WO2011095596A1

WO2011095596A1 - Fed-batch process using concentrated cell culture medium for the efficient production of biologics in eb66 cells

Info

Publication number: WO2011095596A1
Application number: PCT/EP2011/051668
Authority: WO
Inventors: Arnaud LÉON; Patrick Champion-Arnaud; Nicola Beltraminelli; Sylvana Bouletreau
Original assignee: Vivalis
Priority date: 2010-02-04
Filing date: 2011-02-04
Publication date: 2011-08-11
Also published as: EP2531592A1; US20120309056A1

Abstract

The present invention relates to a glucose fed-batch process using concentrated cell culture for the efficient production of biologics, such as viral vaccines and recombinant proteins. In particular, the invention relates to culturing duck embryonic derived stem cells EB66 to obtain high yield of biological products from such cells.

Description

Fed-batch process using concentrated cell culture medium for the efficient production of biologies in EB66 cells

The present invention relates to biotechnology sciences, more specifically to areas of cell culture for the production of biologies, such as viral vaccines and recombinant proteins. In particular, the invention relates to culturing animal cells, more specifically duck embryonic derived stem cells, to obtain high levels of biological products from such cells.

The past twenty years witnessed the transformation of animal cell culture from exploratory biological products production methods to mature manufacturing processes. This is essentially true for the industrial manufacturing of recombinant proteins such as monoclonal antibodies, where cell lines like CHO (Chinese Hamster Ovary) and NSO are now widely used for the mass production of monoclonal antibodies. On the vaccine side, the actual trend is to switch from the old egg-based production process to cell-culture platforms for the production of viral vaccines. Animal cell lines constitute a highly promising alternative to the eggs and chicken embryo fibroblasts (CEFs) production systems because it overcomes viral vaccines production bottlenecks and time constrains (e.g risks of eggs shortage due to avian flu; egg shipment plan) and has additional advantages in connection with the safety of the vaccine (no antibiotic additives present in the vaccine formulation; no toxic preservatives (such as thiomersal) needed; reduced endotoxin levels, no egg allergy issue; no risk of adventitious agent/BSE by cell culture in protein and serum free media; higher purity of virus vaccine preparation). Examples of cell lines for the production of viral vaccines are MDCK (cells derived from the kidney of Madin-Darby dog), PerC6 (cells derived from human embryonic retinal cells genetically modified by inserting the El genes from the human adenovirus type 5) developed by Crucell (Netherland)), VERO (cells derived from epithelial cells of kidney from African green monkey (Cercopithecus aethiops) isolate at the Chiba University in Chiba, Japan), BHK21 (Cells immortalized from baby hamster kidney cells) and duck cell lines (transgenic or not), preferably duck embryonic stem cells, such as EB66 developed by Vivalis (France).

Because of biological products complexity, the costs of production are very high and there is a constant pressure on driving production cost of biological products down. A direct mean to reduce production cost is to improve biologies production yield. The production of virus or recombinant proteins in animal cell culture is dependent upon a variety of factors. For example, the production of virus by mammalian or avian cell culture can be improved using a variety of techniques, such as media optimization, synchronization of the producer cells, increasing infectivity of producer cells, virus adaptation to producer cells etc... However, it remains that the basic parameters that will ultimately impact the cell line productivity are the specific productivity of said cell line, the peak viable cell concentration that is attainable with said cell line and the length of the production process.

If one can achieve, a high concentration of viable producer cells, with a maximal specific productivity, for long period of time, in a given volume, then the overall efficiency of the process would be improved to make the process economical. This is the goal of the present invention to provide a process for culturing high concentration of animal cells for preparing high-titer viral suspension and/or recombinant proteins in cell cultures.

The inventors have now find that duck cell lines, and more specifically duck EB66 cell line, have the remarkable characteristic to grow in animal serum free cell culture medium containing high concentration of sugar source (i.e glucose) up to very high cell density (> 60 millions cells/ml) in fed-batch culture, without or with a low accumulation of toxic compounds in the culture (such as lactate and ammonium), allowing to improve the overall efficiency of the process of biological products production.

The present invention relates to a process for the fed-batch culture of animal cells comprising the steps of:

a) growing the cells, preferably in exponential phase, in a cell growth medium, optionally supplemented with defined supplements, in a culture volume corresponding to a maximum of 75%, preferably to about 50% or less, of the maximum vessel volume, to a cell density greater or equal to 4 million cells/ml, more preferably to a cell density greater or equal to 6, 8, 10, 12, 15, 20, 25, 30, 35, or even 40 million cells/ml;

and wherein said process comprises the steps of:

b) performing a fed-batch culture by feeding the culture with a concentrated cell culture medium and/or at least one source of carbohydrate, preferably a sugar and/or glutamine, until the culture volume reaches the maximum vessel volume; and then

c) optionally, adding for the remaining days of animal cell culture in said vessel, marginal volume of at least one compound selected among one source of carbohydrate (preferably a sugar as an energy source) and a solution of one or more amino-acids, preferably glutamine.

According to a preferred embodiment, said fed-batch culture process comprises the steps of:

a) growing the cells, preferably in exponential phase, in a cell growth medium, optionally supplemented with defined supplements, in a culture volume corresponding to about 50% or less of the maximum vessel volume, to a cell density greater or equal to 10 million cells/ml, preferably 12 million cells/ml, more preferably 15 million cells/ml, or even more preferably to a cell density greater or equal to 20 million cells/ml;

and wherein said process comprises the steps of:

b) performing a fed-batch culture by feeding the culture with a concentrated cell culture medium, optionally supplemented with other ingredients, such as for example D-glucose and glutamine, until the culture volume reaches the maximum vessel volume; and then

c) optionally, adding for the remaining days of animal cell culture in said vessel, marginal volume of a sugar, such as D-glucose and/or amino acids, such as glutamine.

According to a preferred embodiment, the cell density at the end of step b) is greater or equal to 10 million cells/ml, preferably 12 million cells/ml, preferably 15 million cells/ml, more preferably 20 million cells/ml, or even more preferably greater or equal to 25 million cells/ml.

In the process of the invention, step a) is a batch cell culture, steps b) and c) is a fed- batch cell culture. In a second embodiment, the process of the invention, steps a), b) and c) are a fed-batch cell culture. As used herein, the term "batch" describes a batch cell culture which is carried out by placing the cells to be cultured in a fixed volume of culture medium and allowing the cells to grow. Cell numbers increase, usually exponentially, until a maximum is reached, after which growth become arrested and the cells die. This may be due either to exhaustion of a nutrient or accumulation of an inhibitor of growth. Thus, batch culture is characterised in that it proceeds in a fixed volume since nothing is added after placing the cells in the cell growth medium, optionally supplemented with defined supplements. As used herein, the term "fed-batch" describes a batch cell culture (i.e cells are cultured in a medium in a fixed volume) to which substrate, in either solid or concentrated liquid form, is added either periodically or continuously during the run. The volume of the feed might be minimal compared to the volume of the culture. When the feeding is discontinuous, the feeding may occur one time per day, more than one time per day, or less than one time per day. According to a particular embodiment, the glucose and glutamine fed-batch is continuous and the fed-batch of concentrated cell culture medium is discontinuous. According to another particular embodiment, the glucose, the glutamine and the concentrated culture medium fed-batch are discontinuous, preferably once per day. According to a preferred embodiment, the glucose and glutamine fed-batch as well as the fed-batch of concentrated cell culture medium is continuous. Just as in a batch culture, a fed-batch culture is initiated by inoculating cells to the medium, but, in contrast to a batch culture, there is a subsequent inflow of nutrients, such as by way of a concentrated nutrient feed. In contrast to a continuous culture there is no systematic removal of culture fluid or cells from a fed-batch culture. Batch and fed-batch culture are characterized in that it proceeds in a substantially fixed volume, for a fixed duration, and with a single harvest either when the cells have died or at an earlier, predetermined point.

Cell growth medium

By "cell growth medium", "cell culture medium" or "culture media" or "media formulation" it is meant a nutritive solution for culturing or growing cells. The ingredients that compose such media may vary depending on the type of cell to be cultured. In addition to nutrient composition, osmolarity and pH are considered important parameters of culture media.

The cell growth medium comprises a number of ingredients well known by the man skilled in the art, including amino acids, vitamins, organic and inorganic salts, sources of carbohydrate, lipids, trace elements (CuS04, FeS04, Fe(N03)3, ZnS04...), each ingredient being present in an amount which supports the cultivation of a cell in vitro (i.e survival and growth of cells). Ingredients may also include different auxiliary substances, such as buffer substances (like sodium bicarbonate, Hepes, Tris...), oxidation stabilizers, stabilizers to counteract mechanical stress, protease inhibitors, animal growth factors, plant hydrolyzates, anti-clumping agents, anti-foaming agents. If required, a non-ionic surfactant, such as polypropylene glycol can be added to the cell growth medium as an anti-foaming agent. These agents are generally used to protect cells from the negative effects of aeration since, without an addition of a surfactant, the ascending and bursting air bubbles can lead to damage of those cells that are located on the surface of these air bubbles ("sparging"). Characteristics and compositions of the cell growth media vary depending on the particular cellular requirements. Important parameters include osmolality, pH, and nutrient formulations. The cell growth medium is preferably an animal serum-free medium" (SFM), which meant that the cell growth medium is ready to use, that is to say that it does not required serum addition allowing cells survival and cell growth. The cell growth medium is preferably chemically defined, but it may also contained hydrolyzates of various origin, from plant for instance. Preferably, said cell growth medium is "non animal origin" qualified, that is to say that it does not contain components of animal or human origin (FAO status: "free of animal origin"). In SFM, the native serum proteins are replaced by recombinant proteins. Alternatively SFM medium according to the invention does not contain protein (PF medium: "protein free medium") and/or are chemically defined (CDM medium: "chemically defined medium"). SFM media present several advantages: (i) the first of all being the regulatory compliance of such media (indeed there is no risk of contamination by adventitious agents such as BSE, viruses); (ii) the optimization of the purification process; (iii) the better reproducibility in the process because of the better defined medium. Example of commercially available cell growth media are: VP SFM (InVitrogen Ref 11681-020, catalogue 2003), Opti Pro (InVitrogen Ref 12309-019, catalogue 2003), Episerf (InVitrogen Ref 10732-022, catalogue 2003), Pro 293 S-CDM (Cambrex ref 12765Q, catalogue 2003), LC17 (Cambrex Ref BESP302Q), Pro CHO 5- CDM (Cambrex ref 12-766Q, catalogue 2003), HyQ SFM4CHO (Hyclone Ref SH30515- 02), HyQ SFM4CHO-Utility (Hyclone Ref SH30516.02), HyQ PF293 (Hyclone ref SH30356.02), HyQ PF Vero (Hyclone Ref SH30352.02), CDM4PERMAb (Hyclone Ref. SH30871), Ex cell 293 medium (SAFC Biosciences ref 14570-1000M), Ex cell 325 PF CHO Protein free medium (SAFC Biosciences ref 14335-1000M), Ex cell VPRO medium (SAFC Biosciences ref 14560-1000M), Excell EBx Gro-I medium (SAFC Biosciences - ref.14530c). Supplements to the cell growth medium

The cell growth medium may be supplemented with defined supplements such as antibiotic to prevent bacterial contamination. Example of antibiotics include gentamycin, penicillin and streptomycin, Gentamycin is usually used at a final concentration of 10 ng/ml, penicillin at a final concentration of 100 U/ml and streptomycin at a final concentration of 100 μg/ml. The cell growth medium may also be supplemented with defined supplements such as glutamine. Glutamine being unstable in culture medium it is often necessary to supplement the cell growth medium to adjust the glutamine concentration in the medium. In a preferred embodiment, the culture medium used in step a) of the invention is supplemented with glutamine. Preferably glutamine concentration is around 0.5 mM to around 5 mM, preferably between around 1 mM to around 3 mM, and most preferably around 2.5 mM or 3 mM . Alternatively, the cell growth medium may be supplemented during the exponential phase with highly concentrated solutions of ingredients, some of them being marketed as "CHO-Feed" (SAFC cat. N°C1615), and/or CDHF (SAFC cat. N° 14700c). According to a preferred embodiment, the cell growth medium is supplemented one time with defined supplements. According to another embodiment, the cell growth medium is supplemented periodically with defined supplements.

Fed-batch supplementation of the cell growth medium

By concentrated cell culture medium it is meant a formulation of a cell culture medium used to grow cells, and obtained by increasing the concentration of (almost) each component of the cell culture medium. According to a preferred embodiment, the concentrated cell culture medium formulation is obtained by increasing the concentration of each component of the medium except the components which are involved in, or act on, the osmotic pressure and/or osmolarity and/or osmolality, such as salts and buffering agents. A man skilled in the art is able to define such components.

A "IX formulation" is meant to refer to any aqueous solution that contains some or all ingredients found in a cell culture media. The "IX formulation" can refer to, for example, the cell culture media or to any subgroup of ingredients for that media. The concentration of an ingredient in a IX solution is about the same as the concentration of that ingredient found in the cell culture formulation used for maintaining or growing cells. Cell culture media used to grow cells is a IX formulation by definition. When a number of ingredients are present (as in a subgroup of compatible ingredients), each ingredient in a IX formulation has a concentration about equal to the concentration of those ingredients in a cell culture media. For example, RPMI 1640 culture media contains, among other ingredients, 0.2 g/1 L-arginine, 0.05 g/1 L-asparagine, and 0.02 g/1 L-aspartic acid. A "IX formulation" of these amino acids, which are compatible ingredients, contains about the same concentrations of these ingredients in solution. Thus, when referring to a "IX formulation," it is intended that each ingredient in solution has the same or about the same concentration as that found in the cell culture media being described. The concentrations of media ingredients in a IX formulation are well known to those of ordinary skill in the art, See Methods For Preparation of Media, Supplements and Substrate For Serum-Free Animal Cell Culture Alan R. Liss, New York (1984). The osmolarity and/or pH, however, may differ in a IX formulation compared to the culture media, particularly when fewer ingredients are contained by the IX formulation.

A "10X formulation" refers to a solution wherein each ingredient in that solution is about 10 times more concentrated than the same ingredient in the cell culture media. As a way of example RPMI 1640 media, contains, among other things, 0.3 g/1 L-glutamine. By definition, a "10X formulation" contains about 3.0 g/1 glutamine. A "10X formulation" may contain a number of additional ingredients at a concentration about 10 times that found in the IX culture media.

As will be apparent, 1.5X, 2X, 3X, 4X, 5X, 6X, ...10X, ..25X formulation etc... designate solutions that contain ingredients at about 1.5, 2, 3, 4, 5, 6, 10 or 25 fold concentrations, respectively, as compared to a 1 x cell culture media. Again, the osmolarity and pH of the media formulation and concentrated formulation may vary. The solubility of some components in cell culture medium constitutes a limitation to the obtaining of highly concentrated cell culture medium.

In a fed-batch culture, the concentrated cell culture medium is typically rather concentrated to minimize the increase in culture volume while supplying sufficient nutrients for continued cell growth. More preferably, concentrated cell culture medium of the invention is 3X, 3.5X, 4X, 4.5X, 5X, 5.5X, or 6X.

The concentrated cell culture medium used for the fed-batch culture may be in a concentrated cell growth medium as defined above, or may comprise at least one ingredients of the cell growth medium. According to a first embodiment the concentrated cell culture medium is a concentrated formulation of the cell growth medium except that the concentration of components which are involved in, or act on, the osmotic pressure and/or osmolarity and/or osmolality (such as salts and buffering agents) remain at IX concentration. Osmolarity is an important process variable during the cultivation of mammalian cells in vitro. In a particular embodiment, a IX concentration refers to a osmolarity in the range of 260 and 320 milliosmoles (mOsm), basically to mimic the osmolarity of serum at 290 mOsm/kg. Preferably, the concentrated cell culture medium used as a feed is a concentrated formulation of a cell culture medium which is different from the cell growth medium used in step a). According to another embodiment, at least one ingredient might be added to the concentrated cell culture medium used as feed in the fed-batch culture. Ingredients are selected from the group consisting of amino-acids, lipids, carbohydrates, protein hydrolyzates of non-animal origin, surfactant, salts, trace elements and a mixture thereof.

When the ingredient is amino acids, the choice of amino-acid(s) to add to the cell culture may be determined be an analysis of amino-acids consumption by the cells in the culture. In the present invention, by amino acid is intended all naturally occurring alpha amino acids in both their D and L stereoisomer^ forms, and their derivatives. A derivative is defined as an amino acid that has another molecule or atom attached to it. Generally the amino acids are present in the cell growth medium at the start of the culture, but some amino acids may be depleted faster that others depending of cell growth medium; it is therefore required to feed with some amino acids. The non exhaustive list of amino acids (including salts and precursors) that may be added to the culture medium are: glutamine, asparagine, cystine, tyrosine, tryptophan, lysine, histidine, arginine, glycine, valine, methionine, threonine, serine, isoleucine, leucine and phenylalanine. According to a preferred embodiment, the amino-acids added to the medium are selected from the group consisting of asparagine and glutamine, or a mixture thereof. In a more preferred embodiment, glutamine is added, and the feeding of glutamine is performed during step b) and c) to maintain the glutamine concentration in the medium between around 0.5 mM to around 5 mM, preferably between around 1 mM to around 3 mM, and most preferably around 2.5 mM or 3 mM. In a preferred embodiment, the amino acid feeding, preferably of glutamine, occurs on a continuous basis. In another preferred embodiment, the amino acid feeding on a daily basis. In a particular embodiment, amino acid feeding occurs in step b) and c) of the fed-batch process of the invention. In another particular embodiment amino acid feeding occurs only in step c) of the fed-batch process of the invention.

In order to improve cell growth, but also viral or recombinant proteins production, additional ingredients are preferably added to the cell growth medium as a feed (i.e fed- batch process). According to a preferred embodiment, the carbohydrates are added to the medium as a feed. The carbohydrates are selected from the group consisting of D-glucose, D-sucrose and D-galactose or a mixture thereof. According to a more preferred embodiment, the carbohydrate added is D-glucose.

The feeding of D-glucose is performed in step b) and/or c) of the fed-batch process of the invention, preferably during steps b) and c) to maintain the D-glucose concentration in the medium between about 0.5g/l to about 25g/l of D-glucose, preferably between about 5 g/1 to about 22 g/1 of D-glucose, more preferably between about 8 g/1 to about 20 g/1 of D- glucose and even more preferably between about 10 g/1 to about 15 g/1 of D-glucose, in particular, about 11,12, 13,14 or 15 g/1. In another embodiment, the concentration of D- glucose in the culture medium is to be maintained by fed-batch at a concentration preferably equal to or above 5 g/1 of D-glucose, more preferably equal to or above 8 g/1 of D-glucose, and even most preferably equal to or above 10 g/1. In a preferred embodiment, the feeding of D-glucose occurs on a continuous basis. In another preferred embodiment, the feeding of D-glucose occurs on a daily basis. Mammalian cell culture metabolism is characterized by glucoglutamino lysis, that is, high glucose and glutamine uptake combined with a high rate of lactate and nonessential amino acid secretion. Stress associated with acid neutralization and ammonia accumulation necessitates complex feeding schemes and limits cell densities achieved in fed-batch culture (Quek LE et al., Metab Eng. 2010 12(2): 161 -71)

As shown in Figure 11 , the metabolic profile of an avian cell line, namely the duck cell line EB66, presents very low accumulation of inhibitory metabolites with high D- glucose concentrations of 10 g/1. The results obtained in Example 5 show that the increase of the glucose concentration from 6 g/1 to 10 g/1 allows the obtaining of higher IgGl productivity rates as well as higher cell density values. Thus, the surprising metabolic features of the duck EB66 cell line, makes the inventors to envisage according to a preferred embodiment of the invention to maintain the glucose concentration in the cell growth medium by fed-batch at a final concentration of at least 5 g/1 of D-glucose, preferably of at least 8 g/1, and more preferably of around 10 g/1 of D-glucose, but also higher D-glucose concentrations such as about 12 g/1, 14 g/1, 18 g/1, 20 g/1, 22 g/1 or 25 g/1; the upper limit being the saturation of the culture medium.

In a particular embodiment, glucose feeding occurs in step b) and c) of the fed- batch process of the invention. In another particular embodiment, glucose feeding occurs only in step c) of the fed-batch process of the invention.

In a most preferred embodiment, the fed-batch process of the invention comprises the feeding of the culture with a concentrated cell culture medium supplemented with glutamine until the culture volume reaches the maximum vessel volume and then, the addition of marginal volume of D-glucose and glutamine to maintain the concentration of said nutrients to predetermined values. Preferred glucose and glutamine concentration values are those above described.

In a particular embodiment, fed-batch supplementation of the cell growth medium with a concentrated cell culture medium according to step b) is carried out daily, preferably from day 2 or day 3 post cell feeding. Preferably, the volume of feeds is 1/4, 1/6, 1/8, 1/10 or 1/12 of the maximum vessel volume. More preferably the feed volume is 1/8 of the maximum vessel volume.

According to the fed-batch process of the invention, the maximum vessel volume is reached at day 4 to day 12 of post vessel seeding, preferably at day 5, 6, 7, 8, 9, 10, 11, or 12 post- vessel seeding. According to a preferred embodiment, the fed-batch process of the invention, the maximum vessel volume is reached at day 6 post- vessel seeding.

In a preferred embodiment, initial culture volume is about 50% of the maximum vessel volume and addition of feeds of 1/8 of the maximum vessel volume takes place daily during 4 consecutive days. More preferably, initial date of seeding is day 2 or day 3, and the maximum vessel volume is reached at day 5 or day 6, respectively.

According to a preferred embodiment, the process of the invention lasts less than 15 days, more preferably 12 days post- vessel seeding. According to a preferred embodiment, step a) of the process lasts 2 to 5 days, more preferably 3 or 4 days, and even more preferably 3 days.

By "maximum vessel volume", it is meant the optimum fill volume, also referred as working volume, recommended by the manufacturer. The maximum vessel volume is generally, 25% to 80%> of the nominal flask volume. When the vessel is an Erlenmeyer, the maximum vessel volume is preferably around 40%> of the nominal flask volume. Accordingly, in a preferred embodiment the maximum vessel volume of a 250mL Erlenmeyer is 100 mL. When the vessel is a bioreactor, the maximum level is generally linked to the height of the reactor which is reached by the water jacket. Thus, the maxim vessel volume is preferably around 50, 60, 70 or 80% of the nominal flask volume, more preferably around 80% of its nominal volume. Accordingly, in a preferred embodiment, the maximum vessel volume of a so called "2L bioreactor" having a nominal volume of 3L is 2.4 L.

By "marginal volume", it is meant that the volume of compound added to the vessel is negligible compared to the maximum volume of the vessel which is recommended by the manufacturer (less than 1 % of the maximum volume, preferably less than 0.5 % of the maximum volume, such as between about 0.05 % and 0.5 % of the maximum volume). For example, if the maximum volume of the vessel is 2L, adding 1 to 10ml of compounds into the vessel, will be considered as a marginal volume increase.

By growing the cells in exponential phase, also called the log phase, it is meant a period characterized by cell doubling. In this phase, the number of new cells appearing per unit time is proportional to the present population. If growth is not limited, doubling will continue at a constant rate so both the number of cells and the rate of population increase doubles with each consecutive time period. In this phase, the period of growth up to the point at which maximum viable cell population density is reached. For this type of exponential growth, plotting the natural logarithm of cell number against time produces a straight line. The slope of this line is the specific growth rate of the organism, which is a measure of the number of divisions per cell per unit time. The actual rate of this growth (i.e. the slope of the line) depends upon the growth conditions, which affect the frequency of cell division events and the probability of both daughter cells surviving. Exponential growth cannot continue indefinitely, however, because the medium is soon depleted of nutrients and enriched with wastes. By "vessel" it is meant, glass, plastic or metal containers of various sizes that can provide an aseptic environment for growing cells, are termed "culture vessels". The cultivation vessel of the invention is more preferably selected among stirred tank bioreactor, disposable bioreactor (such as Wave™ Bioreactor, Bello™ bioreactor, Nucleo™ bioreactor etc .), spinner flask, shaken Erlenmeyer, tissue culture flasks, Roller Bottles and a cell factory. According to a preferred embodiment, the vessel is a stirred tank stainless steel or disposal bioreactor that allows control of temperature, aeration, pH and other controlled conditions and which is equipped with (i) appropriate inlets for introducing the cells, sterile oxygen, various media for cultivation, etc.; (ii) outlets for removing cells and media; and (iii) means for agitating the culture medium in the bioreactor. Cells cultured according to the process of the present method are preferably in a "suspension state." A "suspension" of cells is to be broadly understood as including all types of suspended or dispersed cell cultures; the term "suspension state" is thus used to distinguish cells that are not cultured in a liquid medium, such as cells cultured by way of adhering on a support (e.g Petri dish or tissue culture flasks). Thus, the term "suspension" includes both freely dispersed cells and agglomerated cells, regardless of whether agglomeration occurs spontaneously or as a result of some exogenously supplied nucleating factor or agent.

As used herein, the term "animal cells" or "animal cell line" describes eukaryotic cells, and more preferably vertebrate cells, and even more preferably mammalian cells and avian cells. In the present invention, the terms "cell line" and "cells" will be used indistinctly. Animal cell lines may be genetically modified or not.

A number of mammalian cell lines are well known in the art and include for example cell lines derived from:

- human cells (e.g. PER.C6 cells which are described, for example, in WO01/38362, WO01/41814, WO02/40665, WO2004/056979, and WO2005/080556), MRC-5 (ATCC CCL-171), WI-38 (ATCC CCL-75), HEK cells, HeLa cells, fetal rhesus lung cells (ATCC CL- 160), human embryonic kidney cells (293 cells); or

- non-human primate (e.g. monkey) cells (e.g Vero cells derived from monkey kidneys),

- dog (e.g. MDCK cells from dog kidneys (as described in WO 97/37000 and WO 97/37001);

- rodent (e.g. hamster cells, such as BHK21-F, HKCC cells, or Chinese hamster ovary (CHO) cells).

As an alternative to mammalian sources, cell lines for use in the invention may be derived from avian sources such as chicken, duck, goose, quail or pheasant. The term "avian" as used herein is intended to have the same meaning as "bird", "aves" or "ανα", and will be used indistinctly. "Avian" refers to any species, subspecies or race of organism of the taxonomic class « ova ». In a preferred embodiment, "avian" refers to any animal of the taxonomix order " ' Anseriformes" (i.e duck, goose, swan and allies), "Galliformes" (i.e chicken, quails, turkey, pheasant and allies) and "Columbiformes" (i.e Pigeon and allies).

Avian cell lines may be derived from a variety of developmental stages including embryonic, chick and adult. Avian cell lines may be genetically modified or not. Preferably, the cell lines are derived from the embryonic cells, such as embryonic stem cells, embryonic fibroblasts, germ cells, or individual organs, including neuronal, brain, retina, kidney, liver, heart, muscle, or extra-embryonic tissues and membranes protecting the embryo. Examples of avian cell lines include avian embryonic stem cells (WOO 1/85938 and WO03/076601), immortalized duck retina cells (WO2005/042728), and genetically modified avian cells expressing telomerase reverse transcriptase (WO2007/077256 and WO2009/004016). Suitable avian embryonic derived stem cells, include the EBx cell lines derived from chicken embryonic stem cells such as EB45, EB14 and EB 14-074 (WO2006/108846) or derived from duck embryonic stem cells, such as EB66, EB26, EB24 and Muscovy duck EBx cell lines (WO2008/129058 & WO2008/142124). More preferably, the duck cell line is EB66 cell line.

In a preferred embodiment the host cell of the invention is a duck cell. According to the invention, a duck cell is defined as a cell providing from an animal belonging to the Anatidae family. According to a preferred embodiment of the invention, the duck cells are immortalized duck cell lines. As used throughout the entire application, "immortalized cell lines" refer to cell lines that proliferate in culture beyond the Hayfiick limit. Among Anatidae family, cells belonging to the Cairina or Anas genus are particularly preferred. Even more preferably, the immortalized avian cell lines belong to the Cairina moschata or to the Anas platyrhynchos species.

In a preferred embodiment, the immortalized cell line is a duck EBx cell line. Establishment of duck EBx cell lines is described for example in WO2008142124 and WO2008129058. In short, the process of establishment of EBx cell lines comprises two steps:

a) isolation, culture and expansion of embryonic stem (ES) cells from duck that do not contain complete endogenous proviral sequences, or a fragment thereof, susceptible to produce replication competent endogenous retroviral particles, more specifically EAV and/or ALV-E proviral sequences or a fragment thereof, in a complete culture medium containing all the factors allowing their growth and in presence of a feeder layer and supplemented with animal serum; optionally, said complete culture medium may comprise additives, such as additional amino -acids (i.e glutamine, . ..), sodium pyruvate, beta-mercaptoethanol, protein hydro lyzate of non-animal origin (i.e yeastolate, plant hydro lyzates, ...);

b) passage by modifying the culture medium so as to obtain a total withdrawal of said factors, said feeder layer and said serum, and optionally said additives, and further obtaining adherent or suspension duck cell lines, named EBx, that do not produce replication-competent endogenous retrovirus particles, capable of proliferating over a long period of time, in a basal medium in the absence of exogenous growth factors, feeder layer and animal serum.

The modification of the culture medium of step b) of the process of establishment EBx cell lines, so as to obtain progressive or total withdrawal of growth factors, serum and feeder layer, can be made simultaneously, successively or separately. The sequence of the weaning of the culture medium may be chosen among:

feeder layer / serum / growth factors;

feeder layer / growth factors / serum;

serum / growth factors / feeder layer;

serum / feeder layer / growth factors;

- growth factors / serum / feeder layer;

growth factors / feeder layer / serum.

In a preferred embodiment, the sequence of the weaning is growth factors / feeder layer / serum.

Particularly preferred are the duck embryonic-derived EBx cells named EB66, EB24, EB26 and Muscovy duck EBx cell lines. The establishment of EB66, EB24, EB26 and Muscovy duck EBx cell lines is described in examples 3, 4, 5 and 6, respectively, of WO2008129058. More preferably, said duck cell line is EB66 cell line. Duck cell lines, specially EB66 cell line, Hybridoma cells (e.g NSO, YB2/0), CHO cells, Baby Hamster Kidney (BHK) cells, PerC6 cells and 293 cells, are particularly well- suited for use in the method of the invention. Cells cultured according to the present method may be genetically modified or not by using recombinant DNA technology.

Production of virus

The process of the fed-batch culture of animal cells is particularly suited for the replication and production of human and animal viruses in the cultured animal cells for the manufacture of human and animal vaccines.

The present invention relates to a process of production of virus in a fed-batch culture of animal cells comprising the steps of:

c) optionally, adding for the remaining days of animal cell culture in said vessel, marginal volume of at least one compound selected among one source of carbohydrate, preferably a sugar as an energy source and a solution of one or more amino-acids, preferably glutamine.

and wherein said process comprises the step of infecting the culture of animal cells with said virus, and wherein the virus infection step is carried out either during step a), between steps a) and b), or during step b).

According to a first preferred embodiment, the virus infection step is carried during step b). According to a second preferred embodiment, the virus infection step is carried between steps a) and b). According to a preferred embodiment, the present invention relates to a process of production of virus in a fed-batch culture in animal cells, preferably duck cell lines, and more preferably duck EB66 cell line, comprising the steps of:

c) optionally, adding for the remaining days of animal cell culture in said vessel, marginal volume of a sugar, such as D-glucose and and/or amino acids, such as glutamine.

According to a preferred embodiment, when producing viruses, the cells of step a) are grown to a cell density greater or equal to 8 million cells/ml, greater or equal to 10 million cells/ml, greater or equal to 12 million cells/ml, more preferably greater or equal to 15 million cell/ml, and even more preferably greater or equal to 20 million cell/ml.

For some viruses, such the virus families of paramyxoviridae (i.e Newcastle disease virus) or orthomyxoviridae (i.e Influenza virus), the fed-batch process of virus production comprises the additional step of adding proteolytic enzyme in the culture medium in conditions that allow or favor virus propagation. The proteolytic enzyme is selected from the group consisting of trypsin, chymotrypsine, thermolysine, pepsine, pancreatine, papai^'ne, pronase, subtilisine A, elastase, furine and carboxypeptidase. According to a preferred embodiment, the enzyme is trypsin. The final concentration of trypsin in cell culture medium is comprises between around 0.5 to 1 mg/ml up to 25 mg/ml. More preferably, the final concentration of trypsin in cell culture medium is comprised between 0.01 to 10 usp/ml (usp: US pharmacopea unit) preferably around between 0.05 to 2 usp/ml, more preferably around between 0.3 to 1 usp/ml. Preferably, the proteolytic enzyme is a recombinant protein produced on a procaryotic host. According to a preferred embodiment, the proteolytic enzyme is added before, during and after the virus infection. According to a preferred embodiment, the proteolytic enzyme is added once daily during step b) until virus harvest.

The term "virus" as used herein includes not only naturally occurring viruses but also attenuated viruses, re-assortant viruses, viral vaccine strains, as well as recombinant viruses and viral vectors, and so on. The virus of the invention are preferably selected from the group consisting of adenoviruses, hepadnaviruses, herpes viruses, orthomyxoviruses, papovaviruses, paramyxoviruses, picornaviruses, poxviruses, reoviruses and retroviruses.

In a preferred embodiment, the viruses, the related viral vectors, viral particles and viral vaccines belong to the family of poxviridae, and more preferably to the chordopoxviridae. In one embodiment, the virus or the related viral vectors, viral particles and viral vaccines are a poxvirus, preferably an avipoxvirus selected among fowlpox virus (i.e TROVAC), canarypox virus (i.e ALVAC), juncopox virus, mynahpox virus, pigeonpox virus, psittacinepox virus, quailpoxvirus, sparrowpoxvirus, starling poxvirus, turkeypox virus. According to another preferred embodiment, the virus is a vaccinia virus selected among Lister-Elstree vaccinia virus strain, modified vaccinia virus such as Modified Vaccinia virus Ankara (MVA) which can be obtained from ATCC (ATCC Number VR- 1508), NYVAC (Tartaglia et al., 1992, Virology, 188:217-232), LC16m8 (Sugimoto et Yamanouchi, 1994, Vaccine, 12:675-681), CVI78 (Kempe et al., 1968, Pediatrics 42:980- 985) and other recombinant or non-recombinant vaccinia virus.

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of ortho-myxoviridae, in particular influenza virus. The influenza virus is selected from the group consisting of human influenza virus, avian influenza virus, equine influenza virus, swine influenza virus, feline influenza virus. Influenza virus is preferably selected in strains A, B and C. Among strains A, one can recite viruses with different subtypes of haemagglutinin and neuraminidase, such as without limitation H1N1, H2N2, H3N2, H4N2, H4N6, H5N1, H5N2, H7N7 et H9N2. Among H1N1 strains, one can recite A/Puerto Rico/8/34, A/New Caledonia/20/99, A/Beijing/262/95, A/Johannesburg/282/96, A/Texas/36/91, A/Singapore/6/86, A/Solomon Islands/03/2006. Among strains H3N2, one can recite A/Panama/2007/99, A/Moscow/10/99, A/Johannesburg/33/94, A/Wisconsin/67/05. Among B strains, one can recite without limitation B/Porto Rico/8/34, B/Johannesburg/5/99, B/Vienna/1/99, B/Ann Arbor/1/86, B/Memphis/1/93, B/Harbin/7/94, N/Shandong/7/97, B/Hong Kong/330/01, B/Yamanashi/166/98, B/Jiangsu/10/03, B/Malaysia 2506/04. The influenza Virus of the invention is selected among wild type virus, primary viral isolate obtained from infected individual, recombinant virus, attenuated virus, temperature sensitive virus, low- temperature adapted virus, reassortant virus, reverse genetic engineered virus.

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of paramyxoviridae. Preferably the virus is a naturally occuring paramyxovirus or a recombinant paramyxovirus selected in the group comprising measles virus, mumps virus, rubella virus, Sendai virus, Respiratory Syncythial virus (PvSV), human para-influenza types I and III, Rinderpest virus, canine distemper virus, Newcastle disease virus, duck para-influenza virus. According to preferred embodiment, the virus is measles virus or a recombinant measles virus. According to another preferred embodiment, the virus is Newcastle Disease virus (NDV) or a recombinant NDV. Example of NDV strain is LaSota strain. When the virus of the invention is NDV, the process of the invention comprises preferably the additional step of adding proteolytic enzyme in the culture medium in conditions that allow virus propagation. According to a preferred embodiment, the enzyme is trypsin. The final concentration of trypsin in cell culture medium is comprises between around 0.01 μg/ml up to 10 μg/ml. More preferably, the final concentration of trypsin in cell culture medium is comprised between 0.01 to 10 usp/ml (usp: US pharmacopea unit) preferably around between 0.3 to 1 usp/ml, more preferably around between 0.4 to 0.75 usp/ml. Interestingly, the EBx cell lines of the invention that may grow in adherence are useful to perform virus titration, and preferably NDV titration, on a plaque assay. Indeed, unlike CEFs and chicken DF1 fibroblasts for which is was not possible to observe any cytopathic effects, virus growth in EBx cells leads to the formation of characteristic giant cells. In addition, NDV viral particles may be determined by haemagglutination assay. Therefore, the invention also pertains to the use of EB66 cells of the invention for the titration of virus, such as NDV virus.

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of togaviridae. Preferably the virus is a naturally occurring alphavirus or a recombinant alphavirus selected in the group comprising Sinbis virus, Semliki forest virus, O'nyong'nyong virus, Chikungunya virus, Mayaro virus, Ross river virus, Eastern equine encephalitis virus, Western Equine encephalitis virus, Venezuelan Equine encephalitis virus. In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of herpesviridae. Preferably the virus is a naturally occuring Marek Disease virus or a recombinant Marek Disease virus. The Marek Disease virus (MDV) is preferably selected among the license vaccine strains of MDV such as : FC126 (HTV), SB-1, 301B/1, CVI988 Clone C, CV1988/C/R6, CVI988/Rispens, R2/23 (Mdl l/75).

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of hepadnaviridae. Preferably the virus is a naturally occuring naturally occuring hepadnavirus or a recombinant hepadnavirus, preferably selected among avian and human hepadnavirus. The avian hepadnavirus is preferably selected among the group consisting of duck hepatitis B virus (DHBV), heron hepatitis B virus (HHBV) and snow goose (SGHBV).

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of birnaviridae, in particular Infectious Bursal Disease virus.

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of flaviviridae, in particular Dengue virus, Japanese encephalitis virus and West Nile virus.

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of coronaviridae, in particular Infectious Bronchitis virus.

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of circoviridae, in particular Chicken Anemia virus.

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of retroviridae. Preferably the virus is a naturally occurring retrovirus selected among reticulo-endotheliosis virus, duck infectious anemia virus, suck spleen necrosis virus, or a recombinant retrovirus thereof.

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of parvoviridae. Preferably the virus is a naturally occurring parvovirus such as duck parvovirus or a recombinant parvovirus thereof.

In another preferred embodiment, the viruses, the related viral vectors, the viral particles and vaccines belong to the family of adenoviridae. Preferably the virus is a naturally occurring adenovirus preferably selected among fowl adenovirus, goose adenovirus, duck adenovirus and pigeon adenovirus or a recombinant adenovirus thereof. Examples of Fowl adenovirus are Fowl adenovirus 1 (CELO), Fowl adenovirus 5 (340), Fowl adenovirus 4 (KR95), Fowl adenovirus 10 (CFA20), Fowl adenovirus 2 (P7-A), Fowl adenovirus 3 (75), Fowl adenovirus 9 (A2-A), Fowl adenovirus 11 (380), Fowl adenovirus 6 (CR119), Fowl adenovirus 7 (YR36), Fowl adenovirus 8a (TR59) Fowl adenovirus 8b (764) and Egg Drop Syndrome virus. Examples of Goose adenovirus are Goose adenovirus 1, Goose adenovirus 2, Goose adenovirus 3. Example of Duck adenovirus is Duck adenovirus 2. Example of Pigeon adenovirus is Pigeon adenovirus 1.

Recombinant viruses include but are not limited to viral vectors comprising a heterologous gene. In some embodiments, a helper function(s) for replication of the viruses is provided by the host cell, a helper virus, or a helper plasmid. Representative vectors include but are not limited to those that will infect avian or mammalian cells.

Virus production process according to the present method can, optionally, include a harvest step and/or purification steps of the produced virus. Viruses may be intracellular or extracellular. Methods of isolating and purifying these viral products include, but are not limited to, centrifugation, ultra- filtration and chromatography.

In preferred embodiment, the process of production of virus in a fed-batch culture in animal cells, is harvested at a time between 8 and 20 days (from the vessel seeding). It is expected that after 8 days already some increase in yield will be obtained as compared to the batch process, whereas processes longer than 20 days would likely suffer from a decrease in quality of the product obtained. The duration of the fed-batch process of virus production will depend of the virus.

According to another embodiment of the invention, the cell infection step is performed simultaneously to the addition of concentrated culture medium to the cell culture according to step b). In a preferred embodiment, the date of infection is 24h post day of the addition of the concentrated culture medium according to step b). Hence, according to a preferred embodiment the initial date of feeding is D2 or D3 and the date of infection is D3 or D4, respectively.

The viral infection might be carried out at an m.o.i (multiplicity of infection) of about 10 to 10^"8, preferably 10^"1 to 10^"6, more preferably about 10^"2 to 10^"5, and more preferably about 10^"4. The man skilled in the art will determine the optimal m.o.i according to the virus type. The infection step is preferably performed when the cell density is at least around 4 million, preferably 6 million cells/ml, more preferably 8 million cells/ml. The production of virus in a fed-batch culture in animal cells according to the invention is performed at a temperature comprises between 32°C to 39°C depending of the virus type. According to a preferred embodiment, step a) is performed at a temperature comprise between 35 and 39°C, more preferably approximately 37°C; step b) and c) are performed at a lower temperature comprises below 37°C, preferably below 35°C, more preferably below 34°C, more preferably below 33°C, and even more preferably below or at 32°C.

The pH of the culture is preferably monitored. The pH shall be in a range from 6.5 to 7.8, preferably around 6.8 to 7.5, and more preferably around 7.2.

The invention also relate to the virus produce by the process of the invention. The instant invention also relates to the vaccine containing the virus of the invention.

Production of recombinant proteins

The process of the fed-batch culture of animal cells is particularly suited for the production of recombinant protein in the cultured animal cells for the manufacture of human and animal therapeutic and prophylactic drugs.

The present invention relates to a process of production of recombinant protein, such as monoclonal antibody, in a fed-batch culture of animal cells comprising the steps of: a) growing the cells, preferably in exponential phase, in a cell growth medium, optionally supplemented with defined supplements, in a culture volume corresponding to a maximum of 75%, preferably to about 50% or less, of the maximum vessel volume, to a cell density greater or equal to 4 million cells/ml, more preferably to a cell density greater or equal to 6, 8, 10, 12, 15, 20, 25, 30, 35, or even 40 million cells/ml;

and wherein said animal cells are genetically modified to express said recombinant protein.

According to a preferred embodiment, the present invention relates to a process of production of recombinant protein, such as monoclonal antibody in a fed-batch culture in animal cells, preferably duck cell lines, and more preferably duck EB66 cell line, comprising the steps of:

Generation of genetically modified cells to express recombinant proteins is well- known by the man skilled in the art. Methods which are well known to and practiced by those skilled in the art can be used to construct expression vectors containing sequences encoding the proteins and polypeptides of interest, as well as the appropriate transcriptional and translational control elements. These methods include in vitro recombinant DNA techniques, synthetic techniques, and in vivo genetic recombination. Such techniques are described for example in Sambrook et al. (1989, Molecular Cloning, A Laboratory Manual, Cold Spring Harbor Press, Plainview, N.Y.) and in Ausubel et al. (1989, Current Protocols in Molecular Biology, John Wiley & Sons, New York, N.Y.).

According to a preferred embodiment, when producing recombinant proteins, the cells of step a) are grown to a cell density greater or equal to 4 million cells/ml, greater or equal to 8 million cells/m, more preferably greater or equal to 10 million cell/ml, and even more preferably greater or equal to 20 million cell/ml.

The production of recombinant proteins, such as monoclonal antibody, in a fed- batch culture in animal cells according to the invention is performed at a temperature comprises between 32°C to 39°C depending of cell type. According to a preferred embodiment, step a) is performed at a temperature comprise between 35 and 39°C, more preferably approximately 37°C; step b) and c) are performed at a lower temperature comprises below 37°C, preferably at 35°C, more preferably at 34°C, more preferably at 33°C, and even more preferably below or at 32°C.

The present method optionally includes harvesting the cultured cells during or subsequent to the period of continuous culture. Harvesting methods include, but are not limited to, centrifugation, settling, filtration and acoustic separation.

The invention also relates to the recombinant proteins produced by the process of the invention, and their uses as human and animal therapeutic and prophylactic drugs.

In preferred embodiment, the process of production of recombinant protein in a fed- batch culture in animal cells, is harvested at a time between 8 and 20 days (from the vessel seeding). It is expected that after 8 days already some increase in yield will be obtained as compared to the batch process, whereas processes longer than 20 days would likely suffer from a decrease in quality of the product obtained. The duration of the fed-batch process of recombinant protein, specially monoclonal antibody, is preferably less than 15 days post vessel seeding.

Examples of proteins of interest that can be advantageously produced by the method of this invention include, without limitation, cytokines, cytokine receptors, growth factors (e.g. EGF, HER-2, FGF-alpha, FGF-beta, TGF-alpha, TGF-beta, PDGF, IGF-1, IGF-2, NGF), growth factor receptors, including fragment of the protein thereof. Other non- limiting examples include growth hormones (e.g. human growth hormone, bovine growth hormone); insulin (e.g., insulin A chain and insulin B chain), pro-insulin, erythropoietin (EPO), colony stimulating factors (e.g. G-CSF, GM-CSF, M-CSF); interleukins (e.g. IL-1 through IL-12); vascular endothelial growth factor (VEGF) and its receptor (VEGF-R), interferons (e.g. IFN-alpha, beta and gamma), tumor necrosis factor (TNF) and their receptors (TNFR-1 and TNFR-2), thrombopoietin (TPO), thrombin, brain natriuretic peptide (BNP); clotting factors (e.g. FactorVIII, Factor IX, von Willebrands factor and the like), anti-clotting factors; tissue plasminogen activator (TPA), urokinase, follicle stimulating hormone (FSH), luteinizing hormone (LH), calcitonin, CD proteins (e. g., CD2, CD3, CD4, CD5, CD7, CD8, CDl la, CDl lb, CD18, CD19, CD20, CD25, CD33, CD44, CD45, CD71, etc.), CTLA proteins (e.g.CTLA4); T-cell and B-cell receptor proteins, bone morphogenic proteins (BNPs, e.g. BMP-1, BMP-2, BMP-3, etc.), neurotrophic factors, e.g. bone derived neurotrophic factor (BDNF), neurotrophins, e.g. rennin, rheumatoid factor, RANTES, albumin, relaxin, macrophage inhibitory protein (e.g. MIP-1, MIP-2), viral proteins or antigens, surface membrane proteins, ion channel proteins, enzymes, regulatory proteins, antibodies, immunomodulatory proteins, (e.g. HLA, MHC, the B7 family), homing receptors, transport proteins, superoxide dismutase (SOD), G-protein coupled receptor proteins (GPCRs), neuromodulatory proteins, Alzheimer's Disease associated proteins and peptides, (e.g. A-beta) and others as known in the art. Fusion proteins and polypeptides, chimeric proteins and polypeptides, as well as fragments or portions, or mutants, variants, or analogs of any of the aforementioned proteins and polypeptides are also included among the suitable proteins, polypeptides and peptides that can be produced by the methods of the present invention.

In a preferred embodiment, the protein of interest is a glycoprotein, and preferably a viral protein. Example of viral proteins (subunits) that can be produced in the methods according to the invention include, without limitation, proteins from enterovirus, such as rhinovirus, aphtovirus, or poliomyelitis virus, herpes virus, such as herpes simplex virus, pseudorabies virus or bovine herpes virus, orthomyxovirus such as influenza virus, a paramyxovirus, such as newcastle disease virus, respiratory syncitial virus, mumps virus or a measles virus, retrovirus, such as human immunodeficiency virus or a parvovirus or a papovavirus, rotavirus or a coronavirus, such as transmissable gastroenteritisvirus or a flavivirus, such as tick-borne encephalitis virus or yellow fever virus, a togavirus, such as rubella virus or eastern-, western-, or venezuelean equine encephalomyelitis virus, a hepatitis causing virus, such as hepatitis A or hepatitis B virus, a pestivirus, such as hog cholera virus or a rhabdovirus, such as rabies virus. According to another embodiment, the protein of interest is a bacterial protein.

In another preferred embodiment, the biological product of interest is an antibody. The term "antibody" as used herein refers to polyclonal and monoclonal antibodies and fragments thereof, and immunologic binding equivalents thereof. The term "antibody" refers to a homogeneous molecular entity, or a mixture such as a polyclonal serum product made up of a plurality of different molecular entities, and broadly encompasses naturally- occurring forms of antibodies (for example, IgD, IgG, IgA, IgM, IgE) and recombinant antibodies such as single-chain antibodies, chimeric and humanized antibodies and multi- specific antibodies. The term "antibody" also refers to fragments and derivatives of all of the foregoing, and may further comprises any modified or derivatised variants thereof that retains the ability to specifically bind an epitope. Antibody derivatives may comprise a protein or chemical moiety conjugated to an antibody. A monoclonal antibody is capable of selectively binding to a target antigen or epitope. Antibodies may include, but are not limited to polyclonal antibodies, monoclonal antibodies (mAbs), humanized or chimeric antibodies, camelized antibodies, single chain antibodies (scFvs), Fab fragments, F(ab')2 fragments, disulfide- linked Fvs (sdFv) fragments, anti-idiotypic (anti-Id) antibodies, intra- bodies, synthetic antibodies, and epitope-binding fragments of any of the above. The term "antibody" also refers to fusion protein that includes a region equivalent to the Fc region of an immunoglobulin.

Preferred antibodies within the scope of the present invention include those comprising the amino acid sequences of the following antibodies: anti-HER2 antibodies including antibodies comprising the heavy and light chain variable regions of huMAb 4D5- 8 (Carteret al., Proc. Natl. Acad. Sci. USA, 89: 4285-4289 (1992), U.S. Patent No. 5,725, 856) or Trastuzumab such as HERCEPTIN™; anti-CD20 antibodies such as chimeric anti- CD20 "C2B8" as in US Patent No. 5,736, 137 (RITUXAN®), a chimeric or humanized variant of the 2H7 antibody as in US Patent No. 5,721,108 or Tositumomab (BEXXAR) ; anti-IL-8 (St John et al., Chest, 103: 932 (1993), and International Publication No. WO 95/23865); anti-VEGF antibodies including humanized and/or affinity matured anti-VEGF antibodies such as the humanized anti-VEGF antibody huA4.6.1 AVASTIN™ (Kim et al., Growth Factors, 7: 53- 64 (1992), International Publication No. WO 96/30046, and WO 98/45331); anti-PSCA antibodies (WO01/40309) ; anti-CD40 antibodies, including S2C6 and humanized variants thereof (WO00/75348) ; anti-CDl la (US Patent No. 5,622,700, WO 98/23761) ; anti-EGFR (chimerized or humanized 225 antibody as in WO 96/40210); anti-CD3 antibodies such as OKT3 (US Patent No. 4,515,893) ; anti-CD25 or anti-tac antibodies such as CHI-621 (SIMULECT) and (ZENAPAX) (See US Patent No. 5,693,762) ; anti-CD4 antibodies such as the cM-7412 antibody (Choy et al. Arthritis Rheum 39(1) : 52-56 (1996) ); anti-CD52 antibodies such as CAMPATH-1H (Riechmann et al. Nature 332: 323-337 (1988); anti-carcinoembryonic antigen (CEA) antibodies such as hMN-14 (Sharkey etal. Cancer Res. 55 (23Suppl): 5935s-5945s (1995); anti-EpCAM antibodies such as 17-1 A (PANOREX); anti-GpIIb/IIIa antibodies such as abciximab or c7E3 Fab (REOPRO); anti-RSV antibodies such as MEDI-493 (SYNAGIS) ; anti-CMV antibodies such as PROTOVIR; anti-hepatitis antibodies such as the anti-HepB antibody OSTAVIR ; anti-human renal cell carcinoma antibody such as ch-G250; anti-humanl7-lA antibody (3622W94); anti-human colorectal tumor antibody(A33) ; anti-human melanoma antibody R24 directed against GD3 ganglioside; anti-human squamous-cell carcinoma (SF- 25); and anti-human leukocyte antigen (HLA) antibodies such as SmartlDIO and the anti- HLA DR antibody Oncolym(Lym-l). According to a preferred embodiment, the transfected cells of the invention, and more specifically duck cell lines, and more specifically EB66 cells, are able to produce at least 5 pg/cell/day of immunoglobulin in batch culture, preferably at least 10 pg/cell/day of immunoglobulin in batch culture, more preferably at least 20 pg/cell/day of immunoglobulin in batch culture, even more preferably at least 30 pg/cell/day of immunoglobulin in batch culture. The two chains assemble within the cell and are then secreted into the culture medium as functional antibody.

Interestingly, the inventors have demonstrated that the antibody, the antibody fragment, or the fusion proteins that include a region equivalent to a Fc region of an immunoglobulin, produced in a duck cell line, such as EB66 cells, by the method of the invention have increased Fc-mediated cellular toxicity. For example, antibody of IgGl subtype, produced in EB66 cells, have an increased ADCC activity compared to the same antibody produced in hybridoma (e.g NS0) and CHO cells. This is achieved by providing the antibodies of interest with the duck glycosylation pattern.

In particular, the transfected duck cells, more specifically EB66 cells of the invention, allow to express a large proportion of antibodies or fragment thereof, carrying a common N-linked oligosaccharide structure of a biantennary-type that comprises long chains with terminal GlcNac that are highly galactosylated and non-fucosylated and which confer strong ADCC activity to antibodies. Among a recombinant antibody population produced in duck cells, more specifically in EB66 cells, the proportion of non-fucosylated antibodies represent at least 30%, more preferably at least 45%, more preferably at least 55%, and more preferably at least 65%> of the antibodies or higher. More precisely, the invention provides a recombinant monoclonal antibody produced by duck cell line, preferably duck EB66 cell line, wherein said antibody is characterized as having approximately 45% or more of non-fucosylated N-linked oligosaccharides structures in the antibody population produced in duck cells.

The instant invention relates to the biological product of interest according the invention as a medicament. The invention also covers the use of a biological product (i. e viral vaccine, recombinant protein, monoclonal antibody...) obtained by the process of the invention, for the preparation of a pharmaceutical composition for the prevention or the treatment of human and animal diseases. Such pharmaceutical compositions preferably include, in addition to the biological product, a physiologically acceptable diluent or carrier.

The examples below explain the invention in more detail. The following preparations and examples are given to enable those skilled in the art to more clearly understand and to practice the present invention. The present invention, however, is not limited in scope by the exemplified embodiments, which are intended as illustrations of single aspects of the invention only, and methods which are functionally equivalent are within the scope of the invention. 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 accompanying drawings. Such modifications are intended to fall within the scope of the appended claims. For the remainder of the description, reference will be made to the legend to the figures below.

FIGURES

FIGURE 1: GLUCOSE FEDBATCH PROCESS USING CONCENTRATED MEDIUM FOR MONOCLONAL ANTIBODY PRODUCTION IN EB66 CELL LINE Fig. 1A: in a simple batch process, monoclonal antibody producing EB66 cells have a short viability (approx. 5 days) which decreases after day 5. EB66 cells reach a maximum viable cell density of approximately 8 million cell/ml. The yield of Igl expressed in EB66 cells reaches 18 μg/ml.

Fig. IB: in a glucose fedbatch process using concentrated medium, monoclonal antibody producing EB66 cells have a longer cell viability (approx. 8 days). EB66 cells reach a maximum viable cell density of approximately 40 million cell/ml. The yield of Igl expressed in EB66 cells reaches approximately 1 g/1. The fedbatch process of the invention allows a 90 fold increase in monoclonal antibody production yield compared to a regular batch process. FIGURE 2: METABOLIC ANALYSIS OF GLUCOSE FEDBATCH PROCESS USING CONCENTRATED MEDIUM FOR MONOCLONAL ANTIBODIES PRODUCTION IN EB66 CELL LINE

The metabolic profile of EB66 cells culture expressing IgGl monoclonal antibodies shows remarkable features: No accumulation of inhibitory metabolites, such as lactate or ammonium, even at a high viable cell density (> 40 million cell/ml) and limited consumption of glutamine.

FIGURE 3: PRODUCTION OF A/H1N1/BEIJING INFLUENZA VIRUS STRAIN IN EB66 CELL LINE USING BATCH PROCESS vs GLUCOSE FEDBATCH PROCESS

Fig. 3 A: in the former standard process, EB66 cells were grown in ExCELL EBx GRO-1 cell growth medium (SAFC Biosciences) during 3 days up to a viable cell density of approximately 6 million cells/ml, then infected with influenza virus strain A/HlNl/Beijing/262/95. One hour after virus infection, 1.5 volumes of fresh virus production medium (SAFC Biosciences) was added to the Erlenmeyer flasks. A day 3 postinfection, the maximal viable cell density is approximately 9 million cells/ml.

Fig. 3B: EB66 cells (passage pl42) were seeded in Shaken Erlenmeyers (250 ml) in ExCELL EBx GRO-I medium supplemented with 2.5 mM glutamine at day 0 at a cell concentration of 0.5x10exp6 cells/ml. EB66 cells were grown as a batch culture in a fixed volume until the day 3, 4 or 5, when the infection with A/HlNl/Beijing/262/95 influenza virus (multiplicity of infection 10^"4 TCID50/cell) is performed. A glucose fedbatch at 8g/l and a daily addition of ExCELL EBx GRO-I medium 4X concentrated medium is initiated at day 3, in order to reach maximum vessel volume at day 7 post infection. When the infection is performed at day 3, 4 and 5, maximum viable cell density is respectively of approximately 15 million cells/ml, 20 million cells/ml and 40 million cells/ml.

FIGURE 4: PRODUCTION OF A/H1N1/BEIJING HAEMAGLUTININ IN STANDARD PROCESS VS GLUCOSE FEDBATCH PROCESS

Haemaglutinin titer measured by serial radial immuno- diffusion assay and expressed in μg/ml of cell culture supernatant obtained at different days post-infection. Fig. 4A: standard process; Fig. 4B: glucose fed-batch using concentrating medium.

FIGURE 5: PRODUCTION OF A/H3N2/WISCONSIN INFLUENZA VIRUS STRAIN IN EB66 CELL LINE USING BATCH PROCESS vs GLUCOSE FEDBATCH PROCESS IN ERLENMEYER

Left panel: in the former standard process, EB66 cells were grown in ExCELL EBx GRO- 1 cell growth medium (SAFC Biosciences) during 3 days up to a viable cell density of approximately 6 million cells/ml, then infected with influenza virus strain A/H3N2/Wisconsin. One hour after virus infection, 1.5 volumes of fresh virus production medium (SAFC Biosciences) was added to the Erlenmeyer flasks. A day 3 post-infection, the maximal viable cell density is approximately 9 million cells/ml.

Right Panel: EB66 cells (passage pl42) were seeded in Shaken Erlenmeyers (250 ml) in ExCELL EBx GRO-I medium supplemented with 2.5 mM glutamine at day 0 at a cell concentration of 0.5xl0exp6 cells/ml. EB66 cells were grown as a batch culture in a fixed volume until the day 3 when a glucose fedbatch at 10 or at 15g/l, a glutamine fedbatch at 2.5 mM and a daily addition of ExCELL EBx GRO-I medium 4X concentrated medium is initiated. The infection with A/H3N2/Wisconsin influenza virus (multiplicity of infection 10^~4 TCID50/cell) is performed at day 5, in order to reach maximum vessel volume at day 7 post seeding. Maximum viable cell density obtained with a glucose fedbatch at lOg/1 and 15g/l is approximately 20 million cells/ml.

FIGURE 6: PRODUCTION OF A/H3N2/WISCONSIN HAEMAGLUTININ IN STANDARD PROCESS VS GLUCOSE FEDBATCH PROCESS

Haemaglutinin titer measured by serial radial immuno- diffusion assay and expressed in μg/ml of cell culture supernatant obtained at different days post-infection. The volumetric haemagglutinin (HA) productivity value obtained in 250 ml Erlenmeyers with the glucose fedbatch process (10 g/1 and 15g/l) using concentrated medium is much higher (approx. 80 μg/ml of HA) than the one obtained with standard process (approx. 30 ug/ml of HA).

FIGURE 7: PRODUCTION OF A/H3N2/WISCONSIN INFLUENZA VIRUS STRAIN IN EB66 CELL LINE USING BATCH PROCESS vs GLUCOSE FEDBATCH PROCESS IN 2L-BIORECATOR

Fig 7A: in the former standard process, EB66 cells were grown in ExCELL EBx GRO-1 cell growth medium (SAFC Biosciences) during 3 days up to a viable cell density of approximately 6 million cells/ml, then infected with influenza virus strain A/H3N2/Wisconsin. One hour after virus infection, 1.5 volumes of fresh virus production medium (SAFC Biosciences) was added to the Erlenmeyer flasks. A day 3 post-infection, the maximal viable cell density is approximately 9 million cells/ml.

Fig7B: EB66 cells (passage pl42) were seeded in Shaken Erlenmeyers (250 ml) in ExCELL EBx GRO-I medium supplemented with 2.5 mM glutamine at day 0 at a cell concentration of 0.5xl0exp6 cells/ml. EB66 cells were grown as a batch culture in a fixed volume until the day 3 when a glucose fedbatch at 8 g/1, a glutamine fedbatch at 2.5 mM and a daily addition of ExCELL EBx GRO-I medium 4X concentrated medium is initiated. The infection with A/H3N2/Wisconsin influenza virus (multiplicity of infection 10^"4 TCID50/cell) is performed at day 4, in order to reach maximum vessel volume at day 6 post seeding. Maximum viable cell density obtained with a glucose fedbatch at 8g/l is approximately 25-30 million cells/ml.

FIGURE 8: PRODUCTION OF A/H3N2/WISCONSIN HAEMAGLUTININ IN STANDARD PROCESS VS GLUCOSE FEDBATCH PROCESS IN 2L BIOREAC TOR

Haemaglutinin titer measured by serial radial immuno- diffusion assay and expressed in μg/ml of cell culture supernatant obtained at different days post-infection. The volumetric haemagglutinin (HA) productivity value obtained in 2L Bioreactor with the glucose fedbatch process (8 g/1) using concentrated medium is much higher (approx. 100 μg/ml of HA) than the one obtained with standard process (approx. 30 μg/ml of HA).

FIGURE 9: FEDBATCH PROCESS FOR MONOCLONAL ANTIBODY PRODUCTION IN EB66 CELL LINE, USING 2X AND 4X CONCENTRATED CULTURE MEDIUM FEEDS

It shows the cell density (line charts) and IgG production (columns) results obtained using a standard batch process of IgGl monoclonal antibody in EB66 cells, referred as "CDM4 Batch" and those obtained with a fed-batch process comprising a first step of batch culture using a CDM4 (Hyclone) medium as seeding media and a second step comprising the use of 2 fold or 4 fold ExCELL EBx GRO-I medium (SAFC) concentrated medium, referred as "CDM4/GroI 2x" and "CDM4/GroI 4x" respectively. Glutamine levels were maintained at 2.5 mM from day 3 to the end of the kinetics.

Results are shown for day 3 (start of the fed-batch process) to day 7. The fed-batch process of the invention allows a 4.5 fold and a 1.6 fold increase for the 4x and the 2x concentrated media, respectively, compared to the regular batch process. EB66 cells reached a maximum viable cell density of about 30 million cell/mL at day 5 with both the 4x and the 2x concentrated media, representing a 2fold increase with regards to the about 15 million cell/mL obtained with the batch process.

FIGURE 10: FEDBATCH PROCESS FOR MONOCLONAL ANTIBODY PRODUCTION IN EB66 CELL LINE USING DIFFERENT GLUCOSE CONCENTRATIONS

It shows the effects of glucose feeds concentration in cell density (line charts) and IgG production (columns) in fed-batch protocol comprising the daily addition of ExCELL EBx GRO-I medium (SAFC) 4X concentrated (Grol 4x) from day 3 and the further addition of glucose feeds to maintain a concentration of 6g/L, 8g/L and 1 Og/L, respectively, to the end of the kinetics. Glutamine levels were maintained at 2.5 mM from day 3 to the end of the kinetics.

Results are shown for day 3 (start of the fed-batch process) to day 7. The provided results show that the concentration of glucose in the culture medium had an impact both in cell density and IgG antibody production, best results were obtained when the glucose concentration was maintained at lOg/L during the fed-batch process.

FIGURE 11: METABOLIC PROFILE OF GLUCOSE FEDBATCH PROCESS USING CONCENTRATED MEDIUM FOR MONOCLONAL ANTIBODIES PRODUCTION IN EB66 CELL LINE

It shows the metabolic profile of EB66 cells clones further to the fed-batch process with Grol 4X on day 3 and day 4 and with glucose stock solution at a final concentration of lOg/L since day 5 to the end of kinetics. Furthermore, a glutamine Fed-batch is carried out at 2,5mM since day 3. The metabolic profile of EB66 cells culture expressing IgGl monoclonal antibodies shows remarkable features: No accumulation of inhibitory metabolites, such as lactate or ammonium, and limited consumption of glutamine even at high glucose concentrations of 1 Og/L.

EXAMPLES

Duck EB66 cell line, which has been established according to the process described in patent applications WO2008/129058 & WO2008/142124, were used in the following examples.

EXAMPLE 1: GLUCOSE FEDBATCH PROCESS USING CONCENTRATED MEDIUM FOR MONOCLONAL ANTIBODY PRODUCTION

In the fed-batch process of the invention, EB66 cells were seeded in 2L-stirred tank bioreactor (Applikon™) at a cell concentration of 0.5x10exp6 cells/ml in a serum- free cell growth medium such as CDM4PerMab (Hyclone) and allowed to grow as a batch culture in a fixed volume. When the viable cell density is greater than 4 millions cells/ml, usually at day 3, a glucose fed-batch process is implemented until for example day 8. The fed-batch process comprises:

- daily addition of 4X concentrated ExCELL EBx GRO-1 cell culture medium (SAFC Biosciences Cat. N°14530c). The formulation of 4X concentrated ExCell EBx GRO- I medium was obtained by a 4 fold increase of the concentration of each component of ExCELL EBx GRO-1 medium, except the components which are involved in, or act on, the osmotic pressure and/or the osmolality, such as salts and buffering agents, which are IX concentrated in the 4X concentrated ExCell EBx GRO-I medium, -daily addition of glucose to maintain glucose concentration in the medium at 10 g/1 concentration;

-daily addition of glutamine to maintain glutamine concentration in the medium at 2.5 mM concentration.

A standard batch process was run in parallel which consists of seeding EB66 cells in 2L- stirred tank bioreactor (Applikon™) at a cell concentration of 0.5x10exp6 cells/ml in a cell growth medium (Hyclone), then growing cells without nutrient feed in a fixed volume during 8 days.

The standard batch process of IgGl monoclonal antibody in EB66 cells (Figure 1) allows to reach a short cell viability (approx. 5 days), a cell density of approximately 8 million cells/ml and low monoclonal antibody production yield of approximately 18 μg/ml.

In a fedbatch process of the invention, monoclonal antibody producing EB66 cells have a longer cell viability (approx. 8 days). EB66 cells reach a maximum viable cell density of approximately 40 million cell/ml. The yield of Igl expressed in EB66 cells reaches approximately 1 g/1.

The fedbatch process of the invention allows a 90 fold increase in monoclonal antibody production yield compared to a regular batch process.

Very interestingly, no accumulation of lactate or ammonium (even at a very high viable cell density of > 40 million cell/ml) is observed with monoclonal antibody producing EB66 cells culture. This appears to be a characteristic of duck cell line such as EB66 cells. In addition, duck cell lines, such as EB66 cells, have also limited consumption of glutamine.

The inventors thus demonstrated that very high cell densities of duck cell, such as EB66 cells, can be achieved by a better control of nutrient consumptions. Today experimental data allowed to reach cell densities up to 70 million cells/ml without accumulation of lactate or ammonium in the culture. Therefore, duck cell line, such as EB66, have the remarkable capability to grow in conditions of high glucose concentrations (> 8 g/1) and to accumulate no or low lactate and ammonium, allowing to reach high cell densities. EXAMPLE 2: GLUCOSE FEDBATCH PROCESS USING CONCENTRATED MEDIUM FOR A/HlNl/Beijing/262/95 INFLUENZA VIRUS STRAIN PRODUCTION

2.1 - Standard process of production of A/HlNl/Beijing/262/95 influenza virus strain The Fedbatch process of the invention was run in parallel to the former standard process that includes the following steps: proliferating EB66 cell line in cell growth medium, infecting the cells with influenza virus, then adding virus production medium and further culturing infected cells to allow virus replication.

Briefly, duck EB66 cells (passage 142) were grown in Shaken Erlenmeyers (250 ml) in one volume of (IX) SAFC BIOSCIENCES ExCELL EBx GRO-I animal serum free medium (Cat N° 14530c) supplemented with 2.5 mM glutamine. At day 3 post seeding, when the cell density is around or greater than 6 million cells/ml, influenza virus infection is performed at a multiplicity of infection of 10^"4 TCID50/ml. One hour after virus infection, 1.5 volumes of fresh animal serum free virus production medium were added (Figure 3A). The maximum viable cell density obtained is approximately 9 million cells/ml.

2.2 - Glucose Fedbatch process using concentrated medium for the production of A/HlNl/Beijing/262/95 influenza virus strain

EB66 cells (passage pl42) were seeded in Shaken Erlenmeyers (250 ml) in ExCELL EBx GRO-I medium supplemented with 2.5 mM glutamine at day 0 at a cell concentration of 0.5x10exp6 cells/ml. EB66 cells were grown as a batch culture in a fixed volume until the day 3, 4 or 5, when the infection with A/HlNl/Beijing/262/95 influenza virus (multiplicity of infection 10^"4 TCID50/cell) is performed.

A glucose fedbatch at 8g/l , a glutamine fedbatch at 2.5 mM and a daily addition of ExCELL EBx GRO-I medium 4X concentrated medium are initiated at day 3, in order to reach maximum vessel volume at day 7 post infection.

The formulation of 4X concentrated ExCell EBx GRO-I medium was obtained by a 4 fold increase of the concentration of each component of ExCELL EBx GRO-1 medium, except the components which are involved in, or act on, the osmotic pressure and/or the osmolality, such as salts and buffering agents, which are IX concentrated in the 4X concentrated ExCell EBx GRO-I medium.

When the infection is performed at day 3, 4 and 5, maximum viable cell density is respectively of approximately 15 million cells/ml, 20 million cells/ml and 40 million cells/ml (Figure 3B). 2.3 - Production of A/HlNl/Beijing/262/95 Haemaggutinin

The concentration of influenza haemagglutimn in the cell culture medium was determined by the SRID method as described by Wood et al. (An improved single-radial- immunodiffusion technique for the assay of influenza haemagglutimn antigen: application for potency determinations of inactivated whole virus and subunit vaccines" J. Biol. Stand. 1977, 5(3):237-247).

Figure 4 presents the SRID analysis performed on samples collected at day 1, day 2, day 3 and day 4 post- infection and obtained with the former process of influenza virus production in EB66 cells (Figure 4A) and the glucose fedbatch process using concentrated medium (Figure 4B). The volumetric haemagglutimn (HA) productivity value is enhanced with the elevation of the EB66 biomass at time of infection. EXAMPLE 3: GLUCOSE FEDBATCH PROCESS USING CONCENTRATED MEDIUM FOR A A/H3N2/WISCONSIN INFLUENZA VIRUS STRAIN PRODUCTION IN SHAKEN ERLENMEYER

3.1 - Former standard process of production of A/H3N2/Wisconsin influenza virus strain

The standard process described in Example 2.1 was run with this second A/H3N2/Wisconsin influenza virus strain. The maximum viable cell density obtained is approximately 8 million cells/ml.

3.2 - Glucose Fedbatch process using concentrated medium for the production of A/H3N2/Wisconsin influenza virus strain

EB66 cells (passage pl42) were seeded in shaken Erlenmeyers (250 ml) in ExCELL EBx GRO-I medium supplemented with 2.5 mM glutamine at day 0 at a cell concentration of 0.5x10exp6 cells/ml. EB66 cells were grown as a batch culture in a fixed volume until the day 3 when the glucose fedbatch was initiated.

The infection with A/H3N2/Wisconsin influenza virus (multiplicity of infection 10^"4 TCID50/cell) was performed at day 5 post seeding when the EB66 cells almost reached maximum viable cell density (approx. 15 million cells/ml).

A glucose fedbatch either at lOg/1 or 15g/l, a glutamine fedbatch at 2.5 mM and a daily addition of ExCELL EBx GRO-I medium 4X concentrated medium are initiated at day 3, in order to reach maximum vessel volume at day 7 post infection. The formulation of 4X concentrated ExCell EBx GRO-I medium was obtained by a 4 fold increase of the concentration of each component of ExCELL EBx GRO-1 medium, except the components which are involved in, or act on, the osmotic pressure and/or the osmolality, such as salts and buffering agents, which are IX concentrated in the 4X concentrated ExCell EBx GRO-I medium.

No major difference in the maximum viable cell density (i.e 20 million cells/ml at day 4 post-infection) is observed when performing a glucose fedbatch at 10 or 15 g/1 (Figure 5). 3.3 - Production of A/H3N2/Wisconsin Haemaggutinin

The concentration of influenza haemagglutinin in the cell culture medium was determined by the SRID method as described by Wood et al..

Figure 6 presents the SRID analysis performed on samples collected at day 1, day 2, day 3, day 4 and day 5 post-infection and obtained either with the standard process of influenza virus production in EB66 cells or the glucose fedbatch process (10 g/1 and 15g/l) using concentrated medium.

The volumetric haemagglutinin (HA) productivity value obtained in 250 ml Erlenmeyers with the glucose fedbatch process (10 g/1 and 15g/l) using concentrated medium is much higher (approx. 80 μg/ml of HA) than the one obtained with standard process (approx. 30 μg/ml of HA).

The glucose fedbatch process using concentrated medium allows to get robust cell culture of EB66 cells that reach high viable cell density (i.e 20 million cells/ml at day 4 post- infection). The increase of biomass at time of infection with the glucose fedbatch process using concentrated medium, allows to get higher haemagglutinin (HA) productivity compared to the standard process.

EXAMPLE 4: GLUCOSE FEDBATCH PROCESS USING CONCENTRATED MEDIUM FOR A/H3N2/WISCONSIN INFLUENZA VIRUS STRAIN PRODUCTION IN 2L-STIRRED TANK BIOREAC TOR

4.1 - Former standard process of production of A/H3N2/Wisconsin influenza virus strain The standard process described in Example 2.1 was run with this second A/H3N2/Wisconsin influenza virus strain. The maximum viable cell density obtained is approximately 10 million cells/ml (Figure 7A). 4.2 - Glucose Fedbatch process using concentrated medium for the production of A/H3N2/Wisconsin influenza virus strain

EB66 cells (passage pi 42) were seeded in 2L-Bioreactor in ExCELL EBx GRO-I medium supplemented with 2.5 mM glutamine at day 0 at a cell concentration of 0.5x10exp6 cells/ml. EB66 cells were grown as a batch culture in a fixed volume until the day 3 when the glucose fedbatch was initiated.

The infection with A/H3N2/Wisconsin influenza virus (multiplicity of infection 10^"4 TCID50/cell) was performed at day 4 post seeding when the EB66 cells almost reached maximum viable cell density (approx. 22 million cells/ml).

A glucose fedbatch either at 8 g/1, a glutamine fedbatch at 2.5 mM and a daily addition of ExCELL EBx GRO-I medium 4X concentrated medium are initiated at day 3, in order to reach maximum vessel volume at day 6 post infection (Figure 7B).

4.3 - Production of A/H3N2/Wisconsin Haemaggutinin

Figure 8 presents the SRID analysis performed on samples collected at day 1, day 2, day 3, day 4, day 5 and day 6 post-infection and obtained either with the standard process of influenza virus production in EB66 cells or the glucose fedbatch process (8 g/1) using concentrated medium.

The volumetric haemagglutinin (HA) productivity value obtained in 250 ml Erlenmeyers with the glucose fedbatch process (8 g/1) using concentrated medium is much higher (approx. 100 μg/ml of HA) than the one obtained with standard process (approx. 30 μg/ml of HA).

The glucose fedbatch process using concentrated medium allows to get robust cell culture of EB66 cells that reach high viable cell density (i.e 25 million cells/ml at day 4 postinfection). The increase of biomass at time of infection with the glucose fedbatch process using concentrated medium, allows to get higher haemagglutinin (HA) productivity compared to the standard process. EXAMPLE 5: FEDBATCH PROCESS DEVELOPMENT

5.1 Screening of concentrated media

EB66 cells expressing a human IgGl antibody were seeded in shaken Erlenmeyers (250 ml) at day 0 at a cell concentration of 0.4x10⁶ cells/ml, in 50 mL of a serum- free medium, CDM4PerMab (Hyclone) + 2,5mM glutamine. EB66 cells were grown as a batch culture in a fixed volume until the day 3 when the feeding was initiated.

The fedbatch protocol included the daily addition of ExCELL EBx GRO-I medium (SAFC) either 2X concentrated (Grol 2x) or 4X concentrated (Grol 4x) up to final volume of 100 mL. In particular, a given volume of the concentrated medium feed was added according to glucose consumption to maintain a glucose level of 6g/L. Concentrated medium feeds were added in day 3 and day 4, reaching the maximum volume of the Erlenmeyer. Afterwards, glucose and glutamine feeds were added in a daily basis to maintain a concentration of 6g/L and 2.5mM, respectively up to a cell viability equal or lower than 40%. A glutamine fedbatch is carried out at 2,5mM since day 3.

The formulation of 2X or 4X concentrated ExCell EBx GRO-I medium was obtained by a 2 fold or 4 fold increase, respectively of the concentration of each component of ExCELL EBx GRO-1 medium, except the components which are involved in, or act on, the osmotic pressure and/or the osmolality, such as salts and buffering agents, which are IX concentrated.

A standard batch process was run in parallel which consisted in seeding the EB66 cell line in shaken Erlenmeyers (250 ml) at day 0 at a cell concentration of 0.4x10⁶ cells/ml in lOOmL of CDM4 (Hyclone) medium + 2,5mM glutamine and then, growing the EB66 cells as a batch culture in a fixed volume, without the addition of nutrient feed until the end of the kinetics. The quantification of the antibodies in the culture supernatant was performed by the ELISA method using a commercial kit for the detection of human IgG antibodies (FastELlSA, RD biotech, France), according to the manufacturer instructions. Cell density and viable cells determination was performed by classic trypan blue exclusion using a Malassez cell counting chamber. Figure 9 shows the cell density and IgG production results obtained using a standard batch process of IgGl monoclonal antibody in EB66 cells, referred as "CDM4 Batch" and those obtained with the above described fed-batch process protocol comprising a first step of batch culture using a CDM4 (Hyclone) medium as seeding media and a second step comprising the use of 2 fold or 4 fold ExCELL EBx GRO-I medium (SAFC) concentrated medium, referred as "CDM4/GroI 2x" and "CDM4/GroI 4x" respectively.

On the one hand, the obtained results show that the fed-batch process of the invention allows a 4.5 fold and a 1.6 fold increase for the 4x and the 2x concentrated media, respectively, in monoclonal antibody production yield compared to the regular batch process. Similar results were obtained using other cell producing clones.

On the other hand, Figure 9 also shows that EB66 cells reached a maximum viable cell density of about 30 million cell/mL. Furthermore, in a fed-batch process of the invention, monoclonal antibody producing EB66 cells have longer cell viability in comparison with a batch production process (results not shown).

It is to be noted that the use of a culture medium 4 fold concentrated in the fed-batch steps did not negatively affect the quality of the antibodies, namely degradation, glycosilation profile, etc. (results not shown).

5.2 Screening of concentrated glucose feed

Further to the selection of a 4x concentrated culture medium (i.e. GROI 4X) as the optimal culture medium for the fed-batch steps of the bioproduction procedure, the glucose fedbatch was also optimized.

The fed-batch protocol included the daily addition of ExCELL EBx GRO-I medium (SAFC) 4X concentrated (Grol 4x) up to final volume of 100 mL. In particular, a given volume of the concentrated medium feed was added according to glucose consumption to maintain a glucose level of 6g/L. Concentrated medium feeds were added in day 3 and day 4, reaching the maximum volume of the Erlenmeyer. Afterwards, glucose and glutamine feeds were added in a daily basis up to a cell viability equal or lower than 40%. A glutamine fed-batch is carried out at 2,5mM since day 3. To test the effects of glucose concentration in cell density as well as in IgG production, glucose feeds were added to maintain a concentration of 6g/L, 8g/L and lOg/L, respectively, to the end of the kinetics.

As in 5.1., the ELISA method was used for the quantification of the IgGl antibody production and cell density and viable cells determination was performed by classic trypan blue exclusion using a Malassez cell counting chamber.

The results provided in Figure 10, show that the concentration of glucose in the culture medium had an impact both in cell density and IgG antibody production, best results were obtained when the glucose concentration was maintained at lOg/L during the fed-batch process.

Figure 11 shows the metabolic profile of EB66 cells clones further to the fed-batch process with Grol 4X on day 3 and day 4 and with glucose stock solution at a final concentration of 10g/L since day 5 to the end of kinetics. A glutamine Fed-batch is carried out at 2,5mM since day 3. It should be noted that no accumulation of inhibitory metabolites, such as lactate or ammonia was observed.

Claims

A process for the fed-batch culture of animal cells comprising the steps of:

a) growing the cells in a cell growth medium, optionally supplemented with defined supplements, in a culture volume corresponding to a maximum of 75% of the maximum vessel volume, to a cell density greater or equal to 4 million cells/ml; and wherein said process comprises the steps of:

b) performing a fed-batch culture by feeding the culture with a concentrated cell culture medium and/or at least one source of carbohydrate and/or glutamine, until the culture volume reaches the maximum vessel volume; and then

c) optionally, adding marginal volume of at least one compound selected among one source of carbohydrate as an energy source and a solution of one or more amino-acids.

The process according to claim 1 wherein animal cells are selected among duck cell lines.

The process according to any of claims 1 to 2 wherein the cell density at step a) is greater or equal to 10 million cells/ml, more preferably greater or equal to 15 million cell/ml, and even more preferably greater or equal to 20 million cell/ml.

The process according to any of claims 1 to 3 wherein the sugar is glucose and wherein the glucose concentration in the cell growth medium is maintained by fed- batch at a final concentration of at least 8 g/1.

The process according to any of claims 1 to 4 wherein the glutamine concentration in the medium is maintained by fed-batch at a final concentration of about 2.5 mM.

The process according to any of claims 1 to 5 wherein the cell density at the end of step b) is above or equal to 25 million cells/ml.

7. The process according to any of claims 1 to 6 wherein the maximum vessel volume is reached at day 6 post vessel seeding.

8. The process according to any of claims 1 to 7 wherein said process lasts less than 15 days.

9. The process according to any of claims 1 to 8 for the production of a recombinant protein, wherein said animal cells are genetically modified to express said recombinant protein, and wherein said process comprises the additional and final step of harvesting said recombinant protein from the nutrient medium.

10. The process according to claim 9 wherein said recombinant protein is a monoclonal antibody.

11. The process according to any of claims 1 to 8 for the production of virus in said animal cells, wherein said process comprises the additional step of infecting the culture of animal cells with said virus, and wherein the infection step is carried either during step a), between step a) and b) or during step b).

12. The process according to claim 11 wherein the infection step is carried during step b).

13. The process according to any of claim 11 and 12 wherein the virus is selected among naturally occurring viruses, attenuated viruses, reassortant viruses, recombinant viruses and viral vectors.

The process according to any of claim 11 to 13 wherein the virus is selected from the group consisting of adenoviruses, hepadnaviruses, herpes viruses, orthomyxoviruses, papovaviruses, paramyxoviruses, picornaviruses, poxviruses, reoviruses and retroviruses.

The process according to any of claims 11 to 14, wherein the concentrated culture medium added in step b) is a 4X concentrated culture medium, optionally supplemented with glucose and/or glutamine and step c) comprises the addition of glutamine feeds, to maintain a concentration of 2.5 mM of glutamine and the addition of glucose feeds to maintain a concentration above 8 g/1, preferably a glucose concentration of 10 g/1.