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We investigated the relationship between the microstructure and mechanical properties of additive manufactured AISI 316L steel regarding the grain aspect ratio and orientation. For this purpose, two types of specimen (vertically and horizontally built) were prepared by a selective laser melting process, and the mechanical behavior was evaluated in different tensile directions. After this, to observe the characteristic grain boundary distributions such as grain size, shape, orientation, and intergranular misorientation, electron backscattering diffraction analysis was conducted on the initial and tensile-strained specimens. The specimen with a lower grain aspect ratio showed enhanced yield and tensile strengths arising from the higher strain hardening rate relative to the specimen with higher grain aspect ratio. In addition, the material composed of grains with a higher Taylor factor showed more accumulated dislocation density during tensile deformation when compared to the material composed of grains with a lower Taylor factor, which also contributed to the increase in tensile strengths because of the enhanced strain hardening rate.

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Graphene oxide quantum dots (GOQDs) are usually prepared using expensive carbon precursors such as carbon nanotubes (CNT) or graphene under the strong acidic condition, which requires an additional purifying process. Here, we first develop a facile pulsed laser ablation in liquid (PLAL) technique for preparing GOQDs using earth-abundant and low-cost coal as a precursor. Only ethanol and coal are used to produce GOQDs with excellent optical properties. The prepared GOQDs exhibit excellent optoelectronic properties which can be successfully utilized in bioimaging applications.

The marine microalga Chlorella sp. was cultivated under mixotrophic conditions using methanol as an organic carbon source, which may also act to maintain the sterility of the medium for long-term outdoor cultivation. The optimal methanol concentration was determined to be 1% (v/v) for both cell growth and lipid production when supplying 5% CO2 with 450 μE/m2/sec of continuous illumination. Under these conditions, the maximal cell biomass and total lipid production were 4.2 g dry wt/L and 17.5% (w/w), respectively, compared to 2.2 g dry wt/L and 12.5% (w/w) from autotrophic growth. Cell growth was inhibited at methanol concentrations above 1% (v/v) due to increased toxicity, whereas 1% methanol alone sustained 1.0 g dry wt/L and 4.8% total lipid production. We found that methanol was preferentially consumed during the initial period of cultivation, and carbon dioxide was consumed when the methanol was depleted. A 12:12 h (light:dark) cyclic illumination period produced favorable cell growth (3.6 g dry wt/L). Higher lipid production was observed with cyclic illumination than with continuous illumination (18.6% (w/w) vs 17.5% (w/w)), and better lipid production was also obtained under mixotrophic rather than autotrophic conditions. Interestingly, under mixotrophic conditions with 12:12 (h) cyclic illumination, high proportions of C16:0, C18:0, and C18:1 were observed, which are beneficial for biodiesel production. These results strongly indicate that the carbon source is important for controlling both lipid composition and cell growth under mixotrophic conditions, and they suggest that methanol could be utilized to scale up production to an open pond type system for outdoor cultivation where light illumination changes periodically.

In this study, we developed a packed-bed immobilized cell reactor containing active β-gal (β-galactosidase) inclusion body (IB)-containing Escherichia coli (E. coli) cells in alginate beads. This packed-bed reactor was operated using a substrate feed solution 0.72 ∼ 38.4 mM ONPG (o-nitrophenyl-β-D-galactoside) prepared in Z buffer supplemented with chloroform and 0.1% SDS (sodium dodecyl sulfate). The production rate of ONP (o-nitrophenol) in the reactor containing cells that were incubated with α-MG (α-methyl D-glucospyranoside) or D-fucose after induction was superior to those prepared with cells that were not incubated with α-MG or D-fucose. The ONP production rate was increased proportionally with ONPG concentration in the substrate feed up to a concentration of 38.4 mM. However, as the ONPG concentration was increased in the substrate feed solution, galactose inhibition inside the alginate beads was increased. This most likely occurred due to problems with diffusion. In addition, partial breakage of alginate beads was observed during the later periods of operation. In this study, we demonstrated that active β-gal IB-containing E. coli cells were sustained in the immobilized cell reactor during operation. Particularly, these findings demonstrate the feasibility of using active IBs in an enzymatic reaction without the need for any purification step. In addition, we showed that these IB-containing cells could be directly used in an immobilized reactor.

We investigated the relevance of the relationship between the compactness of β-galactosidase inclusion bodies (β-gal IBs) and their enhanced enzymatic activity with or without the addition of D-fucose (inducer analog) or methyl α-D-glucopyranoside (α-MG, catabolite repressor) after induction in the araBAD promoter system of Escherichia coli. Experiments conducted to evaluate the solubilization of β-gal IBs in guanidine hydrochloride as well as their trypsin degradation and temperature stability revealed that β-gal IBs expressed in response to the addition of D-fucose or α-MG had a looser structure. Additionally, β-gal IBs expressed when D-fucose or α-MG was added were more quickly solubilized in guanidine hydrochloride or degraded by trypsin-treatment than those produced when these compounds were not added. Moreover, the activity of β-gal IBs expressed when D-fucose or α-MG were added was less stable at various temperatures. Consequently, we deduced that the looser structure of β-gal IBs resulted in enhanced enzymatic activity of β-gal IBs upon addition of D-fucose or α-MG after induction.

In this study, we attempted to assess the process stability of long-term fed-batch ethanol fermentation in the absence and presence of aeration (0.33 vvm). To examine the effect of aeration, a long-term repeated fed-batch operation was conducted for 396 h to mimic a long-term industrial bioethanol production process. In this long-term repeated fed-batch ethanol fermentation experiments, withdrawal-fill operation were conducted every 36 h for 10 repeat cycles. The whole operation was stably sustained in a quasi-steady state. The average maximal cell concentration and the average maximal ethanol production during operation were increased by 81.63 and 12.12%, respectively, when aeration was used. In addition, since aeration was carried out, the average ethanol yield slightly decreased by 4.03% and the average specific ethanol production rate decreased by 46.75% during operation. However, the average ethanol productivity increased by 17.53% when aeration was carried out. After 396 h of long-term repeated fed-batch ethanol fermentation, 1,908.9 g of ethanol was cumulatively produced when aeration was used, which was 12.47%, higher than when aeration was not used (1,697.2 g). Meanwhile, glycerol production was greatly decreased during long-term repeated fed-batch ethanol fermentation, in which the glycerol concentration in the culture broth decreased from about 34∼15 g/L. Thus, we can conclude that cell growth was greatly improved by overcoming ethanol inhibition and glycerol production was remarkably decreased when aeration was carried out, although aeration in ethanol fermentation decreased the specific ethanol production rate and ethanol yield.

In this study, we utilized a unique strategy for fed-batch fermentation using ethanol-tolerant Saccharomyces cerevisiae to achieve a high-level of ethanol production that could be practically applied on an industrial scale. During this study, the aeration rate was controlled at 0.0, 0.13, 0.33, and 0.8 vvm to determine the optimal aeration conditions for the production of ethanol. Additionally, non-sterile glucose powder was fed during fed-batch ethanol fermentation and corn-steep liquor (CSL) in the medium was used as an organic N-source. When aeration was conducted, the ethanol production and productivity were superior to that when aeration was not conducted. Specifically, the maximum ethanol production reached approximately 160 g/L, when the fermentor was aerated at 0.13 vvm. These findings indicate that the use of a much less expensive C-source may enable the fermentation process to be directed towards the improvement of overall ethanol production and productivity in fermentors that are aerated at 0.13 vvm. Furthermore, if a repeated fed-batch process in which the withdrawal and fill is conducted prior to 36 h can be employed, aeration at a rate of 0.33 and/or 0.8 vvm may improve the overall ethanol productivity

In this study, we investigated the effects of aeration on ethanol inhibition and glycerol production during fed-batch ethanol fermentation. When aeration was conducted at 0.13, 0.33, and 0.8 vvm, the ethanol productivity, specific ethanol production rate, and ethanol yield in the presence of greater than 100 g/L of ethanol were higher than when aeration was not conducted. In addition, estimation of the parameters (α and β) in a model equation of ethanol inhibition kinetics indicated that aeration alleviated ethanol inhibition against the specific growth rate and the specific ethanol production rate. Specifically, when aeration was conducted, the glycerol yield and specific glycerol production rate decreased approximately 50 and 70%, respectively. Finally, the results of this study indicated that aeration during fed-batch ethanol fermentation may improve the ethanol concentration in the final culture broth, as well as the ethanol productivity.

To improve the soluble expression of recombinant human interferon-α that was directed by the araBAD promoter system of Escherichia coli, we attempted to control the overall protein expression rate via the addition of a repressor, methyl α-D-glucospyranoside (α-MG). Recombinant interferon-α was usually expressed as an inclusion body at the end of DO (dissolved oxygen)-stat fed-batch culture. However, the addition of 0.0025 to 0.01% α-MG after 0.5% L-arabinose induction effectively inhibited a tendency towards the formation of inclusion bodies, in which 67.6 to 73.1% of the expressed interferon-α was found in the soluble fraction. It was likely that the addition of a repressor after L-arabinose induction partially modulated the transcription rate from the araBAD promoter system and changed the ratio of soluble and insoluble interferon-α expression. This modulation might be considered as a method that can improve the soluble expression level of recombinant protein at the optimal temperature for cell growth.

We investigated the growth inhibition effect of pyroligneous acid on the pathogenic fungus,Alternaria mali, which is known to be the agent of Alternaria blotch of apple plants. Chemical control ofA. mali could be achieved through the use of agrochemical fungicides, while the substitute for agrochemical control is gradually increasing. It was observed that pyroligneous acid exhibited antifungal activity against some plant pathogenic fungi. More specifically, the growth ofA. mali was completely inhibited in pyroligneous acid at a dilution of 1∶32. When its antifungal activity was compared to that of polyoxin B, which is used for the chemical control of Alternaria blotch of apple, it was observed that the antifungal activity of pyroligneous acid diluted at 1∶32 corresponded to 2.0 mg/mL of polyoxin B. Consequently, it is concluded that the diluted pyroligneous acid can substitute for polyoxin B, thereby reducing the use of the agrochemical for the control of Alternaria blotch of apple.

RecombinantSaccharomyces cerevisiae expression systems were developed to produce a novel human anti-angiogenic protein called LK8, an 86 amino-acid kringle fragment protein with three disulfide linkages. Galactose-inducible LK8 expression plasmid was constructed, and LK8 production levels by fourS. cerevisiae strains were compared in order to select an optimal host strain.S. cerevisiae 2805 was the most efficient among the strains tested. Elevating the LK8 gene copy number through multiple integration using δ-sequences as target sites resulted in more than a two-fold increase in the LK8 production level compared with the plasmid-based expression system. The maximum LK8 protein concentration of 25 mg/L was obtained from batch cultivation of the yeast transformant that harbors 16 copies of the LK8 gene. In conclusion, the strain integrated with the multiple LK8 gene secreted the protein with relatively high yield, although, the increased LK8 gene dosage over 11 copies did not lead to further enhancement in batch cultivations.

The human chemokine, the short version of leukotactin-1 (shLkn-1; molecular weight =7.2 kD and 66 amino acids), was expressed and secreted into a culture medium using the methylotrophic yeast,Pichia pastoris. The recombinant shLkn-1 was purified from the culture supernatant using a simple two-step procedure consisting of cation exchange and reverse phase chromatography (RPC), in which shLkn-1 was highly purified (99.5%) with a high recovery yield of 82.7%. The C-terminal truncated derivative of shLkn-1 was found in the supernatant and was separated by RPC. The physicochemical properties of the purified shLkn-1 were verified to be the same as expected. The biological activity of the purified recombinant shLkn-1 was also quantified using a chemotaxis assay. It was observed that the recombinant shLkn-1 had the maximum migration activity at a concentration of 10 nM, as potent as MIP-1α.

The long-term process for producing human granulocyte-colony stimulating factor (hG-CSF) was developed using two-stage cyclic fed-batch culture, in which hG-CSF expressing-recombinant Escherichia coli was directed by an L-arabinose promoter system. For the optimization, the preinduction growth rate during the growth stage and the feeding strategy during the production stage were investigated. The maximum harvest volume during the production stage was predicted before long-term cyclic operation. Based on those optimized strategies, the two-stage cyclic fed-batch culture was performed for 12 cycles (86 h). The cell growths in both stages were maintained at 45–50 g/L and 71–77 g/L, respectively. hG-CSF was stably produced at a level of 8–9 g/L and the plasmid stability was maintained at more than 90%. Volumetric productivity by the two-stage cyclic fed-batch culture was 0.643 g/L/h, which was about 280% higher than that of conventional DO-stat fed-batch culture.

In the hepatitis B surface antigen (HBsAg)-producing recombinant yeast culture medium, the supply of Bacto-yeast nitrogen base without amino acids was found to be inadequate due to the lack of the several kinds of vitamins and trace elements. When the culture medium for this recombinant yeast was supplemented with sufficient vitamins and trace elements, its growth, HBsAg production and the stability of plasmid were improved.

Background Insoluble protein aggregate (inclusion body) is frequently accumulated during the heterologous protein expression by the bacterial inducible promoter system. In this study, although many reports have proposed the methodology to circumvent the aggregate formation [1-3], we tried to control the transcription rate by an addition of the repressor for inducible promoter. The addition of repressor was from The 4th Recombinant Protein Production Meeting: a comparative view on host physiology Barcelona, Spain. 21–23 September 2006

To maintain a constant specific growth rate for a recombinantS.cerevisiae in fed-batch, the medium feeding rate has been controlled with respect to the hourly calculated glucose uptake rate. The recombinant yeast producing HBsAg showed the exponential production trend in proportion to the exponential cell growth. Total cell yield in fed-batch was about 0.402 g cells/g glucose, and HBsAg was produced about ten times more than in batch. Decrease of growth rate by HBsAg produced was not shown.