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Biochemistry, Genetics and Molecular Biology » "New Insights into Cell Culture Technology", book edited by Sivakumar Joghi Thatha Gowder, ISBN 978-953-51-3134-2, Print ISBN 978-953-51-3133-5, Published: May 10, 2017 under CC BY 3.0 license. © The Author(s).

Chapter 3

The Challenge of Human Mesenchymal Stromal Cell Expansion: Current and Prospective Answers

By Christiane Elseberg, Jasmin Leber, Tobias Weidner and Peter Czermak
DOI: 10.5772/66901

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General overview of a dynamic production process for hMSCs including various aspects that influence the final product quality.
Figure 1. General overview of a dynamic production process for hMSCs including various aspects that influence the final product quality.
Schematic drawing of the expansion and harvest process for hMSC‐TERT cells in a 300 mL bed. Peristaltic pumps and hose‐crushing valves ensured process flow and switching. Single‐use oxygen sensors were introduced before and after the packed bed. To avoid carrier settling below the bed, a sieve with a mesh size of 100 µm was inserted at the bottom socket. D1: heating blanket, G1: harvest vessel, G2: buffer vessel, G3: waste vessel, G4: enzyme vessel, G5: reservoir, I1: pH‐probe, I2: pO2‐probe, I3: temperature probe, I4‐I5: pO2‐probe, I6: temperature probe, I7: dielectric spectroscopy, I8: mass determination, K1: measurement chamber, M: motor, P1‐P2: pump, R1: packed‐bed reactor, R2: conditioning vessel, T: water bath for constant temperature, V.1‐V.8: valves, W: balance [39].
Figure 2. Schematic drawing of the expansion and harvest process for hMSC‐TERT cells in a 300 mL bed. Peristaltic pumps and hose‐crushing valves ensured process flow and switching. Single‐use oxygen sensors were introduced before and after the packed bed. To avoid carrier settling below the bed, a sieve with a mesh size of 100 µm was inserted at the bottom socket. D1: heating blanket, G1: harvest vessel, G2: buffer vessel, G3: waste vessel, G4: enzyme vessel, G5: reservoir, I1: pH‐probe, I2: pO2‐probe, I3: temperature probe, I4‐I5: pO2‐probe, I6: temperature probe, I7: dielectric spectroscopy, I8: mass determination, K1: measurement chamber, M: motor, P1‐P2: pump, R1: packed‐bed reactor, R2: conditioning vessel, T: water bath for constant temperature, V.1‐V.8: valves, W: balance [39].
Cell and substrate concentration during hMSC‐TERT expansion in a 300 mL fixed‐bed bioreactor [39]. Model data are based on an initial cell concentration of 1.45 × 107 cell/mL and 0.9 g/L initial glucose concentration using the Euler‐method for first order kinetics.
Figure 3. Cell and substrate concentration during hMSC‐TERT expansion in a 300 mL fixed‐bed bioreactor [39]. Model data are based on an initial cell concentration of 1.45 × 107 cell/mL and 0.9 g/L initial glucose concentration using the Euler‐method for first order kinetics.
Schematic drawing of the expansion process for hMSC‐TERT cells in a 3 L glass STR including a picture of SybrGreen‐stained hMSC‐TERT cells on RapidCell microcarriers; D1: heating blanket, I1: pH probe, I2: pO2 probe, I3: temperature probe, I4: dielectric spectroscopy, M: motor, R: glass stirred tank reactor, V1: valve [39].
Figure 4. Schematic drawing of the expansion process for hMSC‐TERT cells in a 3 L glass STR including a picture of SybrGreen‐stained hMSC‐TERT cells on RapidCell microcarriers; D1: heating blanket, I1: pH probe, I2: pO2 probe, I3: temperature probe, I4: dielectric spectroscopy, M: motor, R: glass stirred tank reactor, V1: valve [39].
Cell density and substrate concentration during hMSC‐TERT expansion in a 3 L glass STR [39]. Model data are based on an initial cell density of 4.24 × 107cell/mL, and 3.5 g/L initial glucose concentration using the Euler method for first order kinetics.
Figure 5. Cell density and substrate concentration during hMSC‐TERT expansion in a 3 L glass STR [39]. Model data are based on an initial cell density of 4.24 × 107cell/mL, and 3.5 g/L initial glucose concentration using the Euler method for first order kinetics.
Detachment of hMSC‐TERT cells using different enzymes for n = 3 measurements each. The cells were grown to confluence in coated or uncoated wells and were detached enzymatically. Cell detachment was analyzed by counting the cells in suspension [35].
Figure 6. Detachment of hMSC‐TERT cells using different enzymes for n = 3 measurements each. The cells were grown to confluence in coated or uncoated wells and were detached enzymatically. Cell detachment was analyzed by counting the cells in suspension [35].

The Challenge of Human Mesenchymal Stromal Cell Expansion: Current and Prospective Answers

Christiane Elseberg1#, Jasmin Leber1#, Tobias Weidner1, 2 and Peter Czermak1, 2, 3, 4
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In the field of cell therapy, allogenic human mesenchymal stromal cells (hMSCs) are often used in clinical trials, creating a demand for cell mass production using efficient dynamic bioreactor systems. As an advanced therapy medicinal product (ATMP), such cells should meet certain special requirements, including product specifications requiring a production process compatible with good manufacturing practice (GMP). The development of processes in which the cells are the product therefore remains a significant challenge. This chapter describes the requirements at different steps in the upstream and downstream phases of such dynamic processes. Potential solutions are presented and future prospects are discussed, including the selection of media and carriers for the strictly adherent growing cells, allowing efficient cell adhesion and detachment. Strategies for dynamic cultivation in bioreactors are described in detail for fixed‐bed and stirred‐tank reactors based on GMP requirements and the integration of process analytical technology (PAT). Following cell harvest, separation and purification, the formulation and storage of the product are also described. Finally, the chapter covers important cell quality characteristics necessary for the approval of ATMPs.

Keywords: hMSC, cell expansion, stirred‐tank reactor, microcarrier, fixed‐bed reactor, PAT, GMP, ATMP, cell harvest, formulation, storage, quality approval

1. Introduction

Intensive research in the field of regenerative medicine has resulted in a large number of clinical trials over the last few years. The unique characteristics and differentiation pathways of human mesenchymal stem/stromal cells (hMSCs) make them promising candidates for future therapeutic strategies. There is a great interest in these cells because they can migrate to injured tissues following implantation or intravenous injection, and they have anti‐inflammatory and regenerative capacity due to the release of cytokines, specific growth factors and other bioactive molecules. In addition to non‐differentiated cells, the differentiation of hMSCs into osteocytes, chondrocytes, adipocytes, tenocytes and muscle cells [1, 2] may allow the treatment of patients with bone and cartilage diseases, gastrointestinal diseases, diabetes, graft‐versus‐host diseases and limbal stem‐cell deficiency [36]. The application of immunomodulatory hMSCs may involve autologous cells (isolated from the patient and used in personalized therapy) or allogenic cells (isolated from another individual, then expanded and used in the patient). Allogenic cells allow off‐the‐shelf treatment for indications affecting a large number of patients. In addition to primary hMSCs, which can be isolated from bone marrow, adipose tissue and the umbilical cord, the genetically modified and immortalized cell line hMSC‐TERT achieves higher passaging numbers while retaining the differentiation potential of primary cells [7, 8]. currently lists 51 clinical trials specifically involving autologous hMSCs, 32 of which are ongoing, whereas 67 studies are listed for allogenic hMSCs, 56 of which are ongoing (accessed May 9, 2016). Since 2005, the number of clinical trials has increased continuously, the majority using allogenic cells [9]. These trials have shown that cell‐dose‐dependent efficacy requires a minimum of 1.5–6 × 107 cells per dose, depending on the indication [10, 11]. Human cells are classed as advanced therapy medicinal products (ATMPs). Only four ATMPs are currently authorized, which may reflect the lack of suitable production processes [12]. This reveals the need for robust and efficient biomass expansion processes for adherent growing hMSCs that yield a high‐quality product. The development of dynamic processes for sensitive, adherent growing cells is challenging because several requirements discussed in this chapter must be fulfilled to mimic in vivo conditions. This article focuses on dynamic processes for primary bone marrow‐derived hMSCs and the hMSC‐TERT cell line for allogenic applications of non‐differentiated cells.

2. Requirements for stem cell expansion

2.1. Cells as a product

In contrast to biopharmaceutical production processes in which the cell synthesizes the product, in the field of cell therapy, the cells are the product. Like any other medical product, cells must be approved by the competent authorities, i.e., the European Medicines Agency (EMA) in Europe or the Food and Drug Administration (FDA) in the USA. Medicines based on genes, cells or tissues are usually defined as ATMPs, a category that includes both hMSCs and the hMSC‐TERT cell line. ATMPs are subject to special guidelines in addition to the standard good manufacturing practice (GMP) requirements. In the EU, such products must be compliant with Regulation 1394/2007, guideline EMEA/CHMP/410869/2006, Directives 2004/23/EC, 2006/17/EC, 2006/86/EC and the revised guideline EMA/CAT/600280/2010. In the USA, such products must be compliant with the FDA Code of Federal Regulations (CFRs) covering investigational new drug (IND) applications (21 CFR 312), biological regulations (21 CFR 600) and GMP (21 CFR 211) [1315]. The International Society for Stem Cell Research (ISSCR) published its updated “Guidelines for Stem Cell Research and Clinical Translation” in May 2016 [16] with commentaries on manufacturing, safety and efficacy to provide standard guidelines and recommendations.

In addition to the regulatory framework, different societies and institutes have listed product characteristics that must be fulfilled [17]. One definition of hMSCs is provided by the International Society for Cell Therapy (ISCT) in their “minimal criteria for defining multipotent mesenchymal stromal cells” [18]. These criteria include the identity of cells, which is characterized by the following cell surface markers: positive expression (>95%) of CD105, CD73 and CD90, and no expression (<2%) of CD45, CD34, CD14 or CD11b, CD79α or CD19 and HLA class II. Also included in the ISCT definition is the adherence to plastic surfaces and the differentiation capacity in vitro into osteoblasts, adipocytes and chondroblasts. These characteristics must be defined and extended specifically for each cell line depending on its source [19].

To meet these regulatory demands and retain the defined cell characteristics, extreme care must be taken during process development in a dynamic system to achieve the highest final product quality. Only a few aspects can be covered in this chapter, showing the complexity of the issue. Figure 1 shows the steps in a general production process including the various aspects that must be addressed.


Figure 1.

General overview of a dynamic production process for hMSCs including various aspects that influence the final product quality.

Different aspects during each step determine the final product quality and process efficiency by affecting cell viability, potency, identity and safety. Each aspect summarized in Figure 1 must also be regarded in the context of GMP, which provides general guidance rather than detailed instruction. Briefly, the processes must ensure the quality of the product at each step and part of the system, as well as the final product. The basic materials should be chemically defined and proven to be within specifications. The quality and purity of all substances must be ensured. Robustness, reproducibility and efficiency must be shown using closed control systems to confirm quality, safety and efficacy throughout the process. The documentation required for each quality‐relevant step is usually completed using standard operating procedures [20]. Process analytical technology (PAT) is one tool that can be used to ensure process quality based on the online and offline monitoring of different parameters [21]. Further examples of GMP include the requirement of animal‐free materials, closed production systems and system validation that confirms the separation of different production processes, favoring disposable equipment. The biological source is one of the major factors that determine process success. The age and health of the human donor as well as the tissue of origin affect cell quality attributes. For both primary hMSCs and hMSC‐TERT cells, the number of passages has a major influence on the final product quality and must be as low as possible [22].

2.2. Process requirements—upstream

2.2.1. Stem cell media

The maintenance of proliferating hMSCs requires special growth media, typically a basal medium comprising salts, glucose, amino acids and a buffer system supplemented with serum. The latter is routinely used because it contains proteins, adhesion factors, vitamins, growth factors, hormones, fatty acids and lipids that promote cell adhesion and attachment (e.g., to collagen, fibronectin, laminin and vitronectin), which is required for in vitro cell proliferation [23]. Important variables include the concentration of each ingredient, and the osmolality, buffering capacity, conductivity, substrate availability and stability (especially thermostability) of the medium. Serum constitutes a risk when hMSCs are produced for clinical applications under GMP and also increases the complexity of downstream processing. Serum should be avoided because it is derived from animals, thus increasing the risk of contamination (e.g., with viruses) and immunogenicity, and its complexity introduces unknown variables that make process standardization difficult to achieve.

To eliminate serum from stem cell production processes, several defined serum‐free formulations have been developed. According to one classification system [24], a “defined medium” can be further divided into the following categories:

  • Serum‐free medium (SFM) containing a broad range of supplementary hormones, growth factors, proteins and polyamines, derived from bovine or human sources

  • Protein‐free medium (PFM) containing peptide fragments from enzymatic or acid hydrolysis of animal or plant source proteins

    • PFM variant A containing human serum albumin, human transferrin, human insulin and animal‐derived lipids

    • PFM variant B, also known as xeno‐free medium (XFM) containing human serum albumin, human transferrin, human insulin and chemically defined lipids

  • Recombinant xeno‐free medium (recXFM) containing either recombinant proteins, hormones and compounds or chemically defined lipids

  • Chemically defined medium (CDM)—a protein‐free basal medium containing low‐molecular‐weight components, synthetic peptides or hormones, and a few recombinant or synthetic versions of proteins.

In‐house serum‐free media for hMSCs have been reported in several studies, often containing additional factors such as bovine/human serum albumin, insulin, transferrin, hormones (e.g., progesterone, hydrocortisone and estradiol), growth factors (e.g., bFGF, TGFβ, EGF or PDGF) or heparin [2528]. The list of commercially available chemically defined, protein‐free, xeno‐free and serum‐free is constantly increasing [29] as discussed in recent reviews [30, 31].

2.2.2. Growth surfaces

The characteristics of the growth surface have a major impact on the cultivation of hMSCs, especially in the context of production processes. The attachment, spreading and proliferation of these adherent cells are strongly influenced by the growth surface and the corresponding cell‐surface interactions. These interactions can induce signaling pathways that are involved in regulating important cellular processes including cell migration, gene expression, cell survival, tissue organization and differentiation [3234].

In dynamic bioreactor systems for adherent cells, microcarriers provide the growth surface in suspension or as a bed. The choice of an appropriate microcarrier, which not only supports attachment and growth but also allows efficient detachment without losing viability, is one of the key design aspects of an hMSC production process. For large‐scale processes, bead‐to‐bead transfer strategies are necessary and should be promoted by the microcarrier. Several microcarrier types are commercially available, and a suitable microcarrier must be selected for each application by considering a combination of factors based on the following list of properties:

  • geometry, size and size distribution, porosity, physical density

  • GMP compliance

  • mechanical stability, autoclavable or sterile delivery

  • core and surface material (glass, polystyrene, gelatin, dextran, protein or synthetic protein fragments), source, surface characteristics (charge, stability, transparency, attachment and harvest, thermosensitivity)

  • compatibility with downstream processing

Some commercially available microcarriers have been developed to improve cell attachment using new synthetic or natural materials, whereas others are optimized for the specific harvest requirements of hMSCs [35]. Nonporous microcarriers are most suitable for hMSC expansion and harvest because successful detachment with high viability is difficult to achieve using porous microcarriers [36].

2.2.3. Cell expansion in bioreactors

The reproducible, cost‐efficient, scalable and automated production of hMSCs in a dynamic, three‐dimensional system is best achieved using microcarriers because they allow controlled inoculation, expansion and cell harvest with the system remaining closed [37]. According to PAT requirements, control loops should include for example pH, temperature, stirrer speed or flow rate, aeration and feeding rate. Online process monitoring is necessary to ensure quality throughout the process, e.g., cell density, media properties (pH, temperature, pO2 and pCO2) and the concentration of metabolites such as glucose, lactate, ammonia and glutamine. The number of parallel systems should be minimized, aiming to achieve a high surface‐volume ratio, which can be realized using systems compatible with microcarrier cultivation. Sterility must be guaranteed by minimizing the contamination risk, and single‐use equipment is an option to achieve this. The system must allow low‐shear oxygenation by internal or external aeration, and a homogeneous nutrient supply, which are also required for PAT. Well‐characterized systems are favorable because they facilitate process validation. Furthermore, the systems should be as simple as possible to avoid errors during system handling.

Several bioreactor types have been described for the expansion of hMSC and hMSC‐TERT cells. The most common are spinner flasks, stirred tank reactors (STRs), wave systems [38], fixed‐bed reactors (FBRs), fluidized bed and wall‐rotating systems [22, 3941] as well as the application of Vertical‐Wheel™ technology [42]. Most published studies describe cell expansion in spinner flasks, but these are difficult to scale up and automate, and the only process control options are pH and oxygen concentration monitoring. Similar drawbacks are associated with wave reactors. The most promising systems are STRs and FBRs. STRs are well‐characterized, scalable and controllable systems that are suitable for automation, whereas FBRs avoid the need for media replacement and also offer the opportunity to combine inoculation, expansion and harvest in one system [4345].

Once the bioreactor system is chosen, the cultivation procedure and process parameters must be defined. The choice of the process mode strongly influences the process parameters, which must be adapted to achieve the defined product specifications [39]. Batch processes are often successful, but fed‐batch processes in STRs are more efficient and can be achieved by the partial addition of media and microcarrier [40, 46]. The microcarrier concentration or bed volume must be chosen in combination with the seeding density, followed by the appropriate inoculation strategy. The seeding density affects cell proliferation, and lower densities (100 cells/cm2) are more suitable than higher densities (5000 cells/cm2) [47], suggesting that a ratio of five cells per bead is optimal [48]. The dispersal of cells on the microcarrier follows a Poisson distribution [49]. Initial seeding densities of 1–3 × 104 cells/cm2 are nearly independent from the available growth surface area. The inoculation strategy is often based on intermittent agitation or flow depending on the system [50, 51].

The rotation speed of a STR is a critical process parameter because the culture should be homogeneous but a low shear stress is necessary to avoid changes to the cell characteristics while at the same time avoiding the formation of bridges between microcarriers by overgrowth [40]. This topic has been reviewed in detail [22, 52]. One solution is to increase the agitation rate during cultivation [53]. The application of a suspension criterion [54] may also facilitate process development and scale‐up, using theoretical process analysis based on power input, microcarrier type and cell growth. Three‐phase systems, such as aerated microcarrier‐based stirred‐tank cultures, show the complex effects of the working volume, carrier concentration and aeration on the power input. Understanding the mixing characteristics of such a system is required to optimize hMSC cultivation [55]. Similarly, for hollow fiber or FBR systems, the flow rate must be defined according to the cell line, microcarrier and system volume [43]. Media exchange is often necessary to avoid nutrient limitation and critical metabolite concentrations [49], but only partial replacement is possible [56] and this increases the risk of contamination.

2.2.4. Cell harvest

Because the cells are the product, adherent hMSCs must be detached and separated from their growth surface. Unlike standard processes, where the cells do not need to be detached, harvest is a very sensitive process step but must still remain cost‐effective and GMP compliant. In static cultures, cell detachment is often achieved using peptidases, usually trypsin (EC, which cleaves peptide chains after most basic amino acids [57]. Cell detachment in dynamic systems is more complex, especially in terms of shear forces. Therefore, the enzyme used to detach cells grown on carriers in dynamic systems must be both gentle and efficient. The molecular basis of cell attachment depends on the microcarrier, so the choice of enzyme for detachment must take this into account. Furthermore, animal‐derived enzymes such as pancreatic trypsin should be avoided [58, 59]. Further aspects that must be addressed include the commercial availability of the enzyme, the final cell density, the incubation time and the temperature. The aim is to maximize the harvest yield and cell viability while maintaining the characteristics of the cells after harvest, processing and formulation.

2.3. Process requirements—downstream

2.3.1. Cell separation, clarification and concentration

After cell detachment, the carrier must be separated from the cells, followed by cell clarification, washing and cell concentration (volume reduction) [60, 61]. For this part of the process, large‐scale applications are still in their infancy. Appropriate methods, such as filtration, must ensure minimal processing time and must be based on inert, single‐use materials. Cell recovery must achieve clarification and volume reduction while preserving cell viability and retaining cell characteristics. Thus, low shear processes are necessary. Impurities must be reduced to levels below 1 ppm. The system should be closed, automated and scalable [62].

For standard biopharmaceutical processes, tangential flow filtration (TFF) [63] is often used for the initial clarification of therapeutic proteins produced in mammalian, bacterial or yeast cell cultures [64]. For the production of ATMPs, TFF processes must be redesigned to meet product quality demands. The filter material, pore size and initial cell concentration, as well as operating parameters such as shear rate and permeate flux, may influence the recovery of viable, high‐quality cells [63]. The impact of shear rate and shear stress on the viability and differentiation potential of hMSCs is well‐characterized [65, 66]. High shear rates are known to reduce membrane fouling during microfiltration [67], so a trade‐off between fouling and cell damage is necessary to achieve a satisfactory hMSC concentration.

2.3.2. Formulation and storage

Allogenic stromal cells should be off‐the‐shelf products available on demand, and appropriate formulation strategies are therefore required allowing the cells to be stored for a specific period of time under defined conditions. Often, allogenic cells are formulated as cell suspensions. Alternative formulations, which prevent immune responses in recipient patients, are cell encapsulation. Inert and biocompatible materials, capsule size and a gentle encapsulation process must ensure that cells retain their viability, identity, purity and differentiation capacity.

The same requirements are relevant to the storage method, including the physical storage form, long‐term product stability/availability and the eventual application of the stored cells to the patient, ideally without prior treatments. The storage form must also fulfill GMP and especially ATMP requirements. One common way to store cell culture and ensure long‐term availability is cryopreservation in liquid nitrogen. Post‐thaw cell survival is sensitive to the freezing and thawing processes, which require cryoprotective agents (CPAs) to prevent the formation of intracellular and extracellular ice crystals that would otherwise expand and destroy cell and organelle membranes [68, 69]. CPAs also minimize osmotic effects that would promote the denaturation of proteins [70]. The nature of the freezing and thawing cycle and the most appropriate CPA must be determined on a case‐by‐case basis for each cell line [71]. A detailed description of the development of cell line‐dependent cryopreservation protocols has been published [72] and the topic has been recently reviewed [73].

A storage system in a GMP environment features a constant temperature in a controlled and monitored environment with a barcode‐based vial‐labelling system. Frequent thawing of the frozen vials and testing according the above‐mentioned aspects are essential to ensure long‐term stability.

3. Stem cell production in dynamic bioreactors

3.1. Media choice

As stated above, animal‐derived raw materials should be avoided and SFM, XFM or preferably CDM should be used for hMSC expansion. Appropriate media are available from several commercial sources (Table 1) and studies published between 2011 and 2015 using these different media for the cultivation of hMSCs have recently been reviewed [74].

Product nameCompanyClassification and comments
(if information available by manufacturer)
The literature
and website
CellGro® MSC MediumCellGenixSFM: albumin (human‐plasma‐derived)insulin (human recombinant, yeast‐derived),
synthetic lipid contains chicken egg‐derived lecithin (licensed medicinal product for human use)
Not cited
Web: [136]
CTS™ StemPro® MSC SFMGibco by Thermo ScientificSFM: coating with CELLstart™ CTS™ necessary[77, 137, 138]
Web: [139]
hMSC High Performance Media Kit XFRoosterBioXFM: standardized, “enriched” basal mediumNot cited
Web: [140]
Human MSC medium, chemically‐definedAmCell BiosciencesrecXFM: components are either chemically synthesized or recombinant produced and purified, none of its ingredients are directly derived from nonhuman animalsNot cited
Web: [141]
Mesenchymal Stem Cell Growth Medium DXF (Defined Xeno Free)PromoCellXFM
fibronectin‐coated plates are necessary
Web: [143]
Mesenchymal Stem Cell Medium—animal component free (MSCM‐acf)ScienCell Research LaboratoriesXFM: no animal‐ or human‐origin materials.
Contains (quantitatively and qualitatively formulated) growth factors, hormones and proteins
Not cited
Web: [144]
MesenCult™‐XF MediumSTEMCELL TechnologiesSFM used in conjunction with the MesenCult™‐SF Attachment SubstrateNot cited
Web: [145]
MesenGro® Human MSC MediumSystem Biosciences/
recXFM: does not contain animal‐derived components, components are either chemically synthesized or recombinantly produced and purifiedNot cited
Web: [146]
MSC NutriStem® XF MediumBiological IndustriesXFM, defined formulation. Use of fibronectin coating is recommended. Drug Master File available[11, 147]
Web: [148]
MSC‐GRO™ Serum‐Free/Xeno‐Free, Complete MediaVitro BiopharmaXFMNot cited
Web: [149]
PowerStem MSC1PAN‐BiotechXFM: free of animal or human serum, without animal derived components, no undefined peptones or hydrolysates, contains hormones, growth factors and enriched human proteins and lipidsNot cited
Web: [150]
PRIME‐XV® MSC Expansion SFMIrvine ScientificSFM: pre‐coated with PRIME‐XV MatrIS F necessary[100, 151]
Web: [152]
SPE‐IV MediaABCell‐BioSFM: animal protein‐free, contains human albumin, synthetic iron carrier, rh‐insulin, nucleosides, α‐monothioglycerol, synthetic lipids, rh‐IGF‐1 and rh‐b‐FGF. Requires the addition of pre‐adhesion molecules such as fibronectin and collagenNot cited
Web: [153]
Stem Cell 1Cell Culture TechnologiesCDM: chemically defined, protein/peptide‐free[35]
Web: [154]
StemMACS MSC Expansion Media Kit XFMiltenyi BiotecXFMNot cited
Web: [155]
StemXVivo Xeno‐Free Human MSC Expansion MediaR&D SystemsXFM
coating with recombinant human fibronectin necessary
Web: [156]
TheraPEAK™ MSCGM‐CD™ Mesenchymal Stem Cell Medium, Chemically DefinedLonzaXFM: contains only constituents of known molecular structure, contains human albumin, recombinant human insulin, pasteurized human transferrin[25, 157, 158]
Web: [159]

Table 1.

Overview of commercially available, SFM and XFM for the cultivation of hMSCs (as of July 2016).

Human platelet lysate has been used as an alternative for bovine serum by several groups, e.g., for umbilical cord‐derived hMSCs [75, 76]. XFM containing a mixture of proteins including human serum albumin and recombinant growth factors was used to expand hMSCs derived from bone marrow (bm‐hMSCs) and adipose tissue on microcarriers [77] and a similar approach with a XFM containing components from human plasma has also been described [78].

A new CDM for hMSC expansion has been described in which each component has a Chemical Abstracts Service (CAS) registration number and none of the components frequently used in XFM formulations are present, such as serum albumin, insulin, transferrin, progesterone, hydrocortisone or estradiol [35]. The absence of attachment‐promoting factors limits the attachment behavior of the hMSCs and the growth surface must therefore be coated with attachment‐promoting substances. To our knowledge, this stem cell 1 medium (Cell Culture Technologies, Switzerland) is the only protein/peptide‐free CDM for hMSC expansion, mainly comprising defined concentrations of low‐molecular weight compounds (50–250 Da, with only one component larger than 1000 Da). The addition of recombinant growth factors in combination with surface coatings makes this medium suitable for the attachment, spreading, growth and detachment of hMSCs derived from different tissues [35].

3.2. Microcarrier choice

Several commercial microcarrier products are available that are suitable for hMSC expansion, as recently reviewed [34]. Microcarriers with surfaces comparable to static tissue culture plastic simplify the transfer of cells from static to dynamic cultivation environments. They have been used successfully for bm‐hMSCs in a 5 L STR [79]. Microcarriers 2–5 mm in diameter are often used for FBR processes, whereas those used in fluidized bed reactors are typically 1 mm in diameter and those used in STRs are generally 100–300 µm in diameter [80]. Glass has been used as a cell culture growth surface for decades [81], and low‐density microcarriers with a copolymer plastic core and a high‐silica glass coating were used for the expansion of hMSC‐TERT in serum‐containing medium [51, 82]. These results are based on a microcarrier choice for the hMSC‐TERT cell line resulting in strong proliferation and a good yield of detached cells for glass and polystyrene microcarriers [36].

Microcarriers should be selected on a case‐by‐case basis. For example, glass‐coated and plastic microcarriers both achieved comparable maximum cell densities (0.91 × 104 and 1.08 × 104 cells/cm2, respectively) for umbilical cord‐derived MSCs expanded in XFM [75] but only the plastic microcarrier achieved an even distribution of cells (75% of carriers occupied after 72 h), which is essential for successful process scale‐up.

Microcarriers coated with extracellular matrix proteins (ECMs) such as collagen can also be used for hMSC expansion [83]. The ECM components encourage cell attachment and growth by providing adhesion ligands on the surface. As discussed above, animal‐derived proteins are discouraged because they increase the risk of contamination and the composition is unpredictable, causing a lack of reproducibility. Microcarriers are therefore coated with synthetic protein fragments. For example, Synthemax microcarriers (Corning) achieved yields and metabolite profiles in bm‐hMSC cultures that were comparable to collagen‐coated microcarriers [84]. They are suitable for XFM applications [78], as are microcarriers with plasma‐treated plastic surfaces that show improved hydrophilicity and wettability to encourage cell attachment [85].

3.3. Stem cell expansion

The following sections focus on the expansion of hMSCs and hMSC‐TERT cells using STR and FBR systems due to the limitations of the other systems described above. We consider PAT applied in STR and FBR systems and the use of disposable bioreactors.

3.3.1. PAT applications

In basic processes, the pH, temperature and oxygen partial pressure are monitored to ensure quality throughout the process. In more advanced processes, the concentrations of cells, substrates and metabolites can also be measured. Online monitoring tools are ideal, but offline data analysis is needed for correlation. The cell density on a microcarrier is often determined offline by cell lysis followed by counting the released nuclei, but this is rather imprecise [86]. Alternatively, an intercalating fluorescent dye such as SybrGreen I can be used to estimate DNA levels, which are linearly related to the cell density, and this can be achieved without cell detachment [86]. Dielectric spectroscopy is a promising tool for the online measurement of cell density [21, 86, 87]. At a frequency of 300 kHz, there is a linear correlation between the permittivity and the cell density up to 5 × 104 cells/cm2 (∼80% confluence). This is sufficient because cell confluence should not be reached. The cell adhesion process can be monitored analyzing the critical frequency. As the cell volume changes during adhesion, the critical frequency declines and remains almost constant throughout the exponential growth phase. When monitoring a process limitation such as oxygen depletion, the permittivity of the cells changes and this is clearly shown in the signal [39, 86]. If the introduction of a probe is not possible (e.g., in FBR processes), the cell density can be determined indirectly, e.g., by calculation from the oxygen or substrate consumption. Mid‐infrared spectroscopy combined with multivariate data analysis is another promising online tool to optimize process monitoring for spinner cultures, particularly in the context of process prediction, contamination risks, speed and economic modeling. An optimized partial least squares regression model has been used to estimate glucose, lactate and ammonia concentrations [88].

3.3.2. Fixed‐bed reactor

FBR systems can be automated, but it is not possible to take samples, so the cell density is determined indirectly by measuring glucose or oxygen consumption. The homogeneity and scalability of FBR systems remain challenging despite intensive development work by Weber and colleagues [43, 44, 89, 90] and by Elseberg [39]. In bed volumes of 14–300 mL, 2 mm diameter solid glass carriers [91] were successfully used to cultivate hMSC‐TERT cells in Eagle's minimal essential medium (EMEM) with serum. The inoculation strategy was 4 × 30 min for each 7 min with 2 × 104 cells/cm2 at a superficial velocity of 0.48 cm/min, achieving an inoculation rate of 50%. During expansion, the superficial velocity was 1.6 cm/min. Process monitoring involved online oxygen measurement (>60%) as well as pH (7.4) and temperature (37°C) control in the conditioning vessel. The system was integrated into a process control system (Figure 2).


Figure 2.

Schematic drawing of the expansion and harvest process for hMSC‐TERT cells in a 300 mL bed. Peristaltic pumps and hose‐crushing valves ensured process flow and switching. Single‐use oxygen sensors were introduced before and after the packed bed. To avoid carrier settling below the bed, a sieve with a mesh size of 100 µm was inserted at the bottom socket. D1: heating blanket, G1: harvest vessel, G2: buffer vessel, G3: waste vessel, G4: enzyme vessel, G5: reservoir, I1: pH‐probe, I2: pO2‐probe, I3: temperature probe, I4‐I5: pO2‐probe, I6: temperature probe, I7: dielectric spectroscopy, I8: mass determination, K1: measurement chamber, M: motor, P1‐P2: pump, R1: packed‐bed reactor, R2: conditioning vessel, T: water bath for constant temperature, V.1‐V.8: valves, W: balance [39].

Offline measurements of glucose and lactate concentrations were used to determine the cell density. Partial media replacement was carried out at glucose concentrations below 0.4 g/L. Expansion was defined as complete at a cell density of 5–5.5 × 104 cells/cm2. Analysis of residence time in the 300 mL reactor during cultivation clearly showed an inhomogeneous cell distribution, which caused an altered flow profile [39]. Shear stress (1.74 × 10-6 N/cm2) was below the critical value of 1.5 × 10-4 N/cm2 [66]. In summary (Figure 3), cultivation for 8 days, starting with 1.2 × 104 cells/cm2, achieved a final cell density of 6.3 ± 0.86 × 104 cells/cm2 (total per batch of approximately 3.16 × 108 cells for 5500 cm2) at an average growth rate of 0.27 d-1 [39]. Complex models and scale‐up considerations have been published [44]. Monod‐based models showed that the glucose uptake rate, and therefore the cell density calculation, depends on the number of passages and the scale. The system could potentially be improved to achieve a more homogeneous cell distribution by optimizing the inoculation strategy.


Figure 3.

Cell and substrate concentration during hMSC‐TERT expansion in a 300 mL fixed‐bed bioreactor [39]. Model data are based on an initial cell concentration of 1.45 × 107 cell/mL and 0.9 g/L initial glucose concentration using the Euler‐method for first order kinetics.

Placenta‐derived hMSCs have been cultivated in a scalable packed‐bed reactor in which the 13 mL bed was encased within a gas‐permeable shell for indirect aeration and nutrient supply [92]. This achieved a low shear of 9.5 × 10-5 Pa at a flow rate of 5 mL/d. The growth surface (160 cm2) was provided by air plasma‐treated polystyrene pellets endowed with a surface chemistry similar to tissue culture plastic. A 10‐fold expansion of initially 1 × 104 cells/cm2 in Dulbecco's modified Eagle's medium (DMEM) with serum was achieved after 1 week in culture, and the cells retained their differentiation capacity. Even so, cell growth in the packed bed culture was slower than growth in static two‐dimensional cultures. Inoculation was performed by rolling the column at 5 rpm for 5 min then resting for a period of 3 h. The cell density was determined by AlamarBlue staining, which caused cell disruption. The system was shown to be scalable and suitable for the automated cultivation of murine MSCs to a volume of 235 mL and a growth surface of 2800 cm2 and therefore appears suitable for hMSC expansion [92].

3.3.3. Stirred tank reactor

Intensive work on the development of a hMSC‐TERT batch process in a 3 L glass STR with a working volume of 1.65 L was described by Elseberg and colleagues, and the cell characteristics were retained [39, 51]. The sterilized bioreactor (Figure 4) was filled with the sterile glass‐surface microcarrier RapidCell [36] at 25 g/L suspended in high‐glucose DMEM supplemented with 10% serum [51]. Cell suspensions were introduced by a syringe at a density of 7 × 103 cells/cm2 in four cycles, comprising 45 min without stirring and 2 min with stirring at 120 rpm [51]. The process parameters pH (7.4), temperature (37°C) and pO2 (<60%) were monitored online, the cell density determined by dielectric spectroscopy. The fluorescence‐based assay described above was used offline to determine cell density, combined with microscopy. During expansion, the rotation speed was increased stepwise from 120 to 160 rpm at 10‐rpm intervals for every 1.2 × 104 cells/cm2 [51]. The cultivation data confirmed that the cell density, substrate consumption and metabolite production were reproducible, and critical values of lactate and ammonia concentrations were not observed. In summary (Figure 5), after 6 days of cultivation, starting at 7 × 103 cells/cm2, a final cell density of 4.5 × 104 cells/cm2 was achieved (equivalent to ∼6.84 × 108 cells for a surface of ∼13,600 cm2) with an average growth rate of 0.32 d-1 in three replicate cultivations [39]. The detailed protocol has been published [93]. Optimization studies should consider bead‐to‐bead transfer as a stepwise fed‐batch process to reduce costs. Furthermore, the online analysis of glucose and lactate would be beneficial. The detailed analysis of each step may also allow the process to be adapted for primary cells.


Figure 4.

Schematic drawing of the expansion process for hMSC‐TERT cells in a 3 L glass STR including a picture of SybrGreen‐stained hMSC‐TERT cells on RapidCell microcarriers; D1: heating blanket, I1: pH probe, I2: pO2 probe, I3: temperature probe, I4: dielectric spectroscopy, M: motor, R: glass stirred tank reactor, V1: valve [39].


Figure 5.

Cell density and substrate concentration during hMSC‐TERT expansion in a 3 L glass STR [39]. Model data are based on an initial cell density of 4.24 × 107cell/mL, and 3.5 g/L initial glucose concentration using the Euler method for first order kinetics.

One of the larger‐scale processes for hMSC production (2.5 L in a 5 L STR) [79] required a cultivation time of 12 days to achieve a cell density of 1.7 × 105 cells/mL. The culture conditions were pH 7.2–6.7 at 37°C and pO2 >45%. This allowed a sixfold expansion while retaining cell characteristics. Oxygenation only occurred during 50% media exchange every second day after day 3. The inoculation density was 6 × 103 cells/cm2 on plastic‐surface microcarriers (P102L by Solohill), which is equivalent to ∼5 cells/bead. The static culture with a down‐pumping impeller was run in static mode for 18 h at 75 rpm to ensure that all microcarriers were distributed evenly throughout the reactor, resulting in better cell growth compared to spinner cultures. The authors found that homogeneity could be achieved with less power input compared to the spinner cultures. Optimization was required in terms of pH and oxygen control, as well as monitoring the cell density to determine the point of confluence during the process.

A further process has been described for hMSCs in a 1.3 L working volume STR [94]. The expansion processes differed according to the source of the hMSCs, such as umbilical cord matrix‐derived hMSCs (UCM‐hMSCs), highlighting the need for tailored process development. The cultivation of UCM‐hMSCs was recently demonstrated using gelatin‐based microcarriers and XFM in a controlled STR culture with a working volume of 800 mL [41]. To increase process efficiency, an automated continuous process (e.g., without intervention for media replacement) was developed based on continuous perfusion in a STR and the cells retained their differentiation capacity [95]. Starting with 0.25 × 105 cells/mL in 400 mL at 40–60 rpm in Mesencult™‐XF media, continuous perfusion was carried out including a cell retention device, such as the ATF‐System for microcarriers by Repligen Corporation, with dilution rates of 0.2 d-1 starting on day 5, or a dip‐tube adapter attached to the bioreactor cap. Inoculation was achieved by intermitted stirring on Synthemax II microcarriers at 16 g/L. This resulted in higher cell densities of 3.7 × 105 cell/mL (expansion ratio = 14.6) and growth rates of 0.016 h-1. No media depletion was observed, and inhibitory substances such as lactate and ammonia remained below critical values of (<6 and <1 mM, respectively [50]). Bead‐to‐bead transfer was further shown to increase process efficiency by the addition of empty microcarriers on day 6 [78].

Single‐use technology is appropriate for economic reasons and to meet GMP requirements because this eliminates the risk of cross‐contamination and facilitates the validation and qualification of the system. The first disposable STR used for the expansion of hMSCs on microcarriers was the Mobius® 3 L bioreactor by Merck‐Millipore with 2.4 L working volume, which yielded ∼600 million hMSCs on collagen‐coated polystyrene microcarriers [83, 96]. The cells retained their basic defining characteristics, i.e., cell surface marker expression and differentiation potential. The cultivation of hMSCs over 12 days in this system was compatible with bead‐to‐bead transfer. This increased the expansion factor to 62‐fold, six time higher than a normal batch process, achieving a yield of 49,750 cells/cm2. Starting with a growth surface of 5400 cm2, the addition of media and microcarrier after 7 days increased this to 10,800 cm2 (+1 L) and 12,960 cm2 on day 11 (+0.4 L) until the end of the process. This process involved non‐cycling inoculation at 35 rpm. During cultivation, the stirrer speed was increased from 55 to 75 rpm and minimal aggregate formation was observed [46]. The mixing characteristics of this three‐phase system showed a certain degree of inhomogeneity, but this was beneficial because the cells were allowed rest phases of low shear stress [55].

The transfer of a process for hMSC‐TERT cells from a geometrically similar glass STR to the single‐use Mobius® 3 L bioreactor has also been described [51]. All parameters were kept constant except the stirrer speed, which was reduced to 60–90 rpm, achieving a 6.9‐fold expansion and comparable growth rates to the glass STR. Even so, carrier aggregation was observed, indicating nonoptimal culture conditions [46]. Other systems include the 1.3 L Bioflo® by Eppendorf for the production of 1.4 × 105 cells/mL, which is also available as a single‐use device [77]. The UniVessel® by Sartorius for hMSC cultivation can produce up to 1.8 × 105 cells/mL in a maximum volume of 2 L [22]. The cell density can be increased by up to three‐fold by reducing shear forces, which can be achieved by changing the impeller blade angle from 30° to 45°, reducing the off‐bottom clearance from 0.411 to 0.26 and increasing the microcarrier density. To our knowledge, the largest volume for hMSC expansion used the BIOSTAT® CultiBag STR 50 L with 5% serum‐supplemented stem cell media by Lonza [22, 54]. Inoculation was implemented during a 4‐h cell attachment phase in 20 L of medium‐containing equilibrated gelatin microcarriers, and the bag was then transferred to the CultiBag STR 50 L starting with a 35 L working volume. The process conditions were 37°C, pO2 >20%, maximum air flow rate of 0.03 vvm, pH 7.2–7.3 and the impeller speed was set to 50–66 rpm. The peak viable cell density was 7.2 × 105 cells/mL, with an expansion factor of 51.5 ± 4.9.

3.4. Cell detachment

As described in Section 2.2, enzymatic cell detachment is often a crucial step for the successful production of hMSCs. Researchers often use recombinant trypsin for process development, but there is an intensive ongoing search for alternatives, mostly studied using static cultures [82]. Here, we discuss the harvesting procedure for the dynamic systems described above and then consider alternatives based on studies using static cultures.

Studies reported by Weber [89] and Salzig and colleagues [82] have shown how cells can be harvested from a FBR system. Success depends on the combination of enzyme choice, incubation time and temperature, and the effects of downstream processing and formulation [82]. After flushing the reactor twice with phosphate buffered saline (PBS), harvesting was carried out by incubating the cells with TrypZean for 15 min at 21°C and cells were flushed out of the reactor with media (37°C) at a superficial velocity of 19 cm/s. The yields were not reproducible due to the inhomogeneous cell and enzyme distribution, and the highest yield was 82.1 ± 2.3%. The final cell density had a strong impact the cell harvest yield. Based on transport limitations, higher cell densities reduced the viability of the cells from 80–90% to 50% [39].

In a glass STR process [39, 46, 51, 93], a partial cell harvest of 300 mL was achieved using a sieve with a mesh size of 100 µm to separate the carriers with the cells from the media. The carriers were then rinsed with PBS and the entire sieve was transferred into a dish containing trypsin solution for incubation at room temperature for 10 min. Detached cells were rinsed off with serum‐containing media. This method achieved a consistent high harvest yield with >95% cell viability. The viability, metabolic activity (determined with water‐soluble tetrazolium salt) and adipogenic differentiation capacity of the cells were comparable to cells from static cultures in T‐flasks, whereas cell growth of re‐cultured cells was slightly slower.

A potentially scalable harvesting method has been developed to recover hMSCs from a 5 L STR with a working volume of 2.5 L, based on studies in spinner flasks with plastic‐surface microcarriers [97]. The duration of the incubation step in trypsin‐EDTA was limited to 7 min and combined with agitation (150 rpm) so that Eddy sizes exceeded the cell size. The harvest efficiency was >95% with a viability of 98%, and cells retained their characteristics [18]. Cell harvest from a 5 L STR would normally require 8–9 min incubation with the enzyme and agitation at 120 rpm. Further studies are required to optimize the incubation time, taking into account carrier‐carrier effects, carrier density and the cell density prior to the harvest [97]. Other groups use the nonmammalian trypsin TrypLE for the detachment of hMSCs [94, 97100] on cationic polystyrene charged microcarriers, which achieves high cell quality even in cultures based on SFM [63, 100].

A promising and safer alternative to trypsin is the prolyl‐specific peptidase (PsP) expressed natively and isolated from the fungus Wolfiporia cocos [58]. Allogenic hMSC‐TERT cells were detached more rapidly with 1.6 U/mL PsP than trypsin, and the new enzyme also showed less severe effects on the growth and metabolism of re‐cultivated cells. The optimal harvest yield was achieved by incubating the cells in PsP for 20 min.

Studies using static cultures have shown that the choice of the enzyme must be considered in combination with the growth surface coating and the type of medium for each cell type on a case‐by‐case basis [35]. The authors compared the detachment of hMSCs and hMSC‐TERT cells with trypsin, Accutase, collagenase and PsP when the cells were grown on untreated surfaces, or surfaces coated with collagen or fibronectin, combined with CDM or serum‐containing media (SCM). These different conditions had a significant impact on the detachment of hMSC‐TERT cells but little impact on primary hMSCs, although the detachment of hMSCs was slightly less in the absence of coatings (Figure 6). All detached cells remained highly viable [35].


Figure 6.

Detachment of hMSC‐TERT cells using different enzymes for n = 3 measurements each. The cells were grown to confluence in coated or uncoated wells and were detached enzymatically. Cell detachment was analyzed by counting the cells in suspension [35].

For gelatin‐based microcarriers, the total digestion of the microcarrier is possible using trypsin, yielding a single‐cell suspension. Although this removes the need for cell‐carrier separation, a longer incubation time is necessary which can change the immunophenotype of the cells, but this can be reverted during re‐cultivation in static cultures [41].

A promising alternative is the use of thermosensitive microcarriers to avoid the need for enzymatic cell detachment. Various materials have been tested, i.e., poly‐N‐isopropylacrylamide, and recently, a successful application has been reported in dynamic systems [101103]. Although proteolytic enzyme treatment is not necessary, mechanical forces are still required to achieve a single cell suspension, as cell‐cell‐contact is not dissociated due to the temperature shift [104]. Future research in this area could offer a replacement for the gold standard of cell detachment with trypsin or its derivatives, particularly if combinations of enzymes and functional surfaces are considered.

3.5. Separation, clarification and concentration

Until recently, the scalable harvesting of hMSCs has received little attention [63, 97]. The separation of single cells from the carrier in STR systems can be achieved by dead‐end filtration [63, 97, 100]. The pore size of the polystyrene filters must be >75 µm to maintain cell viability and quality because hMSCs fall within the size range 15–20 μm, whereas the microcarriers are 125–212 μm [63]. Cells could also be harvested directly from a disposable STR by inserting a sieve [46]. Commercially available systems for cell‐carrier separation in general have been reviewed, and the authors also suggest the option of continuous flow centrifugation, which is available as a closed, single‐use device that can handle approximately 250 L of culture with 15 g/L of microcarrier, but will require modifications for compatibility with ATMPs [40].

For FBRs and the glass STRs described above [39, 51, 89], cell‐carrier separation is achieved by flushing the cells from the bioreactor when enzymatic detachment is complete. The shear forces during this process transiently exceed the critical value of 1.5 × 10-4 N/cm2, which may explain the loss of cell viability. The integration of a measurement chamber including a dielectric spectroscopy probe allowed the definition of parameters that maximized the harvest yield while minimizing the volume. Concentration was achieved by centrifugation and resuspension in a smaller volume [39]. For cells harvested from the FBR process described above, cells retained their capacity for adipogenic differentiation and their metabolic activity was only slightly lower than cells cultured in parallel using T‐flasks. Cells harvested from the STR process after centrifugation consistently showed >90% viability, comparable to cells in static cultures in the same medium [39].

Clarification and volume reduction can be achieved not only by centrifugation [100] or dead‐end filtration [105] but also by TFF to achieve better product purity [63, 106]. Many fully automated, disposable and integrated (concentration and washing) TFF systems are available that are compatible with ATMP processes. TFF systems have linear scalability and operate with low shear forces and pressures. A TFF system with hollow‐fiber modules and polysulfone membranes (24 cm2 surface, pore size >45 µm, sterilized with NaOH) was recently used for the downstream processing of hMSC suspension cultures [63]. The authors showed that 10‐fold concentration in a 0.25 L volume is possible, removing 98% protein and maintaining >95% viability as well as cell identity and potency, at a shear rate of 3000 s-1. The permeate flux was controlled at 250 L m-2 h-1 and cell recovery was more than 80% at densities >2 × 105 cells/mL. The cell density, shear rate and permeate flux were shown to affect yield, viability and quality of the cells [63]. The incorporation of an expanded bed chromatography step using a multimodal prototype resin based on core‐shell bead technology achieved a further 10‐fold increase in efficiency, with a process recovery of 70% in negative mode. The best trade‐off between cell recovery (89%) and protein clearance (67%) was achieved using an intermediate expansion bed rate (1.4) which also retained the cell characteristics. A further diafiltration step can be introduced using a CPA solution for formulation, fill and finish [95]. This reduces the overall diafiltration volumes and achieves a product purity sufficient for clinical applications. TFF combined with negative mode chromatography may therefore represent the beginning of a new generation of downstream processes for hMSCs that can be improved further by the investigation of novel adsorbents [106]. The cost of large‐scale separation, clarification and concentration could be reduced fluidized bed centrifugation [62], whereas TFF would be more appropriate for smaller lots. The raw materials and detailed process parameters must always be chosen according to the cell line, media, microcarrier and expansion process.

3.6. Formulation and storage of stem cells

As discussed above, cryopreservation is the standard storage mode for single‐cell suspensions, and this is also the case for allogenic hMSCs [107]. The standard is a slow freezing rate of 1°C/min down to -80°C and a quick thawing rate (2 min at 37°C for 2 mL vials) using 5–20% dimethylsulfoxide (DMSO) in serum as a CPA [72]. Neither DMSO nor serum are suitable for ATMPs [69, 108]. For other stem cells, successful cryopreservation has been achieved using 5% DMSO in 5% human albumin [109]. A recently published study discussing the long‐term cell banking (up to 8 years) of allogenic hMSC used a cryopreservation method with 20% DMSO, and the cells were suitable for clinical studies within 1 h after thawing and dilution in PBS [110]. Sodium pentaborate pentahydrate combined with low concentrations DMSO is beneficial for tooth germ stem cells [111]. SFM and XFM combined with 5–10% DMSO is suitable for different human progenitor cells [112]. Research is underway to find appropriate alternatives CPAs to avoid the need to remove DMSO (e.g., by diafiltration) before their use in the clinic.

Based on promising preliminary studies [69], ectoin and proline have been investigated as alternative CPAs for hMSC‐TERT cells [108]. They were compared to commercially available Biofreeze SFM lacking DMSO (Biochrom, Germany [113]) combined with methylcellulose supplemented PBS. The cells were stored at -150°C and thawed quickly at 37°C. The highest cell survival rates after 48 h re‐cultivation (89 ± 2%) without DMSO and serum were achieved by supplementing the medium with 1%/10% (w/v) proline/ectoin for 60 min before freezing, and then reducing the temperature by 1°C/min which was shown to be beneficial for other stem cells [108]. The best results (∼99% survival rate) were achieved with Biofreeze SFM in all approaches. Regardless of whether Biofreeze or 1%/10% proline/ectoin was used, the cells retained their adipogenic differentiation capacity. The impact of the duration of pre‐freeze incubation and the cooling rate depended on the CPA combination. To improve outcome of cryopreservation, the authors suggested nucleation temperature control during the freezing process [108]. Another recent report described the formulation of hMSCs using the FDA‐approved commercial serum‐free and xeno‐free CPA known as STEM‐CELLBANKER™ (Amsbio, UK) [29]. The cell viability was >90% (better than DMSO) and no morphological differences were observed, but cell growth was slower. The mesodermal differentiation capacity was not regardless of which CPA was used [29]. The cryopreservation of hMSCs has also been tested using Prime‐XV MSC FreezIS DMSO‐Free (Irvine Scientific, USA) with 30 min incubation at room temperature before cooling to 4°C for 5 min followed by further cooling at 1°C/min down to -80°C for storage in liquid nitrogen vapor. The cells were thawed quickly at 37°C [100]. Other CPAs such as sucrose and high‐molecular‐weight polymers like polyvinylpyrollidone [114] should be investigated as well as studies in larger volumes or geometries (such as syringes) that might be more appropriate for therapeutic approaches [108].

In addition to single‐cell formulations, the encapsulation of cells may be beneficial to prevent allogenic cells triggering an immune response in the patient [115117]. A semi‐permeable membrane allows the diffusion of molecules (e.g., nutrients and therapeutic proteins) but protects the cells from the host immune system and mechanical forces, thus potentially enhancing the therapeutic benefits of hMSCs [118]. Various production methods have been tested to generate small beads (200–400 µm) with a narrow size distribution [119]. The formation of core capsules is often suggested [120] and this can be used to induce line‐specific differentiation [22] even when cells are cultivated in a FBR [90]. Biopolymers such as agarose, Pluronic F‐127 [121] and clinical‐grade alginate are used for this purpose, the latter forming three‐dimensional structures in the presence of multivalent cations.

Cells harvested from FBRs or glass STRs can be encapsulated by suspending 5 × 106 centrifuged cells in 500 µL sodium histamine solution then adding 4.5 mL sterile 1.5% alginate solution. After incubation for 2.5 h, the suspension was dropped into a BaCl2 solution and incubated for 2 h. Finally, the capsules were washed at least three times with PBS, and twice with EMEM and cultured in six‐well plates for further analysis. Encapsulated cells from the FBR showed adipogenic differentiation capacity and high viability (80–90% decreasing after 48 h). Cells encapsulated from T‐flasks consistently showed vitalities >95% [39, 91].

The cryopreservation of encapsulated cells is useful for the long‐term storage and off‐the‐shelf availability of many cell types, including hMSCs [122]. A three‐step slow cooling process [123] with induced ice nucleation using 10% DMSO (also suggested elsewhere [124]) has been shown to maximize cell viability, and the cells retain their metabolic and differentiation capacity. Cell encapsulation may also be beneficial for short‐term storage, such as for transport [125]. The hypothermic (4–23°C) preservation of human adipose‐derived cells encapsulated in 1.2% alginate in XFM/SFM has been discussed [126].

4. Quality approval

Prior to the product release, intensive quality control is required to confirm cell identity and safety according to validated protocols that comply with GMP, the International Conference on Harmonization (ICH) Guidelines and/or the European Pharmacopoeia [17].

4.1. Identity

Cell identity must to be approved, including viability, differentiation capacity and the surface marker profile demanded by the ISCT [18]. Cell viability, metabolic activity and growth rates can be monitored during the production process after every step (after isolation, after expansion, after harvest and clarification, after final formulation). Viability testing and cell counting are achieved using methods such as flow cytometry, including dye exclusion. Different dyes make it possible to detect viable and dead cells even in encapsulated formulations [82].

Immunophenotyping by flow cytometry is used to detect surface markers. Antibodies that bind to specific antigens expressed by the cell are coupled to fluorophores. A repertoire of cell markers can be identified and quantified simultaneously using different dyes. Many of the antigens used to distinguish human cell populations are cluster of differentiation (CD) molecules ( Immunophenotyping by flow cytometry has become the method of choice to identify and sort cells, e.g., in bone marrow aspirates.

The differentiation of hMSCs into osteoblasts, adipocytes or chondroblasts can be induced using established methods [127129]. Several differentiation media are commercially available, although the ingredients are often not fully disclosed (e.g., StemPro® Differentiation Kits for hMSCs by Gibco). The multi‐step process of adipocyte development involves a cascade of transcription factors and cell‐cycle proteins that regulate gene expression. Adipogenesis is induced by insulin, dexamethasone, 3‐isobutyl‐1‐methylxanthine (IBMX) and indomethacin [130]. Differentiation towards the adipogenic lineage can be confirmed by Oil Red O staining of lipid vacuoles in the adipocytes. MSCs undergoing chondrogenic differentiation produce large amounts of ECM when cultured in pellet form, primarily composed of cartilage‐specific molecules such as collagen type II and aggrecan [129]. The latter can be used as evidence for the chondrogenic differentiation of hMSCs and can be stained with Alcian blue, or by the immunostaining of collagen type II. Osteogenic cells show changes in cell morphology, from spindle shaped to cuboidal, and the cells accumulate extracellular calcium deposits (mineralization). Osteoblast mineralization is therefore indicative of the formation of bone mass and can be detected using the dye Alizarin Red S [127].

The successful differentiation of hMSCs and the expression of corresponding CD markers can also be verified by quantitative reverse transcription PCR (qRT‐PCR), which requires the extraction of RNA. Different protocols for RNA extraction from tissues are available, and commercial kits can be used to capture RNA on silica membranes in spin columns or isolate the RNA by phenol/chloroform extraction, followed by precipitation. A recently published study compares different single‐step RNA extraction methods focusing on embedded stem cells [131].

Lineage differentiation capacity needs to be approved only once for a validated process, if no further changes occur. A single‐cell preparation does not need to be re‐evaluated because the differentiation of cells in vitro takes 10–30 days, resulting in ethical discussions for on‐demand product applications. Generally, the benefit‐risk ratio of clinical applications must also be considered [16].

4.2. Safety

The sterility of therapeutic hMSC products must be guaranteed because any contamination (bacteria, bacterial endotoxins, mycoplasma and viruses) present a high risk to the patient. Protocols for tests are provided in the European Pharmacopoeia (EuPh) chapters 2.6.27, 2.6.14 and 2.6.2. The chapter on microbiological examination was revised in September 2016 [132]. This covers a selection of alternative tests because classical microbiological methods are often not suitable for products with a shelf‐life of only a few hours or a few days.

The potential tumorigenicity of therapeutic hMSC products is also relevant [133] but chromosomal abnormalities are rarely observed in freshly‐isolated primary hMSCs [134]. However, primary hMSC populations are heterogeneous, comprising cells of different ages that have undergone different numbers of divisions. The presence of abnormalities is dependent on both the donor and the in vitro culture method. In 2014, an investigation of 92 clinical‐grade bm‐hMSCs showed clonal mutations in only 3 of 86 cases, and none of these showed evidence of a malignant transformation or a change in phenotype [135]. To exclude products containing cells with cytogenetic abnormalities, G‐band karyotyping and fluorescence in situ hybridization (FISH) is necessary, as proposed by the EMA Cell Products Working Party (CPWP) and the Committee for Advanced Therapies (CAT) [133]. The cytogenetic testing of each batch as a release criterion is unnecessary if chromosomal abnormalities are not observed. The cryopreservation of batch samples during manufacturing is useful for later testing if needed.

5. Conclusion

The production of allogenic hMSCs is challenging, and there is intensive research focusing on the different steps in the process. Research institutes and industry have only recently published various reviews on this topic, and to our knowledge, there are still no large‐scale processes with detailed protocols for every process development step, from cell line and media selection through to the final formulation and storage, focusing on the special demands of ATMP production. This chapter has summarized the major issues affecting such a process and has discussed potential future options. Further research is required to develop closed, continuous and efficient processes that meet regulatory demands for high product quality.


This research was financially supported by the Hessen State Ministry of Higher Education, Research and the Arts, within the Hessen initiative for scientific and economic excellence (LOEWE program). The authors thank Dr. Richard M. Twyman for revising the manuscript.


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