High level production of human proapo A-I by fed-batch culture of recombinant Escherichia coli

Three Escherichia coli strains, two recA⁻ strains (DH1 and YK537) and one recA⁺ strain (KS476) harboring human proapo A-I expression plasmid pUS(pAI), were cultivated in fed-batch mode using a synthetic medium and the amounts of human proapo A-I accumulation were compared under various cultivation conditions. In the expression plasmid, nine proapo A-I genes were tandemly ligated downstream of the tac promoter. Experimental results indicated that selection of the host strain and cultivation temperature was important. Among the three E. coli strains checked, strain DH1 yielded the most effective production of human proapo A-I at 30°C.     

High-level production of human leptin by fed-batch cultivation of recombinant Escherichia coli and its purification.

Human leptin is a 16-kDa (146-amino-acid) protein that is secreted from adipocytes and influences body weight homeostasis. In order to obtain high-level production of leptin, the human obese gene coding for leptin was expressed in Escherichia coli BL21(DE3) under the strong inducible T7 promoter. The recombinant leptin was produced as inclusion bodies in E. coli, and the recombinant leptin content was as high as 54% of the total protein content. For production of recombinant human leptin in large amounts, pH-stat fed-batch cultures were grown. Expression of leptin was induced at three different cell optical densities at 600 nm (OD600), 30, 90, and 140. When cells were induced at an OD600 of 90, the amount of leptin produced was 9.7 g/liter (37% of the total protein). After simple purification steps consisting of inclusion body isolation, denaturation and refolding, and anion-exchange chromatography, 144.9 mg of leptin that was more than 90% pure was obtained from a 50-ml culture, and the recovery yield was 41.1%.     

High-level secretory production of human granulocyte-colony stimulating factor by fed-batch culture of recombinant Escherichia coli

Secretory production of human granulocyte colony-stimulating factor fusion protein (hG-CSF) by fed-batch culture of Escherichia coli was investigated in both 2.5-L and 30-L fermentors. To develop a fed-batch culture condition that allows efficient production of hG-CSF, different feeding strategies including pH-stat, exponential and constant feeding were examined. Among these, the constant feeding strategy (0.228 g glucose2min^-1) and the exponential feeding that supports a low specific growth rate (µ=0.116 h^-1) resulted in the best hG-CSF production. Under these conditions, 4.4 g2L^-1 of hG-CSF was produced. The effect of induction time on the protein production was also investigated. For the fed-batch cultures carried out with the pH-stat and exponential feeding strategies, induction at higher cell density (late-exponential phase) resulted in more hG-CSF production compared with induction at lower cell density (early to mid-exponential phase). The constant feeding strategy that supported best hG-CSF production was applied to the scale-up production of hG-CSF in 30 L of fermentor. The maximum dry cell weight and hG-CSF concentration of 51.7 and 4.2 g2L^-1, respectively, was obtained.     

Enhancement of 5-aminolevulinate production with recombinant Escherichia coli using batch and fed-batch culture system

5-Aminolevulinate (ALA) production with recombinant Escherichia coli Rosetta (DE3)/pET28a(+)-hemA was studied. In batch fermentation, the addition of glucose and glycine was effective to improve ALA production. Then the fed-batch fermentation was conducted with continuous feeding of precursors. When the concentrations of succinic acid and glycine were 7.0 g/l and 4.0 g/l, respectively, in the feeding, the ALA yield reached 4.1g/l. But the molar yield (ALA/glycine) was decreased in the fed-batch fermentation compared to batch fermentation. And it was found that the pH control during fed-batch cultivation was very important for the cell growth and ALA production. A two-stage pH value controlling strategy was suggested, in which, the pH value in the first 6h was regulated at pH 5.9, after then at pH 6.2, and the ALA yield was as high as 6.6g/l via fed-batch fermentation.     

Mass production of human epidermal growth factor using fed-batch cultures of recombinant Escherichia coli

Fed-batch cultures of recombinant E. coli HB101 harboring expression plasmid pTRLBT1 or pTREBT1, with acetate concentration monitoring, are investigated to obtain high cell density and large amounts of human epidermal growth factor (hEGF). The expression plasmid pTRlBT1 contains a synthetic hEGF gene attached downstream of the N-terminal fragment of the trp L gene preceded by the trp promoter. The expression plasmid pTREBT1 contains the same coding sequence attached downstream of the N-terminal fragment of the trp E gene preceded by the trp promoter, trp L gene, and attenuator region. E. coli harboring pTREBT1 produces 0.56 mg/L hEGE and immediately degrades it. On the other hand E. coli harboring pTRLBT1 produces 6.8 mg/L hEGF and does not decompose it. Prominent inclusion bodies are observed in E. coli cells harboring pTRLBT1 using an election microscope. To Cultivate E. coli harboring pTRLBT1, a fed-batch culture system, divided into a cell growth step and an hEGF production step, is carried out. The cells grow smoothly without acetate-induced inhibition. Cell concentration and hEGF quantity reach the high values of 21 g/L and 60 mg/L, respectively.     

High-level production of poly(3-hydroxybutyrate-co-3-hydroxyvalerate) by fed-batch culture of recombinant Escherichia coli.

Fermentation strategies for production of high concentrations of poly(3-hydroxybutyrate-co-3-hydroxyvalerate) [P(3HB-co-3HV)] with different 3-hydroxyvalerate (3HV) fractions by recombinant Escherichia coli harboring the Alcaligenes latus polyhydroxyalkanoate biosynthesis genes were developed. Fed-batch cultures of recombinant E. coli with the pH-stat feeding strategy facilitated production of high concentrations and high contents of P(3HB-co-3HV) in a chemically defined medium. When a feeding solution was added in order to increase the glucose and propionic acid concentrations to 20 g/liter and 20 mM, respectively, after each feeding, a cell dry weight of 120.3 g/liter and a relatively low P(3HB-co-3HV) content, 42.5 wt%, were obtained. Accumulation of a high residual concentration of propionic acid in the medium was the reason for the low P(3HB-co-3HV) content. An acetic acid induction strategy was used to stimulate the uptake and utilization of propionic acid. When a fed-batch culture and this strategy were used, we obtained a cell concentration, a P(3HB-co-3HV) concentration, a P(3HB-co-3HV) content, and a 3HV fraction of 141.9 g/liter, 88.1 g/liter, 62.1 wt%, and 15.3 mol%, respectively. When an improved nutrient feeding strategy, acetic acid induction, and oleic acid supplementation were used, we obtained a cell concentration, a P(3HB-co-3HV) concentration, a P(3HB-co-3HV) content, and a 3HV fraction of 203.1 g/liter, 158.8 g/liter, 78.2 wt%, and 10.6 mol%, respectively; this resulted in a high level of productivity, 2.88 g of P(3HB-co-3HV)/liter-h.     

Secretory production of human leptin in Escherichia coli

Human leptin is a 16 kDa (146 amino acids) protein secreted from adipocytes and influences body weight homeostasis. In this study, human leptin was produced and secreted efficiently in Escherichia coli using a novel Bacillus sp. endoxylanase signal peptide. The endoxylanase signal sequence consisted of 28 amino acids (84 bp) was fused to the leptin structural gene. The fused gene was expressed using an inducible promoter (T7 or Trc) by adding 1 mM IPTG. Using T7 promoter in E. coli BL21(DE3), most of protein produced was in a premature form. Using the Trc promoter, which is weaker than T7, leptin was efficiently produced and secreted as a mature form (40% of total proteins) at 37 degrees C. However, most of leptin (about 90%) formed the inclusion bodies in the periplasmic space of E. coli. At 30 degrees C, ca. 90% of leptin was produced in a soluble form, but the total amount of leptin produced was 40% less than that obtained at 37 degrees C. When the periplasmic oxidoreductase of E. coli, DsbA, was co-expressed, 69% of the secreted leptin (26% of total proteins) was produced as soluble form at 37 degrees C without the decrease of the amount of leptin produced.     

Production of poly(3-hydroxybutyrate) by fed-batch culture of filamentation-suppressed recombinant Escherichia coli.

Recombinant Escherichia coli XL1-Blue harboring a high-copy-number plasmid containing the Alcaligenes eutrophus polyhydroxyalkanoate synthesis genes could efficiently synthesize poly(3-hydroxybutyrate) (PHB) in a complex medium containing yeast extract and tryptone but not in a defined medium. One of the reasons for the reduced PHB production in a defined medium was thought to be severe filamentation of cells in this medium. By overexpressing an essential cell division protein, FtsZ, in recombinant E. coli producing PHB, filamentation could be suppressed and PHB could be efficiently produced in a defined medium. A high PHB concentration of 149 g/liter, with high productivity of 3.4 g of PHB/liter/h, could be obtained by the pH-stat fed-batch culture of the filamentation-suppressed recombinant E. coli in a defined medium. It was also found that insufficient oxygen supply at a dissolved oxygen concentration (DOC) of 1 to 3% of air saturation during active PHB synthesis phase did not negatively affect PHB production. By growing cells to the concentration of 110 g/liter and then controlling the DOC in the range of 1 to 3% of air saturation, a PHB concentration of 157 g/liter and PHB productivity of 3.2 g of PHB/liter/h were obtained. For the scale-up studies, fed-batch culture was carried out in a 50-liter stirred tank fermentor, in which the DOC decreased to zero when cell concentration reached 50 g/liter. However, a relatively high PHB concentration of 101 g/liter and PHB productivity of 2.8 g of PHB/liter/h could still be obtained, which demonstrated the possibility of industrial production of PHB in a defined medium by employing the filamentation-suppressed recombinant E. coli.     

利用指数流加补料高密度发酵产β-呋喃果糖苷酶重组大肠杆菌

【目的】对重组大肠杆菌BL21(DE3)/pET22b-β-ffase进行高密度发酵产β-呋喃果糖苷酶工艺研究。【方法】比较溶氧反馈补料和指数流加补料对重组菌发酵产酶的影响,对不同比生长速率和诱导时机进行优化。【结果】确定了双阶段指数流加过程中重组菌生长的比生长速率,分别控制诱导前期比生长速率为0.20 h~(-1),诱导后期比生长速率为0.13 h~(-1),诱导时机为指数中期。获得细胞干重约为51 g/L,最高酶活达到1.79×10~5 U/L,单位菌体产酶量为3 510 U/g,单位产酶速率达到3.58×10~4 U/(L·h),生物量、单位菌体产酶量和产酶速率分别是指数流加未优化前的1.8、1.7和3.0倍。【结论】双阶段指数流加补料工艺能有效提高β-呋喃果糖苷酶的产酶量,为β-呋喃果糖苷酶的进一步工业化奠定基础。     

Characteristics of a DO-controlled fed-batch culture of Escherichia coli

The DO-controlled glucose limited fed-batch technique was investigated in an E. coli process for production of a recombinant protein. The k_Lac^* value (oxygen transfer rate at zero oxygen concentration) was calculated from on-line gas analysis data during the process. In the investigated processes with induced production of recombinant protein, the k_Lac^* value decreased drastically several hours after induction. The reason for the decrease was found in increasing concentrations of DNA in the medium and increased viscosity due to cell lysis. The consequences of such a dramatic decrease in the volumetric oxygen transfer coefficient on the glucose feed and specific rates are described in computer simulations and experimental data.     

Production of soluble human interleukin-6 in cytoplasm by fed-batch culture of recombinant E. coli

The major objective of this study is to identify fed-batch culture conditions optimal for the production of human interleukin-6 (hIL-6) in a soluble form. Five different expression vectors were constructed for the expression of hIL-6 and hIL-6s fused with NusA, maltose binding protein (MBP), thioredoxin (Trx) or ubiquitin (Ubi). A series of flask cultures were conducted in LB medium at 37 degrees C. The intact hIL-6 was expressed mostly in the form of inclusion body. More than 95% of the hIL-6 fused with NusA (NusA/hIL-6) and about 90% of MBP/hIL-6 were expressed in a soluble form, whereas Trx/hIL-6 and Ubi/hIL-6 were expressed mostly in the form of inclusion body. Based on this result, NusA was selected as the fusion partner for the production of hIL-6 in the subsequent experiments. A series of pH-stat fed-batch cultures of an E. coli BL21(DE3) transformed with a NusA/hIL-6 expression vector were conducted in a bioreactor with a working volume of about 3 L. As the amount of nitrogen source was increased in the feeding medium, more soluble NusA/hIL-6 was produced, while the total amount was not significantly changed. Under the best conditions tested, about 90% of NusA/hIL-6 was produced in the soluble form. In this case, the concentration of soluble NusA/hIL-6 was 7.5 g/L with a volumetric productivity of 0.43 g/L-h.     

Enhancement of recombinant cholera toxin B subunit production in Escherichia coli by applying a fed-batch control strategy

Summary High production levels of recombinant cholera toxin B subunit in Escherichia coli were obtained with the design of an efficient fed-batch process and control strategy. The fed-batch results demonstrated a biomass production of 58 g/L (Cell Dry Weight) attaining production levels of heterologous protein of 4.7g/L in the intracellular fraction, 0.96 g/L exported into the periplasm and 0.27 g/L secreted into the culture supernatant.     

Production of poly(3-hydroxybutyrate) from whey by cell recycle fed-batch culture of recombinant Escherichia coli

A new fermentation strategy using cell recycle membrane system was developed for the efficient production of poly(3-hydroxybutyrate) (PHB) from whey by recombinant Escherichia coli strain CGSC 4401 harboring the Alcaligenes latus polyhydroxyalkanoate (PHA) biosynthesis genes. By cell recycle, fed-batch cultivation employing an external membrane module, the working volume of fermentation could be constantly maintained at 2.3 l. The final cell concentration, PHB concentration and PHB content of 194 g l^–1, 168 g l^–1 and 87%, respectively, were obtained in 36.5 h by the pH-stat cell recycle fed-batch culture using whey solution concentrated to contain 280 g lactose l^–1 as a feeding solution, resulting in a high productivity of 4.6 g PHB l^–1 h^–1.     

A simple feedback control of Escherichia coli growth for recombinant aldolase production in fed-batch mode

Fed-batch production of recombinant fuculose-1-phosphate aldolase (FucA) by Escherichia coli XL1 Blue MRF′ (pTrcfuc) has been automated by using a simple feedback specific growth rate control strategy. Non-induced continuous cultures were conducted in order to characterize substrate consumption and carbon dioxide production yields and rates. In fed-batch cultures, substrate feeding rate was adjusted using on-line biomass estimation based on exhaust gas analysis and macroscopic mass balances. Overexpression of recombinant protein induced by isopropyl-β-d-thiogalactopyranoside (IPTG) under trc promoter did not affect significantly the control of specific growth rate during 7 h after induction. Growth and protein production curves were parallel until high level of protein expression started to inhibit cell growth. The proposed specific growth rate control strategy has been successfully applied to both non-induced and induced fed-batch cultures that do not exhibit severe growth rate depression.     

Studies on the production of human parathyroid hormone by recombinant Escherichia coli

Expression of human parathyroid hormone, hPTH(-1-84), by Escherichia coli N4830: pEX-PPTH was studied in controlled bioreactors. The hPTH is expressed as a fusion protein under control of the bacteriophage p_R promoter. In batch runs, low biomass concentrations but high specific hPTH productivities were obtained with complex TY (bactotryptone and yeast extract) medium whereas high biomass concentration and low specific productivities were found when fructose was used instead of bactotryptone (YF medium). The preinduction temperature was always 30°C; the temperature shift to induce production of fusion protein was varied from 36 to 42°C. Formation of hPTH passed a pronounced maximum as a function of induction temperature when using YF medium. However, the optimum temperature shift was 38°C for both media used. For this temperature increase both media yielded about the same volumetric hPTH productivity (approx. 30 mg hPTH/l per hour). By applying a fedbatch strategy for the YF medium, the productivity of the recombinant protein could be further increased more than fourfold. Compared to shake-flask experiments, the hPTH yield could be increased by a factor larger than 20.     

Effect of culture conditions on production of 5-aminolevulinic acid by recombinant Escherichia coli

Aminolevulinic acid (ALA) is formed by the enzyme ALA synthase (hemA gene). Then ALA is converted to Porphobilinogen (PBG) by the ALA dehydratase (hemB gene). For the overproduction of ALA, we used an Escherichia coli BL21(DE3) containing a hemA gene from Bradyrhzobium japonicum, which was created in our previous work. The effects of pH on the ALA synthase and ALA dehydratase were investigated. The ALA synthase and ALA dehydratase activities were dependent on the pH of the medium, with maximal activities occurring at pH 6.5 and 8.0 respectively. At pH 6.5, extracellular ALA reached 23 mM in a jar-fermenter. In addition, the effects of some nutritional factors, such as nitrogen source and the ratio of carbon to nitrogen (C/N) on the fermentative production of ALA were investigated. The highest ALA production was found with 8:1 of C/N ratio. Among various nitrogen sources, the tryptone might be a useful one for ALA production.     

Butanol production from glycerol by recombinant Escherichia coli

Escherichia coli MG1655 (DE3) with the ability to synthesize butanol from glycerol was constructed by metabolic engineering. The genes thil, adhe2, bcs operon (crt, bcd, etfB, etfA, and hbd) were cloned into the plasmid vectors, pETDuet-1 and pACYCDuet-1, then the two resulting plasmids, pACYC-thl-bcs and pET-adhe2, were transferred to E. coli, and the recombinant strain was able to synthesize up to 18.5 mg/L butanol on a glycerol-containing medium. After the glycerol transport protein gene GlpF was expressed, the butanol production was improved to 22.7 mg/L. The competing pathway of byproducts, such as ethanol, succinate, and lactate, was subsequently deleted to improve the 1-butanol production to 97.9 mg/L. Moreover, a NADH regeneration system was introduced into the E. coli, and finally a 154.0 mg/L butanol titer was achieved in a laboratory-scale shake-flask experiment.     

Physiologically motivated strategies for control of the fed-batch cultivation of recombinant Escherichia coli for phenylalanine production

The efficiency of the fed-batch cultivation of recombinant Escherichia coli AT2471 for phenylalanine production is highly dependent on the distribution of the carbon flow between the main process products — biomass, phenylalanine, acetic acid and carbon dioxide. In order to enhance the process performance, the effects of several factors, namely glucose feeding, tyrosine feeding and oxygen supply, were investigated experimentally. As a result, a set of control strategies was developed, designed to tolerate phenylalanine synthesis at the expense of the remaining products. The DO was controlled to prevent acetic acid excretion due to oxygen limitation. The total amount of tyrosine fed was used to provide an optimal balance between biomass synthesis and that of phenylalanine. Special algorithms for control of the glucose feed rate were applied to eliminate the threat of acetic acid excretion due to overfeeding, and at the same time, to reduce excessive CO₂ evolution caused by unnecessarily severe glucose limitation. The joint application of these strategies resulted in greatly improved efficiency in the phenylalanine production process: the final phenylalanine concentration reached 46 g/l, the yield was above 17%, and the productivity-0.85 g/l·h. In combination, these data exceed the results reported by others, and are much higher than those obtained by use before the implementation of the proposed complex of techniques.