The present invention relates to a method of protein enrichment of microalgal biomass, said microalga being more particularly of the genusChlorella, even more particularly of the speciesChlorella sorokinianaorChlorella protothecoides.
Algae—macroalgae and microalgae—have a specific but largely unexplored richness. Their use in the production of food, chemicals and bioenergy remains very rare. They conceal, however, components of great value, whose richness and abundance can be truly appreciated only by the marine animals that feed on them.
Microalgae are in fact sources of vitamins, lipids, proteins, sugars, pigments and antioxidants.
Algae and microalgae are thus of interest to the industries that use them to produce dietary supplements, functional foods, cosmetics or medicines, or for aquaculture.
Microalgae are above all photosynthetic microorganisms which colonize all biotopes exposed to light.
On an industrial scale, their monoclonal culturing is carried out in photobioreactors (autotrophic conditions: with light and CO2) or, for some, also in fermentors (heterotrophic conditions: in darkness in the presence of a carbon source).
A few microalgae species are in fact able to grow in the absence of light:Chlorella, Nitzschia, Cyclotella, Tetraselmis, Crypthecodinium, Schizochytrium.
Furthermore, it is estimated that culturing under heterotrophic conditions costs 1/10 that of culturing under phototrophic conditions because, for the skilled person, heterotrophic conditions make it possible to:
- use fermentors that are identical to those used for bacteria and yeasts and that allow all of the culture parameters to be controlled.
- produce biomasses in much greater amounts than those obtained by light-based culturing.
The profitable use of microalgae generally requires control of the fermentation conditions so as to accumulate the components of interest, such as:
- pigments (chlorophyll a, b and c, β-carotene, astaxanthin, lutein, phycocyanin, xanthophylls, phycoerythrin, etc.) increasingly in demand for their remarkable antioxidant properties and for providing natural colors in foods,
- proteins, in order to optimize their nutritive qualities; or
- lipids, in order to optimize their fatty acid content (up to 60%, even 80% by weight of their dry matter), in particular for:
- biofuel applications, but also
- human or animal food applications, when the selected microalgae produce so-called “essential” (i.e., provided in the diet because they are not naturally produced by humans or animals) polyunsaturated fatty acids, or PUFAs.
To arrive at this result, first high cell density (HCD) fermentation methods were thus thoroughly investigated, so as to obtain maximum yields and productions of proteins or lipids.
The objective of these HCD cultures was to obtain the desired product in the highest possible concentration in the shortest amount of time.
This precept is verified, for example, for the biosynthesis of astaxanthin byChlorella zofingiensis,where the growth of the microalga proved to be directly correlated with the production of this compound (Wang and Peng, 2008,World J Microbiol. Biotechnol.,24(9), 1915-1922).
However, the fact of maintaining growth at its maximum rate (μ, in h−1) is not always correlated with high production of the desired product.
In fact, it quickly became apparent to the specialists in the field that, in order for microalgae to produce large lipid reserves, it is necessary, for example, to subject the microalgae to a nutritional stress that limits their growth.
Now, growth and production are decoupled in fermentation methods.
For example, to promote the accumulation of polyunsaturated fatty acids (here docosahexaenoic acid, or DHEA), patent application WO 01/54510 advises to dissociate cell growth and polyunsaturated fatty acid production.
In the microalgaSchizochytriumsp. strain ATCC 20888, a first growth phase without oxygen limiting is thus carried out so as to promote the production of a high cell density (greater than 100 g/l); then, in a second step, the oxygen supply is gradually reduced so as to stress the microalga, to slow its growth and to initiate the production of the fatty acids of interest.
In the microalgaCrypthecodinium cohnii, the highest docosahexaenoic acid (DHEA, polyunsaturated fatty acid) content is obtained with a low glucose concentration (about 5 g/l), and thus with low a growth rate (Jiang and Chen, 2000,Process Biochem.,35(10), 1205-1209).
These results illustrate clearly that the kinetics of product formation can be positively or negatively associated with microalgae growth, and even a combination of the two.
Consequently, in the case where product formation is not correlated with high cell growth, it is wise to control the cell growth rate.
In general, the skilled person chooses to control microalgae growth by controlling the fermentation conditions (Tp, pH, etc.) or by controlling the supply of nutritional components to the fermentation medium (semi-continuous so-called “fed-batch” conditions).
If the skilled person chooses to control microalgae growth under heterotrophic conditions by means of the supply of carbon sources, he or she generally chooses to adapt the carbon source (pure glucose, acetate, ethanol, etc.) to the microalga (C. cohnii, Euglena gracilis, etc.) according to the metabolite produced (a DHEA-type polyunsaturated fatty acid, for example).
The temperature may be a key parameter as well:
- it has been reported, for example, that the synthesis of polyunsaturated fatty acids by certain microalgae species, such as EPA byChlorella minutissima, is promoted at a temperature lower than that required for the optimal growth of said microalga;
- conversely, the yield of lutein byChlorella protothecoidesgrown heterotrophically is higher when the production temperature is increased from 24° C. to 35° C.
Chlorella protothecoidesis justifiably recognized as one of the best oil-producing microalgae.
Under heterotrophic conditions, it quickly transforms carbohydrates into triglycerides (greater than 50% of its dry matter).
To optimize this triglyceride production, the skilled person is led to optimize the carbon flux toward the production of oil by acting on the nutritional environment of the fermentation medium.
It is thus known that oil accumulates when a sufficient amount of carbon is supplied, but under nitrogen-deficient conditions.
The C/N ratio is thus decisive here, and it is acknowledged that the best results are obtained by acting directly on the nitrogen content, as the glucose content is not limiting.
Not surprisingly, this nitrogen deficiency affects cell growth, resulting in a growth rate that is 30% lower than the normal microalgal growth rate (Xiong et al.,Plant Physiology,2010, 154, pp. 1001-1011).
To explain this result, Xiong et al., in the above-mentioned article, show that, in fact, if theChlorellabiomass is divided into its five principal components, i.e., carbohydrates, lipids, proteins, DNA and RNA (representing 85% of its dry matter), if the C/N ratio has no impact on the DNA, RNA and carbohydrate content, it becomes preeminent for the protein and lipid content.
Thus it is thatChlorellacells grown with a low C/N ratio contain 25.8% proteins and 25.23% lipids, while a high C/N ratio enables the synthesis of 53.8% lipids and 10.5% proteins.
To optimize oil production, it is thus essential for the skilled person to control the carbon flux by diverting it toward oil production, to the detriment of protein production; the carbon flux is redistributed and accumulates in lipid storage substances when the microalgae are placed in nitrogen-deficient medium.
Armed with this teaching, to produce protein-rich biomasses the skilled person is thus led to carry out the opposite of this metabolic control, i.e., to apply fermentation conditions that promote a low C/N ratio instead, and thus:
- to supply to the fermentation medium a large amount of the nitrogen source, while maintaining constant the load of the carbon source that will be converted into proteins; and
- to stimulate the growth of the microalga.
It is a matter of modifying the carbon flux toward the production of proteins (and thus of biomasses), to the detriment of the production of storage lipids.
In the context of the invention, the Applicant company chose to explore a novel pathway by disclosing an alternative solution to that traditionally envisaged by the skilled person.
Thus, the invention relates to a method of protein enrichment of a microalga grown heterotrophically, said microalga being of the genusChlorella, more particularlyChlorella sorokinianaorChlorella protothecoides, said heterotrophic culturing method comprising a step aiming at limiting the growth of said microalga by means of a deficiency in the fermentation medium of a non-nitrogenous nutritional source.
This step is a heterotrophic culturing step where a non-nitrogenous nutritive factor is supplied in the medium in an amount that is insufficient to allow the microalga to grow. It should be noted that “amount that is insufficient” does not mean that this nutritive factor is not supplied. The result of this nutrient-deficient phase is to slow (to limit) cell metabolism, without inhibiting it completely.
In the meaning of the invention, “enrichment” refers to an increase in the protein content of the biomass of at least 15%, preferably at least 20% by weight, so that the protein content of the biomass reaches more than 50% by weight.
The invention covers more specifically a method of heterotrophic culturing of said microalgae comprising a step aiming at limiting the growth of said microalga by means of a deficiency in the fermentation medium of a non-nitrogenous nutritional source.
The present invention thus relates to a method of protein enrichment of a microalga grown heterotrophically, said microalga being of the genusChlorella, more particularlyChlorella sorokinianaorChlorella protothecoides, the method comprising heterotrophic culturing that includes a step aiming at limiting the growth of said microalga by means of a deficiency in the fermentation medium of a non-nitrogenous nutritional source, thus enabling the biomass protein content to reach more than 50% by weight.
By “deficiency in the fermentation medium of a non-nitrogenous nutritional source” is meant a culture wherein at least one of the non-nitrogenous nutritive factors is supplied to the microalga in an amount that is insufficient for it to grow.
In particular, the nutritional source is deficient so as to obtain a growth rate that is 10% to 60% lower than the growth rate with no limiting of said nutritional source. In particular, it is disclosed to decrease the growth rate by 10% to 60% compared with the growth rate with no limiting of glucose, in particular by 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50% or 55% compared with the growth rate with no limiting of glucose. Preferably, the growth rate is decreased by 15% to 55%.
The duration of the culturing phase comprising a deficiency of a nutritive factor, in particular of glucose, is at least 1 h, preferably at least 10 h, more preferably at least 20 h, in particular between 30 h and 60 h.
The result is an absence of residual non-nitrogenous nutritive factor in the culture medium, the microalga consuming this nutritive factor as fast as it is supplied. However, the absence of residual non-nitrogenous nutritive factor in the culture medium is distinguished from a situation in which the microalga is completely deprived of the nutritive factor.
In the context of the invention, the essential criterion is thus the limiting of cell growth induced by stress, namely cellular stress caused by the deficiency in the fermentation medium of a non-nitrogenous nutritive substance.
This strategy is thus quite counter to the technical prejudice according to which, in order to increase the protein content of the biomass, it is inevitably necessary to increase the biomass and thus increase cell growth.
By “a non-nitrogenous nutritional source” is meant a nutritive substance selected, for example, from the group consisting of glucose and phosphates.
As will be exemplified below, it may be advantageously chosen to limit the growth of:
- Chlorella sorokinianaby means of a glucose deficiency in the fermentation medium,
- Chlorella protothecoidesby means of a phosphate deficiency in the fermentation medium.
In particular, for these strains, the nutritive substance is supplied so as to obtain a growth rate of between 0.06 h−1and 0.09 h−1.
In a very specific embodiment, theChlorella sorokinianastrain is the strain UTEX 1663 (The Culture Collection of Algae at the University of Texas at Austin, USA). In a very specific embodiment, theChlorella protothecoidesstrain is the strain CCAP211/8D (The Culture Collection of Algae and Protozoa, Scotland, UK).
Optionally, the growth of said microalga can be limited by adding in the culture medium substances that inhibit cell growth, such as sulfates.
Furthermore, without being bound to any one theory, the Applicant company has found that the glucose flux in microalgae of the genusChlorella sorokinianais normally used according to a quite precise prioritization:
- 1. basal metabolism,
- 2. growth, i.e., formation of a protein-rich biomass,
- 3. storage substances (lipids and carbohydrates such as starch).
This principle explains the natural variations in protein content as the microalga grows, despite the constant supply of nitrogen.
The Applicant company has thus found that in order to enrich the microalgal biomass in proteins it is necessary to limit the growth of the microalga and to control its consumption of nutritive sources other than nitrogen, for example glucose, so as to:
- dedicate the entire consumption of glucose to protein production pathways,
- avoid the accumulation of storage substances such as lipids.
Indeed, avoiding a nitrogen deficiency makes it possible to prevent the diversion of metabolic fluxes toward the production of lipids.
Optionally, it may be advantageous to go so far as to completely block any synthesis of storage material, by the use of specific inhibitors.
Indeed, a certain number of inhibitors of the synthesis pathway for lipids, and even for starch (the storage carbohydrate par excellence of green microalgae), are known:
- for lipids, cerulenin is described as an inhibitor of fatty acid synthesis, and lipstatin, a natural substance produced byStreptomyces toxytricini, as an inhibitor of lipases, etc.;
- for starch, iminosugars (obtained by simple substitution of the endocyclic oxygen atom of sugars with a nitrogen atom) are historically known as powerful inhibitors of glycosidases, glycosyltransferases, glycogen phosphorylases and UDP-Galp mutase.
Thus, the method comprises the fermentation of a microalgal biomass under heterotrophic conditions with a first step of growing the biomass and a second step of depriving the fermentation medium of a non-nitrogenous nutritional source.
This second step makes it possible to enrich the biomass in protein. In particular, it makes it possible for the protein content of the biomass to reach more than 50% by weight (by weight of dry matter).
In a first preferred embodiment in accordance with the invention, the method for heterotrophically culturing said microalgae, in particularChlorella sorokiniana, comprises:
- a first step in which the microalgae are grown, where the glucose supply rate is adjusted to the consumption capacity of said microalgae so as to obtain a large biomass quickly,
- a second step in which the microalgae produce proteins, where the glucose supply rate is set to a value distinctly below the glucose consumption capacity of said microalgae so as to prevent the additional accumulation of storage substances or to promote their consumption.
As will be exemplified below, the first step in which the microalgae are grown is carried out in a discontinuous or “batch” mode in which the entirety of the initial glucose supply is consumed by the microalga, resulting in the production of a base biomass.
The second step in which proteins are produced is carried out under conditions in which:
- either: complete medium is supplied semi-continuously, using a so-called “fed-batch” system, after the initial glucose supply is consumed; the other operational parameters of the fermentation remain unchanged.
Glucose is supplied continuously and the supply rate is then lower than the strain's maximum rate of consumption so that the residual glucose content in the medium is kept at zero.
The strain's growth is thus limited by the availability of glucose (glucose-limiting condition).
- or: a continuous chemostat operation is used, in which the strain's growth rate (μ) is kept at its minimum value, the strain's growth being limited by the glucose supply.
This method of operation makes it possible to obtain a biomass with a high protein content thanks to the limiting of glucose and to the low growth rate imposed, all while ensuring very good productivity.
In a second preferred embodiment in accordance with the invention, the method for heterotrophically culturing said microalgae, in particularChlorella protothecoides, comprises a step in which the microalgae are grown, where a limiting of the phosphate supply limits the growth rate and results in an increase in the protein content. Thus, the heterotrophic culturing of microalgae of the speciesChlorella protothecoidescomprises a step of heterotrophic culturing with a deficiency of phosphates, the growth rate thus being reduced and resulting in an increase in the protein content.
The invention will be better understood with the aid of the following examples, which are meant to be illustrative and non-limiting.
The strain used is aChlorella sorokiniana(strain UTEX 1663—The Culture Collection of Algae at the University of Texas at Austin, USA).
Preculture:
- 600 ml of medium in a 2 l Erlenmeyer flask;
- Composition of the medium (Table 1 below)
| TABLE 1 |
| |
| Macroelements | Glucose | 20 |
| (g/l) | K2HPO4•3H2O | 0.7 |
| | MgSO4•7H2O | 0.34 |
| | Citric acid | 1.0 |
| | Urea | 1.08 |
| | Na2SO4 | 0.2 |
| | Na2CO3 | 0.1 |
| | Clerol FBA 3107 (defoamer) | 0.5 |
| Microelements | Na2EDTA | 10 |
| (mg/l) | CaCl2•2H2O | 80 |
| | FeSO4•7H2O | 40 |
| | MnSO4•4H2O | 0.41 |
| | CoSO4•7H2O | 0.24 |
| | CuSO4•5H2O | 0.24 |
| | ZnSO4•7H2O | 0.5 |
| | H3BO3 | 0.11 |
| | (NH4)6Mo7O27•4H2O | 0.04 |
| |
The pH is adjusted to 7 before sterilization by adding 8 N NaOH.
Incubation proceeds under the following conditions:
- duration: 72 h;
- temperature: 28° C.;
- shaking speed: 110 rpm (Infors Multitron incubator).
The preculture is then transferred to a 30 l Sartorius fermentor.
Biomass Production Culture:
The medium is identical to that of the preculture, but the urea is replaced with NH4Cl.
| TABLE 2 |
| |
| Macroelements | Glucose | 20 |
| (g/l) | K2HPO4•3H2O | 0.7 |
| | MgSO4•7H2O | 0.34 |
| | Citric acid | 1.0 |
| | NH4Cl | 1.88 |
| | Na2SO4 | 0.2 |
| | Clerol FBA 3107 (defoamer) | 0.5 |
| Microelements | Na2EDTA | 10 |
| (mg/l) | CaCl2 | 80 |
| | FeSO4•7H2O | 40 |
| | MnSO4•4H2O | 0.41 |
| | CoSO4•7H2O | 0.24 |
| | CuSO4•5H2O | 0.24 |
| | ZnSO4•7H2O | 0.5 |
| | H3BO3 | 0.11 |
| | (NH4)6Mo7O27•4H2O | 0.04 |
| |
The initial volume (Vi) of the fermentor is adjusted to 13.5 l after inoculation.
It is increased to a final volume of 16-20 l.
The operational parameters of the fermentation are as follows:
| pH | 5.0-5.2 using 28% NH3(w/w) |
| pO2 | >20% (maintained by shaking) |
| Shaking speed | Minimum 300 | rpm |
| Air flow rate | 15 | l/min |
| |
When the initially supplied glucose is consumed, a medium identical to the initial medium, without the defoamer, is supplied in the form of a concentrated solution containing 500 g/l of glucose and—in the same proportions relative to glucose as in the initial medium—the other elements, so as to obtain in the fermentor a glucose content of 20 g/l.
Two other identical additions are supplied in the same manner each time the residual glucose concentration becomes zero.
Clerol FBA 3107 defoamer is added as needed to avoid excessive foaming.
Results:
After 46 h of culturing, 38 g/l of biomass is obtained with a protein content (evaluated by N 6.25) of 36.2%.
In this example, a supply of complete medium (fed-batch mode) is started after the initially supplied glucose is consumed. The other operational parameters of the fermentation remain unchanged.
Glucose is supplied continuously using a 500 g/l concentrated solution. The supply rate is lower than the strain's maximum consumption rate so that the residual glucose content in the medium is kept at zero, i.e., the strain's growth is limited by the availability of glucose (glucose-limiting condition).
This rate increases exponentially over time. The formula used to calculate the addition flow rate is characterized by a factor μ corresponding to the growth rate that the strain can adopt if it consumes all the glucose supplied:
S=So×exp (μ·t)
- S=glucose supply flow rate (in g/h).
- So=initial glucose supply flow rate, determined according to the biomass present at the end of the batch. It is 12 g/h under our conditions.
- μ=flow rate acceleration factor. It should be below 0.11 h−1, which is the strain's growth rate in the absence of nutritional limiting.
- t=duration of the fed-batch operation (in h).
The salts are supplied continuously, if possible, separately or mixed with glucose. But they may also be supplied sequentially in several portions.
Table 4 below gives the salt requirements for 100 g of glucose.
| TABLE 4 |
| |
| Macroelements | Glucose | 100 |
| (g) | K2HPO4•3H2O | 6.75 |
| | MgSO4•7H2O | 1.7 |
| | Citric acid | 5.0 |
| | Na2SO4 | 1.0 |
| Microelements | Na2EDTA | 50 |
| (mg) | CaCl2•2H2O | 400 |
| | FeSO4•7H2O | 200 |
| | MnSO4•4H2O | 2.1 |
| | CoSO4•7H2O | 1.2 |
| | CuSO4•5H2O | 1.2 |
| | ZnSO4•7H2O | 2.5 |
| | H3BO3 | 0.6 |
| | (NH4)6Mo7O27•4H2O | 0.2 |
| |
The concentrations of the elements other than glucose were determined so as to be in excess relative to the strain's nutritional requirements.
Clerol FBA 3107 defoamer is added as needed to avoid excessive foaming.
Results: Effect of the Glucose Supply Rate During the Fed-Batch Operation
Tests were carried out at various glucose supply rates in fed-batch mode. They are characterized by the μ applied. The biomass protein content obtained is evaluated by measuring the total nitrogen expressed in N 6.25.
| TABLE 5 |
|
| μ fed | Duration | Biomass | Productivity | |
| Test | (h−1) | (h) | (g/l) | (g/l/h) | % N 6.25 |
|
|
| 1 | 0.06 | 78 | 43.6 | 0.56 | 49.2 |
| 2 | 0.07 | 54 | 35.1 | 0.65 | 43.1 |
| 3 | 0.09 | 48 | 64.9 | 1.35 | 39.3 |
|
These results show that glucose-limiting makes it possible to increase the protein content.
Indeed, it is observed that, even with a high μ of 0.09, the protein content obtained is higher than that obtained without limiting, as in Example 1 (39.3% versus 36.2%).
Tighter limiting of the metabolism by means of glucose results in an additional increase in protein content.
Under these test conditions, it is necessary to impose on the strain a μ below 0.06 h−1in order to obtain a protein content above 50%.
It should be noted that this condition goes hand in hand with a decrease in productivity: 0.56 g/l/h versus 1.35 g/l/h in test 3.
In this example, a 2 l Sartorius Biostat B fermentor is used.
Fermentation is carried out as in Example 2, but with volumes 1/10 the size: the volume of inoculum is 60 ml and the initial volume is 1.35 l.
The continuous supply of medium is started according to the same principle as in Example 2, the salts being in this case mixed with glucose in the feed tank. The supply rate is accelerated according to the same exponential formula as in Example 2 by applying a p of 0.06 h−1.
Chemostat
When a volume of 1.6 l is reached (a biomass concentration of about 50 g/l), the continuous chemostat-type operation begins:
1. The fermentor is fed continuously at a flow rate of 96 ml/h with a nutritive medium solution, containing 100 g/l of glucose, of the following composition:
| TABLE 6 |
| |
| Macroelements | Glucose | 100 |
| (g/l) | K2HPO4•3H2O | 6.75 |
| | MgSO4•7H2O | 1.7 |
| | Citric acid | 5.0 |
| | Na2SO4 | 1.0 |
| Microelements | Na2EDTA | 50 |
| (mg/l) | CaCl2•2H2O | 400 |
| | FeSO4•7H2O | 200 |
| | MnSO4•4H2O | 2.1 |
| | CoSO4•7H2O | 1.2 |
| | CuSO4•5H2O | 1.2 |
| | ZnSO4•7H2O | 2.5 |
| | H3BO3 | 0.6 |
| | (NH4)6Mo7O27•4H2O | 0.2 |
| |
The concentrations of the elements other than glucose were determined so as to be in excess relative to the strain's nutritional requirements.
2. Medium is removed continuously from the fermentor by means of a siphon tube connected to a pump, so as to keep the culture volume at 1.6 l.
Thus, a 0.06/1 fraction (6%) of the medium is replaced per hour. This replacement rate is called the dilution rate (D).
In accordance with the principle of the chemostat culturing method, the strain's growth rate (μ) is established at the same value because the strain's growth is limited by the glucose supply:
D=μ=0.06 h−1
Results
After 97 h of operation in chemostat mode, the biomass concentration stabilizes at 48 g/l±2 g/l and the protein content at 53±2%.
This mode of operation makes it possible to obtain a biomass with a high protein content thanks to the limiting of glucose and to the low growth rate imposed, all while ensuring very good productivity, of about 2.9 g/l/h, thanks to the high concentration of biomass.
The strain used isChlorella protothecoides(strain CCAP21 1/8D—The Culture Collection of Algae and Protozoa, Scotland, UK).
Preculture:
- 150 ml of medium in a 500 ml Erlenmeyer flask;
- Composition of the medium: 40 g/l of glucose+10 g/l of yeast extract.
Incubation proceeds under the following conditions: duration: 72 h; temperature: 28° C.; shaking speed: 110 rpm (Infors Multitron incubator).
The preculture is then transferred to a 2 l Sartorius Biostat B fermentor.
Biomass Production Culture:
The composition of the culture medium is as follows (in g/l):
| TABLE 7 |
| |
| Glucose | 80 |
| Citric acid | 4 |
| NH4CL | 2 |
| KH2PO4 | 2 (test 1) |
| | or 3 (test 2) |
| Na2HPO4 | 2 (test 1) |
| | or 3 (test 2) |
| MgSO4, 7H2O | 1.5 |
| NaCl | 0.5 |
| Yeast extract | 5 |
| |
The phosphate supply is calculated so as to be limiting in test 1 and in excess in test 2. Clerol FBA 3107 defoamer is added as needed to avoid excessive foaming. The initial volume (Vi) of the fermentor is adjusted to 1 l after inoculation.
The operational parameters of the fermentation are as follows:
| pH | 6.5 using 28% NH3(w/w) |
| pO2 | >20% (maintained by shaking) |
| Shaking speed | Minimum 200 | rpm |
| Air flow rate | 1 | l/min |
| |
Results:
| TABLE 9 |
|
| Duration | Biomass | Cumulative | Residual | % N |
| Test | (h) | (g/l) | μ (h−1) | PO4(mg/l) | 6.25 |
|
|
| 1 | 45 | 36.5 | 0.07 | 0 | 56.1 |
| 2 | 36 | 38.1 | 0.09 | 800 | 48.1 |
|
These results show that a limiting of the phosphate supply, confirmed by the absence of residual phosphate at the conclusion of the fermentation, limits the growth rate (measured by the cumulative μ) and, like the limiting of glucose in the preceding examples, results in an increase in the protein content reaching values distinctly greater than 50%.