Poly(3-hydroxybutyrate) production by Cupriavidus necator using waste glycerol

Polyhydroxyalkanoates (PHAs) have been recognized as good substitutes for the non-biodegradable petrochemically produced polymers. However, their high (real or estimated) current production cost limits their industrial applications. This work exploits two strategies to enhance PHAs substitution potential: the increase in PHA volumetric productivity in high density cultures and the use of waste glycerol (GRP), a by-product from the biodiesel industry, as primary carbon source for cell growth and polymer synthesis. Cupriavidus necator DSM 545 was used to accumulate poly(3-hydroxybutyrate) (P(3HB)) from GRP and from commercial glycerol (PG) as control substrate. On PG, productivities between 0.6 g_PHB L^?1 h^?1 and 1.5 g_PHB L^?1 h^?1 were attained. The maximum cell DW was 82.5 g_DW L^?1, the P(3HB) content being 62%. When GRP was used, 68.8 g_DW L^?1 with a P(3HB) accumulation of 38% resulting in a final productivity of 0.84 g_PHB L^?1 h^?1 was obtained. By decreasing the biomass concentration at which accumulation was triggered, a productivity of 1.1 g_PHB L^?1 h^?1 (50% P(3HB), w/w) was attained using GRP. P(3HB) molecular weights (M_w) ranged from 7.9 × 10⁵ to 9.6 × 10⁵ Da.     

A new bioprocess for the production of prebiotic lactosucrose by an immobilized β-galactosidase

A new bioprocess for the synthesis of lactosucrose was studied using a covalently immobilized β-galactosidase on macrospheres of chitosan. The effects of temperature and pH on the production of lactosucrose and other oligosaccharides were evaluated. At 30 °C and pH 7.0, the maximum concentration of lactosucrose reached to 79 g L⁻¹. The change of the reaction conditions allowed to modify the qualitative profile of the final products without quantitative change in the total of oligosaccharides produced. At pH 7 and 30 °C, products profile was 79 g L⁻¹ of lactosucrose, 37 g L⁻¹ of galactooligosaccharides and 250 g L⁻¹ of total oligosaccharides, while at pH 5 and 64 °C the concentrations for the same compounds were 40, 62 and 250 g L⁻¹, respectively. The immobilization increased the thermal stability up to 260-fold. Using 300 g L⁻¹ of sucrose and 300 g L⁻¹ of lactose, and 8.5 mg of chitosan mL⁻¹, 30 cycles of reuse were performed and the biocatalyst kept the maximal lactosucrose synthesis. These results fulfill some important aspects for the enzyme immobilization and oligosaccharides synthesis: the simplicity of the protocols, the high operational stability of the enzyme and the possibility of driving the final products.     

Bioconversion of phenylpyruvic acid to l-phenylalanine by mixed-gel immobilization of Escherichia coli EP8-10

A mixed-gel of κ-carrageenan and gelatin was used in l-phenylalanine production. The mixed-gel, containing 87.5% κ-carrageenan and 12.5% gelatin [the total gel concentration was 4 wt%], showed the best performance and was selected for further study with Escherichia coli EP8-10. The optimum pH and temperature were 8.5 and 37 °C, respectively. The effects of trehalose and Mg²⁺ were studied in the mixed-gel immobilization. Their optimum concentrations were 5 × 10^?2 and 2 × 10^?3 mol/L, respectively. Under the optimal conditions, 98.3% of the phenylpyruvic acid (PPA) was converted to l-phenylalanine. The activity recovery of the transaminase enzyme in the mixed-gel immobilization was higher than that in single κ-carrageenan immobilization, which was 93.6%. The total PPA conversion rate was over 80% in all 15 batches, suggesting great sustainability in the mixed-gel immobilization. The maximum reaction rate (r_max) was calculated to be 4.75 × 10^?2 mol/(L g h).     

Xylitol production from non-detoxified corncob hemicellulose acid hydrolysate by Candida tropicalis

The interest on use of lignocellulose for producing chemicals is increasing as these feedstocks are low cost, renewable and widespread sources of sugars. Corncob is an attractive raw material for xylitol production due to its high content of xylan. In this study, hemicellulose hydrolysate from corncobs without detoxification was used for xylitol production by Candida tropicalis CCTCC M2012462. Compared with prepared xylose medium, xylitol production with dilute acid hydrolysate medium does not seem to influence specific xylose reductase activity. The decrease in xylitol productivity with dilute acid hydrolysate medium is a result of a lower biomass concentration and lag-phase time. It appears that biomass growth rate is essential for xylitol production. In xylitol fermentation with a low initial inhibitors concentration and substrate feeding strategy, a maximal xylitol concentration of 38.8 g l⁻¹ was obtained after 84 h of fermentation, giving a yield of 0.7 g g⁻¹ xylose and a productivity of 0.46 g l⁻¹ h⁻¹.     

New integrated bioprocess for the continuous production,extraction and purification of lipopeptides produced by Bacillus subtilis in membrane bioreactor

Recently, a bubbleless membrane bioreactor (BMBR) has been successfully developed for biosurfactant production by Bacillus subtilis [1]. In this study, for the first time, continuous culture were carried out for the production of surfactin in a BMBR, both with or without a coupled microfiltration membrane. Results from continuous culture showed that a significant part of biomass was immobilized onto the air/liquid membrane contactor. Immobilized biomass activity onto the air/liquid membrane contactor was monitored using a respirometric analysis. Kinetics of growth, surfactin and primary metabolites production were investigated. Planktonic biomass, immobilized biomass and surfactin production and productivity obtained in batch culture (3 L) of 1.5 days of culture were 4.5 g DW, 1.3 g DW, 1.8 g and 17.4 mg L^?1 h^?1, respectively. In continuous culture without total cell recycling (TCR), the planktonic biomass was leached, but immobilized biomass reached a steady state at an estimated 6.6 g DW. 11.5 g of surfactin was produced after 3 days of culture, this gave an average surfactin productivity of 54.7 mg L^?1 h^?1 for the continuous culture, which presented a surfactin productivity of 30 mg L^?1 h^?1 at the steady state. TCR was then investigated for the continuous production, extraction and purification of surfactin using a coupled ultrafiltration step. In continuous culture with TCR at a dilution rate of 0.1 h^?1, planktonic biomass, immobilized biomass, surfactin production and productivity reached 7.5 g DW, 5.5 g DW, 7.1 g and 41.6 mg L^?1 h^?1 respectively, after 2 days of culture. After this time, biomass and surfactin productions stopped. Increasing dilution rate to 0.2 h^?1 led to the resumption of biomass and surfactin production and these values reached 11.1 g DW, 10.5 g DW, 7.9 g and 110.1 mg L^?1 h^?1, respectively, after 3 days of culture. This study has therefore shown that with this new integrated bioprocess, it was possible to continuously extract and purify several grams of biosurfactant, with purity up to 95%.     

Improvement in natamycin production by Streptomyces natalensis with the addition of short-chain carboxylic acids

Natamycin is an important tetraene (polyene) antibiotic produced in submerged culture by different strains of Streptomyces sp. In the present work, the effects of the addition of short-chain carboxylic acids (acetic, propionic and butyric) on cell growth and the kinetics of natamycin production were investigated during submerged cultivation of Streptomyces natalensis. The addition of acetic and propionic acids showed stimulatory effects on natamycin production when added to the fermentation medium at concentrations below 2 g L^?1 at the beginning of cultivation. In addition, when acetic and propionic acids were added in a mixture (7:1) at a total concentration of 2 g L^?1, antibiotic production increased significantly, reaching 3.0 g L^?1 (approximately 223% and 250% increases in volumetric and specific antibiotic production, respectively, compared with the control culture). Moreover, the addition of carboxylic acids not only increased the antibiotic yield but also decreased the production time from 96 h to only 84 h in shake-flask cultures. A further enhancement in natamycin production was achieved by cultivation in a 2-L stirred-tank bioreactor under controlled pH conditions. The maximum volumetric production of 3.98 g L^?1 was achieved after 84 h in carboxylic acid-supplemented culture (acetate and propionate in a ratio of 7:1).     

Production of yeast chitin–glucan complex from biodiesel industry byproduct

Crude glycerol from the biodiesel industry was used as carbon source for high cell density fed-batch cultivation of Pichia pastoris aiming at producing a chitin–glucan complex (CGC). More than 100 g L^?1 biomass was obtained in less than 48 h. The yield of biomass on a glycerol basis was 0.55 g g^?1 during the batch phase and 0.63 g g^?1 during the fed-batch phase. The chitin–glucan complex was recovered from the yeast cell wall by hot alkaline extraction. CGC content in the cell wall was found to be relatively constant throughout the cultivation (18–26%) with a volumetric productivity of 1.28 g L^?1 h^?1 at the end of the fed-batch phase. The molar ratio of chitin:β-glucan in the extracted biopolymer was 16:84, close to other CGC extracted from Aspergillus biomass. The extracted polymer was characterized by Differential Scanning Calorimetry (DCS) and solid-state Nuclear Magnetic Resonance (NMR) spectroscopy and compared with commercial biopolymers, namely, crab shell chitin and/or chitosan, algal β-glucan (laminarin) and fungal chitin–glucan complex (kiOsmetine).     

Continuous production of selenomethionine-enriched Chlorella sorokiniana biomass in a photobioreactor

This article describes the enrichment of the fresh-water green microalga Chlorella sorokiniana in selenomethionine (SeMet). The microalga was cultivated in a 2.2 L glass-vessel photobioreactor, in a culture medium supplemented with selenate (SeO₄^2?) concentrations ranging from 5 to 50 mg L^?1. Although selenate exposure lowered culture viability, C. sorokiniana grew well at all tested selenate concentrations, however cultures supplemented with 50 mg L^?1 selenate did not remain stable at steady state. A suitable selenate concentration in fresh culture medium for continuous operation was determined, which allowed stable long-term cultivation at steady state and maximal SeMet productivity. In order to do that, the effect of dilution rate on biomass productivity, viability and SeMet content of C. sorokiniana at several selenate concentrations were determined in the photobioreactor. A maximal SeMet productivity of 21 μg L^?1 day^?1 was obtained with 40 mg L^?1 selenate in the culture medium. Then a continuous cultivation process at several dilution rates was performed at 40 mg L^?1 selenate obtaining a maximum of 246 μg L^?1 day^?1 SeMet at a low dilution rate of 0.49 day^?1, calculated on total daily effluent volume. This paper describes for the first time an efficient long-term continuous cultivation of C. sorokiniana for the production of biomass enriched in the high value amino acid SeMet, at laboratory scale.     

Catalytic removal of sulfide by an immobilized sulfide-oxidase bioreactor

A bioreactor packed with chitosan immobilized sulfide-oxidase from Streptomyces species LD048 was developed to treat a liquid stream of sulfide. The inoculation system was composed of glass with a 0.7 L working volume and enzyme activity of 2 mmol S g^?1 carrier. The sulfide removal efficiency was almost 100% when the volumetric loading was increased up to 3.9 mmol S L^?1 h^?1 at a space velocity of 18 h^?1. The maximal elimination capacity was 22.1 mmol S L^?1 h^?1 with a space velocity of 72 h^?1. When the aeration was increased from 0.05 to 0.1 L min^?1, the average removal efficiency improved from 81% to 94%. A removal efficiency of 90% was obtained after 15 days of operation with a load rate of 8.9 mmol S L^?1 h^?1 and a space velocity of 14.28 h^?1. An operational equation based on the ideal plug flow bioreactor and the Michaelis–Menten model predicted the performance of this bioreactor.     

Inulin hydrolysis and citric acid production from inulin using the surface-engineered Yarrowia lipolytica displaying inulinase

The INU1 gene encoding exo-inulinase cloned from Kluyveromyces marxianus CBS 6556 was ligated into the surface display plasmid and expressed in the cells of the marine-derived yeast Yarrowia lipolytica which can produce citric acid. The expressed inulinase was immobilized on the yeast cells. The activity of the immobilized inulinase with 6 × His tag was found to be 22.6 U mg^?1 of cell dry weight after cell growth for 96 h. The optimal pH and temperature of the displayed inulinase were 4.5 and 50 °C, respectively and the inulinase was stable in the pH range of 3–8 and in the temperature range of 0–50 °C. During the inulin hydrolysis, the optimal inulin concentration was 12.0% and the optimal amount of added inulinase was 181.6 U g^?1 of inulin. Under such conditions, over 77.9% of inulin was hydrolyzed within 10 h and the hydrolysate contained main monosaccharides and disaccharides, and minor trisaccharides. During the citric acid production in the flask level, the recombinant yeast could produce 77.9 g L^?1 citric acid and 5.3 g L^?1 iso-citric acid from inulin while 68.9 g L^?1 of citric acid and 4.1 g L^?1 iso-citric acid in the fermented medium were attained within 312 h of the 2-L fermentation, respectively.     

Repeated fed-batch cultivation of Arthrospira (Spirulina) platensis using urea as nitrogen source

Arthrospira (Spirulina) platensis (Nordstedt) Gomont was autotrophically cultivated for biomass production in repeated fed-batch process using urea as nitrogen source, with the aim of making large-scale production easier, increasing cell productivity and then reducing the production costs. It was investigated the influence of the ratio of renewed volume to total volume (R), the urea feeding time (t_f) and the number of successive repeated fed-batch cycles on the maximum cell concentration (X_m), cell productivity (P_x), nitrogen-to-cell conversion yield (Y_x/n), maximum specific growth rate (μ_m) and protein content of dry biomass. The experimental results demonstrated that R = 0.80 and t_f = 6 d were the best cultivation conditions, being able to simultaneously ensure, throughout the three fed-batch cycles, the highest average values of three of the five responses (X_m = 2101 ± 113 mg L^?1, P_x = 219 ± 13 mg L^?1 d^?1 and Y_x/n = 10.3 ± 0.8 g g^?1).     

Bench-scale fermentation of Trichoderma viride on wastewater sludge: Rheology,lytic enzymes and biocontrol activity

Conidiation and lytic enzyme production by Trichoderma viride at different solids concentration of pre-treated municipal wastewater sludge was examined in a 15-L fermenter. The maximum conidia concentration (5.94 × 10⁷ CFU mL⁻¹ at 96 h) was obtained at 30 g L⁻¹ suspended solids. The maximum lytic enzyme activities were achieved around 12–30 h of fermentation. Bioassay against a fungal phytopathogen, Fusarium sp. showed maximum activity in the sample drawn around 96 h of fermentation at 30 g L⁻¹ suspended solids concentration. Entomotoxicity against spruce budworm larvae showed maximum value ≈17290 SBU μL⁻¹ at 30 g L⁻¹ suspended solids concentration at the end of fermentation (96 h). Plant bioassay showed dual action of T. viride, i.e., disease prevention and growth promotion. The rheological analyses of fermentation sludges showed the pseudoplastic behaviour. In order to maintain required dissolved oxygen concentration ≥30%, the agitation and aeration requirements significantly increased at 35 g L⁻¹ compared to 30 and 25 g L⁻¹. The oxygen uptake rate and volumetric oxygen mass transfer coefficient, k_La at 35 g L⁻¹ did not increase in comparison to 30 g L⁻¹ due to rheological complexity of the broth during fermentation. Thus, the successful fermentation operation of the biocontrol fungus T. viride is a rational indication of its potential for mass-scale production for agriculture and forest sector as a biocontrol agent.     

Challenges in enzymatic hydrolysis and fermentation of pretreated Arundo donax revealed by a comparison between SHF and SSF

The perennial herbaceous crop Arundo donax is a potential feedstock for second-generation bioethanol production. In the present work, two different process options were investigated for the conversion of two differently steam-pretreated batches of A. donax. The pretreated raw material was converted to ethanol with a xylose-consuming Saccharomyces cerevisiae strain, VTT C-10880, by applying either separate hydrolysis and fermentation (SHF) or simultaneous saccharification and fermentation (SSF). The highest overall ethanol yield and final ethanol concentration were achieved using SHF (0.27 g g^?1 and 20.6 g L^?1 compared to 0.24 g g^?1 and 19.0 g L^?1 when SSF was used). The performance of both SHF and SSF was improved by complementing the cellulolytic enzymes with hemicellulases. The higher amount of acetic acid in one of the batches was shown to strongly affect xylose consumption in the fermentation. Only half of the xylose was consumed when batch 1 (high acetic acid) was fermented, compared to that 94% of the xylose was consumed in fermentation of batch 2 (lower acetic acid). Furthermore, the high amount of xylooligomers present in the pretreated materials considerably inhibited the enzymatic hydrolysis. Both the formation of xylooligomers and acetic acid thus need to be considered in the pretreatment process in order to achieve efficient conversion of A. donax to ethanol.     

Valorization of olive stones for xylitol and ethanol production from dilute acid pretreatment via enzymatic hydrolysis and fermentation by Pachysolen tannophilus

Olive stones are an agro-industrial by-product abundant in the Mediterranean area that is regarded as a potential lignocellulosic feedstock for sugar production. Statistical modeling of dilute-sulphuric acid hydrolysis of olive stones has been performed using a response surface methodology, with treatment temperature and process time as factors, to optimize the hydrolysis conditions aiming to attain maximum d-xylose extraction from hemicelluloses. Thus, solid yield and composition of solid and liquid phases were assessed by empirical modeling. The highest yield of d-xylose was found at a temperature of 195 °C for 5 min. Under these conditions, 89.7% of the total d-xylose was recovered from raw material. The resulting solids from optimal conditions were assayed as substrate for enzymatic hydrolysis, while fermentability of hemicellulosic hydrolysates was tested using the d-xylose-fermenting yeast Pachysolen tannophilus. Both bioprocesses were considerably influenced by enzyme loading and inoculum size. In the enzymatic hydrolysis step, about 56% of cellulose was converted into d-glucose by using an enzyme/solid ratio of 40 FPU g⁻¹, while in the fermentation carried out with a cell concentration of 2 g L⁻¹ a yield of 0.44 g xylitol/g d-xylose and a global volumetric productivity of 0.11 g L⁻¹ h⁻¹ were achieved.     

Bioprocess development for kefiran production by Lactobacillus kefiranofaciens in semi industrial scale bioreactor

Lactobacillus kefiranofaciens is non-pathogenic gram positive bacteria isolated from kefir grains and able to produce extracellular exopolysaccharides named kefiran. This polysaccharide contains approximately equal amounts of glucose and galactose. Kefiran has wide applications in pharmaceutical industries. Therefore, an approach has been extensively studied to increase kefiran production for pharmaceutical application in industrial scale. The present work aims to maximize kefiran production through the optimization of medium composition and production in semi industrial scale bioreactor. The composition of the optimal medium for kefiran production contained sucrose, yeast extract and K₂HPO₄ at 20.0, 6.0, 0.25 g L⁻¹, respectively. The optimized medium significantly increased both cell growth and kefiran production by about 170.56% and 58.02%, respectively, in comparison with the unoptimized medium. Furthermore, the kinetics of cell growth and kefiran production in batch culture of L. kefiranofaciens was investigated under un-controlled pH conditions in 16-L scale bioreactor. The maximal cell mass in bioreactor culture reached 2.76 g L⁻¹ concomitant with kefiran production of 1.91 g L⁻¹.     

Nitrate removal and greenhouse gas production in a stream-bed denitrifying bioreactor

Denitrifying bioreactors are currently being tested as an option for treating nitrate (NO₃^?) contamination in groundwater and surface waters. However, a possible side effect of this technology is the production of greenhouse gases (GHG) including nitrous oxide (N₂O) and methane (CH₄). This study examines NO₃^? removal and GHG production in a stream-bed denitrifying bioreactor currently operating in Southern Ontario, Canada. The reactor contains organic carbon material (pine woodchips) intended to promote denitrification. Over a 1 year period, monthly averaged removal of influent (stream water) NO₃^? ranged from 18 to 100% (0.3–2.5 mg N L^?1). Concomitantly, reactor dissolved N₂O and CH₄ production, averaged 6.4 μg N L^?1 (2.4 mg N m^?2 d^?1), and 974 μg C L^?1 (297 mg C m^?2 d^?1) respectively, where production is calculated as the difference between inflow and effluent concentrations. Gas bubbles entrapped in sediments overlying the reactor had a composition ranging from 19 to 64% CH₄, 1 to 6% CO₂, and 0.5 to 2 ppmv N₂O; however, gas bubble emission rates were not quantified in this study. Dissolved N₂O production rates from the bioreactor were similar to emission rates reported for some agricultural croplands (e.g. 0.1–15 mg N m^?2 d^?1) and remained less than the highest rates observed in some N-polluted streams and rivers (e.g. 110 mg N m^?2 d^?1, Grand R., ON). Dissolved N₂O production represented only a small fraction (0.6%) of the observed NO₃^? removal over the monitoring period. Dissolved CH₄ production during summer months (up to 1236 mg C m^?2 d^?1), was higher than reported for some rivers and reservoirs (e.g. 6–66 mg C m^?2 d^?1) but remained lower than rates reported for some wastewater treatment facilities (e.g. sewage treatment plants and constructed wetlands, 19,500–38,000 mg C m^?2 d^?1).     

Glucose isomerase production on a xylan-based medium by Bacillus thermoantarcticus

Effects of medium components on intracellular glucose isomerase (GI) production were investigated by Bacillus thermoantarcticus. The highest GI activity was obtained as 1630 U dm^?3 in the medium containing (g dm^?3): 10.6, birchwood-xylan; 5.6, yeast extract; 5.9 (NH₄)₂SO₄ at T = 55 °C in 33 cm^?3 shake-flasks. When birchwood-xylan was replaced with oat spelt- or beechwood-xylan, GI activity decreased to 1372 and 1308 U dm^?3, respectively. Effects of pH at uncontrolled-pH (pH_UC = 6.0) and controlled-pH (pH_C = 6.0) operations, and oxygen transfer at the air inlet rate of 0.5 vvm and agitation rates of 300, 500 and 700 min^?1, were investigated in 3.0 dm³ bioreactor system with 1.65 dm³ working volume in the designed medium. The highest GI activity was attained at 500 min^?1, 0.5 vvm, pH_UC = 6 as 1840 U dm^?3 where cell concentration was 2.3 g dm^?3. The use of agricultural waste xylan, as the carbon source resulted in concomitant production of xylanase and GI. The highest xylanase activity was attained as 9300 U dm^?3 at 500 min^?1 and 0.5 vvm. K_La varied between 0.008–0.033 s^?1 whereas the highest oxygen uptake rate was 0.002 mmol dm^?3 s^?1. Initially biochemical reaction limitations were effective; thereafter, mass transfer resistances became more effective.     

Methanol vapor biofiltration coupled with continuous production of recombinant endochitinase Ech42 by Pichia Pastoris

Methanol biofiltration using methylotrophic microorganisms has been previously reported by various authors. In a previous study, a modified strain of Pichia pastoris was tested for the ability to produce endochitinase (Ech42) when coupled with methanol vapor biodegradation in batch tests. The next challenge was to validate the process in a continuous system. Thus, in the present study, a biofilter packed with perlite and inoculated with P. pastoris transformed with the plasmid pPIC-ech42 was used for methanol vapor biofiltration and the continuous production of recombinant endochitinase (Ech42) for 60 days. The maximum elimination capacity (EC) of methanol obtained was 1320 g m^?3 h^?1 at a loading rate of 1465 g m^?3 h^?1. The extracellular protein production rate in the leachate was 2360 μg h^?1 with a chitinase enzymatic activity of 123 U L^?1. The protein content on the biofilm samples was negligible, indicating the effectiveness of the overall process and of P. pastoris to excrete proteins. The carbon balance indicated that 81% of the consumed methanol was mineralized and 5.8% was incorporated into biomass. The results of this study and the economic balance underscore the promising application of linking methanol vapor biofiltration to the continuous production of recombinant proteins.     

Improved β-carotene production of Rhodotorula glutinis in fermented radish brine by continuous cultivation

Fermentation kinetics of growth and β-carotene production by Rhodotorula glutinis DM28 in batch and continuous cultures using fermented radish brine, a waste generated from fermented vegetable industry, as a cultivation medium were investigated. The suitable brine concentration for β-carotene production by R. glutinis DM28 was 30 g l^?1. Its growth and β-carotene production obtained by batch culture in shake flasks were 2.2 g l^?1 and 87 μg l^?1, respectively, while, in a bioreactor were 2.6 g l^?1 and 186 μg l^?1, respectively. Furthermore, its maximum growth rate and β-carotene productivity in continuous culture obtained at the dilution rate of 0.24 h^?1 were 0.3 g l^?1 h^?1 and 19 μg l^?1 h^?1, respectively, which were significantly higher than those in the batch. Therefore, improved growth rate and β-carotene productivity of R. glutinis in fermented radish brine could be accomplished by continuous cultivation.     

β-carotene production from soap stock by loofa-immobilized Rhodotorula rubra in an airlift photobioreactor

In this study, the soap stock as a sole carbon source was used for growing a carotenoid producing yeast (Rhodotorula rubra). The application of soap stock resulted in increase of carotenoids yield up to 5.36 folds when compared with the grown cultures on glucose. On the best Monod equation fitted on the specific growth rate (μ) data, the maximum specific growth rate (μ_m) and half-saturation concentration (K_S) were respectively determined at 0.064 h⁻¹ and 3.26 g L⁻¹ for total fatty acids presented in soap stock. Further tests on the carotenogenesis process were carried out in a cell-immobilized airlift photobioreactor where the natural loofa sponge was used for immobilization of the cells. The performance of the bioreactor was statistically studied by the response surface methodology (RSM) where aeration rate of 0.11 vvm and light irradiation intensity of 2517 Lx provided an optimum condition for producing β-carotene with a specific production rate of 22.65 mg g_cell⁻¹ day⁻¹.