Improvement of nisin production in pH feed-back controlled,fed-batch culture by <Emphasis Type="Italic">Lactococcus lactis</Emphasis>subsp<Emphasis Type="Italic">. lactis</Emphasis>

Nisin production by Lactococcus lactis subsp. lactisin fed-batch culture was doubled by using a pH feed-back controlled method. Sucrose concentration was controlled at 10 g l^–1 giving 5010 IU nisin ml^–1 compared to 2660 IU nisin ml^–1 in batch culture.     

Cycle changing the medium results in increased nisin productivity per cell in <Emphasis Type="Italic">Lactococcus lactis</Emphasis>

High specific cellular nisin production was aimed by cycle changing the medium of Lactococcus lactis N8 and LAC48. The highest level of nisin production was reached with the 120 min cycles but maximal production was unstable. In shorter cycles (30 and 60 min) cells could be maintained in a high production state up to the end of the fermentation (28 and 14 cycles). N8 produced 19-fold and LAC48 15-fold more nisin with cycle changing the medium than without cycle incubation.     

Influence of growth conditions on the nisin production of bioengineered <Emphasis Type="Italic">Lactococcus lactis</Emphasis> strains

Nisin production of three bioengineered strains, (LAC338, LAC339 and LAC340) with immunity (nisFEG) and/or regulation (nisRK) genes of nisin biosynthesis on plasmids in the Lactococcus lactis LL27 nisin producer, was evaluated under pH-controlled and pH-uncontrolled batch fermentations. Optimization studies showed that fructose and yeast extract yielded the highest nisin activity. The strains LAC338, LAC339, and LAC340 produced 24, 45, and 44% more nisin, respectively, than wild-type L. lactis LL27 after 12-h incubation. However, sharp decreases in the yield of nisin were observed at the late phase of fermentation with LAC339 and LL27 in contrast to LAC340 and LAC338 strains for which the high level of nisin could be maintained longer. Obviously, increasing the copy number of the regulation genes together with immunity genes in the nisin producers retarded the loss of nisin in the late phase of the fermentation.     

Continuous nisin production with bioengineered <Emphasis Type="Italic">Lactococcus lactis</Emphasis> strains

Nisin production in continuous cultures of bioengineered Lactococcus lactis strains that incorporate additional immunity and regulation genes was studied. Highest nisin activities were observed at 0.2 h^–1 dilution rate and 12.5 g l^–1 fructose concentration for all strains. Recombinant strains were able to produce greater amounts of nisin at dilution rates below 0.3 h⁻¹ compared to the control strain. However, this significant difference disappeared at dilution rates of 0.4 and 0.5 h^–1. For the strains LL27, LAC338, LAC339, and LAC340, optimum conditions for nisin production were determined to be at 0.29, 0.26, 0.27, and 0.27 h^–1 dilution rates and 11.95, 12.01, 11.63, and 12.50 g l^–1 fructose concentrations, respectively. The highest nisin productivity, 496 IU ml^–1 h^–1, was achieved with LAC339. The results of this study suggest that low dilution rates stabilize the high specific nisin productivity of the bioengineered strains in continuous fermentation. Moreover, response surface methodology analysis showed that regulation genes yielded high nisin productivity at wide ranges of dilution rates and fructose concentrations.     

A repeated batch process for cultivation of <Emphasis Type="Italic">Bifidobacterium longum</Emphasis>

A repeated batch process was performed to culture Bifidobacterium longum CCRC 14634. An on-line device, oxidation-reduction potential (ORP), was used to monitor cell growth and uptake of nutrients in the culture. The ORP of the culture medium decreased substantially during fermentation until nutrients were depleted. Six cycles of batch fermentation using ORP as a control parameter were successfully carried out. As soon as ORP remained constant or increased, three-quarters of the broth was removed, and the same volume of fresh medium was fed to the fermenter for a new cycle of cultivation. Average cell concentrations of 1.9×10⁹ and 3.4×10⁹ cfu ml^–1 for repeated batch fermentation in MRS (Lactobacilli MRS broth) and WY (containing whey hydrolyzates, yeast extract, l-cysteine) medium, respectively, were achieved. Cell mass productivities for batch, fed-batch and repeated batch fermentation using MRS medium were 0.51, 0.41, and 0.64 g l^–1 h^–1, respectively, and those for batch and repeated batch using WY medium were 0.76, 0.99 g l^–1 h^–1, respectively. The results indicate a possible industrial process to culture Bifidobacteria sp.     

Nitrate and phosphate removal by<Emphasis Type="Italic"> Spirulina platensis</Emphasis>

The cyanobacterium Spirulina platensis was used to verify the possibility of employing microalgal biomass to reduce the contents of nitrate and phosphate in wastewaters. Batch tests were carried out in 0.5 dm³ Erlenmeyer flasks under conditions of light limitation (40 mol quanta m^–2 s^–1) at a starting biomass level of 0.50 g/dm³ and varying temperature in the range 23–40°C. In this way, the best temperature for the growth of this microalga (30°C) was determined and the related thermodynamic parameters were estimated. All removed nitrate was used for biomass growth (biotic removal), whereas phosphate appeared to be removed mainly by chemical precipitation (abiotic removal). The best results in terms of specific and volumetric growth rates ( =0.044 day^–1, Q _x =33.2 mg dm^–3 day^–1) as well as volumetric rate and final yield of nitrogen removal ( =3.26 mg dm^–3 day^–1, =0.739) were obtained at 30°C, whereas phosphorus was more effectively removed at a lower temperature. In order to simulate full-scale studies, batch tests of nitrate and phosphate removal were also performed in 5.0 dm³ vessels (mini-ponds) at the optimum temperature (30°C) but increasing the photon fluence rate to 80 mol quanta m^–2 s^–1 and varying the initial biomass concentration from 0.25 to 0.86 g/dm³. These additional tests demonstrated that an increase in the inoculum level up to 0.75 g/dm³ enhanced both NO₃ ^– and PO₄ ^3– removal, confirming a strict dependence of these processes on biomass activity. In addition, the larger surface area of the ponds and the higher light intensity improved removal yields and kinetics compared to the flasks, particularly concerning phosphorus removal ( =0.032–0.050 day^–1, Q _x =34.7–42.4 mg dm^–3 day^–1, =3.24–4.06 mg dm^–3 day^–1, =0.750–0.879, =0.312–0.623 mg dm^–3 day^–1, and =0.224–0.440).     

Optimization of culture conditions for the production of an extracellular ribonuclease by <Emphasis Type="Italic">Aspergillus niger</Emphasis> in a benchtop bioreactor

SummarySelf-directing optimization was successfully employed to determine the optimal combination of engineering parameters, viz., pH, aeration rate and agitation rate, for extracellular ribonuclease production by Aspergillus niger SA-13-20 in a batch bioreactor. Maximal RNase production of 5.38 IU ml^–1 was obtained at controlled pH of 2.33, aeration rate of 1.67 v/v/m and agitation rate of 850 rev/min. The effect of oxygen on the fermentation was also investigated. With increase in volumetric oxygen transfer coefficients (K_La), cell growth and RNase production first increased and then decreased. RNase production was further increased to 7.10 IU ml^–1 and the fermentation time was shortened from 96 to 72 h by controlling dissolved oxygen concentration at 10% saturation by aerating oxygen after about 28 h of fermentation under the above optimal condition. The kinetic model showed that RNase production by A. niger SA-13-20 was growth-associated.     

Multiple growth inhibition of <Emphasis Type="Italic">Klebsiella pneumoniae</Emphasis> in 1,3-propanediol fermentation

The inhibition of substrate and product on the growth of Klebsiella pneumoniae in anaerobic and aerobic batch fermentation for the production of 1,3-propanediol was studied. The cells under anaerobic conditions had a higher maximum specific growth rate of 0.19 h^–1 and lower tolerance to 110 g glycerol l^–1, compared to the maximum specific growth rate of 0.17 h^–1 and tolerance to 133 g glycerol l^–1 under aerobic conditions. Acetate was the main inhibitory metabolite during the fermentation under anaerobic conditions, with lactate and ethanol the next most inhibitory. The critical concentrations of acetate, lactate and ethanol were assessed to be 15, 19, 26 g l^–1, respectively. However, cells grown under aerobic conditions were more resistant to acetate and lactate but less resistant to ethanol. The critical concentrations of acetate, lactate and ethanol were assessed to be 24, 26, and 17 g l^–1, respectivelyRevisions requested 8 september; Revisions received 2 November 2004     

Enhancement of Nisin Production by <Emphasis Type="Italic">Lactococcus lactis</Emphasis> subsp. <Emphasis Type="Italic">lactis</Emphasis>

Lactococcus lactis subsp lactis BSA (L. lactis BSA) was isolated from a commercial fermented product (BSA Food Ingredients, Montreal, Canada) containing mixed bacteria that are used as starter for food fermentation. In order to increase the bacteriocin production by L. lactis BSA, different fermentation conditions were conducted. They included different volumetric combinations of two culture media (the Man, Rogosa and Sharpe (MRS) broth and skim milk), agitation level (0 and 100 rpm) and concentration of commercial nisin (0, 0.15, and 0.30 µg/ml) added into culture media as stimulant agent for nisin production. During fermentation, samples were collected and used for antibacterial evaluation against Lactobacillus sakei using agar diffusion assay. Results showed that medium containing 50 % MRS broth and 50 % skim milk gave better antibacterial activity as compared to other medium formulations. Agitation (100 rpm) did not improve nisin production by L. lactis BSA. Adding 0.15 µg/ml of nisin into the medium-containing 50 % MRS broth and 50 % skim milk caused the highest nisin activity of 18,820 AU/ml as compared to other medium formulations. This activity was 4 and ~3 times higher than medium containing 100 % MRS broth without added nisin (~4700 AU/ml) and 100 % MRS broth with 0.15 µg/ml of added nisin (~6650 AU/ml), respectively.     

Fed-batch production of <Emphasis Type="SmallCaps">d</Emphasis>-ribose from sugar mixtures by transketolase-deficient <Emphasis Type="Italic">Bacillus subtilis</Emphasis> SPK1

d-Ribose, a five-carbon sugar, is used as a key intermediate for the production of various biomaterials, such as riboflavin and inosine monophosphate. A high d-ribose-producing Bacillus subtilis SPK1 strain was constructed by the chemical mutation of the transketolase-deficient strain, B. subtilis JY1. Batch fermentation of B. subtilis SPK1 with 20 g l^–1 xylose and 20 g l^–1 glucose resulted in 4.78 g l^–1 dry cell mass, 23.0 g l^–1d-ribose concentration, and 0.72 g l^–1 h^–1 productivity, corresponding to a 1.5- to 1.7-fold increase when compared with values for the parental strain. A late-exponential phase was chosen as the best point for switching to a fed-batch process. Optimized fed-batch fermentation of B. subtilis SPK1, feeding a mixture of 200 g l^–1 xylose and 50 g l^–1 glucose after the late-exponential phase reduced the residual xylose and glucose concentrations to less than 7.0 g l^–1 and gave the best results of 46.6 g l^–1d-ribose concentration and 0.88 g l^–1 h^–1 productivity which were 2.0- and 1.2-fold higher than the corresponding values in a simple batch fermentation.     

Production of nisin Z using <Emphasis Type="Italic">Lactococcus lactis</Emphasis> IO-1 from hydrolyzed sago starch

A membrane bioreactor for production of nisin Z was constructed using Lactococcus lactis IO-1 in continuous culture using hydrolyzed sago starch as carbon source. A strategy used to enhance the productivity of nisin Z was to maintain the cells in a continuous growth at high cell concentration. This resulted in a volumetric productivity of nisin Z, as 50,000 IU l⁻¹ h⁻¹ using a cell concentration of 15 g l⁻¹, 30^°C, pH 5.5 and a dilution rate of 1.24 h⁻¹. Adding 10 g l⁻¹ YE and 2 g l⁻¹ polypeptone, other inducers were unnecessary to maintain production of nisin. The operating conditions of the reactor removed nisin and lactate, thus minimizing their effects which allowed the maintenance of cells in continuous exponential growth phase mode with high metabolic activity.     

Scale-up fermentation of recombinant <Emphasis Type="Italic">Candida rugosa</Emphasis> lipase expressed in <Emphasis Type="Italic">Pichia pastoris</Emphasis> using the GAP promoter

The high-cell-density fermentation of Candida rugosa lipase in the constitutive Pichia pastoris expression system was scaled up from 5 to 800 l in series by optimizing the fermentation conditions at both lab scale and pilot scale. The exponential feeding combined with pH-stat strategy succeeded in small scale studies, while a two-stage fermentation strategy, which shifted at 48 h by fine tuning the culture temperature and pH, was assessed effective in pilot-scale fermentation. The two-stage strategy made an excellent balance between the expression of heterogeneous protein and the growth of host cells, controlling the fermentation at a relatively low cell growth rate for the constitutive yeast expression system to accumulate high-level product. A stable lipase activity of approximately 14,000 IU ml⁻¹ and a cell wet weight of ca. 500 g l⁻¹ at the 800-l scale were obtained. The efficient and convenient techniques suggested in this study might facilitate further scale-up for industrial lipase production.     

Cadmium biosorption by <Emphasis Type="Italic">Bacillus</Emphasis><Emphasis Type="Italic"> circulans</Emphasis> strain EB1

Summary A heavy metal resistant bacterium, Bacillus circulans strain EB1 showed a high cadmium biosorption capacity coupled with a high tolerance to this metal when grown in its presence. Bacillus circulans EB1 cells grown in the presence of 28.1 mg cadmium/l were capable of removing cadmium with a specific biosorption capacity of 5.8 mg Cd/g dry wt biomass in the first 8 h. When the cells were pre-conditioned with low concentrations of cadmium in pre-grown medium, the uptake was increased to 6.7 mg Cd/g dry wt biomass. The maximum uptake of␣cadmium was during mid-logarithmic phase of growth. The resting cells (both wet and dry) of EB1 were also able to biosorb cadmium. Specific biosorption capacities of wet and dry biomass were 9.8 and 26.5 mg Cd/g dry wt biomass, respectively. Maximum cadmium removals by both wet and dry cells were at pH 7.0. The results showed that the cadmium removal capacity of resting cells was markedly higher than that of growing cells. Since both growing and resting cells had a high biosorption capacity for cadmium, EB1 cells could serve as an excellent biosorbent for removal of cadmium from natural environments.     

Promoting acid resistance and nisin yield of <Emphasis Type="Italic">Lactococcus lactis</Emphasis> F44 by genetically increasing D-Asp amidation level inside cell wall

Nisin fermentation by Lactococcus lactis requires a low pH to maintain a relatively higher nisin activity. However, the acidic environment will result in cell arrest, and eventually decrease the relative nisin production. Hence, constructing an acid-resistant L. lactis is crucial for nisin harvest in acidic nisin fermentation. In this paper, the first discovery of the relationship between D-Asp amidation-associated gene (asnH) and acid resistance was reported. Overexpression of asnH in L. lactis F44 (F44A) resulted in a sevenfold increase in survival capacity during acid shift (pH 3) and enhanced nisin desorption capacity compared to F44 (wild type), which subsequently contributed to higher nisin production, reaching 5346 IU/mL, 57.0% more than that of F44 in the fed-batch fermentation. Furthermore, the engineered F44A showed a moderate increase in D-Asp amidation level (from 82 to 92%) compared to F44. The concomitant decrease of the negative charge inside the cell wall was detected by a newly developed method based on the nisin adsorption amount onto cell surface. Meanwhile, peptidoglycan cross-linkage increased from 36.8% (F44) to 41.9% (F44A), and intracellular pH can be better maintained by blocking extracellular H⁺ due to the maintenance of peptidoglycan integrity, which probably resulted from the action of inhibiting hydrolases activity. The inference was further supported by the acmC-overexpression strain F44C, which was characterized by uncontrolled peptidoglycan hydrolase activity. Our results provided a novel strategy for enhancing nisin yield through cell wall remodeling, which contributed to both continuous nisin synthesis and less nisin adsorption in acidic fermentation (dual enhancement).     

High efficiency degradation of tetrahydrofuran (THF) using a membrane bioreactor: identification of THF-degrading cultures of<Emphasis Type="Italic"> Pseudonocardia</Emphasis> sp. strain M1 and<Emphasis Type="Italic"> Rhodococcus ruber</Emphasis> isolate M2

A mixed microbial culture capable of growing aerobically on tetrahydrofuran (THF) as a sole carbon and energy source was used as the inoculum in a 10 l working volume membrane bioreactor. Following start-up, the reactor was operated in batch mode for 24 h and then switched to continuous feed with 100% biomass recycle. On average, greater than 96% of THF fed to the reactor was removed during the 8-month study. THF loading rates ranged from 0.62 to 9.07 g l^–1 day^–1 with a hydraulic retention time of 24 h. THF concentrations as high as 800 mg/l were tolerated by the culture. Biomass production averaged 0.28 kg total suspended solids/kg chemical oxygen demand removed, i.e., comparable to a conventional wastewater treatment process. Periodic batch wasting resulted in a solids retention time of 7–14 days. Reactor biomass typically ranged from 4 to 10 g/l volatile suspended solids and the effluent contained no solids. Pure THF-degrading cultures were isolated from the mixed culture based on morphological characteristics, Gram-staining and THF degradation. Based on 16S rDNA analysis the isolates were identified as Pseudonocardia sp. M1 and Rhodococcus ruber M2.     

Modeling of the pyruvate production with<Emphasis Type="Italic"> Escherichia coli</Emphasis> in a fed-batch bioreactor

A family of 10 competing, unstructured models has been developed to model cell growth, substrate consumption, and product formation of the pyruvate producing strain Escherichia coli YYC202 ldhA::Kan strain used in fed-batch processes. The strain is completely blocked in its ability to convert pyruvate into acetyl-CoA or acetate (using glucose as the carbon source) resulting in an acetate auxotrophy during growth in glucose minimal medium. Parameter estimation was carried out using data from fed-batch fermentation performed at constant glucose feed rates of q_VG=10 mL h^–1. Acetate was fed according to the previously developed feeding strategy. While the model identification was realized by least-square fit, the model discrimination was based on the model selection criterion (MSC). The validation of model parameters was performed applying data from two different fed-batch experiments with glucose feed rate q_VG=20 and 30 mL h^–1, respectively. Consequently, the most suitable model was identified that reflected the pyruvate and biomass curves adequately by considering a pyruvate inhibited growth (Jerusalimsky approach) and pyruvate inhibited product formation (described by modified Luedeking–Piret/Levenspiel term).List of symbols c_A acetate concentration (g L^–1) - c_A,0 acetate concentration in the feed (g L^–1) - c_G glucose concentration (g L^–1) - c_G,0 glucose concentration in the feed (g L^–1) - c_P pyruvate concentration (g L^–1) - c_P,max critical pyruvate concentration above which reaction cannot proceed (g L^–1) - c_X biomass concentration (g L^–1) - K_I inhibition constant for pyruvate production (g L^–1) - K_I^A inhibition constant for biomass growth on acetate (g L^–1) - K_P saturation constant for pyruvate production (g L^–1) - K_P inhibition constant of Jerusalimsky (g L^–1) - K_S^A Monod growth constant for acetate (g L^–1) - K_S^G Monod growth constant for glucose (g L^–1) - m_A maintenance coefficient for growth on acetate (g g^–1 h^–1) - m_G maintenance coefficient for growth on glucose (g g^–1 h^–1) - n constant of extended Monod kinetics (Levenspiel) (–) - q_V volumetric flow rate (L h^–1) - q_VA volumetric flow rate of acetate (L h^–1) - q_VG volumetric flow rate of glucose (L h^–1) - r_A specific rate of acetate consumption (g g^–1 h^–1) - r_G specific rate of glucose consumption (g g^–1 h^–1) - r_P specific rate of pyruvate production (g g^–1 h^–1) - r_P,max maximum specific rate of pyruvate production (g g^–1 h^–1) - t time (h) - V reaction (broth) volume (L) - Y_P/G yield coefficient pyruvate from glucose (g g^–1) - Y_X/A yield coefficient biomass from acetate (g g^–1) - Y_X/A,max maximum yield coefficient biomass from acetate (g g^–1) - Y_X/G yield coefficient biomass from glucose (g g^–1) - Y_X/G,max maximum yield coefficient biomass from glucose (g g^–1) - growth associated product formation coefficient (g g^–1) - non-growth associated product formation coefficient (g g^–1 h^–1) - specific growth rate (h^–1) - _max maximum specific growth rate (h^–1)     

Effect of temperature on <Emphasis Type="SmallCaps">d</Emphasis>-arabitol production from lactose by <Emphasis Type="Italic">Kluyveromyces lactis</Emphasis>

d-Arabitol production from lactose by Kluyveromyces lactis NBRC 1903 has been studied by following the time courses of concentrations of cell mass, lactose, d-arabitol, ethanol, and glycerol at different temperatures. It was found that temperature is a key factor in d-arabitol production. Within temperatures ranging from 25 to 39°C, the highest d-arabitol concentration of 99.2 mmol l⁻¹ was obtained from 555 mmol l⁻¹ of lactose after 120 h of batch cultivation at 37°C. The yield of d-arabitol production on cell mass growth increased drastically at temperatures higher than 35°C, and the yield reached 1.07 at 39°C. Increasing the cell mass concentration two-fold after 24 h of culture growth at 37°C, the d-arabitol concentration further increased to 168 mmol l⁻¹. According to the distribution of the metabolic products, metabolic changes related to growth phase were also discussed. The stationary-phase K. lactis cells in the batch culture that is started with exposing the precultured inoculum to high osmotic stress, high oxidative stress, and high heat stress are found to be preferable for d-arabitol production.     

Aquacultural characteristics of <Emphasis Type="Italic">Rhizoclonium</Emphasis><Emphasis Type="Italic">riparium</Emphasis> and an evaluation of its biomass growth potential

A study was made of environmental factors affecting the growth of Rhizoclonium riparium in order to evaluate its suitability for large-scale culturing. The results indicate that under the natural conditions prevailing at Taishi, Taiwan, this species can grow year-round, with a monthly biomass production (oven-dried) of 945–1540 kg ha⁻¹ pond surface (assuming a pond depth of 1 m). The specific growth rate ranged from –2.1 to 10.4% per day. Salinity and temperature, both influenced the rate significantly, with optimal values at 20% and 25 °C, respectively. Short (2-mm) lengths of filaments had a higher specific growth rate than longer (20 mm) filaments. Under rotational culturing conditions, the specific growth rate was reduced when flow was increased.     

Production,Respiration, and Overall Carbon Balance in an Old-growth <Emphasis Type="Italic">Pseudotsuga</Emphasis>-<Emphasis Type="Italic">Tsuga</Emphasis> Forest Ecosystem

Ground-based measurements of stores, growth, mortality, litterfall, respiration, and decomposition were conducted in an old-growth forest at Wind River Experimental Forest, Washington, USA. These measurements were used to estimate gross primary production (GPP) and net primary production (NPP); autotrophic respiration (R_a) and heterotrophic (R_h) respiration; and net ecosystem production (NEP). Monte Carlo methods were used to calculate uncertainty (expressed as ± 2 standard deviations of 200–400 calculations). Live carbon (C) stores were 39,800 g C m^–2 (34,800–44,800 g C m^–2). The store of C in detritus and mineral soil was 22,092 g C m^–2 (20,600–23,600 g C m^–2), and the total C stores were 61,899 g C m^–2 (56,600–67,700 g C m^–2). Total NPP was 597 g C m^–2 y^–1 (453 to 741 g C m^–2 y^–1). R_a was 1309 g C m^–2 y^–1 (845–1773 g C m^–2 y^–1), indicating a GPP of 1906 g C m^–2 y^–1 (1444–2368 g C m^–2 y^–1). R_h, including the respiration of heart rots in tree boles, was 577 g C m^–2 y^–1 (479–675 g C m^–2 y^–1). Long-term NEP was estimated to be +20 g C m^–2 y^–1 (–116 to +156 g C m^–2 y^–1), indicating this stand might be a small sink. These estimates contrast with the larger sink estimated at the same site using eddy-flux methods. Several hypotheses to explain this discrepancy were explored, including (a) undetected biomass increases, (b) underestimates of NPP, (c) unmeasured losses, and (d) a temporal mismatch between the two sets of measurements. The last hypothesis appears the most likely.     

Production of <Emphasis Type="SmallCaps">l</Emphasis>-alanine by metabolically engineered <Emphasis Type="Italic">Escherichia coli</Emphasis>

Escherichia coli W was genetically engineered to produce l-alanine as the primary fermentation product from sugars by replacing the native d-lactate dehydrogenase of E. coli SZ194 with alanine dehydrogenase from Geobacillus stearothermophilus. As a result, the heterologous alanine dehydrogenase gene was integrated under the regulation of the native d-lactate dehydrogenase (ldhA) promoter. This homologous promoter is growth-regulated and provides high levels of expression during anaerobic fermentation. Strain XZ111 accumulated alanine as the primary product during glucose fermentation. The methylglyoxal synthase gene (mgsA) was deleted to eliminate low levels of lactate and improve growth, and the catabolic alanine racemase gene (dadX) was deleted to minimize conversion of l-alanine to d-alanine. In these strains, reduced nicotinamide adenine dinucleotide oxidation during alanine biosynthesis is obligately linked to adenosine triphosphate production and cell growth. This linkage provided a basis for metabolic evolution where selection for improvements in growth coselected for increased glycolytic flux and alanine production. The resulting strain, XZ132, produced 1,279 mmol alanine from 120 g l⁻¹ glucose within 48 h during batch fermentation in the mineral salts medium. The alanine yield was 95% on a weight basis (g g⁻¹ glucose) with a chiral purity greater than 99.5% l-alanine. Electronic supplementary material The online version of this article (doi:) contains supplementary material, which is available to authorized users.