Biological removal of pyridine in heavy oil byRhodococcus sp. KCTC 3218

The removal of organic nitrogen compounds present in crude perroleum and shale oils poses a challenging problem in petroleum industries. The deleterious effect of nitrogen compounds on cracking catalysts and the indication that they contribute to gum formation in gasolines are some of these aspects. Pyridine, a representative nitrogen compound in gaavy oil—was degraded byRhodoccus sp. KCTC 3218 in a water-heavy oil two-phase system. The pyridine degradation rate was affected by the presence of hydrocarbons such as n-hexadecane. This microorganism formed flocs which could be a barrier to mass transfer between the cells in flocs and the pyridine dissolved in water. This problem could be overcome by the addition of a surfactant such as Triton X-100. The ratio of water to heavy oil was important to separate the heavy oil phase from the water phase after treating the heavy oil. The culture medium was emulsified by a sort of biosurfactant secreted by this microorganism. The emulsified oil phase returned to its natural state when the ratio of water to heavy oil was 1.5. Above this ratio, the emulsified oil phase remained an emulsion after decantation. Pyridine in heavy oil was completely degraded in 15 hr at this water to heavy oil ratio of 1.5 when the concentration of pyridine in heavy oil was 700 ppm and the cell concentration was 0.32 g DCW/L.     

Biodegradability of diesel oil

In batch culture diesel oil was degraded rapidly, with a maximum growth rate (for a consortium of microorganisms) of 0.55 h^-1. The corresponding yield Y _SX was 0.1 Cmol/Cmol. In a continuous stirred tank reactor the maximum dilution rate was about 0.25 h^-1, with a yield of 0.3 Cmol/Cmol. With a residence time of 1 day 82% of the influent oil was degraded. In the batch reactor, of the mixture of linear and branched alkanes the linear alkanes were degraded fastest and with the highest yield. Only after most of the linear alkanes had disappeared were the branched alkanes consumed. In a CSTR a large part of the branched alkanes was not degraded.     

Catalytic Packed-Bed Reactor Configuration for Biodiesel Production Using Waste Oil as Feedstock

Pumice, a natural porous silica material, exchanged with potassium is an efficient heterogeneous particulate catalytic material for triglycerides and free fatty acids transesterification reaction from sunflower oil and waste frying oil at low temperature. In this work, a packed-bed catalytic configuration reactor using this catalytic material was developed for biodiesel fuel production from sunflower oil and frying oil feedstock. Reactor operation variables as methanol/oil molar ratio, catalyst amount, reaction time, and reaction temperature were studied. Results were compared with those obtained from the same transesterification reaction proceeding in a slurry batch reactor. The packed-bed catalytic reactor configuration can be useful in order to minimize catalyst mechanical damage occurring in the slurry reactor due to continuous stirring. The possibility of using a packed-bed reactor shows some advantages because the catalyst stays confined in the reactor bed and the reaction products can be easily separated, besides the mechanical stability of the catalyst particles is achieved.     

Improvement of biodesulfurization activity of alginate immobilized cells in biphasic systems

The immobilization of Pseudomonas delafieldii R-8 in calcium alginate beads has been studied in order to improve biodesulfurization activity in oil/water (O/W) biphasic systems. A gas jet extrusion technique was performed to produce immobilized beads. The specific desulfurization rate of 1.5 mm diameter beads was 1.4-fold higher than that of 4.0 mm. Some nonionic surfactants can significantly increase the activity of immobilized cells. The desulfurization rate with the addition of 0.5% Span 80 increased 1.8-fold compared with that of the untreated beads. The rate of biodesulfurization was markedly enhanced by decreasing the size of alginate beads and adding the surfactant Span 80, most likely resulting from the increasing mass transfer of substrate to gel matrix.     

Effect of various additives on enzymatic hydrolysis of castor oil

Hydrolysis of castor oil using lipase enzyme is carried out in a batch reactor at room temperature (35–40 °C). In order to reduce the cost of enzyme catalyzed reaction, water in oil emulsion and a 3:1 ratio of oil to water is selected. The concentration of enzyme in the reaction mixture is optimized. The effect of various additives like solvent and salt which can enhance the rate of reaction is studied. It is found that the glycerol has no effect on the hydrolysis of oil. The reusability of the lipase enzyme has also been tested. The yield of enzymatic hydrolysis of castor oil is compared with those of coconut oil and olive oil.     

Enzymatic production of biodiesel from cotton seed oil using t-butanol as a solvent

The enzymatic production of biodiesel by methanolysis of cottonseed oil was studied using immobilized Candida antarctica lipase as catalyst in t-butanol solvent. Methyl ester production and triacylglycerol disappearance were followed by HPLC chromatography. It was found, using a batch system, that enzyme inhibition caused by undissolved methanol was eliminated by adding t-butanol to the reaction medium, which also gave a noticeable increase of reaction rate and ester yield. The effect of t-butanol, methanol concentration and temperature on this system was determined. A methanolysis yield of 97% was observed after 24h at 50 degrees C with a reaction mixture containing 32.5% t-butanol, 13.5% methanol, 54% oil and 0.017 g enzyme (g oil)(-1). With the same mixture, a 95% ester yield was obtained using a one step fixed bed continuous reactor with a flow rate of 9.6 mlh(-1) (g enzyme)(-1). Experiments with the continuous reactor over 500 h did not show any appreciable decrease in ester yields.     

Aerobic MTBE biodegradation in the presence of BTEX by two consortia under batch and semi-batch conditions

This study explores the effect of microbial consortium composition and reactor configuration on methyl tert-butyl ether (MTBE) biodegradation in the presence of benzene, toluene, ethylbenzene and p-xylenes(BTEX). MTBE biodegradation was monitored in the presence and absence of BTEX in duplicate batch reactors inoculated with distinct enrichment cultures: MTBE only (MO—originally enriched on MTBE) and/or MTBE BTEX (MB—originally enriched on MTBE and BTEX). The MO culture was also applied in a semi-batch reactor which received both MTBE and BTEX periodically in fresh medium after allowing cells to settle. The composition of the microbial consortia was explored using a combination of 16S rRNA gene cloning and quantitative polymerase chain reaction targeting the known MTBE-degrading strain PM1^T. MTBE biodegradation was completely inhibited by BTEX in the batch reactors inoculated with the MB culture, and severely retarded in those inoculated with the MO culture (0.18 ± 0.04 mg/L-day). In the semi-batch reactor, however, the MTBE biodegradation rate in the presence of BTEX was almost three times as high as in the batch reactors (0.48 ± 0.2 mg/L-day), but still slower than MTBE biodegradation in the absence of BTEX in the MO-inoculated batch reactors (1.47 ± 0.47 mg/L-day). A long lag phase in MTBE biodegradation was observed in batch reactors inoculated with the MB culture (20 days), but the ultimate rate was comparable to the MO culture (0.95 ± 0.44 mg/L-day). Analysis of the cultures revealed that strain PM1^T concentrations were lower in cultures that successfully biodegraded MTBE in the presence of BTEX. Also, other MTBE degraders, such as Leptothrix sp. and Hydrogenophaga sp. were found in these cultures. These results demonstrate that MTBE bioremediation in the presence of BTEX is feasible, and that culture composition and reactor configuration are key factors.     

Biodiesel production by enzymatic process using Jatropha oil and waste soybean oil

In this study, non-edible Jatropha oil and postcooking waste soybean oil were utilized for enzymatic biodiesel production. The process was optimized by using a statistical method. In addition, a novel continuous process using co-immobilized Rhizopus oryzae and Candida rugosa lipases was developed. The optimum conditions for the batch process were determined to be a reaction temperature of 45oC, an agitation speed of 250 rpm, 10 wt% of water, and 20% of immobilized lipases. A conversion of about 98% at 4 h could be achieved for biodiesel production using Jatropha oil, while a conversion of about 97% at 4 h was achieved from waste soybean oil. A packed bed reactor charged with co-immobilized lipases was employed for continuous biodiesel production from Jatropha and waste soybean oil. The reactor consisted of a jacketed glass column (ID 25 mm × 130 mm), in which a temperature of 45°C was maintained by water circulation. A maximum conversion of about 80% in 24 h at a flow rate of 0.8 mL/ min was achieved with the continuous process, whereas in the two-stage continuous process, a conversion of about 90% in 72 h was attained at a flow rate of 0.1 mL/min.     

Improvement of biodesulfurization rate by assembling nanosorbents on the surfaces of microbial cells

To improve biodesulfurization rate is a key to industrialize biodesulfurization technology. The biodesulfurization rate is partially affected by transfer rate of substrates from organic phase to microbial cell. In this study, gamma-Al2O3 nanosorbents, which had the ability to selectively adsorb dibenzothiophene (DBT) from organic phase, were assembled on the surfaces of Pseudomonas delafieldii R-8 cell, a desulfurization strain. gamma-Al2O3 nanosorbents have the ability to adsorb DBT from oil phase, and the rate of adsorption was far higher than that of biodesulfurization. Thus, DBT can be quickly transferred to the biocatalyst surface where nanosorbents were located, which quickened DBT transfer from organic phase to biocatalyst surface and resulted in the increase of biodesulfurization rate. The desulfurization rate of the cells assembled with nanosorbents was approximately twofold higher than that of original cells. The cells assembled with nanosorbents were observed by a transmission electron microscope.     

Enzymatic conversion of sunflower oil to biodiesel in a solvent-free system: Process optimization and the immobilized system stability

The feasibility of using the commercial immobilized lipase from Candida antarctica (Novozyme 435) to synthesize biodiesel from sunflower oil in a solvent-free system has been proved. Using methanol as an acyl acceptor and the response surface methodology as an optimization technique, the optimal conditions for the transesterification has been found to be: 45 ^oC, 3% of enzyme based on oil weight, 3:1 methanol to oil molar ratio and with no added water in the system. Under these conditions, >99% of oil conversion to fatty acid methyl ester (FAME) has been achieved after 50 h of reaction, but the activity of the immobilized lipase decreased markedly over the course of repeated runs. In order to improve the enzyme stability, several alternative acyl acceptors have been tested for biodiesel production under solvent-free conditions. The use of methyl acetate seems to be of great interest, resulting in high FAME yield (95.65%) and increasing the half-life of the immobilized lipase by about 20.1 times as compared to methanol. The reaction has also been verified in the industrially feasible reaction system including both a batch stirred tank reactor and a packed bed reactor. Although satisfactory performance in the batch stirred tank reactor has been achieved, the kinetics in a packed bed reactor system seems to have a slightly better profile (93.6 ± 3.75% FAME yield after 8–10 h), corresponding to the volumetric productivity of 48.5 g/(dm³ h). The packed bed reactor has operated for up to 72 h with almost no loss in productivity, implying that the proposed process and the immobilized system could provide a promising solution for the biodiesel synthesis at the industrial scale.     

Biodegradation and detoxification of phenolic compounds by pure and mixed indigenous cultures in aerobic reactors

Degradation and detoxification of a mixture of persistent compounds (2-chlorophenol, phenol and m-cresol) were studied by using pure and mixed indigenous cultures in aerobic reactors. Biodegradation assays were performed in batch and continuous flow reactors. Biodegradation was evaluated by determining total phenols, ultraviolet spectrophotometry and chemical oxygen demand (COD). Microbial growth was measured by the plate count method. Scanning electronic microscopy was employed to observe the microbial community in the reactor. Detoxification was evaluated by using Daphnia magna toxicity tests. Individual compounds were degraded by pure bacteria cultures within 27 h. The mixture of 2-clorophenol (100 mgl⁻¹), phenol (50 mgl⁻¹) and m-cresol (50 mgl⁻¹) was degraded by mixed bacteria cultures under batch conditions within 36 h: 99.8% of total phenols and 92.5% of COD were removed; under continuous flow conditions 99.8% of total phenols and 94.9% of COD were removed. Mineralization of phenolic compounds was assessed by gas chromatography performed at the end of the batch assays and in the effluent of the continuous-flow reactor. Toxicity was not detected in the effluent of the continuous-flow reactor.     

Preparation of astaxanthin by lipase-catalyzed hydrolysis from its esters in a slug-flow microchannel reactor

Natural astaxanthin is widely used as a food and cosmetics additive because of its multiple biological activities. However, astaxanthin produced by Haematococcus pluvialis is generally esterified, and its activity is far less than that of free astaxanthin. Hydrolysis of astaxanthin esters to free astaxanthin by enzymes can overcome the drawbacks of chemical saponification methods. In this paper, a slug-flow microchannel reactor was constructed and tested in enzymatic hydrolysis of astaxanthin esters. The reactor consists of a “T” slug-flow generator, a stainless-steel microchannel, two constant-flow pumps, and a temperature controller. The reactor has the advantages of simple configuration and easy scale-up, and is suitable for two-phase biochemical reactions. Using the microchannel reactor, astaxanthin esters in H. pluvialis oil were efficiently hydrolyzed to free astaxanthin by lipase from Aspergillus niger. After hydrolysis, the content of free astaxanthin in H. pluvialis oil was 18.8 mg/L, 7.83-times higher than that before hydrolysis (2.13 mg/L). The hydrolysis rate reached 75.4 %. These results indicate that the microchannel reactor can be useful for the production of free astaxanthin from its esters.     

Exploitation of olive oil mill wastewater for combined biohydrogen and biopolymers production

The present study aimed to the investigation of the feasibility of the combined biohydrogen and biopolymers production from OMW (Olive oil Mill Wastewater), using a two stage system. H₂ and volatile fatty acids (VFAs) were produced via anaerobic fermentation and subsequently the acidified wastewater was used as substrate for aerobic biodegradable polymer production. Two different bioreactors, one of CSTR type and a SBR were used for the anaerobic and the aerobic process respectively. The anaerobic reactor was operated at different hydraulic retention times (HRTs) with OMW, diluted 1:4 (v/v) with tap water, as feed. The main VFAs produced were acetate, butyrate and propionate, in different ratios depending on the HRT. Valerate, isovalerate and isobutyrate were also detected in small quantities. Selective effluents of the acidogenic/hydrogen producing reactor were subsequently used as feed for the aerobic reactor. The aerobic reactor was inoculated with an enriched PHAs producing bacteria culture, and was operated in sequential cycles of nitrogen offer (growth phase) and nitrogen limitation (PHAs accumulation phase). The operational program of the SBR was determined according to the results from batch test, and its performance was evaluated for a period of 100 days. During the accumulation phase butyrate was consumed preferably, indicating that the dominant PHA produced is polyhydroxybutyrate. The higher yield of PHAs observed was 8.94% (w/w) of dry biomass weight.     

Hydrolysis of triglyceride by the whole cell of Pseudomonas putida 3SK in two-phase batch and continuous reactors systems

Batch and continuous hydrolysis of olive oil in an organic-aqueous two-phase system using the live whole cell of Pseudomonas putida 3SK as a source of a lipase is investigated. The strain was not only fully viable and grown well, but also produced extracellular lipase simultaneously. The degree of hydrolysis, depending on olive oil concentration in the solvents, was maximal at 13.5% (w/v) and decreased with the increase of the substrate concentration. At the optimal condition, a degree of hydrolysis higher than 95% was achieved with 24 h at 30 degrees C when the reaction was carried out in a two-phase batch stirred reactor. For long-term operation a continuous stirred reactor was designed. When the reaction was carried out in a continuous stirred reactor, the degree was hydrolysis reached 86% at a dilution rate of 0.2 h(-1). Satisfactory performance of a two-phase bioreactor was obtained in a long-term continous operation, which lasted for at least 30 days by feeding organic solvent containing olive oil and aqueous media separately. (c) 1994 John Wiley & Sons, Inc.     

Comparison of the emulsion characteristics of Rhodococcus erythropolis and Escherichia coli SOXC-5 cells expressing biodesulfurization genes

Biodesulfurization of fuel oils is a two-phase (oil/water) process which may offer an interesting alternative to conventional hydrodesulfurization due to the mild operating conditions and reaction specificity afforded by the biocatalyst. For biodesulfurization to realize commercial success, a variety of process considerations must be addressed including reaction rate, emulsion formation and breakage, biocatalyst recovery, and both gas and liquid mass transport. This study evaluates emulsion formation and breakage using two biocatalysts with differing hydrophobic characteristics. A Gram-positive (Rhodococcus erythropolis) biocatalyst, expressing the complete 4S desulfurization pathway, and a Gram-negative biocatalyst (Escherichia coli), expressing only the gene for conversion of dibenzothiophene (DBT) to DBT sulfone, are compared relative to their ability to convert DBT and the ease of phase separation as well as biocatalyst recovery following desulfurization.     

Lipase catalysed hydrolysis of ricebran oil by free and immobilised enzyme system in batch stirred reactor

A change of the reaction rate was observed for the lipasecatalysed hydrolysis of ricebran oil in a batch stirred tank reactor using immobilized lipase enzyme as compared to free enzyme. The reactor rate was observed to be controlled mainly by factors like temperature, pH, initial enzyme concentration, initial substrate concentration and initial products concentration.     

Hydrolysis of olive oil catalyzed by surfactant-coated<Emphasis Type="Italic">Candida rugosa</Emphasis> lipase in a hollow fiber membrane reactor

In this study, we invetigated the hydrolysis of olive oil catalyzed by a surfactant-coatedCandida rugosa lipase in a hydrophilic polyacrylonitrile hollow fiber membrane reactor and then compared the results to those using the native lipase. The organic phase was passed through the hollow inner fibers of the reactor and consisted of either the coated lipase and olive oil dissolved in isooctane or the coated lipase dissolved in pure olive oil. The aqueous phase was pumped through the outer space. After 12 h and with conditions of 30°C, 0.12 mg enzyme/mL and 0.62 M olive oil, the substrate conversion of the coated lipase reached 60%. This was twice the conversion for the same amount of native lipase that was pre-immobilized on the membrane surface. When using pure olive oil, after 12 h the substrate conversion of the coated lipase was 50%. which was 1.4 times higher than that of the native lipase.     

A novel process of cyclodextrin production by the use of specific adsorbents: Part II. A new reactor system for selective production of α-cyclodextrin with specific adsorbent

We have developed a novel process of α-cyclodextrin (α-CD) production by using a new adsorbent that is characterized by its exceedingly powerful selectivity for α-CD compared with other CDs. α-CD production was carried out in a closed reactor system that was composed of a main reactor, wherein liquefied starch was converted to CDs by cyclodextrin glucosyltransferase (CGTase: EC 2.4.1.19), and a column packed with the adsorbent. While the reaction mixture was circulated in the system, α-CD was selectively adsorbed in the column and its concentration in the mixture of the main reactor was kept at a low level. This low concentration of α-CD stimulated the conversion of starch to CDs and as a result, enhanced its yield based on added starch. When 8.3 % (w/v) of liquefied starch was used in the reactor system, the yield of α-CD was 22.2% and α-CD occupied 58.7 % of the reaction mixture of total CDs synthesized. Meanwhile, in a batch system without the adsorbent, the yield of α-CD and its fraction were 10.8% and 45.0%, respectively. After the conversion reaction, and following the preliminary washing with water through the column. α-CD was easily eluted with hot water, resulting in a high purity of about 95%.     

Analysis of petroleum biodesulfurization in an airlift bioreactor using response surface methodology

For the first time, growing cells of Gordonia alkanivorans RIPI90A were used for biodesulfurization (BDS) of diesel. This process was carried out in an internal airlift bioreactor. BDS parameters (oil/water phase ratio and initial sulfur concentration) were optimized in flasks using response surface methodology. Predicted results were found to be in good agreement with experimental results. Initial sulfur concentration had a remarkable effect on BDS process. Maximum removal of sulfur (21 mg/l) can be achieved at oil/water phase ratio of 25% (v/v) and initial sulfur concentration of 28 mg/l. Moreover, effect of superficial gas velocity (Ug) and working volume (v) on volumetric gas liquid mass transfer coefficient was studied in an airlift bioreactor for BDS of diesel. The best results were achieved at Ug and v of 2.5l/min and 6.6l, respectively. Subsequently, BDS of diesel was investigated in an airlift bioreactor under optimized conditions. Sulfur reduction after 30 h was 14 mg/l.     

Continuous steroid biotransformations in microchannel reactors

The use of microchannel reactor based technologies within the scope of bioprocesses as process intensification and production platforms is gaining momentum. Such trend can be ascribed a particular set of characteristics of microchannel reactors, namely the enhanced mass and heat transfer, combined with easier handling and smaller volumes required, as compared to traditional reactors. In the present work, a continuous production process of 4-cholesten-3-one by the enzymatic oxidation of cholesterol without the formation of any by-product was assessed. The production was carried out within Y-shaped microchannel reactors in an aqueous-organic two-phase system. Substrate was delivered from the organic phase to aqueous phase containing cholesterol oxidase and the product formed partitions back to the organic phase. The aqueous phase was then forced through a plug-flow reactor, containing immobilized catalase. This step aimed at the reduction of hydrogen peroxide formed as a by-product during cholesterol oxidation, to avoid cholesterol oxidase deactivation due to said by-product. This setup was compared with traditional reactors and modes of operation. The results showed that microchannel reactor geometry outperformed traditional stirred tank and plug-flow reactors reaching similar conversion yields at reduced residence time. Coupling the plug-flow reactor containing catalase enabled aqueous phase reuse with maintenance of 30% catalytic activity of cholesterol oxidase while eliminating hydrogen peroxide. A final production of 36 m of cholestenone was reached after 300 hours of operation.