WO2004072292A1 - Procede et dispositif pour la production de biomolecules en continu - Google Patents
Procede et dispositif pour la production de biomolecules en continu Download PDFInfo
- Publication number
- WO2004072292A1 WO2004072292A1 PCT/CA2004/000184 CA2004000184W WO2004072292A1 WO 2004072292 A1 WO2004072292 A1 WO 2004072292A1 CA 2004000184 W CA2004000184 W CA 2004000184W WO 2004072292 A1 WO2004072292 A1 WO 2004072292A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- membrane
- filtration
- bioreactor
- culture medium
- target
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P21/00—Preparation of peptides or proteins
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07K—PEPTIDES
- C07K1/00—General methods for the preparation of peptides, i.e. processes for the organic chemical preparation of peptides or proteins of any length
- C07K1/14—Extraction; Separation; Purification
- C07K1/34—Extraction; Separation; Purification by filtration, ultrafiltration or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P21/00—Preparation of peptides or proteins
- C12P21/02—Preparation of peptides or proteins having a known sequence of two or more amino acids, e.g. glutathione
Definitions
- the present invention relates to a method and a device used for the production of recombinant biomolecules.
- this method and this device allow the production of biomolecules continuously, using growing microorganisms in a bioreactor and a means of continuously taking a defined amount of suspension of microorganisms to subject it, continuously, to stages of filtration allowing the production of purified or concentrated biomolecules.
- Biotechnology represents a most important strategic research area.
- the major biotechnology companies identified produce recombinant bioreactors for the production of recombinant or natural biomolecules with high added value.
- biological molecules essentially protein
- HLA high-density lipoprotein
- P53 molecules high-density lipoprotein
- interferons anti-carcinogenic
- insulin antibiotics
- the first bioreactors with membranes combined the purification capacity of microorganisms and the separation possibilities of membrane filtration techniques. It is based on the use of a membrane bioreactor where secondary settling is replaced by tangential microfiltration. Filtration allows the retention of suspended particles depending on their size.
- the characteristic of the process is that it is compact and modular.
- Batch production has several disadvantages compared to continuous production. The most important consist in the operating costs which are more expensive compared to a production in continuous mode, the lower production yield, longer maintenance and preparation (monitoring) times and consequently times of use. shorter. This last point translates into higher capital costs. Finally, the continuous mode ensures a greater production capacity than the batch mode. In the case of this platform, the optimized continuous production capacity is more than five (5) times higher than that of batch production.
- a first object of the present invention consists of a process for the continuous production of biomolecules of interest produced by microorganisms.
- this process comprises the following stages: a) growing microorganisms expressing the recombinant biomolecules of interest in a bioreactor; b) transferring a portion of the suspension of producer microorganisms and a fraction of the medium into a container; c) separating and concentrating the microbial biomass from the culture medium resulting from biofermentation; in the case of exogenous molecules, the recombinant biomolecules produced are found in the filtration permeate; in the case of endogenous molecules, the biomolecules are released by cell lysis (sonication).
- the membrane filtration sequence (s) consist of separating, concentrating and purifying the recombinant biomolecules of interest from the substances and other nutrients composing the medium (amino acids, organic acids, mineral elements, etc.); in the case of non-secreted molecules (endogenous), the biomolecules of interest are released from the cell compartments by lysis (sonication) and the membrane filtration sequences, consist in a first step in separating the biomolecules of interest from the cell lysate ( cell debris, constituent proteins, etc.) and in a second step to separate, concentrate and purify the biomolecules of interest from the remaining medium (permeate from the first filtration step); and e) harvesting the biomolecules of interest.
- the invention also relates to a device for the continuous production of microbial biomolecules comprising: a) a bioreactor; b) a source of nutrients, and a means for introducing said nutrients into the bioreactor; c) a means of aerating the bioreactor; d) a means for agitating the bioreactor; e) a first transient tank and a means of introducing the suspension of producer microorganism into said transient tank; f) a first filtration means and a means for introducing the suspension of microorganisms into the first filtration means from the first transient tank; g) a second reservoir for the suspension of biomolecules and a means of introducing the suspension of biomolecules into the reservoir after a first filtration; h) a second filtration means and a means for introducing the suspension of biomolecules having undergone a first filtration into the second filtration means from the second reservoir; and i) a third reservoir for the suspension of biomolecules of interest and means for introducing
- Another object of the present invention consists in a process for the continuous production and n of target polypeptides by a microorganism comprising the steps of: a) allowing the growth of a microorganism producing at least one target polypeptide in a bioreactor supplied with medium growing independently over a predetermined period of time; b) allow a portion of the culture medium to be transferred independently in a first container, so that this container promotes the accumulation of volumes withdrawn from the bioreactor in compensation for the volumes of fresh medium added continuously, the container being refrigerated at 4 ° C to allow the accumulation and residence of a mixture of cells and culture broth before their sonication, a second refrigerated container of the same capacity and nature as the first container used for storage at 4 ° C of the mixture after sonication; c) autonomously inducing the separation of the target polypeptides from the portion of the culture medium by at least one passage through at least one first membrane, chosen (nature and cutoff threshold) according to the filtration objectives, the characteristics of the solution
- Said bioreactor can be an external membrane bioreactor.
- the target polypeptides are preferably native or recombinant proteins and are produced in the culture medium or endogenously, that is to say that they are accumulated, in the producer cell. They can be selected from enzymes, transport proteins, antioxidant proteins or food proteins.
- microorganisms which can be used to carry out the present invention can be chosen from the group of bacteria, yeasts, molds, viruses, a protozoan, a fungus, or even a yeast, a plant cell, an animal cell, or an insect cell.
- the growth of the producer cells preferably corresponds, but not limitatively, to a point at the end of the logarithmic growth phase, with an optical density (OD) of 1.8, at a concentration of 0.2 ⁇ 10 10 cells per milliliter, this cell concentration being obtained between 7 and 8 hours after the start of the biofermentation and 2 hours after the departure of the pumps provided for transfers between the bioreactor and the first and second containers, the starting of the pumps for adding fresh medium being carried out at a flow rate of 37 ml / min, for the type of fermenter used, and purging at an equivalent flow rate having been optimized and the average time for starting the pumps was determined at 5.30 am after the start of fermentation , the OD being equal to 1.5, the OD and the cell concentration remaining stable and constant (variability ⁇ 10% calculated on the basis of 30 fermentations) throughout the bioferment production stage Eur.
- a device for the continuous production of at least one target polypeptide comprising:
- a source of culture medium and nutritive substrates and a means allowing them to be introduced into the bioreactor; - a means of aerating the bioreactor;
- a first reservoir intended for the sterile conservation of the culture medium and a means for allowing its transfer autonomously and continuously into said bioreactor; - at least a first filtration means (microfiltration) and a means of separating the cells (biomass) in the concentrate of the partially consumed culture medium (permeate) by a filtration means (microfiltration) from the biofermenter; means ensuring that after the membrane separation, the concentrate remains in the first reservoir and the permeate is conveyed to a second reservoir, this second reservoir being arranged to form a suspension of filtered target polypeptide;
- Said bioreactor is preferably, but not limited to, an external membrane bioreactor, the first filtration means a membrane, membrane a ceramic membrane, the second filtration means also a membrane, which may alternatively be or cumulatively or in combination a microfiltration, ultrafiltration, nanofiltration, reverse osmosis or dialysis membrane.
- Fig. 1 shows a diagram illustrating a device for producing recombinant biomolecules which can be used for carrying out the present invention.
- Fig. 2 illustrates a device for producing recombinant molecules expressed in the intracellular compartments of bacteria
- Fig 3 illustrates a diagram of different stages of filtration allowing the separation, the concentration and the purification of a molecule produced in an endogenous way in a bacterium
- Fig. 4 illustrates an example of a diagram of different filtration steps allowing the separation, the concentration and the purification of a secreted molecule
- Fig. 5 illustrates the evolution of the permeate flow rate as a function of the concentration rate during the separation of cellular debris
- Fig. 6 illustrates the evolution of the permeate flow as a function of the concentration rate during separation of GFP
- Fig. 7 illustrates the evolution of the total proteins and of the TOC in the concentrate during the diafiltration.
- the technology used is based on the production of microorganisms producing the biomolecules of interest and on the extraction / purification of these biomolecules by filtration on membranes. These two technologies are combined to develop a technological platform for production and extraction / purification.
- the production / separation system of the present invention is preferably composed of a series of process and technology sequences making it possible to produce, extract and purify, continuously or without interruption, the protein molecules of interest at using a bioreactor coupled with membrane technologies.
- Membrane technologies which include microfiltration, ultrafiltration, nanofiltration and reverse osmosis, once the molecule has been produced and secreted in the medium, have the function of separating, extracting and purifying it according to desired parameters. purity. Those skilled in the art will understand that these methods can also be used when the microorganisms have undergone prior lysis.
- the system can be used for the continuous production of exogenous and / or endogenous biomolecules for various applications, biopesticides (bactericides, fungicides, etc.), nutraceuticals and functional foods (probiotics), agro-food (additives, food supplements, enzymes , digestive aids, etc.) and pharmaceuticals.
- biopesticides bactericides, fungicides, etc.
- nutraceuticals and functional foods probiotics
- agro-food additives, food supplements, enzymes , digestive aids, etc.
- the present invention does not show any return of bacteria in the fermenter (bioreactor).
- the claimed production system is continuous, while the systems used in the treatment of wastewater are stopped when the sludge matures, that is to say when the biological treatment has come to an end. In this case, we speak of a fermentation in batch mode.
- the microbial strains found in the treatment of wastewater are heterogeneous while the biological systems used for the growth and production of biomolecules continuously are pure strains and, in the majority of cases, preferentially recombinant. Continuity of growth and production is ensured by coupling the bioreactor and the membranes, the latter being arranged either in series or in parallel, as required (system with variable geometry).
- the nutrients are continuously added to the bioreactor and an equivalent volume of culture broth is taken synchronously to be conveyed to the membrane filtration system.
- the nature of the molecules of interest which can be produced by the method and the system of the present invention are essentially protein molecules. These can be food proteins or those with biological activity such as enzymes (proteases, lipases, dehydrogenase, oxidase, etc.) or transport proteins (hemoglobin, myoglobin, transferin) or antioxidants (cosmetics). Recombinant proteins from the food industry offer great potential.
- a single-cell fermenter is optimized for continuous production of protein molecules. The extraction is carried out using a membrane system in order to separate the molecules from the producing cells.
- the determination of the factors allowing the continuous operation of the bioreactor, its control and its optimization, are based on the following parameters: pH, temperature, oxygen diffusion, dilution volumes, etc.
- the ensuing phase taking into account the choice of membrane made beforehand, makes it possible to extract, concentrate and purify the biomolecule produced.
- the biological molecules that the system can produce are the molecules secreted in the medium and the molecules not secreted.
- the separation, concentration and purification of the secreted biomolecules does not require a continuous cell lysis step, whereas such a step is required for the treatment of non-secreted molecules.
- the bioreactor must contain the microorganisms which produce the biomolecules to be extracted and purified;
- Ventilation should be optimized according to the mode and respiratory rate of the microorganisms;
- the reactor must be equipped with a system, the shape of which, preferably but not limited to cylindrical geometry, has been optimized as a function of the production system to be used in order to provide optimum agitation and homogenization of the medium and good diffusion of l oxygen therein;
- the pressure pump can be of different types but a centrifugal type pump gives the best results.
- the outer membranes are chosen according to the biomolecule that we want to extract.
- the first membrane sequence is a membrane chosen at a cutoff threshold which allows the biomolecule to pass, but which retains cells and other large compounds.
- the membrane used is preferably a ceramic membrane because they are very resistant membranes. In fact, they can easily be sterilized thermally or chemically. They can be easily cleaned with chemicals or by pressure reversal (sending air or water). These are qualities that are not found in conventional organic membranes. In addition, these membranes are autoclavable.
- the cutoff threshold is strict. A ceramic membrane with a cutoff threshold of one micron will not allow any molecule larger than one micron to pass through. Conversely, polymeric membranes may allow a few particles of one micron to pass through. This notion is very important when talking about the profitability of extraction. Finally, the ceramic membranes are certified safe in the food industry, cosmetics, nutraceuticals and are pharmaceutical grade.
- the first filtration produces two fractions: a concentrate composed mainly of cells and a permeate composed of all the molecules not retained by the membrane.
- a concentrate composed mainly of cells
- a permeate composed of all the molecules not retained by the membrane.
- biomolecules of interest are found completely in the permeate.
- the biomolecules of interest are found in the concentrate (in the cell compartments).
- Their release is carried out by cell lysis (sonication) and their extraction is carried out by membrane filtration which consists in separating the lysate into a concentrate (composed mainly of cellular debris and molecules of high molecular weight) and a permeate which contains the molecule target and the set of substances that cross the membrane.
- the first filtration allows on the one hand to reduce the costs of lysis (sonication) and on the other hand to remove a large part of the organic and mineral substances present from the broth of fermentation.
- the membranes used during this extraction step do not have the significant separation power of the target biomolecules in order to reduce the losses in target product.
- the concentration and the purification which follow the extraction can be carried out according to different membrane techniques which can partially or totally ensure the purification at the targeted level.
- Diafiltration is a purification operation which consists, once the desired concentration level has been reached, of continuing filtration by adding concentrate of a diafiltration solution to the tank. This can be either demineralized water or a buffer solution.
- the addition of the diafiltration solution can be continuous (at a rate equivalent to that of the permeate extracted) or batchwise (addition to the concentrate and extraction by the permeate of successive equal volumes).
- the concentration of target molecule remains constant (the target molecule does not pass through the membrane and the volume of the concentrate does not change) and the compounds not retained by the membrane will continue to pass into the permeate. This therefore results in an increase in the degree of purity.
- the purification must be optimized in order to use as few chemicals as possible. Among the membrane techniques used in this platform, we find microfiltration, ultrafiltration and nanofiltration.
- the finished product must consist of purified and concentrated biomolecules.
- the concentrate should contain microorganisms and nutrients in high concentrations.
- the pH, temperature, agitation and dissolved oxygen are also optimized.
- a culture medium comprising a suspension of microorganisms 5 is stored in a bioreactor 1. Nutrients are added to the suspension of microorganism 5 in the bioreactor through a conduit 3. An aerator 2 and an agitator 4 respectively provide aeration adapted to the microorganism and the homogeneity of the suspension of microorganisms 5.
- a pump 7 ensures the transfer of a portion of the suspension of microorganism 5 into a transient tank 9 through a conduit 25.
- a conduit 39 located at the lower end of the transient tank 9 and a pump 13 ensure the continuous transfer of the suspension to be purified to a primary filtration membrane 15.
- the concentrate of microorganisms is conveyed to the transient tank 9 through a conduit 27 while the permeate is directed to a primary filtrate reservoir 17 through a conduit 29.
- the primary filtrate 41 is conveyed by a conduit 35 and a pump 23 to a second filtration membrane 19.
- the concentrate is conveyed to the primary filtrate reservoir 17 by a conduit 31 while the permeate is conveyed to the final solution reservoir 21 by a conduit 33.
- the solution produced is composed of cells, various metabolites, nutrients not consumed, etc. Since GFP (target molecule) is endogenous, it is found inside cells.
- the objective of membrane filtration aims to separate, concentrate and purify the target molecule (GFP). As shown in Fig. 3, the separation, concentration and purification process by membrane filtration is composed of the following steps:
- Step 1 Concentration and separation of cells from the rest of the medium.
- Step 2 Lysis of cells to release GFP from cell compartments.
- Step 3 Separation of cellular debris and macromolecules.
- Step 4 Concentration of GFP and purification by diafiltration.
- the membrane filtration sequences to achieve separation, concentration and purification are reduced to two stages (Fig. 4).
- the first consists in the separation of cells and molecules of high molecular weight.
- the target molecule is in the permeate.
- the second filtration step is a concentration of ⁇ -lactamase followed by a diafiltration to increase its purity.
- the membranes used in the various filtration stages are ceramic membranes. This type of membranes is characterized by a high resistance to chemicals and to temperature and therefore they meet the requirements of bioprocesses (disinfection and sterilization).
- the membrane used in the first filtration step is a microfiltration membrane with a pore size of 0.2 ⁇ m.
- the separation of cellular debris and macromolecules (step 3) was carried out on a 300 kD membrane cut-off threshold (MWCO).
- Concentration and purification (steps 4) were carried out on an ultrafiltration membrane with a cutoff threshold of 15kD. This membrane makes it possible to effectively concentrate (little loss) the target molecule and it lets through a large proportion of dissolved matter of low molecular weight.
- the membranes used come from the company TAMI.
- the membranes used have an outside diameter of 2.5 cm (23 channels) and a length of 1.1 m.
- the filtering surface is 0.35 m.
- the concentration of the cells by membrane filtration was carried out at an average pressure of 16 psi (or 110 kPa), at a feed rate of approximately 20 l / min and at a temperature of 7 ⁇ 1 ° C.
- the separation of cellular debris was carried out at 6.2 psi (42 kPa), at a feed rate of 2 1 / min and at a temperature of 7 ⁇ 1 ° C.
- GFP concentration and diafiltration were carried out at an average pressure of 7.5 psi (52 kPa), at a feed rate of 2 1 / min and at a temperature of 7 ⁇ 1 ° C.
- the average pressure is calculated from the measurements of the pressure at the inlet and the outlet of the membrane module. All tests filtration were carried out at constant pressure. However, the filtration system used can be operated either at constant pressure (clogging results in a reduction in the permeate flow), or at constant permeate flow (in this case, the clogging effect is compensated by an increase in pressure).
- Each membrane filtration operation included the following steps:
- the lysis of the cells was carried out using a continuous sonication device.
- the optimal sonication conditions adopted are: an intensity of 100% and. a residence time of 4 minutes. These conditions correspond to the best rate of lysis of the cells present in the concentrate without affecting the integrity of the target molecule (GFP).
- the growth of the fermenting cells as well as the separation and the concentration of the cells by membrane filtration were determined from the optical density measurements at the wavelength of 600 nm made using a Pharmacia spectrophotometer. Biotech Novaspec II. The effectiveness of this rapid method of analysis has been validated by agar culture tests.
- the determination of the cells in the microfiltration permeate (step 1) was carried out by culture on agar, due to the low values of optical density (OD at 600 nm) obtained.
- the performance of membrane processes with regard to the separation, concentration and purification of GFP was determined by fluorescence measurements.
- the device used is a luminotox TM from the company Lab-Bell TM.
- the Rushton blades which have a higher shear factor than the propeller blades ensure a more homogeneous distribution of the air and consequently of the oxygen (the percentage of diffusion of oxygen is higher with the blades Rushton), the bubbles generated by this type of agitation are small and better distributed compared to the other types tested.
- the diffusion of oxygen that results from the use of Rushton blades has resulted in faster growth kinetics than those obtained with propeller blades.
- the mixed blades give intermediate growth kinetics, between those obtained with the Rushton blades and the propeller blades.
- the aeration of the fermenter was ensured by a pump of Maxima R type.
- the aeration rates which were tested are 2L / min, 3.5L / min and 6L / min.
- the flow rate of 6 1 / min gave the best results translated into growth rate and quantity of ⁇ -Lactamase and of GFP produced continuously.
- the production of ⁇ -Lactamase was substantially equivalent in the case of a flow rate of 3.5 and 61 / min.
- the first stage of membrane filtration is microfiltration which consists in separating the cells from the rest of the solution. This filtration therefore produces a concentrate (mainly composed of cells) and a permeate, composed of all the substances not retained by the microfiltration membrane (buffer, nutrients, etc.). The target molecule, being endogenous, it is therefore at this stage of the operation inside the cells.
- the membrane used in this filtration step is a ceramic membrane with a pore size of 0.2 ⁇ m.
- the diafiltration volume was set at twice the volume of the concentrate (ie 30 liters). Table 1 summarizes the results of this operation.
- the results (table 1) show that the concentration of the cells is complete, it corresponds to the concentration rate determined from the volumes (initial volume / volume of the concentrate).
- the DO concentration at 600nm is lower, which indicates that part of the dissolved matter has been removed (approximately 20% of the DO at 600nm).
- the removal of the TOC is 87%.
- the OD at 600nm further decreases under the effect of the diafiltration, thereby improving the rate of removal of dissolved matter present in the cell concentrate (removal of 30% of the initial OD).
- the filtration of the culture broth leads to a rapid drop in the permeate flow rate by more than 90% compared to the flow rate measured with demineralized water (including the effect of viscosity since the permeability to demineralized water was carried out at 25 ° C.). This rapid loss is followed by a slight gradual drop in the permeate flow under the effect of the concentration.
- the permeate flow varied between 24 l / m 2 / h at the start of the concentration and around 17 l / m 2 / h at the end of the concentration.
- the clogging is reversible in nature since rinsing with water made it possible to recover approximately 50% of the permeability of the membrane and washing with a sodium hypochlorite solution completely restored the initial permeability of the membrane.
- step 2 Cell lysis by sonication
- This step consists of a lysis of cells to release GFP (endogenous molecule) from cell compartments.
- the process used to carry out cell lysis is sonication.
- the sonication parameters (sonication intensity and time) have been optimized so as to obtain the best lysis yields while preserving the integrity of the target molecule (GFP).
- the sonication was carried out on the cell concentrate produced in the first filtration (step 1) to which a resuspension buffer (PI buffer: Tris-HCl, 500mM, pH 8; EDTA lOOmM; Sodium azide ⁇ .2% (P / N)) is added.
- the volume of the buffer represents 10% of the total volume of the solution.
- the sonication performance results are summarized in Table 2.
- the sonication conditions applied allowed the lysis of 83% of the cells.
- the results show a release of a large quantity of proteins (measurement of proteins total) and an increase in organic carbon (part of the TOC is provided by the buffer) in the lysate. It should be noted that the TOC and total protein measurements were carried out after centrifugation of the samples at 14000 g for 20 minutes.
- step 2 After the release of the target molecule from the cell compartments (step 2), the solution undergoes a second membrane filtration whose objective is to separate the cellular debris and the molecules of high molecular weight from the rest of the solution. This filtration therefore produces a concentrate, composed essentially of cellular debris, and a permeate containing the target molecule is the rest of the compounds of low molecular weights.
- FIG. 3 shows the evolution of the permeate flow as a function of the concentration rate (initial volume / volume of the concentrate) during filtration.
- the permeate flow is characterized by a rapid drop of more than 90% (including the viscosity effect due to the fact that the measurement of the permeability to demineralized water in summer performed at 25 ° C) after a few minutes of filtration (compared to that measured with demineralized water). Then there is a gradual decrease with the increase in the concentration rate which stabilizes around 41 / m 2 / h.
- the permeability of the membrane was restored to its initial level by chemical washing (sodium hypochlorite solution).
- This filtration step aims on the one hand to concentrate the GFP and on the other hand to increase the purity by diafiltration.
- the objective of the concentration operation is to reduce the volume of the solution with a minimum loss of the target molecule (GFP).
- the choice of the most suitable membrane for carrying out this operation corresponds to that which allows effective concentration of the target molecule (minimizing losses) and removal of the maximum impurity.
- the results obtained are summarized in the table. We can note the efficiency of the membrane used to concentrate GFP (loss rate of about 7%). In addition, the membrane allowed the removal of 87% of the TOC present in the initial solution.
- the evolution of the permeate flow as a function of the concentration rate is characterized by a rapid drop of approximately 84% (compared to the pemeat flow measured with demineralized water at the same pressure and at a temperature of 25 ° C) followed by a slight gradual decrease under the effect of concentration.
- the permeate flow stabilizes around 31 / m 2 / h (pressure of 7.5 psi and a temperature of 7 ⁇ 1 ° C).
- the purification by diafiltration is carried out on the same filtration system of step 4 (Fig. 1). Once the desired concentration rate is reached (step 4), we start filtration in diafiltration mode.
- This consists of adding a buffer solution to the concentrate of the concentrate (TE: Tris-HCl, 10mM, pH8; EDTA, ImM; Sodium azide 0.02%).
- TE Tris-HCl, 10mM, pH8; EDTA, ImM; Sodium azide 0.02%.
- the objective of diafiltration is to increase the degree of purity of the target molecule (GFP) in the concentrate.
- GFP target molecule
- the role of the buffer is to preserve the integrity and stability of GFP.
- Table 5 show the characteristics of the concentrate before and after diafiltration.
- FIG. 9 shows the evolution of TOC and of total proteins in the concentrate as a function of the volume of diafiltration.
- Microfiltration on a 0.2 ⁇ m porosity membrane makes it possible to concentrate all of the cells present in the fermentation broth and to considerably reduce the volume of the solution. It also leads to the removal of a significant part of the dissolved matter (20% of the DO at 600nm and 87% of the TOC). In addition, removal rates of dissolved material can be increased by diafiltration.
- 300kD leads to the total removal of cellular debris (total elimination of the DO at 600nm). In addition, it retains 41% of total protein and 16% of TOC, compared to centrifugation at 14000g for 20 minutes.
Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/545,272 US20060172376A1 (en) | 2003-02-11 | 2004-02-11 | Method and device for the continuous production of biomolecules |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US44627403P | 2003-02-11 | 2003-02-11 | |
US60/446,274 | 2003-02-11 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2004072292A1 true WO2004072292A1 (fr) | 2004-08-26 |
Family
ID=32851025
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CA2004/000184 WO2004072292A1 (fr) | 2003-02-11 | 2004-02-11 | Procede et dispositif pour la production de biomolecules en continu |
Country Status (3)
Country | Link |
---|---|
US (1) | US20060172376A1 (fr) |
CA (1) | CA2457262A1 (fr) |
WO (1) | WO2004072292A1 (fr) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
HUE027136T2 (en) * | 2004-09-30 | 2016-08-29 | Bayer Healthcare Llc | Tools and procedures for the integrated, continuous production of biological molecules |
EP2682168A1 (fr) | 2012-07-02 | 2014-01-08 | Millipore Corporation | Dispositif de tirage et métier à filer |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4766205A (en) * | 1985-11-13 | 1988-08-23 | Beatrice Companies, Inc. | Method for isolation of recombinant polypeptides in biologically active forms |
-
2004
- 2004-02-11 US US10/545,272 patent/US20060172376A1/en not_active Abandoned
- 2004-02-11 WO PCT/CA2004/000184 patent/WO2004072292A1/fr active Application Filing
- 2004-02-11 CA CA002457262A patent/CA2457262A1/fr not_active Abandoned
Non-Patent Citations (3)
Title |
---|
BERTHOLD WOLF ET AL: "Interaction of cell culture with downstream purification: A case study", CYTOTECHNOLOGY, vol. 15, no. 1-3, 1994, pages 229 - 242, XP008031410, ISSN: 0920-9069 * |
KLINSPOHN U ET AL: "INTEGRATED ENZYME PRODUCTION IN CONTINUOUS OPERATION BY UTILIZATIONOF POTATO PULP", JOURNAL OF BIOTECHNOLOGY, ELSEVIER SCIENCE PUBLISHERS, AMSTERDAM, NL, vol. 29, no. 1/2, 1 May 1993 (1993-05-01), pages 109 - 119, XP000609000, ISSN: 0168-1656 * |
MAYER A F ET AL: "AN EXPRESSION SYSTEM MATURES: A HIGHLY EFFICIENT AND COST-EFFECTIVE PROCESS FOR PHYTASE PRODUCTION BY RECOMBINANT STRAINS OF HANSENULA POLYMORPHA", BIOTECHNOLOGY AND BIOENGINEERING. INCLUDING: SYMPOSIUM BIOTECHNOLOGY IN ENERGY PRODUCTION AND CONSERVATION, JOHN WILEY & SONS. NEW YORK, US, vol. 63, no. 3, 1999, pages 373 - 381, XP000853785, ISSN: 0006-3592 * |
Also Published As
Publication number | Publication date |
---|---|
CA2457262A1 (fr) | 2004-08-11 |
US20060172376A1 (en) | 2006-08-03 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US20080213868A1 (en) | Concentrated aqueous suspensions of microalgae | |
US20120094361A1 (en) | Method of Separation of Algal Biomass from Aqueous or Marine Culture | |
FR2656874A1 (fr) | Procede de production et d'extraction d'anti-oxydants a partir d'une culture de micro-organismes et photobioreacteur pour la mise en óoeuvre de ce procede. | |
KR102567418B1 (ko) | 세포 배양 시스템 및 세포 배양 방법 | |
FR2836910A1 (fr) | Procede de degradation de la matiere organique par voie mycelienne | |
EP3022289A1 (fr) | Procédé optimise de rupture des parois de chlorelles par homogénéisation a très haute pression | |
FR2599625A1 (fr) | Procede de production d'activateur du plasminogene biologiquement actif | |
EP2996991B1 (fr) | Procédé et dispositif de traitement d'une biomasse mélangée à de l'eau pour produire de l'eau potable, du biogaz et des matières sèches combustibles | |
Ortiz Tena et al. | Characterization of an aerated submerged hollow fiber ultrafiltration device for efficient microalgae harvesting | |
CH680985A5 (fr) | ||
Rossi et al. | Harvesting of cyanobacterium Arthrospira platensis using inorganic filtration membranes | |
WO2004072292A1 (fr) | Procede et dispositif pour la production de biomolecules en continu | |
EP2512258B1 (fr) | Procede pour reduire la teneur bacterienne d'un milieu alimentaire et/ou biologique d'interet, contenant des gouttelettes lipidiques | |
Taddei et al. | Yeast cell harvesting from cider using microfiltration | |
EP1092471A1 (fr) | Adjuvant de filtration de liquides et son utilisation pour la décontamination microbienne | |
Mondal et al. | Partial refinement of fungal chitinase (Beauveria bassiana) with multistage membrane filtration | |
Khan et al. | Pilot-scale crossflow ultrafiltration of four different cell-sized marine microalgae to assess the ultrafiltration performance and energy requirements | |
WO2023118401A1 (fr) | Procede de captation des phytotoxines dans un reacteur biologique | |
CN111183217A (zh) | 用于收获微藻的方法 | |
FR2660932A1 (fr) | Procede et dispositif de fermentation semi-continue, notamment pour la fabrication d'un melange biologique a base d'acide propionique. | |
WO2024088564A1 (fr) | Fraction hydrosoluble de plantes limpide | |
FR2731162A1 (fr) | Procede d'extraction d'au moins un actif a partir de cellules vegetales indifferenciees | |
JP2018050498A (ja) | 細胞培養用中空糸膜及び細胞培養方法 | |
RU2190014C2 (ru) | Способ получения концентрата живых микроорганизмов | |
FR2731587A1 (fr) | Procede pour eliminer les cellules somatiques des milieux alimentaires ou biologiques, et produits correspondants |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): BW GH GM KE LS MW MZ SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IT LU MC NL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
ENP | Entry into the national phase |
Ref document number: 2006172376 Country of ref document: US Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 10545272 Country of ref document: US |
|
122 | Ep: pct application non-entry in european phase | ||
WWP | Wipo information: published in national office |
Ref document number: 10545272 Country of ref document: US |