METHODS TO CONTROL PROTEIN HETEROGENEITY
The instant invention relates to the field of protein production, and in particular to compositions and processes for controlling and limiting the heterogeneity of proteins expressed in host cells.
The present application is a divisional application of U.S. application Ser. No. 13/804,220, filed Mar. 14, 2013, which claims priority to U.S. Provisional Application No. 61/696,219, filed on Sep. 2, 2012, the disclosure of each of which are incorporated by reference herein in their entirety.
1. INTRODUCTIONThe instant invention relates to the field of protein production, and in particular to compositions and processes for controlling and limiting the heterogeneity of proteins expressed in host cells.
2. BACKGROUND OF THE INVENTIONThe production of proteins for biopharmaceutical applications typically involves the use of cell cultures that are known to produce proteins exhibiting varying levels of heterogeneity. The basis for such heterogeneity includes, but is not limited to, the presence of distinct glycosylation substitution patterns. For example, such heterogeneity can be observed in increases in the fraction of proteins substituted with agalactosyl fucosylated biantennary oligosaccharides NGA2F+NGA2F−GlcNAc and decreases in the fraction of proteins substituted with galactose-containing fucosylated biantennary oligosaccharides NA1F+NA2F. Such heterogeneity can be assayed by releasing oligosaccharides present on the protein of interest via enzymatic digestion with N-glycanase. Once the glycans are released, the free reducing end of each glycan can be labeled by reductive amination with a fluorescent tag. The resulting labeled glycans are separated by normal-phase HPLC (NP-HPLC) and detected by a fluorescence detector for quantitation.
Technological advances in recombinant protein production analysis have provided unique opportunities for identifying the extent of heterogeneity exhibited by a particular protein population, particularly in the context of large-scale production of recombinant proteins. Although such advances have allowed for the robust characterization of protein heterogeneity, there remains a need in the art to identify culture conditions and production methods that allow for control over the development of such heterogeneity. Control of protein heterogeneity is particularly advantageous in the context of cell culture processes used for commercially produced recombinant bio-therapeutics as such heterogeneity has the potential to impact therapeutic utility. The instant invention addresses this need by providing compositions and processes to control protein heterogeneity.
3. SUMMARY OF THE INVENTIONThe present invention is directed to compositions and methods that control (modulate or limit) protein heterogeneity arising in a population of proteins, e.g., in the context of recombinant protein production.
In certain embodiments, the heterogeneity corresponds to the glycosylation state of individual members of a population of proteins. In certain embodiments, control is exerted over the type of glycosylation substitutions present on individual members of a population of proteins. In certain embodiments, control is exerted over the extent of glycosylation substitutions present on individual members of a population of proteins. In certain embodiments, control is exerted over both the type and extent of glycosylation substitutions present on individual members of a population of proteins. In certain embodiments, such control results in a decrease in the amount of NGA2F+NGA2F−GlcNac oligosaccharides and/or an increase in the amount of NA1F+NA2F oligosaccharides linked to the protein of interest. In certain embodiments, such control results in an increase in the amount of NGA2F+NGA2F−GlcNac oligosaccharides and/or a decrease in the amount of NA1F+NA2F oligosaccharides linked to the protein of interest.
In certain embodiments, control over protein glycosylation heterogeneity is exerted by employing specific hydrolysates during production of the protein of interest, for example, but not by way of limitation, in adaptation cultures performed in media supplemented with hydrolysates. In certain embodiments, control over protein glycosylation heterogeneity is exerted by maintaining certain yeastolate to phytone ratios during production of the protein of interest. In certain embodiments, control over protein glycosylation heterogeneity is exerted by the addition of asparagine during the production of the protein of interest. In certain embodiments the amount of asparagine present in the cell culture media will range from about 0 mM to about 26 mM.
In certain embodiments, control over the heterogeneity of the protein compositions described herein is exerted by employing one or more of the foregoing methods during the production and purification of the desired proteins, such as antibodies or antigen-binding portions thereof, described herein.
The heterogeneity of the proteins of interest in the resultant sample product can be analyzed using methods well known to those skilled in the art, e.g., weak cation exchange chromatography (WCX), capillary isoelectric focusing (cIEF), size-exclusion chromatography, Poros™ A HPLC Assay, Host Cell Protein ELISA, Protein A ELISA, and western blot analysis.
In yet another embodiment, the invention is directed to one or more pharmaceutical compositions comprising an isolated protein, such as an antibody or antigen-binding portion thereof, and an acceptable carrier. In another aspect, the compositions further comprise one or more pharmaceutically acceptable carriers, diluents, and/or pharmaceutical agents.
For clarity and not by way of limitation, this detailed description is divided into the following sub-portions:
-
- 5.1 Definitions; and
- 5.2 Control of Heterogeneity:
- 5.2.1 Supplementation of CD Media with Yeast and/or Plant Hydrolysates
- 5.2.2 Changing Yeast to Plant Hydrolysate Ratio in Cell Culture Medium
- 5.2.3 Supplementation with Asparagine
5.1 DEFINITIONS
In order that the present invention may be more readily understood, certain terms are first defined.
As used herein, the term “glycosylation” refers to the addition of a carbohydrate to an amino acid. Such addition commonly, although not exclusively, occurs via a nitrogen of asparagine or arginine (“N-linked” glycosylation) or to the hydroxy oxygen of serine, threonine, tyrosine, hydroxylysine, or hydroxyproline side-chains (“O-linked” glycosylation). In eukaryotes, N-linked glycosylation occurs on the asparagine of the consensus sequence Asn-Xaa-Ser/Thr, in which Xaa is any amino acid except proline (Komfeld et al., Ann Rev Biochem 54: 631-664 (1985); Kukuruzinska et al, Proc. Natl. Acad. Sci. USA 84: 2145-2149 (1987); Herscovics et al, FASEB J. 7:540-550 (1993); and Orlean, Saccharomyces Vol. 3 (1996)). O-linked glycosylation also takes place at serine or threonine residues (Tanner et al., Biochim. Biophys. Acta. 906: 81-91 (1987); and Hounsell et al, Glycoconj. J. 13: 19-26 (1996)). However, other glycosylation patterns can be formed, e.g., by linking glycosylphosphatidyl-inositol to the carboxyl-terminal carboxyl group of a protein.
The term “antibody” includes an immunoglobulin molecule comprised of four polypeptide chains, two heavy (H) chains and two light (L) chains inter-connected by disulfide bonds. Each heavy chain is comprised of a heavy chain variable region (abbreviated herein as HCVR or VH) and a heavy chain constant region (CH). The heavy chain constant region is comprised of three domains, CH1, CH2 and CH3. Each light chain is comprised of a light chain variable region (abbreviated herein as LCVR or VL) and a light chain constant region. The light chain constant region is comprised of one domain, CL. The VH and VL regions can be further subdivided into regions of hypervariability, termed complementarity determining regions (CDRs), interspersed with regions that are more conserved, termed framework regions (FR). Each VH and VL is composed of three CDRs and four FRs, arranged from amino-terminus to carboxy-terminus in the following order: FR1, CDR1, FR2, CDR2, FR3, CDR3, FR4.
The term “antigen-binding portion” of an antibody (or “antibody portion”) includes fragments of an antibody that retain the ability to specifically bind to an antigen (e.g., in the case of Adalimumab, hTNFα). It has been shown that the antigen-binding function of an antibody can be performed by fragments of a full-length antibody. Examples of binding fragments encompassed within the term “antigen-binding portion” of an antibody include (i) a Fab fragment, a monovalent fragment comprising the VL, VH, CL and CH1 domains; (ii) a F(ab′)2 fragment, a bivalent fragment comprising two Fab fragments linked by a disulfide bridge at the hinge region; (iii) a Fd fragment comprising the VH and CH1 domains; (iv) a Fv fragment comprising the VL and VH domains of a single arm of an antibody, (v) a dAb fragment (Ward et al., (1989) Nature 341:544-546, the entire teaching of which is incorporated herein by reference), which comprises a VH domain; and (vi) an isolated complementarity determining region (CDR). Furthermore, although the two domains of the Fv fragment, VL and VH, are coded for by separate genes, they can be joined, using recombinant methods, by a synthetic linker that enables them to be made as a single protein chain in which the VL and VH regions pair to form monovalent molecules (known as single chain Fv (scFv); see, e.g., Bird et al. (1988) Science 242:423-426; and Huston et al. (1988) Proc. Natl. Acad. Sci. USA 85:5879-5883, the entire teachings of which are incorporated herein by reference). Such single chain antibodies are also intended to be encompassed within the term “antigen-binding portion” of an antibody. Other forms of single chain antibodies, such as diabodies are also encompassed. Diabodies are bivalent, bispecific antibodies in which VH and VL domains are expressed on a single polypeptide chain, but using a linker that is too short to allow for pairing between the two domains on the same chain, thereby forcing the domains to pair with complementary domains of another chain and creating two antigen binding sites (see, e.g., Holliger, P., et al. (1993) Proc. Natl. Acad. Sci. USA 90:6444-6448; Poljak, R. J., et al. (1994) Structure 2:1121-1123, the entire teachings of which are incorporated herein by reference). Still further, an antibody or antigen-binding portion thereof may be part of a larger immunoadhesion molecule, formed by covalent or non-covalent association of the antibody or antibody portion with one or more other proteins or peptides. Examples of such immunoadhesion molecules include use of the streptavidin core region to make a tetrameric scFv molecule (Kipriyanov, S. M., et al. (1995) Human Antibodies and Hybridomas 6:93-101, the entire teaching of which is incorporated herein by reference) and use of a cysteine residue, a marker peptide and a C-terminal polyhistidine tag to make bivalent and biotinylated scFv molecules (Kipriyanov, S. M., et al. (1994) Mol. Immunol. 31:1047-1058, the entire teaching of which is incorporated herein by reference). Antibody portions, such as Fab and F(ab′)2 fragments, can be prepared from whole antibodies using conventional techniques, such as papain or pepsin digestion, respectively, of whole antibodies. Moreover, antibodies, antibody portions and immunoadhesion molecules can be obtained using standard recombinant DNA techniques, as described herein. In one aspect, the antigen binding portions are complete domains or pairs of complete domains.
As used herein, the term “recombinant host cell” (or simply “host cell”) refers to a cell into which a recombinant expression vector has been introduced. It should be understood that such terms are intended to refer not only to the particular subject cell but to the progeny of such a cell. Because certain modifications may occur in succeeding generations due to either mutation or environmental influences, such progeny may not, in fact, be identical to the parent cell, but are still included within the scope of the term “host cell” as used herein. In certain embodiments the host cell is employed in the context of a cell culture.
As used herein, the term “cell culture” refers to methods and techniques employed to generate and maintain a population of host cells capable of producing a recombinant protein of interest, as well as the methods and techniques for optimizing the production and collection of the protein of interest. For example, once an expression vector has been incorporated into an appropriate host, the host can be maintained under conditions suitable for high level expression of the relevant nucleotide coding sequences, and the collection and purification of the desired recombinant protein. Mammalian cells are preferred for expression and production of the recombinant of the present invention; however other eukaryotic cell types can also be employed in the context of the instant invention. See, e.g., Winnacker, From Genes to Clones, VCH Publishers, N.Y., N.Y. (1987). Suitable mammalian host cells for expressing recombinant proteins according to the invention include Chinese Hamster Ovary (CHO cells) (including dhfr-CHO cells, described in Urlaub and Chasin, (1980) PNAS USA 77:4216-4220, used with a DHFR selectable marker, e.g., as described in Kaufman and Sharp (1982) Mol. Biol. 159:601-621, the entire teachings of which are incorporated herein by reference), NS0 myeloma cells, COS cells and SP2 cells. Other, non-limiting, examples of useful mammalian host cell lines are monkey kidney CV1 line transformed by SV40 (COS-7, ATCC CRL 1651); human embryonic kidney line (293 or 293 cells subcloned for growth in suspension culture, Graham et al., J. Gen Virol. 36:59 (1977)); baby hamster kidney cells (BHK, ATCC CCL 10); Chinese hamster ovary cells/-DHFR (CHO, Urlaub et al., Proc. Natl. Acad. Sci. USA 77:4216 (1980)); mouse sertoli cells (TM4, Mather, Biol. Reprod. 23:243-251 (1980)); monkey kidney cells (CV1 ATCC CCL 70); African green monkey kidney cells (VERO-76, ATCC CRL-1587); human cervical carcinoma cells (HELA, ATCC CCL 2); canine kidney cells (MDCK, ATCC CCL 34); buffalo rat liver cells (BRL 3A, ATCC CRL 1442); human lung cells (W138, ATCC CCL 75); human liver cells (Hep G2, HB 8065); mouse mammary tumor (MMT 060562, ATCC CCL51); TRI cells (Mather et al., Annals N.Y. Acad. Sci. 383:44-68 (1982)); MRC 5 cells; FS4 cells; and a human hepatoma line (Hep G2), the entire teachings of which are incorporated herein by reference.
When using the cell culture techniques of the instant invention, the protein of interest can be produced intracellularly, in the periplasmic space, or directly secreted into the medium. In embodiments where the protein of interest is produced intracellularly, the particulate debris, either host cells or lysed cells (e.g., resulting from homogenization), can be removed by a variety of means, including but not limited to, by centrifugation or ultrafiltration. Where the protein of interest is secreted into the medium, supernatants from such expression systems can be first concentrated using a commercially available protein concentration filter, e.g., an Amicon™ or Millipore Pellicon™ ultrafiltration unit, which can then be subjected to one or more additional purification techniques, including but not limited to affinity chromatography, including protein A affinity chromatography, ion exchange chromatography, such as anion or cation exchange chromatography, and hydrophobic interaction chromatography.
As used herein a “recombinant expression vector” can be any suitable recombinant expression vector, and can be used to transform or transfect any suitable host. For example, one of ordinary skill in the art would appreciate that transformation or transfection is a process by which exogenous nucleic acid such as DNA is introduced into a cell wherein the transformation or transfection process involves contacting the cell with the exogenous nucleic acid such as the recombinant expression vector as described herein. Non-limiting examples of such expression vectors are the pUC series of vectors (Fermentas Life Sciences), the pBluescript series of vectors (Stratagene, LaJolla, Calif.), the pET series of vectors (Novagen, Madison, Wis.), the pGEX series of vectors (Pharmacia Biotech, Uppsala, Sweden), and the pEX series vectors (Clontech, Palo Alto, Calif.).
As used herein, the term “recombinant protein” refers to a protein produced as the result of the transcription and translation of a gene carried on a recombinant expression vector that has been introduced into a host cell. In certain embodiments the recombinant protein is an antibody, preferably a chimeric, humanized, or fully human antibody. In certain embodiments the recombinant protein is an antibody of an isotype selected from group consisting of: IgG (e.g., IgG1, IgG2, IgG3, IgG4), IgM, IgA1, IgA2, IgD, or IgE. In certain embodiments the antibody molecule is a full-length antibody (e.g., an IgG1 or IgG4 immunoglobulin) or alternatively the antibody can be a fragment (e.g., a Fc fragment or a Fab fragment).
As used herein, the term “Adalimumab”, also known by its trade name Humira® (Abbott Laboratories) refers to a human IgG antibody that binds the human form of tumor necrosis factor alpha. In general, the heavy chain constant domain 2 (CH2) of the Adalimumab IgG-Fc region is glycosylated through covalent attachment of oligosaccharide at asparagine 297 (Asn-297). Adalimumab produced by Chinese hamster ovary (CHO) cells exists in 6 oligosaccharide forms, designated as NGA2F, NGA2F−GlcNAc, NA1F, NA2F, M5 and M6. Weak cation-exchange chromatography (WCX) analysis of the antibody has shown that it has three main charged-variants (i.e. Lys 0, Lys 1, and Lys 2). These variants, or “charged isomers,” are the result of incomplete posttranslational cleavage of the C-terminal lysine residues. In addition, WCX analysis has show that production of the antibody can result in the accumulation of two acidic species, identified herein as AR1 and AR2.
The term “about”, as used herein, is intended to refer to ranges of approximately 10-20% greater than or less than the referenced value. In certain circumstances, one of skill in the art will recognize that, due to the nature of the referenced value, the term “about” can mean more or less than a 10-20% deviation from that value.
The term “control”, as used herein, is intended to refer to both limitation as well as to modulation. For example, in certain embodiments, the instant invention provides methods for controlling diversity that decrease the diversity of certain characteristics of protein populations, including, but not limited to, glycosylation patterns. Such decreases in diversity can occur by: (1) promotion of a desired characteristic, such as a favored glycosylation pattern; (2) inhibition of an unwanted characteristic, such as a disfavored glycosylation pattern; or (3) a combination of the foregoing. As used herein, the term “control” also embraces contexts where heterogeneity is modulated, i.e., shifted, from one diverse population to a second population of equal or even greater diversity, where the second population exhibits a distinct profile of the characteristic of interest. For example, in certain embodiments, the methods of the instant invention can be used to modulate the types of oligosaccharide substitutions present on proteins from a first population of substitutions to a second equally diverse, but distinct, population of substitutions.
5.2 CONTROL OF PROTEIN HETEROGENEITY
5.2.1 Supplementation of CD Media with Yeast and/or Plant Hydrolysates
It is well known that the pattern of glycoforms that arise in recombinant proteins, including monoclonal antibodies, can be affected by culture conditions during production. (Nam et al., The effects of culture conditions on the glycosylation of secreted human placental alkaline phosphatase produced in Chinese hamster ovary cells. Biotechnol Bioeng. 2008 Aug. 15; 100(6): 1178-92). Consistency in the quality of the glycoproteins is important because glycosylation may impact protein solubility, activity, and circulatory half-life. (Gawlitzek et al., Effect of Different Cell Culture Conditions on the Polypeptide Integrity and N-glycosylation of a Recombinant Model Glycoprotein. Biotechnol. Bioeng. 1995; 46:536-544; and Hayter et al., Glucose-limited Chemostat Culture of Chinese Hamster Ovary Cells Producing Recombinant Human Interferon-γ. Biotechnol. Bioeng. 1992; 39:327-335).
In certain instances, such glycosylation-based heterogeneity can take the form of differences in the galactose composition of N-linked oligosaccharides. For example, a terminal galactose is added to NGA2F by β-galactosyltransferase enzyme in the presence of manganese chloride, to produce NA1F (in the case of an addition of a single terminal galactose) or NA2F (in the case of an addition of two terminal galactose molecules). This galactosyltransferase-mediated reaction employs UDP-galactose as the sugar substrate and Mn2+ as a cofactor for galactosyltransferase. Thus, without being bound by theory, it is believed that a change in protein homogeneity taking the form of an increase in the fraction of N-linked oligosaccharide NGA2F and a decrease in the fraction of NA1F+NA2F N-linked oligosaccharides could be caused by either an insufficient amount of the substrate (UDP-galactose), the cofactor for galactosyltransferase (Mn2+), or both.
The experiments disclosed herein demonstrate that, in certain embodiments, supplementation of CD cell culture media with yeast and/or plant hydrolysates can modulate product quality of a mAb by, in certain embodiments, decreasing the NGA2F+NGA2F−GlcNac and, in certain embodiments, increasing the NA1F+NA2F oligosaccharides. These results were achieved in multiple CD media available from multiple vendors (Life Sciences Gibco, HyClone, and Irvine Scientific), using yeast and/or plant hydrolysates (for example, but not by way of limitation, soy, wheat, rice, cotton seed, pea, corn, and potato) from multiple vendors (BD Biosciences, Organotechnie, Sheffield/Kerry Biosciences, Irvine Scientific, and DMV International). In experiments where yeast or plant hydrolysates were added individually, a dose-dependent effect in the extent of reduction of NGA2F+NGA2F−GlcNac oligosaccharides (and a corresponding increase in the NA1F+NA2F oligosaccharides) with increasing yeast or plant hydrolysates concentration in culture CD media was observed. For example, but not by way of limitation, yeast hydrolysates can be used to supplement a CD cell culture media at concentrations ranging from about 2 g/L to about 11 g/L to achieve the desired reduction of NGA2F+NGA2F−GlcNac oligosaccharides and a corresponding increase in the NA1F+NA2F oligosaccahrides. In certain non-limiting embodiments, yeast hydrolysates can be used to supplement a CD cell culture media at concentrations of about 2 g/L, about 5 g/L, or about 11 g/L. In certain non-limiting embodiments, plant hydrolysates can be used to supplement a CD cell culture media at concentrations ranging from about 2 g/L to about 15 g/L to achieve the desired reduction of NGA2F+NGA2F−GlcNac oligosaccahrides and a corresponding increase in the NA1F+NA2F oligosaccharides. In certain non-limiting embodiments, plant hydrolysates can be used to supplement a CD cell culture media at concentrations of about 2 g/L, about 4 g/L, 7 g/L, 10 g/L, or about 15 g/L.
In certain embodiments, the concentration of yeast and/or plant hydrolysates is maintained in such a manner as to reduce the NGA2F+NGA2F−GlcNac sum in a protein or antibody sample by about 1%, 1.2%, 1.5%, 2%, 2.2%, 2.5%, 3%, 3.2%, 3.5%, 4%, 4.2%, 4.5%, 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, 95%, 100%, and ranges within one or more of the preceding. In certain embodiments, the concentration of yeast and/or plant hydrolysates is maintained in such a manner as to increase the NA1F+NA2F sum in a protein or antibody sample by about 1%, 1.2%, 1.5%, 2%, 2.2%, 2.5%, 3%, 3.2%, 3.5%, 4%, 4.2%, 4.5%, 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, 95%, 100%, and ranges within one or more of the preceding.
In certain embodiments, control over the glycosylation distribution of proteins produced by cell culture can be exerted by maintaining the appropriate yeast hydrolysate concentration in the cell culture expressing the protein of interest as described herein. Specific culture conditions can be used in various cultivation methods including, but not limited to, batch, fed-batch, chemostat and perfusion, and with various cell culture equipment including, but not limited to, shake flasks with or without suitable agitation, spinner flasks, stirred bioreactors, airlift bioreactors, membrane bioreactors, reactors with cells retained on a solid support or immobilized/entrapped as in microporous beads, and any other configuration appropriate for optimal growth and productivity of the desired cell line
5.2.2 Changing Yeast to Plant Hydrolysate Ratio in Cell Culture Medium
The instant disclosure relates to control of the glycosylation distribution in mammalian cell culture processes, including where specific components, such as hydrolyzed yeast and soy-based supplements, are commonly used and are typical constituents of suspension culture media in such processes. These nutrients are important for ensuring both robust cell growth and production of glycoproteins. However, the present invention utilizes these components in such a way to affect the critical quality attributes of the glycoprotein. For example, but not by way of limitation, by adjusting the concentration ratio of these two hydrolysates, yeast and soy (phytone), within the range of about 0.25 to about 1.55, the resultant glycosylation distribution can be modified. As outlined in Example 1, non-limiting embodiments of the present invention include supplements comprising 100% yeast hydrolysate as well as those that are 100% plant hydrolysate. Thus, this disclosure provides a means to modulate glycosylation variations introduced by process inputs, such as raw materials, and other variability inherent in dynamic manufacturing operations. Ultimately, the disclosure enables in-process control of protein glycosylation with respect to desired product specifications.
In certain embodiments, the ratio of these two hydrolysates, yeast and soy (phytone), is maintained in such a manner as to reduce the NGA2F+NGA2F−GlcNac sum in a protein or antibody sample by about 1%, 1.2%, 1.5%, 2%, 2.2%, 2.5%, 3%, 3.2%, 3.5%, 4%, 4.2%, 4.5%, 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, 95%, 100%, and ranges within one or more of the preceding. In certain embodiments, the ratio of these two hydrolysates, yeast and soy (phytone), is maintained in such a manner as to increase the NA1F+NA2F sum in a protein or antibody sample by about 1%, 1.2%, 1.5%, 2%, 2.2%, 2.5%, 3%, 3.2%, 3.5%, 4%, 4.2%, 4.5%, 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, 95%, 100%, and ranges within one or more of the preceding.
In certain embodiments, control over the glycosylation distribution of protein produced by cell culture can be exerted by maintaining the appropriate yeast to plant hydrolysate ratio in the cell culture expressing the protein of interest as described herein. Specific culture conditions can be used in various cultivation methods including, but not limited to, batch, fed-batch, chemostat and perfusion, and with various cell culture equipment including, but not limited to, shake flasks with or without suitable agitation, spinner flasks, stirred bioreactors, airlift bioreactors, membrane bioreactors, reactors with cells retained on a solid support or immobilized/entrapped as in microporous beads, and any other configuration appropriate for optimal growth and productivity of the desired cell line
5.2.3 Supplementation with Asparagine
The instant disclosure relates to control of the glycosylation distribution in mammalian cell culture processes, including where specific components, such as amino acids and amino acid-based supplements, are commonly used and are typical constituents of suspension culture media. These nutrients are important for ensuring both robust cell growth and production of glycoproteins. However, this present invention utilizes these components, and in particular asparagine and/or glutamine in such a way to affect the critical quality attributes of the glycoprotein. For example, but not by way of limitation, by adjusting the concentration of one or both of these two amino acids the resultant glycosylation distribution can be modified. Thus, this disclosure provides a means to modulate glycosylation variations introduced by process inputs, such as raw materials, and other variability inherent in dynamic manufacturing operations. Ultimately, the disclosure enables in-process control of protein glycosylation with respect to desired product specifications.
The experiments disclosed herein demonstrate that, in certain embodiments, supplementation of cell culture media with asparagine and/or glutamine can modulate product quality of a mAb by, in certain embodiments, increasing the NGA2F+NGA2F−GlcNac and, in certain embodiments, decreasing the NA1F+NA2F oligosaccharides. For example, but not by way of limitation, the percentage of NGA2F+NGA2F−GlcNac can be increased by 2-4% and the percentage of NA1F+NA2F was decreased by 2-5% when 0.4 to 1.6 g/L asparagine is added on either day 0 or days 6 or 7, as outlined in Example 5, below. Similarly, addition of 0.4 g/L glutamine, to the culture run described in Example 5, below, increased the percentage of NGA2F+NGA2F−GlcNac by 1% and lowered the percentage of NA1F+NA2F by 1%. Finally, adding both asparagine and glutamine (0.4 g/L of each), to the cell culture run described in Example 5, below, increased the percentage of NGA2F+NGA2F−GlcNac by 3% and decreased the percentage of NA1F+NA2F by 4%. In addition, the cell growth profile is the same when 0.8 and 1.6 g/L of asparagine was added, but a dose dependent effect on oligosaccharide distribution was observed, indicating that the effect on oligosaccharide distribution was due to the addition of asparagine and not the increased maximum viable cell density or delayed drop in viability. In certain embodiments, the total amount of asparagine in the cell culture media will range from about 0 mM to about 26 mM. In certain embodiments, for example those embodiments where a hydrolysate media is employed, the range of asparagine in the cell culture media will range from about 1.3 mM to about 14.6 mM. In certain embodiments, for example, but not limited to, those embodiments where GIA1 media is employed, the range of asparagine in the cell culture media will range from about 12.3 mM to about 25.7 mM.
In certain embodiments, the concentration of asparagine and/or glutamine is maintained in such a manner as to reduce the NA1F+NA2F sum in a protein or antibody sample by about 1%, 1.2%, 1.5%, 2%, 2.2%, 2.5%, 3%, 3.2%, 3.5%, 4%, 4.2%, 4.5%, 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, 95%, 100%, and ranges within one or more of the preceding. In certain embodiments, the concentration of asparagine and/or glutamine is maintained in such a manner as to increase the NGA2F+NGA2F−GlcNac sum in a protein or antibody sample by about 1%, 1.2%, 1.5%, 2%, 2.2%, 2.5%, 3%, 3.2%, 3.5%, 4%, 4.2%, 4.5%, 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, 95%, 100%, and ranges within one or more of the preceding.
In certain embodiments, control over the glycosylation distribution of protein produced by cell culture can be exerted by maintaining the appropriate asparagine and/or glutamine concentration in the cell culture expressing the protein of interest as described herein. Specific culture conditions can be used in various cultivation methods including, but not limited to, batch, fed-batch, chemostat and perfusion, and with various cell culture equipment including, but not limited to, shake flasks with or without suitable agitation, spinner flasks, stirred bioreactors, airlift bioreactors, membrane bioreactors, reactors with cells retained on a solid support or immobilized/entrapped as in microporous beads, and any other configuration appropriate for optimal growth and productivity of the desired cell line.
EXAMPLES Example 1 Control of Heterogeneity by Addition of Hydrolysates to CD Media GIA-1 for Culture of an Adalimumab-Producing CHO Cell Line #1Control of heterogeneity of therapeutic monoclonal antibodies (mAbs) can aid in ensuring their efficacy, stability, immunogenicity, and biological activity. Media composition has been shown to play a role in product quality of mAbs together with process conditions and choice of cell line. In certain embodiments, the present invention provides methods for fine-tuning the product quality profile of a mAb produced in various Chinese hamster ovary (CHO) cell lines by supplementation of yeast and/or plant hydrolysates to chemically defined (CD) media. In certain embodiments, the resulting mAb product is characterized by having a decreased content of complex agalactosylated glycans NGA2F and NGA2F−GlcNac and increased levels of terminally galactosylated glycans NA1F and NA2F. In certain embodiments, addition of increasing amounts of yeast, soy or wheat hydrolysates from several suppliers to a CD medium resulted in altered product quality profiles in a concentration-dependent manner.
In the studies summarized in this example, the effects on glycosylation resulting from the addition of yeast (Bacto TC Yeastolate: 2, 5, 11 g/L), soy (BBL Phytone Peptone: 2, 4, 7, 10, 15 g/L), or wheat (Wheat Peptone E1: 2, 4, 7, 10, 15 g/L) hydrolysates to CD medium GIA-1 (Life Technologies Gibco; proprietary formulation) in the adalimumab-producing CHO cell line #1 were investigated.
1.1 Materials and Methods
Adaptation and production media were supplemented with Bacto TC Yeastolate, BBL Phytone Peptone, or Wheat Peptone E1 according to the experimental design in
The adalimumab-producing cultures were expanded for 3 passages (3 days each) in their respective adaptation media in a combination of 250 mL (50 mL or 100 mL working volume) and 500 mL (150 mL working volume) Corning vented non-baffled shake flasks and maintained on an orbital shaker at 110 RPM in a 35° C., 5% CO2 dry incubator. At each passage, cultures were inoculated at an initial viable cell density (VCD) of approximately 0.5×106 cells/mL.
Production cultures were initiated in duplicate 500 mL Corning, vented, non-baffled shake flasks each containing 200 mL culture in dry incubators at 35° C., 5% CO2, and 110 RPM. Initial VCD was approximately 0.5×106 cells/mL. A 1.25% (v/v) 40% glucose stock solution was fed when the media glucose concentration was less than 3 g/L.
For all studies described throughout this application, samples were collected daily and measured for cell density and viability using a Cedex cell counter. Retention samples for titer analysis (2×1.5 mL per condition) via Poros A method were collected daily after culture viability fell below 90%. Samples were centrifuged at 12,000 RPM for 5 min and the supernatant was stored at −80° C. until further analysis. The harvest procedure was performed by centrifugation of the culture sample at 3,000 RPM for 30 min followed by storage of the supernatant in 125 mL PETG bottles at −80° C. until protein A purification, oligosaccharide, and WCX-10 analysis.
For the oligosaccharide assay, the oligosaccharides are released from the protein by enzymatic digestion with N-glycanase. Once the glycans are released, the free reducing end of each glycan is labeled by reductive amination with a fluorescent tag, 2-aminobenzamide (2-AB). The resulting labeled glycans are separated by normal-phase HPLC (NP-HPLC) in acetonitrile: 50 mM ammonium formate, pH 4.4, and detected by a fluorescence detector. Quantitation is based on the relative area percent of detected sugars. The relative area percents of the agalactosyl fucosylated biantennary oligosaccharides (NGA2F+[NGA2F−GlcNac]) and the galactose-containing fucosylated biantennary oligosaccharides NA1F+NA2F are reported and discussed.
1.2 Culture Growth and Productivity
The majority of cultures grew to a similar peak VCD in the range of 9-11×106 cells/mL. Cultures supplemented with 11 g/L yeast hydrolysate BD TC yeastolate experienced slight inhibition of growth (
1.3 Oligosaccharide Analysis
Addition of yeast, soy, or wheat hydrolysates to CD media GIA-1 lowered the percentage of glycans NGA2F+NGA2F−GlcNac by 1-14% and increased the percentage of NA1F+NA2F glycans by 2-12% compared to control condition (NGA2F+NGA2F−GlcNac: 89%; NA1F+NA2F: 6%) (
In the study summarized in this example, the effects of combined yeast and soy hydrolysates addition to CD media from multiple suppliers: Life Technologies Gibco (OptiCHO and GIA-1), Irvine Scientific (IS CHO-CD), and HyClone/Thermo Scientific (CDM4CHO) on product quality in the adalimumab-producing CHO cell line #1 utilized in Example 1 were evaluated.
2.1 Materials and Methods
The liquid or powder formulation media were purchased from multiple vendors (Life Technologies Gibco—OptiCHO and GIA-1; Irvine Scientific—IS CHO-CD; and HyClone/Thermo Scientific—CDM4CHO), reconstituted per the manufacturers' recommendations, and supplemented with Bacto TC Yeastolate and BBL Phytone Peptone according to the experimental design in
Cultures were expanded for 3 passages (3 days each) in their respective adaptation media in a combination of 250 mL (50 mL or 100 mL working volume) and 500 mL (150 mL working volume) Corning vented non-baffled shake flasks and maintained on an orbital shaker at 110 RPM in a 35° C., 5% CO2 dry incubator. Production cultures were initiated in duplicate 500 mL (200 mL working volume) Corning vented non-baffled shake flasks at an initial VCD of approximately 0.5×106 cells/mL. The shake flask study was run in an extended batch-mode by feeding a glucose solution (1.25% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L.
2.2 Culture Growth and Productivity
Commercially available CD media supported markedly different culture growth profiles with maximum VCD of 2-9×106 cells/mL and culture duration ranging from 7 to 15 days (
2.3 Oligosaccharide Analysis
The combined addition of yeast and soy hydrolysates to various commercially available CD media lowered the percentage of NGA2F+NGA2F−GlcNac glycans by 2-10% compared to control (
In the study summarized in this example, we investigated the effects on glycosylation resulting from the addition of yeast (5, 11 g/L), soy (4, 7 g/L) or wheat (4, 7 g/L) hydrolysates from multiple vendors (BD Biosciences, Sheffield/Kerry Biosciences, DMV International, Irvine Scientific, and Organotechnie) to CDM GIA-1 in the adalimumab-producing CHO cell line #1.
3.1 Materials and Methods
Adaptation and production media were supplemented with Bacto TC Yeastolate, BBL Phytone Peptone, or Wheat Peptone E1 according to the experimental design in
Cultures were expanded for 3 passages (3 days each) in their respective adaptation media in a combination of 250 mL (50 mL or 100 mL working volume) and 500 mL (150 mL working volume) Corning vented non-baffled shake flasks and maintained on an orbital shaker at 110 RPM in a 35° C., 5% CO2 dry incubator. Production cultures were initiated in duplicate 500 mL (200 mL working volume) Corning, vented, non-baffled shake flasks at an initial VCD of approximately 0.5×106 cells/mL. The shake flask study was run in an extended-batch mode by feeding a glucose solution (1.25% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L.
3.2 Culture Growth and Productivity
Culture growth and viability profiles were comparable among all test conditions (
3.3 Oligosaccharide Analysis
Addition of yeast, soy or wheat hydrolysates to CD media GIA-1 decreased the NGA2F+NGA2F−GlcNac glycans in a dose-dependent manner for all hydrolysate vendors evaluated (
To identify the role which the ratio of yeast to plant hydrolysate plays in connection with the generation of protein heterogeneity, experiments employing a range of different hydrolysate ratios were undertaken. The cell culture medium employed in each experimental process contains both yeast and soy hydrolysate (phytone). The ratios of yeast to soy hydrolysate (by weight) are 1.55, 0.67 and 0.25. The total weight of yeastolate and soy hydrolysate were not changed in each experimental process. Two distinct yeastolate lots were used in connection with these experiments (see
4.1. Materials and Methods
The CHO cell line #1 was employed in the studies covered here. The production medium used in this experiment contains basal medium PFCHO, Bacto TC yeastolate and phytone peptone. The pH of all media was adjusted to 7.15; and media osmolality was adjusted to 373-403 mOsmol/kg with sodium chloride. For each experiment, 500 mL shakers with 200 mL working volume were employed at the following conditions: 35° C. constant temperature; 5% CO2; and 110 RPM. Cultures were inoculated at an initial viable cell density (VCD) of approximately 0.5×106 cells/mL. Two mL of 40% w/w glucose solution was added to each shaker when the glucose concentration dropped below 2 g/L. The shakers were harvested when the viable cell density decreased to approximately 50%. The harvest broth was centrifuged at 3200 rpm for 30 min at 5° C. to remove cells and the supernatant was stored at −80° C.
Samples were taken daily from each shaker to monitor growth. The following equipment was used to analyze the samples: Cedex cell counter, Radiometer blood gas analyzer, YSI glucose analyzer, and osmometer. The harvest samples stored at −80° C. were later thawed and analyzed for titer with Poros A HPLC method. In addition, the thawed samples were filtered through a 0.2 μm filter, purified by Protein A chromatography, and then oligosaccharide analysis was performed as described in Example 1.
4.2 Cell Growth and Productivity
In the first hydrolysate study, the viable cell densities for the reduced ratios of yeastolate to phytone (i.e. Y/P=0.67 and Y/P=0.25) were much lower than the viable cell density for the 1.55 ratio of yeastolate to phytone (
4.3. Oligosaccharide Analysis
Glycosylation profiles for hydrolysate studies 1 and 2 are shown in
As shown in
Therefore, this study successfully demonstrated that reducing the ratio of yeastolate to phytone could alter oligosaccharide profile using two different lots of yeast hydrolysate.
Example 5 Control of Heterogeneity by Supplementation with AsparagineThe present invention relates to methods for modulating the glycosylation profile of a monoclonal antibody (mAb) by varying the concentration of asparagine in cell culture media. Cell culture medium components, such as asparagine, are commonly used and are typical constituents of suspension culture media. These nutrients are important for ensuring both robust cell growth and production of glycoproteins. It has been shown that the cell viability and product titer can be enhanced by the addition of asparagine to a glutamine-free production medium (Genentech, Inc. “Production of Proteins in Glutamine-Free Cell Culture Media” WO2011019619 (2010)). However, the present invention provides methods to modify glycosyaltion distribution by adjusting the concentration of asparagine. Without being bound by theory, it is thought that the effect of asparagine on glycosylation profile of an antibody is through its conversion to glutamine and/or aspartate. Asparagine is the amide donor for glutamine and can be converted to glutamine and/or aspartate (H Huang, Y Yu, X Yi, Y Zhang “Nitrogen metabolism of asparagine and glutamate in Vero cells studied by 1H/15 N NMR spectroscopy” Applied microbiology and biotechnology 77 (2007) 427-436). Glutamine and aspartate are important intermediates in pyrimidine synthesis; and it is known that enhancing de novo pyrimidine biosynthesis could increase intracellular UTP concentration (Genentech, Inc. “Galacosylation of Recombinant Glycoproteins” US20030211573 (2003)). In addition, studies have suggested that glutamine and aspartate limitation is expected to inhibit amino sugar synthesis (G B Nyberg, R R Balcarcel, B D Follstad, G Stephanopoulos, D I Wang “Metabolic effects on recombinant interferon-gamma glycosylation in continuous culture of Chinese hamster ovary cells” Biotechnology and Bioengineering 62 (1999) 336-47; D C F Wong, K T K Wong, L T Goh, C K Heng, M G S. Yap “Impact of dynamic online fed-batch strategies on metabolism, productivity and N-glycosylation quality in CHO cell cultures” Biotechnology and Bioengineering 89 (2005) 164-177). Both UTP and amino sugar are required for the synthesis of UDP−GlcNac, which is the substrate for protein glycosylation process. It is also possible that the effect of asparagine on glycosyaltion is via increasing ammonia concentration in the cell culture medium since it is showed that the addition of ammonia in CHO cultures could reduce the extent of glycosylation of synthesized EPO (M. Yang and M. Butler “Effect of Ammonia on the Glycosylation of Human Recombinant Erythropoietin in Culture” Biotechnol. Prog. 16 (2000) 751-759). We have found that ammonia concentration was increased after asparagine addition into the cell culture media.
In the studies summarized in Example 5, we investigated the effects on product quality attributes resulting from the addition of asparagine to hydrolysate based medium in an adalimumab-producing CHO cell line, generically named CHO cell line #1. Two experiments were performed in the instant Example. For the first experiment, glutamine and/or asparagine were added (at an individual concentration of 0.4 g/L) on day 6. For the second experiment, asparagine was added at different dosage (i.e. 0.4 g/L, 0.8 g/L or 1.6 g/L) either on day 0 (before inoculation) or together with the first glucose shot (happened on day 7).
5.1 Materials and Methods
The CHO cell line #1 was employed in the studies covered here. Upon thaw, cells were expanded in a 19-days seed train and then transferred into seed reactors for up to 7 days in growth medium. The cells were then brought to the laboratory and used in the small scale bioreactor experiments. The media used in these experiments contains basal media PFCHO (proprietary formulation), Bacto TC Yeastolate and Phytone Peptone.
Three litter Applikon bioreactors were sterilized and then charged with production medium. At inoculation, cells were aseptically transferred into each bioreactor to reach an initial cell density of 0.5×106 viable cells/mL. After inoculation, the bioreactors were set to the following conditions: pH=7.1, T=35° C., DO=30%, and agitation=200 rpm. The pH was shifted from 7.1 to 6.9 over the first 2.5 days and held at 6.9 for the remainder of the run. The percentage of dissolved oxygen was controlled by sparging a mixture of air and oxygen. The addition of 0.5 N NaOH or sparging of CO2 maintained the pH. When the glucose concentration fell below 2 g/L, approximately 1.25% (v/v) of glucose solution (400 g/kg) was added to the cell culture.
For the first experiment, glutamine and/or asparagine were added (at an individual concentration of 0.4 g/L) together with the first glucose shot (happened on day 6). For the second experiment, asparagine was added at different dosage (i.e. 0.4 g/L, 0.8 g/L or 1.6 g/L) either on day 0 (before inoculation) or together with the first glucose shot (happened on day 7).
Samples were taken daily from each reactor to monitor growth. The following equipment was used to analyze the samples: Cedex cell counter for cell density and viability; Radiometer ABL 5 blood gas analyzer for pH, pCO2 and pO2; YSI 7100 analyzer for glucose and lactate concentration. Some of the daily samples and the harvest samples were centrifuged at 3,000 RPM for 30 min and then the supernatants were stored at −80° C. Later, the thawed harvest samples were filtered through a 0.2 μm filter, purified by Protein A chromatography, and then oligosaccharide analysis was performed and then oligosaccharide analysis was performed as described in Example 1.
5.2 Culture Growth and Productivity
In both of the experiments performed in 3 L bioreactor in hydrolysate based media with CHO cell line #1 described in the instant Example, the addition of glutamine and/or asparagine together with a glucose shot increased the maximum cell density (
A drop in viability was delayed, as compared to control cultures, in both experiments described in the instant Example for approximately 3 days when glutamine and/or asparagine was added on day 6 or 7 (
5.3 Oligosaccharide Analysis
The experiments described in the instant Example indicate that oligosaccharide distribution is altered with the addition of asparagine and/or glutamine. The addition of asparagine increased NGA2F+NGA2F−GlcNac in a dose dependent manner. Compared to control, the percentage of NGA2F+NGA2F−GlcNac was increased by 1.0-3.9% and the percentage of NA1F+NA2F was decreased by 1.1-4.3% when 0.4 to 1.6 g/L asparagine was added on either day 0 or days 6 or 7 (
In the study summarized in this example, the effects on glycosylation resulting from the addition of yeast, soy or wheat hydrolysates to CD media IS CHO-CD (Irvine Scientific) in the adalimumab-producing CHO cell line #1 utilized in Example 1 were evaluated.
6.1 Materials and Methods
Adaptation and production media (Irvine Scientific IS CHO-CD 91119) were supplemented with Bacto TC Yeastolate, BBL Phytone Peptone, or Wheat Peptone E1 according to the experimental design in
Cultures were expanded for 3 passages (3 days each) in their respective adaptation media in a combination of 250 mL (50 mL or 100 mL working volume) and 500 mL (150 mL working volume) Corning vented non-baffled shake flasks and maintained on an orbital shaker at 110 RPM in a 35° C., 5% CO2 dry incubator. Production cultures were initiated in duplicate 500 mL (200 mL working volume) Corning vented non-baffled shake flasks at an initial VCD of approximately 0.5×106 cells/mL. The shake flask study was run in an extended-batch mode by feeding a glucose solution (1.25% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L.
6.2 Culture Growth and Productivity
Addition of yeast, soy or wheat hydrolysates to Irvine IS CHO-CD media increased the maximum VCD and culture length for most conditions studied compared to the control (
6.3 Oligosaccharide Analysis
Supplementation of Irvine IS CHO-CD media with yeast hydrolysates decreased the percentage of NGA2F+NGA2F−GlcNac glycans by 3-4%, and increased the percentage of NA1F+NA2F glycans by the same percentage compared to control (NGA2F+NGA2F−GlcNac: 73%; NA1F+NA2F: 25%) (
In the study summarized in this example, the effects on glycosylation resulting from the addition of yeast, soy or wheat hydrolysates to CD media GIA-1 in an adalimumab-producing CHO cell line, generically named CHO cell line #2 were evaluated.
7.1 Materials and Methods
Adaptation and production media were supplemented with Bacto TC Yeastolate, BBL Phytone Peptone, or Wheat Peptone E1 according to the experimental design in
Cultures were expanded for 3 passages (3 days each) in their respective adaptation media in a combination of 250 mL (50 mL or 100 mL working volume) and 500 mL (150 mL working volume) Corning vented non-baffled shake flasks and maintained on an orbital shaker at 180 RPM in a 35° C., 5% CO2 dry incubator. Production cultures were initiated in duplicate 500 mL (200 mL working volume) Corning vented non-baffled shake flasks at an initial VCD of approximately 0.5×106 cells/mL. The shake flask study was run in an extended-batch mode by feeding a glucose solution (1.25% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L.
7.2 Culture Growth and Productivity
Supplementation of yeast, soy or wheat hydrolysates to CD media GIA-1 extended the culture length by 1 to 3 days and decreased the maximum VCD in a dose-dependent manner (
7.3 Oligosaccharide Analysis
Addition of yeast hydrolysates decreased the percentage of NGA2F+NGA2F−GlcNac glycans by 3-5%, and increased the percentage of NA1F+NA2F glycans by 5-8% compared to control (NGA2F+NGA2F−GlcNac: 89%; NA1F+NA2F: 3%) (
In the study summarized in this example, the effects on glycosylation resulting from the addition of yeast, soy or wheat hydrolysates to CD media GIA-1 in an adalimumab-producing CHO cell line, generically named CHO cell line #3 were evaluated.
8.1 Materials and Methods
Adaptation and production media were supplemented with Bacto TC Yeastolate, BBL Phytone Peptone, or Wheat Peptone E1 according to the experimental design in
Cultures were expanded for 3 passages (3 days each) in their respective adaptation media in a combination of 250 mL (50 mL or 100 mL working volume) and 500 mL (150 mL working volume) Corning vented non-baffled shake flasks and maintained on an orbital shaker at 140 RPM in a 36° C., 5% CO2 dry incubator. Production cultures were initiated in duplicate 500 mL (200 mL working volume) Corning vented non-baffled shake flasks at an initial VCD of approximately 0.5×106 cells/mL. The shake flask study was run in an extended-batch mode by feeding a glucose solution (1.25% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L.
8.2 Culture Growth and Productivity
Supplementation of production CD media with high concentrations of hydrolysates—11 g/L yeast, 15 g/L soy or 15 g/L wheat hydrolysates, decreased the culture growth rate and increased the culture length compared to the control (
8.3 Oligosaccharide Analysis
Supplementation of CD media GIA-1 with yeast, soy or wheat hydrolysates decreased the percentage of NGA2F+NGA2F−GlcNac glycans and increased the percentage of NA1F+NA2F glycans in a dose-dependent manner (
In the studies summarized in this example, the effects on glycosylation resulting from the addition of yeast, soy or wheat hydrolysates to CD media GIA-1 in a CHO cell line producing mAb #1 were evaluated.
9.1 Materials and Methods
Adaptation and production media were supplemented with Bacto TC Yeastolate (BD Biosciences; catalog #255772), BBL Phytone Peptone (BD Biosciences; catalog #211096), or Wheat Peptone E1 (Organotechnie; catalog #19559) according to the experimental design in
Cultures were expanded for 4 passages (3 days each) in their respective adaptation media in a combination of 250 mL (50 mL or 100 mL working volume) and 500 mL (150 mL working volume) Corning vented non-baffled shake flasks and maintained on an Infors Multitron orbital shaker at 140 RPM in a 36° C., 5% CO2 incubator. Production cultures were initiated in duplicate 500 mL (200 mL working volume) Corning vented non-baffled shake flasks at approximately 1.0×106 cells/mL initial VCD. The study was run in an extended-batch mode by feeding a glucose solution (1.0% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L.
9.2 Culture Growth and Productivity
Supplementation of yeast, soy or wheat hydrolysates to the CD media GIA-1 did not affect culture growth profiles dramatically (
9.3 Oligosaccharide Analysis
Addition of yeast hydrolysates to CD media GIA-1 lowered the percentage of NGA2F+NGA2F−GlcNac glycans by 3%, and increased the percentage of NA1F+NA2F glycans by 4% compared to control (NGA2F+NGA2F−GlcNac: 92%; NA1F+NA2F: 5%) (
In the study summarized in this example, the effects on glycosylation resulting from the addition of yeast, soy or wheat hydrolysates to CD media GIA-1 in a CHO cell line producing mAb #2 were evaluated.
10.1 Materials and Methods
Adaptation and production media were supplemented with Bacto TC, BBL Phytone Peptone, or Wheat Peptone E1 according to the experimental design in
Upon thaw, cells were cultured in CD media GIA-1 growth media in a combination of Corning vented non-baffled shake flasks and maintained on a shaker platform at 140 RPM and 20 L cell bags. Cultures were propagated in a 35° C., 5% CO2 dry incubator. Production cultures were initiated in duplicate 500 mL (200 mL working volume) Corning vented non-baffled shake flasks at an initial VCD of approximately 0.5×106 cells/mL. The shake flask study was run in an extended-batch mode by feeding a glucose solution (1.25% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L. For this study, samples were collected daily and measured for cell density and viability using a NOVA cell counter.
10.2 Culture Growth and Productivity
Supplementation of yeast, soy or wheat hydrolysates to CD media GIA-1 did not impact culture growth for most conditions studied compared to control (
10.3 Oligosaccharide Analysis
Addition of yeast hydrolysates to CD media GIA-1 lowered the percentage of NGA2F+NGA2F−GlcNac glycans by 3% (
In the study summarized in this example, the effects on glycosylation resulting from the individual or combined addition of yeast, soy, and/or wheat hydrolysates to CD media GIA-1 in the adalimumab-producing CHO cell line #1 utilized in Example 1 were evaluated.
11.1 Materials and Methods
Adaptation and production media were supplemented with Bacto TC Yeastolate, BBL Phytone Peptone, and/or Wheat Peptone E1 according to the experimental design in
Cultures were expanded for 3 passages (3 days each) in their respective adaptation media in a combination of 250 mL (50 mL or 100 mL working volume) and 500 mL (150 mL working volume) Corning vented non-baffled shake flasks and maintained on an orbital shaker at 110 RPM in a 35° C., 5% CO2 dry incubator. Production cultures were initiated in duplicate 500 mL (200 mL working volume) Corning vented non-baffled shake flasks at an initial VCD of approximately 0.5×106 cells/mL. The shake flask study was run in an extended-batch mode by feeding a glucose solution (1.25% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L.
11.2 Culture Growth and Productivity
Supplementation of yeast, soy, and/or wheat hydrolysates to CD media GIA-1 resulted in slight growth inhibition and reduced maximum VCD compared to the control (
11.3 Oligosaccharide Analysis
Supplementation of yeast hydrolysates only to CD media GIA-1 decreased the percentage of NGA2F+NGA2F−GlcNac glycans by 4% and increased the percentage of NA1F+NA2F glycans by 6% compared to control (NGA2F+NGA2F−GlcNac: 90%; NA1F+NA2F: 4%) (
The addition of two hydrolysates (yeast and soy; yeast and wheat; soy and wheat) further decreased the percentage of NGA2F+NGA2F−GlcNac glycans and increased the percentage of NA1F+NA2F glycans by a couple of percentages compared to the addition of each component individually (
In the study summarized in this Example, the effects on product quality attributes resulting from the addition of asparagine to CD media GIA-1 in an adalimumab-producing CHO cell line, generically named CHO cell line #1 were investigated.
12.1 Materials and Methods
The CHO cell line #1 was employed in the study covered here. Upon thaw, cells were expanded in a 19-days seed train and then transferred into seed reactors for up to 7 days in growth medium. The cells were then brought to the laboratory and adapted in 500-mL shaker flasks with 200 mL working volume in CD media GIA1 medium for 13 days with 3 passages. The shaker flasks were placed on a shaker platform at 110 RPM in a 35° C., 5% CO2 incubator.
The chemical defined growth or production media, was prepared from basal IVGN CD media GIA1. For preparation of the IVGN CD media formulation, the proprietary media was supplemented with L-glutamine, insulin, sodium bicarbonate, sodium chloride, and methotrexate solution. Production media consisted of all the components in the growth medium, excluding methotrexate. In addition, 5 mM of Galactose (Sigma, G5388) and 10 μM of Manganese (Sigma, M1787) were supplemented into production medium. Osmolality was adjusted by the concentration of sodium chloride. All media was filtered through filter systems (0.22 μm PES) and stored at 4° C. until usage.
Production cultures were initiated in duplicate 500 mL Corning, vented, non-baffled shaker flasks each containing 200 mL culture in dry incubators with 5% CO2 at 35° C. and 110 RPM. Initial VCD was approximately 0.5×106 cells/ml. The shake flask study was run in an extended batch mode by feeding a glucose solution (1.25% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L. Asparagine stock solution (20 g/L) was fed to culture on Day 6 to increase Asparagine concentration by 0, 0.4, 1.2 and 2.0 g/L.
Samples were taken daily from each reactor to monitor growth. The following equipment was used to analyze the samples: Cedex cell counter for cell density and viability; YSI 7100 analyzer for glucose and lactate concentration.
Some of the daily samples and the harvest samples were centrifuged at 3,000 rpm for 30 min and then supernatants were stored at −80° C. The thawed harvest samples were subsequently filtered through a 0.2 μm filter, purified by Protein A chromatography, and then oligosaccharide analysis was performed as described in Example 1.
12.2 Culture Growth and Productivity
Feeding of asparagine to CD media GIA-1 did not impact culture growth for most conditions studied as compared to the control (
12.3 Oligosaccharide Analysis
The effect of asparagine addition on oligosaccharide distribution was consistent with the experiments performed in hydrolysate based media described above. The addition of asparagine increased NGA2F+NGA2F−GlcNAc glycans in a dose dependent manner (
The percentage of NA1F+NA2F in the control sample (without asparagine addition) was as high as 22.3% (
In the study summarized in Example 13, the effects on product quality attributes resulting from the addition of asparagine to CD media GIA-1 in an adalimumab-producing CHO cell line, generically named CHO cell line #3 were investigated.
13.1 Materials and Methods
The CHO cell line #3 was employed in the study covered here. Upon thaw, adalimumab producing cell line #3 was cultured in CD media GIA-1 in a combination of vented shake flasks on a shaker platform @ 140 rpm and 20 L wave bags. Cultures were propagated in a 36° C., 5% CO2 incubator to obtain the required number of cells to be able to initiate production stage cultures.
The chemical defined growth or production media was prepared from basal IVGN CD media GIAL For preparation of the IVGN CD media formulation, the proprietary media was supplemented with L-glutamine, sodium bicarbonate, sodium chloride, and methotrexate solution. Production media consisted of all the components in the growth medium, excluding methotrexate. In addition, 10 mM of Galactose (Sigma, G5388) and 0.2 μM of Manganese (Sigma, M1787) were supplemented into production medium. Osmolality was adjusted by the concentration of sodium chloride. All media was filtered through filter systems (0.22 μm PES) and stored at 4° C. until usage.
Production cultures were initiated in duplicate 500 mL Corning, vented, non-baffled shaker flasks each containing 200 mL culture in dry incubators with 5% CO2 at 36° C. and 140 RPM. Initial VCD was approximately 0.5×106 cells/ml. The shake flask study was run in an extended batch mode by feeding a glucose solution (1.25% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L. Asparagine stock solution (20 g/L) was fed to culture on Day 6 to increase asparagine concentration by 0, 0.4, 0.8, 1.2, 1.6, and 2.0 g/L.
Samples were taken daily from each reactor to monitor growth. The following equipment was used to analyze the samples: Cedex cell counter for cell density and viability; YSI 7100 analyzer for glucose and lactate concentration.
Some of the daily samples and the harvest samples were centrifuged at 3,000 rpm for 30 min and then supernatants were stored at −80° C. The thawed harvest samples were subsequently filtered through a 0.2 μm filter, purified by Protein A chromatography, and then oligosaccharide analysis was performed as described in Example 1.
13.2 Culture Growth and Productivity
The experiment described in the instant Example used a different cell line (i.e., CHO cell line #3) in CD media GIA-1. Culture growth and viability profiles were comparable among all test conditions with different dosage of asparagine added on day 6 (
13.3 Oligosaccharide Analysis
Again, the addition of asparagine increased NGA2F+NGA2F−GlcNac (
In the studies summarized in Example 14, the effects on product quality attributes resulting from the addition of asparagine to CD media GIA-1 from Life Technologies Gibco in a CHO cell line producing monoclonal antibody #2 were investigated. In this instant Example, asparagine was either supplemented into culture media during media preparation or added on day 5 of the cell culture process.
14.1 Materials and Methods
mAb #2 producing cell line was employed in the study covered here. Upon thaw, cells were cultured in chemically defined growth media in a combination of vented baffled shake flasks (Corning) on a shaker platform at 140 RPM. All media pH was adjusted to approximately 7.2 and the media osmolality was adjusted to 280-330 mOsmol/kg.
Cultures were propagated in a 35° C., 5% CO2 incubator to obtain the required number of cells to be able to initiate production stage cultures. Production cultures were initiated in duplicate 500 mL vented non-baffled Corning shake flasks (200 mL working volume) at an initial viable cell density (VCD) of approximately 0.5×106 cells/mL. The shake flask study was run in an extended batch mode by feeding a glucose solution (1.25% (v/v) of 40% solution) when the media glucose concentration fell below 3 g/L. Asparagine (Sigma, Catalog Number A4284) were solubilized in Milli-Q water to make a 30 g/L stock solution. All media was filtered through Corning or Millipore 1 L filter systems (0.22 μm PES) and stored at 4° C. until usage.
For asparagine supplemented into culture media during media preparation, asparagine stock solution was supplemented to production media to increase asparagine concentration by 0, 0.4, 0.8 and 1.6 g/L. After addition of asparagine, media was brought to a pH similar to non-supplemented (control) media using 5N hydrochloric acid/5N NaOH, and it was brought to an osmolality similar to non-supplemented (control) media by adjusting the concentration of sodium chloride. For asparagine addition study, asparagine stock solution was added to culture on Day 5 to increase Asparagine concentration by 0, 0.4, 0.8 and 1.6 g/L.
For all studies described throughout this invention, samples were collected daily and measured for cell density and viability using a NOVA cell counter. Retention samples for titer analysis via Poros A method were collected by centrifugation at 12,000 RPM for 5 min when the culture viability began declining. The cultures were harvested by collecting 125 mL aliquots and centrifuging at 3,000 RPM for 30 min when culture viability was near or below 50%. All supernatants were stored at −80° C. until analysis. The harvest samples were Protein A purified and then oligosaccharide analysis was performed as described in Example 1.
14.2 Culture Growth and Productivity
Adding asparagine to CD media GIA-1 during medium preparation or on day 5 of the cell culture did not impact culture growth for most conditions studied as compared to the non-supplemented 0 g/L controls (
14.3 Oligosaccharide Analysis
The addition of asparagine during medium preparation increased NGA2F+NGA2F−GlcNac glycans in a dose dependent manner (
The addition of asparagine on day 5 of the culture also increased NGA2F+NGA2F−GlcNac glycans in a dose dependent manner (
The present invention is not to be limited in scope by the specific embodiments described herein. Indeed, various modifications of the invention in addition to those described herein will become apparent to those skilled in the art from the foregoing description and the accompanying figures. Such modifications are intended to fall within the scope of the appended claims. Furthermore, the strategies described herein can be easily implemented either in-process or ad hoc to control the oligosaccharide distribution, thus reducing the potential impact of raw material changes. For example, Adalimumab production strategies can use these techniques to achieve maximized cell growth and specific productivity without compromising product quality.
Patents, patent applications, publications, product descriptions, GenBank Accession Numbers, and protocols that may be cited throughout this application, the disclosures of which are incorporated herein by reference in their entireties for all purposes. For example, but not by way of limitation, patent applications designated by the following attorney docket numbers are incorporated herein by reference in their entireties for all purposes: 082254.0104; 082254.0235; 082254.0236; 082254.0238; and 082254.0242.
Claims
1. A process for producing a recombinantly-expressed immunoglobulin, comprising culturing a mammalian cell which recombinantly expresses the immunoglobulin during a production stage in a cell culture media comprising asparagine, thereby producing the recombinantly-expressed immunoglobulin,
- wherein the level of agalactosyl fucosylated biantennary oligosaccharides (sum of NGA2F and NGA2F−GlcNac) present on the produced immunoglobulin is increased as compared to the level of agalactosyl fucosylated biantennary oligosaccharides (sum of NGA2F and NGA2F−GlcNac) of immunoglobulin produced in cell culture media which does not comprise said asparagine during the production stage; and/or wherein the level of galactose containing fucosylated biantennary oligossacharides (sum of NA1F and NA2F) present on the produced immunoglobulin is decreased as compared to the level of galactose containing fucosylated biantennary oligossacharides (sum of NA1F and NA2F) of immunoglobulin produced in cell culture media which does not comprise said asparagine during the production stage.
2. The process of claim 1, wherein the immunoglobulin is an anti-TNFα antibody.
3. The process of claim 1, wherein the cell which expresses the immunoglobulin is a CHO cell.
4. The process of claim 3, wherein the immunoglobulin is adalimumab.
5. The process of claim 4, wherein the cell culture media comprises asparagine at a concentration of between 0.4 g/L to 2.0 g/L during the production stage.
6. The process of claim 4, wherein the cell culture media comprises asparagine at a concentration of at least 0.4 g/L, at least 0.8 g/L, at least 1.2 g/L, at least 1.6 g/L or at least 2.0 g/L.
7. The process of claim 4, wherein the cell culture media further comprises glutamine.
8. The process of claim 7, wherein the cell culture media comprises glutamine at a concentration of at least 0.4 g/L.
9. The process of claim 4, wherein the level of agalactosyl fucosylated biantennary oligosaccharides (sum of NGA2F and NGA2F−GlcNAc) present on the produced immunoglobulin is 64%-88%, 70%-88% or 75%-85%; and/or wherein the level of fucosylated biantennary oligosaccharides (sum of NA1F and NA2F) present on the produced immunoglobulin is 1%-30%, 2%-25%, 5%-20%, 5%-15%, 10%-20% or 27%-31%.
10. The process of claim 4, wherein the process is a fed batch process.
11. The process of claim 4, wherein the cell culture media further comprises a yeast hydrolysate and/or a plant hydrolysate; optionally, wherein the yeast hydrolysate is selected from the group consisting of Bacto TC Yeastolate, HyPep Yeast Extract and UF Yeast Hydrolysate; and/or wherein the plant hydrolysate is selected from the group consisting of a soy hydrolysate, a wheat hydrolysate, a rice hydrolysate, a cotton seed hydrolysate, a pea hydrolysate, a corn hydrolysate, a potato hydrolysate, BBL Phytone Peptone, HyPep 1510, SE50 MAF-UF, UF Soy Hydrolysate, Wheat Peptone E1, HyPep 4601 and Proyield WGE80M Wheat.
12. The process of claim 11, wherein the yeast hydrolysate is present in the cell culture media at a concentration of between 2 g/L to 11 g/L and/or wherein the plant hydrolysate is present in the cell culture media at a concentration of between 2 g/L to 15 g/L.
13. The process of claim 4, wherein the cell culture media is a chemically defined cell culture media.
14. The process of claim 4, wherein the production stage initiates at an initial viable cell density of approximately 0.5×106 cells/mL.
15. The process of claim 1, further comprising collecting and isolating the recombinantly-expressed immunoglobulin.
16. The process of claim 4, wherein the asparagine is present at a concentration of less than or equal to 26 mM.
17. A process for producing a recombinantly-expressed immunoglobulin, comprising culturing a mammalian cell which recombinantly expresses the immunoglobulin in a cell culture media comprising at least 0.8 g/L of asparagine, thereby producing the recombinantly-expressed immunoglobulin,
- wherein the level of agalactosyl fucosylated biantennary oligosaccharides (sum of NGA2F and NGA2F−GlcNac) present on the produced immunoglobulin is increased as compared to the level of agalactosyl fucosylated biantennary oligosaccharides (sum of NGA2F and NGA2F−GlcNac) of immunoglobulin produced in cell culture media which does not comprise said asparagine; and/or wherein the level of galactose containing fucosylated biantennary oligossacharides (sum of NA1F and NA2F) present on the produced immunoglobulin is decreased as compared to the level of galactose containing fucosylated biantennary oligossacharides (sum of NA1F and NA2F) of immunoglobulin produced in cell culture media which does not comprise said asparagine.
18. The process of claim 17, wherein the immunoglobulin is an anti-TNFα antibody.
19. The process of claim 17, wherein the cell which expresses the immunoglobulin is a CHO cell.
20. The process of claim 19, wherein the immunoglobulin is adalimumab.
21. The process of claim 20, wherein the cell culture media comprises asparagine at a concentration of at least 1.2 g/L, at least 1.6 g/L or at least 2.0 g/L.
22. The process of claim 20, wherein the cell culture media comprises asparagine at a concentration of between 0.8 g/L to 2.0 g/L.
23. The process of claim 20, wherein the cell culture media further comprises glutamine.
24. The process of claim 23, wherein the cell culture media comprises glutamine at a concentration of at least 0.4 g/L.
25. The process of claim 20, wherein the level of agalactosyl fucosylated biantennary oligosaccharides (sum of NGA2F and NGA2F−GlcNAc) present on the produced immunoglobulin is 64%-88%, 70%-88% or 75%-85%; and/or wherein the level of fucosylated biantennary oligosaccharides (sum of NA1F and NA2F) present on the produced immunoglobulin is 1%-30%, 2%-25%, 5%-20%, 5%-15%, 10%-20% or 27%-31%.
26. The process of claim 20, wherein the process is a fed batch process.
27. The process of claim 20, wherein the culture media further comprises a yeast hydrolysate and/or a plant hydrolysate; optionally, wherein the yeast hydrolysate is selected from the group consisting of Bacto TC Yeastolate, HyPep Yeast Extract and UF Yeast Hydrolysate; and/or wherein the plant hydrolysate is selected from the group consisting of a soy hydrolysate, a wheat hydrolysate, a rice hydrolysate, a cotton seed hydrolysate, a pea hydrolysate, a corn hydrolysate, a potato hydrolysate, BBL Phytone Peptone, HyPep 1510, SE50 MAF-UF, UF Soy Hydrolysate, Wheat Peptone E1, HyPep 4601 and Proyield WGE80M Wheat.
28. The process of claim 27, wherein the yeast hydrolysate is present in the cell culture media at a concentration of between 2 g/L to 11 g/L and/or wherein the plant hydrolysate is present in the cell culture media at a concentration of between 2 g/L to 15 g/L.
29. The process of claim 20, wherein the cell culture media is a chemically defined cell culture media.
30. The process of claim 17, further comprising collecting and isolating the recombinantly-expressed immunoglobulin.
Type: Application
Filed: Dec 3, 2015
Publication Date: May 19, 2016
Inventors: Lisa M. Rives (Natick, MA), Cornelia Bengea (Auburn, MA), Xiaobei Zeng (Carolina, PR)
Application Number: 14/958,211
