Enzymatic hydrolysis of cellulose in aqueous two-phase systems. II. Semicontinuous conversion of a model substrate, solka floc BW 200

A model substrate, Solka Floc BW 200, was semicontinuously hydrolyzed in an aqueous two-phase system based on crude dextran and polyethylene glycol over a period of more than 450 h. With an initial concentration of 75 g/L and intermittent addition of cellulose an average concentration of 50 g/L sugar was semicontinuously produced at dilution rates of 0.006-0.012 h(-1). The conversion of substrate varied between 49 and 66%. The enzyme consumption measured as FPU/g reducing sugar (RS) produced could be reduced by a factor two when compared to a batch process since, in the aqueous two phase system investigated, the enzyme could be recycled two times.     

(R)-phenylacetylcarbinol production in aqueous/organic two-phase systems using partially purified pyruvate decarboxylase from Candida utilis

Aqueous/organic two-phase systems have been evaluated for enhanced production of (R)-phenylacetylcarbinol (PAC) from pyruvate and benzaldehyde using partially purified pyruvate decarboxylase (PDC) from Candida utilis. In a solvent screen, octanol was identified as the most suitable solvent for PAC production in the two-phase system in comparison to butanol, pentanol, nonanol, hexane, heptane, octane, nonane, dodecane, methylcyclohexane, methyl tert butyl ether, and toluene. The high partitioning coefficient of the toxic substrate benzaldehyde in octanol allowed delivery of large amounts of benzaldehyde into the aqueous phase at a concentration less than 50 mM. PDC catalyzed the biotransformation of benzaldehyde and pyruvate to PAC in the aqueous phase, and continuous extraction of PAC and byproducts acetoin and acetaldehyde into the octanol phase further minimized enzyme inactivation, and inhibition due to acetaldehyde. For the rapidly stirred two-phase system with a 1:1 phase ratio and 8.5 U/mL carboligase activity, 937 mM (141 g/L) PAC was produced in the octanol phase in 49 h with an additional 127 mM (19 g/L) in the aqueous phase. Similar concentrations of PAC could be produced in the slowly stirred phase separated system at this enzyme level, although at a much slower rate. However at lower enzyme concentration very high specific PAC production (128 mg PAC/U carboligase at 0.9 U/mL) was achieved in the phase separated system, while still reaching final PAC levels of 102 g/L in octanol and 13 g/L in the aqueous phase. By comparison with previously published data by our group for a benzaldehyde emulsion system without octanol (50 g/L PAC, 6 mg PAC/U carboligase), significantly higher PAC concentrations and specific PAC production can be achieved in an octanol/aqueous two-phase system.     

Enhancement of substrate concentration in microbial stereoinversion through one-pot oxidation and reduction by aqueous two-phase system

An extractive biocatalytic method of aqueous two-phase system was employed for stereoinversing (R)-1-phenyl-1,2-ethanediol into (S)-1-phenyl-1,2-ethanediol by Candida parapsilosis CCTCC M203011. It was observed that substrate and product inhibitions in microbial stereoinversion through one-pot oxidation and reduction were removed efficiently by extractive biocatalysis in aqueous two-phase system with PEG 4000/phosphate potassium system, and that the substrate concentration was enhanced from 15 to 30 g/L with product optical purity of 99.02% e.e. and yield of 90% after 60 h. Simultaneously, it was observed that change in cell morphology impedes the further enhancement of substrate concentration in this system but can be reversibly changed after stereoinversion or cultivation in systems without PEG.     

Semicontinuous cellulase production in an aqueous two-phase system with Trichoderma reesei rutgers C30

Cellulases [see 1,4(1,3;1,4)-β-d-glucan 4-glucanohydrolase, EC 3.2.1.4] from Trichoderma reesei, Rutgers C30, can be semicontinuously produced in an aqueous two-phase system composed of dextran and poly(ethylene glycol) using Solka Floc BW 200 as substrate. When substrate was intermittently added along with fresh top phase, which replaced the withdrawn top phase containing the produced enzymes, a yield of 1740 U endo-β-d-glucanase/g cellulose and 59.3 FPU/g cellulose was extracted with the top phase. Without fresh substrate added, a yield of 3920 U endo-β-d-glucanase/g cellulose and 127.7 FPU/g cellulose was extracted after five runs.     

Efficient Repeated Use of Alcohol Dehydrogenase with NAD + Regeneration in an Aqueous-organic Two-phase System

Bioconversion of cinnamyl alcohol to cinnamaldehyde was carried out in an aqueous-organic two-phase reaction system by the repeated use of horse liver alcohol dehydrogenase (HLADH) and NAD + with coenzyme regeneration. Both HLADH and the coenzyme were efficiently entrapped in the aqueous phase, while the substrate was supplied successively from the organic phase and the product was accumulated in the organic phase. Optimum conditions for cinnamaldehyde production in the aqueous-organic two-phase system were also examined, including substrate concentration, pH, and organic solvent type. Under suitable conditions, both HLADH and NAD + in the aqueous-organic two-phase system could be reused, and NAD + cycling numbers of 3040 were obtained after repeated operation for 40 &#117 h.     

Efficient Repeated Use of Alcohol Dehydrogenase with NAD + Regeneration in an Aqueous-organic Two-phase System

Bioconversion of cinnamyl alcohol to cinnamaldehyde was carried out in an aqueous-organic two-phase reaction system by the repeated use of horse liver alcohol dehydrogenase (HLADH) and NAD + with coenzyme regeneration. Both HLADH and the coenzyme were efficiently entrapped in the aqueous phase, while the substrate was supplied successively from the organic phase and the product was accumulated in the organic phase. Optimum conditions for cinnamaldehyde production in the aqueous-organic two-phase system were also examined, including substrate concentration, pH, and organic solvent type. Under suitable conditions, both HLADH and NAD + in the aqueous-organic two-phase system could be reused, and NAD + cycling numbers of 3040 were obtained after repeated operation for 40 λh.     

Extractive bioconversion of 2-phenylethanol from L-phenylalanine by Saccharomyces cerevisiae

The bioconversion of L-phenylalanine (L-Phe) to 2-phenylethanol (PEA) by the yeast Saccharomyces cerevisiae is limited by the toxicity of the product. PEA extraction by a separate organic phase in the fermenter is the ideal in situ product recovery (ISPR) technique to enhance productivity. Oleic acid was chosen as organic phase for two-phase fed-batch cultures, although it interfered to some extent with yeast viability. There was a synergistic inhibitory impact toward S. cerevisiae in the presence of PEA, and therefore a maximal PEA concentration in the aqueous phase of only 2.1 g/L was achieved, compared to 3.8 g/L for a normal fed-batch culture. However, the overall PEA concentration in the fermenter was increased to 12.6 g/L, because the PEA concentration in the oleic phase attained a value of 24 g/L. Thus, an average volumetric PEA production rate of 0.26 g L(-1) h(-1) and a maximal volumetric PEA production rate of 0.47 g L(-1) h(-1) were achieved in the two-phase fed-batch culture. As ethanol inhibition had to be avoided, the production rates were limited by the intrinsic oxidative capacity of S. cerevisiae. In addition, the high viscosity of the two-phase system lowered the k(l)a, and therefore also the productivity. Thus, if a specific ISPR technique is planned, it consequently has to be remembered that the productivity of this bioconversion process is also quickly limited by the k(l)a of the fermenter at high cell densities.     

Biodegradation of phenol at high initial concentrations in two-phase partitioning batch and fed-batch bioreactors

A two-phase organic-aqueous system was used to degrade phenol in both batch and fed-batch culture. The solvent, which contained the phenol and partitioned it into the aqueous phase, was systematically selected based on volatility, solubility in the aqueous phase, partition coefficient for phenol, biocompatibility, and cost. The two-phase partitioning bioreactor used 500 mL of 2-undecanone loaded with high concentrations of phenol to deliver the xenobiotic to Pseudomonas putida ATCC 11172 in the 1-L aqueous phase, at subinhibitory levels. The initial concentrations of phenol selected for the aqueous phase were predicted using the experimentally determined partition coefficient for this ternary system of 47.6. This system was initially observed to degrade 4 g of phenol in just over 48 h in batch culture. Further loading of the organic phase in subsequent experiments demonstrated that the system was capable of degrading 10 g of phenol to completion in approximately 72 h. The higher levels of phenol in the system caused a modest increase in the duration of the lag phase, but did not lead to complete inhibition or cell death. The use of a fed-batch approach allowed the system to ultimately consume 28 g of phenol in approximately 165 h, without experiencing substrate toxicity. In this system, phenol delivery to the aqueous phase is demand based, and is directly related to the metabolic activity of the cells. This system permits high loading of phenol without the corresponding substrate inhibition commonly seen in conventional bioreactors. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 55: 155-162, 1997.     

Production of a key chiral intermediate of Betahistine with a newly isolated Kluyveromyces sp. in an aqueous two-phase system

(S)-(4-Chlorophenyl)-(pyridin-2-yl)methanol [(S)-CPMA] is an important chiral intermediate of anti-allergic drug Betahistine. Carbonyl reductase-producing microorganisms were isolated from soil samples for the stereoselective reduction of (4-chlorophenyl)-(pyridin-2-yl)methanone (CPMK) to (S)-CPMA. Among over 400 microorganisms isolated, one strain exhibiting the highest activity was selected and identified as Kluyveromyces sp. After optimization, the biotransformation reaction catalyzed by Kluyveromyces sp. CCTCC M2011385 whole-cell gave product (S)-CPMA in 81.5% ee and 87.8% yield at substrate concentration of 2 g/L in aqueous phase. Using an aqueous two-phase system (ATPs) consisted of PEG4000 (20%, w/w) and Na₂HPO₄ (14%, w/w), the product reached 86.7% ee and 92.1% yield at a higher substrate concentration of 6 g/L. The substrate tolerance and biocompatibility of microbial cells are greatly improved in ATPs by accumulating substrate/product in the upper PEG solution. This study, for the first time, reports the production of (S)-CPMA catalyzed by microbial cells.     

Importance of solute partitioning in biphasic oxidation of benzyl alcohol by free and immobilized whole cells of pichia pastoris

Using free and immobilized whole cells of Pichia pastoris, the biocatalytic oxidation of benzyl alcohol was investigated in different two-phase systems. This reaction was strongly influenced by both the substrate and product inhibitions, and the production rate of benzaldehyde in the aqueous system became maximum at the initial substrate concentration of ca. 29 g/L with the aldehyde formation less than 4 to 5 g/L even after a longer reaction period. The reaction rates in the two-liquid phase systems were predominantly determined by the partitioning behaviors of the substrate and product between the two phases rather than by enzyme deactivation by the organic solvents. In the two-liquid phase systems, consequently, the organic solvent acted as a reservior to reduce these inhibitory effects, and it was essential to select the organic solvent providing the optimal partitioning of the substrate into the aqueous phase as well as the preferential extraction of the product into the organic phase. The whole cells immobilized in a mixed matrix composed of silicone polymer [>50% (v/v)] and Ca alginate gel (<50%) worked well in the xylene and decane media, providing comparable activities with the free cells. The production rate of aldehyde was also influenced by the solute partitioning into the hydrophilic alginate phase where the cells existed. (c) 1994 John Wiley & Sons, Inc.     

Enhanced production of lactic acid through the use of a novel aqueous two-phase system as an extractive fermentation system

 In order to enhance the productivity of lactic acid and reduce the end-product inhibition of fermentation, the partitioning and growth of four different strains of lactic acid bacteria in three different aqueous two-phase systems were studied. Polyethyleneglycol/ dextran, polyethyleneglycol/hydroxypropyl starch polymer (HPS), and a random copolymer of ethylene oxide and propylene oxide (EO-PO)/HPS were used as polymer systems. One strain each of Lactococcus lactis subsp. lactis and of Lactobacillus delbrueckii subsp. delbrueckii partitioned completely to the interface and bottom phase in two-phase systems with low polymer concentrations of EO-PO/HPS100 and EO-PO/ HPS200. The growth and production of lactic acid by two of three L. lactis strains in a two-phase system with 5.5% (w/w) EO-PO and 12.0% (w/w) HPS100 were reduced by less than 10% compared with a reference fermentation in a normal growth medium. The viability of L. lactis subsp. lactis ATCC 19435 was maintained for at least 50 h and with four top-phase replacements during extractive fermentation in the EO-PO/HPS100 system. Moreover, when cell density reached the stationary phase in the first extractive fermentation, the lactate production in this aqueous two-phase system was maintained. Received: 2 October 1995/Received revision: 16 January 1996/Accepted: 22 January 1996     

Purification of lipase produced by a new source of Bacillus in submerged fermentation using an aqueous two-phase system

This work discusses the application of an aqueous two-phase system for the purification of lipases produced by Bacillus sp. ITP-001 using polyethylene glycol (PEG) and potassium phosphate. In the first step, the protein content was precipitated with ammonium sulphate (80% saturation). The enzyme remained in the aqueous solution and was dialyzed against ultra-pure water for 18 h and used to prepare an aqueous two-phase system (PEG/potassium phosphate). The use of different molecular weights of PEG to purify the lipase was investigated; the best purification factor (PF) was obtained using PEG 20,000g/mol, however PEG 8000 was used in the next tests due to lower viscosity. The influence of PEG and potassium phosphate concentrations on the enzyme purification was then studied: the highest FP was obtained with 20% of PEG and 18% of potassium phosphate. NaCl was added to increase the hydrophobicity between the phases, and also increased the purification factor. The pH value and temperature affected the enzyme partitioning, with the best purifying conditions achieved at pH 6.0 and 4°C. The molecular mass of the purified enzyme was determined to be approximately 54 kDa by SDS-PAGE. According to the results the best combination for purifying the enzyme is PEG 8000g/mol and potassium phosphate (20/18%) with 6% of NaCl at pH 6.0 and 4°C (201.53 fold). The partitioning process of lipase is governed by the entropy contribution.     

Extractive lactic acid fermentation in poly (ethyleneimine)-based aqueous two-phase system

The potential of an aqueous two-phase system composed of a polycation, poly(ethyleneimine) (PEI), and an uncharged polymer, (hydroxyethyl) cellulose (HEC), for extractive lactic acid fermentation was tested. Batch fermentation with 20 g/L glucose in two-phase medium using Lactococcus lactis without external pH control resulted in 3-4 times higher amount of lactate and biomass produced as compared to that in a conventional one-phase medium. Lactic acid was preferentially partitioned to the PEI-rich bottom phase. However, the cells which favored the HEC-rich top phase in a fresh two-phase medium were partitioned to a significant extent to the bottom phase after fermentation. Addition of phosphate buffer or pH adjustment to 6.5 after fermentation caused fewer cells to move to the bottom phase. With external pH control, fermentation in normal and two-phase medium showed no marked differences in glucose consumption and lactic acid yield, except that about 1.3 times higher cell density was obtained in the two-phase broth, especially at initial glucose concentrations of 50-100 g/L. Use of higher concentration of phosphate during batch fermentation in the two-phase medium with 50 g/L sugar provided a 15% higher yield of lactic acid, but the growth rate of cells was nearly half of the normal, thus affecting the productivity. Continuous fermentation with twice the normal phosphate concentration resulted in higher cell density, product yield, and productivity in two-phase medium than in monophasic medium. (c) 1996 John Wiley & Sons, Inc.     

Pilot scale processing of detergent-based aqueous two-phase systems

Detergent based aqueous two-phase systems have several specific properties, e.g., extreme small density differences between the two liquid phases (0.003-0.005 g/cm(3)), low interfacial tensions (5-10 muN/m) and complex rheological behavior of the product containing detergent-rich phase, which make processing difficult. We describe the successful separation of these aqueous two-phase systems in the pilot scale (1-20 kg) in the presence and absence of microbial cells, either by settling under gravity or in centrifugal separators. The performance of self-desludging liquid-liquid separators and of a nozzle separator was analyzed in detail to judge large scale application. With a feed rate of 16 L/h, stable operation was possible in the desludging machine. Up to 56 L/h could be processed with very close control of the hydrodynamic balance. In a small nozzle separator, feed rates of 90 L/h could be realized, but the purity of the separated phases and the yield of the top phase was slightly lower than in the liquid-liquid separator. The presence of surface-active components in the feed may alter the separation characteristics of the phase systems significantly. (c) 1997 John Wiley & Sons, Inc. Biotechnol Bioeng 55: 339-347, 1997.     

Transient performance of two-phase partitioning bioreactors treating a toluene contaminated gas stream

Two-phase partitioning bioreactors (TPPBs) consist of a cell-containing aqueous phase and an immiscible organic phase that sequesters and delivers toxic substrates to cells based on equilibrium partitioning. The immiscible organic phase, which acts as a buffer for inhibitory substrate loadings, makes it possible for TPPBs to handle high volatile organic compound (VOC) loadings, and in this study the performance of liquid n-hexadecane and solid styrene butadiene (SB) polymer beads used as partitioning phases were compared to a single aqueous phase system while treating transient loadings of a toluene contaminated air stream by Achromobacter xylosoxidans Y234. The TPPBs operated as well-mixed stirred tanks, with total working volumes of 3 L (3 L aqueous for the single-phase system, 2 L aqueous and 1 L n-hexadecane for the solvent system, and 2.518 L aqueous volume and 500 g of SB beads for the polymer system). Two 60-min step changes (7 and 17 times the nominal loading rates, termed "small" and "large" steps, respectively) were imposed on the systems and the performance was characterized by the overall removal efficiencies, instantaneous removal efficiency recovery times (above 95% removal), and dissolved oxygen recovery times. For the small steps, with a nominal loading of 343 g/m3/h increasing to 2,400 g/m3/h, the TPPB system using n-hexadecane as the second phase performed best, removing 97% of the toluene fed to the system compared with 90% for the polymer beads system and only 69% for the single-phase system. The imposed large transient gave similar results, although the impact of the presence of a second sequestering phase was more pronounced, with the n-hexadecane system maintaining much reduced aqueous toluene concentrations leading to significantly improved performance. This investigation also showed that the presence of both n-hexadecane and SB beads improved the oxygen transfer within the systems.     

Expanded application of a two-phase partitioning bioreactor through strain development and new feeding strategies

This research demonstrated the microbial treatment of concentrated phenol wastes using a two-phase partitioning bioreactor (TPPB). TPPBs are characterized by a cell-containing aqueous phase and an immiscible and biocompatible organic phase that partitions toxic substrates to the cells on the basis of their metabolic demand and the thermodynamic equilibrium of the system. Process limitations imposed by the capability of wild-type Pseudomonas putida ATCC 11172 to utilize long chain alcohols were addressed by strain modification (transposon mutagenesis) to eliminate this undesirable biochemical characteristic, enabling use of a range of previously bioavailable organics as delivery solvents. Degradation of phenol in a system with the modified strain as catalyst and industrial grade Adol 85 NF (primarily oleyl alcohol) as the solvent was demonstrated, with the system ultimately degrading 36 g of phenol within 38 h. Volumetric phenol consumption rates by wild type P. putida ATCC 11172 and the genetically modified derivative revealed equivalent phenol degrading capabilities (0.49 g/L x h vs 0.47 g/L x h respectively, in paired fermentations), with the latter presenting a more efficient remediation option due to decreased solvent losses arising from the modified strain's forced inability to consume the delivery solvent as a substrate. Two feeding strategies and system configurations were evaluated to expand practical applications of TPPB technology. The ability to operate with a lower solvent ratio over extended periods revealed potential for long-term application of TPPB to the treatment of large masses of phenol while minimizing solvent costs. Repeated recovery of 99% of phenol from concentrated phenol solutions and subsequent treatment within a TPPB scheme demonstrated applicability of the approach to the remediation of highly contaminated "effluents" as well as large masses of bulk phenol. Operation of the TPPB system in a dispersed manner, rather than as two distinct phases, resulted in volumetric consumption rates similar to those previously achieved only in systems operated with enriched air.     

Development of a novel bioreactor system for treatment of gaseous benzene

A novel, continuous bioreactor system combining a bubble column (absorption section) and a two-phase bioreactor (degradation section) has been designed to treat a gas stream containing benzene. The bubble column contained hexadecane as an absorbent for benzene, and was systemically chosen considering physical, biological, environmental, operational, and economic factors. This solvent has infinite solubility for benzene and very low volatility. After absorbing benzene in the bubble column, the hexadecane served as the organic phase of the two-phase partitioning bioreactor, transferring benzene into the aqueous phase where it was degraded by Alcaligenes xylosoxidans Y234. The hexadecane was then continuously recirculated back to the absorber section for the removal of additional benzene. All mass transfer and biodegradation characteristics in this system were investigated prior to operation of the integrated unit, and these included: the mass transfer rate of benzene in the absorption column; the mass transfer rate of benzene from the organic phase into the aqueous phase in the two-phase bioreactor; the stripping rate of benzene out of the two-phase bioreactor, etc. All of these parameters were incorporated into model equations, which were used to investigate the effects of operating conditions on the performance of the system. Finally, two experiments were conducted to show the feasibility of this system. Based on an aqueous bioreactor volume of 1 L, when the inlet gas flow and gaseous benzene concentration were 120 L/h and 4.2 mg/L, respectively, the benzene removal efficiency was 75% at steady state. This process is believed to be very practical for the treatment of high concentrations of gaseous pollutants, and represents an alternative to the use of biofilters.     

Biodegradation of toluene at high initial concentration in an organic–aqueous phase bioprocess with nitrate respiration

An aerobic organic–aqueous system with forced aeration was shown to be inefficient in preventing significant volatile aromatic compounds loss in gassed systems since air sparging in n-hexadecane under abiotic conditions could reduce the toluene concentration from 2.1 g/L to about 0.5 g/L in 3 days with a gassing rate of 1VVM at 20 °C. However, the presence of such an organic phase was found to significantly reduce substrate loss in aerobic conditions in comparison to pure aqueous systems. It was thus decided to develop a new bioprocess based on an anaerobic microbial system operated in an organic–aqueous phase with nitrate respiration. The denitrifying bacterium used, Thauera aromatica K172, was produced by cultivation on sodium benzoate as carbon source under anaerobic conditions. This cultivated biomass (1.5 g/L) was shown to retain its ability to efficiently metabolize toluene in a biphasic medium without any significant loss of organic compound in the gas phase. Toluene biodegradation was thus performed in a biphasic system using a fed-batch technique involving sequential adding of both toluene and nitrate. The reaction rate with an initial concentration of toluene close to 14.5 g/L in hexadecane was found to be close to 0.5 g/L day and the molar stoichiometry of solute metabolization to nitrate reduction was close to 1:6. This work demonstrated that the denitrifying bacteria could efficiently degrade toluene in hexadecane–aqueous phase systems in which toxic compound release in the environment was prevented.     

Production of alkaline protease by Bacillus licheniformis in an aqueous two-phase system

Alkaline protease production by Bacillus licheniformis was studied in an aqueous two-phase system composed of 5% (w/w) polyethylene glycol 6000 (PEG 6000) and 5% (w/w) dextran T500. The top phase was continuous and rich in PEG while the bottom phase was dispersed and rich in dextran. The cells were retained in the bottom phase and at the interface. The two-phase system produced less enzyme in total amount than the control in the early phase, but after 50 h the enzyme produced in the control system decreased while the aqueous two-phase system continued its production and finally the total enzyme activity reached 1.3 times that of the control culture. In order to improve the productivity of protease, repeated batch cultivation were successfully carried out four times by optimizing the top phas composition of freshly added media, which resulted in 13.8, 35.9, 27.8 and 34.7 units ml⁻¹ h⁻¹ of protease based on the amounts of replaced top phases, respectively.     

Hydrogen sulfide removal by immobilized Thiobacillus novellas on SiO2 in a fluidized bed reactor

The removal of hydrogen sulfide (H2S) from aqueous media was investigated using Thiobacillus novellas cells immobilized on a SiO2 carrier (biosand). The optimal growth conditions for the bacterial strain were 30 degrees C and initial pH of 7.0. The main product of hydrogen sulfide oxidation by T. novellus was identified as the sulfate ion. A removal efficiency of 98% was maintained in the three-phase fluidized-bed reactor, whereas the efficiency was reduced to 90% for the two-phase fluidized-bed reactor and 68% for the two-phase reactor without cells. The maximum gas removal capacity for the system was 254 g H2S/m3/h when the inlet H2S loading was 300 g/m3/h (1,500 ppm). Stable operation of the immobilized reactor was possible for 20 days with the inlet H2S concentration held to 1,100 ppm. The fluidized bed bioreactor appeared to be an effective means for controlling hydrogen sulfide emissions.