Large-Scale Refolding and Enzyme Reaction of Human Preproinsulin for Production of Human Insulin
Large-Scale Refolding and Enzyme Reaction of Human Preproinsulin for Production of Human Insulin
Journal of Microbiology and Biotechnology. 2015. Oct, 25(10): 1742-1750
Copyright © 2015, The Korean Society For Microbiology And Biotechnology
  • Received : April 23, 2015
  • Accepted : June 29, 2015
  • Published : October 28, 2015
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About the Authors
Chang-Kyu Kim
Division of Animal Resources and Life Science, Sangji University, Wonju 220-702, Republic of Korea
Seung-Bae Lee
Division of Animal Resources and Life Science, Sangji University, Wonju 220-702, Republic of Korea
Young-Jin Son
Department of Pharmacy, Sunchon National University, Jeonnam, Suncheon 540-742, Republic of Korea

Human insulin is composed of 21 amino acids of an A-chain and 30 amino acids of a B-chain. This is the protein hormone that has the role of blood sugar control. When the recombinant human proinsulin is expressed in Escherichia coli , a serious problem is the formation of an inclusion body. Therefore, the inclusion body must be denatured and refolded under chaotropic agents and suitable reductants. In this study, H27R-proinsulin was refolded from the denatured form with β-mercaptoethanol and urea. The refolding reaction was completed after 15 h at 15℃, whereas the reaction at 25℃ was faster than that at 15℃. The refolding yield at 15℃ was 17% higher than that at 25℃. The refolding reaction could be carried out at a high protein concentration (2 g/l) using direct refolding without sulfonation. The most economical and optimal refolding condition for human preproinsulin was 1.5 g/l protein, 10 mM glycine buffer containing 0.6 M urea, pH 10.6, and 0.3 mM β-mercaptoethanol at 15℃ for 16 h. The maximum refolding yield was 74.8% at 15℃ with 1.5 g/l protein. Moreover, the refolded preproinsulin could be converted into normal mature insulin with two enzymes. The average amount of human insulin was 138.2 g from 200 L of fermentation broth after enzyme reaction with H27R-proinsulin. The direct refolding process for H27R-proinsulin was successfully set up without sulfonation. The step yields for refolding and enzyme reaction were comparatively high. Therefore, our refolding process for production of recombinant insulin may be beneficial to the large-scale production of other biologically active proteins.
Inclusion body is a dense, amorphous protein deposit that can be found in both the cytoplasmic and periplasmic spaces of bacteria [2] . The formation of inclusion bodies has some advantages commercially [14] . First, the isolation step of target protein is comparatively simple using collecting inclusion bodies. Second, the aggregated inclusion bodies can escape from cleavage by intracellular proteases [8] . Despite of these advantages, we need additional steps in order to recover the activity of the inclusion body [1] . After cell disruption and centrifugation to collect the inclusion body, it is solubilized by denaturants such as guanidine hydrochloride or urea [9 , 19 , 30 , 31] . After inclusion body solubilization, a sulfonation step is used to increase the yield of refolding [30 , 33] . During the refolding process, reducing agents such as β-mercaptoethanol, dithiothreitol, and dithioerythritol are used to cut disulfide bonds between cysteine residues and to prevent the misfolded form of the target protein [9 , 18] . The unfolded and reduced forms of target proteins are refolded in order to recover their biological activity, using the refolding process [5 , 9 , 18 , 34] .
The synthesis of human insulin using recombinant DNA technology is achieved by using Escherichia coli or Saccharomyces cerevisiae as a host cell [6 , 32] . When human insulin is produced in recombinant E. coli , a proinsulin fusion protein is usually expressed as an inclusion body to increase the stability and the level of expression in the cell. The proinsulin fusion protein is the precursor of active human insulin and must be refolded to be transformed into an active form. In vitro refolding of the proinsulin fusion protein is accompanied by the formation of the correct disulfide bonds. Oxidative folding of proinsulin is a widely used process with high yield [7 , 16] . Human proinsulin contains three disulfide bonds that are essential for its native conformation. The formation of the native disulfide bonds is the rate-determining step during proinsulin folding [23] . During consecutive purification steps, the proinsulin fusion protein is converted into the mature form of insulin using an in vitro enzyme reaction with two enzymes (carboxypeptidase B and trypsin) [3 , 15 , 22 , 27] .
In this study, we describe the protocols of refolding and the enzyme processes for preproinsulin protein. A direct refolding process has many advantages. Using this process, we can shorten the overall production process and increase the production yield. Our results suggested that the direct refolding process of proinsulin fusion protein may be informative for recombinant protein production in E. coli .
Materials and Methods
- Reagents
The main reagents and restriction enzymes were purchased from Takara (Takara Korea, Seoul, Korea). QUICK-Clone cDNA was ordered from BD Science (Clontech 7156-1; Franklin Lakes, NJ, USA), and E. coli JM109 was purchased from Stratagene (La Jolla, CA, USA) as a bacterial host strain. All other reagents were purchased from Sigma (St. Louis, MO, USA).
- Bacterial Strain and Plasmid Construction
E. coli JM109 ( endA 1 recA 1 gyrA 96 hsdR 17 relA 1 supE 44 thiΔ ( lac-proAB ) F' [ traD 36 proAB + lacI q lacZΔM 15]) purchased from Stratagene was used for the expression of proinsulin. Plasmid pPT was composed of the P2 promoter [20] and lac operator, T7 ribosome binding site, ColE1 origin of replication, ampicillin resistance gene, and a multiple cloning site. Plasmid pPT-H27Rpi was constructed from plasmid pPT to express the preproinsulin gene in E. coli [13] . The plasmid pPT-H27Rpi expressed H27R-preproinsulin with a leader peptide containing a 28-amino-acid sequence, Met-Thr-Met-Ile-Thr-Asn-Ser-Pro-Glu-Ile- Ser-His-His-His-His-His-His-His-His-His-His-Gln-Leu-Ile-Ser-Glu-Ala-Arg, and proinsulin.
- Fed-Batch Fermentation
The medium used for stock and seed culture of recombinant E. coli strain was composed of 10 g/l tryptone, 5 g/l yeast extract, 5 g/l NaCl, 100 mg/l ampicillin, and 0.1 g/l antifoaming agent. The 500 ml seed culture was grown overnight at 30℃ and 200 rpm in a rotary shaker. The nutrient sources were three types of solutions, including initial production medium and feeding solutions I and II. The production medium for fed-batch fermentation contained (per liter) 6 g glucose, 4 g Yeast extract, 4 g KH 2 PO 4 , 8 g Na 2 HPO 4 ·12H 2 O, 3 g MgSO 4 ·7H 2 O, 0.2 g FeSO 4 ·7H 2 O, 0.075 g MnSO 4 ·5H 2 O, 0.013 g CoCl 2 ·6H 2 O, 0.075 g ZnSO 4 ·7H 2 O, 0.013 g CuCl 2 ·2H 2 O, 100 mg ampicillin, 0.013 g Na 2 MoO 4 2H 2 O, and 0.2 g antifoaming agent (Silicon fluid SAG-471; Union Carbide, USA). Feed solution I contained (per liter) 600 g glucose, and solution II contained (per liter) 150 g yeast extract, 20 g MgSO 4 , 0.2 g FeSO 4 ·7H 2 O, 0.075 g MnSO 4 ·5H 2 O, 0.013 g CoCl 2 ·6H 2 O, 0.075 g ZnSO 4 ·7H 2 O, 0.013 g CuCl 2 ·2H 2 O, 0.013 g Na 2 MoO 4 ·2H 2 O, and 1 g antifoaming agent.
Fed-batch culture was performed in a 300 L fermenter (B. Braun Biotech International, Germany) with a working volume of 200 L. The dissolved oxygen concentration was maintained at 20% air saturation by modulation of the agitation speed up to 700 rpm and the aeration rate up to 2 vvm, and by a manual change of internal pressure. The pH of the culture broth was controlled at 6.8 using ammonia water. The substrate feeding strategy was the glucose concentration control method based on pH-stat and glucose concentration in the culture broth, which was maintained below 0.05%. The culture temperature was initially 30℃ and then changed to 37℃. Elevation of culture temperature was carried out as previously reported [29] . For the three-step process, the culture temperature was raised from 30℃ to 37℃ by three shifts of the same interval. Each increment of temperature took 10 min and was maintained for 1 h. The temperature shifting was started at the optical density of 30 at 600 nm (OD 600 = 30).
- Solubilization and Sulfitolysis for Refolding of S-Sulfonated Preproinsulin
The cells were harvested by centrifugation at 12,000 rpm with a continuous centrifuge (Tomoe, Japan). The cells were resuspended in resuspension buffer (10% sucrose, 0.1 M Tris, 50 mM ethylenediamine tetraacetic acid (EDTA), 0.2 M sodium chloride, pH 7.9). The cells were lysed under 13,000 psi with a high-pressure homogenizer (Rannie, Denmark). The disrupted cells were centrifuged at 12,000 rpm. The supernatant was discarded and the precipitate was collected. The collected inclusion bodies containing preproinsulin were washed with inclusion body washing solution of various compositions of washing solution that consisted of Tris, EDTA, Triton X-100, lysozyme, and urea [10] . The washed inclusion bodies were collected by centrifugation at 12,000 rpm. The inclusion bodies containing preproinsulin were solubilized and converted to their S-sulfonated forms by oxidative sulfitolysis. The inclusion bodies were suspended in 20 mM Tris–HCl, 1 mM EDTA, and 8 M urea at a protein concentration of 10–15 mg/ml. To enhance solubility, the pH was adjusted to 11 and then readjusted to 9.5. The protein concentration was analyzed by the Bradford assay method after resolving the collected inclusion body. To start the sulfitolysis reaction, 0.2 M sodium sulfite and 20 mM sodium tetrathionate were added and the mixtures were incubated with stirring for 4 h at 25℃. HPLC analysis of S-sulfonated preproinsulin (SSPPI) production was used to optimize the reaction time. The reaction was stopped by diluting 10-fold with water and adjusting the pH to 4.5 for SSPPI precipitation. The pellets were centrifuged at 6,000 rpm, suspended in 20 ml of deionized water, and solubilized by raising the pH to 10.6. The SSPPI solution was diluted in refolding buffer (0.6M urea, 10 mM glycine, pH 10.6) containing β-mercaptoethanol. The diluted solution was mixed gently for 16 h at 15℃ and 25℃.
- Direct Refolding of Preproinsulin and Acid Precipitation
The washed inclusion bodies were solubilized in solubilization buffer (4 M urea, 10 mM glycine, pH 10.6). The solution was diluted with refolding buffer (0.6 M urea, 10 mM glycine, pH 10.6) to final protein concentrations of 0.5, 1.0, 1.5, and 2.5 g/l. Refolding was performed with various protein concentrations at various β-mercaptoethanol concentrations. The solution was incubated for 16 h at 15℃ and 25℃. The refolding kinetics were analyzed at 15℃ and 25℃. After the refolding reaction ended, the pH of the solution was adjusted to 5.5 with 5 N HCl and the sample was centrifuged at 12,000 rpm. The supernatant containing the refolded preproinsulin was collected and the precipitate was removed.
- Bioconversion of Preproinsulin into Mature Insulin Using Recombinant Carboxypeptidase B and Trypsin
Purified preproinsulin (98% purity) was obtained as described previously [27] . The refolded preproinsulin in the supernatant was collected and used as a substrate for enzymatic modification at 15℃ for 16 h. Then 0.45 unit trypsin and 0.2 unit recombinant carboxypeptidase B (CPB) [11] per 0.5 mg of the refolded preproinsulin were added into the enzyme reaction mixture. After incubation of the refolded preproinsulin at pH 8.5 for 2 h with citraconic anhydride, trypsin and CPB were added into the reaction mixture containing hydrogen peroxide. HPLC analysis was performed as described in a previous report [28] .
- Analytical Methods
Cell growth was monitored by measuring the absorbance of the culture broth at 600 nm (OD 600 ) using a spectrophotometer (Shimadzu UV-265, Japan). The glucose concentration was measured by a glucose analyzer (YSI 2700 STAT, OH, USA). Protein concentration was measured by the Bradford method.
The GRAVY (grand average of hydropathy) value was calculated by adding the hydropathy value for each residue and dividing by the length of the sequence, at gravy.html . We obtained the hydrophilicity plot of the expressed protein based on the Kyte-Doolittle-Hydropathy method using ExPASy ProtScale [12] .
Refolded preproinsulin and insulin were analyzed on an HPLC system (Alliance 2695; Waters, MA, USA) equipped with a Protein & Peptide C18 analytical column (250 mm × 4.6 mm i.d., particle size 5 μm; Vydac, USA) heated at 40℃. Solvent A was prepared with 0.5M sodium dihydrogen phosphate and 0.1M sodium perchlorate (pH 2.5) and solvent B with 100% acetonitrile. The flow rate was 1 ml/min and the gradient condition was as follows: starting with 56% solvent A and 44% solvent B mobile phase, the gradient was increased linearly to 60% solvent B in 27 min. After injection of 20 μl samples, absorbance at 214 nm wavelength was monitored by a UV detector (Waters, USA).
The human insulin preparation was lyophilized and subjected to amino acid analysis. Amino acid composition analysis and N-terminal amino acid sequencing were carried out with technical assistance from Korea Basic Science Institute (Daejeon, Korea). The amino acid composition of human insulin was analyzed by the Pico-Tag method (Waters) after hydrolysis in constant boiling with 6 M HCl containing 0.5% (w/v) phenol at 110 ℃ for 24 h. For cysteine content analysis, cysteine residues were oxidized to cysteic acid with a mixture of formic acid and hydrogen peroxide (19:1 (v/v)). In the case of tryptophan analysis, lyophilized human insulin was hydrolyzed in constant boiling with 4 M methanesulfonic acid at 110 ℃ for 24 h. The N-terminal amino acid sequences of each chain of human insulin were analyzed using an automated Edman degradation method with a Procise 491 Protein sequencing system (Applied Biosystems, CA, USA).
We performed peptide mapping analysis to confirm the identity of purified human insulin. The high-performance liquid chromatography system was equipped with a 214 nm detector and a 4.6 mm × 150 mm column that contained packing C18 reverse phase resin (Grace Vydac, USA). The flow rate was 1 ml/min. The column temperature was maintained at 40℃. Solution A (10% acetonitrile, 20% sulfate buffer, 70% water) and Solution B (40% acetonitrile, 20% sulfate buffer, 40% water) were prepared and used as mobile phases. Elution was carried out with a linear gradient of the two mobile solutions. The reference human insulin and purified recombinant human insulin were resolved with 0.01 N hydrochloric acid and transfered into a clean vial. Then 10 mM HEPES ( N -2-hydroxyethyl-piperazine- N’ -2-ethane sulfonic acid) buffer and enzyme solution ( Staphylococcus aureus V-8 protease) were added into the samples and incubated at 25℃ for 6 h. Sulfate buffer (2.0 M ammonium sulfate, 0.5 M sulfuric acid) was added to quench the reaction. Then these samples were analyzed and chromatograms of the samples were compared.
- Purification and Washing of Inclusion Bodies Containing H27R-Preproinsulin
The fermentation broth was centrifuged in order to collect the E. coli cells. The fermentation graph is depicted in Fig. 1 . The cells were resuspended in buffer solution and lysed with a high-pressure homogenizer [26] . The inclusion bodies were collected, and soluble proteins and cell debris were removed by centrifugation [17] . The separated inclusion bodies containing H27R-preproinsulin were washed with a washing solution in order to remove other components of the cell wall and membrane. The cell wall of E. coli comprises phospholipid, protein, peptidoglycan, etc. , so Triton X-100, lysozyme, and EDTA were used as washing reagents [4] . Triton X-100 can remove phospholipid [21] , and lysozyme can cleave the backbone of peptidoglycan. The action site of EDTA is the site of insertion of lipopolysaccharide (LPS) into the outer membrane [25] .
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Profiles of cell growth and preproinsulin production in fed-batch fermentation of E. coli JM109/pPT-H27Rpi.
The inclusion bodies were washed with various compositions of washing solution. The washing solution was composed of Tris, EDTA, Triton X-100, lysozyme, and urea. As shown in Table 1 , inclusion bodies were washed with five different washing solutions. The unfolded protein was refolded and analyzed in order to compare the efficiency of each washing solution. The refolding yield was 74.8% when the inclusion bodies were washed with washing solution 2 and refolded at protein concentration 1.5 g/l with 0.3 mM β-mercaptoethanol. The composition of washing solution 2 was 20 mM Tris, 1 mM EDTA, 0.02% lysozyme, 1% Triton X-100, and 0.5 M urea. After washing the inclusion bodies with washing solution, the samples were centrifuged at 12,000 rpm to collect the inclusion bodies containing H27R-preproinsulin.
Comparison of washing efficiency for inclusion body.
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aTE, 20 mM Tris buffer (1 mM EDTA, pH 7.0). bTx-100, detergent Triton X-100. cRefolding yield was calculated after pH precipitation process of refolding. dWashing solution 5 was distilled water.
- Direct Refolding of Preproinsulin
The washed inclusion body was solubilized in solubilization buffer (4 M urea, 10 mM glycine, pH 10.6). Then the solution was diluted with refolding buffer (0.6 M urea, 10 mM glycine, pH 10.6) and β-mercaptoethanol was added [24] . The solution was incubated for 16 h at 15℃ in order to refold unfolded H27R-preproinsulin. The refolding reaction was successfully completed without sulfonation. The results of refolding with various protein concentrations at different β-mercaptoethanol concentrations are summarized in Table 2 . When the refolding was carried out at 1.5 g/l of protein with 0.3 mM β-mercaptoethanol, the refolding yield was 74.2%. The optimal refolding condition of H27R-proinsulin could be optimized through many experiments. As shown in Fig. 2 , there was no difference in the peak of oxidative refolding with sulfonation and that of direct refolding based on the RP-HPLC chromatogram. Moreover, there was no difference between oxidative refolded and direct refolded preproinsulins that were subsequently converted to insulin using trypsin and recombinant carboxypeptidase B ( Fig. 3 ). Thus, the direct refolding method was successfully performed.
Comparison of refolding yield with various protein concentrations at various β-mercaptoethanol concentrations.
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aRefolding yield was calculated after pH precipitation process of refolding.
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Comparison of refolded proinsulin RP-HPLC chromatograms between oxidative refolding (dashed line) and direct refolding (solid line). The arrow indicates the refolded proinsulins.
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Reverse phase HPLC chromatogram of human insulin from preproinsulin after enzymatic conversion. Human insulin from the oxidative refolded preproinsulin (dashed line) and the direct refolded preproinsulin (solid line). The arrow indicates the human insulin.
The refolding kinetics were examined while the refolding reaction was carried out at 15℃ and 25℃. When the refolding was performed at 15℃ and 25℃, the refolding yields were 75.3% and 62.8%, respectively (data not shown). An analysis sample was collected from the direct refolding reactor at every 1.5 h over 20 h, and the results are shown in Fig. 4 A. When the effect of temperature on the refolding process was analyzed, the refolding yield at 15℃ was 17% higher than that at 25℃ but the elapsed time for refolding at 25℃ was faster than that at 15℃. The refolding process could successfully be performed even at high concentration of protein (2 g/l). The RP-HPLC chromatograms of refolding kinetics are shown in Figs. 4 B and 4 C for 15℃ and 25℃. The refolded preproinsulin (RPI), misfolded preproinsulin (peak 1), and unfolded preproinsulin (peak 2) were separated at 15.4, 18.6, and 21.0 min, respectively. We found that the peak of refolded preproinsulin at 15℃ was sharper and higher than that of refolded preproinsulin at 25℃. This indicates that refolding at 15℃ was better than that at 25℃.
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Refolding kinetics of the preproinsulin. (A) Refolding kinetics of the direct refolded preproinsulin at 15℃ and 25℃. Closed circles indicate the refolding at 25℃, and open circles indicate that at 15℃. (B) RP-HPLC chromatogram of refolding kinetics at 15℃. (C) RP-HPLC chromatogram of refolding kinetics at 25℃. The refolded preproinsulin (RPI), misfolded preproinsulin (Peak 1), and unfolded preproinsulin (Peak 2) were separated at retention times 14.4, 18.5, and 21 min, respectively. The arrow indicates the changing heights of peaks.
After the refolding reaction, the refolding solution was adjusted to pH 5.5. The misfolded preproinsulin and other impurities were removed through precipitation and centrifugation, and the supernatant containing refolded preproinsulin was collected.
- Effect of Leader Peptide on Refolding of the Fused Preproinsulin
The hydrophilicity analysis for H27R-proinsulin and Met-proinsulin were performed with amino acid sequences for two recombinant proteins (data not shown). The hydropathic results showed that the leader peptide of H27R proinsulin was hydrophilic. The GRAVY value for H27R-proinsulin was –0.36, whereas that for Met-proinsulin was –0.05. A negative value in the hydropathic score indicates a hydrophilic protein, whereas a positive value indicates a hydrophobic protein [12] . Thus H27R-proinsulin was more hydrophilic than Met-proinsulin.
- Conversion of Preproinsulin into Insulin Using Recombinant Carboxypeptidase B and Trypsin
The refolded recombinant preproinsulin was produced by the E. coli JM109/pPT-H27Rpi transformant. Recombinant carboxypeptidase B and trypsin were used in the conversion of H27R-proinsulin into insulin. The H27R (28 amino acids), leader peptide, and C-peptide were enzymatically removed from the H27R-proinsulin fusion protein. Before the enzyme reaction, H27R-proinsulin was citraconylated as described previously [28] . The products were analyzed by RP-HPLC after enzyme reaction with H27R-proinsulin. Fig. 5 shows the RP-HPLC chromatogram of enzyme reaction kinetics of H27R-proinsulins refolded at 15℃ and 25℃. The mature insulin, the intermediate, and the misfolded preproinsulin peaks appeared at retention times (RT) of approximately 9.6, 10.8, and 11.5 min, respectively. The average step yields of the nine batches are summarized in Table 3 . In nine pilot-scale batches, the average step yields for refolding, acid precipitation, and enzyme reaction were 69.7%, 99.3%, and 56.6%, respectively. The average amount of human insulin after enzyme reaction was 138.2 g from 200 L of culture broth.
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Enzyme reaction kinetics of refolded preproinsulin. Human insulin was separated at 9.6 min. (A) The human insulin peak from the refolded preproinsulin at 15℃ and (B) the human insulin peak from the refolded preproinsulin at 25℃. The arrow indicates the changing heights of peaks.
Average step yields from several pilot scale batches with H27R preproinsulin.a
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aBased on treatment of 200 L culture broth. bEach value represents the mean of nine performances ± SD. cThe value of conversion to refolded preproinsulin (51 amino acids / 112 amino acids).
- Comparison with Human Insulin Standard and Purified Human Insulin
The amino acid composition data showed that the composition of purified recombinant human insulin was in agreement with the theoretical composition and the composition of human insulin standard ( Table 4 ).
Comparison of amino acid composition of purified human insulin, reference human insulin, and theoretical pancreatic human insulin.
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Comparison of amino acid composition of purified human insulin, reference human insulin, and theoretical pancreatic human insulin.
Peptide mapping analysis is usually used to compare the protein structure of protein product with that of a reference material. The peptide map chromatogram of purified human insulin was performed by cleaving the subunits into some number of small fragments by cutting with endopeptidase Glu C, which specifically digests the protein at the C-terminus of glutamate. The cutting samples were separated on a RP-HPLC column with on-line UV monitoring. Fig. 6 shows chromatograms of human insulin standard and purified human insulin. Four fragments were detected in cutting of the standard and purified human insulins with endopeptidase Glu C. Fragment I contains the peptides from A5 to A17 and from B1 to B13. Fragment II contains the peptides from A18 to A21 and from B14 to B21. Fragment III contains the peptide from B22 to B30. Fragment IV contains the peptide from A1 to A4. The peptide map chromatogram of purified human insulin was found to be in agreement with that of the human insulin standard.
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Peptide map chromatograms of (A) standard and (B) purified human insulin by Glu-C protease. Fragment I (retention time (RT) 53 min): amino acids A5 to A17 and B1 to B13. Fragment II (RT 21 min): amino acids A18 to A21 and B14 to B21. Fragment III (RT 17 min): amino acids B22 to B30. Fragment IV (RT 4 min): amino acids A1 to A4.
This experiment was performed in order to decrease the refolding volume and increase the refolding yield. To slow down the aggregation process, refolding is usually performed at low protein concentrations, in a range of 10-100 μg/ml [14] . Before the optimal refolding condition was established in this study, the refolding reaction was performed with 0.5 g/l of protein and 0.1 mM β-mercaptoethanol. The demerit of performance of refolding at 0.5 g/l of protein was that the volume of refolding solution was very large. However, when the refolding was carried out at 1.5 g/l of protein with 0.3 mM β-mercaptoethanol, it was possible to considerably decrease the volume of refolding solution. In addition to the decrease of the volume of refolding solution, the refolding yield was increased by optimization of the refolding conditions for H27R-proinsulin. It is difficult to set up the refolding reaction conditions for specific proteins, because the refolding reaction is very dynamic. In this study, we set the optimal refolding conditions for H27R-proinsulin and confirmed the identity of refolded H27R-proinsulin and mature human insulin after enzyme reaction using RPHPLC. We checked the hydropathic score of the expressed preproinsulin compared with proinsulin. A negative hydropathic score indicates a hydrophilic protein, whereas a positive value indicates a hydrophobic protein. The addition of the leader peptide, H27R, on the proinsulin resulted in a more hydrophilic expressed preproinsulin. It is possible to make H27R-proinsulin more soluble and for it to be refolded without sulfonation. Using the direct refolding method, it is possible to decrease the total volume of refolding solution, to decrease the number of process steps for production of human insulin, and to increase the total production yield. Therefore, this production process may be a more viable process for human insulin production. After the enzyme reaction, 138.2 g of human insulin was produced from 200 L of fermentation broth using the production process. Thus, 0.691 g of human insulin was produced from 1 L of fermentation broth. It was confirmed that the purified recombinant human insulin was the same as human insulin standard.
In conclusion, the optimal refolding condition for H27Rproinsulin was 1.5 g/l of protein, 0.3 mM β-mercaptoethanol, 0.6 M urea, 10 mM glycine, and pH 10.6 at 15℃ for 16 h. The leader peptide of H27R-proinsulin was more hydrophilic than Met-proinsulin. Therefore, direct refolding of H27Rproinsulin was possible without sulfonation. The average amount of produced human insulin was 138.2 g from a 200 L pilot-scale fermentation broth.
This study was financially supported by the Ministry of Education(MOE) and National Research Foundation of Korea(NRF) through the Human Resource Training Project for Regional Innovation(2015H1C1A1035828) and Sangji University Research Fund, 2014.
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