- Open Access
Influence of production process design on inclusion bodies protein: the case of an Antarctic flavohemoglobin
© Parrilli et al; licensee BioMed Central Ltd. 2010
- Received: 29 October 2009
- Accepted: 24 March 2010
- Published: 24 March 2010
Protein over-production in Escherichia coli often results in formation of inclusion bodies (IBs). Some recent reports have shown that the aggregation into IBs does not necessarily mean that the target protein is inactivated and that IBs may contain a high proportion of correctly folded protein. This proportion is variable depending on the protein itself, the genetic background of the producing cells and the expression temperature. In this paper we have evaluated the influence of other production process parameters on the quality of an inclusion bodies protein.
The present paper describes the recombinant production in Escherichia coli of the flavohemoglobin from the Antarctic bacterium Pseudoalteromonas haloplanktis TAC125. Flavohemoglobins are multidomain proteins requiring FAD and heme cofactors. The production was carried out in several different experimental setups differing in bioreactor geometry, oxygen supply and the presence of a nitrosating compound. In all production processes, the recombinant protein accumulates in IBs, from which it was solubilized in non-denaturing conditions. Comparing structural properties of the solubilized flavohemoglobins, i.e. deriving from the different process designs, our data demonstrated that the protein preparations differ significantly in the presence of cofactors (heme and FAD) and as far as their secondary and tertiary structure content is concerned.
Data reported in this paper demonstrate that other production process parameters, besides growth temperature, can influence the structure of a recombinant product that accumulates in IBs. To the best of our knowledge, this is the first reported example in which the structural properties of a protein solubilized from inclusion bodies have been correlated to the production process design.
- Inclusion Body
- Tryptophan Residue
- Dissolve Oxygen Tension
- Microaerophilic Condition
- Production Process Design
Protein over-production in Escherichia coli (E. coli) often results in formation of inclusion bodies (IBs). Aggregation most probably occurs as a consequence of interactions among the newly-formed folding intermediates which expose hydrophobic residues at their surface . For a long time it was believed that IBs were compact, insoluble aggregates of misfolded proteins , remaining in the cell as biologically inactive deposits.
However, some recent reports have shown that the aggregation into IBs does not necessarily mean that the target protein is inactivated [3, 4]. Structural data collected from many model proteins revealed the presence of significant proportions of native-like secondary structure in IBs proteins [5, 6]. Consequently, it is not surprising that the analysis of the biological properties of IBs formed by enzymes demonstrated in some cases the occurrence of enzymatic activity inside the IBs [3, 7]. These evidences introduced the concept that IBs are composed, at least partially, by functional polypeptides, whose deposition is necessarily driven by discrete aggregation determinants, that act irrespective of the global folding state of the protein . It has been observed that IBs containing a high proportion of correctly folded protein can be easily solubilized under non-denaturing conditions  by using mild detergents or polar solvents, widely preserving the target protein folding.
The prevalence and extent of native structure and biological activity of IB proteins is variable depending on the protein itself, the genetic background of the producing cells and the expression temperature [6, 10].
Flavohemoglobins (flavoHbs) have been identified in a number of bacteria and yeasts . These proteins are characterized by a modular structure, where a N-terminal hemoglobin domain, displaying a classical three-over-three α-helical sandwich motif around a single heme b , is linked to a C-terminal FAD-containing reductase domain which resembles ferredoxin reductase . The flavoHbs C-terminal domain binds NAD(P)H and transfers electrons to the heme in the globin domain via FAD [14, 15].
A flavoHb encoding gene (PSHAa2880) was identified by in silico genome analysis of the Antarctic Gram-negative marine eubacterium Pseudoalteromonas haloplanktis TAC125 (P. haloplanktis TAC125) . In the present paper, the recombinant production of the psychrophilic flavoHb (hereinafter called Ph flavoHb) in E. coli cells was carried out in several different experimental setups in order to identify the best production condition. Indeed, previously reported results on E. coli flavoHb demonstrated that the heterologous over-production of flavoHb may lead to host cell damage due to the action of flavoHb as a potent generator of products of oxygen radical partial reduction (i.e., superoxide and peroxide) [23–25]. Due to the expected toxicity of the recombinant product, flavoHb recombinant productions were carried out exploring several expression systems and/or microbial cell factories, with different results . Amongst many other examples reported in literature, recombinant production of E. coli flavoHb in E. coli was obtained in absence of oxygen and in presence of nitrosating compound, an experimental setup in which the hmp gene expression is physiologic and the flavoHb activity is required .
Starting from the above information, in the present work, the recombinant production of the flavoHb from the Antarctic Gram-negative bacterium P. haloplanktis TAC125  was performed in E. coli cells exploring some conditions differing in presence of a nitrosating compound and in O2 supply.
All production processes resulted in the accumulation of the recombinant protein in IBs, from which it was solubilized in non-denaturing conditions. Comparing structural properties of the solubilized Ph flavoHbs, i.e. deriving from the different production processes, our data demonstrated that the protein preparations differ significantly in the presence of cofactors (heme and FAD) and in their secondary and tertiary structure, demonstrating the impact of the specific production process design on the quality of inclusion bodies protein.
Recombinant production of P. haloplanktis TAC125 flavohemoglobin in E. coli cells resulted in full deposition of the protein in the inclusion bodies
The PSHAa2880 gene was PCR amplified to suitably introduce NdeI and SalI restriction sites, and cloned into pET22b vector corresponding sites, thus generating the recombinant pET22b-2880 plasmid.
E. coli BL21(DE3) cells were transformed with the recombinant vector and, keeping in mind that proteins coming from psychrophilic micro-organisms are often characterized by a moderate to extreme thermal-lability , the production of the Ph flavoHb was carried out at 20°C. However, two different production process setups were explored. First, E. coli BL21(DE3)(pET22b-2880) recombinant cells were grown in a 7.5 L automatic fermenter, in which the recombinant mesophilic cells were grown aerobically at 20°C till the culture density reached the value of 0.6 OD at 600 nm. Induction was then performed by IPTG, in the following conditions: i) addition of heme and FAD precursors (i.e. D-aminolevulinic acid, FeCl3, and riboflavin); ii) addition of the nitrosating compound sodium nitroprusside (SNP), and iii) in microaerophilic conditions (dissolved oxygen tension always below 5% of saturation). Microareophilic conditions were achieved by stopping air supply during the next 16-18 hr of fermentation. The second experimental condition consisted in growing recombinant cells in shake flask at 20°C until the culture absorbance at 600 nm reached 0.6 OD, when the protein production was induced in the same conditions as in automatic fermenter but without SNP and in aerobic conditions.
Then, cells coming from the above production processes were analyzed looking for production and soluble/insoluble distribution of the recombinant protein by cell fractionation followed by SDS-PAGE analysis. Both production processes resulted in the total deposition of recombinant flavohemoglobin as cytosolic inclusion bodies (IBs), that were called flask-flavoHb IBs and ferm-flavoHb IBs if derived from cells grown in shake flasks or in fermenter, respectively.
Recombinant P. haloplanktis TAC125 flavohemoglobin is solubilized from inclusion bodies by non-denaturing solutions
Percentage of solubilization of IBs in different solvents
% solubilized protein
0.5% Triton X-100 in 40 mM Tris/HCl, pH 8.0
8 ± 0.6
10 ± 0.9
5% DMSO in 40 mM Tris/HCl, pH 8.0
9 ± 0.9
5 ± 0.4
5% di n-propanol in 40 mM Tris/HCl, pH 8.0
6 ± 0.7
5 ± 0.1
0.2% N-lauroyl sarcosine in 40 mM Tris/HCl, pH 8.0
95 ± 1.0
57 ± 0.8
1% Na-deoxycholate in 40 mM Tris/HCl, pH 8.0
22 ± 1.5
12 ± 0.3
The two solubilized IBs preparations also differ in their respective protein composition. As shown in figure 1, flask-flavoHb IBs seems to contain several proteins other than flavoHb (panel B), while IBs produced in fermenter contains almost only the psychrophilic recombinant protein (panel A).
Structural comparison of recombinant P. haloplanktis TAC125 ferm- and flask-flavoHb
Flavohemoglobins extracted from either flask-flavoHb IBs (flask-flavoHb) or ferm-flavoHb IBs (ferm-flavoHb) were subjected to further analyses to investigate the presence of the two protein cofactors, i.e. heme and FAD.
Percentage of calculated secondary structures of ferm-flavoHb and flask-flavoHb
Estimation of protein secondary structure from CD spectra by K2d
Influence of different process parameters on inclusion bodies protein
Several recent reports have shown that IBs could contain proteins that posses a native-like secondary structure and an enzymatic activity [3, 5–7]. Moreover, it has been reported that IBs containing a high proportion of correctly folded protein can be easily solubilized under non-denaturing conditions 
In this paper we report a case in which using different process designs, we always obtained the complete accumulation of the recombinant proteins in IBs, from which the products were easily solubilized under non-denaturing conditions. Although their common attitude to get solubilized, recombinant proteins deriving from the different production processes differ in presence of cofactors and in their secondary and tertiary structure. In detail, we produced the flavohemoglobin from the Antarctic Gram-negative bacterium P. haloplanktis TAC125  in E. coli cells in fermenter in the presence of a nitrosating compound (the SNP) and in microaerobiosis. In parallel, Ph flavoHb was produced in E. coli recombinant cells in standard conditions, i.e. grown in shake flasks by an aerobic production scheme and in absence of SNP. Both processes, carried out at 20°C, resulted in the total accumulation of the recombinant protein in cytoplasmic inclusion bodies. The treatment of ferm-flavoHb IBs and flask-flavoHb IBs with a N-lauroyl sarcosine solution highlighted unexpected differences in i) the solubilization yield, and ii) the composition of the solubilized matter. This evidence prompted us to carry out a structural comparison of the two recombinant Ph flavoHbs, in order to assess if the production setup could influence the main structural features of IBs proteins. Data reported in the present paper demonstrate that the two proteins differ significantly, mainly in the presence of FAD and heme cofactors. Indeed, when subjected to suitable spectroscopic analyses, proofs of the presence of heme and FAD were collected only in the case of ferm-flavoHb. Furthermore, CD spectra demonstrate that both proteins possess a secondary structure, but the ferm-flavoHb content of alpha-helix and beta-sheets is higher than that observed in the protein produced in flask.
Taking advantage from the presence of three tryptophan residues along the Ph flavoHb protein sequence, fluorescence emission spectra of tryptophan residues were recorded. Both spectra are characterized by a λmax emission signal around 338 nm, a result indicative that the Trp residues are not exposed to the solvent. Indeed, in these experimental conditions, unfolded proteins usually present a shift of λmaxtowards 350 nm. As expected, when the proteins were chemically denatured by guanidinium chloride, a shift of the λmax emission signal was observed (new maximum at 366 nm, data not shown). These data are highly suggestive that both proteins display a 3D structure, although likely not identical. In fact, fluorescence intensity at λmax of flask-flavoHb is about three times higher than that of the protein produced in fermenter. This different spectroscopic behaviour is not justified by the likely quenching effect of FAD cofactor associated only to the ferm-flavoHb. Therefore, the observed difference in intensity of λmax signal could be due to some amino acids residues close to tryptophan residues that work as fluorescence quencher in ferm-flavoHb. These results are suggestive of a different chemical surrounding around the tryptophan residues in flask-flavoHb and ferm-flavoHb proteins, thus supporting the conclusion that the two proteins differ in 3D structure too.
Furthermore, a systematic approach was applied to understand which process parameter was crucial for obtaining a protein endowed with FAD and heme cofactors. It turned out that the synergic effect of microareophilic growth conditions and the presence of SNP was essential. This experimental setup likely mimics the physiologic conditions in which flavoHb activity is required. The occurrence of a suitable physical-chemical environment and/or the induction of specific protein chaperones could justify the unique cofactors incorporation observed.
Without a structural/functional characterization of native Ph flavoHb, a final assessment on the quality of the recombinant proteins produced in this work cannot be formulated. However, the presence of FAD and heme cofactors, together with the collected indirect evidences of a different secondary and, eventually, tertiary structures, looks very promising of a better quality of flavoHb obtained in the presence of a nitrosating compound and in microaerobiosis.
The present paper describes the recombinant production of a flavohemoglobin, a multidomain protein requiring FAD and heme cofactors for its activity. Two significantly different production process designs were explored, both resulting in the full product accumulation in IBs. Data reported here demonstrate that other process parameters, besides growth temperature, influence the quality of a recombinant product even if it accumulates in IBs. To the best of our knowledge, this is the first reported example in which the quality of protein solubilized from inclusion bodies has been correlated to the production process design.
Bacterial strains, plasmid and culture condition
The E. coli BL21(DE3) (Novagen) strain was routinely used for cloning and expressing recombinant gene. Cells were grown in Luria-Bertani (LB) medium at 20°C. When required, ampicillin (Sigma) was added at 100 μg/ml. Plasmid pET-22b (Novagen) was utilized for cloning and expression. Restriction and modifying enzymes were obtained from Promega. The oligonucleotides were custom synthesized from PRIMM.
Cloning of the PSHAa2880gene
The primer pairs for the PSHAa2880 gene (Oligo 2880 fw 5' TTCATATGTTATCTGATAAAACTATTGAAA 3', Oligo 2880 rv 5' AAGTCGACTTATAGATCTTGATGCGG 3') were designed on the basis of the P. haloplanktis TAC125-genome sequence . Sequences corresponding to the Nde I site and a Sal I site were introduced in the forward and reverse primers, respectively. The amplifications were performed in a mixture containing 80 ng of P. haloplanktis TAC125-genomic DNA as template, 50 pmol of each oligonucleotide primer, 1.8 mM MgCl2, 50 mM KCl, 20 mM Tris-HCl pH 8.3, 0.1% gelatine, 200 μM dNTP in a final volume of 50 μl. The mixtures were incubated at 95°C for 10 min, then 1.25 units of Taq DNA polymerase were added. Twenty cycles of amplification (consisting of 1 min at 95°C, 1.5 min at 60°C and 1 min plus 5 sec/cycle at 72°C) were carried out and followed by a cycle in which the extension reaction at 72°C was prolonged for 15 min in order to complete DNA synthesis. The amplified fragment was cloned and its nucleotide sequence checked to rule out the occurrence of any mutation during synthesis. The Nde I-Sal I-digested fragment of the PSHAa2880 gene was then subcloned into the corresponding sites of the expression vector pET-22b, obtaining the plasmid pET22b-2880. The recombinant vector was used to transform E. coli BL21(DE3) cells, that were used for the following production processes. All DNA manipulation were performed as previously described 
Shake Flask Culture
For the over-expression of cold-adapted flavoHb in flask, a single colony of recombinant E. coli BL21(DE3) (pET22b-2880) was inoculated in LB medium supplemented with 4 g/L glucose and ampicillin (100 μg/ml) and allowed to grow at 20°C, in the rotary shaker, until absorbance at 600 nm reached ~0.6 OD. The culture was then induced with 1 mM isopropyl-β-D-thiogalactopyranoside and further incubated for another 16-18 h at 20°C in the presence of 50 μM of D-aminolevulinic acid, 3 μM FeCl3, 100 μM riboflavin. After production, the cell culture was aliquoted, centrifuged, and the supernatant was discarded. The bacterial pellet was stored for further analysis.
A proper preinoculum of overnight grown recombinant E. coli BL21(DE3) (pET22b-2880) was diluted in 4.5 L of LB medium supplemented with 4 g/L glucose and ampicillin (100 μg/ml) in a 7.5-L Techfors S (Infors, HT Switzerland) automatic fermenter. Cells were grown aerobically at 20°C till the culture density reached the value of 0.6 OD at 600 nm. Induction was then performed by 1 mM IPTG, in the presence of 50 μM mM D-aminolevulinic acid, 3 μM FeCl3, 100 μM riboflavin and 0.4 mM sodium nitroprusside (SNP). Then, air supply was stopped during the next 16-18 hr of fermentation keeping a microaerophilic conditions (dissolved oxygen tension always below 5% of saturation).
In case of production of the Ph flavoHb in aerobic condition with and without SNP the preinoculum of overnight grown recombinant E. coli BL21(DE3) (pET22b-2880) was diluted in 2.5 L of medium and dissolved oxygen tension was maintained always above 30% of saturation.
After production, the cell culture was collected, centrifuged, and the supernatant was discarded. The bacterial pellet was stored for further analysis.
Protein inclusion bodies extraction
Biomass was harvested at the end of the production process by centrifugation, and the wet bacterial pellet was re-suspended in 10 mM Tris/HCl, pH 8.0. Samples were kept on ice and disrupted by sonication using an Branson sonicator (Model B-15), using a program consisting of 20 cycles (30" on, 60" off, intensity 4.5). After disruption of the cells, samples were centrifuged at 5000 rpm for 30 min at a constant temperature of 4°C. The supernatant was discarded, and the inclusion bodies fraction was washed twice with chilled water, divided in several aliquots and incubated overnight for the solubilization at 4°C in 40 mM Tris/HCl, pH 8.0 buffer containing alternatively:
0.5% Triton X-100;
0.2% N-lauroyl sarcosine.
As negative control the insoluble matter was treated with water. After the incubation, the suspensions were centrifuged at 4400 × g for 15 minutes at 4°C. The supernatants were analyzed by SDS-PAGE.
Protein concentration measurements
The Bradford method  was applied to determine protein concentration. In case of protein solubilized from IBs with different solvents a qualitative measure of protein content was determined by measuring the amount of light absorbed at 280 nm (Abs280).
UV-Vis absorption spectra were recorded in UNIKON 930 spectrophotometer. Fluorescence measurements were carried out in a PERKIN ELMER LS 50B fluorospectrometer. Circular dichroism (CD) spectra were obtained in a Jasco spectropolarimeter (model J-715) equipped with a thermostatically controlled cell holder.
We are grateful to Prof. Leila Birolo (Dipartimento di Chimica Organica e Biochimica, Università degli Studi di Napoli Federico II Napoli Italia) for critical reading of the manuscript and very helpful discussions. Thank to Rosaria Varlese for her excellent technical support with the fermentation units. This work was supported by grant of Programma Nazionale di Ricerca in Antartide 2004 (Prof. Marino) and Ministero dell'Università e della Ricerca Scientifica (Progetti di Rilevante Interesse Nazionale 2007 - Prof. Di Donato).
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