Plant Cell Culture | Encyclopedia MDPI

Plant Cell Culture: Comparison

Please note this is a comparison between Version 1 by Francisco Cruz-Sosa and Version 2 by Conner Chen.

The large-scale production of plant-derived secondary metabolites (PDSM) in bioreactors to meet the increasing demand for bioactive compounds for the treatment and prevention of degenerative diseases is nowadays considered an engineering challenge. Plant cell culture (PCC) is nowadays recognized as a promising, renewable, sustainable, and environmentally friendly alternative to obtain PDSM out of wild plants. PCC accounts for the virtues of whole-plant cultivation systems and offers significant advantages, such as controlled manufacture due to standardized environmental conditions, i.e., it is not seasonal dependent, makes use of low amounts of water, and pesticides and herbicides are not required, achieving better quality in the desired product.

medicinal plant
bioactive compounds
plant-derived secondary metabolites (PDSM)
cell suspension culture (CSC)

1. Types of Cell Cultures

Calluses relate to the massive growth of cells and the buildup of agglomerated dedifferentiated cells, that may be able to revamp the complete plant, acquiring features like meristematic cells and developing new stem cells, which are able to form new individual plants ^[1][50]. Somatic embryos are obtained by the tissue formation from somatic cells or callus, having as the main objective the micropropagation of species seeds. Hairy roots culture is usually obtained by the infection of plant cells with Agrobacterium rhizogenes, resulting in the transformation of callus into differentiated tissues ^[2][48].

Even though there are several studies where the production of PDSM from callus cultures and differentiated cells/tissues are used, the cell suspension culture from dedifferentiated cells is mostly preferred ^[3][4][51,52]. Cell suspension cell culture (CSC) is considered as a simple and cost-effective method, allowing suitable conditions for cells to produce compounds identical to those from parental cells to be achieved, offering advantages such as setting stable systems for continuous PDSM production with homogeneity in yields and quality, as well as offering the possibility of synthesizing new compounds and greater potential for PDSM commercial application ^[3][5][51,53]. Therefore, CSC has been demonstrated to be the selected biotechnological tool for obtaining high-value PDSM, such as taxol ^[5][6][53,54], resveratrol ^[7][8][55,56], and ginsenosides ^[9][57], among others. To this end, further discussions will be centered on CSC for producing PDSM at laboratory and larger scales using different bioreactor configurations. Table 1 shows recent successful examples where plant cell culture is used for producing PDSM with pharmacological relevance.

Table 1. PDSM from medicinal plants successfully produced in the in vitro plant cell culture, bioactivities, and yield comparison.

Compound	Plant Species	Biological Activity/ Pharmaceutical Use	Extraction Yield		Type of Culture	Ref.
Compound	Plant Species	Biological Activity/ Pharmaceutical Use	Mother Plant	In Vitro Cell Culture	Type of Culture	Ref.

* Schemes were created with BioRender.com.

Engineering Aspects in the Plant Cell Suspension Culture

Engineers designing or optimizing bioreactor technologies must both consider the effect of operating conditions on the complex interaction between transport phenomena, thermodynamics, growth kinetics, metabolic activity, and maintenance of plant cell cultures and, based on it, propose methodologies to transfer information observed in flask cultures to larger bioreactor scales. Some operational conditions are critical because they can cause a decrease in biomass, a low PDSM production, or a loss of cell viability. Table 4 shows some CSC that have been successfully scaled from flask cultures to large-scale bioreactors.

Table 4. Comparison of operating conditions used for SCC in flask and bioreactor to produce PDSM. The list of examples makes no claim to be complete.

Species	Compounds	Operation Variables Evaluated		Biomass Production		PDSM Production	Ref.
Species	Compounds	In Shake Flask	In Bioreactor	In Shake Flask	In Bioreactor	PDSM Production	Ref.
Shikonin	Lithospermum erythrorhizon Alkanna tinctoria Tausch	Anticancer, antibacterial, anti-inflammatory, hepatic steatosis attenuator, antitumor, and antioxidants	10−20 mg/g	150−200 mg/g	CSC	^[10]^[11]^[12]^[13]^[14][58,59,60,61,62]
Shikonin	Echium plantagineum L.		10−20 mg/g	36.25 mg/L	HRC	^[15][63]
Anthraquinones	Morinda citrifolia Rubia cordifolia Senna obtusifolia	Antimicrobial, antifungal, hypotensive, analgesic, antimalarial, gastroprotective, antioxidant, hepatoprotective and antileukemic, and mutagenic functions	3 mg/g	100–200 mg/g	HRC CCC CSC	^[16]^[17]^[18]^[19][64,65,66,67]
Rosmarinic acid	Ocimum basilicum	Antioxidant, anti-inflammatory, antiviral activities	8.78–9.4 mg/g	12.32–21.28 mg/g	CSC	^[20]^[21][68,69]
	⁴⁴
	^]
	[
	90
,
91
]
Phenolic Acids
Verbena officinalis
Verbena officinalis
Antimicrobial, secretolytic, expectorant, and diuretic agent

136.59 mg/g
136.59 mg/g
126.55 mg/g
CCC
^[
^[	⁴⁵
^]	⁴⁵
^]	[
92	[
92	]
	]
(rosmarinic, chlorogenic, and ferulic acid)	189.91 mg/g	CSC
Resveratrol	Vitis vinifera L.	Reduced coronary heart disease mortality rates and atherosclerosis, inhibiting low-density lipoprotein oxidation, and carcinogenesis	NR	277.89 µg/g	CSC	^[46][7]

CSC means cell suspension culture; HRC means hairy root culture; CCC means callus cell culture, ARC adventitious root culture; NR means not reported.

2. Plant Cell Suspension Culture

Plant cell suspension culture (CSC) represents a cost-effective and simple biological process for the synthesis of PDSM at large scales ^[3][51]. This production concept takes advantage of plant cells as biosynthetically totipotent structures, being capable of obtaining bioactive compounds with identical properties to those contained in plant stem cells, offering potential advantages regarding quality and yield of PDSM ^[3][47][51,93]. To this end, although there are engineering challenges, CSC offers greater potential for industrial applications in large-scale bioreactors than plant tissue and organ cultures. Although the latter ones offer better genetic stability in propagated cells, the design of the bioreactors for their maintenance usually requires greater investments and careful experimentation in the preliminary scale-up stage ^[48][49][42,94].

At a laboratory scale, CSC, in general, uses dedifferentiated plant cells and involves four essential stages as shown in Figure 1 ^[48][42].

Figure 1. General steps for obtaining cell suspension culture. PDSM means plant-derived secondary metabolites. * Schemes were created with BioRender.com.

Success in the operation of suspension cultures depends on the induction and obtention of friable callus (stage 3) through the exposure to growth regulators, such as auxins and cytokinin. The final step (stage 4) comprises the transfer and maintenance of this cell culture in a liquid. CSC may become unstable when subjected to prolonged culture times, causing differences in the quality and quantity of PDSM; this behavior is due to the consumption and reduced availability of nutrients in the culture media, in addition to genetic variations that can restrict the conservation of the high-yield cell line ^[50][9]. Among the strategies used for improving the production of PDSM in CSC is the modification in the culture media composition (different carbon, nitrogen, and phosphorous sources) for optimizing the nutrient availability during the culture time ^[51][50][6,9], and the use of biotic or abiotic elicitors that trigger the defense response from plant cells promoting the secondary metabolism through the introduction of chemical or physical stresses ^[46][3][52][7,51,95]. Biotic elicitors are complex compounds derived from biological sources, including plant-derived polysaccharides, such as pectin and cellulose, and microbial-derived polysaccharides, such as chitin and glucan ^[51][53][6,44], and plant immune-signaling molecules, such as jasmonic acid ^[54][96], salicylic acid ^[55][56][97,98], and methyl jasmonate ^[54][96]. Abiotic elicitors include inorganic salts, heavy metals, UV irradiation, high salinity, and pressure ^[57][99].

3. Commercial Production of PDSM from CSC

The current production of various drugs, cosmetics, and food ingredients is obtained using plant cell cultures, especially in the form of CSC, as these offer several advantages over other technologies, such as better control during the production of PDSM, a larger feasibility for the scaling up of the process, and shorter production cycles, being environmentally responsible and sustainable processes. The application of CSC to obtain commercial products dates back to the 1960s ^{[46][50][58][59]}[7,9,24,100]. Table 2 shows a selection of plant cell extracts that have been successfully manufactured at a commercial scale for pharmaceutical purposes. So, by way of history, the first report about industrial manufacturing of bioactive compounds derived from CSC was found for Shikonin from L. erythrorhizon by Mitsui Petrochemical Ind., now Mitsui Chemicals, Inc. (Tokyo, Japan). To date, Taxol^®, manufactured by Phyton Biotech, Inc. (Delta, BC, Canada), and Genexol, the commercial name for paclitaxel compound by Samyang Genex, represent the cancer drugs with greater demand in the market, with annual sales reaching up to 200–300 kg per year ^[60][101]. In agreement with the information available at the website for manufacturers, the production volume for PDSM increases from a few cubic meters to 75 m³ equivalent, to reach 880 m³ per year ^[61][102].

Table 2. Plant-derived products manufactured from plant CSC which have entered into the pharmaceutical industry. The list of products makes no claim to be complete.

Product	Species	Pharmaceutical Use	DescriptionManufacturer, Tradename, and Scale of Production	Type of Culture	Reference
Advantages	Disadvantages	Ref.
Rosmarinic acid	Coleus blumei	Anti-inflammatory	ANattermann & Cie. Gmbh, www.sanofi.de (accessed on 30 October 2021)	CSC	^[62][103]
Scrophularia striata
Echinacea polysaccharides	Echinacea purpurea
Bubble column (BC)		It is classified in the pneumatic-type bioreactor. They are constructed in cylindric columns where gas injection represents the only energy entrance to the system. BC bioreactors operate under constant bubbling where gas flows from the bottom to the top through nozzles, perforated plates, or spray rings, allowing not only the aeration process, but also helping the mixing and circulation of the fluid, without the need to install mechanical accessories.	Phenylethanoid glycosidesSimple structure as no mechanical force is required to shake.	50 mL SCC in 100 mL flask 110 rpm Easier maintenance and reduces the risk of contamination due to the lack of mobile parts. Reduced effect of the shear stress.	25 °C	5.0 L SCC in STR 10 L Fg: 0.5–1.0 L/min 110−170 rpm 25 ± 1 °C DarknessHigh foam formation under high gas flow rates. Poor oxygen transfer capabilities. Poor fluid mixing in highly viscous fluids. High levels of foaming under high-aeration conditions	^[58]^[49	14.16 g/L^]^[^75][24,94,116]	15.64 g/L	The acteoside content in CSC in the bioreactor was about threefold higher than that in the shake flask	^[81][122]
Immunostimulant, anti-inflammatory	⁷⁷
Buddleja cordata	Verbascoside, linarin and hydroxycinnamic acids	50 mL SCC in 250 mL flasks 110 rpm 26 ± 2 °C	STR 2 L Fg: 1 vvm (ring diffuser Rushton impeller 400 rpm	^[	⁶³^][100,104]
	26 ± 2 °C		16/8 h light to dark photoperiod	^]	^[⁷⁸^][24,117,118,119]
11.8 g/L	13.62 g/L	The content of phenolics was twofold higher in STR.	^[	⁸²	^]	^[

[138,144]. There are, in the literature, several models that have no mechanistic grounds but account for some biological features of the cell growth ^[97][104][138,145]. These models offer an acceptable description of the cell growth and metabolic activity due to fluctuation in the concentration of substrates and products. In these models, cell mass is divided into compartments, and the rate of formation of each compartment has different stoichiometry and kinetics.

Table 5. Models used to describe kinetics and deactivation in whole cells ^{[96][99][100][101]}[137,140,141,142].

Mathematical Equation	Conventional Name
$\begin{array}{l} r_{x} = µ = \frac{µ_{\max} [S_{i}]}{[S_{i}] + K_{m}} \\ r_{s} = Y_{xs} µ \end{array}$	Monod kinetics
$\begin{array}{l} r_{x} = µ = \frac{µ_{\max} [S_{i}]}{({[S_{i}]}^{2} / K_{i}) + [S_{i}] + K_{m}} \\ r_{s} = Y_{xs} µ \end{array}$	⁸³	^]	[	123	,	124	]	$\begin{array}{l} r_{x} = µ = \frac{µ_{\max} [S_{i}]}{({[S_{i}]}^{2} / K_{i}) + [S_{i}] + K_{m}} \\ r_{s} = Y_{xs} µ \end{array}$	Expanded Monod kinetics
Berberines	Stirred tank bioreactor (STB)Thalictrum minun	Anticancer; antibiotic; anti-inflammatory	Mitsui Chemicals, Inc., (75,000 Lbr)	CSC	^[64][105]
Berberines	Airlift (ALB)	Anticancer; antibiotic; anti-inflammatory		It is classified in the pneumatic-type bioreactor. This configuration is considered reasonably like STR, excepting for the impeller. They are tower reactors where fluid broth is mixed with a gas stream, which is compressed and injected at the bottom of the discharge pipe. The gas–fluid mix allows the creation ofdifferences in density and upward displacement. It is more suitable for hairy root and somatic embryo cultures.	^[64][105]	Diversa, 75,000 L bioreactor	CSC	^[59]
$\begin{array}{l} r_{x} = µ = \frac{µ_{\max} [S_{i}]}{[S_{i}] + K_{m}} (1 - \frac{[P]}{{[P]}_{\max}}) \\ r_{s} = Y_{xs} µ \end{array}$	It is grouped in the mechanically agitated bioreactor. This bioreactor consists in a mixer (turbine or propeller) installed within the tank reactor and may be equipped with gassing inlet stream. It can operate in batch, semi-continuous, or continuous mode	^[76]^[79][117,120
Rubia tinctorum	]	.	Anthraquinone	$\begin{array}{l} r_{x} = µ = \frac{µ_{\max} [S_{i}]}{[S_{i}] + K_{m}} (1 - \frac{[P]}{{[P]}_{\max}}) \\ r_{s} = Y_{xs} µ \end{array}$ 25 mL SCC in 250 mL flasks 100 rpm 25 ± 2 °C 16/8 h photoperiod (140 µmol m⁻² s⁻¹)Efficient fluid mixing systems. High oxygen mass transfer capability. Convenient for high-viscous fluids. Comply with Good Manufacturing Practices. Easy scale-up. Highly adaptable to production scale and products. Impeller alternative.	High energy cost owing to mechanical agitation.	1.0 L SCC in STR 2 L Fg: 1 vvm Turbine impeller 450 rpm 25 ± 2 °C 16/8 h photoperiod Contamination risk with mechanical seal. Some cells and metabolites are susceptible to shearing generated by the impeller and bursting gas bubbles. Depending on the operation mode, this configuration can represent high costs of maintenance, cleaning, and startup.	^[49]^[76]^[79]^[80][94,117,120,121]

(140 µmol m

⁻²

⁻¹

)

330 g/L

220 g/L

Anthroquinone production was 2.5 times higher in STR

\begin{array}{l} r_{x} = µ = \frac{µ_{\max} [S_{i}]}{[S_{i}] + K_{m}} (1 - \frac{[P]}{{[P]}_{\max}}) \\ r_{s} = Y_{xs} µ \end{array}

^84][125

Expanded Monod kinetics]

Coptis japonica

https://www.mitsuichemicals.com/

(accessed on 30 October 2021)

CSC

Arnebia sp.

\begin{array}{l} r_{x} = µ = µ_{\max} (1 - \exp (- [S_{i}] / K_{m})) \\ r_{s} = Y_{xs} µ \end{array}

Shikonin

\begin{array}{l} r_{x} = µ = µ_{\max} (1 - \exp (- [S_{i}] / K_{m})) \\ r_{s} = Y_{xs} µ \end{array}

25 mL CSC in 250 mL flasks

\begin{array}{l} r_{x} = µ = µ_{\max} (1 - \exp (- [S_{i}] / K_{m})) \\ r_{s} = Y_{xs} µ \end{array}

Air-lift bioreactor

\begin{array}{l} r_{x} = µ = µ_{\max} (1 - \exp (- [S_{i}] / K_{m})) \\ r_{s} = Y_{xs} µ \end{array}

1249.2 g/L

480 g/L

The shikonin content was 2.6 times higher in the bioreactor than in the flask. Production remained without significant differences in both bioreactors

^[85][126]

Origanum vulgare

23.53 mg/g

31.25 mg/g

CSC

^[22]^[

Podophyllotoxin

Podophyllum spp.

Anticancer

Nippon Oil Company, Ltd.

²³^][70,71]

CSC

⁶⁵

[

106]

Satureja khuzistanica

https://www.freepatentsonline.com/5336605.html

12 mg/g

(accessed on 30 October 2021)

\begin{array}{l} r_{x} = µ = µ_{\max} (1 - \exp (- [S_{i}] / K_{m})) \\ r_{s} = Y_{xs} µ \end{array}

Monod’s teacher Tessier kinetics.

100 rpm

\begin{array}{l} r_{x} = µ = \frac{µ_{\max} [S_{i}]}{[S_{i}] + K_{S} X} \\ r_{s} = Y_{xs} µ \end{array}

2 L working volume

\begin{array}{l} r_{x} = µ = \frac{µ_{\max} [S_{i}]}{[S_{i}] + K_{S} X} \\ r_{s} = Y_{xs} µ \end{array}

Contois kinetics.

OC38 mg/g

25 ± 2 °C

\begin{array}{l} r_{x} = µ = µ_{\max} (1 - \frac{X}{K_{S}}) \\ r_{s} = Y_{xs} µ \end{array}

⁶⁶

CSC

^][107]^[24][25][72,73]

Coleus blumei

30 mg/g

270 mg/g

CSC

^[26][32]

Docetaxel

Taxus baccata

Ovarian cancer treatment

Phyton Biotech, Inc., Taxotere (150 kg/year)

CSC

^[67]^[68]

Salvia officinalis

30 mg/g

360 mg/g

CSC

[

108

109

]

Continuous light

Fg: 2 L/min (sparger ring)

https://phytonbiotech.com/ (accessed on 30 October 2021)

(70 µmol/m² s ¹)

Berberine

Thalictrum minus

Effects antitumor, anticancer, lower blood lipid, lower blood glucose, anti-osteoporosis, anti-osteoarthritis, antibiotic, and anti-inflammatory

0.1 mg/g

0.8 mg/mL

Paclitaxel

Taxus spp.

Anticancer: FDA approved for the treatment of ovarian, breast, and lung cancers

CSC

Phyton Biotech, Inc., Taxol ^® (1000 kg/year)

CSC

^[69][110]

^[27]^[28]^[29^[³²^][74,75^][,76^30][,77^31]

STR 2 L

]

1249.2 g/L

450 g/L

Coptis japonica

20–40 mg/g

132 mg/g

CSC

Coscinium fenestratum

1 mg/g

178 mg/g

CCC

https://phytonbiotech.com/ (accessed on 30 October 2021)

Samyang Genex Corporation., Genexol (32,000 Lbr) https://samyangbiopharm.com/eng/ProductIntroduce/injection01 (accessed on 30 October 2021)

CSC

^[70][111]

Ginsenosides

Panax ginseng

Antitumor, immunological, anti-inflammation, anticancer, antidiabetic, and cardiovascular-protective

0.015–8 mg/g

36.4–80 mg/g

HRC

Six-blade turbine impeller 100 rpm

⁹

³³^][57

^[71][112]

³⁴

,81]

3.4–28.9 mg/g

Fg: 2 L/min

ScopolamineCSC

Duboisia

spp.

Anticholinergic; antimuscarinic; motion sickness, nausea, and intestinal cramping

Sumitomo Chemical Co., Ltd., Tokyo, Japan

(50–20,000 Lbr) https://www.sumitomo-chem.co.jp/pharma-chem/ (accessed on 30 October 2021)

HRC

^[72]^[73][113,114]

25 ± 2 °C

Ocinum basilicum

Rosmarinic acid

100 rpm

7 L CSC in STR 10 L

Biomass was 8.4 times higher in bioreactor than in flask

Production increased 1.66 times in bioreactor

^[21][69]

15.1–105.6 mg/g

Shikonin

ARC

Lithospermum erythrorhizon

Anti-HIV, antitumor, anti-inflammatory

Xi’an NEO Biotech, Shikonin 95%

CSC

^59][100]

Panax japonicus

25 ± 2 °C

Marine impeller 100 rpm

20–50 mg/g

CSC

Fg: 25 L/min

Panax notoginseng

60 mg/g

CCC

Satureja khuzistanica

Rosmarinic acid

200 mL CSC in 1 L flask

1 L CSC in culture bags 2 L

13.6 g/L

18.7 g/L

Production increased 2.5 times in bioreactor

^[86][127]

71.94 mg/g

ARC

110 rpm

40 mg/g

CSC

Diosgenin

Dioscorea deltoidea

Anticancer, antidiabetic, anticoagulant, antithrombosis, anti-inflammatory, antiviral, anti-ageing

0.4−3 mg/g

72 mg/g

CSC

^[35][82]

3.5–16 mg/g

http://www.extractneo.com/about (accessed on 30 October 2021)

CCC

Batch mode

Dioscorea bulbifera

25 °C

12 mg/g

CCC

20–30 rpm

Helicteres isora L.

1–5 mg/g

8.64 mg/L

CSC

^[36][83]

23 mg/g

CCC

^[37][84]

Ajmalicine

Catharanthus roseus

Antihypertensive, obstructive circulatory diseases treatment

3 mg/g

63 mg/L

CCC

^[38][85]

10 mg/g

25 °C

Fg: 0.1 vvm

Darkness

Vitis labrusca L.

Resveratrol

100 mL CSC in 300 mL flasks

STR 5 L

≈35 g DW

Production increased 1.15 times in bioreactor

^[87][128]

110 rpm

Marine impeller 110 rpm

23 °C

Fg: 0.15 vvm

CSC

^[39]^[40][86,87]

Darkness

34 mg/L

Santalum album L.

HRC

Squalene

100 mL CSC in 250 L flask

Airlift bioreactor 7 L

1.05 mg/g

1.25 mg/g

Production increased 1.71 times in bioreactor in four weeks of culture

^88][129]

Paclitaxel

Taxus chinensis

Anticancer

0.02 mg/g

1.5 mg/g

CSC

^[41][88]

Podophyllotoxin

90 rpm

Batch mode

Linum narbonense

Vigorous antimitotic and antiviral activities and anticancer

0.5 mg/g

1.57 mg/g

CCC

^[42][89]

Juniperus chinensi

0.025 mg/g

189.91 mg/g

CSC

Linum flavum

1.6 mg/g

2 mg/g

CSC

Artemisinin

Artemisia annua L.

Treat multi-drug-resistant strains of falciparum malaria

1–15 mg/g

9.33–110.2 mg/L

CSC

^[43]^[

CSC: cell suspension culture; HRC: hairy root culture; OC: organ culture.

4. Typical Bioreactor Configurations

Bioreactors are defined as containers used to provide a controlled environment to transfer nutrients and oxygen to cell cultures in adequate concentrations that allow the cell to maintain its primary and secondary metabolic activity. Because plant cells, as well as other micro-organisms, are more sensitive and less stable than chemical compounds, bioreactor designs must be robust enough to provide a greater degree of control over process disturbances and contamination and achieve high productivities, high quality products, and cost effectiveness. The bioreactor design and its optimal operation depend on the determination of the operating conditions giving rise to the required product formation, minimizing the cost of the process ^[74][115]. The most common bioreactor configurations utilized for commercial and large-scale production consist in stirred tank bioreactor (STB), wave stirred bioreactor (WSB), air-lift bioreactor (ALB), and bubble column (BC). The selection of the bioreactor configuration is frequently established by its optimal performance in terms of metabolic activity and kinetics of cell cultures, economic costs, and its flexible operation regarding maintenance of cultures by controlling operational conditions, such as temperature, pH, aseptic, mixing, aeration, and scalability. Table 3 shows some characteristics, advantages, and disadvantages of these types of bioreactors.

Table 3. Comparison of bioreactor configurations commonly used for plant cell culture.

Bioreactor Configuration	Schematic Diagram *
Easy maintenance and reduces the risk of contamination due to the absence of mobile parts.
	Reduced effect of the shear stress.	Higher oxygen transfer than that in BC. The energy required is provided by the compressed gas.	High levels of foam formation under high gas flow rates. Poor fluid mixing in highly viscous fluids. Relatively poor oxygen transfer capabilities.	^[58]^[76]^[
28 °C
70–80 rpm

Fg: 4 L/min

28 ± 2 ° C

NR means Not reported.

The scaling up of CSC carried out in a flask culture demands the use of bioreactor engineering to characterize the impact of operating conditions on growth kinetics, cell deactivation, and transport phenomena and, hence, on the metabolic activity and production rates of PDSM. To this end, in what follows, main aspects to be considered during the scaling up of CSC, from the screening of plant cells to the industrial-scale bioreactor design, are mentioned and analyzed.

The screening of a set of plant cells is considered as the first stage during the scaling up of CSC ^[48][49][42,94]. Screening takes place in shake flasks. In these laboratory bioreactors, hydrodynamic and transport phenomena negatively impact on the growth kinetics, cell viability, metabolic activity, and production rates of PDSM. For instance, in these bioreactors, the production of PDSM involves two-phase systems (liquid culture phase and cell culture phase) neglecting the effect of operating conditions, including the impact of the oxygen concentration, on the microscopic and macroscopic performance of the shake flask. In this context, apparent results regarding cell growth kinetics, cell viability rates, and production rates of PDSM are observed. In these conditions, promising plant cells are identified and selected to be evaluated in larger bioreactor configurations, such as those presented in Table 3.

The second step accounts for characterization of cell growth kinetics, cell viability rates, metabolic activity, and production rates of PDSM under controlled operating conditions in bench-scale bioreactors with similar configurations to those systems to be implemented at the commercial scale, i.e., bench-scale bioreactors accounting for three phases (liquid–gas–cells) (see Table 3). Thus, during the analysis of bench-scale systems, the coupling of experimentation with mathematical modeling is essential for stating the basis for the scaling up of CSC ^[89][90][91][130,131,132]. Herein, cell growth kinetics and production rates of PDSM are the main response variables to maximize during CSC. It is worth mentioning that their experimental and theoretical characterization makes possible the connection between the microscopic world of the metabolic cell activity and the macroscopic world of the bioreactor performance and, hence, the downstream processing. Besides, the experimental characterization of these cell mechanisms and their analysis using mathematical models lead to the construction of the engineering tool for the scaling up and optimization of the bioreactor configuration, allowing a better understanding of CSC during the production of PDSM. In particular, the use of bench-scale bioreactors allows for identifying and controlling those operating conditions where transport phenomena favor the kinetics of the CSC.

Based on the kinetics, since in CSC it is not possible to develop intrinsic kinetic models, there are two types of models that can be developed in bench-scale bioreactors: extrinsic ones, where transport phenomena are explicitly included during the modeling of the bioreactor; and apparent ones, where transport phenomena resistances impact during the experimentation but they are not considered during the modeling of the bench-scale bioreactors ^{[90][92][93][94][95][96]}[131,133,134,135,136,137]. Thus, to determine extrinsic kinetic models, it is recommended to carry out a regime analysis to identify and model those transport phenomena limiting the production of PDSM. Experiments make possible the development of the corresponding model, relating kinetics with macroscopic variables, namely the concentration of substrates and PDSM, cell growth, and cell viability involved during the operation of the bench-scale bioreactor. The kinetic model depends on the quality of the experimental data and it is only reliable for the range of operational conditions utilized during its development. When the kinetic model is based on metabolic steps of the reaction, the mathematical complexity increases but leads to a better physical representation of the CSC during the production of PDSM. Besides, the loss of cell viability caused by operational aspects, i.e., a toxic compound, cell shear stress, or cell sintering, is modeled by empirical expressions whose parameters involve physical meaning ^[97][138], such as the generalized power law equation (GPLE) ^{[98][99][100]}[139,140,141]. Finally, the Monod model offers an adequate explanation for the reaction rates of growing cells, but it has no mechanistic basis ^[101][102][142,143]. Moreover, the Monod model is only applicable when cells are in a metabolic equilibrium, namely when the composition of the macromolecules in the cell remains in a pseudo-steady state during the CSC. Table 5 presents some kinetic models to describe cell growth rate. It is worth mentioning that, in transient experiments, when the concentration of a substrate or PDSM is brusquely modified, Monod kinetics are not suitable and the kinetic model must account for the cell metabolism ^[97][103]

$\begin{array}{l} r_{x} = µ = µ_{\max} (1 - \frac{X}{K_{S}}) \\ r_{s} = Y_{xs} µ \end{array}$
Logistic kinetics.
$\begin{array}{l} \frac{d θ_{x}}{d t} = - k_{in} {(θ_{x} - θ_{s s})}^{m} \\ r = r_{s} = θ_{x} \frac{k [S_{i}]}{[S_{i}] + K_{m}} \end{array}$
$\begin{array}{l} \frac{d θ_{x}}{d t} = - k_{in} {(θ_{x} - θ_{s s})}^{m} \\ r = r_{s} = θ_{x} \frac{k [S_{i}]}{[S_{i}] + K_{m}} \end{array}$
$\begin{array}{l} \frac{d θ_{x}}{d t} = - k_{in} {(θ_{x} - θ_{s s})}^{m} \\ r = r_{s} = θ_{x} \frac{k [S_{i}]}{[S_{i}] + K_{m}} \end{array}$	Cell deactivation kinetics

In bench-scale bioreactors, it is experimentally complicated to minimize transport resistances ^{[98][99][100][105]}[139,140,141,146]. In the fluid bulk, concentration, temperature, or radiative gradients can be present. Hydrodynamics impact on mass and heat transfer mechanisms from the gas phase to the liquid phase and from the liquid phase to the cell phase. Moreover, cell growth can impact on mass and heat transfer mechanisms. Although complicated, a proper kinetic analysis must account for the effect of fluid dynamics on transport phenomena and, hence, on cell growth, cell viability, and metabolic activity.

During the screening at the laboratory bioreactors or during the operation of the bench-scale bioreactor, the response surface methodology (RSM) is a potential tool to guide experimental designs. RSM leads to the following advantages ^{[106][107][108][109][110]}[147,148,149,150,151]:

(1)

It defines an establishment of the relationship between responses (yield, cell viability, oxygen concentration, etc.) and control operating conditions (temperature, pressure, initial concentration, power input, agitation rate, etc.).

(2)

It predicts the effect of control operating condition on responses.

(3)

It gives inferences on the significance of the operating conditions on the performance of the reactor.

(4)

It allows the determination of the operating window where the bioreactor meets its best performance.

On the above end, RSM couples experimental designs, and mathematical and statistical methods ^[111][112][152,153]. Firstly, an experimental design is proposed; the evaluation of this experimental design constitutes the so-called response surface design (RSD). The suitability of the RSD depends on its orthogonally, ratability, and uniform precision ^[112][153]. Secondly, the empirical model is then developed; it is approximated by a polynomial equation that accounts for elements that consist of powers and cross-product powers, constant coefficients referred to as parameters, and a random experimental error. Albeit empirical, first-degree and second-degree polynomial equations are usually used to fit observations and carry out the optimization. To this end, every model and its reliability depends on the RSD, i.e., first-order designs are used to fit observations with the first-degree models, and observations out of second-order designs are fitted with second-degree models ^{[111][112][113]}[152,153,154]. The most common first-order designs are 2k factorial, Plackett–Burman, and simplex designs, while the most common second-order designs are 3k factorial, central composite, and the Box–Behnken designs. Note that the choice of a proper RSD is essential since the quality of prediction, as measured by the size of the prediction variance, depends on it; thus, the lower the variance, the better the fit of the responses. On this basis, a single RSD is not able to satisfy all criteria, but it is considered as robust if it meets the assumptions related to the model and the error distribution ^[111][112][152,153]. Finally, the assessing of the results uses both statistical tests, i.e., F-value, t-value, and confidence interval, and graphical tests, i.e., variance dispersion graphs, fraction of design space plots, and quantile plots. Graphical methods ^[108][109][149,150] based on quantile dispersions have also been used to compare experimental designs for estimating variance components in an analysis of variance (ANOVA) situation. RSM can lead to the identification of the operational window where CSC presents its higher yields to PDSM, which, in turn, will be essential in the conceptual design and scaling up of the bioreactor configuration.

Because of the advent of computation in the last years, the bioreactor design not only depends on empirical, but also deterministic approaches, which allows the proper determination of hydraulics, fluid dynamics, mass transport, heat transfer, radiative transfer, and kinetics from different bioreactor configurations at various scales. This information is transferred to design and scale up the industrial bioreactor. The design of this reactor strongly depends on the development of a model coupling kinetics and transport phenomena at both the cell and bioreactor level, including the fluid and the gas phase. This is, however, a complex task, since it needs experiments and mathematical solutions that are not trivial. It is worth stressing that, during the construction of this model, fluid dynamics are yet the bottleneck during the scaling up of a bioreactor configuration because of their impact on transport phenomena, kinetics, and, hence, on the global production of PDSM.

Based on the above, a model accounting for kinetic, deactivation, and all transport mechanisms should be developed from the laboratory to the bench scale. This model should be constructed following a framework based on computational fluid dynamics (CFD). The model needs to be validated at the bench scale before using it to design the industrial bioreactor. The preliminary dimensions of the reactor need to be obtained from the utilization of the practical know-how reported in the literature or experimental and modeling results obtained at the bench scale. It will make the scaling up process more efficient and reliable. Developing a model for the use of CFD allows the consideration of fluid dynamics along with its effect on transport phenomena, which leads to obtaining operating conditions where mixing, hydrodynamics, and transport phenomena are improved without affecting the operating cost of the process. A criterion when designing the industrial-scale bioreactor is to achieve a compromise between operating expenses and yield of the PDSM. At the end of the scaling-up process, the experimentation and investment cost as that compared using an empirical or heuristic approach will be significantly minimized.

In addition to the aforementioned, the scaling up of CSC becomes more challenging when observing how operating conditions impact on the production of PDSM. Operating conditions influence in different scenarios and magnitudes the performance of cell cultures during the production of PDSM, from the supply of nutrients (oxygen, light, ionic strength, pH) to the implementation of mechanical and pneumatic work to keep the process operating in optimal conditions. In further sections, a discussion about the main operating variables in bioreactors and their effect on the performance of cell culture will be provided.