Purification of docosahexaenoic acid ethyl ester using a silver-ion-immobilized porous hollow-fiber membrane module

Docosahexaenoic acid ethyl ester (DHA-Et) was purified by adsorption on Ag-ion-immobilized membranes via selective interaction between silver ion and carbon-carbon double bonds of DHA-Et. Silver ions were immobilized onto sulfonic-acid-group-containing porous hollow-fiber membranes at an Ag ion density of 1.4 mol/kg of membrane, and 30 membranes were housed in one module (inner diameter = 18 mm and effective length = 80 mm). The adsorption isotherms of DHA-Et in various organic solvents revealed that DHA-Et was adsorbed on the immobilized Ag ions with a DHA-Et/Ag ion molar binding ratio of 1/5 in methanol, and that acetonitrile was the solvent of choice for the elution of the adsorbed DHA-Et. Permeation of bonito oil ethyl ester solution in methanol through the Ag-ion-immobilized hollow-fiber membrane module demonstrated that the displacement adsorption of other lower unsaturated fatty-acid ethyl esters by DHA-Et proceeded along the membrane thickness. The purity of DHA-Et was improved to 99 wt % by permeating first bonito oil ethyl ester containing 95 wt % DHA-Et and then acetonitrile through the module.     

Protein binding to amphoteric polymer brushes grafted onto a porous hollow-fiber membrane

Three kinds of ampholites, i.e., 3-aminopropionic acid (NH2C2H4COOH), (2-aminoethyl)phosphonic acid (NH2C2H4PO3H2), and 2-aminoethane-1-sulfonic acid (NH2C2H4SO3H), were introduced into an epoxy group-containing polymer brush grafted onto a porous hollow-fiber membrane with a porosity of 70% and pore size of 0.36 microm. The amphoteric group density of the hollow-fiber ranged from 0.50 to 0.72 mmol/g. Three kinds of proteins, i.e., lactoferrin (Lf), cytochrome c (Cyt c), and lysozyme (Ly), were captured by the amphoteric polymer brush during the permeation of the protein solution across the ampholite-immobilized porous hollow-fiber membrane. Multilayer binding of the protein to the amphoteric polymer brush, with a degree of multilayer binding of 3.3, 8.6, and 15 for Lf, Cyt c, and Ly, respectively, with the (2-aminoethyl)phosphonic acid-immobilized porous hollow-fiber membrane, was demonstrated with a negligible diffusional mass-transfer resistance of the protein to the ampholite immobilized. The 2-aminoethane-1-sulfonic acid-immobilized porous hollow-fiber membrane exhibited the lowest initial flux of the protein solution, 0.41 m/h at a transmembrane pressure of 0.1 MPa and 298 K, and the highest equilibrium binding capacity of the protein, e.g., 130 mg/g for lysozyme. Extension and shrinkage of the amphoteric polymer brushes were observed during the binding and elution of the proteins.     

Production of tomato flavor volatiles from a crude enzyme preparation using a hollow-fiber reactor

In recent years there has been an increase in the interest in the production of compounds by isolation from natural sources or through processes that can be deemed "natural". This is of particular interest in the food and beverage industry for flavors and aromas. Hexanal, organoleptically known to possess "green character", is of considerable commercial interest. The objective of this study was to determine if the enzyme template known to be responsible for the synthesis of hexanal from linoleic acid (18:2) in tomato fruits could be harnessed using a hollow-fiber reactor. A hollow-fiber reactor system was set up and consisted of a XAMPLER ultrafiltration module coupled to a reservoir. The enzyme template was extracted from ripe tomato fruits and processed through an ultrafiltration unit (NMWC of 100 kDa) to produce a retentate enriched in soluble and membrane-associated lipoxygenase (LOX) and hydroperoxide lyase (HPL). This extract was recirculated through the lumen of the hollow-fiber ultrafiltration unit with the addition of substrate in the form of linoleic acid, with buffer addition to the reaction flask to maintain a constant retentate volume. Product formation was measured in the permeate using solid phase microextraction (SPME) developed for this system. At exogenous substrate concentrations of 16 mM and a transmembrane pressure of 70 kPa, hexanal production rates are in the order of 5.1 microg/min. Addition of Triton X-100 resulted in membrane fouling and reduced flux. The reactor system has been run for periods of up to 1 week and has been shown to be stable over this period.     

Production of high-quality particulate methane monooxygenase in high yields from Methylococcus capsulatus (bath) with a hollow-fiber membrane bioreactor

In order to obtain particulate methane monooxygenase (pMMO)-enriched membranes from Methylococcus capsulatus (Bath) with high activity and in high yields, we devised a method to process cell growth in a fermentor adapted with a hollow-fiber bioreactor that allows easy control and quantitative adjustment of the copper ion concentration in NMS medium over the time course of cell culture. This technical improvement in the method for culturing bacterial cells allowed us to study the effects of copper ion concentration in the growth medium on the copper content in the membranes, as well as the specific activity of the enzyme. The optimal copper concentration in the growth medium was found to be 30 to 35 micro M. Under these conditions, the pMMO is highly expressed, accounting for 80% of the total cytoplasmic membrane proteins and having a specific activity as high as 88.9 nmol of propylene oxide/min/mg of protein with NADH as the reductant. The copper stoichiometry is approximately 13 atoms per pMMO molecule. Analysis of other metal contents provided no evidence of zinc, and only traces of iron were present in the pMMO-enriched membranes. Further purification by membrane solubilization in dodecyl beta-D-maltoside followed by fractionation of the protein-detergent complexes according to molecular size by gel filtration chromatography resulted in a good yield of the pMMO-detergent complex and a high level of homogeneity. The pMMO-detergent complex isolated in this way had a molecular mass of 220 kDa and consisted of an alphabetagamma protein monomer encapsulated in a micelle consisting of ca. 240 detergent molecules. The enzyme is a copper protein containing 13.6 mol of copper/mol of pMMO and essentially no iron (ratio of copper to iron, 80:1). Both the detergent-solubilized membranes and the purified pMMO-detergent complex exhibited reasonable, if not excellent, specific activity. Finally, our ability to control the level of expression of the pMMO allowed us to clarify the sensitivity of the enzyme to NADH and duroquinol, the two common reductants used to assay the enzyme.     

Phenol biodegradation in hybrid hollow-fiber membrane bioreactors

Hollow-fiber membrane bioreactors were developed with granular activated carbon (GAC) for the biodegradation of phenol using Pseudomonas putida. Hollow fibers showed similar structure with/without GAC incorporated; while GAC hollow fiber had a stronger phenol adsorption capacity. In batch biotransformation experiments, complete depletion of 1000 mg phenol l⁻¹ (at which concentration free cells cannot grow) was accomplished in the reactor within 18 h in the hybrid bioreactor, comparing with 23 h in the GAC free bioreactor. Desorption and bioregeneration of the hollow-fiber membrane were believed to be the key for the enhancement of bioreactor performance. At continuous running, the GAC bioreactor showed its superiority over the GAC free bioreactor during start-up and elevated loading phase. More than 90% of the phenol was transformed in the GAC bioreactor when the phenol loading was <24 mg h⁻¹. The better bioreactor performance may be due to the enhanced mass transportation and adsorption capacity with the incorporation of GAC.     

Liquid chromatographic determination of penicillins by postcolumn alkaline degradation using a hollow-fiber membrane reactor

A high-performance liquid chromatographic method using a hollow-fiber membrane reactor is described for the determination of penicillins. This method involves separation of penicillins on a C18 column, postcolumn reaction with sodium hydroxide and mercury (II) chloride introduced into the main flow stream using sulfonated hollow-fiber membrane reactors immersed in each solution (4 M sodium hydroxide and 3 X 10(-2) M mercury (II) chloride plus 10(-2) M nitric acid), and detection at 290 nm based on the uv absorbance of the degradation products. At penicillin concentrations of 5 micrograms/ml, within- and between-run precisions (relative standard deviation) were 0.24-2.39 and 1.19-4.13%, respectively. The detection limits of the proposed method were 1-5 ng at a signal-to-noise ratio of 3. The method was applied to assays of ampicillin and its metabolites in human serum and urine.     

Mathematical model of microporous hollow-fiber membrane extractive fermentor

A mathematical model is presented for a microporous hollow-fiber membrane extractive fermentor (HFEF). The model is based on the continuous flow of the aqueous nutrient phase and cells through the shell space of the fermentor where the fermentation reaction occurs. The product diffuses from the shell space through the hollow-fiber membrane where it is continuously removed by solvent flowing concurrently through the fiber lumen. Results for ethanol production show that the HFEF has a volumetric productivity significantly higher than that possible using conventional methods. The model predicts the existence of an optimum volume fraction of hollow fibers in the fermentor that maximizes the total volumetric productivity. This optimum is the result of a classic trade-off between the volume fraction of the fermentor required for fermentation and that required for efficient removal of the ethanol product to minimize product inhibition.     

Development of a novel membrane aerated hollow-fiber microbioreactor

A new challenge in biotechnological processes is the development of flexible bioprocessing platforms, allowing strain selection, facilitating scale-up and integrating separation steps. Miniaturization of such a cultivation system allows parallel use and the saving of resources but makes the supply of oxygen to the cells difficult. In this work we present a membrane aerated hollow-fiber microbioreactor (HFMBR) which consists of an acrylic glass module equipped with two different types of membrane fibers. Fibers of polyethersulfone and polyvinyldifluoride were used for substrate and oxygen supply, respectively. Cultivation of E. coli as model organism and production of His-tagged GFP were carried out in the extracapillary space of the membrane aerated HFMBR and compared with cultivations in shaking flask which are commonly used for screening experiments. The measurement of the oxygen transfer capacity and the online monitoring of the dissolved oxygen during the cultivation were performed using a fiber optic oxygen sensor. Online measurement of the optical density was also integrated to the bioreactor. Due to efficient oxygen transfer, a better cell growth than in the shaking flask experiments was achieved, while no negative influence on the GFP productivity was observed in the membrane aerated bioreactor. Thus the feasibility of a future integrated downstreaming could also be demonstrated.     

A hollow-fiber membrane bioreactor for the removal of trichloroethylene from the vapor phase

A hollow-fiber membrane bioreactor was used to separate trichloroethylene (TCE) from a gaseous waste stream with subsequent cometabolic biodegradation by a pure culture of Methylosinus trichosporium OB3b PP358. The two-stage bioreactor system was successfully operated for 20 days. PP358 was grown in a continuous-flow chemostat and circulated through the fiber lumen of a hollow-fiber membrane module (HFMM), while TCE contaminated air (141 to 191 microg/L) was pumped through the HFMM shell. Between 54% -84% TCE transfer and 92%-96% TCE cometabolism were obtained in the HFMM reactor loop. Short shell-residence times, 1.6 to 5.0 minutes, demonstrated quick throughput of TCE contaminated air. Best-fit computer modeling of the biological experiments estimated mass transfer coefficients between 2.0 x 10(-3) cm/min and 5.6 x 10(-3) cm/min. The average pseudo-first-order biodegradation rate constant for the biological experiments was 0.46 L/mg TSS/d. These results demonstrate that the hollow-fiber membrane bioreactor represents an attractive technology for the bioremediation of gaseous waste streams.     

Removal of endotoxin from water by microfiltration through a microporous polyethylene hollow-fiber membrane

The microporous polyethylene hollow-fiber membrane has a unique microfibrile structure throughout its depth and has been found to possess the functions of filtration and adsorption of endotoxin in water. The membrane has a maximum pore diameter of approximately 0.04 micron, a diameter which is within the range of microfiltration. Approximately 10 and 20% of the endotoxin in tap water and subterranean water, respectively, was smaller than 0.025 micron. Endotoxin in these water sources was efficiently removed by the microporous polyethylene hollow-fiber membrane. Escherichia coli O113 culture broth contained 26.4% of endotoxin smaller than 0.025 micron which was also removed. Endotoxin was leaked into the filtrate only when endotoxin samples were successively passed through the membrane. These results indicate that endotoxin smaller than the pore size of the membrane was adsorbed and then leaked into the filtrate because of a reduction in binding sites. Dissociation of 3H-labeled endotoxin from the membrane was performed, resulting in the removal of endotoxin associated with the membrane by alcoholic alkali at 78% efficiency.     

Production of cycloisomaltooligosaccharides from dextran using enzyme immobilized in multilayers onto porous membranes

Anion-exchange porous hollow-fiber membranes with a thickness of about 1.2 mm and a pore size of about 0.30 microm were used as a supporting matrix to immobilize cycloisomaltooligosaccharide glucanotransferase (CITase). CITase was immobilized to the membrane via anion-exchange adsorption and by subsequent enzymatic cross-linking with transglutaminase, the amount of which ranged from 3 to 110 mg per gram of the membrane. The degree of enzyme multilayer binding was equivalent to 0.3-9.8. Dextran, as the substrate, was converted into seven- to nine-glucose-membered cycloisomaltooligosaccharides (CI-7, -8, and -9) at a maximum yield of 28% in weight at a space velocity of 10 per hour during the permeation of 2.0% (w/w) dextran solution across the CITase-immobilized porous hollow-fiber membrane. The yield of CIs increased with increasing degree of CITase multilayering.     

Ethanol stripping by pervaporation using porous PTFE membrane

In a shell-and-tube type of module containing either porous or nonporous tubular membranes, the sweeping action of a flow inert gas in the shell side was used to strip ethanol from an aqueous ethanol solution flowing countercurrently in the tube side. A calculation of the overall mass transfer coefficient, K_G, of the membrane used was made for this system. In ethanol stripping tests using a module containing polytetrafluoreethylene (PTFE) tubular membranes, the K_G was found to be more affected by the liquid flow rate than the gas flow rate. Moreover, the gas side mass transfer coefficient, k_G, was estimated to be about 5×10⁻⁵ mol/cm²·s·atm. The liquid side mass transfer coefficient, k_L, on the other hand, was found to increase linearly with the linear velocity of the aqueous solution. Also, at an average solution temperature range of 21 to 32°C, no significant change in the K_G was observed. Comparison of the K_G of different tubular membranes revealed that the K_G of the PTFE membrane was higher than that of polypropylene or silicone membranes under the given experimental conditions.     

Removal of endotoxin from water by microfiltration through a microporous polyethylene hollow-fiber membrane.

The microporous polyethylene hollow-fiber membrane has a unique microfibrile structure throughout its depth and has been found to possess the functions of filtration and adsorption of endotoxin in water. The membrane has a maximum pore diameter of approximately 0.04 micron, a diameter which is within the range of microfiltration. Approximately 10 and 20% of the endotoxin in tap water and subterranean water, respectively, was smaller than 0.025 micron. Endotoxin in these water sources was efficiently removed by the microporous polyethylene hollow-fiber membrane. Escherichia coli O113 culture broth contained 26.4% of endotoxin smaller than 0.025 micron which was also removed. Endotoxin was leaked into the filtrate only when endotoxin samples were successively passed through the membrane. These results indicate that endotoxin smaller than the pore size of the membrane was adsorbed and then leaked into the filtrate because of a reduction in binding sites. Dissociation of 3H-labeled endotoxin from the membrane was performed, resulting in the removal of endotoxin associated with the membrane by alcoholic alkali at 78% efficiency.     

The gelatin sponge-chorioallantoic membrane assay

Here we present a method for the quantification of angiogenesis and antiangiogenesis in the chick embryo chorioallantoic membrane (CAM) based on the implantation of a gelatin sponge on the top of the growing CAM on day 8 of development. After implantation, the sponge is treated with a stimulator of blood vessel formation in the absence or presence of an angiogenesis inhibitor. On day 12, blood vessels that are growing into the sponge are counted at macroscopic and microscopic levels. The estimated timeline for carrying out this protocol is 10 d. The presence of a vascular network in the CAM requires a careful analysis to distinguish new capillaries from pre-existing ones. This limitation does not occur in the avascular cornea assay, which may also take advantage of different genetic backgrounds when carried out in transgenic or knockout mice. Nevertheless, the gelatin sponge-CAM assay is simple, inexpensive and suitable for large-scale screening.     

Lipase kinetics: hydrolysis of triacetin by lipase from Candida cylindracea in a hollow-fiber membrane reactor

The aptitude of a hollow-fiber membrane reactor to determine lipase kinetics was investigated using the hydrolysis of triacetin catalyzed by lipase from Canadida cylindracea as a model system. The binding of the lipase to the membrane appears not to be very specific (surface adsorption), and probably its conformation is hardly altered by immobilization, resulting in an activity comparable to that of the enzyme in its native form. The reaction kinetics defined on the membrane surface area were found to obey Michaelis-Menten kinetics. The specific activity of the lipase in the membrane reactor was found to be significantly higher than in an emulsion reactor. The activity and stability of the enzyme immobilized on a hydrophilic membrane surface seem not to be influenced significantly by the choice of the membrane material. The hollow-fiber membrane reactor is a suitable tool to assess lipase kinetics in a fast and convenient way.     

Production of membrane proteins using cell-free expression systems

Production of membrane proteins (MPs) is a challenging task as their hydrophobic nature and their specific requirements in cellular expression systems frequently prevent an efficient synthesis. Cell-free (CF) expression systems have been developed in recent times as promising tools by offering completely new approaches to synthesize MPs directly into artificial hydrophobic environments. A considerable variety of CF produced MPs has been characterized by functional and structural approaches and the high success rates and the rapidly accumulating data on quality and expression efficiencies increasingly attract attention. In addition, CF expression is a highly dynamic and versatile technique and new modifications for improved performance as well as for extended applications for the labeling, throughput expression and proteomic analysis of MPs are rapidly emerging.     

High conversion in asymmetric hydrolysis during permeation through enzyme-multilayered porous hollow-fiber membranes

We describe a novel porous hollow-fiber support for immobilizing aminoacylase in multilayers. Epoxy-group-containing polymer chains were grafted onto a porous hollow-fiber membrane by radiation-induced graft polymerization of glycidyl methacrylate, and subsequently a diethylamino group as an anion-exchange group was introduced into the graft chain. Aminoacylase was adsorbed in multilayers by allowing the amioacylase buffer solution to permeate through the pores across the hollow fiber; the graft chains provided three-dimensional space for the enzymes because of their electrostatic repulsion. The adsorbed enzyme at a degree of multilayer binding of 15 was cross-linked with glutaraldehyde to prevent leakage. An acetyl-DL-methionine solution was allowed to permeate through the pores surrounded by the aminoacylase-immobilized graft chain. Production of L-methionine was observed at a 4.1 mol/h per L of the fiber for a space velocity of 200 h(-1), defined as the flow rate of the effluent penetrating the outside surface of the hollow fiber divided by the membrane volume including the lumen.     

Production of membrane proteins using cell-free expression systems

Different overexpression systems are widely used in the laboratory to produce proteins in a reasonable amount for functional and structural studies. However, to optimize these systems without modifying the cellular functions of the living organism remains a challenging task. Cell-free expression systems have become a convenient method for the high-throughput expression of recombinant proteins, and great effort has been focused on generating high yields of proteins. Furthermore, these systems represent an attractive alternative for producing difficult-to-express proteins, such as membrane proteins. In this review, we highlight the recent improvements of these cell-free expression systems and their direct applications in the fields of membrane proteins production, protein therapy and modern proteomics.