The present invention relates to a process for producing mutant forms of diphtheria toxin, and in particular to a process for producing a non-toxic mutant of diphtherialtoxin, for example the mutant known as CRM107, and a toxic conjugate thereof, which can be used for therapeutic purposes.
Diphtheria toxin is a proteinaceous toxin which is synthesised and secreted by toxigenic strains of Corynebacterium diphtheriae, i.e. strains which are lysogenic for a bacteriophage carrying the toxin gene. It is initially synthesized as a 535 amino acid am is polypeptide which undergoes proteolysis to form the toxin which is composed of two subunits, named A and B, joined by a disulphide bond. The A subunit is the enzymatic domain. It catalyses the ADP ribosylation of Elongation Factor 2, thereby inactivating EF-2. EF-2 is an essential enzyme involved in protein synthesis, and its inactivation results in cessation of protein synthesis and death of an xe2x80x98infectedxe2x80x99 eucaryotic cell. The A subunit is only active intracellularly, but since alone it is unable to bind to or cross the cell membrane it is not toxic when applied extracellularly. It is the B subunit which is responsible for getting the active A subunit into the cells; it does this by binding to the surface of cells by means of a cell surface receptor and then it facilitates the passage of the A subunit across the cell membrane into the cytoplasm where the toxic effects of the A subunit may be exerted.
Diphtheria toxin is highly cytotoxic; a single molecule can be lethal for an xe2x80x98infected cellxe2x80x99 and a dose as low as 10 ng/kg can kill animals and humans. There has thus beer, some considerable interest in investigating therapeutic strategies which utilise the toxic A subunit. The native toxin whilst being highly cytotoxic is non-specific, i.e. it will attack any cell which carries a receptor for the B subunit.
Certain mutant forms of the diphtheria toxin have been reported which are deficient in the cell binding and/or translocation function. These include toxin molecules which have a mutation in the B subunit which results in reduced binding to cells, such as for example mutants CRM9, CRM 45, CRM102, CRM103 and CRM107, as described by Nicholls and Youle in Genetically Engineered Toxins, Ed: Frankel, Marcel Dekker, Inc, 1992. The resulting toxin molecules are essentially non-toxic since the A subunit is unable to reach its site of action. These mutations can have a dramatic effect. Thus CRM107 has an amino acid substitution at position is 525, where serine in the native toxin has been replaced by phenylalanine, resulting in a more than 1000 fold reduction in the cell binding property with little or no effect on the translocating properties of the B subunit. The A subunit in such mutants is unaffected, and, if it can be targeted into the cytoplasm, is as toxic as the native toxin.
In designing cytotoxic drugs, there is thus interest in utilising these mutant forms of diphtheria toxin to taraet specific cell populations without affecting normal cells, by modifying the mutant toxin by linking it in some way to a moiety which is capable of binding to cells, and in particular to a moiety which is specific for certain cells or cell types, such as an antibody to a specific receptor, or a moiety such as a protein for example transferrin, which has a binding partner e.g. in the form of a receptor expressed only or at least predominantly on the surface of cells which are to be killed. In this way, it is possible to harness the cytotoxic properties of the diphtheria toxin A subunit, without affecting, or with only limited effect on, normal cells.
One area where modified forms of mutant diphtheria toxin such as modified CRM107 may be used is in the treatment of certain cancerous conditions, and in particular malignant gliomas. Malignant glioma is the most common CNS neoplasm in adults. No therapy is currently available and prognosis of patients with high grade gliomas, anaplastic astrocytomas and glioblastoma multiforme is thus bleak, with death usually occurring within one year of diagnosis. Mutated diphtheria toxin CRM107, particularly in the form of a targeted conjugate, provides a therapy for conditions such as this, and in particular, conjugates of CRM107 with the iron binding protein transferrin. This is particularly suitable for treatment of tumours including brain neoplasms because transferrin receptors are expressed at a high level on the surface of rapidly dividing cells such as glioma cells, but are absent on the surface of normal brain tissue. Thus mutated diphtheria toxin-transferrin conjugates may be selectively targeted to neoplastic tissue, where the toxin is internalised, and the A subunit kills the infected, cell.
For clinical use, large quantities of mutant diphtheria toxin are needed. There are however problems in producing diphtheria toxin from toxin producing strains of C. diphtheriae, and moreover, difficulties have been encountered in scaling up laboratory scale fermentation conditions to produce sufficient quantities of toxin, and in particular mutant forms of diphtheria toxin, for therapeutic use. Thus there are problems in obtaining toxin in sufficient yield and purity and large scale production thus tends to be inefficient. These difficulties need to be overcome in order to be able to exploit the promise of these so-called targeted mutant toxin derived drugs.
It is known in the art that diphtheria toxin production is dependent on the conditions under which the producing strain is grown. In particular, both iron content of the growth medium and the carbon source which are essential for bacterial growth have been found to have an effect on toxin production. Thus, it has been known for some time that iron in large concentrations has an inhibitory effect upon toxin production, in other words, toxin production is negatively regulated by iron. Thus for toxin preparation, low iron growth media is used, with iron generally in the range of 50-100 xcexcg/l.
Whilst glucose is commonly used as a carbon source for bacterial growth, it has also been known for some time that fermentation of glucose by C. diphtheriae can affect diphtheria toxin production. Thus it is known that fermentation of glucose by C. diphtheriae can lead to acidic fermentation products including acetic, formic and lactic acid, at least some of which are thought to be bacteriostatic and even possibly bactericidal for the bacteria. Glucose fermentation thus can affect the rate of bacterial growth with corresponding effects on toxin production. It has also been proposed that the acidic fermentation products may have an effect on the stability of the toxin. For this reason, other carbon sources such as maltose and glycerol, used either as the sole carbon source, or as an at least partial substitute for glucose have been used in the art for culturing toxin producing strains of C. diphtheriae. Neither of these carbon sources is however as efficient an energy source as glucose.
We have now developed a new fermentation process which enables diphtheria toxin to be produced by C. diphtheriae in good yield utilising glucose as the carbon source.
Thus viewed from one aspect, the present invention provides a method for the production of diphtheria toxin wherein a microorganism capable of producing diphtheria toxin is fermented using glucose as a carbon source, said method Comprising adding glucose to a growing culture whereby the addition of glucose maintains a microorganism growth effective to support diphtheria toxin production.
As used herein, the term xe2x80x98diphtheria toxinxe2x80x99 is used to refer to the naturally occurring protein, as well as mutated forms, particularly for therapeutic purposes mutated forms of the B subunit which have reduced or no binding function whilst retaining at least a degree of translocation function and preferably retaining at least some A subunit: enzymatic activity, variants for example proteins which have amino acid substitutions, additions or deletions and fragments thereof, particularly fragments which retain the cytotoxic activity of the A subunit. The method of the invention may be used to prepare the naturally occurring diphtheria toxin, as well as mutant forms, such as the aforementioned non-toxic mutants such as CRM107.
The naturally occurring diphtheria toxin may be obtained from toxin producing strains available from a variety of publicly available sources including the American Type Culture Collection. CRM 107 may be obtained from the strain Corynebacterium diphtheriae monolysogen C7 xcex2tox 107, which is obtainable from National Institutes of Health, 6011 Executive Boulevard, Rockville Md.20852, USA (Dr Richard Youle). Mutant forms of the toxin, such as the mutant forms described by Laird et al, J. Virology, 19, 220-227, 1976, and by Nicholls and Youle in Genetically Engineered Toxins, Ed: Frankel, Marcel Dekker, Inc, 1992, including CRM107, may also be prepared by methods known in the art, for example by the methods described in Laird et al (supra) or by expression in C. diphtheriae or other microorganisms using the techniques of recombinant DNA technology (Sambrook et al, Molecular Cloning, a Laboratory Manual, Cold Spring Harbor Laboratory Press, 1989), and also by site directed mutagenesis, based on the known nucleotide sequence (Greenfield et al, Proc Nat Acad Sci. 50, 6953-7, 1993) of the wild type structural gene for diphtheria toxin carried by corynebacteriophage xcex2.
In the method of the invention, glucose is added as required,to a growing culture, preferably an exponential culture, more preferably a late exponential phase culture, and/or may be added as required to a growing culture in stationary phase, preferably a batch fermentation culture.
This method contrasts with conventional batch fermentation, wherein an initial supply of nutrients is not renewed, and thus the culture grows exponentially for only a few generations until an essential nutrient is exhausted, and with conventional continuous culture in which fresh growth medium is added continuously at a constant rate whilst culture is simultaneously removed resulting in much longer exponential growth periods.
The fed batch method according to the invention offers an advantage over prior methods which utilise glucose as a carbon source for growth of C. diphtheriae and synthesis of toxin. Thus for example, Fass et al., Appl. Microbiol. Biotechnol. 43, 83-88 (1995) describe a two stage process in which glucose and iron are simultaneously depleted at the end of the exponential growth phase, and toxin is thus produced only once the culture enters stationary phase. In contrast, the controlled glucose addition in accordance with the invention enables toxin to be produced during the late exponential phase as well as during the stationary phase by prolonging the late exponential and early stationary phases, and as a result enables toxin to be produced and accumulated for a longer time thereby increasing the cumulative toxin production capacity of a culture.
The method may be used to produce diphtheria toxin both from its natural producer, C. diphtheriae and also from other microbial hosts, such as bacteria for example E. coli transformed with toxin genes or modified toxin genes.
The fed batch fermentation method is particularly applicable for the production of diphtheria toxin by toxin producing strains of C. diphtheriae because of the inhibitory effect which certain nutrients or their metabolites may have on toxin production, if their concentration is not controlled carefully. The fed batch method of the invention thus enables a low level of glucose to be maintained in the medium whilst at the same time providing the necessary carbon source required for growth. Thus by carefully monitoring the levels of glucose and/or pH of the fermentation culture, glucose levels may be controlled to achieve a balance between on the one hand providing sufficient and efficient carbon source to support bacterial growth, and toxin production, and on the other hand limiting the generation of inhibitory fermentation by-products which can have a detrimental effect on toxin production. By adding glucose to the fermentation medium as required during the fermentation, the pH can be controlled using the organic acids produced from glucose metabolism without the additional complication of adding exogenous inorganic acid, whilst enabling toxin to be produced during both the exponential and stationary growth phases. Thus glucose can be used both as a source of acid and as a carbon source to increase cell density.
In the method of the invention, growth is initiated in a glucose-based medium comprising conventional levels of glucose, for example within the range 0.8 to 2.5% such as about 1.5% glucose. The improvement over the prior methods is that glucose is added to the culture medium during the fermentation, commencing during the exponential growth phase or during the stationary phase at such time as is required to maintain the pH within a range optimal for microorganism growth and toxin production, preferably from 7.0 to 7.5, preferably from 7.1 to 7.3, for example at around 7.2. As mentioned above, certain acidic substances are by products of glucose metabolism, and these acids assist in controlling the pH of the fermentation medium.
If necessary, the pH may additionally be controlled by addition of acid or base as appropriate to maintain the pH of the culture at an appropriate level for toxin expression, for example at about pH 7.2xc2x10.2.
Thus we have found that by controlling the glucose concentration within the fermentation culture by periodic addition to maintain the pH within the aforementioned range, it is possible to maximise cell growth and toxin production by minimising toxin degradation de to fluxes in pH. Thus we have observed that as the C. diphtheriae cells enter the logarithmic growth phase, pH and glucose concentration decreases. We have also found that the purity of the toxin decreased as the pH of the medium decreased. Without wishing to be bound by theory, it is believed that this might be due to proteolytic breakdown. Toxin purity was also observed to decrease as fermentation progressed at pH""s below about 7, and also at pH""s in excess of about 8.0. It is for this reason that the glucose (and the pH levels determined thereby) levels are desirably maintained within this range.
The progress of fermentation may be monitored by measuring various parameters indicative of bacterial growth and toxin production either in samples aseptically removed from the culture vessels or by direct measurement in the fermentation broth. For example pH may be monitored within the fermentation broth by means of a pH probe. Glucose may be monitored by a variety of methods known in the art, either directly or indirectly, for example methods described in clinical Diagnosis and Management by Laboratory Methods, 18 Edn, John Bernard Henry, Editor, WB Saunders Company, Philadelphia, 1991. Examples of direct measurement include sugar assays for example those based on chemical reactions such as for example enzymic reactions, for example reactions based on the use of glucose oxidase, such as calorimetric reactions. Examples include measurement by means of dipsticks for example glucose chemstrip BG from Boehringer Mannheim and use of an on-line glucose monitor. Since pH has been shown to decrease in proportion to glucose consumption, glucose may also be monitored indirectly by monitoring pH of the broth. Toxin production may be monitored in a variety of known ways, such as for example, SDS PAGE (Laemmli, Nature 227, 680-684, 1970), ELISA (Nielsen et al, Journal of Clinical Microbiology, 25, 1280-1284, 1987) or an ADP-ribosylation assay (Blanke et al., Biochemistry 33, 5155 (1994) or by a combination of these methods. Generally, glucose addition will commence when the level of glucose in the medium drops to levels such that, but for the addition of glucose to generate acidic byproducts, acid would need to be added to control the pH of the fermentation medium. Generally, additional glucose may be added when the level of glucose in the fermentation medium drops below about 10 g/L, preferably below 2 g/L and more particularly below about 1 g/L. At this level, the exponential growth phase of the culture is extended and the pH of the media decreased by increased metabolism of glucose. In this way, glucose feeding may be used to control pH and stabilise the toxin as well as to maintain growth of culture to obtain high cell density.
We have thus found that with the glucose fed batch fermentation method according to the invention, in a culture medium comprising 10-15 g/L glucose, the exponential phase of bacterial growth commences generally 5 hours after the start of fermentation, with toxin production starting within approximately 9 hours after the start of fermentation. With periodic addition of glucose commencing generally 8 hours after the start of fermentation, such as about 9 hours, for example when the culture is in the last 25% increase in growth curve OD value, we have been able to achieve toxin production for at least 13.5 hours. In such a fed batch method, additional glucose in the range of 7 g/L to 15 g/L may be consumed.
By the fed batch glucose feeding method of the invention, we have been able to achieve a cell density in the range of 45-60 (OD at 590 nm) and a toxin production in the range of 145-165 mg/ml culture.
In addition to a carbon source, there are other minimum nutritional requirements for growth of C. diphtheriae. These include trace metals, phosphate and a nitrogen source. Generally casamino acids and yeast extractare included in bacterial growth media to provide a nitrogen and amino acid source. Growth media for C. diphtheriae, such as CY medium (Fass et al., Applied Micobiol. Biotechnol. 43, 83-88 (1995)) generally contains at least 2% yeast extract. We have however found that increasing the carbon to nitrogen ratio by reducing the amount of yeast extract below this conventional level, to between 0.5-1.5% such as between 0.75 to 1% for example around 1% yeast extract, improves the fed batch fermentation method according to the invention. Thus we have found that reducing the conventional amount of yeast extract results in a significant improvement in yield of toxin. We have also found an improvement in yield can be obtained by using cystine as opposed to cysteine which can be used in bacterial growth media. Thus a 5-fold increase in yield of CRM107 has been observed when using 1% yeast extract and using a medium containing 0.7 g/l cystine as compared to 2% yeast extract in a medium containing 0.26 g/l cysteine in a 10 liter fermentation according to the invention.
Accordingly, the use of a growth medium containing no more than 1% yeast extract constitutes a preferred aspect of the method of the invention.
We have found that the reduced yeast extract fermentation conditions also have other benefits in addition to increased toxin yieldin diphtheria toxin production. Thus as will be described in more detail below, reducing the yeast extract content of the growth medium has additional benefits in purification of the toxin.
The present invention also relates to a method for purifying diphtheria toxin from a culture supernatant of a toxin producing bacterial strain.
Diphtheria toxin is secreted in large quantities from synthesising bacteria such as corynebacteria; it can reach up to 70% of the total protein in the culture medium. This level is sufficiently high that for small, laboratory scale cultures, a straightforward precipitation for example using ammonium sulphate or trichloroacetic acid of the culture medium may be effective alone to purify the toxin. However, difficulties are encountered when using large scale cultures. The precipitation steps are time consuming and due to difficulties in handling and dialysing such large volumes of material, there is loss of toxin product. We have now developed a purification method which is capable of handling large volumes of material and overcomes these disadvantages.
Thus viewed from a further aspect, the present invention provides a method of purifying diphtheria toxin from a culture of toxin producing bacteria, said method comprising contacting a toxin containing preparation with an ion exchange matrix, eluting a fraction containing the toxin, applying the eluate to a hydrophobic matrix, and eluting a fraction containing the toxin.
The starting material for purification may for example be a toxin containing supernatant, a toxin containing cellular fraction or a toxin containing preparation derived from a culture supernatant, for example a concentrated supernatant, such as an ultrafiltered supernatant, or a diafiltered supernatant.
In toxin purification methods known in the art, the ion exchange step is performed after the hydrophobic interaction chromatography step, because the art taught that culture supernatant cannot be directly applied to an ion exchange matrix, such as DEAE cellulose. Such matrices are capable of binding proteins only under conditions of low ionic strength, and it has thus been thought that the ionic strength of culture medium would be too high to achieve efficient binding (Rappuoli et al, J. Chromatography, 268, 543-548, 1983).
We have however found that contrary to this perception in the art, it is indeed possible to apply a culture supernatant onto an ion exchange matrix, such as immobilised DEAE. Preferably, because toxin generally binds to ion (exchange media at low ionic strength, the culture supernatant is diafiltered prior to applying to the matrix, for example in the form of a column. This has enabled the two chromatographic separation steps to be operated in the sequence of ion exchange chromatography (IEC) before hydrophobic interaction chromatography (HIC). In addition, diafiltration may serve as a purification step.
Thus viewed from another aspect, the present invention provides a method of purifying diphtheria toxin from a culture of toxin producing bacteria said method comprising chromatographic steps of ion exchange chromatography and hydrophobic interaction chromatography, characterised in that said method comprises carrying out an ion exchange chromatography before hydrophobic interaction chromatography.
We have found that this purification method according to the invention results in a higher toxin yield as compared to the conventional process, without sacrifice to purity (i.e. without significant levels of contaminating proteins). Thus we have found that by carrying out an IEC step before HIC, a purity of up to around 98% can be achieved.
Preferably, the starting material is a culture supernatant for example a culture supernatant from a culture which is fermented using glucose as a carbon source in accordance with the invention. As mentioned above, the use of lower amounts of yeast extract than is conventional at least in glucose culture media, for example about 1% has additional advantages besides improved yield. Thus we have observed that yeast extract contributes to pigmentation of the growth medium, contributing to contaminants which can make the subsequent purification process less effective. Accordingly, the ability to reduce the levels of contaminants at the outset represents an advantage for subsequent purification. Culture media with lower yeast content are less pigmented, and accordingly advantageous.
Thus viewed from a further aspect, the present invention provides a method of purifying diphtheria toxin comprising
(1) fermenting a microorganism strain capable of producing diphtheria toxin using glucose as a carbon source, said method comprising adding glucose to a growing culture whereby the addition of glucose maintains microorganism growth effective to support diphtheria toxin production; and
(2) purifying the diphtheria toxin from the culture by contacting a toxin containing preparation derived therefrom with an ion exchange matrix, eluting a fraction containing the toxin, applying the eluate to a hydrophobic matrix, and eluting a fraction containing the toxin.
Preferably, the microorganism is a bacteria, such as C. diphtheriae. In the case of C. diphtheriae, where toxin is secreted into the culture supernatant, the method may be tarried out directly on culture supernatant or on a preparation derived therefrom such as for example a diafiltered culture supernatant. Thus a preliminary step may involve a primary clarification of the culture broth to obtain a toxin-containing culture supernatant. Thus bacteria may be separated from the culture broth by methods known in the art, such as centrifugation or filtration, for example, ultrafiltration, and the resulting supernatant diafiltered or applied directly to the first matrix, the ion exchange matrix. In the case of expression in other microorganisms, such as E. coli genetically modified with toxin, toxin may be found intracellularly, for example in the periplasm or cytoplasm. In such cases, primary recovery steps may depend upon the cellular location. The toxin may be extracted from the cells by methods known in the art, for example as described by Skopes in Protein Purification, Principles and Practice, 3rd edn, Pub: Springer Verlag, followed by purification in accordance with the method of the invention.
Filtration to clarify the fermentation broth may be effected by methods known in the art, for example with membranes such as hollow fibre or spiral wound membranes, such as by means of a 0.1 or 0.2 xcexcm filter, for example a hollow fiber filter, such as that obtainable from A/G Technology, or a 0.4 or 0.65 xcexcm hollow fibre or spiral wound membrane, or a 300K or 500K filter.
For ease of handling, particularly where large volumes are concerned, such as would be the case for industrial, scale purification for pharmaceutical purposes, a degree of concentration of the supernatant may be effected prior to the ion exchange step. The cell free culture supernatant may be concentrated, generally 5 to 50 fold, preferably 15 to 25 fold, such as 20 fold, using protein concentration methods known in the art, for example by means of ultrafiltration with porous materials for example in the form of filters, membranes or hollow fibres. For ease of handling, filters are Preferred. For ultrafiltration/concentration, filters having a molecular weight cut off smaller, preferably 20% smaller than the toxin, are preferred, preferably 30K filters (i.e. filters which have a 30000 dalton molecular weight cut off). Suitable materials for such filters are known in the art and include polymeric materials such as mixed-cellulose, polyether sulfone or PVDF, for example polysaccharides such as cellulose, and polysulfones. Preferred materials are those which have a lower capacity or ability to absorb toxin. Cellulose filters are particularly preferred, for example filters made from regenerated cellulose such as the xe2x80x98YMxe2x80x99 based filters and other membranes which have little protein binding capacity for example the Flat plate tangential flow bioconcentrators produced by Amicon. The use of cellulose filters for ultrafiltration thus constitutes a preferred aspect of the purification method according to the invention.
IEC may be carried out directly on the culture supernatant, using an appropriately sized bed volume as determined by one skilled in the art. Optionally, the concentrated clarified supernatant may be further treated prior to chromatographic purification, for example by diafiltration. In this way, ionic strength may be reduced by removing salts and other ions smaller than the molecular weight cut off size of the diafiltration membrane. The reduction in ionic strength has benefits for the ensuing ion exchange step, since at reduced ionic strength, less toxin is retained by the ion exchange matrix and yield is thus improved. Furthermore, a partial purification is achieved by the diafiltration membrane. Diafiltration may thus be carried out against a low ionic strength buffer, for example Tris, Tricine, MES, Bis-Tris, TES, MOPS and phosphate, in a concentration of from about 0.1 mM to about 100 mM, preferably from about 10 to about 50 mM, for example 10 mM, having a pH of from about 5 to about 8, preferably from about 6 to about 8 for example about 7.4 to 7.6, using for example a 30 000 cut off membrane which will result in removal of salts, low molecular weight media components and secreted proteins less than 30 000 dalton molecular weight. Such components may otherwise bind to the ion exchange matrix and reduce its capacity to bind toxin.
Diafiltration may be carried out for example using materials of the type used for the ultrafiltration step, against buffers such as low ionic strength buffers such as Tris, Tricine, MES, BiS-Tris, TES, MOPS or phosphate, in a concentration of from about 0.1 mM to about 100 mM, preferably from about 10 to about 50 mM, for example 10 mM, having a pH of from about 5 to about 8, preferably from about 6 to about 8 for example about 7.4 to 7.6, for example 10 mM potassium phosphate pH 7.6 so as to reduce the conductivity of the concentrated culture supernatant as low as possible, preferably below about 5 mS/cm.
Treatment of the culture supernatant in this way prior to IEC thus overcomes the problems of the prior art method which requires that HIC has to take place before IEC. The combination of diafiltration and ultrafiltration not only reduces the ionic strength, but serves as an initial purification and allows the volume to be reduced This means that smaller columns may be used, thereby reducing the time required for the chromatographic steps to be carried out.
A further advantage is that toxin purification according to he method of the invention is faster overall than she conventional method, thus limiting the time during which the toxin is exposed to room temperature and vulnerable to degradation.
The chromatographic steps may be carried out using ion exchange or hydrophobic matrices as appropriate in batch or column form, the latter being preferred for both speed and convenience. The matrix may be a conventional support as known in the art for example inert supports based on cellulose, polystyrene, acrylamide, silica, fluorocarbons, cross-linked dextran or cross-linked agarose.
Any conventional ion exchange resin may be used. Examples include Q sepharose and diethylaminoethyl (DEAE) and quaternary amine resins. The anion exchange material may be packed into a column, whose size will be dependent upon the volume of culture supernatant to be used. The appropriate column size may be determined by those skilled in the art according to the total protein in the concentrated media. Generally, for large scale cultures of the order of 40-50 liters, 2 liter supernatant concentrates may be applied to columns of volume 1.25 l. The column may first be equilibrated with a buffer for example a low ionic strength buffer such as Tris, Tricine, MES, Bis-Tris, TES, MOPS or phosphate, in a concentration of from about 0.1 mM to about 100 mM, preferably from about 10 to about 50 mM, for example 10 mM, having a pH of from about 5 to about 8, preferably from about 6 to about 8 for example about 7.4 to 7.6, for example the buffer used to diafilter the concentrated supernatant, such as 10 mM potassium phosphate pH 7.6. The culture supernatant or concentrate may then be loaded, the column washed with a buffer of low ionic strength and the same pH as the equilibration buffer to wash off any unbound protein, for example the equilibration buffer.
Bound toxin may then be eluted in a variety of ways. These include altering the pH or increasing the ionic strength of the buffer. Thus toxin may be eluted by a gradient increase of buffer with high ionic strength, such as Tris, Tricine, MES, Bis-Tris, TES, MOPS or phosphate, in a concentration of from about 10 mM to about 1.0M, preferably from about 10 mM to about 500 mM, containing salts like NaCl, KCl or ammonium sulphate at a concentration of from about 0.1M to 1.0M. These buffers may have a pH of from about 5 to about 8, preferably from about 6 to about 8 for example about 7.0 to 7.6. One example of a preferred buffer is 10 mM potassium phosphate containing 500 mM KCl at pH 7.6. The protein will be eluted between 100 to 150 mM KCl in the buffer.
The toxin containing eluate may then be applied to the hydrophobic matrix. Optionally but preferably, the ionic strength of the eluate may be increased prior to the second hydrophobic interaction step, by mixing with a buffer of appropriate ionic strength or by diafiltration. This may facilitate binding of toxin to the hydrophobic resin. Thus the eluate may be mixed with a high ionic strength buffer for example Tris, tricine, MES, Bis-Tris, TES, MOPS or phosphate,in a concentration of from about 10 mM to about 1.0M, preferably from about 10 mM to about 500 mM, containing salts like NaCl, KCl or ammonium sulphate at a concentration of about 0.1M to 1M. The buffers may have a pH of from about 5 to about 8, preferably from about 6 to about 8 for example about 7.0 to 7.6. One example of a preferred buffer is 10 mM potassium phosphate buffer containing 500 mM ammonium sulphate with a pH of 7.0. Diafiltration may be carried out using methods known in the art, for example using ultrafiltration membranes, such as 30K or 10K cut off hollowfiber filters obtainable from A/G technology or spiral wound filters from Amicon, or Ultrasette (Omega) (Pall Filtron) and using buffers such as the aforementioned tris, phosphate, acetate or HEPES.
Hydrophobic matrices are known in the art. These include the aforementioned supports carrying hydrophobic moieties such as alkyl, for example butyl, hexyl, octyl, acetyl or phenyl groups, for example alkyl agarose such as decyl agarose.
The hydrophobic matrix material may be packed into a column, whose size will be dependent upon the volume of culture supernatant to be used. The appropriate column size may be determined by those skilled in the art. Generally, for large scale cultures of the order of 40-50 liters, the eluate from the IEC step will be generally in a volume of 11 to 21 and will be applied to columns whose size may be determined by those skilled in the art according to the amount of protein, but may be of the order of 250 ml for protein concentration of up to 100 mg/ml. The column may first be equilibrated with a high ionic strength buffer, for example Tris, Tricine, MES, Bis-Tris, TES, MOPS or phosphate, in a concentration of from about 10 mM to about 1.0M, preferably from about 10 mM to about 500 mM, containing salts like NaCl, KCl or ammonium sulphate at a concentration of about 0.1M to 1.0M, having a pH of from about 5 to about 8, preferably from about 6 to about 8 for example about 7.6, for example the buffer used to diafilter the concentrated supernatant or the buffer mixed with the eluate, such as for example 50 mm potassium phosphate with 1M ammonium sulphate pH 7.0. The IEC eluate, or eluate mixed with high ionic strength buffer or diafiltered eluate may then be loaded, the column washed with a high ionic strength buffer for example Tris, Tricine, MES, Bis-Tris, TES, MOPS or phosphate, in a concentration of from about 10 mM to about 1.0M, preferably from about 10 mM to about 500 mM, containing salts like NaCl, KCl or ammonium sulphate at a concentration of about 0.1M to 1.0M, having a pH of from about 5 to about 8, preferably from about 6 to about 8 for example about 7.6, such as for example the column equilibration buffer to remove any unbound proteins.
Bound toxin may then be eluted in a variety of ways for example by gradient increase of a polar solvent in the wash buffer or by gradient increase of a low ionic strength buffer, for example Tris, Tricine, MES, Bis-Tris, TES, MOPS or phosphate, in a concentration of from about 10 mM to about 1.0M, preferably from about 10 mM to about 500 mM, containing salts like NaCl, KCl or ammonium sulphate at a concentration of about 0.1M to 1.0M, having a pH of from about 5 to about 8, preferably from about 6 to about 8 for example about 7.6, for example 50 mM phosphate containing 1M ammonium sulphate pH 7.0 to 50 mM phosphate buffer pH 7.0 without ammonium sulphate. Toxin may be eluted in such a gradient as the ammonium sulphate concentration is reduced to approximately 700 mM.
By using the method of the invention, we have been able to purify diphtheria toxin mutant CRM107 from large volumes of culture supernatant, of the order of 50 l with an average yield of 32% of the starting material and purity greater than 98% as measured by HPSEC (high performance size exclusion chromatography). This for the first time enables the properties of diphtheria toxin mutants such as the binding mutant CRM107 to be exploited for preparing therapeutic products.
When the purified toxin is a mutant toxin to be used to prepare targeted toxin derived therapeutic agents, the toxin may conveniently be eluted with a buffer suitable for carrying out the conjugation or attachment of the toxin with a cell specific binding or targeting moiety, for example a cell recognition moiety such as an antibody to a cell surface moiety or an antigen binding fragment thereof or a protein which has a binding partner on the cell surface for example in the form of a receptor, such receptors having some degree of selectivity, i.e. being present on some but not all cell types.
As used herein, xe2x80x98cell specificxe2x80x99 or xe2x80x98cell selectivexe2x80x99 refers to a moiety which has a targeting or binding affinity for a cell surface moiety which is not present on all cells, and thus which is selective for certain cells or groups or types of cells or specific receptors. In other words, it encompasses a moiety which enables a diphtheria toxin or mutant toxin conjugated to it to be targeted selectively.
Thus according to a further aspect, the present invention provides a process for preparing a diphtheria toxin conjugate comprising linking a diphtheria toxin produced by the method of the invention with a cell specific binding or targeting moiety.
Examples of cell specific moieties include antibodies to moieties exposed on the surface of particular cells, and proteins such as growth factors or transferrin whose binding partners in the form of receptors are expressed only on particular cell types, or predominantly only on specific cell types.
Conjugation may be effected by methods known in the art such as chemical cross-linking or covalent bond formation. Preferably the conjugation is be means of covalent bond formation for example between maleimido groups introduced onto one component of the conjugate and thiol groups introduced onto the other. In such a method, one of the two components is modified by introduction of maleimide groups and the other is modified by means of introduction of thiol groups. Preferably the diphtheria toxin or mutant is modified by means of maleimide groups and the cell specific targeting moiety by means of thiol groups. Preferably, for the preparation of anticancer agents such as those for the treatment of malignant glioma, the cell selective moiety is transferrin since transferrin receptors are expressed in quantity in rapidly dividing cells such as glioma cells but are essentially absent on other cells in the CNS. In such conjugates, generally the diphtheria toxin element is modified with maleimide and the transferrin element with thiol groups. However, diphtheria toxin element may be modified with thiol groups and the transferrin element with maleimide.
Conventional modifying agents known in the art may be used. Examples include esterifying compounds, thiol activating compounds and carboxyl modifying agents such as N ethyl maleimide and maleimidobenzoyl-N-hydroxysuccinimidyl ester (MBS) and 2-iminothiolane. In a typical conjugation, MBS may be added to diphtheria toxin in a ratio of from 1 to 100 times molar excess, such as 2 to 5 preferably 3.5 times, incubated at a temperature of 2 to 50xc2x0 C. for example 15 to 20xc2x0 C. such as room temperature, for 5 minutes to 24 hours, such as from 20 to 40 minutes such as 30 minutes followed by removal of excess reagent by techniques known in the art such as gel filtration for example using Sephadex G-25 desalting. The eluate may then be cooled prior to the conjugation reaction. Crude intermediates may be removed prior to conjugation by methods known in the art such as precipitation, dialysis, chromatography, extraction. Transferrin may be thiolated by means of incubation with 2-iminothiolane in a ratio of 1 to 100 times molar excess, such as 5 to 10 times molar excess preferably 7 to 8 times such as 7.7 times at a temperature of 2 to 50xc2x0 C., for example 35-40xc2x0 C., for 5 minutes to 24 hours, such as 20 to 40 minutes such as 30 minutes followed by removal of excess reagent by techniques known in the art such as gel filtration. For the conjugation, the two functionalised reagents may be mixed in a ratio of 1 to 2 preferably at a temperature of 2 to 8xc2x0 C. for 4 to 24 hours, preferably 12 to 20 hours, for example 18 hours.
According to a yet further aspect, the present invention provides a method of treatment of a CNS neoplasm comprising administering to a subject a diphtheria toxin conjugate produced by the method of the invention.
According to a still yet further aspect, the present invention provides the use of a diphtheria toxin conjugate produced by the method of the invention in the manufacture of a medicament for use in the treatment of CNS neoplasm
USPTO Backgrounds
USPTO Backgrounds