Direct alcoholic fermentation of starchy biomass using amylolytic yeast strains in batch and immobilized cell systems

Summary Direct alcoholic fermentation of dextrin or soluble starch with selected amylolytic yeasts was studied in both batch and immobilized cell systems. In batch fermentations, Saccharomyces diastaticus was capable of fermenting high dextrin concentrations much more efficiently than Schwanniomyces castellii. From 200 g·l^–1 of dextrin S. diastaticus produced 77 g·l^–1 of ethanol (75% conversion efficiency). The conversion efficiency decreased to 59% but a higher final ethanol concentration of 120 g·l^–1 was obtained with a medium containing 400 g·l^–1 of dextrin. With a mixed culture of S. diastaticus and Schw. castellii 136 g·l^–1 of ethanol was produced from 400 g·l^–1 of dextrin (67% conversion efficiency). S. diastaticus cells attached well to polyurethane foam cubes and a S. diastaticus immobilized cell reactor produced 69 g·l^–1 of ethanol from 200 g·l^–1 of dextrin, corresponding to an ethanol productivity of 7.6g·l^–1·h^–1. The effluent from a two-stage immobilized cell reactor with S. diastaticus and Endomycopsis fibuligera contained 70 g·l^–1 and 80 g·l^–1 of ethanol using initial dextrin concentrations of 200 and 250 g·l^–1 respectively. The corresponding values for ethanol productivity were 12.7 and 9.6 g·l^–1·h^–1. The productivity of the immobilized cell systems was higher than for the batch systems, but much lower than for glucose fermentation.     

Stimulation of conversion rates and bacterial activity in a silage-fed two-phase biogas process by initiating liquid recirculation

The effects of liquid recirculation on a liquefaction-acidogenic reactor in an anaerobic two-phase digesting system operating with grass-clover silage was studied during 40 days after initiating recirculation of effluent from the methanogenic reactor to the liquefaction-acidogenic reactor. An increase in alkalinity and, thus, an increase in pH from 5.2 to 6.0 occurred in the liquefaction-acidogenic reactor. During the same period, a 10-fold increase (from 0.2 to 1.9 g·l^–1·h^–1) in the degradation rate of mannitol and an almost 9-fold increase in the activity of hydrogenotrophic methanogens was observed. The estimated number of these bacteria increased by one order of magnitude. The average degradation rate of lactate increased 3-fold, probably as a consequence of the more efficient hydrogen consumption by the hydrogenotrophic methanogens. An observed increase in net mineralization of organic nitrogen compounds was probably the main reason for an enhanced net production of organic acids (from 0.2 to 0.9 g·l^–1·d^–1). The liquefaction of cellulose and hemicellulose was low from the start of recirculation (3% and 20% reduction, respectively) and did not seem to be affected by the liquid recirculation. This was in accordance with the low number of cellulose degraders (4.0·10² counts·ml^–1) observed. The results from this investigation show that the initiation of liquid recirculation in silage-fed two-phase biogas processes will stimulate the activity of hydrogenotrophic methanogens in the liquefaction-acidogenic reactor. This will lead to more thermodynamically favourable conditions for acidification reactions which are dependent upon interspecies transfer of reducing equivalents.Abbreviations COD chemical oxygen demand - CSTR completely stirred tank reactor - HRT hydraulic retention time - LA-reactor liquefaction-acidogenic reactor - M-reactor methanogenic reactor - MPN most probable number - OLR organic loading rate - SMA specific methanogenic activity - SRT solids retention time - TKN total Kjeldahl nitrogen - ts total solids - tss total suspended solids - vs volatile solids - vss volatile suspended solids     

d(−)lactic acid production by suspended and aggregated continuous cultures of Bacillus laevolacticus

Summary A new method of d(–)lactic acid production based on the aggregated form of growth of Bacillus laevolacticus in continuous culture in an anaerobic gaslift reactor is presented. With glucose as the substrate a bacterial dry weight of 25 g·1^–1 and a lactic acid production rate of 13 g·1^–1·h^–1 was attained. In conventional glucose-limited chemostat cultures elevated levels of lactic acid stimulated specific lactic acid production while the formation rates of other end-products remained unaffected. In glucose-limited aggregated cultures lactic acid positively influenced the aggregation of cells, improving the volumetric production rate. It is concluded that lactic acid itself is a positive effector in the optimisation of lactic acid production with aggregated cultures of B. laevolacticus.Offprint requests to: J. P. de Boer     

Continuous ethanol production by Zymomonas mobilis in a fluidized bed reactor. Part I. Kinetic studies of immobilization in macroporous glass beads

A model has been developed to calculate the ethanol production in a well-mixed fluidized bed reactor. This model takes into account diffusion and the reaction inside porous glass beads and the activity of suspended cells in the fluidized bed reactor. The associated model parameters have been determined from the literature and by kinetic studies with Zymomonas mobilis in a continuous stirred tank reactor. The model permits good predictions of steady-state data in a fluidized bed reactor at residence times longer than 1–1.5 h. The immobilization of Z. mobilis in a fluidized bed reactor results in high ethanol space-time yields of more than 50 g·^–1·h^–1 at a glucose conversion of 80% (glucose in substrate: 120 gl^–1). At 99% conversion a space-time yield of 30 g·^–1·^–1 can be achieved when two fluidized bed reactors operate as cascade.     

Nutritional and hormonal requirements of Ginkgo biloba embryo-derived callus and suspension cell culture

Calli were obtained from Ginkgo biloba embryos grown on Murashige and Skoog (MS) medium. The G. biloba cells could grow on either MS or Gamborg B5 mineral salt medium supplemented with sucrose (3% and 2%, respectively) and naphthaleneacetic acid (NAA) and kinetin (K) in concentrations ranging from 0.1 to 2.0 mg·L^–1. Best growth and maintenance of callus cultures were achieved using MS medium supplemented with 2 mg·L^–1 NAA and 1 mg·L^–1 K (N₂K₁MS). Light was required to maintain healthy growth of the callus tissue.In both MS and B5 based media, sucrose was hydrolyzed extracellularly before being taken up by Ginkgo cell suspension cultures. Specific growth rates of 0.13 d^–1 and 0.08 d^–1 were obtained in MS medium supplemented with 1 mg·L^–1 NAA, 0.1 mg·L^–1 K and 30 g·L^–1 sucrose (N₁K_0.1MS) and B5 medium supplemented with the same growth regulator regime and 20 g·L^–1 sucrose (N₁K_0.1B5) respectively. Complete phosphate and ammonium uptake was observed in 11 days when cultured in MS medium and 10 days and 4 days respectively when cultured in B5 medium. During the culture, G. biloba cells consumed only 64% and 29% of the nitrate content of N₁K_0.1MS and N₁K_0.1B5 media respectively. Maximum dry biomass concentrations were 13.4 g·L^–1 and 7.9 g·L^–1, and yields on carbohydrate were 0.39 and 0.45 in N₁K_0.1MS and N₁K_0.1B5 media respectively. The better performance of MS cultures came from the higher sucrose and nitrogen salts concentrations of this medium.Abbreviations B5 Gamborg mineral salt medium - d.w. Dry weight - K Kinetin - MS Murashige and Skoog mineral salt medium - N or NAA Naphthaleneacetic acid - N_iK_jMS i and j are the respective concentrations (mg·L^–1) of NAA and K - n Number of experimental points - r Linear regression correlation coefficient     

Bacterial productivity and microbial biomass in tropical mangrove sediments

Bacterial productivity (³H-thymidine incorporation into DNA) and intertidal microbenthic communities were examined within five mangrove estuaries along the tropical northeastern coast of Australia. Bacteria in mangrove surface sediments (0–2 cm depth) were enumerated by epifluorescence microscopy and were more abundant (mean and range: 1.1(0.02–3.6)×10¹¹ cells·g DW^–1) and productive (mean: 1.6 gC·m^–2· d^–1) compared to bacterial populations in most other benthic environments. Specific growth rates (¯x=1.1) ranged from 0.2–5.5 d^–1, with highest rates of growth in austral spring and summer. Highest bacterial numbers occurred in winter (June–August) in estuaries along the Cape York peninsula north of Hinchinbrook Island and were significantly different among intertidal zones and estuaries. Protozoa (10⁵–10⁶·m^–2, pheopigments (0.0–24.1g·gDW^–1) and bacterial productivity (0.2–5.1 gC·m^–2·d^–1) exhibited significant seasonality with maximum densities and production in austral spring and summer. Algal biomass (chlorophylla) was low (mean: 1.6g·gDW^–1) compared to other intertidal sediments because of low light intensity under the dense forest canopy, especially in the mid-intertidal zone. Partial correlation analysis and a study of possible tidal effects suggest that microbial biomass and bacterial growth in tropical intertidal sediments are regulated primarily by physicochemical factors and by tidal flushing and exposure. High microbial biomass and very high rates of bacterial productivity coupled with low densities of meiofaunal and macroinfaunal consumers observed in earlier studies suggest that microbes may be a sink for carbon in intertidal sediments of tropical mangrove estuaries.     

Continuous ethanol production by Zymomonas mobilis in a fluidized bed reactor. Part II: Process development for the fermentation of hydrolysed B-starch without sterilization

A continuous fluidized bed reactor operation system has been developed for ethanol production by Zymomonas mobilis using hydrolysed B-starch without sterilization. The operation system consists of two phases. In the first phase macroporous glass carriers in a totally mixed fluidized bed reactor were filled up totally with a monoculture of Z. mobilis by fast computer-controlled colonization, so that in the subsequent production phase no contaminants, especially lactic-acid bacteria, could penetrate into the carrier beads. In the production phase the high concentration of immobilized Z. mobilis cells in the fluidized bed reactor permits unsterile fermentation of hydrolysed B-starch to ethanol at short residence times. This results in wash-out conditions for contaminants from the substrate. Long-term experimental studies (more than 120 days) of unsterile fermentation of hydrolysed B-starch in the laboratory fluidized bed reactor (2.2 l) demonstrated stable operation up to residence times of 5 h. A semi-technical fluidized bed reactor plant (cascade of two fluidized bed reactors, each 55 l) was operated stably at a mean residence time of 4.25 h. Glucose conversion of 99% of the unsterile hydrolysed B-starch was achieved at 120 g glucose/l^–1 in the substrate, resulting in an ethanol concentration of 50 g·l^–1 and an ethanol space-time yield of 13 g·l^–1·h^–1. This is a factor of three compared to ethanol fermentation of hydrolysed B-starch with Z. mobilis in a continuous stirred tank reactor, which can only be operated stably under sterile conditions. Correspondence to: D. Weuster-Botz     

Fermentative production of 1,3-propanediol from glycerol by Clostridium butyricum up to a scale of 2m3

Summary The conversion of glycerol to 1,3-propanediol (PD) by Clostridium butyricum DSM 5431 was studied in anaerobic culture. Growth and product formation were optimal at pH = 7.0 and T = 35° C, while aeration rate and stirrer speed were found to have no significant influence. As increasing amounts of initial glycerol led to inhibition of growth, cultivations were done in fed-batch operation. Comparative cultivations were carried out in an air-lift (ALR) and a stirred-tank reactor (STR) having equal working volumes (V _L = 30 l) and no difference in product formation was found. The process was scaled up to reactor sizes of 1.2 m³ (ALR) and 2.0 m³ (STR). The same results were obtained irrespective of reactor volume as well as reactor type (STR/ALR). PD concentrations of approximately 50–58 g·l^–1 and overall productivities of 2.3–2.9 g·l^–1 ·h^–1 could be reached. Offprint requests to: W.-D. Deckwer     

Oxygen availability for bacterial growth with a flow microcalorimeter

Summary The enthalpy change associated with aerobic growth of E. coli K₁₂ on minimal media with succinic acid as sole carbon and energy source, determined by flow microcalorimetry (with aerobic mixing cell) was 733.01±15.32 kJ·mol^–1. Molar growth yield was 39.6±1.2 g·mol^–1. When the microcalorimetric growth was limited by oxygen supply, the power-time curve was altered and the total heat evolved was less than the enthalpy change. The maximum thermal output corresponding to a fully aerobic growth in the calorimetric cell was 1.89×10^–3 W·ml^–1. Thus, the oxygen uptake rate was about 0.39 ml O₂·h^–1·ml^–1.     

Production of ψ-linolenic acid by the fungus Mucor rouxii on cheap nitrogen and carbon sources

Summary The production of -linolenic acid (GLA) by the fungus Mucor rouxii CBS 416.77 was studied on low budget nitrogen and carbon sources, i.e. rape meal, cocos expeller and two types of yeast extract (nitrogen sources), and starch, starch hydrolysate, beet molasses and cocos expeller (carbon sources). As references, Difco yeast extract and glucose were used. In flask cultivations the three yeast extracts were fully interchangeable, while the Difco yeast extract (the most expensive of those tested) gave a higher productivity of GLA in fermentor cultures (14 mg·l^–1·h^–1). The yield of lipids and GLA were increased in the order yeast extract < rape meal < cocos expeller. Thus the amount of lipid increased from 0.56 to 2.8 g·l^–1, and that of GLA from 0.15 to 0.33 g·l^–1. Use of beet molasses or cocos expeller as carbon sources gave poor growth. Starch and starch hydrolysate resulted in better productivity of GLA than glucose (4.7 and 4.9 compared to 3.4 mg·l^–1·h^–1). Offsprint requests to: A.-M. Lindberg     

The production of 2,3-butanediol by fermentation of high test molasses

Summary Klebsiella oxytoca fermented 199 g·l^–1 high test or invert molasses using batch fermentation with substrate shift to produce 95.2–98.6 g 2,3-butanediol·l^–1 and 2,4–4.3 g acetoin·l^–1 with a diol yield of 96–100% of the theoretical value and a diol productivity of 1.0–1.1 g·l^–1·h^–1. Fermentation was performed numerous times with molasses in repeated batch culture with cell recovery. Such repeated batch fermentation, in addition to a high product yield, also showed a very high product concentration. For example, 118 g 2,3-butanediol·l^–1 and 2.3 g acetoin·l^–1 were produced from 280 g·l^–1 of high test molasses. The diol productivity in this fermentation amounted to 2.4 g·l^–1·h^–1 and can undoubtedly be further increased by increasing the cell concentration. Because the Klebsiella cultures ferment 2,3-butanediol at an extremely high rate once the sugar has been consumed, the culture was inhibited completely by the addition of 15 g ethanol·l^–1 and switching off aeration. Offprint requests to: A. S. Afschar     

Evaluation of solvents for extractive butanol fermentation with Clostridium acetobutylicum and the use of poly(propylene glycol) 1200

Summary In an effort to improve the viability of acetone-butanol-ethanol fermentation by extractive fermentation, 63 organic solvents, including alkanes, alcohols, aldehydes, acids, and esters, were experimentally evaluated for biocompatibility with Clostridium acetobutylicum by observing gas evolution from cultures in contact with candidate solvents. Thirty-one of these solvents were further tested to determine their partition coefficient for butanol in fermentation medium. The biocompatible solvent with the highest partition coefficient for butanol (4.8), was poly(propylene glycol) 1200, which was selected for fermentation experiments. This is the highest partition coefficient reported to date for a biocompatible solvent. Extractive fermentations using concentrated feeds were observed to produce up to 58.6 g·l^–1 acetone and butanol in 202 h, the equivalent of three control fermentations in a single run. Product yields (based on total solvent products and glucose consumed) of 0.234 g·g^–1 to 0.311 g·g^–1 and within run solvent productivities of 0.174 g·l^–1·h^–1 to 0.290 g·l^–1·h^–1 were consistentwith conventional fermentations reported in the literature. The extended run-time of the fermentation resulted in an overall improvement in productivity by reducing the fraction of between-run down-time for fermentor cleaning and sterilization.     

Alcoholic fermentation of glucose and xylose by Pichia stipitis,Candida shehatae,Saccharomyces cerevisiae and Zymomonas mobilis: oxygen requirement as a key factor

Summary To investigate simultaneous alcoholic fermentation of glucose and xylose derived from lignocellulosic material by separate or co-culture processes, the effect of oxygen transfer rate (OTR) on the fermentation of 50 g/l xylose by Pichia stipitis NRRL Y 7124 and Candida shehatae ATCC 22984, and the fermentation of 50 g/l glucose by Saccharomyces cerevisiae CBS 1200 and Zymomonas mobilis ATCC 10988 was carried out in batch cultures. The kinetic parameters of the xylose-fermenting yeasts were greatly dependent on the OTR. The optimum OTR values were found to be 3.9 and 1.75 mmol·1^–1·h^–1 for C. shehatae and P. stipitis, respectively. By contrast the fermentative parameters of S. cerevisiae were poorly affected by the OTR range tested (0.0–3.5 mmol·l^–1·h^–1) Under these conditions the ethanol yields ranged from 0.41 g·g^–1 to 0.45 g·g^–1 and the specific ethanol productivity was around 0.70 g·g^–1·h^–1. Z. mobilis gave the highest fermentative performance under strictly anaerobic conditions (medium continually flushed with nitrogen): under these conditions, the ethanol yield was 0.43 g·g^–1 and the average specific ethanol productivity was 2.3 g·g^–1·h^–1. Process considerations in relation to the effect of OTR on the fermentative performance of the tested strains are discussed. Offprint requests to: J. P. Delgenes     

Continuous degradation of phenol(s) by Pseudomonas putida P8 entrapped in polyacrylamidehydrazide

Summary The continuous degradation of phenol by immobilized cells of Pseudomonas putida P8 under different conditions was investigated. The bacterial cells were entrapped in polyacrylamidehydrazide (PAAH) and cultivated in a columnar fluidized-bed bioreactor. Working with a dilution rate of 0.067 h^-1 the phenol content in the feed was varied to find the capacity of an one-stage system with complete phenol degradation.Under sterile conditions and with phenol as the sole carbon source a degradation rate of 7.2 g·l^-1·d^-1 was reached whereas in non-sterile waste water only 3.12 g·l^-1·d^-1 were degraded. In any case the immobilized cells showed a stable phenol degradation activity and even simultaneously fed cresols or 4-chlorophenol were utilized completely.     

Digestion and energy metabolism in a small arboreal marsupial,the Greater Glider (Petauroides volans), fed high-terpeneEucalyptus foliage

Summary The digestion and metabolism ofEucalyptus radiata foliage was studied in a small (1–1.5 kg) arboreal marsupial, the greater glider (Petauroides volans). Mean dry matter intake was 44 g·kg^–0.75·d^–1 and mean cell wall digestibility was 34%; these values fall within the range of other marsupials fedEucalyptus foliage. Digestible energy content ofE. radiata was high compared to other eucalypts because of the high content and digestibility of essential oils. However, excretion of essential oils and their metabolites in the urine meant that greater gliders retained only 55% of their digestible energy intakes (0.61 MJ · kg^–0.75· d^–1) as metabolizable energy (ME). Low ME intakes were not offset by low standard metabolic rates (2.39 W · kg^–0.75), but the efficiency with which ME substituted for tissue energy was high (94%), so that greater gliders were able to maintain energy balance and body mass onE. radiata foliage.Abbreviations ME metabolizable energy - DE digestible energy - RQ respiratory quotient - FHP fasting heat production     

Transfer factor of131I from the fallout to human thyroid dose equivalent after the Chernobyl accident

Summary A similar pattern of variation with time in observed maxima of daily dose equivalent rates in human thyroids (TD - µSv·d^–1) and of daily fallout radioactivities (FR - kBq·m^–2) has been found after the Chernobyl accident. An estimate of the time-lag between the maxima in TD lines and the preceding FR peaks was made of about seven days for adult and nine days for juveniles. Applying this time-lag it was possible to estimate transfer factors from the fall-out to thyroid dose equivalent: the highest estimated values were 221 µSv/kBq·m^–2 for adult and 641 µSv/kBq·m^–2 for juvenile thyroids. These values differ from those published by UNSCEAR (United Nations 1988), which have been calculated for various regions of Czechoslovakia, from ingestion and inhalation intake estimates. A broad variation of transfer factor values could be expected to result from such transfer calculations using ingestion and inhalation estimates. The findings also support the concept of a need for prolonged iodine prophylaxy after emissions of radioiodine into the environment.Abbreviations TD dose equivalent rates in thyroids [µSv·d^–1] - FR fall-out radioactivity (-ies) [kBq·m^–2]     

Organic reduction of tapioca wastewaters using modified RBC

A modified Rotating Biological Contactor (RBC) was used for the treatability studies of synthetic tapioca wastewaters. The RBC used was a four stage laboratory model and the discs were modified by attaching porous nechlon sheets to enhance biofilm area. Synthetic tapioca wastewaters were prepared with influent concentrations from 927 to 3600 mg/l of COD. Three hydraulic loads were used in the range of 0.03 to 0.09 m³·m^–2·d^–1 and the organic loads used were in the range of 28 to 306 g COD· m^–2·d^–1. The percentage COD removal were in the range from 97.4 to 68. RBC was operated at a rotating speed of 18 rpm which was found to be the optimal rotating speed. Biokinetic coefficients based on Kornegay and Hudson models were obtained using linear analysis. Also, a mathematical model was proposed using regression analysis.List of Symbols A m² total surface area of discs - d m active depth of microbial film onany rotating disc - K _s mg ·l^–1 saturation constant - P mg·m^–2·^–1 area capacity - Q l·d^–1 hydraulic flow rate - q m³·m^–2·d^–1 hydraulic loading rate - S ₀ mg·l^–1 influent substrate concentration - S _e mg·l^–1 effluent substrate concentration - w rpm rotational speed - V m³ volume of the reactor - X _f mg·l^–1 active biomass per unit volume ofattached growth - X _s mg·l^–1 active biomass per unit volume ofsuspended growth - X mg·l^–1 active biomass per unit volume - Y _s yield coefficient for attachedgrowth - Y _A yield coefficient for suspendedgrowth - Y yield coefficient, mass of biomass/mass of substrate removed Greek Symbols hr mean hydraulic detention time - (_max)_A d^–1 maximum specific growth rate forattached growth - (_max)_s d^–1 maximum specific growth rate forsuspended growth - _max d^–1 maximum specific growth rate - d^–1 specific growth rate - _v mg·l^–1·hr^–1 maximum volumetric substrateutilization rate coefficient     

Studies on the variables and kinetics of SCP production from nopal fruit juice

Summary Submerged batch cultivation under controlled environmental conditions of pH 3.8, temperature 30°C, and K_La200 h^–1 (above 180 mMO₂ l ^–1 h^–1 oxygen supply rate) produced a maximum (12.0 g·l ^–1) SCP (Candida utilis) yield on the deseeded nopal fruit juice medium containing C/N ratio of 7.0 (initial sugar concentration 25 g·l ^–1) with a yield coefficient of 0.52 g cells/g sugar. In continuous cultivation, 19.9 g·l ^–1 cell mass could be obtained at a dilution rate (D) of 0.36 h^–1 under identical environmental conditions, showing a productivity of 7.2 g·l ^–1·h^–1. This corresponded to a gain of 9.0 in productivity in continuous culture over batch culture. Starting with steady state values of state variables, cell mass (C_X–19.9 g·l ^–1), limiting nutrient concentration (C_ln–2.5 g·l ^–1) and sugar concentration (C_S–1.5 g·l ^–1) at control variable conditions of pH 3.8, 30°C, and K_La 200 h^–1 keeping D=0.36 h^–1 as reference, transient response studies by step changes of these control variables also showed that this pH, temperature and K_La conditions are most suitable for SCP cultivation on nopal fruit juice. Kinetic equations obtained from experimental data were analysed and kinetic parameters determined graphically. Results of SCP production from nopal fruit juice are described.Nomenclature C_ln concentration of ammonium sulfate (g·l ^–1) - C_S concentration of total sugar (g·l ^–1) - C_X cell concentration (g·l ^–1) - D dilution rate (h^–1) - K_ln Monod's constant (g·l ^–1) - m maintenance coefficient (g ammonium sulfate cell^–1 h^–1) - m_(S) maintenance coefficient (g sugar g cell^–1 h^–1) - t time, h - Y yield coefficient (g cells/g ammonium sulfate) - Y_m maximum of Y - Y_S yield coefficient based on sugar consumed (g cells · g sugar^–1) - Y_S(m) maximum value of Y_S - ^µm maximum specific growth rate constant (h^–1)     

Production of 4-decanolide by semicontinuous fermentation of Tyromyces sambuceus

Summary Tyromyces sambuceus was cultivated in a stirred tank reactor under semicontinuous conditions for 70 days. Over longer periods of time in submersion, values of 220 and 330 mg·L^–1 of 4-decanolide could be maintained; after dispersion of the headspace mycelia, a single peak product concentration of 880 mg·L^–1 was attained. The productivity was subject to large variations, peak values were 18 and 11 mg·L^–1·h^–1. Depending on the culture conditions, specific growth rates of up to 0.05 h^–1 were reached.     

Performance and kinetic evaluation of anaerobic moving bed biofilm reactor for treating milk permeate from dairy industry

High strength milk permeate derived from ultra-filtration based cheese making process was treated in an anaerobic moving bed biofilm reactor (AMBBR) under mesophilic (35 °C) condition. Total chemical oxygen demand (TCOD) removal efficiencies of 86.3–73.2% were achieved at organic loading rates (OLR) of 2.0–20.0 g TCOD L⁻¹ d⁻¹. A mass balance model gave values of methane yield coefficient (Y_G/S) and cell maintenance coefficient (k_m) of 0.341 L CH₄ g⁻¹ TCOD_removed and 0.1808 g TCOD_removed g⁻¹ VSS d⁻¹, respectively. The maximum substrate utilization rate U_max was determined as 89.3 g TCOD L⁻¹ d⁻¹ by a modified Stover–Kincannon model. Volumetric methane production rates (VMPR) were shown to correlate with the biodegradable TCOD concentration through a Michaelis–Menten type equation. Moreover, based on VMPR and OLR removed from the reactor, the sludge production yield was determined as 0.0794 g VSS g⁻¹ TCOD_removed.