August 1997/ Accepted in revised form 28 May 1998     

The production of xylitol from d-xylose by fermentation with Hansenula polymorpha

We have analysed the influence of the initial pH of the medium and the quantity of aeration provided during the batch fermentation of solutions of d-xylose by the yeast Hansenula polymorpha (34438 ATCC). The initial pH was altered between 3.5 and 6.5 whilst aeration varied between 0.0 and 0.3 vvm. The temperature was kept at 30 °C during all the experiments. Hansenula polymorpha is known to produce high quantities of xylitol and low quantities of ethanol. The most favourable conditions for the growth of xylitol turned out to be: an initial pH of between 4.5 and 5.5 and the aeration provided by the stirring vortex alone. Thus, at an initial pH of 5.5, the maximum specific production rate (μ_m) was 0.41 h⁻¹, the overall biomass yield (Y _x/s ^G) was 0.12 g g⁻¹, the specific d-xylose-consumption rate (q _s ) was 0.075 g g⁻¹ h⁻¹ (for t = 75 h), the specific xylitol-production rate (q _Xy ) was 0.31 g g⁻¹ h⁻¹ (for t = 30 h) and the overall yields of ethanol (Y _E/s ^G) and xylitol (Y _Xy/s ^G) were 0.017 and 0.61 g g⁻¹ respectively. Both q _s and q _Xy decreased during the course of the experiments once the exponential growth phase had finished. Received: 26 March 1998 / Received revision: 30 June 1998 / Accepted: 2 July 1998     

Kinetic analysis on the two-step processes of AOB and NOB in aerobic nitrifying granules

Complete granulation of nitrifying sludge was achieved in a sequencing batch reactor. For the granular sludge, batch experiments were conducted to characterize the kinetic features of ammonia oxidizers (AOB) and nitrite oxidizers (NOB) in the granules using the respirometric method. A two-step nitrification model was established to determine the kinetic parameters of both AOB and NOB. In addition to nitrification reactions, the new model also took into account biomass maintenance and mass transfer through the granules. The yield coefficient, maximum specific growth rate, and affinity constant for ammonium for AOB were 0.21 g chemical oxygen demand (COD) g⁻¹ N, 0.09 h⁻¹, and 9.1 mg N L⁻¹, respectively, whereas the corresponding values for NOB were 0.05 g COD g⁻¹ N, 0.11 h⁻¹, and 4.85 mg N L⁻¹, respectively. The model developed in this study performed well in simulating the oxygen uptake rate and nitrogen conversion kinetics and in predicting the oxygen consumption of the AOB and NOB in aerobic granules.     

Simultaneous nutrients and carbon removal during pretreated swine slurry degradation in a tubular biofilm photobioreactor

The biodegradation potential of an innovative enclosed tubular biofilm photobioreactor inoculated with a Chlorella sorokiniana strain and an acclimated activated sludge consortium was evaluated under continuous illumination and increasing pretreated (centrifuged) swine slurry loading rates. This photobioreactor configuration provided simultaneous and efficient carbon, nitrogen, and phosphorous treatment in a single-stage process at sustained nitrogen and phosphorous removals efficiencies ranging from 94% to 100% and 70–90%, respectively. Maximum total organic carbon (TOC), NH₄ ⁺, and PO₄ ³⁻ removal rates of 80 ± 5 g C m_r ⁻³ day⁻¹, 89 ± 5 g N m_r ⁻³ day⁻¹, and 13 ± 3 g P m_r ⁻³ day⁻¹, respectively, were recorded at the highest swine slurry loadings (TOC of 1,247 ± 62 mg L⁻¹, N–NH₄ ⁺ of 656 ± 37 mg L⁻¹, P–PO₄ ³⁺ of 117 ± 19 mg L⁻¹, and 7 days of hydraulic retention time). The unusual substrates diffusional pathways established within the phototrophic biofilm (photosynthetic O₂ and TOC/NH₄ ⁺ diffusing from opposite sides of the biofilm) allowed both the occurrence of a simultaneous denitrification/nitrification process at the highest swine slurry loading rate and the protection of microalgae from any potential inhibitory effect mediated by the combination of high pH and high NH₃ concentrations. In addition, this biofilm-based photobioreactor supported efficient biomass retention (>92% of the biomass generated during the pretreated swine slurry biodegradation).