LT7069B - Cell culture method - Google Patents

Abstract

The invention provides a method for producing a clarified cell culture comprising a recombinant protein, wherein the method comprises: i) inoculating a bioreactor with a host cell to provide a cell culture, wherein said host cell is an Escherichia coli transformed with an expression system comprising: a) a nucleic acid encoding a recombinant protein operably linked to a first inducible promotor; and b) a nucleic acid encoding a T4 lysozyme protein in frame with a nucleic acid encoding PelB secretory signal peptide operably linked to a second inducible promotor, ii) fermenting the cell culture under conditions that: a) allow the expression of the recombinant protein; and b) allow permeabilization of the cell so as to form a spheroplast that secretes the recombinant protein; iii) clarifying the fermented cell culture comprising the secreted recombinant protein, wherein said clarifying comprises a primary clarification step using a first clarification filter having a pore size that provides a retention range of at least about 0.4 μm or more, wherein the clarification step does not comprise centrifugation.

Description

TECHNICAL FIELD

The present invention relates to a system for expressing recombinant proteins using E. coli.

STATE OF THE ART

Escherichia coli is a frequently chosen microorganism for the production of recombinant proteins. The main reasons for this popularity are the high growth rates and resolution levels, as well as the simple and inexpensive culture media required. However, E. coli is a poor protein secreter, and methods for intracellular protein production using E. coli require cell disruption and removal of cellular debris. In contrast, cellular production of recombinant proteins and enzymes greatly reduces the complexity of the bioprocess production method and improves the quality of the recombinant product, while simplifying protein detection and purification. Furthermore, an environment free of cell-associated proteolytic degradation has been shown to provide an optimal environment for the formation of protein spatial structures.

Various technologies can be used to facilitate the production of intracellular proteins from E. coli. Typically, the initial steps of these methods involve lysing or disrupting bacterial cells to disrupt the bacterial cell wall and release cellular proteins into the extracellular environment. After this release, the required proteins are purified from the extracts, usually by several chromatographic steps.

Several methods have been shown to be useful for the release of intracellular proteins from bacterial cells. These include the use of chemical lysing, physical disruption methods, or a combination of chemical and physical methods (Felix, H., Anai. Biochem. 120:211-234 (1982)).

Chemical methods of disrupting bacterial cell walls that have proven suitable include treating the cells with organic solvents such as toluene (Putnam, S.L., and Koch, A.L., Anai. Biochem. 63:350-360 (1975); Laurent, S.J., and Vannier , F. S., Biochimie 59:747-750 (1977); Felix, H., Biochem. 120:211-234 (1982)) by chaotropes such as guanidine salts (Hettwer, D., Biotechnol. Bioeng. 33:886-895 (1989)), antibiotics such as polymyxin B (Schupp, J.M., et al., BioTechniques 19:18-20 (1995); Felix, H., Anai. Biochem. 120:211 -234 (1982)), or enzymes such as lysozyme or lysostaphin (McHenty, C.S., and Kornberg, A., J. Biol. Chem. 252(18):6478-6484 (1977); Cull, M., and McHenry, C.S., Meth. 182:147-153;Hughes, J., Suppl. 016 (1992); , et al., in Molecular Cloning: A Laboratory Manual, 2nd ed., Cold Spring Harbor, N.Y.: Cold Spring Harbor Laboratory Press (1989), pp. 17-38; Ausubel, F.M., et al., in Current Protocols in Molecular Biology, New York: John Wiley & Sons (1993), pp. 4.4.1-4.47). The effects of these various chemicals can be enhanced by simultaneously treating the bacterial cells with detergents such as Triton X-100®, sodium dodecyl sulfate (SDS) or Brij 35 (Laurent, S.J., and Vannier, F.S., Biochimie 59:747-750 (1977) ; Felix, H., Biochem. 120:211234; Hettwer, H., Bioeng., 33:886-895 (1989). , Meth. Enzymol. 182:147-153 (1990); Schupp, J.M., et al., BioTechniques 19:18-20 (1995)), or proteins or protamines such as bovine serum albumin or spermidine (McHenry, C.H. and Kornberg, A. Biol. 252(1977); Anai. Biochem. 1982 ., J. Cell Biochem. Suppl. 0 16 (Part B):84 (1992)).

In addition to these various chemical treatments, several physical degradation methods have been used. These physical methods include osmotic shock, such as suspension of cells in a hypotonic solution in the presence or absence of emulsifiers (Roberts, J.D., and Lieberman, M.W., Biochemistry 18:4499-4505(1979); Felix, H., Anai. Biochem. 120 :211-234(1982)), drying (Mowshowitz, D.B., Anai. Biochem. 70:94-99 (1976)), mixing with granules such as ball milling (Felix, H., Anai. Biochem. 120: 211234 (1982); Cull, M., and McHenry, Meth. Enzymol. 182:182:147-153 (1990)), e.g. freeze-thaw cycles (Lazzarini, R. A., Nature New Biol. 243:17-20 (1975); Felix, H., Biochem. 120:211-234 (1982) sonication (Amos, H., et al., J. Bacteriol. 94: 232-240 (1967); Ausubel, F. M., et al., in Current Protocols in Molecular Biology, New York, John Wiley & Sons (1993), pp. 4.4.1-4.47) using a French press pressure chamber (Ausubel, F. M., et al., in Current Protocols in Molecular Biology, New York, John Wiley & Sons (1993), pp. 16.8.6-16.8.8). Other methods combine these chemical and physical disruption methods, such as lysozyme treatment followed by sonication or pressure to maximize cell disruption and protein release (Ausubel, F. M., et al., in Current Protocols in Molecular Biology, New York , John Wiley & Sons (1993), pp. 4.4.1 -4.47).

These disruption methods have several advantages, including their ability to rapidly and completely disrupt bacterial cells in a way that maximizes the release of intracellular proteins.

However, these methods also have distinct drawbacks. For example, physical methods essentially involve tearing and breaking down bacterial cell walls and plasma membranes. These processes result in extracts that contain many solids, such as membrane or cell wall fragments, which must be removed from the extracts by conventional centrifugation before the recombinant proteins can be purified. This need for centrifugation limits the size of the batch that can be processed at one time to the size of the available centrifuge volume; thus, large-scale production preparations are impractical, if not impossible. In addition, physical methods and many chemical methods usually lead to the release of not only desired intracellular proteins, but also unwanted nucleic acids and membrane lipids from cells (the latter especially occur when organic solvents are used). These unwanted cellular components also complicate subsequent purification processes of desired proteins by increasing the viscosity of the extracts (Sambrook, J., et al., in: Molecular Cloning: A Laboratory Manual, 2nd ed., Cold Spring Harbor, N.Y.: Cold Spring Harbor Laboratory Press (1989), pp 17-38; Cull, C.S., Meth. Enzymol. 182:147-153 (1990)) and binds with high avidity and affinity to nucleic acid modifying proteins such as DNA polymerases. RNA polymerases and restriction enzymes.

Naturally occurring lytic and symbiotic bacteriophages have the ability to induce host cell lysis by expressing specific proteins during the lytic cycle. These lysing proteins have been identified and extensively studied, for example, in T4 and T7 bacteriophages. Lysing proteins include both holins and lysozymes. Cholins form stable and non-specific lesions in the cytoplasmic membrane, which allow lysozymes to enter the peptidoglycan layer. Lysozymes exhibit muralis activity against three different types of covalent bonds (glycosidic, amide and peptide) in the peptidoglycan polymer of the cell wall. Together, the activity of choline and lysozyme disrupts the two cell membranes of gram-negative bacteria, thereby causing cell lysis.

E. coli was engineered to express T4 bacteriophage lysis proteins to provide programmed cell lysis to improve the downstream efficiency and cost-effectiveness of recombinant protein production (M. Morita, K. Asami, Y. Tanji, and H. Unno, "Programmed Escherichia coli Cell Lysis by Expression of Cloned T4 Phage Lysis Genes," Biotechnology Progress , vol. 3, pp. 573-576, 2001).

Escherichia coli-based constructs are the gold standard for the production of recombinant proteins where post-translational modifications are unnecessary. The main reasons for the popularity of E. coli are its high growth rates and expression levels, as well as its simple and inexpensive culture media.

However, E. coli is not a perfect host because it does not normally secrete proteins into the extracellular medium. Thus, one problem with methods using E. coli is that the cell disruption step becomes limiting and is not cost-effective on a pilot or industrial scale when implementing a closed and/or continuous process.

One problem with these methods is that the resulting recombinant proteins usually contain impurities. This is, for example, a problem in the production of nucleic acid-modifying enzymes, as enzyme preparations are typically contaminated with nucleic acids (eg, RNA and DNA). This phemeric nucleic acid can come not only from the organisms that are the source of the enzyme, but also from unknown organisms present in the reagents and materials used to purify the enzyme after its release from the cells. This is particularly true for reverse transcriptase or DNA polymerase enzymes, as they are commonly used in nucleic acid molecule amplification and synthesis methods (eg polymerase chain reaction (PCR), especially RT-PCR). In such a sample, the presence of contaminating DNA or RNA in enzyme preparations is a major problem, as it can lead to false amplification or synthesis results. In addition, with the growing demand for enzymes as biocatalysts in pharmaceuticals, additional requirements are placed on the quality of enzyme preparations, such as specificity, consistency when passing from one series to another, the absence of impurities of animal origin and antibiotics, which must necessarily meet regulatory requirements.

Thus, there remains a need for methods of producing recombinant proteins comprising E. coli that are substantially free of impurities such as nucleic acids. These techniques can eliminate the risk of contamination, for example from the environment and personnel, and enable a faster and parallel production process in a single-process facility.

BRIEF DESCRIPTION OF THE INVENTION

According to the present invention, there is provided a method for producing a clarified cell culture comprising a recombinant protein, wherein the method comprises:

(i) inoculating the bioreactor with a host cell to obtain a cell culture, wherein said host cell is Escherichia coli, a transformed expression system comprising:

(a) a nucleic acid encoding a recombinant protein operably linked to a first inducible promoter, wherein the protein is 2-O-methyltransferase (OMT); and

b) a nucleic acid encoding a T4 lysozyme protein in frame with a nucleic acid encoding a PelB secretory signal peptide operably linked to a second inducible promoter;

(ii) cell culture fermentation under conditions which:

(a) enables expression of the recombinant polypeptide; and

b) allowing penetration into the cell to form a spheroplast secreting the recombinant polypeptide, wherein said fermentation step comprises adding a stabilizing agent to the cell culture;

iii) purification of the fermented cell culture comprising the secreted recombinant protein, wherein said purification comprises:

a) adding a flocculating agent to the cell culture, wherein the flocculating agent is polyethyleneimine (PEI);

b) a pre-clarification step of the flocculated cell culture using a first clarification filter having a pore size of at least about 0.4 µm or greater retention limits, wherein the clarification step does not include centrifugation.

Conveniently, in the methods of the present invention, the method further comprises a secondary clarification step using a second filter having a pore size that provides retention limits of at least about 0.22 um.

Suitably, in the methods of the present invention, the primary clarification step uses a first filter having a pore size that provides retention limits of at least about 0.4 to about 0.8 pm.

Suitably, in the methods of the present invention, the secondary clarification step uses a second filter having a pore size of at least about 0.4-0.8 pm, or at least about 1.0 to about 3.0 pm retention limits.

Suitably, in the methods of the present invention, the primary clarification step and/or the secondary clarification step is microfiltration, wherein the microfiltration is optionally depth filtration.

Suitably, in the methods of the present invention, microfiltration is selected from normal flow filtration (NFF) or tangential flow filtration (TFF).

Suitably, in the methods of the present invention, the clarified cell culture has a turbidity of less than about 20 NTU.

Conveniently, in the methods of the present invention, the process is carried out in a closed system such that a sterile flow is maintained between the bioreactor and the first and second clarification filters.

Conveniently, in the methods of the present invention, the process also includes the step of subjecting said clarified cell culture to one or more of the purification steps of said recombinant protein.

Suitably, in the methods of the present invention, the stabilizing agent comprises sucrose, Na2SO4 and Brij 35, optionally 1 M sucrose, 0.5 M Na2SO4 and 0.5% Brij 35.

The present invention also provides a method of producing a protein comprising:

(i) culturing a recombinant Escherichia coli cell under conditions which:

(a) enables expression of the protein; and

(b) enables cell penetration to form a spheroplast that secretes the recombinant polypeptide; and (ii) isolating the protein from the culture without complete knockdown of the recombinant cell, wherein the cell comprises an expression system comprising:

(a) a nucleic acid encoding a protein operably linked to a first inducible promoter, wherein the protein is 2-O-methyltransferase (OMT); and

(b) a nucleic acid encoding a T4 lysozyme protein in frame with a nucleic acid encoding a PelB secretory signal peptide operably linked to a second inducible promoter.

Suitably, the methods of the invention do not include: (i) mechanical cell disruption; (ii) addition of an exogenous enzyme that degrades the cell wall; and (iii) transforming the cell with expression vectors containing a nucleic acid encoding an exogenous enzyme that disrupts the cytoplasmic membrane.

Conveniently, in the methods of the present invention, the nucleic acid encoding the protein operably linked to the first inducible promoter is present in the first construct, and the nucleic acid encoding T4 lysozyme in frame with the nucleic acid encoding the PelB secretory signal peptide is present in the second construct.

Conveniently, in the methods of the present invention, the first inducible promoter and the second inducible promoter are induced sequentially.

Conveniently, in the methods of the present invention, the first inducible promoter and the second inducible promoter are simultaneously induced.

Suitably, in the methods of the present invention, the first inducible promoter is an IPTG-inducible promoter, optionally wherein the IPTG-inducible promoter is PT7.

Suitably, in the methods of the present invention, the second inducible promoter is an arabinose-inducible promoter, wherein optionally the arabinose-inducible promoter is araB.

Conveniently, in the methods of the present invention, the T4 lysozyme enzyme is encoded by the gene E.

Suitably, in the methods of the present invention, the E. coli is Escherichia coli JS007 strain or Escherichia coli B strain.

Suitably, in the methods of the present invention, the fermentation or culturing comprises changing the temperature from a first temperature to a second temperature, wherein optionally the second temperature is lower than the first temperature.

The invention also provides a recombinant protein produced using the methods of the invention.

BRIEF DESCRIPTION OF THE DRAWINGS

Embodiments of the invention are described below with reference to the accompanying drawings, in which:

the plasmid structures are shown in the figure: (A) target gene expression vector pLATE31-VP39delta32-KnR, (B) T4 gene gpe expression vector pACYC184PT7-pelB-gpe-lacl.

the figure shows a microscopic image of E. coli cells before and after induction of gpe gene expression.

the figure shows a 12% SDS-PAGE gel of E. coli JS007/ pLATE31-VP39delta32-KnR/pACYCPT7-pelB-gpe-lacl cultured cell extract and media samples after induction of 2-O-methyltransferase. (1, 7 and 13) PageRuler™ Plus Prestained Protein Ladder, 10-250 kDa (Thermo Fisher); (2) cell sample after 1 h induction of protein synthesis; (3) cell sample after 2 h induction of protein synthesis; (4) cell sample after 3 h induction of protein synthesis; (5) cell sample after 5 h induction of protein synthesis; (6) cell sample after 17 h induction of protein synthesis; (8) medium sample after 1 h induction of protein synthesis; (9) medium sample after 2 h induction of protein synthesis; (10) medium sample after 3 h induction of protein synthesis; (11) medium sample after 5 h induction of protein synthesis; (12) medium sample after 17 h induction of protein synthesis; 2-O-methyltransferase released into the medium is marked with an arrow.

the figure shows the resolution of the OMT shown in the Biostat bioreactor.

Figure 1 shows a comparison of the growth dynamics of OMT culture in Biostat A bioreactor systems (4 days and overnight feeding (OV) time).

the figure shows a comparison of the dynamics of OMT activity in Biostat A bioreactor systems without autolysis and with autolysis (4 days and overnight feeding (OV) time).

Figure 1 shows a schematic of the purification process used to obtain various recombinant proteins such as OMT (2-O-methyltransferase).

DETAILED DESCRIPTION

The reader's attention is directed to all articles and documents that are filed with or prior to this specification relating to this application and that are open to the public in connection with this specification, and the contents of all such articles and documents are incorporated herein by reference.

Accordingly, the invention provides a method for producing a purified cell culture comprising a recombinant protein, wherein the method comprises:

(i) inoculating the bioreactor with a host cell to obtain a cell culture, wherein said host cell is Escherichia coli, a transformed expression system comprising:

(a) a nucleic acid encoding a recombinant protein operably linked to a first inducible promoter, wherein the protein is 2-O-methyltransferase (OMT); and

b) a nucleic acid encoding a T4 lysozyme protein in frame with a nucleic acid encoding a PelB secretory signal peptide operably linked to a second inducible promoter;

(ii) cell culture fermentation under conditions which:

(a) enables expression of the recombinant polypeptide; and

(b) enables cell penetration to form a spheroplast that secretes the recombinant polypeptide;

wherein said fermentation step comprises adding a stabilizing agent to the cell culture;

iii) purifying the fermented cell culture comprising the secreted recombinant protein, wherein said purification comprises

c) adding a flocculating agent to the cell culture, wherein the flocculating agent is polyethyleneimine (PEI);

d) a pre-clarification step of the flocculated cell culture using a first clarification filter having a pore size of at least about 0.4 µm or greater retention limits, wherein the clarification step does not include centrifugation.

As an advantage, the inventors have found that recombinant E. coli spheroplasts secrete the protein prior to cell lysis.

The inventors have shown that the coordinated expression of a nucleic acid encoding T4 lysozyme linked to a pectate lyase B (PelB) secretion signal sequence together with a nucleic acid encoding a recombinant polypeptide (eg, 2-O-methyltransferase) provides a highly efficient way to express large amounts of the recombinant protein. quantities, e.g. 2-O-methyltransferase, without the need to collect the recombinant cells from the fermentation culture and subsequently lyse the cells mechanically or enzymatically to release the recombinant protein. In the event that the T4 phage lysozyme gene is cloned under a tightly controlled promoter such as araB, periplasmic accumulation of T4 phage lysozyme can be induced by the addition of an inducer (eg, arabinose) during the appropriate fermentation process. Expression of T4 phage lysozyme with a PelB signal sequence facilitates translocation of T4 lysozyme to the periplasmic region, where the enzyme degrades the peptidoglycan layer, leading to morphological changes in the cell leading to spheroplast formation.

A recombinant polypeptide gene, such as a 2-O-methyltransferase gene, is cloned under the control of an inducible promoter such as PT7 or lacllV5, polymerase expression can be induced by adding an inducer such as IPTG at an appropriate point in the fermentation process. Realizing the nucleic acid expression of a recombinant peptide such as 2-Omethyltransferase and T4 phage lysozyme under the control of a separate promoter allows their expression to independently regulate the production of each enzyme during fermentation. The inventors have shown that spheroplasts induced by T4 lysozyme secrete a recombinant protein such as 2-O-methyltransferase into the culture supernatant without the need for a secretion signal sequence. The inventors have observed that recombinant expression of a recombinant protein such as 2-O-methyltransferase has no deleterious effect on the host cell. Indeed, the inventors showed that induced spheroplasts were able to de novo express a recombinant peptide, such as 2-O-methyltransferase, at least 4 or 5 hours after T4 lysozyme induction. In addition, the inventors have demonstrated that the resulting fermented cell culture can be successfully clarified using a clarification filter with an unusually large pore size, which provides retention limits of at least about 0.4 um. This was completely unexpected as the primary clarification methods recommended for E.coli are based on tangential flow filtration using a <0.2 um pore size filter combined with centrifugation to remove cell debris.

Additionally, the inventors have demonstrated that fermented spheroplast cell cultures can be efficiently purified without centrifugation. By eliminating the need for a centrifugation step, fermentation and clarification can be carried out in a closed system, thus eliminating the risk of external contamination.

Thus, in E. coli, a transformed expression system that enables cell permeability, in combination with a clarification process that does not require centrifugation, not only reduces the risk of contamination during protein production, but additionally eliminates a number of downstream processing methods in the production stages, including: cell collection, mechanical and/or enzymatic cell lysing, separation of cell debris, precipitation of nucleic acids followed by separation by filtration or centrifugation. Thus, the defined methods provide high protein yields at high cell densities and scale-up. In addition, eliminating the need to lyse host cells and the associated centrifugation steps reduces large-scale processing times compared to conventional churning-based methods.

Resolution system

The method of the invention uses an expression system that comprises i) a nucleic acid encoding a recombinant protein operably linked to a first inducible promoter; and ii) a nucleic acid encoding a T4 lysozyme protein in frame with a nucleic acid encoding a PelB secretory signal peptide operably linked to a second inducible promoter, wherein the protein is 2-O-methyltransferase (OMT).

As used herein, the term "2-O-methyltransferase" or "OMT" refers to an enzyme that adds a methyl group at the 2'-0 position of the first nucleotide adjacent to the cap structure at the 5' end of the RNA. The 2-O-methyltransferase can be derived from the Vaccinia virus gene vp39. 2-Omethyltransferase can be optimized for expression in E.coli bacteria. 2-O-Methyltransferase can be linked to: NCBI Sequence ID: AGJ91263.1, Protein Name: Multifunctional Poly-A Polymerase Small Subunit VP39 [Vaccinia virus]. Accordingly, the 2-Omethyltransferase may comprise the sequence SEQ ID NO. 1.

As used herein, the term "T4 lysozyme," "E protein," or "gpe" refers to a cytoplasmic muramidase that facilitates lysis of T4 phage-infected bacterial cells, thereby releasing replicated phage particles (Tsugitaand Inouye, J. Mol. Biol., 37: 20112 ( 1968); Tsugita and Inouye, J. Biol. Chem., 243: 391-97 (1968), Uniprot accession: D9IEF7), or a mutant, derivative or fragment having DNA polymerase activity. It is encoded by the T4 bacteriophage gene and hydrolyzes the bonds between N-acetylglucosamine and N-acetylmuramic acid residues in the rigid peptidoglycan layer of the E. coli cell envelope. The enzyme is a single polypeptide chain with a molecular weight of 18.3 kDa. It is approximately 250-fold more active than HEW-lysozyme on bacterial peptidoglycan (Matthews et al., J. Mol. Biol., 147: 545-558 (1981)). The optimal pH value for T4 lysozyme enzyme activity is 7.3, and for HEW-lysozyme - 9 (The Worthington Manual; pp 219-221). The T4 enzyme may have the sequence defined in NCBI reference sequence: NP_049736.1. The T4 enzyme may have the sequence SEQ ID NO. 2.

As used herein, the term "recombinant" refers to proteins that are engineered, prepared, expressed, engineered, produced and/or isolated by recombinant means, such as polypeptides expressed using a recombinant expression vector transfected into a host cell. In some embodiments, the recombinant protein is a functional variant derived from a known 2-O-methyltransferase (OMT) polypeptide. In some embodiments, the polypeptide sequence of the functional variant is at least 70%, 75%, 80%, 82%, 84%, 85%, 86%, 87%, 88%, 89%, 90%, 91%, 92%, 93 %, 94%, 95%, 96%, 97%, 98%, 99%, identical to the 2-O-methyltransferase (OMT) polypeptide sequence of SEQ ID NO. 1. The percentage of identity between two sequences depends on the number of identical sequence positions, taking into account the number of gaps and the length of each gap that must be introduced to optimally align the two sequences. Comparison of sequences and determination of the percentage identity between two sequences can be performed using a mathematical algorithm. In a preferred embodiment, the percent identity between two amino acid sequences is determined using the (Needleman et al. (1970) J. Mol. Biol. 48:444-453) algorithm that was incorporated into the GAP program in the GCG software package (available at http:/ /www.qcq.com) using the BLOSUM 62 matrix or the PAM250 matrix and a gap weight of 16, 14, 12, 10, 8, 6, or 4 and a length weight of 1, 2, 3, 4, 5, or 6. Also in another preferred embodiment, the percent identity of two nucleotide sequences is determined using the GAP program in the GCG software package (available at http://www.gcg.com) using the NWSgapdna.CMP matrix and a gap weight of 40, 50, 60, 70, or 80 , and a length weight equal to 1, 2, 3, 4, 5, or 6. A particularly preferred set of parameters (and one that should be used if one skilled in the art is unsure of which parameters should be applied to determine whether a molecule satisfies the sequence identity of the invention or in homology constraints) is a BLOSUM 62 scoring matrix with a gap penalty of 12, a gap expansion penalty of 4, and a frameshift gap penalty of 5. Alternatively, the percent identity between two amino acid or nucleotide sequences can be determined using an algorithm (Meyers et al. (1989) CABIOS 4:11-17)) which was entered into the ALIGN program (version 2.0) using the PAM120 weight residue table, a gap length penalty of 12 and a spacing penalty of 4.

Expression systems for use in the method of the present invention can be formed using methods well known in the art. In general, a cDNA or genomic DNA encoding a recombinant protein such as 2-O-methyltransferase or T4 lysozyme is suitably inserted into a replicable vector for expression in E. coli cells under the control of an appropriate E. coli promoter. Suitable vectors are well known in the art and the selection of an appropriate vector will depend on the size of the nucleic acid to be inserted into the vector and the host cell to be transformed by the vector. Each vector has different components. For example, bacterial transformation vectors will include a recombinant polypeptide signal sequence as well as a recombinant polypeptide promoter. Preferably, they include the origin of replication and one or more marker genes.

Preferably, the vectors are derived from species compatible with the host cell and are used in conjunction with bacterial hosts, i.e. i.e. vector compatible with E. coli. Preferably, the vector contains a site of replication and markers to ensure phenotypic selection of the transformed cells. Expression vectors for use in the present invention preferably have a nucleic acid sequence that allows the vector to replicate in one or more selected host cells. Such sequences are well known for various bacteria.

Expression vectors for use in the present invention preferably contain a selectable gene or a selectable marker. This gene encodes a protein essential for the survival or growth of transformed host cells grown in a selective culture medium. Host cells not transformed by the vector but carrying the selection gene do not survive in the culture medium. Typical selection genes encode proteins that (a) confer resistance to antibiotics or other toxins such as ampicillin, neomycin, methotrexate, or tetracycline, (b) complement auxotrophic deficiencies, or (c) supply important nutrients not present in the complex medium.

Expression vectors for use in the present invention contain an inducible promoter that is recognized by the host bacterial organism and that is operably linked to a nucleic acid encoding a polypeptide of interest, ie. i.e. recombinant protein such as 2-O-methyltransferase or T4 lysozyme.

Inducible promoters suitable for use with bacterial hosts such as E. coli include the β-lactamase and lactose promoter systems (Chang et al., Nature, 275: 615 (1978); Goeddel et al., Nature, 281: 544 (1979 )), the arabinose promoter system, including the araBAD promoter (Guzman et al., J. Bacteriol., 174: 7716-7728 (1992); Guzman et al., J. Bacteriol., 177: 4121-4130 (1995); Siegele and Hu, Proc. Acad. USA, 94: 8168-8172 (Haldimann et al., 180: 1277-1286) thoptophan (trp) promoter system (Goeddel, Nucleic Acids Res., 8: 4057 (1980) and EP 36,776), PLtetO-1 and Plac/ara-1 promoter (Lutz and Bujard, Nucleic Acids Res., 25: 1203-1210 (1997)) and hybrid promoters such as the tac promoter (deBoer et al., Proc. Natl. Acad. Sci. USA, 80: 21-25 (1983)).

As used herein, the term "inducible promoter" refers to a promoter that, upon binding to a transcription factor, directs transcription at an increased or decreased rate.

As used herein, the term "transcription factor" refers to any factor that can bind to the regulatory or control region of a promoter and thereby affect transcription. Transcription factor synthesis or promoter binding ability in a host cell can be controlled by treating the host with an "inducer" or by removing a "repressor" from the host cell environment. Accordingly, to regulate the expression of an inducible promoter, an inducer is added to or a repressor removed from the culture medium of the host cell.

As used herein, the phrase "causing expression" or "inducing expression" refers to increasing transcription from specific genes by acting on cells containing such genes as an effector or inducer.

As used herein, the term "inducer" is a chemical or physical agent that, when introduced into cells, increases the amount of transcription from specific genes. These may be small molecules whose effects are specific to particular operons or groups of genes and may include sugar, alcohol, metal ions, hormones, heat, cold, and the like. For example, isopropylthio^-galactoside (IPTG) and lactose are inducers of the lac UV5 promoter, while L-arabinose is a suitable inducer of the arabinose (araB) promoter.

As used herein, the term "inducible promoter" refers to a promoter that, upon binding to a transcription factor, directs transcription at an increased or decreased rate.

As used herein, the term "controlled" refers to a nucleic acid sequence operably linked to another nucleic acid sequence. For example, a promoter or enhancer is operably linked to a coding sequence if it affects transcription of the sequence. This requires that the attached DNA sequences are adjacent to each other and that the secretory peptides are in the reading frame.

Accordingly, E. coli is transformed using pBR322, a plasmid derived from E. coli species. See eg, Bolivar et al., Gene, 2:95 (1977). Plasmid pBR322 contains genes conferring resistance to ampicillin and tetracycline to allow identification of transformed cells. Plasmid pBR322 or another microbial plasmid or phage also typically contains or is modified to contain promoters that can be used by the bacterial organism to express selectable marker genes. An expression system of the invention comprises a nucleic acid encoding a recombinant protein operably linked to a first inducible promoter.

The expression system of the present invention also comprises a nucleic acid encoding a T4 lysozyme protein in frame with a nucleic acid encoding a PelB secretory signal peptide operably linked to a second inducible promoter.

As used herein, the term "secretory signal peptide" or "signal peptide" refers to a peptide that can be used to secrete a recombinant polypeptide into the periplasm of a bacterial host. The signal for the heterologous polypeptide may be endogenous to the bacteria or it may be exogenous, including signals specific to the polypeptide produced by the host bacteria. Typically, the signal sequence can be a component of the vector or part of the polypeptide DNA inserted into the vector. Preferably, the vector has a nucleic acid encoding a signal sequence at the N-terminus of the T4 lysozyme protein. Preferably, the secretory signal peptide is pectate lyase B (PelB). In one embodiment, the PelB sequence may be from Erwinia spp. Accordingly, disclosed herein is a gpe with a pelb signal sequence that comprises the sequence of SEQ ID NO. 2. The secretion signal sequence may be directly linked to the nucleotide sequence encoding the recombinant polypeptide, e.g. 2-O-methyltransferase. Alternatively, between the secretory signal peptide and the nucleotide sequence encoding the recombinant polypeptide, e.g. 2O-methyltransferase, may be a spacer. A spacer may comprise more or less than 9 nucleotides, such as, for example, 5 to 20 nucleotides.

For the construction of vectors containing one or more of the components described above, well-known ligation techniques are used. The DNA fragments are broken down and religated into the form needed to create suitable vectors.

Confirmation that the constructed plasmids and vectors contain the correct sequences can be obtained by transforming E. coli K12 strain 294 (ATCC 31,446) or other suitable strains and selecting the transformants for resistance to ampicillin or tetracycline.

In one embodiment, the vector expresses the 2-O-methyltransferase under the control of the IPTG-inducible pT7 promoter or the IPTG-inducible lacIIIV5 promoter. The vector is preferably a pLATE31 vector. In one embodiment, the vector is a pBR322 vector. In one embodiment, the vector is pLATE31-VP39delta32-KnR as described herein.

In one embodiment, the vector expresses a T4 phage lysozyme containing an N-terminal PelB signal sequence under the control of the araB promoter. For example, the T4 bacteriophage lysozyme gene gpe with a pelB signal peptide can be cloned into a tightly controlled pLATE11 vector (cat. K1241, Thermo Fisher) to reduce lyse gene expression in uninduced cells, a fragment containing the transcription terminator rrnBT1-T2 prevents basal gene expression from a vector derived from promoter-like elements T7 RNA polymerase promoter that drives transcription of the cloned gpe gene and two flanking lac operator sequences provide tight control of gene expression Ptet promoter reduces basal expression from T7 promoter T7 terminator terminates transcription from T7 promoter, and the lac repressor, which provides tight basal expression control from the T7 promoter, can be subcloned into the pACYC184 vector, which contains the p15A origin of replication and is compatible with plasmids containing the ColE1 ori (plasmid pACYC184 - PT7pelB-gpe-lacl). Accordingly, in one embodiment, the vector is pACYC184PT7-pelB-gpe-lacl. In one embodiment, the vector is pLATE11. In one embodiment, the vector is a pBR322 vector. In one embodiment, the vector is a pET29 vector. In one embodiment, the vector is pLysS lacl-PcsP-pelB-gpe, where lacl-PcsP is a cold-inducible promoter csp in tandem with the IPTG-inducible lacl operon. In one embodiment, the vector is pACYCI 84-lacl-Pcsp-PelB-gpe.

The host cell

The method of the invention uses a host cell, i.e. i.e. E. coli transformed or transfected with the expression systems described above.

As used herein, the term "transformed" or "transformation" refers to the introduction of DNA into an organism such that the DNA is replicated either as an extrachromosomal element or as a chromosomal integration. Depending on the host cell used, transformation is performed using standard techniques appropriate for such cells.

Recombinant cells for use in the methods of the present invention can be produced using recombinant DNA techniques known to those skilled in the art (see, e.g., Kotewicz, M.L., et al., Nucl. Acids Res. 16:265 (1988); Soltis , D. A., and A. M., Proc. Acad. Sci. 85:3372-3376). Such recombinant cells can be cultured by standard microbiological techniques using culture medium and incubation conditions suitable for the growth of certain types of active cultures, which are well known to those skilled in the art (see, e.g., Brock, T.D., and Freeze, H., J .Bacteriol. 98(1):289-297; Imahori, K. 24(1):102-112.

Transformation refers to the introduction of DNA into an organism such that the DNA is replicated as an extrachromosomal element or as a chromosomal integration. Depending on the host cell used, transformation is performed using standard techniques appropriate for such cells. Calcium treatment with calcium chloride, as described in Sambrook et al., Molecular Cloning: A Laboratory Manual (New York: Cold Spring Harbor Laboratory Press, 1989), is commonly used for bacterial cells that contain essential cell wall barriers. Another transformation method uses polyethylene glycol/DMSO as described in Chung and Miller, Nucleic Acids Res., 16: 3580(1988). Another method is the use of a technology called electroporation.

As used herein, the terms "cell", "cell line" and "cell culture" are used interchangeably and all include progeny. Thus, the words "transformants" and "transformed cells" include the primary cell and the cultures derived therefrom, regardless of the number of passages.

Here, Escherichia coli or E. coli' means a gram-negative, facultative anaerobic rod-shaped coliform bacterium of the genus Escherichia. E. coli host strains for fermentation of recombinant DNA products are well known in the art and include E. coli B (eg, BL21(DE3) or derivatives thereof, E. coli W3110 (ATCC 27,325), E. coli 294 ( ATCC 31,446) and E. coli*1776 (ATCC 31,537) E. coli B and E. coli JS007 are preferred hosts for the methods of this invention.

According to the method of the invention, E. coli can be transformed with one or two expression vectors containing a nucleic acid encoding a recombinant protein and a nucleic acid encoding a T4 lysozyme protein. In one embodiment, bacterial cells are transformed with two vectors, respectively, containing a nucleic acid encoding a recombinant protein and a nucleic acid encoding a T4 lysozyme protein. In an alternative embodiment, the nucleic acid encoding the recombinant protein and the nucleic acid encoding the T4 lysozyme protein are present in a single vector used to transform bacterial cells.

E. coli cells are transformed with the expression vector(s) of the present invention described above and cultured in conventional nutrient media modified to be suitable for inducing the various promoters, if induction is to be effected.

In one embodiment, the host cell is E. coli, preferably E. coli B or E. coli JS007 strain, transformed with a vector expressing 2-O-methyltransferase under the control of the IPTG-inducible PT7 or IPTG-inducible lacllV5 promoter. The vector can be any suitable vector such as pLATE31 or pBR322 vector.

In one embodiment, the host cell is E. coli, preferably an E. coli B strain such as BL21(DE3) or preferably an E. coli JS007 strain, transformed with a vector expressing T4 phage lysozyme containing an N-terminal PelB signal sequence under the control of the araB promoter. The vector can be any suitable vector such as pLATE11 or pBR322 vector.

In one embodiment, the host cell is E. coli, preferably E. coli B or preferably E. coli JS007 strain, transformed with a vector expressing 2-O-methyltransferase under the control of an IPTG-inducible promoter, such as the PT7 or lacllV5 promoter, and T4 phage lysozyme, containing the N-terminal PelB signal sequence under the control of the araB promoter. The vector can be any suitable vector described herein, such as the pACYC184 vector or the pBR322 vector.

Cell culture

The transformed host cells described above are fermented to express a nucleic acid encoding a protein (eg, 2-O-methyltransferase) and a nucleic acid encoding T4 lysozyme.

As used herein, the terms "fermentation" and "cultivation" are used interchangeably to refer to cells grown in large quantities in a culture medium. These include an exponential phase characterized by cell doubling, resulting in massive growth, and a stationary phase in which the cell growth rate and death rate are equal, often due to a growth-limiting factor such as depletion of a key nutrient and/or an inhibitory product such as an organic acid , formation.

In the process of the invention, expression of each of the recombinant protein and T4 lysozyme is controlled by induction of associated promoters. Induction of each protein (e.g., 2-Omethyltransferase) and T4 lysozyme promoters can be performed sequentially or simultaneously.

Induction of the expression of the nucleic acid encoding the recombinant protein and T4 lysozyme is carried out, preferably by adding an inducer to the culture. Usually, the inducer is added after the cells are cultured until a certain optical density is reached, e.g. OD600 0.5, 1.0, 1.5, 2.0, 2.5, 3.0, 3.5, 4.0, 4.5, 5.0 or greater. In one embodiment, the T4 lysozyme inducer is added together with the recombinant protein inducer. In one embodiment, the T4 lysozyme inducer is added sequentially after induction of the recombinant protein.

In one embodiment, induction of each recombinant protein and T4 lysozyme promoters occurs simultaneously. In this embodiment, the promoters of T4 lysozyme and the nucleic acid encoding the polymerase may be identical. Although the promoters can be any promoter suitable for this purpose, it is preferred that the promoters for the recombinant protein and the polymerase are IPTG-inducible promoters, such as the T7 promoter.

In one embodiment, the induction of each of the recombinant protein and T4 lysozyme promoters is sequential, with induction of the T4 lysozyme promoter beginning about 1, 2, 3, 4, 5, 6, 7, 8, 9, 10 or more hours after induction of the recombinant protein promoter. In this embodiment, the promoters of the T4 lysozyme-encoding nucleic acid and the polymerase-encoding nucleic acid must be different so that expression of the nucleic acid-encoded recombinant protein is induced before expression of the nucleic acid-encoded T4 lysozyme or at a much higher level when the promoters are induced. Although the promoters can be any promoter suitable for this purpose, it is preferred that the promoters for the recombinant protein and the polymerase are an arabinose promoter and an IPTG-inducible promoter, respectively.

When the T4 lysozyme inducer is added sequentially, the inducer is typically added after the desired amount of recombinant protein has accumulated (eg, as determined by optical density reaching a target amount that has been observed in the past and that correlates with the accumulation of the desired polypeptide). Typically, induction of T4 lysozyme occurs after inoculation after about 75-90%, preferably about 80-90%, of the total fermentation time. For example, induction of the T4 lysozyme promoter can occur from about 30 hours, preferably 32 hours, to about 36 hours after inoculation in a 40 hour fermentation process. For example, induction of the T4 lysozyme promoter can occur about 1, 2, 3, 4, 5, 6, 7, 8, 9, 10 or more hours after induction of expression of the recombinant protein (eg, 2-Omethyltransferase).

Induction of T4 lysozyme permeabilizes the cell to form a spheroplast that secretes a recombinant protein (eg, 2-O-methyltransferase). As used herein, the term "permeabilizes" refers to making openings in the cell wall without removing it completely. A "spheroplast" is a cell in which the cell wall of a gram-negative bacterium is partially lost and becomes spherical. Spheroplastization can be performed by treating gram-negative bacteria with lysozyme, penicillin, or the like. Since the cell membrane of spheroplastized Gram-negative bacteria is partially lost, information about the interaction between the target protein and the polypeptide (electrophysiological changes) can be analyzed by electrophysiological method. Moreover, the same polypeptide is present in high concentration in the spheroplast of a single cell, which is a favorable condition for measuring the activity of the polypeptide on the target protein. Generally, spheroplasts that retain substantially all of the nucleic acids present in the spheroplast while allowing intracellular proteins (including recombinant protein) to move across the spheroplast membrane.

Typically, the culturing step is carried out at a high cell density, that is, when the cell density is between 15 and 150 g dry weight/liter, preferably at least about 40, more preferably about 40-150, most preferably about 40 to 100. In addition, culturing can using any, even very large volumes of 100,000 liters. The volume is preferably about 100 liters or more, preferably at least about 500 liters, and most preferably from about 500 liters to 100,000 liters.

The E. coli cells used to produce the polypeptide of interest described in the present invention are cultured in a suitable medium in which the promoters can be induced as conventionally described, e.g., Sambrook et al.

The terms medium, cell culture medium, and fermentation medium are used interchangeably herein and refer to a solution containing nutrients required by bacteria, i.e. i.e. E. coli, grow. Generally, the cell culture medium contains essential and essential amino acids, vitamins, energy sources, lipids and micronutrients that the cell needs for minimal growth and/or survival. Preferably, the medium is chemically defined in that all its components and their concentrations are known. If cells are cultured in a fed-batch mode as described below, the term "culture medium" refers to both basal and nutrient medium, unless otherwise specified. The pH value of the medium can be anywhere between pH 5 and 9, depending mainly on the host organism.

In order to accumulate the recombinant gene product, i.e. i.e. recombinant protein, such as 2-O-methyltransferase, the host cell is cultured under conditions sufficient to accumulate the gene product. Such conditions include, for example, temperature, nutrients, and cell density conditions that allow protein expression and accumulation within the cell. Moreover, such conditions are those under which the cell can perform the basic cellular functions of transcription, translation, and the movement of proteins from one cell compartment to another for secreted proteins, as is known to those skilled in the art.

Different cell culture strategies are available, including closed vessel culture, perfusion culture, continuous culture, and fed-batch culture.

In one embodiment of the methods of the present invention, the temperature is changed during the cultivation process from a first temperature to a second temperature, i.e. i.e. the temperature is actively reduced. Preferably, the second temperature should be lower than the first. The first temperature can be 37 °C ± 0.2 °C. The second temperature may be in the range of 25°C to 36°C, preferably in the range of 28°C to 36°C, more preferably in the range of 28°C to 32°C, most preferably in the range from 29 °C to 31 °C. The second temperature can be 29 °C, 30 °C or 31 °C. In one embodiment, the first temperature is 37°C and the second temperature is 30°C.

Gene expression can be measured in a sample directly, for example, using a conventional Northern blot technique to quantify mRNA transcription (Thomas, Proc. Natl. Acad. Sci. USA, 77: 5201-5205 (1980)).

In some embodiments, the bacteria are cultured in a bioreactor. As described herein, the methods of the invention have been shown to be particularly suitable for large-scale production, e.g., in a bioreactor or vessels having a volume greater than 1 L. In some embodiments, the bioreactor is at least about 1 L in volume, at least about 5 L in volume, at least about 10 L volume, at least about 15 L volume, at least about 20 L volume, at least about 30 L volume, at least about 40 L volume, at least about 50 L volume, at least about 100 L volume, at least about 200 L volume, at least about 250 I volume, at least about 500 I volume, at least about 750 I volume, at least about 1000 I volume, at least about 1500 I volume, at least about 2000 I volume, at least about 2500 I volume, at least about 3000 I volume, at least about 3500 I volume , at least about 4000 I volume, at least about 5000 I volume, at least about 7500 I volume, at least about 10,000 I volume, at least 15,000 I volume, at least 20,000 I volume, at least 30,000 I volume, at least 50,000 I volume, at least about 100,000 I volume, at least about 150,000 I volume, at least about 200,000 I volume, at least about 250,000 I volume, at least about 300,000 I volume, at least about 350,000 I volume, at least about 400,000 I volume, at least about 450,000 I in volume or at least about 500,000 I in volume.

Since the recombinant polypeptide (eg, 2-O-methyltransferase) is successfully secreted into the cell culture supernatant during the cultivation process, the recombinant polypeptide can be isolated at the end of the cultivation process by separating the cell culture supernatant containing the recombinant protein. This method successfully eliminates the need to lyse the transformed cells in order to isolate the recombinant protein. This reduces the amount of cellular debris and the release of nucleic acids and other molecules that can affect the quality of the recombinant protein product.

Collecting the cells marks the end of the fermentation/cultivation. Cells can be harvested at any point in the fermentation considered sufficient to complete the fermentation process and yield the expressed recombinant protein. Cell harvesting can occur between 10 and 60 hours after induction of conditions allowing expression of the recombinant protein. For example, cells can be harvested 15 to 40 hours after induction. At the time of cell harvesting, the fermented culture medium includes cells that have been autolyzed and whose membrane has been permeabilized. For example, about 50% or more of the harvested cells may have been autolyzed. Alternatively, about 50%, 55%, 60%, 65%, 70%, 80% or 85% of the harvested cells were autolysed.

As used herein, the terms "cell lysis," "lick," or "lysing" refer to the release of DNA from a cell as a result of complete disruption of the cell membrane. If a cell loses its DNA, it can be considered non-viable, i.e. dead. i.e. dead In contrast, "membrane permeability" and "permeability" refer to disruption of the integrity of the cell membrane that results from leakage of the recombinant product into the cell culture supernatant without complete lysis of the cell membrane. The method of the invention makes it possible to isolate the recombinant protein without completely disrupting the cells. More precisely, the method of the invention provides for the isolation of the recombinant protein, which must be carried out without mechanical disruption of the cell; without adding an exogenous enzyme that degrades the cell wall; without transforming the cell with expression vectors containing a nucleic acid encoding an exogenous enzyme that disrupts the cytoplasmic membrane, e.g. T4 choline protein. Accordingly, in embodiments, the method of the invention does not include any of the following steps: (i) mechanical cell disruption; (ii) addition of an exogenous enzyme that degrades the cell wall; and (iii) transforming the cell with expression vectors containing a nucleic acid encoding an exogenous enzyme that disrupts the cytoplasmic membrane, e.g. T4 choline protein.

Methods are known to monitor both release of the recombinant product and cell lysis. Common to both is the detection of marker molecules, e.g. cellular product showing shedding or DNA lysis. Methods for measuring release include photometry (Dietzsch, J. Biotechnol., 163, pp. 362-370 (2013); Wurm, Eng. Life Sci., 17 pp. 215-222 (2017)) and high performance liquid chromatography (Amand, Biotechnol., 30, pp. 249-255; Kaiser Eng., 8 pp. 138 (2008); Methods for measuring licks include colorimetric assays with hand-held photometers (at-line) or coupled with liquid control systems (at/on-line) (Rajamanickam, Anai. Bioanal. Chem., 409, pp. 667-671 (2017)) and infrared/Raman spectroscopy (Abu-Absi, Pharm. Bioprocess., 2, pp. 267-284 (2014); Buckley, Appl. Spectrosc., 71, pp. 1085-1116 (2017); ΟΙθββη, Anai. Bioanal. Chem., 409 pp. 651-666 (2017); Biotechnol., 33, pp. 285-298 (2017) Autolysis can be measured indirectly by DNA concentration in purified harvested cells or by capacity.

Secreted recombinant proteins are sensitive to cell culture instability, such as aggregating and forming improper spatial structure after secretion/cell lysis. In certain embodiments, a stabilizing agent is added to the cell culture. The stabilizer can be added before, during or after fermentation. Examples of suitable stabilizers include potassium chloride, DTT, sodium chloride, trehalose, sucrose, glycine, betaine, mannitol, potassium citrate, CuCL, proline, xylitol, NDSB 201, CTAB, K2PO4 Na2SO4, and Brij 35. In certain embodiments, the stabilizing additive may include amino acids such as arginine.

In certain embodiments, a nucleic acid inactivating agent (eg, benzonase) can be used to remove free nucleic acid (DNA and/or RNA) from the cell culture. The nucleic acid inactivating agent can be added before, during or after fermentation. Preferably, the nucleic acid inactivating agent is not centrifuged prior to cell culture clarification. Thus, any method of the invention may include (i) adding a nucleic acid (eg, DNA) inactivating agent (such as benzonase) to the cell culture in the absence of a further centrifugation step.

Clarification

According to the methods of the present invention, autolyzed and/or permeabilized cells are separated from the culture medium prior to isolation and purification of the product from the cell medium by clarification.

As used herein, the terms "clarify", "clarification", "clarification step" refer to a process comprising one or more steps used to remove solid impurities from a cell culture to obtain a liquid crude filtrate containing a recombinant protein.

The efficiency of the clarification step is critical to facilitate subsequent processing steps that require the purification of the biomolecule of interest. Parameters that can affect the clarification step include total cell concentration, cell viability, initial turbidity of the cell culture for clarification, concentration of biomolecule produced by cultured cells, and size of cell debris. As used herein, the term total cell concentration (TCC) refers to the number of cells in a given culture volume. As used herein, the term viable cell concentration (VCC) refers to the number of viable cells in a given volume of culture as determined by standard known viability assays. As used herein, the term "viability" refers to the percentage of living cells. Generally, the higher the TCC, the greater the biomass to be removed from the cell culture and the greater the effect on clarification. As used herein, the term "turbidity" refers to the turbidity or turbidity of a liquid caused by a large number of individual particles. In particular, turbidity indicates the amount of matter and small particles in a liquid that can scatter light. Typically, cell culture turbidity correlates with cells in culture, cell debris, nucleic acids, and host cell protein (HCP) in addition to the recombinant polypeptide.

The clarification step reduces the initial turbidity of the fermented cell culture to a lower turbidity of the clarified cell culture to produce a clarified cell culture with the highest concentration of the biomolecule of interest and a lower amount of other cell culture material.

In one embodiment, the initial turbidity of the fermented cell culture is greater than about 10,000 NTU, about 20,000 NTU, about 30,000 NTU. In some embodiments, the initial turbidity of the fermented cell culture is between about 10,000 NTU and about 150,000 NTU, and more specifically includes between about 30,000 NTU and about 100,000 NTU.

In one embodiment, the clarified cell culture has a turbidity equal to or less than about 40, 30, 25, or 20 NTU. The clarified cell culture preferably has a turbidity of about 20 NTU or less.

For the clarification method to be effective, it is also important to maximize throughput. As used herein, the terms "capacity" or "carrying capacity" or "capacity" may be used interchangeably and refer to the volume clarified in a functional unit of clarification, such as the volume filtered through a filter, more specifically the volume normalized to the filter area (L/m ² ) .

Clarification of the cell culture of the invention includes a primary clarification step. As used herein, the terms "primary clarification" refer to the removal of large particles such as whole cells and cell debris. In embodiments, the primary clarification may be followed by a secondary clarification step. As used herein, the term "secondary clarification" generally refers to the removal of smaller particles, such as particles smaller than whole cells. Each of the primary and secondary clarification stages uses a filter as the functional unit of clarification.

In a preferred embodiment, the primary clarification step and/or the secondary clarification step is microfiltration. Typically, microfiltration is used to separate particles of 0.1-10 µm in size from the solution. It is most often used to separate a polymer with a molecular weight of 1 χ 10 ⁵ g/mol. In addition, microfiltration can be used for sediments, protozoa, large bacteria, etc. remove In the present invention, microfiltration can easily be used to remove whole cells and cell debris. Typically, the microfiltration process is carried out using a pressure pump or a vacuum pump with a speed of 0.1-5 m/s, preferably 1-3 m/s, and a pressure of 50-600 kPa, preferably 100-400 kPa.

In a preferred embodiment, the primary clarification step and/or the secondary clarification step is depth filtration. As used herein, the term "depth filtration" refers to a technology that utilizes filters of a certain sensitivity to trap media particles throughout the filter and not just on the surface of the filter. Depth filters are typically composed of cellulose fibers or synthetic polymer fibers such as polyacrylic or polystyrene. These fibers form a three-dimensional network with a certain porosity. A depth filter may be suitable for primary and/or secondary extraction or only for primary or secondary extraction. Filters suitable for primary and/or secondary regeneration are also known as single-stage filters. Single-stage filters can be used to perform both primary and secondary extraction, or they can be used as filters for primary extraction and in combination with the subsequent use of a secondary extraction filter. In certain embodiments, this depth filter is positively charged. The interaction between the positively charged filter and the colloidal particles in the fermented cell culture successfully allows the removal of such small impurities, while the larger particles are retained by the porosity of the filter matrix.

The filter may be composed of a variety of materials well known in the art. Such materials may include, but are not limited to, polymeric materials such as nylon, cellulosic materials (eg, cellulose acetate), polyvinylidene fluoride (PVDF), polyethersulfone, polyamide, polysulfone, polypropylene, and polyethylene terephthalate. In certain embodiments, filters used to clarify cell lysates may include, but are not limited to, StaxTM depth filter systems (Pall Life Sciences), ULTIPLEAT PROFILE™ filters (Pali Corporation, Port Washington, NY), SUPOR™ membrane filters (Pall Corporation, Port Washington, NY). Commercial depth filters include StaxTM depth filter systems (Pall Life Sciences), Millistak+ Pod depth filter system, XOHC media (Millipore Corporation), Zeta Plus™ depth filter (3M Purification Inc.), and others.

In embodiments, pre-clarification is performed with a first filter having a pore size of at least about 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1.0, 2.0, 3.0, 4.0, 5.0, 6.0 7.0, 8.0, 9.0, 10.0, 11.0, 12.0, 13.0, 14.0, 15.0, 16.0 , 17.0, 18.0, 19.0, 20.0 um (micrometer) or greater retention limits. In another embodiment, the first filter has a pore size that provides retention limits from about 0.4 um to about 20.0 um. In another embodiment, the first filter has a pore size that provides retention limits from about 0.4 um to about 9.0 um. In another embodiment, the first filter has a pore size that provides retention limits from about 0.4 um to about 3.0 um. In another embodiment, the first filter has a pore size that provides retention limits of about 0.4 um to about 0.8 um. In another embodiment, the first filter has a pore size that provides retention limits from about 1.0 um to about 3.0 um. In another embodiment, the first filter has a pore size that provides retention limits from about 1.0 um to about 20.0 um. In another embodiment, the first filter has a pore size that provides retention limits from about 1.0 um to about 9.0 um. In another embodiment, the first filter has a pore size that provides retention limits from about 4.0 um to about 20.0 um. In another embodiment, the first filter has a pore size that provides retention limits from about 4.0 um to about 9.0 um. In a certain embodiment, the first clarification step is performed using a first depth filtration.

The clarification efficiency can be improved by increasing the filter bandwidth. As used herein, the terms "permeability" or "carrying capacity" or "capacity" are used interchangeably and refer to the volume clarified by a functional unit of clarification, such as the volume filtered through a filter, or rather, the volume normalized by the filter area (L/m ² ).

In one embodiment, the maximum throughput of the pre-clarification step is at least 50, 60, 70, 80, 90, 100, 150, 200, 250, 300, 350, 400, 450, 500, 550, 600, 650, 700, 750, 800 , 850, 900, 950, 1000 L/m ² .

In embodiments, the secondary clarification is performed by a second filter, e.g. depth filter with a pore size of at least 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1.0, 2.0, 3, 0, 4.0, 5.0, 6.0, 7.0, 8.0, 9.0, 10.0, 11.0, 12.0, 13.0, 14.0, 15.0, 16.0, 17.0, 18.0, 19.0, 20.0 μΜ or higher retention limits. In another embodiment, the second filter has a pore size that provides retention limits of about 0.4 pm to about 3.0 pm. In another embodiment, the second filter has a pore size that provides retention limits between about 0.4 pm and about 0.8 pm. In another embodiment, the second filter has a pore size that provides retention limits from about 1.0 pm to about 3.0 pm. In a certain embodiment, the second clarification step is performed using a second depth filtering.

In embodiments, a filter of the same pore size is used in the primary clarification and secondary clarification steps. In embodiments, both the first and second filters have a pore size that provides retention limits of about 0.4 pm to about 0.8 pm, both the first and second filters have a pore size that provides retention limits of about 1.0 pm to around 3.0 pm.

In one embodiment, the maximum throughput of the secondary clarification step is at least about 50, 60, 70, 80, 90, 100, 150, 200, 250, 300, 350, 400, 450, 500, 550, 600, 650, 700, 750, 800, 850, 900, 950, 1000 L/m ² .

In one embodiment of the present invention, a cell culture pretreatment step is performed prior to primary clarification to increase clarification efficiency, such as flocculation.

As used herein, the term "flocculation" refers to the aggregation, precipitation, and/or agglomeration of insoluble particles such as cellular material, including cells, cellular debris, host cell proteins, DNA, and other components, caused by the addition of a suitable flocculating agent to a fermented cell culture. Increasing the particle size of the insoluble components present in the fermented cell culture improves the efficiency of separation, such as clarification by filtration. Flocculation can be initiated by known methods, including lowering the pH value of the cell culture or adding a flocculating agent. Non-limiting examples of a flocculating agent include calcium phosphate, caprylic acid, divalent cations, or positively charged polymers such as polyamine, polyethyleneimine (PEI), chitosan, or polydiallyldimethylammonium chloride (e.g., pDADMAC) that cause particle aggregation through interactions with the negatively charged cell surface and cell remains. In one embodiment, the flocculating agent is a positively charged polymer, preferably polyethyleneimine (PEI). In embodiments, the flocculating agent is PEI and is added to the fermented cell culture at about 0.10% (v/v) to about 0.50% (v/v). In embodiments, the flocculating agent is PEI and added to the fermented cell culture at a concentration of from about 0.15% (v/v) to about 0.25% (v/v). In embodiments, the flocculating agent is added to the fermented cell culture at a concentration of about 0.10% (v/v), 0.15% (v/v), 0.20% (v/v), 0.25% (v/v ) or 0.30% (v/v). In embodiments, the flocculating agent is PEI and added to the fermented cell culture at a concentration equal to about 0.15% (v/v) or about 0.25% (v/v).

In one embodiment, the flocculating agent is added directly to the fermented cell culture liquid at the end of the fermentation, and the flocculated material, including the cells, is removed from the cell culture liquid by filtration. In one embodiment, the flocculating agent is added prior to harvesting the cells.

In preferred embodiments, fermentation and clarification are performed as a closed system method. As used herein, the term "closed system method" refers to a method or process that is performed in closed sterile systems under controlled environmental conditions without any risk of external contamination from the operator or the laboratory environment. It is especially important to use a closed system when creating products of the GGP class. In substantially preferred embodiments, the methods of the invention are closed system methods that do not involve centrifugation, since centrifugation cannot be performed in a closed system and requires transfer of an intermediate product (lysed cells) to centrifugation vessels. Post-fermentation clarification can be carried out by transferring the fermented culture from the bioreactor in a flow in closed tube systems to the clarification filters, without any operator contact.

Further processing of the purified protein

In embodiments, the recombinant protein can be isolated directly from the clarified culture medium. Isolation of the recombinant protein may be followed by purification to ensure adequate purity of the recombinant protein. Various methods of protein purification are well known to those skilled in the art.

Suitable purification techniques include, but are not limited to, ammonium sulfate or ethanol precipitation, acid extraction, gel electrophoresis, immunoadsorption, anion or cation exchange chromatography, phosphocellulose chromatography, hydrophobic interaction chromatography, affinity chromatography, immunoaffinity chromatography, gel filtration, liquid chromatography (LC ), high performance LC (HPLC), high performance LC (FPLC), hydroxyapatite chromatography, leectin chromatography and immobilized metal affinity chromatography (IMAC). Most preferably, recombinant proteins are purified by liquid chromatography techniques including ion exchange, affinity and gel filtration.

Thus, the methods of the invention provide substantially pure recombinant proteins. Substantially pure, as used herein, refers to a preparation or sample that is substantially free of impurity components, proteins, etc.

Throughout the description and statements of this specification, the words "comprising" and "comprising" and their variations mean "including but not limited to" and do not refer to (and do not exclude) other parts, accessories, components or steps. Throughout the description and definition of this specification, the singular includes the plural unless the context otherwise requires. In particular, when the indefinite article is used, the specification shall be understood to include both the plural and the singular unless the context otherwise requires.

Signs, integers, characteristics, compounds, chemical moieties, or groups described in connection with a particular aspect, embodiment, or example of the invention are to be understood as applicable to any other aspect, embodiment, or example described herein unless inconsistent therewith. All features disclosed in this specification (including any accompanying definitions, abstracts and drawings) and/or all steps of the method or process so disclosed may be combined in any combination except combinations in which at least some of such features and/or stages are incompatible with each other. The invention is not limited to the details of any of the above embodiments. The invention includes any new or any new combination of features disclosed in this specification (including any accompanying definitions, abstracts and drawings), or any new or any new combination of steps in any method or process so disclosed.

The reader's attention is directed to all articles and documents filed with or prior to this specification relating to this application and open to the public in connection with this specification, and the contents of all such articles and documents are incorporated herein by reference.

EXAMPLES example

Construction of the vaccinia virus 2-O-methyltransferase gene vp39

The expression-optimized E. coli vp39 gene was cloned into the pLATE31 vector (Thermo Fisher). NCBI Sequence ID: AGJ91263.1, Protein Name: Multifunctional poly-A polymerase small subunit VP39 [Vaccinia virus] (Figure 1A). The amino acid sequence of the 2-O-methyltransferase used in this example is disclosed herein as SEQ ID NO. 1.

Construction of the T4 bacteriophage lysozyme gene gpe

The T4 bacteriophage lysozyme gene gpe was cloned into a tightly controlled pLATE11 vector (cat. no. K1241, Thermo Fisher) to reduce lysozyme gene expression in uninduced cells. In addition, the pelB signal peptide for translocation of the produced protein to the periplasmic space was fused to the N terminus of Gpe. A fragment containing the transcription terminator rrnBT1-T2 prevented basal gene expression from vector-derived promoter-like elements, the T7 RNA polymerase promoter that drives transcription of the cloned gpe gene, and two flanking sequences of the lac operator provide tight control of gene expression, the Ptet promoter reduces basal expression from the T7 promoter, the T7 terminator, which terminates transcription from the T7 promoter, and the lac repressor, which ensures tight control of basal expression from the T7 promoter, were subcloned into the pACYC184 vector, which contains the p15A origin of replication and is compatible with plasmids containing the ColE1 ori (plasmid pACYC184-PT7-pelBgpe-lacl) (Figure 1B).

This example used a modified polypeptide called Gpe, whose sequence is derived from Escherichia coli T4 bacteriophage lysozyme. NCBI reference sequence: NP_049736.1, protein name: glycoside hydrolase family protein (Escherichia phage T4). PelB signal sequence: 1 - 22, T4 bacteriophage lysozyme 23 164. The Gpe protein sequence with the PelB signal sequence is disclosed herein as SEQ ID NO. 2.

Expression strain preparation

E. coli strain JS007 (Thermo Fisher Scientific) was transformed with plasmid pLATE31-VP39delta32-KnR and plated on LB (non-animal origin) AOF agar with kanamycin (50 g/L). The expression strain E. coli JS007 pLATE31-VP39delta32KnR was cotransformed separately with the lysis plasmid pACYC-PT7-pelB-gpe-lacl containing the gpe gene of the T4 bacteriophage lysozyme gene. Transformants with both plasmids were plated on LB agar with kanamycin (50 mg/l) and chloramphenicol (25 mg/l). Both transformations were based on the calcium temperature shock method. A research cell bank (RCB) was generated after culturing the transformants for 3 h in liquid TB4 AOF medium with the required antibiotics at 37 °C and 220 rpm. A sterile 50% glycerol solution was used to produce 25% glycerol RCB, which was dispensed into xogenic tubes and stored at −70°C.

Growing medium

Transformations and plasmid propagation were performed in solid and liquid LB AOF medium containing peptone (10 g/L), yeast extract (5 g/L), NaCl (10 g/L), and solid medium supplemented with 15 g/L microbial agar, as well as the necessary antibiotics. Batch fed and closed culture cultivation was carried out in glycerol-based (AOF) broth of non-animal origin (TB4 AOF and TB AOF) containing (per liter): peptone 12 g, yeast extract 24 g, (ΝΗ4)2δθ4 2.68 g , KH2PO4 2.3 g, K2HPO4 12.5 g and glycerol from 4 to 10 g. In addition, prior to cultivation, TB10 medium was supplemented with the following sterile solutions: 3 ml (1 M) MgBO4 and 2 ml of a trace element solution with the composition (per liter): CaCl2 ^x 2H2O 0.5 g, Ζηδθ4 ^x 7H2O 0.18 g, Μηδθ4 ^x H2O 0.1 g, Na2EDTA 20.1 g, FeCI3 ^x 6H2O 16.7 g, CuBO ₄ ^x 5H2O 0.16 g, CoCI2 ^x 6H2O 0.18 g; as well as 1 ml of kanamycin (50 mg ml/l) and 1 ml of chloramphenicol (30 mg/l).

Expression and autolysis conditions in shake flasks

Inoculum for serial protein production in shake flasks was prepared by culturing the selected clone overnight in a 250 mL shake flask with 50 mL TB4 AOF medium containing 4 g/L vegetable glycerol at 37 °C. For protein production, the appropriate seed culture was transferred to fresh TB10 AOF medium containing 10 g/L glycerol to a final volume of 50 mL in 250 mL Erlenmeyer shake flasks. The culture was grown at 37°C and 220 rpm until reaching a cell density of OD600 1.5-2.0. Induction was performed with 0.1 mM IPTG. The temperature at the induction point was changed to 32 °C, and cultivation was continued for 17 h at 220 rpm.

Expression and autolysis conditions in the bioreactor

Resuscitation of the cell bank culture (preparation of the inoculum) was performed by shake-flask cultivation in 250 mL Erlenmeyer flasks with septa containing 50 mL volumes of TB4 AOF medium with 4 g/L glycerol, 3 mL/L 1 M MgSO4, 2 mL/L Mkt- MSM, 50 mg/l kanamycin. and 25 mg/L chloramphenicol at 37 °C, 230 rpm. 4-6 children Subsequently, the inoculum seeding volume, calculated using the formula 0.5/preinoculum OD, was transferred to fresh 2000 mL Erlenmeyer flasks with septa containing 500 mL volume of TB4 AOF medium with 4 g/L glycerol, 3 mL/L 1 M MgSO4, 2 ml/l Mkt-MSM, 50 mg/l kanamycin and 25 mg/l chloramphenicol for inoculum cultivation at 25 °C, 260 rpm, 16-18 hours.

Batch culture fermentation was carried out in 5 L Biostat A bioreactors with TB10 AOF medium containing 10 g/l glycerol, 3 ml/l 1 M MgSO4, 2 ml/l Mkt-MSM, 3 ml/l 10 mg/ml thiamine- HCI, 50 mg/l kanamycin, 25 mg/l chloramphenicol and 0.2 ml/l Pluronic, initial culture volume 3 I. The actual volume of inoculum needed to seed the bioreactors was calculated using the formula: (fermentation volume [ml] χ inoculum target OD (0.1) )) / measured inoculum OD. The initial cultivation parameters are as follows: temperature maintained at 37 °C, pO2 at 30%, adjusting the mixing speed and automatically adjusting the air flow (from 500 to 1600 ccm), pH adjusted at 7.0 ± 0.1 by addn. NFUOH (25%) or H3PO4 (42.5%). The fed-batch culture phase was maintained with a feed solution containing 60 g/L plant peptone solution, 60 g/L yeast extract, 10.57 g/L (NH4)2SO4, 2 ml/L Mkt-MSM, 80 ml/L 1 M MgSO4 400 g/l glycerol, 50 mg/l kanamycin and 25 mg/l chloramphenicol. The delivery profile was set to maintain a media delivery rate of 20 mL/hr/L for a total of 8 hours with a pump speed of 13.5%. Protein expression and induction of cell lysis were performed by adding a solution of IPTG (final concentration 0.1 mM) to the bioreactor, followed by lowering the temperature from 37 to 25 °C over a 30-minute period and reducing the pO2 from 30% to 3% over a 30-minute period. . The duration of induction of protein expression and cell lysis was 18-22 h, and the optical density of the medium at 600 nm (OD600) was measured throughout the process to estimate cell concentration.

For better cell disruption, an osmotic shock was performed by adding 71.01 g/l 0.5 M NažSCM and 5 g/l 0.5% Brij 35. After the addition of osmotic agents, the automatic support of pOž, pH value, temperature and air flow was turned off, and was only supported at 700 rpm. mixing speed. Subsequently, all bioreactor suspensions were collected and transferred to other groups to start the clarification steps.

Protein separation study using SDS-PAGE analysis method

Cells and medium fractions were separated by centrifugation at 30 m in., 14000 rpm, at 4 °C. Medium fractions were stored at 4 °C. Cell samples taken from a culture flask or fermenter were resuspended in slurring buffer at a ratio of 1 g of biomass resuspended in 10 ml of slurring buffer (50 mM Tris-HCl, 50 mM NaCl, 0.1 mM EDTA). The biomass was sonicated for 60 seconds at 4 °C. Soluble and insoluble protein fractions were separated by centrifugation for 20 min, 14000 rpm, 4 °C. The total protein fraction consists of a suspension of cell debris (crude extract). Cell samples for SDS-PAGE separation were prepared as follows: 20 μl of crude extract sample, 25 μl of 4× SDS-PAGE loading buffer, 5 μΙ of 2M DTT, and 50 μΙ of deionized water so that the final sample volume was 100 μΙ. Media samples for SDS-PAGE separation were prepared as follows: 70 μΙ culture medium, 25 μΙ 4 χ SDS-PAGE loading buffer, 5 μΙ 2M DTT so that the final sample volume was 100 μΙ. The samples were heated for 10 minutes at 95 °C. 10 μΙ of sample was applied to each lane of a 4-12% gradient SDS-PAGE gel.

Clarification of fermentation culture

To clarify the fermentation culture, sodium sulfate to a final concentration of 0.5 M and Brij 35 to a final concentration of 0.5% (w/v) were added to the bioreactor under agitation at 250-350 rpm. 30-60 minutes 32 °C. PEI (Lupasol, Polyethyleneimine, BASF) was then added to the bioreactor to a final concentration of 0.25% (v/v), and stirring was continued for at least 10 minutes at 250-350 rpm. The material from the bioreactor was transferred to separate tanks and mixed with water in a ratio of 2:5 (v/v) at 50-100 rpm for 10-20 min. The culture was left to sediment from 3 hours to overnight. After sedimentation, the culture supernatant was clarified by filtration through depth filtration capsules K050P (Pall, ID 7007786) and then filtered through a 0.22 um filter capsule (Pall, ID NP6UEAVP1S).

In detail, the clarification process included the following steps (Figure 7).

E.coli autolysate clarification process: starting material: 250 I of lysed cell culture, after 16-18 days. target protein expression in stirred tank reactors. Final OD of cells/cell debris ~ 15-30 OD. The analysis showed that the resulting cell lysis efficiency was 75-80% of the total cell volume.

1.0 Preparation of E.coli lysate for filtration: during all manipulations in a stirred bioreactor (HyperformaTM 300 I, Thermofisher Scientific) all automatic controls in the fermentation vessel: Air/Oz flow, pH value. Stirring was maintained at 375 rpm and the temperature was set to < 12 °C.

Disruption of cell structures, stabilization of enzymes and flocculation of nucleic acids. Dry materials were added directly to the bioreactor vessel one at a time to achieve a final concentration of 1 M sucrose, 0.5 M Na2SO4 and 0.5% Brij 35. The high viscosity solution is thoroughly stirred at 375 rpm. 20-40 minutes at 12 °C. Stirring was then maintained at 100 rpm. at speed ΙΟΙ 8 vai. < 12 °C. Flocculation was performed by adding PEI (Lupasol, polyethyleneimine, BASF) to the bioreactor vessel to a final concentration of 0.25% (v/v). Stirring is continued for at least 15 minutes at 350 rpm. The solution from the bioreactor was transferred to separate containers, diluted with water (molecular biology grade) 2.5 times, stirred at 200-300 rpm. 10-20 minutes After that, stirring was completely stopped. The culture is left to sediment for ~3 hours.

Clarification: filter preparation. STAX filter capsules K050P (Pall, ID 7007786) were washed with 10 filter volumes of water. Not exceeding 0.2 BAR pressure back pressure. After sedimentation, the culture supernatant was clarified by filtration through depth filtration capsules K050P (Pall, ID 7007786). Retention 0.4-0.8 μΜ (about 0.05 m ² filter area is needed to filter 1 L of fermentation medium), not exceeding 1.2 BAR back pressure. Secondary clarification can be done using a 0.22 um filter capsule (Pall, ID NP6UEAVP1S). The same clarification process can be performed using filtration systems: 1-3 μΜ (P100) (Pall, ID 7007836).

E. coli is not a perfect host, especially for closed batch fermentation, because it does not normally secrete proteins into the extracellular medium. The cell disruption step becomes limiting and is not cost-effective on an experimental or industrial scale when the goal is to implement a closed and/or continuous process flow. The present invention provides a cell lysis method that is a programmed cell lysis system based on the expression of the cloned T4 bacteriophage gene gpe to produce a squelch protein. The gene gpe encodes lysozyme, which breaks down peptidoglycan in the E. coli cell wall.

A self-destructive Escherichia coli has been created that produces a foreign target protein. E. coli JS007 was co-transformed with two vector plasmids, the target gene expression vector pLATE31-VP39delta32-KnR and the grunt gene expression vector pACYC184-PT7-pelB-gpe-lacl. The lysis protein was produced after the expression of the target gene, thus simplifying the cell lysis process. In this example, expression of the cloned T4 phage gene gpe was used to disrupt E. coli that produced OMT as a target protein. Expression of the gpe gene did not induce rapid cell lysis, but weakened the cell wall. Translocation of the lysis protein Gpe from the cytoplasm to the periplasm facilitated the enzymatic degradation of the murein layer, which is responsible for maintaining the rigidity of the cell structure. Microscopic observation revealed that cells producing Gpe in the periplasmic space after 4 h underwent morphological changes from rod-shaped to elliptical spheroplasts (Figure 2).

Induction of 2-O-methyltransferase in E. coli JS007/pLATE31-VP39delta32KnR/pACYC-PT7-pelB-gpe-lacl culture was performed using 0.1 mM IPTG. Lysozyme gene induction was performed simultaneously. The culture was grown overnight at 32 °C. Samples from the induced culture and medium were taken 1, 2, 3, 5, and 17 h after the induction of protein synthesis. E. coli cell debris observed in the culture medium indicated that cell lysis had occurred. The highest yield of 2-O-methyltrasferase in the medium was obtained after 17 hours of expression/lysis in the E. coli JS007/pLATE31-VP39delta32KnR/pACYC-PT7-pelB-gpe-lacl strain. The amount of 2-O-methyltrasferase was determined by SDS PAGE (Figure 3).

Batch culture OMT production was performed in 5 L Biostat A bioreactors with an initial culture volume of 3 L. As shown in Figure 4, protein expression and induction of cell lysis were performed by adding IPTG solution (final concentration 0.1 mM) to the bioreactor. induction point target OD600 14 - 17.5. The intermittent feed culture phase was initiated after the DO peak, which usually occurred 10-25 m in. after induction of protein expression and lysis. The batch culture process was controlled automatically according to a process profile that maintained a medium delivery rate of 20 ml/hr/1 I for a total of 8 hours at a pump speed of 13.5%. After 15 minutes of IPTG induction, temperature was reduced from 37 to 25°C over a 30-minute period, and pO2 was reduced from 30% to 3% 1 hour after induction with IPTG over a 30-minute period. After the induction phase of protein expression and cell lysis (18-22 h), the gas supply, pH value and temperature control were turned off, and only 700 rpm was maintained for osmotic shock. mixing speed. After 30 minutes of osmotic shock, all bioreactor suspensions were collected, and clarification steps were started.

To compare the reproducibility and study the growth rate, the fermentation processes were carried out together with Biostat A bioreactors. Growth rate was determined by periodic optical density measurements as shown in Figure 5. The results revealed that the growth rate of the culture in both processes is similar, but the cultures from F2 and F4 fed overnight had a higher optical density at the end of the process, although the cultures from F6 and F3 with 4 va. feeding - higher activity, when their values were 43.7 and 55.0 U/ul.

In order to investigate how the autolysis system and feeding time determine trends in protein activity, similar fermentation processes were initiated. The autolysis and fed-batch culture systems were found to increase the OMT yield by 18-fold as shown in Figure 6, but slightly decreased with increased feeding time.

The biosynthesis parameters used in development were successfully scaled up from 5 I Univessel Glass Biostat A bioreactors to 300 I stainless steel fermenter capacity to ensure that the optimized process was transferred to production facilities. The optimized process parameters were evaluated based on the target protein yield. Comparing the results of the old production technologies with the new approach technologies, where there is an E. coli system with autolysis, it was found that using the autolysis system, the yield of OMT increased by about 70 times - from 857 mg to 60000 mg (amount of 300 I bioreaktohaus) after clarification and purification processes.

Depth filtration-based clarification of cell debris without nuclease treatment. Here, the best mixture of high ionic strength building salts, osmotic agents and detergent was used to stabilize the enzymes, prevent precipitation/aggregation, and prevent interaction with extremely hydrophobic lysozyme and membrane proteins. Nucleic acid flocculation has also been used to create a filter plate that includes small flocculation particles. This has been successfully demonstrated using unusual 0.4-0.8 pm filter pairs. It also worked with 1-3 pm pore filters. The size of an E. coli cell is: 1.0-2.0 micrometers in length and a radius of about 0.5 micrometers. The primary purification methods that are commonly recommended for E. coli bacteria are tangential flow filtration with a pore size of less than 0.2 micrometers or centrifugation, which is the most common method to remove cell debris, large or small flocculants.

The newly developed expression system includes genetic elements to produce target proteins and co-produce the ruffling enzymes in a controlled manner in the periplasmic space of the cell during the desired growth period, if needed. Experimental data showed that the coexpressed phage buzzing enzyme does not completely lyse the cells, but instead forms protoplasts that resemble cells. This suggested that the translocation of lysozyme from the cytoplasm to the periplasm facilitated the enzymatic degradation of the murein layer, which is responsible for maintaining the firmness of the cell structure. Protoplasts release/secrete target proteins into the culture medium without the help of secretory leader peptides in shake flask and microbial bioreactor production. The protoplasts remain viable for at least 4 hours after the induction of ruminants, i.e. y, they de novo produce and secrete the protein of interest, resulting in increased amounts of the target protein in the culture medium over time. OMT protein expression was performed in a Biostat A fermenter using E. coli JS007 pLATE31-VP39delta32-KnR, pACYC-PT7pelB-gpe-lacl cells, and processes were later scaled up to a 300 L single-use fermenter. Up to 70 times higher yield was obtained after the clarification and purification processes compared to the denoised resolution. Normal intracellular expression of OMT yields 857 mg, and with autolysis 60,000 mg from a 300 I bioreactor. A cell lysis method mediated by the expression of a cloned T4 phage lysis gene to isolate intracellular target proteins is demonstrated and can be applied to other recombinant proteins by replacing the OMT.

A one-pot process in a fermentation vessel that produces recombinant proteins by cell autolysis followed by protein stabilization and nucleic acid precipitation to eliminate at least 5 separate downstream processing steps: cell harvesting, mechanical and/or enzymatic cell lysis, cell debris separation, precipitation of the nucleic acid and subsequent separation by filtration or centrifugation.

SEQUENCE of vp39 protein without C-terminal amino acids: 1-301, His tag: 302309: - NCBI sequence ID: AGJ91263.1, protein name: multifunctional poly-A polymerase small subunit VP39 [Vaccinia virus] mdvvsldkpfmyfeeidneldyepesanevakklpyqgqlllgelfflsklqrhgildgatvvy fynlgviikwmlidgrhhdpilnglrdvtlvtrfvdeeylrsikkqlhpsk iilisdvrskrggnepstadllsnyalqnvmisilnpvasslkwrcpfpdqwikdfyiphgnkmlq pfapsysaemrllsiytgenmrltrvtksdavnyekkmyylnkivrnkvvvnfdypnqeydyfhmy fmlrtvycnktfpttkakvlflqqsifrflnipttstghhhhhhg ( SEQ ID NO: 1)

Gpe protein sequence with PelB signal sequence (NCBI reference sequence: NP_049736.1, protein name: glycoside hydrolase family protein (Escherichia phage T4). PelB signal sequence: 1-22, T4 bacteriophage lysozyme 23-164):

mkyllptaaagllllaaqpamamnifemlhderlrlkiykdtegyytigighlltkspslnaaks eldkaigrncngvitkdeaeklfnqdvdaavrgilrnaklkpvydsldavrrcalinmvfqmgetg vagftnslrmlqqkrwdeaavnlaksiwynqtpnrakrvittfrtgtwdayknl (SEQ ID NO: 2)

Claims (21)

DEFINITION OF THE INVENTION 1. A method of producing a purified cell culture comprising a recombinant protein, wherein the method comprises: (i) inoculating the bioreactor with a host cell to provide a cell culture, wherein said host cell is Escherichia coli, a transformed expression system comprising: (a) a nucleic acid encoding a recombinant protein operably linked to a first inducible promoter, wherein the protein is 2-O-methyltransferase (OMT); and b) a nucleic acid encoding a T4 lysozyme protein in frame with a nucleic acid encoding a PelB secretory signal peptide operably linked to a second inducible promoter, ii) fermentation in cell culture under conditions which: (a) enables expression of the recombinant polypeptide; and b) permeabilizing the cell to form a spheroplast secreting the recombinant polypeptide, wherein said fermentation step comprises adding a stabilizing agent to the cell culture; iii) purifying the fermented cell culture comprising the secreted recombinant protein, wherein said purification comprises e) adding a flocculating agent to the cell culture, wherein the flocculating agent is polyethyleneimine (PEI); f) primary clarification of the flocculated cell culture using a first clarification filter having a pore size of at least about 0.4 µm or greater retention limits, where the clarification step does not include centrifugation. 2. The method of claim 1, wherein the method further comprises a secondary clarification step using a second filter having a pore size that provides retention limits of at least about 0.22 um. 3. A method according to claim 1 or 2, wherein the primary clarification step uses a first filter having a pore size that provides retention limits of at least about 0.4 to about 0.8 pm. 4. The method of claim 4, wherein the second clarification step uses a second filter having a pore size that provides retention limits of at least about 0.4-0.8 pm or at least from about 1.0 pm to about 3.0 pm. 5. A method according to claim 1 or 2, characterized in that the primary clarification step and/or the secondary clarification step is microfiltration, wherein the microfiltration is optionally deep filtration. 6. A method according to claim 5, characterized in that the microfiltration is selected from normal flow filtration (NFF) or tangential flow filtration (TFF). 7. A method according to any of the preceding claims, wherein the clarified cell culture has a turbidity of less than about 20 NTU. 8. A method according to any of the preceding claims, characterized in that the method is carried out in a closed system such that a sterile flow is maintained between the bioreactor and the first and second clarification filters. 9. A method according to any of the preceding claims, further comprising the step of subjecting said clarified cell culture to one or more purification steps of said recombinant protein. 10. A composition according to any preceding claim, wherein the stabilizing agent comprises sucrose, Na2SO4 and Brij 35, optionally 1 M sucrose, 0.5 M Na2SO4 and 0.5% Brij 35. 11. A protein production method comprising: i. culturing a recombinant Escherichia coli cell under conditions that: (a) enables expression of the protein; and (b) allows the cell to become permeable to form a spheroplast that secretes the protein; and ii. isolation of the protein from culture without complete knockdown of the recombinant cell, wherein the cell comprises an expression system comprising: (a) a nucleic acid encoding a protein operably linked to a first inducible promoter, wherein the protein is 2-O-methyltransferase (OMT); and (b) a nucleic acid encoding T4 lysozyme in frame with a nucleic acid encoding a PelB secretory signal peptide operably linked to a second inducible promoter. 12. A method according to any one of claims 1-11, characterized in that the method does not include: (i) mechanical disruption of the cells; (ii) addition of an exogenous enzyme that degrades the cell wall; and (iii) transforming the cell with expression vectors containing a nucleic acid encoding an exogenous enzyme that disrupts the cytoplasmic membrane. 13. The method according to any one of claims 1-12, wherein the nucleic acid encoding the protein operably linked to the first inducible promoter is in the first construct and the nucleic acid encoding T4 lysozyme is in frame with the nucleic acid encoding PelB. secretory signal peptide, is present in the second construct. 14. The method according to any one of claims 1-13, characterized in that the first inducible promoter and the second inducible promoter are induced sequentially. 15. The method according to any one of claims 1-13, characterized in that the first inducible promoter and the second inducible promoter are simultaneously induced. 16. The method of any preceding claim, wherein the first inducible promoter is an IPTG-inducible promoter, optionally wherein the IPTG-inducible promoter is PT7. 17. The method of any preceding claim, wherein the second inducible promoter is an arabinose-inducible promoter, optionally wherein the arabinose-inducible promoter is araB. 18. A method according to any one of the preceding claims, characterized in that the T4 lysozyme enzyme is encoded by the gene E. 19. A method according to any one of the preceding claims, characterized in that the E. coli is an Escherichia coli JS007 strain or an Escherichia coli B strain. 20. A method according to any of the preceding claims, wherein the fermentation or culturing comprises changing the first temperature to a second temperature, optionally wherein the second temperature is in the range of 25°C to 36°C and the first temperature is in the range of 36.8° C to 37.2 °C. 21. A recombinant protein produced by the method according to any one of claims 1-20.