WO2007089851A2 - Compositions and methods for treating collagen-mediated diseases - Google Patents

Compositions and methods for treating collagen-mediated diseases Download PDF

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Publication number
WO2007089851A2
WO2007089851A2 PCT/US2007/002654 US2007002654W WO2007089851A2 WO 2007089851 A2 WO2007089851 A2 WO 2007089851A2 US 2007002654 W US2007002654 W US 2007002654W WO 2007089851 A2 WO2007089851 A2 WO 2007089851A2
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WIPO (PCT)
Prior art keywords
collagenase
drug product
fermentation
lane
sample
Prior art date
Application number
PCT/US2007/002654
Other languages
French (fr)
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WO2007089851A3 (en
Inventor
Gregory L. Sabatino
Jr. Benjamin J. Del Tito
Phillip J. Bassett
Hazel A. Tharia
Antony G. Hitchcock
Original Assignee
Auxilium International Holdings, Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to EP12155233.5A priority Critical patent/EP2474321B1/en
Priority to AU2007211313A priority patent/AU2007211313C1/en
Application filed by Auxilium International Holdings, Inc. filed Critical Auxilium International Holdings, Inc.
Priority to NZ569882A priority patent/NZ569882A/en
Priority to JP2008552504A priority patent/JP5309289B2/en
Priority to BRPI0708017-4A priority patent/BRPI0708017A2/en
Priority to CN200780008746.5A priority patent/CN101400788B/en
Priority to ES07762860T priority patent/ES2709202T3/en
Priority to EP18209918.4A priority patent/EP3508571B1/en
Priority to CA2637262A priority patent/CA2637262C/en
Priority to KR1020117006197A priority patent/KR20110046537A/en
Priority to DK07762860.0T priority patent/DK1987141T3/en
Priority to EP07762860.0A priority patent/EP1987141B8/en
Priority to MX2008009756A priority patent/MX2008009756A/en
Priority to IL291175A priority patent/IL291175B2/en
Publication of WO2007089851A2 publication Critical patent/WO2007089851A2/en
Publication of WO2007089851A3 publication Critical patent/WO2007089851A3/en
Priority to IL192878A priority patent/IL192878A/en
Priority to ZA2010/01779A priority patent/ZA201001779B/en
Priority to IL245434A priority patent/IL245434A/en
Priority to IL254184A priority patent/IL254184B/en
Priority to IL264361A priority patent/IL264361B/en
Priority to IL277322A priority patent/IL277322B/en

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    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K38/00—Medicinal preparations containing peptides
    • A61K38/16—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof
    • A61K38/43—Enzymes; Proenzymes; Derivatives thereof
    • A61K38/46—Hydrolases (3)
    • A61K38/48—Hydrolases (3) acting on peptide bonds (3.4)
    • A61K38/4886—Metalloendopeptidases (3.4.24), e.g. collagenase
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K38/00—Medicinal preparations containing peptides
    • A61K38/16—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof
    • A61K38/43—Enzymes; Proenzymes; Derivatives thereof
    • A61K38/46—Hydrolases (3)
    • A61K38/48—Hydrolases (3) acting on peptide bonds (3.4)
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K9/00—Medicinal preparations characterised by special physical form
    • A61K9/0012—Galenical forms characterised by the site of application
    • A61K9/0019—Injectable compositions; Intramuscular, intravenous, arterial, subcutaneous administration; Compositions to be administered through the skin in an invasive manner
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K9/00—Medicinal preparations characterised by special physical form
    • A61K9/08—Solutions
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K9/00—Medicinal preparations characterised by special physical form
    • A61K9/14—Particulate form, e.g. powders, Processes for size reducing of pure drugs or the resulting products, Pure drug nanoparticles
    • A61K9/19—Particulate form, e.g. powders, Processes for size reducing of pure drugs or the resulting products, Pure drug nanoparticles lyophilised, i.e. freeze-dried, solutions or dispersions
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P17/00—Drugs for dermatological disorders
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P17/00—Drugs for dermatological disorders
    • A61P17/02—Drugs for dermatological disorders for treating wounds, ulcers, burns, scars, keloids, or the like
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P17/00—Drugs for dermatological disorders
    • A61P17/10—Anti-acne agents
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P19/00—Drugs for skeletal disorders
    • A61P19/02—Drugs for skeletal disorders for joint disorders, e.g. arthritis, arthrosis
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P19/00—Drugs for skeletal disorders
    • A61P19/04—Drugs for skeletal disorders for non-specific disorders of the connective tissue
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P35/00—Antineoplastic agents
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P43/00—Drugs for specific purposes, not provided for in groups A61P1/00-A61P41/00
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N9/00—Enzymes; Proenzymes; Compositions thereof; Processes for preparing, activating, inhibiting, separating or purifying enzymes
    • C12N9/14—Hydrolases (3)
    • C12N9/16—Hydrolases (3) acting on ester bonds (3.1)
    • C12N9/18—Carboxylic ester hydrolases (3.1.1)
    • C12N9/20—Triglyceride splitting, e.g. by means of lipase
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N9/00—Enzymes; Proenzymes; Compositions thereof; Processes for preparing, activating, inhibiting, separating or purifying enzymes
    • C12N9/14—Hydrolases (3)
    • C12N9/48—Hydrolases (3) acting on peptide bonds (3.4)
    • C12N9/50—Proteinases, e.g. Endopeptidases (3.4.21-3.4.25)
    • C12N9/52—Proteinases, e.g. Endopeptidases (3.4.21-3.4.25) derived from bacteria or Archaea
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12Y—ENZYMES
    • C12Y304/00—Hydrolases acting on peptide bonds, i.e. peptidases (3.4)
    • C12Y304/24—Metalloendopeptidases (3.4.24)
    • C12Y304/24007—Interstitial collagenase (3.4.24.7), i.e. matrix metalloprotease 1 or MMP1

Definitions

  • Collagen is the major structural constituent of mammalian organisms and makes up a large portion of the total protein content of skin and other parts of the animal body. In humans, it is particularly important in the wound healing process and in the process of natural aging. Various skin traumas such as burns, surgery, infection and accident are often characterized by the erratic accumulation of fibrous tissue rich in collagen and having increased proteoglycan content. In addition to the replacement of the normal tissue which has been damaged or destroyed, excessive and disfiguring deposits of new tissue sometimes form during the healing process. The excess collagen deposition has been attributed to a disturbance in the balance between collagen synthesis and collagen degradation.
  • Collagen-mediated diseases Numerous diseases and conditions are associated with excess collagen deposition and the erratic accumulation of fibrous tissue rich in collagen. Such diseases and conditions are collectively referred to herein as "collagen-mediated diseases".
  • Collagenase has been used to treat a variety of collagen-mediated diseases.
  • Collagenase is an enzyme that has the specific ability to digest collagen.
  • Collagenase for use in therapy may be obtained from a variety of sources including mammalian (e.g. human), crustacean (e.g. crab, shrimp), fungal, and bacterial (e.g. from the fermentation of Clostridium, Streptomyces, Pseudomonas, or Vibrio).
  • Collagenase has also been genetically engineered.
  • C. histotyticum C. histotyticum
  • the crude collagenase obtained from C. his may be purified using any of a number of chromatographic techniques.
  • One drawback of the fermentation process from C. his is that it yields uncertain ratios of the various collagenases such as collagenase I and collagenase II, often used in therapeutic compositions to treat collagen mediated conditions.
  • the culture has historically required the use of meat products. This meat culture was originally derived from the H4 strain of Clostridium histolyticum, Dr. I. Mandl's laboratory in Columbia University in 1956 and deposited with the ATCC. Lyophilized vials were made out of the cooked meat culture and named as ABC Clostridium histolyticum master cell bank.
  • a therapeutic collagenase preparation in which the ratio of collagenase I to collagenase II in the preparation can be easily and efficiently determined and controlled to obtain superior, and consistent enzyme activity and therapeutic effect, would be desirable.
  • the present invention provides a collagenase composition comprising a combination of highly purified collagenase I and collagenase II.
  • the collagenase I and collagenase II are present in a mass ratio of about 1 to 1.
  • the composition of the invention provides improved and consistent therapeutic effect while lowering the potential for side effects.
  • the invention further provides methods for preparing a collagenase composition of the invention, pharmaceutical formulations comprising a composition of the invention and methods for treating patients suffering from a collagen-mediated disease using a collagenase composition of the invention.
  • Figure 1 depicts growth curves (OD vs time) of C. histolyticum in 5L DCFT24a,b fermentations.
  • Figure 2 depicts net growth curves (Net OD vs time) of C. histolyticum in 5L DCFT24a,b fermentations.
  • Figure 3 is a 8% Tris-glycine SDS PAGE gel from the second fermentation:
  • Lane 2 Collagenase l - 0.27 ⁇ g
  • Lane 3 Collagenase II - 0.29 ⁇ g
  • Lane 4 2Oh (6.12 ⁇ L of sample) — Harvest point Lane 5: I9h (6.12 ⁇ L of sample)
  • Lane 7 16h (6.12 ⁇ L of sample)
  • Lane 8 15h (6.12 ⁇ L of sample)
  • Lane 9 14h (6.12 ⁇ L of sample)
  • Lane 10 13h (6.12 ⁇ L of sample)
  • Lane 11 11.6h - 19h (6.12 ⁇ L of sample)
  • Lane 12 10.5h (6.12 ⁇ L of sample);
  • Figure 4 is a 8% Tris-glycine SDS PAGE gel from the first fermentation:
  • Lane 1 High Molecular Weight Marker Lane 2: Collagenase l - 0.27 ⁇ g
  • Lane 3 Collagenase II - 0.29 ⁇ g
  • Lane 6 17h (6.12 ⁇ L of sample)
  • Lane 7 16h (6.12 ⁇ L of sample)
  • Lane 10 13h (6.12 ⁇ L of sample) Lane 11: 11.4h (6.12 ⁇ L of sample) Lane 12: 10.4h (6.12 ⁇ L of sample);
  • Figure 5 is a Semi-quantitative SDS PAGE gel for the second fermentation, harvest point sample: Lane 1: High Molecular Weight Marker Lane 2: 0.87 ⁇ L of sample (1/7 dilution of fermentation sample) Lane 3: 1.22 ⁇ L of sample (1/5 dilution of fermentation sample) Lane 4: 1.53 ⁇ L of sample (1/4 dilution of fermentation sample) Lane 5: 2.04 ⁇ L of sample (1/3 dilution of fermentation sample) Lane 6: 0.27 ⁇ g collagenase I Lane 7: 0.18 ⁇ g collagenase T Lane 8: O.135 ⁇ g collagenase I Lane 9: 0.29 ⁇ g collagenase II Lane 10: O.193 ⁇ g collagenase II Lane 11 : 0.145 ⁇ g collagenase II; Figure 6 represents fermentation strategy used for DCFT26a and DCFT26b; Figure 7 depicts growth curves (OD vs time) of C. histolyticum in 5L DCFT26a,b fermentations; Figure 8 depicts net growth curves (Net OD vs time)
  • Figure 9 is a SDS PAGE gel for DCFT26a:
  • Lane 2 Collagenase I - 0.67 ⁇ g
  • Lane 3 Collagenase II - 0.72 ⁇ g
  • Lane 4 2Oh (6.12 ⁇ L of sample) - Harvest Point
  • Lane 5 19h (6.12 ⁇ L ofsample)
  • Lane 6 18h (6.12 ⁇ L ofsample)
  • Lane 7 17h (6.12 ⁇ L ofsample)
  • Lane 8 16h (6.12 ⁇ L ofsample)
  • Lane 9 14h (6.12 ⁇ L of sample)
  • Lane 10 13h (6.12 ⁇ L ofsampIe
  • Lane 11 1 Ih (6.12 ⁇ L of sample);
  • Figure 10 is a SDS PAGE gel for DCFT26b:
  • Lane 3 19h (6.12 ⁇ L of sample)
  • Lane 4 18h (6.12 ⁇ L of sample)
  • Lane 11 Collagenase I - 0.67 ⁇ g
  • Lane 12 Collagenase 11 - 0.72 ⁇ g;
  • Figure 11 is a semi-quantitative SDS PAGE gel for DCFT26a, harvest point sample:
  • Lane 8 0.87 ⁇ L of sample (1/7 dilution of fermentation sample)
  • Lane 9 1.22 ⁇ L of sample (1/5 dilution of fermentation sample)
  • Lane 10 1.53 ⁇ L of sample (1/4 dilution of fermentation sample)
  • Lane 11 2.04 ⁇ L of sample (1/3 dilution of fermentation sample);
  • Figure 12 is a Semi-quantitative SDS PAGE gel for DCFT26b, harvest point sample:
  • Lane 8 2.04 ⁇ L of sample (1/3 dilution of fermentation sample)
  • Lane 9 1.53 ⁇ L of sample (1/4 dilution of fermentation sample)
  • Lane 10 1.22 ⁇ L of sample (1/5 dilution of fermentation sample)
  • Lane 11 0.87 ⁇ L of sample (1/7 dilution of fermentation sample);
  • Figure 13 is a SDS PAGE gel for post-dialysed ammonium sulphate precipitated (100g/L and 150 g/L) samples, DCFT26a, harvest point sample:
  • Lane 1 High Molecular Weight Marker
  • Lane 4 6.12 ⁇ L of supernatant sample from SCl 1
  • Lane 5 post dialysed sample - 100g/L AS (Neat)
  • Lane 6 post dialysed sample — 100g/L AS (1/5)
  • Lane 7 post dialysed sample - 100g/L AS (1/10)
  • Lane 8 post dialysed sample — 150g/L AS (Neat)
  • Lane 9 post dialysed sample — 150g/L AS (1/5)
  • Lane 10 post dialysed sample - 150g/L AS (1/10);
  • Figure 14 is a SDS PAGE gel for post-dialysed ammonium sulphate precipitated (200g/L and 250 g/L) samples, DCFT26a, harvest point:
  • Lane 2 0.67 ⁇ g collagenase I and 0.72 ⁇ g collagenase II
  • Lane 3 0.27 ⁇ g collagenase I and 0.29 ⁇ g collagenase II
  • Lane 6 post dialysed sample — 200g/L AS (1/5)
  • Lane 7 post dialysed sample - 200g/L AS (1/10)
  • Lane 8 post dialysed sample — 250g/L AS (Neat)
  • Lane 9 post dialysed sample - 250g/L AS (1/5)
  • Lane 10 post dialysed sample - 250g/L AS (1/10);
  • Figure 15 is a SDS PAGE gel for post-dialysed ammonium sulphate precipitated (300g/L and 400 g/L) samples, DCFT26a, harvest point: Lane 1: High Molecular Weight Marker
  • Lane 3 0.27 ⁇ g collagenase I and 0.29 ⁇ g collagenase II Lane 4: 6.12 ⁇ L of supernatant sample from SC 11
  • Lane 7 post dialysed sample - 300g/L AS ( 1 /10 di lution)
  • Lane 8 post dialysed sample - 400g/L AS (Neat)
  • Lane 9 post dialysed sample — 4000g/L AS (1/5 dilution)
  • Lane 10 post dialysed sample - 400g/L AS ( 1 /10 dilution);
  • Figure 16 depicts a Growth curves (OD vs time and net OD vs time) of C. histolyticum in PBFT57 fermentation;
  • Figure 17 is a Semi-quantitative SDS PAGE gel, harvest point sample:
  • Lane 4 0.135 ⁇ g collagenase I
  • Lane 5 0.29 ⁇ g collagenase II
  • Lane 8 2.04 ⁇ L of sample (1/3 dilution of fermentation harvest sample)
  • Lane 9 1.53 ⁇ L of sample (1/4 dilution of fermentation harvest sample)
  • Lane 10 1.22 ⁇ L of sample (1/5 dilution of fermentation harvest sample)
  • Lane 11 0.87 ⁇ L of sample (1/7 dilution of fermentation harvest sample);
  • Figure 18a is a quantitative SDS PAGE gel for post-dialysed 50OmL sample from fermentation PBFT57, harvest point sample. 400g/L of ammonium sulphate added:
  • Lane 2 0.272 ⁇ g collagenase I and 0.286 ⁇ g collagenase II
  • Lane 3 0.181 ⁇ g collagenase I and 0.190 ⁇ g collagenase II
  • Lane 5 0.109 ⁇ g collagenase I and 0.114 ⁇ g collagenase II
  • Lane 6 post dialysed sample - 400g/L AS (1/15 dilution)
  • Lane 7 post dialysed sample - 400g/L AS (1/20 dilution)
  • Lane 8 post dialysed sample - 400g/L AS (1/25 dilution)
  • Lane 9 post dialysed sample - 400g/L AS (1/30 dilution)
  • Lane 10 post dialysed sample - 400g/L AS (1/35 dilution)
  • Figure 18b is a SDS PAGE of the supernatants after centrifugation of the ammonium sulphate precipitated samples:
  • Lane 1 High Molecular Weight Marker Lane 2: 0.27 ⁇ g Col I and 0.29 ⁇ g Col II
  • Lane 4 Supernatant (neat) of post ammonium sulphate precipitated sample (400g/L fast addition)
  • Lane 5 Supernatant (neat) of post ammonium sulphate precipitated sample (440g/L slow addition)
  • Lane 8 Supernatant (neat) of post ammonium sulphate precipitated sample (400g/L, pH 6)
  • Lane 9 Supernatant (neat) of post ammonium sulphate precipitated sample (400g/L, oxygenated);
  • Figure 19 is a Semi-quantitative SDS PAGE gel showing diluted samples from the harvest point supernatant and the post dialysed ammonium sulphate (with 400g/L - fast addition) precipitated sample:
  • Lane 2 Fermentation sample - harvest (neat)
  • Lane 3 Fermentation sample - harvest (1/1 dilution)
  • Lane 4 Fermentation sample - harvest (1/2 dilution)
  • Lane 5 Fermentation sample - harvest (1/3 dilution)
  • Lane 6 Fermentation sample - harvest (1/4 dilution)
  • Lane 7 Post dialysed sample - harvest (1/17.54 dilution) corresponds to lane 1
  • Lane 8 Post dialysed sample - harvest (1/35.08 dilution) corresponds to lane 2
  • Lane 9 Post dialysed sample - harvest (1/52.62 dilution) corresponds to lane 3
  • Lane 10 Post dialysed sample - harvest (1/70.16 dilution) corresponds to lane 4
  • Lane 11 Post dialysed sample - harvest (1/87.70 dilution) corresponds to lane 5;
  • Figure 20 is a semi-quantitative SDS PAGE gel for PBFT57 showing diluted samples from the harvest point supernatant and the post dialysed ammonium sulphate (with 520g/L) precipitated sample:
  • Lane 7 Post dialysed sample - harvest (1/15.63) corresponds to lane
  • Lane 8 Post dialysed sample - harvest (1/31.26) corresponds to lane
  • Lane 9 Post dialysed sample - harvest (1/46.89) corresponds to lane
  • Lane 10 Post dialysed sample - harvest (1/62.52) corresponds to lane
  • Lane 11 Post dialysed sample - harvest (1/78.15) corresponds to lane
  • Figure 21 depicts growth curves (Net OD vs time) of C. histolyticum strains 004 and 013 in PBFT58c,d fermentations;
  • Figure 22 is a SDS PAGE gel for PBFT58c (Strain 004):
  • Lane 1 High Molecular Weight Marker Lane 2: Collagenase l - l .OO ⁇ g
  • Lane 3 Collagenase l - 0.67 ⁇ g
  • Lane 5 Collagenase II - 0.72 ⁇ g
  • Lane 6 16.25h (6.12 ⁇ L of sample)
  • Lane 7 17h (6.12 ⁇ L of sample)
  • Lane 10 20.5h (6.12 ⁇ L of sample);
  • Figure 23 is a SDS PAGE gel for PBFT58d (Strain 013): Lane 1 : High Molecular Weight Marker
  • Lane 2 Collagenase l - l.OO ⁇ g
  • Lane 3 Collagenase l - 0.67 ⁇ g
  • Lane 5 Collagenase II - 0.72 ⁇ g
  • Lane 6 16.25h (6.12 ⁇ L of sample)
  • Lane 10 20.5h (6.12 ⁇ L of sample);
  • Figure 24 is a semi-quantitative SDS PAGE gel for PBFT58c (strain 004), harvest point sample:
  • Lane 3 0.18 ⁇ g collagenase I and 0.19 ⁇ g collagenase II
  • Lane 4 0.135 ⁇ g collagenase l and 0.145 ⁇ g collagenase II
  • Lane 10 L22 ⁇ L of sample
  • Figure 25 is a semi-quantitative SDS PAGE gel for PBFT58d (strain 013), harvest point sample:
  • Lane 3 0.18 ⁇ g collagenase I and 0.19 ⁇ g collagenase II
  • Lane 4 0.135 ⁇ g collagenase I and 0.145 ⁇ g collagenase II
  • Figure 26 is SDS PAGE gel for post-dialysed harvest point sample (520g/L ammonium sulphate) of PBFT58c fermentation (strain 004): Lane 1 : High Molecular Weight Marker Lane 2: 0.27 ⁇ g collagenase I and 0.29 ⁇ g collagenase II
  • Lane 4 0.135 ⁇ g collagenase I and 0.145 ⁇ g collagenase II
  • Lane 5 0.108 ⁇ g collagenase I and 0.116 ⁇ g collagenase II
  • Lane 8 post dialysed harvest point sample — (1/10 dilution)
  • Lane 9 post dialysed harvest point sample — (I/I 5 dilution)
  • Lane 10 post dialysed harvest point sample — (1/20 dilution);
  • Figure 27 is a SDS PAGE gel for post-dialysed harvest point sample (400g/L ammonium sulphate) of PBFT58d fermentation (strain 013): Lane 1 : High Molecular Weight Marker
  • Lane 2 0.27 ⁇ g collagenase I and 0.29 ⁇ g collagenase IT Lane 3: 0.18 ⁇ g collagenase I and 0.19 ⁇ g collagenase II
  • Lane 4 0.135 ⁇ g collagenase I and 0.145 ⁇ g collagenase II
  • Lane 5 0.108 ⁇ g collagenase I and 0.116 ⁇ g collagenase II
  • Lane 6 post dialysed harvest point sample —
  • Neat Lane 7 post dialysed harvest point sample — (1/5 dilution)
  • Lane 8 post dialysed harvest point sample — (1/10 dilution)
  • Lane 9 post dialysed harvest point sample — (1/15 dilution)
  • Lane 10 post dialysed harvest point sample — (1/20 dilution);
  • Figure 28 is illustrates a flow chart of the Experimental procedure used for screening the alternative vegetable peptones;
  • Figure 29 illustrates a fed-batch strategy for DCFT27a,b fermentations
  • Figure 30 depicts growth curves (Net OD vs time) of C. histolyticum in 5L DCFT27a and DCFT27b fed-batch fermentations;
  • Figure 31 depicts growth curves (Net OD vs time) of C. histolyticum in 5L PBFT59a,b,c batch fermentations;
  • Figure 32 depicts a growth curve (Net OD vs time) of C. histolyticum in 5L DCFT27d fed-batch fermentation
  • Figure 33a is a SDS PAGE gel for DCFT27d (Phytone supplemented with amino acids): Lane 1 : High Molecular Weight Marker
  • Lane 5 14h (6.12 ⁇ L of sample)
  • Lane 6 13h (6.12 ⁇ L of sample)
  • Lane 7 1 1.3h (6.12 ⁇ L of sample)
  • Lane 8 0.27 ⁇ g Collagenase I and 0.29 ⁇ g Collagenase U;
  • Figure 33b represents a schematic diagram of the inoculation procedure
  • Figure 33c represents a flow chart of an approximately 200 L fed batch inoculation process
  • Figure 34 shows a chromatogram after hydroxyapatite chromatography
  • Figure 35 shows a chromatogram after a fractogel TMAE anion exhange
  • Figure 36 is an 8% Tris-Glycine SDS-PAGE analysis of Pre HA 5 Post HA and Post TMAE material from 5 L scale rocess:
  • Figure 37 shows a chromatogram after a fractogel TMAE anion exhange
  • Figure 38 is an 8% Tris-Glycine SDS-PAGE analysis of Q Sepharose IEX chromatography of post TMAE material run in the presence leupeptin:
  • Figure 39 is an 8% Tris-Glycine SDS-PAGE analysis of Q Sepharose IEX chromatography of post TMAE material run in the presence of leupeptin.
  • Gel 2- Peak 2 (ABCI :
  • Figure 40 shows a chromatogram after a Q Sepharose HP anion exchange with modified gradient
  • Figure 41 shows a chromatogram after a Superdex 75 Gel Permeation chromatography of ABCII;
  • Figure 42 is a 12% Bis-Tris SDS-PAGE analysis of Superdex 75 GPC of concentrated ABC II run in the presence of arginine:
  • Figure 43 shows a chromatogram after a Superdex 75 Gel Permeation chromatography of ABCI
  • Figure 44 is a 4-12% Bis-Tris SDS-PAGE analysis of Superdex 75 GPC of concentrated ABC I run in the presence of arginine:
  • Figure 46 represents a flow chart of the fermentation procedure for process 3.
  • Figure 47 represents a flow chart of the purification procedure for process 3.
  • Figure 48 is a SDS-PAGE (reduced) Coomasie stained for Intermediates AUXI and AUXII: Lane
  • Figure 49 is a SDS-PAGE (reduced) Coomasie stained for Drug Substance:
  • Figure 50 is SDS-PAGE (reduced) Silver stained Drug Substance: Lane
  • Figure 51 depicts a comparison of C. histolyticum grown on Proteose Peptone #3 in a batch fermentation to the existing fermentation process using Phytone peptone during fed-batch cultivation;
  • Figure 52 is a SDS-PAGE analysis of the collagenase product at the harvest point (2Oh) of a 5L Proteose Pe tone #3 batch fermentation GCFT03b 8% Tris-Glycine):
  • Figure 53 is a SDS-PAGE analysis of the collagenase product at the harvest point (2Oh) of a 5L Phytone fed-batch fermentation (GCFT03d) (8% Tris-Glycine):
  • Figure 54 illustrates three fermentations of Clostridium histolyticum grown on 50g/L PP3 demonstrating a reproducible growth profile:
  • Figure 55 is a SDS-PAGE analysis showing the time course of GCFT05d (batch fermentation with Proteose Peptone #3), 8% Tris Glycine gel, colloidal stained):
  • Figure 56 is a SDS-PAGE analysis showing the time course of GCFT05d (batch fermentation with Proteose Peptone #3), (8% Tris Glycine gel, silver stained):
  • Figure 57 is a SDS-PAGE analysis showing the time course of DCFT24b (fed- batch fermentation using Phytone peptone), (8% Tris Glycine gel, colloidal stained):
  • Figure 58 illustrates a comparison of growth curves from C. histolyticum fermentations using different lots of PP3:
  • Figure 59 illustrates a small scale comparison of three lots of PP3 and evaluation
  • Figure 60 depicts a growth profiles of two 5L fermentations utilizing PP3 at lOOg/L:
  • Figure 61 is a SDS-PAGE analysis of the time course of PBFT70c, 100g/L PP3 (lot # 5354796) fermentation (8% Tris-Glycine):
  • Figure 62 is a SDS-PAGE analysis of the timecourse of PBFT70d, 100g/L PP3 (lot # 5325635) fermentation (8% Tris-Glycine):
  • Figure 63 represents a densitometry analysis of SDS-PAGE to compare cell growth to product formation from 5L fermentation PBFT70c:
  • Figure 64 illustrates a Comparison of lOOg/L PP3 process at 5L and 200L scale:
  • Figure 65 is a SDS-PAGE analysis of the time course of the 200L fermentation (8% Tris-GIycine):
  • Figure 66 represents a densitometry analysis of SDS-PAGE to compare cell growth to product formation from 200L fermentation:
  • Figure 67 is a SDS-PAGE analysis of the time course of the 200L fermentation (4- 12% Bis-Tris):
  • Figure 68 shows a standard curve for densitometry quantification of collagenase concentration.
  • Figure 69 represents a schematic illustration of the fermentation and harvest of Clostridium histolyticum.
  • Figures 70 are chromatograms resulting from Hydrophobic interaction chromatography using Phenyl Sepharose FF (low sub): (a) is full scale chromatogram and (b) is an expanded chromatogram showing fraction collection.
  • Figure 71 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the Mustang Q step to the TFFl step.
  • the gel is stained with Colloidal blue and overloaded 10 (2.5 ⁇ g total rotein/lane to show contaminant bands:
  • Figure 72 is an Ion exchange chromatogram (Q Sepharose HP) of the post HIC material after concentration and d ⁇ afiltration into 1OmM Tris, 20OuM leupeptin pH 8.
  • Figure 73 is a 4-12% Bis Tris SDS-PAGE analysis of fractions from peak 1 15 (AUXII) eluted during the ion exchange column (figure 5).
  • Gel 1 the gel is stained with Colloidal blue:
  • Figure 74 is a 4-12% Bis Tris SDS-PAGE analysis of fractions from peak 1 (AUXII) eluted during the ion exchange column (figure 5).
  • Gel 2 the gel is stained with Colloidal blue:
  • Figure 75 is a 4-12% Bis Tris SDS-PAGE analysis of fractions from peak 2 (AUXI) eluted during the ion exchange column (figure 5).
  • Gel 3 the gel is stained with Colloidal blue:
  • Figure 76 is a 4-12% Bis Tris SDS-PAGE analysis of fractions from peak 2 (AUXI) eluted during the ion exchange column (figure 5).
  • Gel 4 the gel is stained with
  • Figure 77 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the anion exchange step to final product. The gel is stained with Colloidalblue. GeI 1: l ⁇ g/lane loading:
  • Figure 78 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the anion exchange step to final product. The gel is stained with Colloidal blue. Gel 2: 2.5 ⁇ g/lane loading:
  • Figure 79 is a SDS-PAGE with 8% Tris Glycine (NB Ref AS/ 1640/020):
  • Figure 80 is a SDS-PAGE with 8% Tris Glycine:
  • Figure 81 is a SDS-PAGE gel: 1. High Molecular Weight Markers
  • Figure 82 represents analytical chromatography analysis.
  • Figure 83 shows protein concentration determination by UV.
  • Figure 84 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the 2OL demonstration run-through taken at the point of manufacture and stored at -20 0 C. The gel is stained with Colloidal blue, l loadin :
  • Figure 85 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the 2OL demonstration run-through after 22hrs at Room Temperature. The gel is stained with Colloida
  • Figure 86 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the 2OL demonstration run-through after 22hrs at 37°C. The gel is stained with Colloidal blue:
  • Figure 87 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the 2OL demonstration run-through after 94hrs at Room Temperature. The gel is stained with Colloidal blue:
  • Figure 88 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the 2OL demonstration run-through after 94hrs at 37°C. The gel is stained with Colloidal blue:
  • Figure 89 is a 8% Tris-Glycine SDS-PAGE analysis of selected post IEX AUX I and post IEX AUX II fractions. Fractions were selected from the 2OL demonstration run which were enriched for the required contaminant protein. The gel is stained with Colloidal blue:
  • Figure 90 is a 8% Tris-Glycine SDS-PAGE analysis of selected post IEX AUX I and post IEX AUX II fractions. Fractions were selected from purified material generated from fermentation 2OL PP3 and enriched for the ⁇ 90kDa contaminant protein. The gel is stained with Colloidal blue:
  • the invention provides a novel collagenase drug substance comprising a mixture of highly purified collagenase I and collagenase II in a mass ratio of about 1 to 1. It has been discovered that a composition comprising a mixture of collagenase I and collagenase II in an artificial mass ratio of 1 to 1 provides highly reproducible and optimal enzymatic activity and imparts superior therapeutic effect while lowering the potential for side effects. Tt is understood that the terms "drug substance”, “drug product” or “collagenase composition” can be used interchangeably.
  • the present invention provides a drug substance consisting of collagenase I and collagenase II having the sequence of Clostridium histolyticum collagenase I and collagenase II, respectively, having a mass ratio of about 1 to 1 with a purity of at least 95% by area, and preferably a purity of at least 98% by area.
  • the present invention provides a drug substance, wherein the drug substance having at least one specification selected from table A below:
  • the invention provides a process for producing a drug substance consisting of collagenase I and collagenase Il having the sequence of Clostridium histolyticum collagenase I and collagenase II, respectively, having a mass ratio of about 1 to 1 with a purity of at least 95% by area, comprising the steps of: a) fermenting Clostridium histolyticum; b) harvesting a crude product comprising collagenase I and collagenase II; c) purifying collagenase I and collagenase II from the crude harvest via filtration and column chromatography; and d) combining the collagenase I and collagenase II purified from step (c) at a ratio of about 1 to 1.
  • the fermentation step is conducted in the presence of a porcine derived, a phytone peptone or a vegetable peptone medium. More preferably, the porcine derived medium is proteose peptone #3.
  • the invention provides a fermentation procedure comprising the steps of: a) innoculating the medium in a first stage with Clostridium histolyticum and agitating the mixture; b) incubating the mixture from step (a) to obtain an aliquot; c) inoculating the medium in a second stage with aliquots resulting from step (b) and agitating the mixture; d) incubating mixtures from step (c); e) inoculating the medium in a third stage with aliquots resulting from step (d) and agitating; f) incubating mixtures from step (e); g) inoculating the medium in a fourth stage with an aliquot resulting from step (f) and agitating; h) incubating mixtures from step (g); and i) harvesting culture resulting from step (h) by filtration.
  • the fermentation procedure comprises the steps of: a) Inoculating 3 x 25mL PP3 (proteose peptone) medium with 3 x 250 ⁇ L of WCB (25mL cultures in 3 x 125mL shake flasks, contained within Anaerobe gas jar) at a temperature set point of 37°C, and agitating the mixture at 125rpm; b) incubating the mixture from step (a) for 12 hours; c) inoculating Inoculate 4 x 20OmL PP3 medium with 4 x 5mL aliquots from 1 of the above 25 mL cultures (20OmL cultures in 4 x 50OmL shake flasks, contained within Anaerobe gas jar) at a temperature set point of 37 0 C, and agitating the mixture at 125rpm; d) incubating mixtures from step (c) for 12 hours; e) inoculating 14.4L of PP3 medium with 3 x 20OmL culture
  • the invention provides a purification procedure comprising the steps of: a) filtering the crude harvest through a Mustang Q anion-exchange capsule filter; b) adding ammonium sulphate; preferably to a final concentration of IM; c) filtering the crude harvest; preferably through a 0.45 ⁇ m filter; d) subjecting the filtrate through a HTC column; preferably a phenyl sepharose 6FF (low sub); e) adding leupeptin to the filtrate; preferably to a final concentration of 0.2 mM to post HIC eluted product; f) removing the ammonium sulfate and maintaining leupeptin for correct binding of collagenase I and collagenase II with buffer exchange by TFF; preferably with buffer exchange by TFF; g) filtering the mixture of step (f); preferably through a 0.45 ⁇ m filter; h) separating collagenase I and collagenase II using Q-Sepharose HP; i)
  • the drug substance of the present invention includes both collagenase I and collagenase II.
  • a preferred source of crude collagenase is from a bacterial fermentation process, specifically the fermentation of C. histolyticum (C. his). In one embodiment of the invention, a fermentation process is described.
  • the crude collagenase obtained from C. his may be purified by a variety of methods known to those skilled in the art, including dye ligand affinity chromatography, heparin affinity chromatography, ammonium sulfate precipitation, hydroxylapatite chromatography, size exclusion chromatography, ion exchange chromatography, and metal chelation chromatography. Crude and partially purified collagenase is commercially available from many sources including Advance Biofactures Corp., Lynbrook, New York.
  • Both collagenase I and collagenase II are metalloproteases and require tightly bound zinc and loosely bound calcium for their activity (Eddie L. Angleton and H. E. Van Wart, Biochemistry 1988, 27, 7406- 7412). Both collagenases have broad specificity toward all types of collagen (Steinbrink, D; Bond, M and Van Wart, H; (1985), JBC, 260 p2771-2776). Collagenase I and Collagenase II digest collagen by hydrolyzing the triple-helical region of collagen under physiological conditions (Steinbrink, D; Bond, M and Van Wart, H; (1985), JBC, 260 p2771 - 2776). Even though each collagenase shows different specificity (e.g.
  • Col lagenase Il has a higher activity towards all kinds of synthetic peptide substrates than collagenase I as reported for class II and class I collagenase in the literatures. [Bond, M.D. (1984), Biochemistry, 23: p.3085-3091. Hesse, F, (1995), Transplantation Proceedings, 27: p.3287-3289].
  • collagen mediated-diseases examples include but are not limited to: Dupuytren's disease; Peyronie's disease; frozen shoulder (adhesive capsulitis), keloids; hypertrophic scars; depressed scars such as those resulting from inflammatory acne; post-surgical adhesions; acne vulgaris; lipomas, and disfiguring conditions such as wrinkling, cellulite formation and neoplastic fibrosis.
  • U.S. Pat. Nos. 6,086,872 and 5,589,171 incorporated herein by reference disclose the use of collagenase preparations in the treatment of Dupuytren's disease.
  • U.S. Pat. No. 6,022,539 incorporated herein by reference discloses the use of collagenase preparations in the treatment of Peyronie's disease.
  • the composition of the invention is also useful for the dissociation of tissue into individual cells and cell clusters as is useful in a wide variety of laboratory, diagnostic and therapeutic applications. These applications involve the isolation of many types of cells for. various uses, including microvascular endothelial cells for small diameter synthetic vascular graft seeding, hepatocytes for gene therapy, drug toxicology screening and extracorporeal liver assist devices, chondrocytes for cartilage regeneration, and islets of Langerhans for the treatment of insulin-dependent diabetes mellitus. Enzyme treatment works to fragment extracellular matrix proteins and proteins which maintain cell-to-cell contact. Since collagen is the principle protein component of tissue ultrastructure, the enzyme collagenase has been frequently used to accomplish the desired tissue disintegration. In general, the composition of the present invention is useful for any application where the removal of cells or the modification of an extracellular matrix, are desired.
  • Collagenase compositions of the invention may also be prepared by mixing either a specific number of activity units or specific masses of the preferably purified enzymes. Collagenase activity can be measured by the enzyme's ability to hydrolyze either synthetic peptide or collagen substrate. Those skilled in the art will recognize that enzyme assays other than those disclosed herein may also be used to define and prepare functionally equivalent enzyme compositions.
  • Another aspect of the present invention is the reproducible optimization of the 1 to 1 mass ratio of collagenase I to collagenase II in the composition of the invention. The reproducibility of the ratio of collagenase I to collagenase II has previously been a challenge because of several factors.
  • the invention also provides pharmaceutical formulations of the compositions of the invention.
  • the pharmaceutical formulations of the present invention comprise a therapeutically effective amount of a collagenase composition of the present invention formulated together with one or more pharmaceutically acceptable carriers or excipients.
  • the term "pharmaceutically acceptable carrier or excipient” means a non-toxic, inert solid, semi-solid or liquid filler, diluent, encapsulating material or formulation auxiliary of any type.
  • materials which can serve as pharmaceutically acceptable carriers are sugars such as lactose, glucose and sucrose; starches such as corn starch and potato starch; cellulose and its derivatives such as sodium carboxymethyl cellulose, ethyl cellulose and cellulose acetate; powdered tragacanth; malt; gelatin; talc; glycols such as propylene glycol; esters such as ethyl oleate and ethyl laurate; agar; buffering agents such as magnesium hydroxide and aluminun hydroxide; alginic acid; pyrogen-free water; isotonic saline; Ringer's solution; ethyl alcohol, and phosphate buffer solutions, as well as other non-toxic compatible lubric
  • compositions of this invention may be administered parenteral Iy, topically, or via an implanted reservoir.
  • parenteral as used herein includes subcutaneous, intracutaneous, intravenous, intramuscular, intraarticular, intraarterial, intrasynovial, intrasternal, intrathecal, intralesional and intracranial injection or infusion techniques.
  • the composition is injected into the disfiguring tissue.
  • the composition is injected into the cord or plaque.
  • local administration is defined herein to embrace such direct injection.
  • Injectable preparations for example, sterile injectable aqueous or oleaginous suspensions, may be formulated according to the known art using suitable dispersing or wetting agents and suspending agents.
  • the sterile injectable preparation may also be a sterile injectable solution, suspension or emulsion in a nontoxic parenterally acceptable diluent or solvent, for example, as a solution in 1, 3-butanediol.
  • acceptable vehicles and solvents that may be employed are water, Ringer's solution, U.S.P. and isotonic sodium chloride solution.
  • sterile, fixed oils are conventionally employed as a solvent or suspending medium.
  • any bland fixed oil can be employed including synthetic mono- or diglycerides.
  • fatty acids such as oleic acid are used in the preparation of injectables.
  • the injectable formulations can be sterilized, for example, by filtration through a bacterial-retaining filter, or by incorporating sterilizing agents in the form of sterile solid compositions which can be dissolved or dispersed in sterile water or other sterile injectable medium prior to use.
  • the sterile solutions may also be lyophilized for later use.
  • Dosage forms for topical or transdermal administration of a compound of this invention include ointments, pastes, creams, lotions, gels, powders, solutions, sprays, inhalants or patches.
  • the active component is admixed under sterile conditions with a pharmaceutically acceptable carrier and any needed preservatives or buffers as may be required.
  • the ointments, pastes, creams and gels may contain, in addition to an active compound of this invention, excipients such as animal and vegetable fats, oils, waxes, paraffins, starch, tragacanth, cellulose derivatives, polyethylene glycols, silicones, bentonites, silicic acid, talc and zinc oxide, or mixtures thereof.
  • excipients such as animal and vegetable fats, oils, waxes, paraffins, starch, tragacanth, cellulose derivatives, polyethylene glycols, silicones, bentonites, silicic acid, talc and zinc oxide, or mixtures thereof.
  • Powders and sprays can contain, in addition to the compounds of this invention, excipients such as lactose, talc, silicic acid, aluminum hydroxide, calcium silicates and polyamide powder, or mixtures of these substances.
  • Sprays can additionally contain customary propellants such as chlorofluorohydrocarbons.
  • Transdermal patches have the added advantage of providing controlled delivery of a compound to the body. Such dosage forms can be made by dissolving or dispensing the compound in the proper medium.
  • Absorption enhancers can also be used to increase the flux of the compound across the skin. The rate can be controlled by either providing a rate controlling membrane or by dispersing the compound in a polymer matrix or gel.
  • the drug substance of the invention is a lyophilized injectable composition formulated with lactose.
  • each milligram of injectable collagenase is formulated with 1.9 mg of lactose.
  • each milligram of injection collagenase preferably has approximately 2800 SRC units and 51000 units measured with a potency assay using a synthetic substrate, pzGPGGPA.
  • the collagenase composition of the invention is a lyophilized injectable composition formulated with Sucrose, Tris at a pH level of about 8.0.
  • 1.0 mg of the drug substance of the invention is formulated in 60 mM Sucrose, 10 mM Tris, at a pH of about 8.0 (this equates to 20.5 mg/mL of sucrose and 1.21 mg/mL of Tris in the formulation buffer).
  • Examples of some of the formulations include, but not limited to: for a 0.58 mg of the drug substance dose, 18.5 mg of sucrose and 1.1 mg of Tris are added in each vial, where the targeting a vial fill volume is 0.9 ml; and for a 0.58 mg of the drug substance dose, 12.0 mg sucrose (multicompendial) and 0.7 mg of Tris (multicompendial).
  • methods are provided for treating collagen- mediated diseases comprising the step of administering to a patient in need thereof, a therapeutically effective amount of a composition of the invention, or a therapeutically effective amount of a pharmaceutical formulation of the invention.
  • a therapeutically effective amount of a compound of the invention is meant an amount of the compound which confers a therapeutic effect on the treated subject, at a reasonable benefit/risk ratio applicable to any medical treatment.
  • the therapeutic effect may be objective (i.e., measurable by some test or marker) or subjective (i.e., subject gives an indication of or feels an effect).
  • Effective doses will also vary depending on route of administration, as well as the possibility of co-usage with other agents. It will be understood, however, that the total daily usage of the compositions of the present invention will be decided by the attending physician within the scope of sound medical judgment.
  • the specific therapeutically effective dose level for any particular patient will depend upon a variety of factors including the disorder being treated and the severity of the disorder; the activity of the specific compound employed; the specific composition employed; the age, body weight, general health, sex and diet of the patient; the time of administration, route of administration, and rate of excretion of the specific compound employed; the duration of the treatment; drugs used in combination or contemporaneously with the specific compound employed; and like factors well known in the medical arts.
  • the drug substance for injectable collagenase consists of two microbial collagenases, referred to as Collagenase AUX I and Collagenase ABC I and Collagenase AUX II and Collagenase ABC II. It is understood that the terms “Collagenase I”, “ABC I”, “AUX I”, “collagenase AUX I”, and “collagenase ABC I” mean the same and can be used interchangeably. Similarly, the terms “Collagenase II”, “ABC II”, “AUX II”, “collagenase AUX II”, and “collagenase ABC II” refer to the same enzyme and can also be used interchangeably. These collagenases are secreted by bacterial cells.
  • Collagenase AUX I has a single polypeptide chain consisting of approximately 1000 amino acids with a molecular weight of 115 kDa.
  • Collagenase AUX II has also a single polypeptide chain consisting of about 1000 amino acids with a molecular weight of 1 10 kDa. Even though the literature indicates that there are sequence homologies in regions of collagenase AUX I and AUX II, the two polypeptides do not seem to be immunologically cross reactive as indicated by the western blot analysis.
  • the drug substance (collagenase concentrate) has an approximately 1 to 1 mass ratio for collagenase AUX I and AUX II.
  • the collagenase concentrate has an extinction coefficient of 1.528.
  • PROCESS 2 Fermentation Process This work was set out to develop a fermentation process that aimed at delivering a target yield of 250mg/L of total collagenases ABC I & II from the 5L fermentation scale process in an animal free component growth media.
  • Figure 1 shows the growth curves (ODeoo n m vs time) from the two fermentations
  • Figure 2 shows the net growth curves (Net OD ⁇ oo nm vs time). It was observed that the cells from the first fermentation grew very fast and reached their maximum OD after approximately 10 hours. This was due to the fact that the media in the batch phase was very rich. During the fed-batch phase the cells did not appear to grow. The OD values decreased slightly, which could be partly attributed to the fact that the cells were dying and to the dilution effect of the feed in to the fermenter.
  • SDS PAGE gels SDS PAGE analysis (8% Tris - Glycine gels) of the supernatant samples were carried out for each for the two fermentations. The gels are shown in Figure 3 and 4. A semi - quantitative SDS PAGE gel was also produced for the harvest point sample of the second fermentation.
  • the SDS PAGE gel analysis in Figure 4 indicated that very low amounts of the collagenases were expressed. This could be due to the fact that the cells grew very fast during the batch phase and as a result the maximum cell concentration was reached after approximately 10. hours. In contrast, very high level of collagenase expression was observed in the second fermentation, probably due to the fact that the cells grew more slowly during the short batch phase and continued to grow during the fed-batch phase.
  • the invention relates to an improved fermentation method for C. his wherein cell growth is controlled and slow during the short batch phase and continuing growth during the fed-batch phase. Slow growth is defined to mean that the rate of growth during the short batch phase does not result in a maximum cell concentration prior to the fed-batch phase, such as within about 10 hours of the beginning of the fermentation process. In a preferred embodiment, the rate of growth is approximately that resulting from the second fermentation cycle described herein.
  • the next step was to perform an additional set of fed-batch fermentations using slightly modified fed-batch strategies and media.
  • the aim was to improve the scalability and robustness of the fermentation process.
  • the media recipe for this fermentation was the same as above, with the exception that the phytone peptone and the yeast extract in the batch phase were filter sterilised instead of being autoclaved. This was done in order to avoid autoclaving the yeast extract and phytone, which can potentially affect their composition by heat and denaturation of proteins in the media.
  • the amount of yeast extract and phytone peptone was increased. This was done so that the concentration of yeast extract and peptone in the feed was less than that in DCFT26a and thus easier to make up and filter sterilise.
  • the strategy followed was the same, a 6h batch phase followed by a 14h fed-batch phase. Tables 3 and 4 present the media recipes, whereas Figure 6 the strategy used for both fermentations.
  • Figure 7 shows the growth curves (ODgoo nm vs time) from the two fermentations, whereas Figure 8 shows the net growth curves (Net OD ⁇ oo nm vs time).
  • the growth curves for DCFT26a and DCFT26b were very similar to that of DCFT24b shown in Figure 2.
  • the cells grew slowly during the fed-batch phase and reached a final net OD 6 oonm of approximately 3.5.
  • the invention relates to the use of the media recipe (of course, amounts set forth therein are approximated) set forth above in DCFT26b and the use of ammonium sulphate to precipitate collagenase wherein about 400 g/liter of ammonium sulfate is added to the collagenase-containing medium. 3 rd set of fed-batch fermentations
  • the primary aim was to assess the reproducibility of the developed fed- batch strategy.
  • a fed-batch fermentation was performed which was a replicate fermentation of DCFT26b.
  • the ammonium sulphate / precipitation steps were investigated in more detail compared to the previous small-scale study. More specifically, the aim was to examine the effect of various ammonium sulphate concentrations, from 60% (400g/L) up to 80% (530g/L) on the recovery of collagenases and clostripain in the post precipitated / dialysed samples.
  • two methods of treating the harvested supernatant samples were also assessed, i.e., shifting the pH and oxygenating the media.
  • Figure 16 shows the growth curve (OD ⁇ oonm vs time) and the net growth curve (Net OD 6 oo nm vs time) from the fermentation.
  • the growth curve was very similar to that ofDCFT26b, indicating the good reproducibility of the process.
  • Ammonium sulfate precipitation of fermentation harvest samples In order to evaluate the efficiency of the ammonium sulphate precipitation step, 7 x 50OmL supernatant samples were harvested. These were precipitated using the following six methods.
  • the pellets were re-suspended in 16.5mL of WFI and dialysed against 10OmM of K2HPO 4 (pH 6.7), with the exception of method 4, where the pellet was re-suspended in 16.SmL of 10OmM Of K 2 HPO 4 (pH 6) and dialysed against the same buffer. SDS PAGE gels were then performed in order to estimate the amounts of collagenases in the post-dialysed samples and evaluate the recovery of the precipitation /dialysis steps.
  • Fermentations of C. histolyticum 013 and 004 strains in the media containing animal derived components were performed. The aim was to compare strain 013 to strain 004 and evaluate the effect of the animal components on cell growth, collagenase expression and on the levels of contaminants.
  • the lyophilised strain was re-constituted in PBS and plated out onto
  • TSB/Proteose agar plates (30g/L TSB, 10g/L proteose peptone, 12g/L agar. The plates were incubated in an anaerobic jar in the presence of anaerobic gas packs.
  • PBFT58d (strain 013).
  • Table 6 presents the recipe of the TSB/Proteose media used.
  • Figure 21 shows the growth curves obtained (Net ODeoon m vs time).
  • strain 013 continued to grow slowly up to the harvest point (20 hours) whereas strain 004 grew up to a net OD ⁇ oo nm of approximately 2.7 and then stopped growing.
  • the final OD obtained using the animal derived TSB/Proteose media was lower.
  • SDS PAGE gels (8% Tris-Glycine gels) of the supernatant samples taken throughout the fermentations are shown in Figure 22 and Figure 23.
  • the invention relates to collagenase compositions which are free of clostripain, such as those produced by the fermentation processes described herein.
  • Enzymatic assay of clostripain was set up to measure the clostripain activity of post dialyzed samples. The following method was used: Enzymatic assay of clostripain:
  • Unit definition One unit will hydrolyze 1.0 ⁇ mole of BAEE per minute at pH 7.6 at 25°C in the presence of 2.5 mM DTT. Analysis of post dialvsed samples for clostripain activity:
  • the clostripain activity assay was used to analyze the post-dialyzed samples from the fermentations with the TSB/Proteose (PBFT58) and the vegetable based fed- batch fermentation (PBFT57). Table 8 summarizes the results. The results demonstrate that there was very low clostripain activity in the case of TSB/Proteose fermentations. In contrast the clostripain activity in the case of the fed-batch PBFT58 was very high.
  • Table 9 Composition of media used in shake flask experiment. All media were filter sterilised.
  • the shake flasks were incubated for 18 hours.
  • the cultures were analysed for ODeoon m and viable cell ocunts.
  • the cultures were filtered and the supernatants analysed by SDS PAGE.
  • the results from the OD ⁇ oonm measurements and viable cell counts are summarised in Table 10.
  • DCFT27a vegetable extract
  • Table 11 describes the media recipes, whereas Figure 29 the strategy used.
  • PBFT59a vegetable tryptone
  • PBFT59b vegetable extract
  • PBFT59c vegetable extract no.l
  • peptones were used at concentrations of 50g/L in an effort to mimic the concentration of the proteose peptone in the animal media (Proteose / Peptone) and the concentration of phytone peptone that was used previously.
  • the media recipe is shown in Table 12.
  • a fed-batch fermentation was carried out using the standard phytone peptone media supplemented with three amino acids, i.e., glutamine, tryptophan and asparagine. This fermentation was performed as the concentrations of these particular amino acids were lower in the phytone peptone compared to the animal TSB/Proteose media, based on the amino acid composition of these components, provided by the manufacturers. The aim here was to investigate whether addition of these amino acids could reduce any nutrient limitation that may be a contributing factor for the expression of clostripain.
  • the media recipe is shown in Table 13.
  • the fermentation strategy used was the standard fed-batch strategy used for DCFT26 and PBFT57 fermentations (see Figure 6).
  • Figure 33a shows the SDS PAGE gel of the supernatant samples taken throughout the fermentation.
  • the level of collagenases is similar to that seen for the standard fed-batch fermentation (see Figure 10 for SDS PAGE gel from DCFT26b). Although clostripain is still present in the fermentation, it did seem that its level was lower than that in DCFT26b.
  • the clostripain activity of the post-dialysed harvest point sample was estimated using the clostripain activity assay.
  • the clostripain activity of the post-dialysed harvest point sample taken from the 2OL lyophilization batch was also estimated. Since this particular batch was purified without showing significant collagenase degradation, knowledge of its clostripain activity would be informative.
  • Table 14 summarizes the enzymatic activities of the post-dialyzed samples. It also includes the enzymatic activities for the standard fed-batch fermentation PBFT57 and the animal TSB/Proteose peptone presented in Table 8, for comparative purposes.
  • the results from DCFT27d indicate that the addition of the amino acids reduces the activity of clostripain produced by the strain.
  • the ratio of clostripain to collagenase is approximately four fold lower in the amino acid supplemented fermentation compared to the control fed-batch fermentation.
  • the ratio of clostripain to collagenase in the animal-derived fermentation was ten fold lower than the amino acid supplemented fed-batch fermentation. It is possible that the reduction of clostripain activity may result in significant reduction on the degradation of collagenases during purification.
  • a series of 5L fermentations were conducted to assess several fed-batch fermentation strategies.
  • the strategies were assessed based on their yield of collagenase, quantity of contaminants and scalability. Based on these results an optimum fed-batch strategy was identified that resulted in a productivity of total collagenases of approximately 280 mg/L.
  • the fermentation strategy was modified by slightly increasing the batch media concentration and reducing the fed-batch media concentration to improve its scalability. This change to the fermentation strategy had no effect on the productivity or levels of contaminants.
  • the second objective was to optimize the primary recovery step of the collagenases. Optimization of this step involved improvement in the yield of the process step or a reduction in the quantity of contaminants recovered or an increase in scalability.
  • a range of ammonium sulphate concentrations from 100 to 520 g/L were assessed. The effect of lowering the pH to 6.0 and oxygenating the media were also assessed. All ammonium sulphate concentrations below 400g/L showed very low recoveries of collagenase. No difference in the recovery of collagenase or clostripain was observed in any of the ammonium sulphate concentrations between 400 and 520 g/L.
  • the pellet from the 400 g/L precipitation was the easiest to re- suspend and this concentration was therefore defined as the optimum level.
  • a second set of fermentations was therefore carried out using the alternative peptones at 50 g/L in a batch strategy.
  • Vegetable Tryptone Sigma, 16922
  • Vegetable Extract Sigma, 05138
  • Vegetable Extract No. 1 (Sigma, 04316) were used as alternative peptones for these experiments.
  • SDS-PAGE no expression of collagenase or clostripain was seen.
  • a fed-batch fermentation using Phytone peptone was supplemented with three amino acids, glutamine, tryptophan and asparagine. These amino acids were identified as being present in lower amounts in the non-animal media.
  • the growth profile of the fermentation was very similar to that of the fed- batch fermentation without amino acid supplementation.
  • the media was filter sterilized Inoculation procedure
  • a vial from the internal cell bank was thawed and 0.025mL was used to inoculate 5mL of the inoculum media in a 3OmL universal.
  • the 5mL culture was incubated at 37°C in an anaerobic jar in the presence of anaerobic gas generators. After approximately 13 to 15 hours of incubation, 4mL of the culture was used to inoculate 20OmL of the inoculum media in a 50OmL flask. As previously the flask was placed in an anaerobic jar in the presence of anaerobic gas generators.
  • the invention further relates to an approximately 200 liter fed batch process as described in the flow chart in Figure 33c. Viable cell counting method
  • IM EDTA (to achieve final concentration of 1OmM).
  • the high molecular weight (HMW) marker was prepared by adding lO ⁇ l of concentrated stock to 80 ⁇ l reducing agent (1 Ox), 31 O ⁇ l WFI and 400 ⁇ l sample buffer (2x). The diluted HMW standard was then heated at 95 0 C for 5 minutes before aliquoting and storage at -2O 0 C for use in subsequent gels. Samples (15 ⁇ l) containing collagenases were run directly (i.e. with no prior heat treatment) on 8% Tris-Glycine gels using Tris-Glycine running buffer at 130V for -lhour 50m ⁇ ns. After electrophoresis, the gels were stained with colloidal blue stain reagent as per the manufacturer's instructions. Purification Process
  • Step 1 Ammonium sulfate precipitation of culture media supernatant
  • Buffer 1OmM Tris, 3mM CaCl 2 , 15OmM NaCl, 0.1 M Arginine pH8 Step8.
  • the AUXI and AUXII are pooled and concentrated individually, diafiltered into water and then pooled to form the final drug product.
  • Table 17 Purification from Q-Sepharose IEX to post Superdex 75 GPC.
  • Buffer B 1OmM Potassium Phosphate, 2M NaCl, pH6.7
  • Figure 35 illustrates a chromatogram after Fractogel TMAE anion exchange.
  • the unbound fraction pooled to give ⁇ 650mL at 0.5mg/mL. Dialysed into 1OmM Tris at pH8.
  • Figure 36 shows a SDS-PAGE gel of Pre HA, Post HA and Post TMAE material from 5L scale process. The gel is stained wth Colloidal blue.
  • O Sepharose HP anion exchange with original elution gradient Column size: 10OmL in XK50/20 (5.0cm bed height)
  • Buffer A 1 OmM Tris, 3mM CaCl 2 , 200 ⁇ M leupeptin, pH8.0
  • Buffer B 1OmM Tris, 3mM CaCl 2 , 36OmM NaCl, 200 ⁇ M leupeptin, pH8.0
  • Flow rate 18.0 mL/min
  • Elution 0-40% B over 20 CV
  • Figure 37 illustrates a chromatogram after Q Sepharose HP anion exchange with original elution gradient. Arginine is added to 0.1 M to ABCI and ABCII containing fractions. Peak 1 fraction (ABCII) pooled to give ⁇ 220mL at 0.55mg/mL which was concentrated by stirred-cell to give ⁇ 45mL at 2.8mg/mL. Peak 2 fractions (ABCI 5 excluding gelatinase shoulder) pooled to give ⁇ 19OmL at
  • Figure 38 shows a SDS-PAGE gel of Q Sepharose IEX chromatography of post TMAE material run in the presence of leupeptin for Peak 1 (ABCII). The gel is stained wth Colloidal blue.
  • Figure 39 shows a SDS-PAGE gel of Q Sepharose IEX chromatography of post TMAE material run in the presence of leupeptin for Peak 2 (ABCl). The gel is stained wth Colloidal blue.
  • Buffer A 1 OmM Tris, 3OmM NaCl, 3mM CaCl 2 , 200 ⁇ M leupeptin, pH8.0
  • Buffer B 1 OmM Tris, 3mM CaCl 2 , 36OmM NaCl, 200 ⁇ M leupeptin, ⁇ H8.0 Sample: 3mg post TMAE, post dialysis into 1 OmM Tris, 3OmM NaCl,
  • Figure 40 illustrates a chromatogram after Q Sepharose HP anion exchange with modified elution gradient. Good separation of ABCI and ABCII is observed. The second part of the gradient can be made steeper to sharpen ABCI peak.
  • Improvement of the peak can also be made using 5mL CV loaded at 3 and 1 Omg/mL media.
  • Figure 41 illustrates a chromatogram after superdex 75 gel permeation chromatography of ABCII (Peak 1 from IEX). Peak pooled to give ⁇ 60rnL ABC II at 1.2mg/mL.
  • Figure 42 shows a SDS-PAGE gel of superdex 75 gel permeation chromatography of concentrated ABC II run in the presence of arginine. The gel is stained wth Colloidal blue.
  • Buffer 1OmM Tris, 3mM CaCl 2 , 15OmM NaCl, 0.1 M arginine, pH8.0
  • Figure 43 illustrates a chromatogram after superdex 75 gel permeation chromatography of ABCI (Peak 2 from IEX). Peak pooled to give ⁇ 60mL ABC I at l.lmg/mL.
  • Figure 44 shows a SDS-PAGE gel of superdex 75 gel permeation chromatography of concentrated ABC I run in the presence of arginine. The gel is stained wth Colloidal blue. Scale up column sizing
  • Figure 44b illustrate a 5L purification process flow scheme.
  • the dialysis steps of the purification process described above can be substituted with ultrafiltration/diaf ⁇ ltrat ⁇ on (UF/DF) operations using dialysis and stirred cells will be replaced by TFF, tangential flow filtration.
  • UF/DF ultrafiltration/diaf ⁇ ltrat ⁇ on
  • the invention includes the collagenase products that are produced by (or can be produced by) the above purification processes.
  • Such collagenase products possess exceptional high degrees of purity and retained enzymatic activity.
  • the compositions are free of clostripain (e.g., possess negligible or undetectable levels of clostripain).
  • Figure 45 depicts a flow chart of the fermentation for process 3.
  • the Pall Mustang Q filter has been implemented for residual DNA and impurity clearance to further enhance yields and simplify the production process train and validation requirements.
  • the Quaternary Amine Sepharose High Performance (Q HP) operating parameters have been optimized to eliminate the Gel Permeation Chromatography (GPC) step.
  • the drug substance formulation has been modified to include 10 mM Tris, 60 mM Sucrose, pH 8.0, improving both product solubility and drug substance and drug product stability. The optimization process took place in two stages. The initial process
  • Process 2 utilizes an animal-free medium for all cell banking and fermentation stages with the fed-batch fermentation performed at the 20 Liter scale.
  • the downstream process has been adapted from Process 1 to include Mustang Q filtration for residual DNA removal and Superdex 75 GPC for additional host cell contaminant clearance.
  • Leupeptin has also been added to the chromatography buffer systems to prevent proteolytic degradation.
  • Process 2 material has been bridged analytically with Process 1 material (Table 21 A), and was tested in a side-by-side pre-clinical study outlined herein. Process 2 material has been proposed for use in the early stage of the Phase 3 clinical program.
  • the specifications for Process 2 intermediates and drug substance are detailed in Tables 22 and 23 respectively.
  • the initial in vitro potency assay was a bovine collagenase assay and did not differentiate collagenase types I and II. This assay was utilized for the material used in the open label, DUPYlOl and DUPY 202 clinical studies only, with the 0.58 mg dose typically resulting in a potency of 10,000 Units. Analysis of Process 1 material utilizing the current separate in vitro potency assays for type I collagenase and type II collagenase typically results in 1,700 to 3,500 Units/dose (0.58 mg dose) for type I collagenase and 43,000 to 69,000 Units/dose (0.58 mg dose) for type II collagenase.
  • Fig. 47 The purity level of Process 2 intermediates is shown in Fig. 47, a reduced SDS-PAGE Coomasie stained gel. The gel shows a single band for each intermediate with no other minor bands evident. AUX-I has an apparent MW of 1 15 IeDa and compares with the reference (ABC I), while AUX-II has an apparent MW of 110 IeDa and compares with the reference (ABC II).
  • Fig. 48 shows a reduced SDS-PAGE Coomasie stained gel depicting drug substance. As with the intermediates, drug substance manufactured by Process 2 compares with the reference (Process 1). A silver stained SDS-PAGE gel is depicted in Fig. 49 further substantiating the high purity level of the Process 2 drug substance.
  • the fermentation resulted in a higher product yield of >350mg/L total collagenase opposed to ⁇ 230mg/L from Process 2 (by semi quantitative SDS-PAGE analysis). Further fermentations using PP3 demonstrated that significantly less clostripain was produced using the animal derived fermentation medium. The first three fermentations (using one batch of PP3) demonstrated very consistent growth profiles. When the product was analysed by SDS-PAGE the yield and purity of collagenase was found to be very reproducible between the three fermentations.
  • the optimized fermentation process utilizing 100g/L PP3 was finally scaled to 200L.
  • the 200L growth profile was very similar to that seen at 5L scale.
  • SDS- PAGE analysis of the fermentation filtrate showed a high yield from the 200L fermentation, ⁇ 320mg/L total collagenase (by quantitative densitometry analysis).
  • the purity of the collagenase product (post fermentation) was similar at both 5L and 200L scale.2OL of the 200L fermentation filtrate was processed by the DSP group to represent a partial scale-up for the downstream process ⁇ infra).
  • the Proteose Peptone #3 fermentation process (Process 3) generated collagenase with a higher yield and with less clostripain than the existing Phytone process.
  • PP3 was shown to yield C. histofyticum cultivations with reproducible growth curves despite using various batches of PP3. Both the yield and purity of collagenase were also shown to be reproducible when using various lots of PP3. Evaluation of Proteose Peptone #3 as a raw material for production of collagenase from Clostridium histofyticum.
  • FIG. 51 compares the growth curve of the 50g/L PP3 (a lower . concentration than the Phytone concentration in Process 2) fermentation to the Phytone fed-batch fermentation.
  • the PP3 cultivation demonstrates a very rapid specific growth rate during exponential growth before entering stationary phase approximately 8 hours after inoculation.
  • the PP3 fermentation reached a maximum optical density (600nm) of 4.7 units.
  • the culture was left for a further 12 hours in stationary phase to monitor product formation / degradation.
  • Figure 52 shows SDS-PAGE semi-quantitative analysis of the concentration of the collagenase products from the 20 hour point of the PP3 cultivation.
  • Figure 53 shows the same analysis for the Phytone fed-batch process. It can be observed that the PP3 fermentation generates more product than the Phytone based process (an increase from 230mg/L to 360mg/L total collagenase, based on the semi-quantitative analysis in figures 52 and 53). The PP3 culture also expressed AUXI and AUXII at a 1 :1 ratio, whereas the Process 2 produced the two proteins at a 1:1.6 ratio. Reproducibility of Proteose Peptone #3 batch fermentation.
  • Figure 55 and 56 show SDS-PAGE analysis of the time course of PP3 fermentation GCFT05d (harvested at 11 hours).
  • the gel depicted in figure 55 has been stained with colloidal blue and the gel in figure 56 has been silver stained.
  • a third higher molecular weight band can be observed above the two collagenase bands on the gels in figures 55 and 56. It is thought that this band corresponds to an AUXI precursor protein reported in the literature.
  • the precursor band is present during the exponential growth phase. At the end of exponential growth the precursor band decreases in intensity and is not present after 11 hours (in GCFT05d).
  • Figure 57 shows SDS-PAGE analysis of samples from the time course of a standard Phytone fed-batch fermentation. A 40 kDa contaminant can be observed on the gel in figure 57. This 40 kDa contaminant band from the Phytone fed-batch process was identified as the protease clostripain.
  • optical densities (600nm) in the inoculum cultures showed very little variation (OD600 of 5mL stage; 2.9 - 3.6 units, OD600 of 20OmL stage; 4.5 - 5.9 units) and no reduction from previous inocula using PP3 lot # 5354796.
  • the variation and reduced optical density (600nm) only manifested itself in the final (fermentation) stage of the cultivation. This suggests that reason for the variation was a nutrient limitation in the PP3 and the quantity of the limiting nutrient varied between batches of PP3.
  • Figure 59 shows the results from the small scale experiment. It can be observed that lot 5325635 and 5332398 showed reduced optical densities (600nm) in the third stage of approximately 2.5 units, these were deemed to be "poor” batches of PP3. Lot 5354796 maintains an optical density (600nm) of 5 units in the third stage of cultivation, this was deemed to be a "good” batch of PP3. Interestingly when the concentration of a "poor" batch of PP3 (5332398) was increased to 100g/L the same optical density (600nm) was achieved in the second and third stage of the cultivation. This data does support the theory that the deviations in growth profiles are caused by variation in the quantity of a limiting nutrient between batches of PP3. It was not possible to identify this nutrient by analytical testing of the batches of PP3. Evaluation of Proteose Peptone #3 at lOOg/L in 5L fermentation
  • Figures 61 and 62 show SDS-PAGE analysis of the two fermentations utilising lOOg/L PP3.
  • the gels demonstrate consistent expression of collagenase in both fermentations.
  • the samples from both fermentations appear to contain similar levels of contaminant described in figure 56, although PBFT70d appears contain slightly more of the 4OkDa band (clostripain). It is possible that these small differences are due to staining or loading differences.
  • the quantity of clostripain produced using the PP3 process is significantly lower than the Phytone process.
  • the precursor band appears to persist longer into the time course of the fermentation. It was recommended that future fermentations at 100g/L should be extended to a 14 hour harvest.
  • the presence of the precursor band highlights the importance of the harvest point definition and its qualification during process validation.
  • Figure 63 displays data from densitometry analysis of the gel in figure 61.
  • the chart compares product and precursor formation (densitometry peak area) to cell growth (OD600).
  • Product formation appears to be consistent with cell growth and the rate of production decreases as the cultivation enters stationary phase.
  • the precursor band decreases in intensity as exponential growth ends but is still present at the harvest point of the fermentation.
  • Figure 65 shows SDS-PAGE analysis of the time course of the 200L fermentation.
  • the gel shows product formation during the course of the fermentation.
  • the material at the 14 hour harvest point contains no detectable precursor and very low levels of contaminants.
  • the product generated from the 200L fermentation appears very similar to that produced from the 5L process, indicating that the increased generation number of the 200L process has not had a detrimental effect.
  • Figure 66 displays data from densitometry analysis of the gel in figure 64.
  • the chart compares product and precursor formation (densitometry peak area) to cell growth (OD600).
  • Product formation appears to be consistent with cell growth and the rate of production decreases as the cultivation enters stationary phase.
  • the precursor band decreases in intensity as exponential growth ends.
  • the precursor band decreases in intensity more rapidly in the 200L fermentation than the 5L cultivation, PBFT70c (figure 63).
  • Figure 67 shows SDS-PAGE analysis using a 4- 12% Bis-Tris gel on the 200L fermentation time course. The approximate molecular weights of the detected contaminants are annotated on the gel.
  • the harvest process (clarification by filtration) developed for Process 2 was evaluated during the 200L scale up fermentation.
  • the cell culture was successfully clarified using the existing process with no blockage of the filter train.
  • the harvest process is described in the materials and methods section.2OL of filtrate from the 200L fermentation was processed by DSP to demonstrate a partial scale up of the downstream Process 3 (infra). Quantification of product yield by Densitometry analysis
  • a more accurate and quantifiable method was required to determine product concentration during the upstream process step than the semi-quantitative SDS- PAGE analysis (figures 62 and 63).
  • the fermentation filtrate has a high quantity of pigment and peptides from the growth medium that makes standard protein quantification techniques such as UV and the Bradford assay unusable.
  • the semiquantitative analysis carried out previously was modified and updated by carrying out densitometry analysis of the Coomassie stained gels.
  • the method involved loading a range of quantities (0.2 - 1.2 ⁇ g / lane) of mixed AUXI and AUXII reference material and dilutions of the sample to be quantified onto a Tris Glycine gel.
  • the phosphates for the inoculum preparation (table 25) were autoclaved in a IL bottle at 121 0 C for 20 minutes.
  • the bulk media (table 26) was initially heated in a microwave to 60 0 C to fully dissolve components before autoclaving in a IL bottle at 121°C for 20 minutes.
  • the PSA 1 (table 27) was filtered through a 0.2 ⁇ m Sartopore 2 150cm 2 filter into a 25OmL sterile bottle.
  • Table 26 Bulk medium composition for inoculum preparation
  • “Medium recipe includes PP3 at 50 and lOOg/L.
  • the phosphate solution for the 5L scale (table 29) was autoclaved in a IL bottle at 121 0 C for 20 minutes.
  • the bulk medium (table 30) was added directly to the 5 L vessel and autoclaved at 121 0 C for 20 minutes.
  • the PSA 1 (table 31) was filtered through a 0.2 ⁇ m Sartopore 2 150cm 2 filter into a 50OmL sterile bottle.
  • the 25OmL phosphate solution and 20OmL PSA 1 was separately pumped into the 5L vessel on completion of autoclaving and cooling of the vessel.
  • *Medi ⁇ uu recipe includes PP3 at 50 and lOOg/L.
  • the phosphate solution (table 37) was filtered through a 0.2 ⁇ m Sartopore 2 300cm 2 filter into a Gammasart Biosystem SAlO 1OL bag.
  • the bulk media (table 38) was added directly to the 200L vessel prior to SIP sterilisation of the vessel.
  • the PSA 1 solution (table 39) was filtered through a 0.2 ⁇ m 300cm 2 filter into a Gammasart Biosystem SAlO 1OL bag.
  • the 1OL phosphates and 8L PSA 1 were separately pumped into the 200L vessel on completion of SIP and cooling of the vessel.
  • Table 37 Phosphate composition for 200L fermentation
  • Figure 69 illustrates overviews of the process flows for the Phytone and PP3 fermentation processes at 5 and 200L scale. 5L scale fermentation
  • a vial of the WCB (2005#1019D) was thawed and 50 ⁇ L aliquots were used to binoculate 8x5mL of inoculum media in 3OmL gamma irradiated universals.
  • the 5mL cultures were incubated at 37°C in an anaerobic jar in the presence of 3 anaerobic gas packs. After approximately 12 hours of incubation (OD600 3.0-4.0) 2 ⁇ 5mL cultures were selected and used to inoculate 2x200mL inoculum media in 50OmL Erlenmeyer flasks.
  • the two flasks were placed together in an anaerobic jar with 3 gas packs and were incubated at 37°C in a shaking incubator (70 rpm) for 12 hours. After 12 hours of incubation (OD600 6.0-7.0) each 20OmL inoculum was used to inoculate a 5L vessel.
  • the working volume of the 5/7L vessels FT Applikon vessels was 5L of which 4% (v/v) was inoculum from the 200 mL stage.
  • the agitation rate was set at 100 rpm.
  • the pH, dO2 and temperature were controlled at 7.00 units, 0% of saturation and 37°C respectively.
  • the pH was controlled with additions of either HCl (5M) or NaOH (5M).
  • the dO2 concentration was maintained at 0% by continuous sparging of nitrogen, with a flowrate of 1 L/min.
  • Samples were taken during the fermentation and filtered through 0.2 ⁇ m filters before storing at -20 0 C for analytical purposes.
  • the fermentations began to enter stationary phase at an OD600 of 6.0-7.0. After 12 hours the fermenter was cooled to 10-20 0 C before commencing harvest recovery. 200L scale fermentation
  • a vial of the WCB (2005#1019D) was thawed and 50 ⁇ L aliquots were used to inoculate 8> ⁇ 5mL of inoculum media in 3OmL gamma irradiated universale.
  • the 5mL cultures were incubated at 37°C in an anaerobic jar in the presence of 3 anaerobic gas packs. After approximately 12 hours of incubation (OD600 3.0-4.0), 4x5mL cultures were selected and used to inoculate 4 ⁇ 200mL inoculum media in 50OmL Erlenmeyer flasks.
  • the working volume of the 2OL vessels was 15L of which 4% (v/v) was inoculum from the 20OmL stage.
  • the agitation rate was set at 100 rpm.
  • the pH, dO2 and temperature were set at 7.00 units, 0% and 37°C respectively.
  • the pH was controlled with additions of either HCl (5M) or NaOH (5M).
  • the dO2 concentration was maintained at 0% by continuous headspace sparging of nitrogen, with a flowrate of 20 L/min.
  • 8L of culture were used to inoculate the 200L vessel.
  • the running conditions were identical to the 2OL scale.
  • the final optical density (600nm) at harvest was 6.0-7.0. After 14 hours the fermenter was cooled to 10-20 0 C before commencing harvest recovery.
  • the 5 L cultures were pumped with a flow rate of 5 L/h through a Millistak+ 10" Opticap depth filter (Mi ⁇ lipore, KC0HC10FF1) and 0.2 ⁇ m Sartopore 2 300cm 2 filter into sterile 25OmL bio-containers.
  • the processed material was either stored at -20 0 C or stored at 4°C overnight before processing by DSP. 200L Harvest
  • the 200L harvest was performed using a filtration harvest train.
  • the culture was pumped with a flow rate of 200 L/h through a Milistak+ (MCOHCl OFSl) disposable depth filter with a filtration area of 4x1 m2 followed by two 0.2 ⁇ m Express Opticap XL 10 filters, 2*0.49m 2 (Millipore, KHGESIOTTI).
  • the process time for primary clarification was 1 hour.
  • An additional 10 min was allowed at the end of the harvest to retrieve residual product held up in the filters.
  • the clarified supernatant was collected in a 200L Stedim Palletank with the filtrate weight recorded. 2OL of filtrate was passed through a Mustang Q high affinity DNA column with a flowrate ⁇ 6 L/min and collected into two sterile 20 L stedim bags, prior to storage at 4°C overnight.
  • Optical Density measurements The spectrophotometer was blanked using PBS at wavelength 600 nm. Fermentation samples were diluted by factors of 10, 20 or 100 (dependent on cell density) using PBS.
  • Fermentation samples were filtered through 0.2 ⁇ m filters before preparing them for SDS-PAGE analysis.
  • lO ⁇ l of filtered sample was added to 1 O ⁇ l sample buffer (2x), 2.5 ⁇ l reducing agent (1Ox) and 2 ⁇ l of 0.1 M EDTA (to achieve final concentration of 1OmM).
  • the high molecular weight (HMW) marker was prepared by adding lO ⁇ l of concentrated stock to 80 ⁇ l reducing agent (1Ox) 5 31 O ⁇ l WFI and 400 ⁇ l sample buffer (2x). The diluted HMW standard was then heated to 95oC for 5 minutes before aliquoting and storage at-20oC for use in subsequent gels.
  • the fermentation samples were prepared for SDS-PAGE analysis by adding lO ⁇ l of 0.2 ⁇ m filtered sample to 4 ⁇ l sample buffer (4x), 1.5 ⁇ l reducing agent (1Ox) and 1.7 ⁇ l of 0.1M EDTA (to achieve final concentration of 1OmM). 15 ⁇ L of fermentation sample and lO ⁇ L of Mark 12 marker were run on a 4-12% Bis-Tris gel and run using MES running buffer at 200V, 400mA and IOOW for ⁇ 40mins.
  • the gels were immersed in a 10OmL fixing solution (4OmL dH2O, 5OmL methanol, 1OmL acetic acid) for 10 minutes before replacing with a 95mL staining solution (55 mL dH2O, 2OmL methanol, 2OmL stainer A) for a further 10 minutes.
  • 5mL of stainer B was added to the staining solution and the gels were left to stain for 5 h on an orbital shaker at 60 rpm before de-staining with 20OmL WFI. The gel was left in WFI for 15-20 h until excess stain was removed after which the gel was scanned and dried according to the manufactures instructions.
  • Significant process changes were introduced in the development of Process 3 in order to make the. purification more robust and more amendable to scale up and subsequent process validation.
  • One significant factor in facilitating this process change was in the choice of fermentation component.
  • Process 2 had been based on the requirement to maintain a phytone based fermentation media whereas for process 3 proteose peptone No. 3 was use.
  • the process run-through is split into the key steps of the down stream purification and the collagenases AUXI and AUXII.
  • AUXI and AUXII co-purify in the initial steps of the purification and are only separated during the anion exchange chromatography step (performed using Q-Sepharose HP media). AUXI and AUXII are then processed separately and formulated. The intermediates are then mixed in a 1:1 ratio (based on protein content determined by UV) and filtered to form the drug substance. In developing process 3, key steps associated with process 2 were removed.
  • Process 3 differed from process 2 in three main areas. Firstly, the ammonium sulphate precipitation step and hydroxyapatite chromatography steps were removed; secondly, the gel permeation chromatography (GPC) step was eliminated and thirdly, all buffer exchange steps were performed by tangential flow filtration. The precipitation step was replaced by the use of hydrophobic interaction chromatography (HIC) at the client's recommendation. Development of this step resulted in the successful implementation of HIC for (i) product capture (thereby serving as a concentration step) and (ii) some protein and pigment contaminant removal.
  • HIC hydrophobic interaction chromatography
  • the HIC step was also subsequently shown to reduce levels of dsDNA.
  • the introduction of HIC and inclusion of a Mustang Q step removed the need for both the ammonium sulphate precipitation step and the hydroxyapatite chromatography step.
  • the overall effect was to simplify the up front capture of product and to remove a potential hold step associated with Process 2. This latter point had significance in that previously the fermentation could be assessed prior to down stream purification since the pellets resulting from the precipitation step could be held at -20 0 C prior to processing.
  • Process 3 represented a simpler process that was more amenable to scale up and validation than Process 2.
  • the reduction in consumable cost was apparent by the elimination of the need for hydroxyapaptite and gel permeation media and by the reduced number of steps requiring leupeptin.
  • An overview of the purification scheme for Process 3 is given in figure 46. Non-GMP demonstration run at 2OL scale
  • Process 3 was performed at 2OL scale in the process development laboratories in order to demonstrate if material of suitable quality could be generated using this modified process at 2OL scale.
  • a key requirement for processing was the ability to limit potential protease activity by performing steps chilled wherever possible and by the inclusion of the cysteine protease inhibitor leupeptin at key stages in the procedure.
  • a full 2OL of fermentation filtrate was processed since the feedstock was generated from 200L fermentation PP3. Details of the fermentation and subsequent harvest and filtration are documented in a separate report. Mustang Q treatment of fermentation filtrate
  • HIC served three functions in the purification. Firstly, the product was reduced in volume since conditions were identified in which collagenases bound to the resin. Secondly, some pigment and protein contaminant was removed at this stage and thirdly, pico green analysis from this run indicated reduction of dsDNA.
  • the HIC step was performed using supernatant processed directly from the fermentation (after Mustang Q treatment) and, as a result a hold step, (evident in Process 2 as the ammonium sulphate pellet) was no longer present for Process 3.
  • product (20L) from the Mustang Q step was diluted with a 3M-ammonium sulphate solution to a final concentration of IM. After filtration, product was loaded onto the column and eluted using a 2-step isocratic elution.
  • the protein concentration of the HIC load material was difficult to determine accurately and was estimated in two ways. Firstly, a Bradford assay was performed on the material prior to ammonium sulphate addition. This was performed with undiluted material in order to standardise the contribution from pigment present in the fermentation media, which was known to interfere with the assay. Secondly, the estimate was based on volume of fermentation media loaded per mL of column resin. The column load was estimated to be 5.9mg of total protein/mL resin by Bradford assay or alternatively ⁇ 13mL of fermentation media per mL of resin. An estimate of the total amount of target protein eluted from the column was determined as 3.4g using UV (see Table 42).
  • Peak 1 This peak was shown to contain protein contaminants although some AUXII was also eluted at this stage (figure 71). This loss in product was expected and had been noted previously.
  • the elution volume for peak 1 removal was set at 5 column volumes. Peak 2, containing the majority of the product, was then eluted using buffer with no ammonium sulphate. Peak 2 was collected as a single pool with the chromatography method programmed so that collection began after V* of a column volume of elution buffer had been applied to the column. Collection was then terminated after a total of 4 column volumes had been collected.
  • TFF using 3OkDa membranes was introduced following the HIC in order to reduce the volume of product (5-fold) and to exchange the buffer into conditions suitable for binding to the anion exchange column.
  • the sufficient reduction in ammonium sulphate such that the conductivity of the IEX load sample was ⁇ 1.8mS.
  • the diafiltration buffer was chilled and leupeptin added prior to use to reduce the likelihood of proteolysis. No loss in protein was estimated over the course of this step (>100% recovery) although this may reflect the inaccuracy in protein concentration estimation at this stage in the process due to the presence of pigment in the pre TFFl material.
  • the Q-Sepharose column was loaded at a maximum capacity of 5mg total protein per mL resin. As a result, not all of the available material from the TFF step was utilized in this step (see Table 421).
  • fractions 6-12 were pooled for the AUXII product and fractions 19-26 pooled for AUXI.
  • the step yields and protein concentrations present in the material pooled from the Q-Sepharose run are included in table 42.
  • the separated AUXI and AUXII products from the Q Sepharose column were processed separately by TFF using a 3OkDa membrane. This step was required to; (i) remove/reduce leupeptin in the final product (ii) formulate the intermediates into the correct buffer (1 OmM Tris, 6OmM sucrose pH 8) and (iii) to achieve the required target protein concentration of 0.9-1.lmg/mL.
  • a total of 799mg ( ⁇ 683mL at 1.17mg/mL) of AUXII and 860mg (796mL at 1.08mg/mL) of AUXI was concentrated to a target concentration of 1.75mg/mL.
  • Buffer samples illustrated in table 46 were reserved from the 2OL demonstration and retested after storage at 2-8°C.
  • the pH, conductivity, temperature and appearance of the buffers were noted at the time of completion and after 12-13 days storage.
  • the results of this study are given in table 47. Small differences were observed in the values for pH and conductivity but this may be due to differences in temperature between the original buffers and the tested retains.
  • the HIC buffers showed the largest variation in conductivity and temperature.
  • future studies on buffer stability should include specification of an accepted temperature range for recording all parameters. In all cases, the buffer retains were clear in appearance at time zero and after the required hold time.
  • the N-terminus of the 55kDa contaminant band associated with AUXI (Lanes 1-5; figure 89) was shown to match a region of the Col G sequence for collagenase AUXI whereas the 4OkDa contaminant band from AUXII (Lanes 6-10; figure 89) was identical to a region of the Col H sequence for collagenase AUXII.
  • a previous attempt was made to sequence the 9OkDa band associated with both the AUXI and AUXII products (figure 90). Sequencing of the 9OkDa contaminant associated with the AUXI product was successful in that identity was correlated with the N-terminus of the AUXI sequence. In contrast, it was not possible to obtain a complete sequence for the 9OkDa contaminant associated with AUXII 5 which suggested that the two 9OkDa contaminants were different products.
  • This pooling criterion is based on the assumption that (i) the quality of material generated from the engineering run is appropriate for the GMP material and (ii) the approximation of the densitometry method is acceptable. If the aim is to generate material of higher quality in the GMP campaign, the specification for pooling criteria will need to be revised. Specification for pooling from the IEX
  • Table 50 Theoretical relative amounts of product and impurities in the post IEX pools from the 200L Engineering run, as determined by densitometry analysis. The fractions pooled are highlighted in red. The theoretical average product purity is calculated as 92.3% and 95.8% for the AUXI and AUXII intermediates respectively.
  • Table 52 Average relative quantities of product and impurities in the post IEX fractions from the 200L Engineering run, as determined by densitometry analysis.
  • Table 53 Theoretical relative amounts of product and impurities in the post IEX pools from the 200L Engineering run, as determined by densitometry analysis. The fractions pooled are highlighted in red. The theoretical average product purity is calculated as 92.3% and 95.8% for the AUXI and AUXII intermediates respectively.
  • IM NaOH at a flow rate of 30mL/min for 30minutes.
  • the capsule was then preconditioned for the same time and flow-rate using IM NaCl.
  • the capsule was equilibrated with 2L of Mustang Q Equilibration buffer (1OmM Tris, IM ammonium sulphate, pH 8), at a flow rate of 60mL/min.
  • the outlet flow was checked to ensure the pH was ⁇ 8.
  • the maximum recommended operating flow rate for the capsule was 600mL/min.
  • the filtered material was stored in 2 x 1OL Stedim bags at 2-8°C overnight.
  • This packing flow rate was utilized as equivalent to the maximum operating flow rate for the K-prime system available in GMP.
  • the adaptor was brought down to the top of the bed and the column packed at 192cm/hr for 1 Omins before screwing the adaptor into the top of the resin and packing at 192cm/hr for a further 1 Omins, during which no compression of the resin was observed.
  • the pack test was carried out using the AKTA Pilot method: HIC 150OmL Pack Test. For this, the column was equilibrated with 1 column volume (CV) of 20OmM NaCl in WFI and pack tested with 15mL (1% CV) of IM NaCl in WFI at a flow rate of 313mL/min (150cm/hr).
  • the column was flushed with 2CV WFI and stored with 2CV 1OmM NaOH.
  • the packed column had an asymmetry of 1.2, a plate count of 2659 plates/meter, a CV of 1525mL and bed height of 12.2cm.
  • Phenyl Sepharose 6 FF (low sub) column was sanitised with 0.5M NaOH for 60 minutes, washed with 2 column volumes (CV) WFI and equilibrated with 5CV 1OmM Tris, pH 8 (HIC Buffer B) followed by 5CV 1OmM Tris, LOM ammonium sulphate, pH 8 (HIC Buffer A). Preparation of the HIC load
  • the HIC run was performed at a constant linear flow rate of 150cm/hour using chilled buffers maintained at 2-8°C.
  • 30L feedstock (equivalent to 2OL post- Mustang Q filtrate) was loaded onto the 1525mL Phenyl Sepharose 6 FF (low sub) column previously equilibrated with 2CV 1 OmM Tris, 1.0M ammonium sulphate, pH 8 (HIC Buffer A). Unbound material was washed off the column with lOCV HIC Buffer A. The column was then washed with 5CV 1OmM Tris, 0.3M ammonium sulphate, pH 8 (HIC Buffer A2) and bound proteins eluted with lOCV 1OmM Tris, pH 8 (HIC Buffer B). The first 0.67 CV (IL) of the elution buffer was discarded and a post-HIC pool of 4CV was collected. Leupeptin was added
  • the ProFlux Ml 2 TFF system was set up according to the manufacturer's instructions with two PelHcon 2 "Mini" Filter 3OkDa MWCO PES membranes, sanitised with 0.5M NaOH for 60 minutes and stored in 0.1 M NaOH until use.
  • the system was drained and flushed with 14L WFI and the normal water permeability (NWP) measured as 23L/m2/hr/psi at 25°C at a trans-membrane pressure (TMP) of 15psig (inlet pressure of 20psig and outlet pressure of 10 psig).
  • TMP trans-membrane pressure
  • the system was flushed with 0.5L 1OmM Tris, pH 8 (diafiltration buffer) and equilibrated with IL of the same buffer for 10 minutes.
  • the conductivity and pH of the permeate was determined and checked against that of the diafiltration buffer to ensure the membranes were equilibrated prior to use. Concentration and diafiltration
  • the concentration and diafiltration steps were performed with chilled dialfiltration buffer (1OmM Tris, pH 8) containing 200 ⁇ M leupeptin.
  • the TFF system was flushed with IL chilled buffer just before use. 2L of the post-HIC material (6.3L total volume) was pumped into the TFF system reservoir and recirculated for 10 minutes without back-pressure to condition the membrane.
  • the level sensor on the reservoir was set to 1.2L and the post-HIC material concentrated at a TMP of 15psig (inlet pressure of 20psig and outlet pressure of lOpsig) until all the material had entered the system.
  • the permeate was collected and stored at 2-8°C for analysis.
  • the inlet tubing was connected to the diafiltration buffer and diafiltration of the material was performed at a TMP of 15psig (inlet pressure of 20psig and outlet pressure of lOpsig) for approximately 8.5 turnover volumes (TOV), maintaining the volume of material in the reservoir at 1.2L.
  • TMP 15psig
  • TOV turnover volumes
  • the conductivity and pH of the permeate was determined after 5, 7 and 8.5 TOV and checked against that of the diafiltration buffer.
  • the retentate was drained from the system and stored at 2-8°C. 25OmL diafiltration buffer was pumped into the reservoir, recirculated around the system for 10 minutes without backpressure to rinse the system, drained, the rinse repeated and both rinses were stored separately at 2-8°C.
  • the protein concentration of the retentate and rinses were determined (by UV) and the first rinse (204.8g weight) added to the retentate (1231.4g weight). This post TFFl material (1.4kg) was then filtered through a Sartopore 2 0.8+0.45 ⁇ m filter capsule and stored at 2-8 0 C overnight until further processing by Q Sepharose ion exchange chromatography.
  • a Vantage S90 column was packed using an AKTA Pilot chromatography system with Q Sepharose HP media in WFI to give a packed column with a 10cm bed height, therefore a column volume (CV) of 62OmL.
  • the packing was performed in accordance to the manufacturers instruction but with the pressure limit of the Vantage column imposed (0.3MPa) which equated to a packing flow rate of
  • Fractions 6 to 12 were pooled as AUX II collagenase with the volume determined as 683g (after sampling) and the concentration by UV analysis measured as 1.17mg/mL.
  • Fractions 19 to 26 were pooled as AUX I collagenase with the volume determined as 796g (after sampling) and the concentration by UV measured as 1.08mg/mL.
  • Tangential Flow Filtration step 2 (TFF2 2OL scale run) Equipment: ProFlux M12 TFF system (Millipore)
  • the ProFIux M 12 TFF system was set up according to the manufacturer's instructions with one Pellicon 2 "Mini" Filter 3OkDa MWCO PES membrane, sanitised with 0.5M NaOH for 60 minutes and stored in 0.1 M NaOH until use.
  • the system was drained and flushed with 14L WFI and the normal water permeability (NWP) measured as 19.5L/m2/hr/psi for the membrane used for AUXI and as 14.5L/rri2/hr/psi at 25°C for the membrane used for AUXII at 25°C and at a transmembrane pressure (TMP) of 15psig (inlet pressure of 20psig and outlet pressure of lOpsig).
  • NWP normal water permeability
  • the concentration and diafiltration steps were performed separately on each of the post IEX pools of AUXI and AUXII. All steps were performed using chilled formulation buffer (1OmM Tris, 6OmM sucrose, pH 8) maintained at 2-8°C.
  • the TFF system was flushed with IL chilled buffer just before use.
  • the post-IEX pool (683g weight of AUXIl and 796g weight of AUXI) was pumped into the TFF system reservoir and recirculated at 10% pump speed for 10 minutes without backpressure to condition the membrane.
  • the level sensor on the reservoir was set to approximately 40OmL and the AUXI or AUXII pool concentrated at a TMP of 15psig (inlet pressure of 20psig and outlet pressure of lOpsig) until the volume in the reservoir had been reduced to approximately 360-39OmL (this assumed a system hold up volume of 10OmL).
  • the target volume reduction was based on achieving a theoretical concentration of 1.75mg/mL for the product assuming no loss in protein during the concentration operation.
  • the permeate was collected and stored at 2-8°C for analysis.
  • the inlet tubing was connected to the formulation buffer and diafiltration performed at a TMP of 15psig (inlet pressure of 20psig and outlet pressure of lOpsig).
  • TOV turnover volumes
  • 25OmL formulation buffer was used to wash residual product from the membranes by re-circulated around the system for 10 minutes (without backpressure). After draining the rinse solution, a second wash was performed and both rinse 1 and rinse
  • Bio-Rad Protein Assay Dye Reagent Concentrate (500-0006, Bio-Rad) A BSA standard curve was prepared by diluting the BSA with water, to known concentrations.
  • the Bio-Rad protein assay dye reagent was prepared by diluting one part concentrate with four parts water. Test samples were prepared by diluting with water. 50 ⁇ L of test sample either neat or diluted was added to a cuvette and 2.5mL diluted regent added. Samples were prepared in duplicate. The samples were incubated for lOminutes before reading the OD. The standard curve of ODs95nm vs. protein concentration was obtained by measuring the ODs95nm of BSA solutions of known concentration. The test samples were then assayed and the protein concentration determined from the standard protein assay curve.
  • Samples were prepared for reducing SDS-PAGE by adding 12 ⁇ l of sample to 20 ⁇ l sample Buffer (2x), 4 ⁇ l reducing agent (1Ox) and 4 ⁇ l of 0.1M EDTA (to achieve final concentration of 1OmM).
  • the high molecular weight (HMW) marker was prepared by adding lO ⁇ l of concentrated stock to 80 ⁇ l reducing agent (1Ox) 3 310 ⁇ l WFI and 400 ⁇ l sample buffer (2x). The diluted HMW standard was then heated at 95oC for 5 minutes before aliquoting and storage at — 20oC for use in subsequent gels. Samples (20 ⁇ l load volume) containing collagenases were run directly (i.e.
  • Tris-Glycine gels were prepared for reducing SDS-PAGE by adding 16.5 ⁇ l of sample to 7.5 ⁇ l sample buffer (4x), 3 ⁇ l reducing agent (1Ox) and 3 ⁇ l of 0.1M EDTA (to achieve final concentration of 1OmM). MARK 12 marker loaded neat (lO ⁇ l). Samples (15 ⁇ l load volume) containing collagenases were run directly (i.e.
  • Ethylenediaminetetra-acetic acid disodium salt (EDTA) (AnalaR, BDH) Purified water Reducing SDS-PAGE
  • the post-IEX samples were run on 4-12% Bis-Tris gels using MES running buffer at l ⁇ g/Iane loading.
  • Samples were prepared by adding 20 ⁇ L of diluted post- IEX material to 8 ⁇ L Sample Buffer (4x), 3 ⁇ L Reducing Agent (1Ox) and 3.4 ⁇ L of 0.1M EDTA. 15 ⁇ L of each sample was loaded into the well directly after mixing (i.e. with no heat treatment) and run at 200V for 40mins. After electrophoresis, the gels were stained with Colloidal Blue stain reagent according to the manufacturers instructions but with a fixed staining duration to reduce staining variation (10 minute fix, 5 hours stain, 15-20 hours destain with purified water).
  • Buffers for the 2OL demonstration run were filtered after preparation through a 0.45/0.2 ⁇ m filter capsule into 10 or 2OL Stedim bags for storage at 2-8°C prior to use- When the majority of the buffer had been filtered, approximately 75mls of the remaining buffer was collected into pre-labelled 125ml PETG biotainers and stored at 2-8oC. The pH, conductivity, temperature and date of buffer preparation were recorded. On completion of the 2OL demonstration run, the buffer samples were retrieved from cold storage and retested for pH, conductivity, and appearance. The temperature of the buffer at the time of testing was also recorded.
  • Electrophoresis Power Supply EPS 601 (Amersham Pharmacia Biotech) Xcell SureLock Mini-Cell Electrophoresis System, (Invitrogen) Rocky shaker platform, (Scientific Laboratory Supplies) Chemicals: Novex 8% Tris-Glycine Gel, 1.5mm, 10 well, (Invitrogen) High Molecular Weight Marker, (BioRad)
  • a scale up fermentation was carried out at 200L.
  • the fermentation used the optimized concentration of PP3 (100g/L).
  • the fermentation was successful and replicated both the growth profile and product yield/quality observed at 5L scale.
  • the harvest process (clarification by filtration) developed for Process 2 was evaluated during the 200L scale up fermentation.
  • the cell culture was successfully clarified using the existing process with no blockage of the filtration train.
  • the quantification of collagenase concentration in crude fermentation samples was improved using densitometry analysis of Coomassie stained Tris Glycine gels.
  • a standard curve of mixed AUXI and AUXII was loaded with dilutions of fermentation samples.
  • the relationship between collagenase concentration and densitometry peak area was shown to be linear within the range of the sample dilutions.
  • the concentrations of collagenase in the samples were then extrapolated using their peak area and the standard curve. This method estimated the yield of collagenase to be 280 - 350mg/L from the 100g/L PP3 process at 5 and 200L scale.
  • the optimised PP3 fermentation process generated a higher biomass concentration (OD600 7 units) and increased product yield (280 - 350mg/L total collagenase, by quantitative densitometry) when compared to the Phytone fed-batch process.
  • the fermentation filtrate contained significantly less clostripain than the Phytone process.
  • the ratio of AUXI: AUXII was closer to 1 compared to that observed during evaluation of Process 2.
  • the PP3 process increased the product yield, purity (post-fermentation) and reproducibility of the fermentation. Purification
  • Process 3 was developed in an accelerated time frame in order to improve the processes previously developed at Cobra (Process 2) and run at 2OL scale in GMP. Major improvements to the process were made in order to simplify the purification procedure, facilitate robustness as well as make the process more amenable to scale up to 200L. These improvements were also considered key to assisting process validation.
  • Process 3 was performed using material from a 200L fermentation of Clostridium histolyticum in which a full 2OL of fermentation was purified. Material was processed directly from the fermentation and no hold steps were implemented. Following filtration, product was passed through a Mustang Q filter since small- scale experiments demonstrated reduction of dsDNA (as detected by pico green analysis) using this procedure. Analysis of in-process samples from the 20L demonstration run however, showed no reduction in dsDNA suggesting that the robustness and application of this step required further investigation. A comparison of the parameters used for the 2OL run-through and previous small-scale experiments demonstrated dsDNA removal when the capsule was oversized by a factor of 1000 (based on the DNA binding capabilities of 15-25mg DNA/mL capsule described by the manufacturer).
  • Product from the Mustang Q capsule was prepared for hydrophobic interaction chromatography (HIC) by the addition and mixing of an ammonium sulphate solution (3M) to achieve a final concentration of IM.
  • HIC hydrophobic interaction chromatography
  • 3M ammonium sulphate solution
  • This provided conditions suitable for collagenase binding to Phenyl Sepharose FF (low sub) media.
  • a proportion of protein contaminants and pigment were then eluted from the HIC column using a step elution of 0.3M ammonium sulphate followed by collagenase product elution with a solution containing no ammonium sulphate. Criteria for collection of the product peak were established as a fixed volume of 4 column volumes (although this was later extended to 5 column volumes for the 200L scale demonstration run).
  • Leupeptin was then added immediately following elution and the material held for a period of 2 days at 2- 8°C.
  • the yield from this step was difficult to determine accurately due to the complex nature of the feedstock.
  • the process step yield was estimated as (i) 38% based on Bradford assay of the load and UV of the eluted material or (ii) 47% based on collagenase content in the load estimated by densitometry and UV of the eluted material.
  • 0.17g of total protein was eluted from the HIC column for the equivalent of every IL of fermentation filtrate applied.
  • the post HIC pool was prepared for Q-Sepharose purification by concentration (5- fold) and buffer exchange using tangential flow filtration (TFFl) using 2 x 0.1 m2 3OkDa membranes. No loss was detected over this step and the reported increase in protein recovered may reflect the inaccuracy of UV at this point in the process. Inaccuracy could be attributed to pigment contamination or the use of the extinction coefficient for collagenases, which will be less accurate for material earlier in the purification when a complex of proteins are likely to be present.
  • the TFF step was completed by a product filtration step before holding the material at 2- 8°C over night.
  • the Q-Sepharose column was a key purification step in Process 3 and resulted in the separation of the AUXI and AUXII collagenases.
  • the contaminants associated with process 3 were different to those in process 2 and appeared to closely co-purify with the AUXI and AUXII products. It was possible however, to remove the contaminants from the products by fractionation of the product peaks since the contaminants appeared to elute at either the leading or tail edges of both peaks.
  • the contaminants were denoted by their relative molecular mass on reducing SDS-PAGE.
  • Those associated with the AUXII product were identified as (i) 4OkDa (associated with the leading edge of the peak) and (ii) 75kDa and 9OkDa (associated with the trailing edge of the peak).
  • N-terminal amino acid sequencing indicated that the 4OkDa was AUXII related since the sequence matched identity with a region of the Col H sequence. In comparison, no identity could be confirmed for the 9OkDa contaminant due to issues of low signal.
  • Contaminants associated with AUXI product were (i) 55kDa (associated with the leading edge of the peak) and (ii) 9OkDa (associated with the trailing edge of the peak).
  • N-terminal sequencing showed both the 55kDa and 9OkDa contaminants to be identified as AUXI-related where the 55kDa contaminant showed sequence identity with a mid region in the Col G sequence and the 9OkDa showed identical N-terminal match to AUXI.
  • Fractions containing AUXl or AUXII product from the Q-Sepharose column were formulated separately by TFF (denoted TFF2) using 1 x 0.1 m2 3OkDa membrane for each collagenase.
  • Product was filtered following the TFF2 step and the overall step yields for TFF and filtration estimated as 97.5% for AUXI and 92.2% for AUXII.
  • samples were referred to as intermediates and were retained at 2-8°C for QC analysis and prior to mixing of the drug substance.
  • the overall process yield was estimated for the 2OL demonstration run in which all available material from the 2OL of fermentation feedstock had been processed and assuming all material had been mixed as drug substance. This gave a predicted yield of 1.6g drug substance for the 2OL scale purification. This equated to a process recovery of 17.8% based on then assumption that the initial estimate of 9g (using the Bradford assay) for the amount of total protein available to load onto the HIC column was accurate. Alternatively, if the total available protein was related to the collagenase content in the HIC load (as estimated by densitometry) the overall process yield was calculated as 22%.
  • Tables 54 and 55 detailed the analytical specifications AUX-I and AUX-II intermediates and also for Drug Substance for Process 3.

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Abstract

A drug product comprising a combination of highly purified collagenase I and collagenase II from Colostridium histolyticum is disclosed. The drug product includes collagenase I and collagenase II in a ratio of about 1 to 1, with a purity of greater than at least 95%. The invention further disclosed improved fermentation and purification processes for preparing the said drug product.

Description

COMPOSITIONS AND METHODS FOR TREATING COLLAGEN-MEDIATED
DISEASES
RELATED APPLICATIONS
This application claims the benefit of U.S. Provisional Application No. 60/763,470 filed on January 30, 2006 and U.S. Provisional Application No.
60/784,135, filed March 20, 2006. The entire teachings of the above applications are incorporated herein by reference.
BACKGROUND OF THE INVENTION
Collagen is the major structural constituent of mammalian organisms and makes up a large portion of the total protein content of skin and other parts of the animal body. In humans, it is particularly important in the wound healing process and in the process of natural aging. Various skin traumas such as burns, surgery, infection and accident are often characterized by the erratic accumulation of fibrous tissue rich in collagen and having increased proteoglycan content. In addition to the replacement of the normal tissue which has been damaged or destroyed, excessive and disfiguring deposits of new tissue sometimes form during the healing process. The excess collagen deposition has been attributed to a disturbance in the balance between collagen synthesis and collagen degradation.
Numerous diseases and conditions are associated with excess collagen deposition and the erratic accumulation of fibrous tissue rich in collagen. Such diseases and conditions are collectively referred to herein as "collagen-mediated diseases". Collagenase has been used to treat a variety of collagen-mediated diseases. Collagenase is an enzyme that has the specific ability to digest collagen. Collagenase for use in therapy may be obtained from a variety of sources including mammalian (e.g. human), crustacean (e.g. crab, shrimp), fungal, and bacterial (e.g. from the fermentation of Clostridium, Streptomyces, Pseudomonas, or Vibrio). Collagenase has also been genetically engineered. One common source of crude collagenase is from a bacterial fermentation process, specifically the fermentation of C. histotyticum (C .his). The crude collagenase obtained from C. his may be purified using any of a number of chromatographic techniques. One drawback of the fermentation process from C. his is that it yields uncertain ratios of the various collagenases such as collagenase I and collagenase II, often used in therapeutic compositions to treat collagen mediated conditions. Further, the culture has historically required the use of meat products. This meat culture was originally derived from the H4 strain of Clostridium histolyticum, Dr. I. Mandl's laboratory in Columbia University in 1956 and deposited with the ATCC. Lyophilized vials were made out of the cooked meat culture and named as ABC Clostridium histolyticum master cell bank.
Various ratios of collagenase I to collagenase II in a therapeutic collagenase preparation have different biological effects. Therefore, a therapeutic collagenase preparation in which the ratio of collagenase I to collagenase II in the preparation can be easily and efficiently determined and controlled to obtain superior, and consistent enzyme activity and therapeutic effect, would be desirable.
SUMMARY OF THE INVENTION The present invention provides a collagenase composition comprising a combination of highly purified collagenase I and collagenase II. Preferably, the collagenase I and collagenase II are present in a mass ratio of about 1 to 1. When used as a pharmaceutical composition for treating collagen-mediated diseases, the composition of the invention provides improved and consistent therapeutic effect while lowering the potential for side effects.
The invention further provides methods for preparing a collagenase composition of the invention, pharmaceutical formulations comprising a composition of the invention and methods for treating patients suffering from a collagen-mediated disease using a collagenase composition of the invention.
BRIEF DESCRIPTION OF THE DRAWINGS
The foregoing and other objects, features and advantages of the invention will be apparent from the following more particular description of preferred embodiments of the invention, as illustrated in the accompanying drawings in which like reference characters refer to the same parts throughout the different views. The drawings are not necessarily to scale, emphasis instead being placed upon illustrating the principles of the invention. Figure 1 depicts growth curves (OD vs time) of C. histolyticum in 5L DCFT24a,b fermentations.
Figure 2 depicts net growth curves (Net OD vs time) of C. histolyticum in 5L DCFT24a,b fermentations. Figure 3 is a 8% Tris-glycine SDS PAGE gel from the second fermentation:
Lane 1 : High Molecular Weight Marker
Lane 2: Collagenase l - 0.27μg
Lane 3: Collagenase II - 0.29μg
Lane 4: 2Oh (6.12μL of sample) — Harvest point Lane 5: I9h (6.12μL of sample)
Lane 6: 17h (6.12μL of sample)
Lane 7: 16h (6.12μL of sample) Lane 8: 15h (6.12μL of sample)
Lane 9: 14h (6.12μL of sample) Lane 10: 13h (6.12μL of sample)
Lane 11: 11.6h - 19h (6.12μL of sample) Lane 12: 10.5h (6.12μL of sample); Figure 4 is a 8% Tris-glycine SDS PAGE gel from the first fermentation:
Lane 1 : High Molecular Weight Marker Lane 2: Collagenase l - 0.27μg
Lane 3: Collagenase II - 0.29μg
Lane 4: 2Oh (6.12μL of sample) — Harvest point
Lane 5: 19h (6.12μL ofsample)
Lane 6: 17h (6.12μL of sample) Lane 7: 16h (6.12μL of sample)
Lane 8: 15h (6.12μL of sample)
Lane 9: 14h (6.12μL of sample)
Lane 10: 13h (6.12μL of sample) Lane 11: 11.4h (6.12μL of sample) Lane 12: 10.4h (6.12μL of sample);
Figure 5 is a Semi-quantitative SDS PAGE gel for the second fermentation, harvest point sample: Lane 1: High Molecular Weight Marker Lane 2: 0.87μL of sample (1/7 dilution of fermentation sample) Lane 3: 1.22μL of sample (1/5 dilution of fermentation sample) Lane 4: 1.53μL of sample (1/4 dilution of fermentation sample) Lane 5: 2.04μL of sample (1/3 dilution of fermentation sample) Lane 6: 0.27μg collagenase I Lane 7: 0.18μg collagenase T Lane 8: O.135μg collagenase I Lane 9: 0.29μg collagenase II Lane 10: O.193μg collagenase II Lane 11 : 0.145μg collagenase II; Figure 6 represents fermentation strategy used for DCFT26a and DCFT26b; Figure 7 depicts growth curves (OD vs time) of C. histolyticum in 5L DCFT26a,b fermentations; Figure 8 depicts net growth curves (Net OD vs time) of C. histolyticum in 5L
DCFT26a,b fermentations;
Figure 9 is a SDS PAGE gel for DCFT26a:
Lane 1 : High Molecular Weight Marker
Lane 2: Collagenase I - 0.67μg Lane 3: Collagenase II - 0.72μg Lane 4: 2Oh (6.12μL of sample) - Harvest Point Lane 5: 19h (6.12μL ofsample) Lane 6: 18h (6.12μL ofsample) Lane 7: 17h (6.12μL ofsample) Lane 8: 16h (6.12μL ofsample) Lane 9: 14h (6.12μL of sample) Lane 10: 13h (6.12μL ofsampIe) Lane 11 : 1 Ih (6.12μL of sample);
Figure 10 is a SDS PAGE gel for DCFT26b:
Lane 1 : High Molecular Weight Marker
Lane 2: 20h (6.12μL of sample) - Harvest point
Lane 3: 19h (6.12μL of sample) Lane 4: 18h (6.12μL of sample)
Lane 5 : 17h (6.12μL of sample)
Lane 6: 16h (6.12μL of sample)
Lane 7: 15h (6.12μL of sample)
Lane 8: 14h (6.12μL of sample)
Lane 9: 13h (6.12μL of sample)
Lane 10: Hh (6.12μL of sample)
Lane 11 : Collagenase I - 0.67μg
Lane 12: Collagenase 11 - 0.72μg; Figure 11 is a semi-quantitative SDS PAGE gel for DCFT26a, harvest point sample:
Lane 1 : High Molecular Weight Marker
Lane 2: 0.27μg collagenase I
Lane 3 : 0.18μg collagenase I
Lane 4: 0.135μg collagenase I
Lane 5: 0.29μg collagenase II
Lane 6: 0.193 μg collagenase II
Lane 7: 0.145 μg collagenase II
Lane 8: 0.87μL of sample (1/7 dilution of fermentation sample)
Lane 9: 1.22μL of sample (1/5 dilution of fermentation sample)
Lane 10: 1.53μL of sample (1/4 dilution of fermentation sample)
Lane 11: 2.04μL of sample (1/3 dilution of fermentation sample); Figure 12 is a Semi-quantitative SDS PAGE gel for DCFT26b, harvest point sample:
Lane 1 : High Molecular Weight Marker
Lane 2: 0.27μg collagenase I
Lane 3 : 0.18μg collagenase I
Lane 4: 0.135μg collagenase I
Lane 5: 0.29μg collagenase II
Lane 6: 0.193μg collagenase II
Lane 7: 0.145μg collagenase II
Lane 8: 2.04μL of sample (1/3 dilution of fermentation sample) Lane 9: 1.53μL of sample (1/4 dilution of fermentation sample)
Lane 10: 1.22μL of sample (1/5 dilution of fermentation sample) Lane 11: 0.87μL of sample (1/7 dilution of fermentation sample); Figure 13 is a SDS PAGE gel for post-dialysed ammonium sulphate precipitated (100g/L and 150 g/L) samples, DCFT26a, harvest point sample: Lane 1 : High Molecular Weight Marker
Lane 2: 0.67μg collagenase I and 0.72μg collagenase II
Lane 3: 0.27μg collagenase I and 0.29μg collagenase II
Lane 4: 6.12μL of supernatant sample from SCl 1 Lane 5: post dialysed sample - 100g/L AS (Neat)
Lane 6: post dialysed sample — 100g/L AS (1/5)
Lane 7: post dialysed sample - 100g/L AS (1/10)
Lane 8: post dialysed sample — 150g/L AS (Neat)
Lane 9: post dialysed sample — 150g/L AS (1/5) Lane 10: post dialysed sample - 150g/L AS (1/10);
Figure 14 is a SDS PAGE gel for post-dialysed ammonium sulphate precipitated (200g/L and 250 g/L) samples, DCFT26a, harvest point:
Lane 1 : High Molecular Weight Marker
Lane 2: 0.67μg collagenase I and 0.72μg collagenase II Lane 3: 0.27μg collagenase I and 0.29μg collagenase II
Lane 4: 6.12μL of supernatant sample from SCI l
Lane 5: post dialysed sample — 200g/L AS (Neat)
Lane 6: post dialysed sample — 200g/L AS (1/5)
Lane 7: post dialysed sample - 200g/L AS (1/10) Lane 8: post dialysed sample — 250g/L AS (Neat)
Lane 9: post dialysed sample - 250g/L AS (1/5)
Lane 10: post dialysed sample - 250g/L AS (1/10);
Figure 15 is a SDS PAGE gel for post-dialysed ammonium sulphate precipitated (300g/L and 400 g/L) samples, DCFT26a, harvest point: Lane 1: High Molecular Weight Marker
Lane 2: 0.67μg collagenase I and 0.72μg collagenase II
Lane 3: 0.27μg collagenase I and 0.29μg collagenase II Lane 4: 6.12μL of supernatant sample from SC 11
Lane 5: post dialysed sample - 300g/L AS (Neat sample)
Lane 6: post dialysed sample - 300g/L AS (1/5 dilution)
Lane 7: post dialysed sample - 300g/L AS ( 1 /10 di lution) Lane 8: post dialysed sample - 400g/L AS (Neat)
Lane 9: post dialysed sample — 4000g/L AS (1/5 dilution)
Lane 10: post dialysed sample - 400g/L AS ( 1 /10 dilution); Figure 16 depicts a Growth curves (OD vs time and net OD vs time) of C. histolyticum in PBFT57 fermentation; Figure 17 is a Semi-quantitative SDS PAGE gel, harvest point sample:
Lane 1 : High Molecular Weight Marker
Lane 2: 0.27μg collagenase I
Lane 3: 0.18μg collagenase I
Lane 4: 0.135μg collagenase I Lane 5: 0.29μg collagenase II
Lane 6: 0.193μg collagenase II
Lane 7: 0.145μg collagenase II
Lane 8: 2.04μL of sample (1/3 dilution of fermentation harvest sample) Lane 9: 1.53μL of sample (1/4 dilution of fermentation harvest sample)
Lane 10: 1.22μL of sample (1/5 dilution of fermentation harvest sample)
Lane 11: 0.87μL of sample (1/7 dilution of fermentation harvest sample);
Figure 18a is a quantitative SDS PAGE gel for post-dialysed 50OmL sample from fermentation PBFT57, harvest point sample. 400g/L of ammonium sulphate added:
Lane 1 : High Molecular Weight Marker
Lane 2: 0.272μg collagenase I and 0.286μg collagenase II Lane 3: 0.181μg collagenase I and 0.190μg collagenase II
Lane 4: 0.136μg collagenase I and 0.142μg collagenase II
Lane 5: 0.109μg collagenase I and 0.114μg collagenase II Lane 6: post dialysed sample - 400g/L AS (1/15 dilution)
Lane 7: post dialysed sample - 400g/L AS (1/20 dilution)
Lane 8: post dialysed sample - 400g/L AS (1/25 dilution)
Lane 9: post dialysed sample - 400g/L AS (1/30 dilution) Lane 10: post dialysed sample - 400g/L AS (1/35 dilution)
Lane 11 : High Molecular Weight Marker;
Figure 18b is a SDS PAGE of the supernatants after centrifugation of the ammonium sulphate precipitated samples:
Lane 1 : High Molecular Weight Marker Lane 2: 0.27μg Col I and 0.29 μg Col II
Lane 3: Supernatant (neat) of post ammonium sulphate precipitated sample (400g/L slow addition)
Lane 4: Supernatant (neat) of post ammonium sulphate precipitated sample (400g/L fast addition) Lane 5: Supernatant (neat) of post ammonium sulphate precipitated sample (440g/L slow addition)
Lane 6: Supernatant (neat) of post ammonium sulphate precipitated sample (480g/L slow addition)
Lane 7: Supernatant (neat) of post ammonium sulphate precipitated sample (520g/L slow addition)
Lane 8: Supernatant (neat) of post ammonium sulphate precipitated sample (400g/L, pH 6)
Lane 9: Supernatant (neat) of post ammonium sulphate precipitated sample (400g/L, oxygenated); Figure 19 is a Semi-quantitative SDS PAGE gel showing diluted samples from the harvest point supernatant and the post dialysed ammonium sulphate (with 400g/L - fast addition) precipitated sample:
Lane 1: High Molecular Weight Marker
Lane 2: Fermentation sample - harvest (neat) Lane 3: Fermentation sample - harvest (1/1 dilution)
Lane 4: Fermentation sample - harvest (1/2 dilution) Lane 5: Fermentation sample - harvest (1/3 dilution) Lane 6: Fermentation sample - harvest (1/4 dilution) Lane 7: Post dialysed sample - harvest (1/17.54 dilution) corresponds to lane 1 Lane 8: Post dialysed sample - harvest (1/35.08 dilution) corresponds to lane 2 Lane 9: Post dialysed sample - harvest (1/52.62 dilution) corresponds to lane 3 Lane 10: Post dialysed sample - harvest (1/70.16 dilution) corresponds to lane 4 Lane 11 : Post dialysed sample - harvest (1/87.70 dilution) corresponds to lane 5;
Figure 20 is a semi-quantitative SDS PAGE gel for PBFT57 showing diluted samples from the harvest point supernatant and the post dialysed ammonium sulphate (with 520g/L) precipitated sample:
Lane 1 : High Molecular Weight Marker
Lane 2: Fermentation sample - harvest (neat)
Lane 3: Fermentation sample - harvest (1/1 dilution)
Lane 4: Fermentation sample - harvest (1/2 dilution)
Lane 5: Fermentation sample - harvest (1/3 dilution)
Lane 6: Fermentation sample - harvest (1/4 dilution)
Lane 7: Post dialysed sample - harvest (1/15.63) corresponds to lane
1
Lane 8: Post dialysed sample - harvest (1/31.26) corresponds to lane
2
Lane 9: Post dialysed sample - harvest (1/46.89) corresponds to lane
3
Lane 10: Post dialysed sample - harvest (1/62.52) corresponds to lane
4
Lane 11 : Post dialysed sample - harvest (1/78.15) corresponds to lane
5; Figure 21 depicts growth curves (Net OD vs time) of C. histolyticum strains 004 and 013 in PBFT58c,d fermentations;
Figure 22 is a SDS PAGE gel for PBFT58c (Strain 004):
Lane 1 : High Molecular Weight Marker Lane 2: Collagenase l - l .OOμg
Lane 3: Collagenase l - 0.67μg
Lane 4: Collagenase II - 1.08μg
Lane 5: Collagenase II - 0.72μg
Lane 6: 16.25h (6.12μL of sample) Lane 7: 17h (6.12μL of sample)
Lane 8: 18h (6.12μL of sample)
Lane 9: 19h (6.12μL of sample)
Lane 10: 20.5h (6.12μL of sample); Figure 23 is a SDS PAGE gel for PBFT58d (Strain 013): Lane 1 : High Molecular Weight Marker
Lane 2: Collagenase l - l.OOμg
Lane 3: Collagenase l - 0.67μg
Lane 4: Collagenase II - 1.08μg
Lane 5: Collagenase II - 0.72μg Lane 6: 16.25h (6.12μL of sample)
Lane 7: 17h (6.12μL of sample)
Lane 8: 18h (6.12μL of sample)
Lane 9: 19h (6.12μL of sample)
Lane 10: 20.5h (6.12μL of sample); Figure 24 is a semi-quantitative SDS PAGE gel for PBFT58c (strain 004), harvest point sample:
Lane 1 : High Molecular Weight Marker
Lane 2: 0.27μg collagenase I and 0.29μg collagenase II
Lane 3: 0.18μg collagenase I and 0.19μg collagenase II Lane 4: 0.135μg collagenase l and 0.145μg collagenase II
Lane 5: 0.108μg collagenase I and 0.116μg collagenase II
Lane 6: 6.12μL ofsample Lane 7: 3.06μL of sample
Lane 8: 2.04μL of sample
Lane 9: 1.53μL of sample
Lane 10: L22μL of sample; Figure 25 is a semi-quantitative SDS PAGE gel for PBFT58d (strain 013), harvest point sample:
Lane 1 : High Molecular Weight Marker
Lane 2: 0.27μg collagenase I and 0.29μg collagenase II
Lane 3 : 0.18μg collagenase I and 0.19μg collagenase II Lane 4: 0.135μg collagenase I and 0.145μg collagenase II
Lane 5: 0.108μg collagenase I and 0.116μg collagenase II
Lane 6: 6.12μL of sample
Lane 7: 3.06μL of sample
Lane 8: 2.04μL of sample Lane 9: 1.53μL of sample
Lane 10: 1.22μL of sample;
Figure 26 is SDS PAGE gel for post-dialysed harvest point sample (520g/L ammonium sulphate) of PBFT58c fermentation (strain 004): Lane 1 : High Molecular Weight Marker Lane 2: 0.27μg collagenase I and 0.29μg collagenase II
Lane 3: 0.18μg collagenase I and 0.19μg collagenase II
Lane 4: 0.135μg collagenase I and 0.145μg collagenase II
Lane 5 : 0.108μg collagenase I and 0.116μg collagenase II
Lane 6: post dialysed harvest point sample — Neat Lane 7: post dialysed harvest point sample - (1/5 dilution)
Lane 8: post dialysed harvest point sample — (1/10 dilution)
Lane 9: post dialysed harvest point sample — (I/I 5 dilution)
Lane 10: post dialysed harvest point sample — (1/20 dilution); Figure 27 is a SDS PAGE gel for post-dialysed harvest point sample (400g/L ammonium sulphate) of PBFT58d fermentation (strain 013): Lane 1 : High Molecular Weight Marker
Lane 2: 0.27μg collagenase I and 0.29μg collagenase IT Lane 3: 0.18μg collagenase I and 0.19μg collagenase II
Lane 4: 0.135μg collagenase I and 0.145μg collagenase II
Lane 5: 0.108μg collagenase I and 0.116μg collagenase II Lane 6: post dialysed harvest point sample — Neat Lane 7: post dialysed harvest point sample — (1/5 dilution)
Lane 8: post dialysed harvest point sample — (1/10 dilution)
Lane 9: post dialysed harvest point sample — (1/15 dilution)
Lane 10: post dialysed harvest point sample — (1/20 dilution); Figure 28 is illustrates a flow chart of the Experimental procedure used for screening the alternative vegetable peptones;
Figure 29 illustrates a fed-batch strategy for DCFT27a,b fermentations; Figure 30 depicts growth curves (Net OD vs time) of C. histolyticum in 5L DCFT27a and DCFT27b fed-batch fermentations;
Figure 31 depicts growth curves (Net OD vs time) of C. histolyticum in 5L PBFT59a,b,c batch fermentations;
Figure 32 depicts a growth curve (Net OD vs time) of C. histolyticum in 5L DCFT27d fed-batch fermentation;
Figure 33a is a SDS PAGE gel for DCFT27d (Phytone supplemented with amino acids): Lane 1 : High Molecular Weight Marker
Lane 2: 18h (6.12μL of sample)
Lane 3: 17h (6.12μL of sample)
Lane 4: 15h (6.12μL of sample)
Lane 5: 14h (6.12μL of sample) Lane 6: 13h (6.12μL of sample)
Lane 7: 1 1.3h (6.12 μL of sample)
Lane 8: 0.27 μg Collagenase I and 0.29μg Collagenase U;
Figure 33b represents a schematic diagram of the inoculation procedure; Figure 33c represents a flow chart of an approximately 200 L fed batch inoculation process;
Figure 34 shows a chromatogram after hydroxyapatite chromatography; Figure 35 shows a chromatogram after a fractogel TMAE anion exhange; Figure 36 is an 8% Tris-Glycine SDS-PAGE analysis of Pre HA5 Post HA and Post TMAE material from 5 L scale rocess:
Figure imgf000014_0001
Figure 37 shows a chromatogram after a fractogel TMAE anion exhange;
Figure 38 is an 8% Tris-Glycine SDS-PAGE analysis of Q Sepharose IEX chromatography of post TMAE material run in the presence leupeptin:
Figure imgf000014_0002
Figure 39 is an 8% Tris-Glycine SDS-PAGE analysis of Q Sepharose IEX chromatography of post TMAE material run in the presence of leupeptin. Gel 2- Peak 2 (ABCI :
Figure imgf000014_0003
Figure imgf000015_0001
Figure 40 shows a chromatogram after a Q Sepharose HP anion exchange with modified gradient;
Figure 41 shows a chromatogram after a Superdex 75 Gel Permeation chromatography of ABCII; Figure 42 is a 12% Bis-Tris SDS-PAGE analysis of Superdex 75 GPC of concentrated ABC II run in the presence of arginine:
Figure imgf000015_0002
Figure 43 shows a chromatogram after a Superdex 75 Gel Permeation chromatography of ABCI;
Figure 44 is a 4-12% Bis-Tris SDS-PAGE analysis of Superdex 75 GPC of concentrated ABC I run in the presence of arginine:
Figure imgf000015_0003
4 GPC load lμg 15
5 Fraction D4 15
6 Fraction D3 15
7 Fraction D2 15
8 Fraction Dl 15
9 Fraction El 15
10 Fraction E2 15
11 Fraction E3 15
12 Fraction E4 15; Figure 45 represents a flow chart of one proposed manufacturing process;
Figure 46 represents a flow chart of the fermentation procedure for process 3;
Figure 47 represents a flow chart of the purification procedure for process 3;
Figure 48 is a SDS-PAGE (reduced) Coomasie stained for Intermediates AUXI and AUXII: Lane
1. High Molecular Weight Markers
2. 0.132mg/ml ABC-I Reference
3. 0.0265mg/ml ABC-I Reference
4. 0.132mg/ml AUX-I Intermediate 5. 0.0265mg/ml AUX-I Intermediate
6. 0.132mg/ml ABC-II Reference
7. 0.0265mg/ml ABC-II Reference
8. 0.132mg/ml AUX-II Intermediate
9. 0.0265mg/ml AUX-II Intermediate; Figure 49 is a SDS-PAGE (reduced) Coomasie stained for Drug Substance:
Lane
1. High Molecular Weight Markers
2. 0.132mg/ml Mixed BTC Reference
3. 0.0265mg/ml Mixed BTC Reference 4. 0.132mg/ml Drug Substance
5. 0.0265mg/ml Drug Substance;
Figure 50 is SDS-PAGE (reduced) Silver stained Drug Substance: Lane
1. HMW marker
2. Mixed BTC reference 1.3μg
3. Blank 4. Drug Substance 1.3 μg
5. Drug Substance 0.27μg
6. Drug Substance 0.13 μg.
Figure 51 depicts a comparison of C. histolyticum grown on Proteose Peptone #3 in a batch fermentation to the existing fermentation process using Phytone peptone during fed-batch cultivation;
Figure imgf000017_0001
Figure 52 is a SDS-PAGE analysis of the collagenase product at the harvest point (2Oh) of a 5L Proteose Pe tone #3 batch fermentation GCFT03b 8% Tris-Glycine):
Figure imgf000017_0002
Figure 53 is a SDS-PAGE analysis of the collagenase product at the harvest point (2Oh) of a 5L Phytone fed-batch fermentation (GCFT03d) (8% Tris-Glycine):
Figure imgf000018_0002
Figure 54 illustrates three fermentations of Clostridium histolyticum grown on 50g/L PP3 demonstrating a reproducible growth profile:
Figure imgf000018_0001
Figure 55 is a SDS-PAGE analysis showing the time course of GCFT05d (batch fermentation with Proteose Peptone #3), 8% Tris Glycine gel, colloidal stained):
Figure imgf000018_0003
Figure 56 is a SDS-PAGE analysis showing the time course of GCFT05d (batch fermentation with Proteose Peptone #3), (8% Tris Glycine gel, silver stained):
Figure imgf000018_0004
Figure 57 is a SDS-PAGE analysis showing the time course of DCFT24b (fed- batch fermentation using Phytone peptone), (8% Tris Glycine gel, colloidal stained):
Figure imgf000019_0001
Figure 58 illustrates a comparison of growth curves from C. histolyticum fermentations using different lots of PP3:
Figure imgf000019_0003
Figure 59 illustrates a small scale comparison of three lots of PP3 and evaluation
Θbatch 5354796 (5DgΛ.) Dbatch 53323BS (5O8A-) of 100g/L PP3 : βbatc*! 5325835 (5OQJL) CJbateh 533238.3 (100g/L)
Figure 60 depicts a growth profiles of two 5L fermentations utilizing PP3 at lOOg/L:
Figure imgf000019_0004
Figure 61 is a SDS-PAGE analysis of the time course of PBFT70c, 100g/L PP3 (lot # 5354796) fermentation (8% Tris-Glycine):
Figure imgf000019_0002
Figure 62 is a SDS-PAGE analysis of the timecourse of PBFT70d, 100g/L PP3 (lot # 5325635) fermentation (8% Tris-Glycine):
Figure imgf000020_0004
Figure 63 represents a densitometry analysis of SDS-PAGE to compare cell growth to product formation from 5L fermentation PBFT70c:
Figure imgf000020_0001
Figure 64 illustrates a Comparison of lOOg/L PP3 process at 5L and 200L scale:
Figure imgf000020_0003
Figure 65 is a SDS-PAGE analysis of the time course of the 200L fermentation (8% Tris-GIycine):
Figure imgf000020_0005
Figure 66 represents a densitometry analysis of SDS-PAGE to compare cell growth to product formation from 200L fermentation:
Figure imgf000020_0002
Figure 67 is a SDS-PAGE analysis of the time course of the 200L fermentation (4- 12% Bis-Tris):
Figure imgf000020_0006
Figure 68 shows a standard curve for densitometry quantification of collagenase concentration.
Figure 69 represents a schematic illustration of the fermentation and harvest of Clostridium histolyticum.
5 Figures 70 (a) and (b) are chromatograms resulting from Hydrophobic interaction chromatography using Phenyl Sepharose FF (low sub): (a) is full scale chromatogram and (b) is an expanded chromatogram showing fraction collection.
Figure 71 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the Mustang Q step to the TFFl step. The gel is stained with Colloidal blue and overloaded 10 (2.5μg total rotein/lane to show contaminant bands:
Figure imgf000021_0001
Figure 72 is an Ion exchange chromatogram (Q Sepharose HP) of the post HIC material after concentration and dϊafiltration into 1OmM Tris, 20OuM leupeptin pH 8.
Figure 73 is a 4-12% Bis Tris SDS-PAGE analysis of fractions from peak 1 15 (AUXII) eluted during the ion exchange column (figure 5). Gel 1 : the gel is stained with Colloidal blue:
Figure imgf000021_0002
Figure 74 is a 4-12% Bis Tris SDS-PAGE analysis of fractions from peak 1 (AUXII) eluted during the ion exchange column (figure 5). Gel 2: the gel is stained with Colloidal blue:
Figure imgf000022_0002
Figure 75 is a 4-12% Bis Tris SDS-PAGE analysis of fractions from peak 2 (AUXI) eluted during the ion exchange column (figure 5). Gel 3: the gel is stained with Colloidal blue:
Figure imgf000022_0003
Figure 76 is a 4-12% Bis Tris SDS-PAGE analysis of fractions from peak 2 (AUXI) eluted during the ion exchange column (figure 5). Gel 4: the gel is stained with
Colloidal blue:
Figure imgf000022_0001
Figure 77 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the anion exchange step to final product. The gel is stained with Colloidalblue. GeI 1: lμg/lane loading:
Figure imgf000023_0001
Figure 78 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the anion exchange step to final product. The gel is stained with Colloidal blue. Gel 2: 2.5μg/lane loading:
Figure imgf000023_0002
Figure 79 is a SDS-PAGE with 8% Tris Glycine (NB Ref AS/ 1640/020):
1. High Molecular Weight Markers
2. Blank Lane.
3. 1 μg Fermentation Filtrate Day 4
4. 1 μg Fermentation Filtrate Day 5
5. 1 μg Post Mustang Q Day 4
6. l μg Post HIC Day 3
7. 1 μg Post HIC Day 6 3. 1 μg Post TFF Day 2 9. 1 μg Post TFF Day 4
Figure 80 is a SDS-PAGE with 8% Tris Glycine:
1. High Molecular Weight Markers
2. 1 μg AUX-I Reference.
3. 1 μg AUX-II Reference
4. 1 μg Post IEX AUX-I Day 5
5. 1 μg Post IEX AUX-I Day 12
6. 1 μg Post IEX AUX-II Day 5
7. 1 μg Pest IEX AUX-II Day 12 Figure 81 is a SDS-PAGE gel: 1. High Molecular Weight Markers
2. 1 μg AUX-I Reference
3. 1 μg AUX-π Reference.
4. 1 μg AUX-I Intermediate Day 5
5. 1 μg AUX-I Intermediate- Day 12
6. 1 μg AUX-π Intermediate Day 5
7. 1 μg AUX-π Intermediate Day 12
Figure 82 represents analytical chromatography analysis. Figure 83 shows protein concentration determination by UV. Figure 84 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the 2OL demonstration run-through taken at the point of manufacture and stored at -200C. The gel is stained with Colloidal blue, l loadin :
Figure imgf000024_0001
Figure 85 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the 2OL demonstration run-through after 22hrs at Room Temperature. The gel is stained with Colloida
Figure imgf000024_0002
Figure 86 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the 2OL demonstration run-through after 22hrs at 37°C. The gel is stained with Colloidal blue:
Figure imgf000025_0003
Figure 87 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the 2OL demonstration run-through after 94hrs at Room Temperature. The gel is stained with Colloidal blue:
Figure imgf000025_0002
Figure 88 is a 4-12% Bis-Tris SDS-PAGE analysis of in-process samples from the 2OL demonstration run-through after 94hrs at 37°C. The gel is stained with Colloidal blue:
Figure imgf000025_0001
Figure 89 is a 8% Tris-Glycine SDS-PAGE analysis of selected post IEX AUX I and post IEX AUX II fractions. Fractions were selected from the 2OL demonstration run which were enriched for the required contaminant protein. The gel is stained with Colloidal blue:
Figure imgf000026_0001
Figure 90 is a 8% Tris-Glycine SDS-PAGE analysis of selected post IEX AUX I and post IEX AUX II fractions. Fractions were selected from purified material generated from fermentation 2OL PP3 and enriched for the ~90kDa contaminant protein. The gel is stained with Colloidal blue:
DETAILED DESCRIPTION OF THE INVENTION The invention provides a novel collagenase drug substance comprising a mixture of highly purified collagenase I and collagenase II in a mass ratio of about 1 to 1. It has been discovered that a composition comprising a mixture of collagenase I and collagenase II in an artificial mass ratio of 1 to 1 provides highly reproducible and optimal enzymatic activity and imparts superior therapeutic effect while lowering the potential for side effects. Tt is understood that the terms "drug substance", "drug product" or "collagenase composition" can be used interchangeably.
In one embodiment, the present invention provides a drug substance consisting of collagenase I and collagenase II having the sequence of Clostridium histolyticum collagenase I and collagenase II, respectively, having a mass ratio of about 1 to 1 with a purity of at least 95% by area, and preferably a purity of at least 98% by area.
In another embodiment, the present invention provides a drug substance, wherein the drug substance having at least one specification selected from table A below:
Table A
Figure imgf000027_0001
Figure imgf000028_0001
In one aspect, the invention provides a process for producing a drug substance consisting of collagenase I and collagenase Il having the sequence of Clostridium histolyticum collagenase I and collagenase II, respectively, having a mass ratio of about 1 to 1 with a purity of at least 95% by area, comprising the steps of: a) fermenting Clostridium histolyticum; b) harvesting a crude product comprising collagenase I and collagenase II; c) purifying collagenase I and collagenase II from the crude harvest via filtration and column chromatography; and d) combining the collagenase I and collagenase II purified from step (c) at a ratio of about 1 to 1.
In one preferred embodiment, the fermentation step is conducted in the presence of a porcine derived, a phytone peptone or a vegetable peptone medium. More preferably, the porcine derived medium is proteose peptone #3.
In one embodiment, the invention provides a fermentation procedure comprising the steps of: a) innoculating the medium in a first stage with Clostridium histolyticum and agitating the mixture; b) incubating the mixture from step (a) to obtain an aliquot; c) inoculating the medium in a second stage with aliquots resulting from step (b) and agitating the mixture; d) incubating mixtures from step (c); e) inoculating the medium in a third stage with aliquots resulting from step (d) and agitating; f) incubating mixtures from step (e); g) inoculating the medium in a fourth stage with an aliquot resulting from step (f) and agitating; h) incubating mixtures from step (g); and i) harvesting culture resulting from step (h) by filtration. In a preferred embodiment, the fermentation procedure comprises the steps of: a) Inoculating 3 x 25mL PP3 (proteose peptone) medium with 3 x 250μL of WCB (25mL cultures in 3 x 125mL shake flasks, contained within Anaerobe gas jar) at a temperature set point of 37°C, and agitating the mixture at 125rpm; b) incubating the mixture from step (a) for 12 hours; c) inoculating Inoculate 4 x 20OmL PP3 medium with 4 x 5mL aliquots from 1 of the above 25 mL cultures (20OmL cultures in 4 x 50OmL shake flasks, contained within Anaerobe gas jar) at a temperature set point of 370C, and agitating the mixture at 125rpm; d) incubating mixtures from step (c) for 12 hours; e) inoculating 14.4L of PP3 medium with 3 x 20OmL culture (15L culture in 2OL fermenter) at a temperature set point of 37°C and pH set point of 7.00, and agitating the mixture at 125rpm; f) incubating mixtures from step (e) for 12 hours; g) inoculating 192L of PP3 medium with 8L of 15L culture (200L culture in 270L fermenter) at a temperature set point of 37°C and pH set point of 7.00, and agitating the mixture at 125rpm; h) incubating mixtures from step (g) for 14 hours; and i) harvesting 200L culture by filtration (depth followed by 0.2μm) via
Millipore Millistak 4m2 and 0.2μm filter (2 x Millipore Express XL 10 filters) at a flow rate of 200L/h.
Tn one embodiment, the invention provides a purification procedure comprising the steps of: a) filtering the crude harvest through a Mustang Q anion-exchange capsule filter; b) adding ammonium sulphate; preferably to a final concentration of IM; c) filtering the crude harvest; preferably through a 0.45 μm filter; d) subjecting the filtrate through a HTC column; preferably a phenyl sepharose 6FF (low sub); e) adding leupeptin to the filtrate; preferably to a final concentration of 0.2 mM to post HIC eluted product; f) removing the ammonium sulfate and maintaining leupeptin for correct binding of collagenase I and collagenase II with buffer exchange by TFF; preferably with buffer exchange by TFF; g) filtering the mixture of step (f); preferably through a 0.45 μm filter; h) separating collagenase I and collagenase II using Q-Sepharose HP; i) preparing TFF concentration and formulation for collagenase I and collagenase II separately; wherein TFF is a tangential flow filtration using 10 and/or 3OK MWCO (molecular weight cut-off) PES or RC - polyethersulfone or regenerated cellulose filter membranes. Provides means to retain and concentrate select protein and exchange the protein from one buffer solution into another; and j) filtering through a 0.2 μm filtration system.
The drug substance of the present invention includes both collagenase I and collagenase II. A preferred source of crude collagenase is from a bacterial fermentation process, specifically the fermentation of C. histolyticum (C. his). In one embodiment of the invention, a fermentation process is described. The crude collagenase obtained from C. his may be purified by a variety of methods known to those skilled in the art, including dye ligand affinity chromatography, heparin affinity chromatography, ammonium sulfate precipitation, hydroxylapatite chromatography, size exclusion chromatography, ion exchange chromatography, and metal chelation chromatography. Crude and partially purified collagenase is commercially available from many sources including Advance Biofactures Corp., Lynbrook, New York.
Both collagenase I and collagenase II are metalloproteases and require tightly bound zinc and loosely bound calcium for their activity (Eddie L. Angleton and H. E. Van Wart, Biochemistry 1988, 27, 7406- 7412). Both collagenases have broad specificity toward all types of collagen (Steinbrink, D; Bond, M and Van Wart, H; (1985), JBC, 260 p2771-2776). Collagenase I and Collagenase II digest collagen by hydrolyzing the triple-helical region of collagen under physiological conditions (Steinbrink, D; Bond, M and Van Wart, H; (1985), JBC, 260 p2771 - 2776). Even though each collagenase shows different specificity (e.g. each have a different preferred amino sequence for cleavage), together, they have synergistic activity toward collagen [Mandl, I., (1964), Biochemistry, 3: p.1737-1741; Vos- Scheperkeuter, GH, ( 1997), Cell Transplantation, 6 : p.403-412] . Col lagenase Il has a higher activity towards all kinds of synthetic peptide substrates than collagenase I as reported for class II and class I collagenase in the literatures. [Bond, M.D. (1984), Biochemistry, 23: p.3085-3091. Hesse, F, (1995), Transplantation Proceedings, 27: p.3287-3289].
Examples of collagen mediated-diseases that may be treated by the compositions and methods of the invention include but are not limited to: Dupuytren's disease; Peyronie's disease; frozen shoulder (adhesive capsulitis), keloids; hypertrophic scars; depressed scars such as those resulting from inflammatory acne; post-surgical adhesions; acne vulgaris; lipomas, and disfiguring conditions such as wrinkling, cellulite formation and neoplastic fibrosis. U.S. Pat. Nos. 6,086,872 and 5,589,171 incorporated herein by reference disclose the use of collagenase preparations in the treatment of Dupuytren's disease. U.S. Pat. No. 6,022,539 incorporated herein by reference discloses the use of collagenase preparations in the treatment of Peyronie's disease.
In addition its use in treating collagen-mediated diseases, the composition of the invention is also useful for the dissociation of tissue into individual cells and cell clusters as is useful in a wide variety of laboratory, diagnostic and therapeutic applications. These applications involve the isolation of many types of cells for. various uses, including microvascular endothelial cells for small diameter synthetic vascular graft seeding, hepatocytes for gene therapy, drug toxicology screening and extracorporeal liver assist devices, chondrocytes for cartilage regeneration, and islets of Langerhans for the treatment of insulin-dependent diabetes mellitus. Enzyme treatment works to fragment extracellular matrix proteins and proteins which maintain cell-to-cell contact. Since collagen is the principle protein component of tissue ultrastructure, the enzyme collagenase has been frequently used to accomplish the desired tissue disintegration. In general, the composition of the present invention is useful for any application where the removal of cells or the modification of an extracellular matrix, are desired.
Collagenase compositions of the invention may also be prepared by mixing either a specific number of activity units or specific masses of the preferably purified enzymes. Collagenase activity can be measured by the enzyme's ability to hydrolyze either synthetic peptide or collagen substrate. Those skilled in the art will recognize that enzyme assays other than those disclosed herein may also be used to define and prepare functionally equivalent enzyme compositions. Another aspect of the present invention is the reproducible optimization of the 1 to 1 mass ratio of collagenase I to collagenase II in the composition of the invention. The reproducibility of the ratio of collagenase I to collagenase II has previously been a challenge because of several factors. First, commercial fermentation of Clostridium generally results in a 1 to 2 ratio of collagenase I and collagenase II. Second, the purification procedures are known to alter this ratio significantly resulting in inconsistent ratios of purified product. The optimized fixed mass ratio of the composition of the present invention maximizes the synergistic activity provided by the two different collagenases resulting in superior therapeutic benefit. The invention also provides pharmaceutical formulations of the compositions of the invention. The pharmaceutical formulations of the present invention comprise a therapeutically effective amount of a collagenase composition of the present invention formulated together with one or more pharmaceutically acceptable carriers or excipients. As used herein, the term "pharmaceutically acceptable carrier or excipient" means a non-toxic, inert solid, semi-solid or liquid filler, diluent, encapsulating material or formulation auxiliary of any type. Some examples of materials which can serve as pharmaceutically acceptable carriers are sugars such as lactose, glucose and sucrose; starches such as corn starch and potato starch; cellulose and its derivatives such as sodium carboxymethyl cellulose, ethyl cellulose and cellulose acetate; powdered tragacanth; malt; gelatin; talc; glycols such as propylene glycol; esters such as ethyl oleate and ethyl laurate; agar; buffering agents such as magnesium hydroxide and aluminun hydroxide; alginic acid; pyrogen-free water; isotonic saline; Ringer's solution; ethyl alcohol, and phosphate buffer solutions, as well as other non-toxic compatible lubricants such as sodium lauryl sulfate and magnesium stearate, as well as coloring agents, releasing agents, coating agents, perfuming agents, preservatives and antioxidants can also be present in the composition, according to the judgment of the formulator.
The pharmaceutical compositions of this invention may be administered parenteral Iy, topically, or via an implanted reservoir. The term parenteral as used herein includes subcutaneous, intracutaneous, intravenous, intramuscular, intraarticular, intraarterial, intrasynovial, intrasternal, intrathecal, intralesional and intracranial injection or infusion techniques. In a preferred embodiment, the composition is injected into the disfiguring tissue. In the case of Peyronie's or Duputyren's diseases or adhesive capsulitis, the composition is injected into the cord or plaque. The term "local administration" is defined herein to embrace such direct injection.
Furthermore, particularly good results can be obtained by immobilizing the site of injection after administration. For example, the site of administration can be immobilized for 4 or more hours. Injectable preparations, for example, sterile injectable aqueous or oleaginous suspensions, may be formulated according to the known art using suitable dispersing or wetting agents and suspending agents. The sterile injectable preparation may also be a sterile injectable solution, suspension or emulsion in a nontoxic parenterally acceptable diluent or solvent, for example, as a solution in 1, 3-butanediol. Among the acceptable vehicles and solvents that may be employed are water, Ringer's solution, U.S.P. and isotonic sodium chloride solution. In addition, sterile, fixed oils are conventionally employed as a solvent or suspending medium. For this purpose any bland fixed oil can be employed including synthetic mono- or diglycerides. In addition, fatty acids such as oleic acid are used in the preparation of injectables. The injectable formulations can be sterilized, for example, by filtration through a bacterial-retaining filter, or by incorporating sterilizing agents in the form of sterile solid compositions which can be dissolved or dispersed in sterile water or other sterile injectable medium prior to use. The sterile solutions may also be lyophilized for later use. Dosage forms for topical or transdermal administration of a compound of this invention include ointments, pastes, creams, lotions, gels, powders, solutions, sprays, inhalants or patches. The active component is admixed under sterile conditions with a pharmaceutically acceptable carrier and any needed preservatives or buffers as may be required.
The ointments, pastes, creams and gels may contain, in addition to an active compound of this invention, excipients such as animal and vegetable fats, oils, waxes, paraffins, starch, tragacanth, cellulose derivatives, polyethylene glycols, silicones, bentonites, silicic acid, talc and zinc oxide, or mixtures thereof.
Powders and sprays can contain, in addition to the compounds of this invention, excipients such as lactose, talc, silicic acid, aluminum hydroxide, calcium silicates and polyamide powder, or mixtures of these substances. Sprays can additionally contain customary propellants such as chlorofluorohydrocarbons. Transdermal patches have the added advantage of providing controlled delivery of a compound to the body. Such dosage forms can be made by dissolving or dispensing the compound in the proper medium. Absorption enhancers can also be used to increase the flux of the compound across the skin. The rate can be controlled by either providing a rate controlling membrane or by dispersing the compound in a polymer matrix or gel.
In one preferred embodiment, the drug substance of the invention is a lyophilized injectable composition formulated with lactose. In one embodiment each milligram of injectable collagenase is formulated with 1.9 mg of lactose. In another embodiment, each milligram of injection collagenase preferably has approximately 2800 SRC units and 51000 units measured with a potency assay using a synthetic substrate, pzGPGGPA.
In another preferred embodiment, the collagenase composition of the invention is a lyophilized injectable composition formulated with Sucrose, Tris at a pH level of about 8.0. Most preferably, 1.0 mg of the drug substance of the invention is formulated in 60 mM Sucrose, 10 mM Tris, at a pH of about 8.0 (this equates to 20.5 mg/mL of sucrose and 1.21 mg/mL of Tris in the formulation buffer). Examples of some of the formulations include, but not limited to: for a 0.58 mg of the drug substance dose, 18.5 mg of sucrose and 1.1 mg of Tris are added in each vial, where the targeting a vial fill volume is 0.9 ml; and for a 0.58 mg of the drug substance dose, 12.0 mg sucrose (multicompendial) and 0.7 mg of Tris (multicompendial). In accordance with the invention, methods are provided for treating collagen- mediated diseases comprising the step of administering to a patient in need thereof, a therapeutically effective amount of a composition of the invention, or a therapeutically effective amount of a pharmaceutical formulation of the invention. By a "therapeutically effective amount" of a compound of the invention is meant an amount of the compound which confers a therapeutic effect on the treated subject, at a reasonable benefit/risk ratio applicable to any medical treatment.
The therapeutic effect may be objective (i.e., measurable by some test or marker) or subjective (i.e., subject gives an indication of or feels an effect). Effective doses will also vary depending on route of administration, as well as the possibility of co-usage with other agents. It will be understood, however, that the total daily usage of the compositions of the present invention will be decided by the attending physician within the scope of sound medical judgment. The specific therapeutically effective dose level for any particular patient will depend upon a variety of factors including the disorder being treated and the severity of the disorder; the activity of the specific compound employed; the specific composition employed; the age, body weight, general health, sex and diet of the patient; the time of administration, route of administration, and rate of excretion of the specific compound employed; the duration of the treatment; drugs used in combination or contemporaneously with the specific compound employed; and like factors well known in the medical arts.
The drug substance for injectable collagenase consists of two microbial collagenases, referred to as Collagenase AUX I and Collagenase ABC I and Collagenase AUX II and Collagenase ABC II. It is understood that the terms "Collagenase I", "ABC I", "AUX I", "collagenase AUX I", and "collagenase ABC I" mean the same and can be used interchangeably. Similarly, the terms "Collagenase II", "ABC II", "AUX II", "collagenase AUX II", and "collagenase ABC II" refer to the same enzyme and can also be used interchangeably. These collagenases are secreted by bacterial cells. They are isolated and purified from Clostridium histolyticum culture supernatant by chromatographic methods. Both collagenases are special proteases and share the same EC number (E.C 3.4.24.3). Collagenase AUX I has a single polypeptide chain consisting of approximately 1000 amino acids with a molecular weight of 115 kDa. Collagenase AUX II has also a single polypeptide chain consisting of about 1000 amino acids with a molecular weight of 1 10 kDa. Even though the literature indicates that there are sequence homologies in regions of collagenase AUX I and AUX II, the two polypeptides do not seem to be immunologically cross reactive as indicated by the western blot analysis.
The drug substance (collagenase concentrate) has an approximately 1 to 1 mass ratio for collagenase AUX I and AUX II. The collagenase concentrate has an extinction coefficient of 1.528.
All references cited herein, whether in print, electronic, computer readable storage media or other form, are expressly incorporated by reference in their entirety, including but not limited to, abstracts, articles, journals, publications, texts, treatises, internet web sites, databases, patents, and patent publications. Examples
The compositions and processes of the present invention will be better understood in connection with the following examples, which are intended as an illustration only and not limiting of the scope of the invention. Various changes and modifications to the disclosed embodiments will be apparent to those skilled in the art and such changes and modifications including, without limitation, those relating to the processes, formulations and/or methods of the invention may be made without departing from the spirit of the invention and the scope of the appended claims. PROCESS 2: Fermentation Process This work was set out to develop a fermentation process that aimed at delivering a target yield of 250mg/L of total collagenases ABC I & II from the 5L fermentation scale process in an animal free component growth media. Various potential alternative nitrogen sources were screened to see if they had any affect on collagenase expression over and the above the phytone component currently used in the growth media. An experiment comparing productivities from two strains of C. histolyticum, 004 and 013, was to determine any differences between the two strains with respect to growth kinetics, collagenase productivity and production of contaminating proteases grown in an animal derived media. This comparison highlighted significant differences between growing the C. histolyticum strain in animal derived media as opposed to animal free growth media.
Previous results described that increased concentrations of phytone and yeast extract were shown to support higher biomass concentrations and hence higher levels of total collagenase expression. In an attempt to further increase biomass concentrations and total collagenase productivity of the optimised batch fermentation media, a fed-batch fermentation strategy was designed. Two 5L fermentations were performed, one with a high concentration of media in the batch phase followed by a low concentration feeding phase, the second with a low concentration of media in the batch phase followed with a high concentration feeding phase. Both fermentations produced high biomass concentrations, however the high concentration batch phase showed relatively low levels of collagenase expression. The low concentration batch fermentation showed very high levels of collagenase expression (—280 mg/L), however this culture also produced significant quantities of the contaminating protease, clostripain.
Although the low concentration batch fermentation gave very good results with respect to expression of the collagenases, the highly concentrated phytone and yeast extract feed solution was very difficult to prepare. Two additional fermentations were performed, the first was a repeat of the previous successful fed- batch fermentation the second had a slightly higher concentration batch phase media composition with a lower concentrated feeding solution. Both fermentations achieved similar biomass concentrations and showed the same expression profile of the collagenases and clostripain. The quantity of collagenase produced was again estimated at approximately 280mg/L in both fermentations. However, these fermentations produced significant quantities of the contaminating protease clostripain.
A selection of alternative nitrogen sources were assessed for their ability to replace the phytone peptone used in the fed-batch fermentation strategy. The C. histolyticum grew extremely well on the vegetable peptones reaching optical densities (600nm) of 4 to 5 units. However, SDS-PAGE analysis of these fermentations showed no expression of either collagenase or clostripain. Due to the luxuriant cell growth observed on these peptones it was thought that the concentration of complex nitrogen source was too high resulting in an inhibition of protease expression. A second set of fermentations was therefore carried out using the alternative peptones at 50 g/L in a batch strategy. When the fermentations were analyzed by SDS-PAGE no expression of collagenase or clostripain was seen again. A fed-batch fermentation using phytone peptone was supplemented with three amino acids, glutamine, tryptophan and asparagine. These amino acids were identified as being present in lower amounts in the non-animal media. The growth profile of the fermentation was very similar to that of the fed-batch fermentation without amino acid supplementation. SDS-PAGE analysis showed a similar yield of collagenase but a slightly lower level of clostripain. The clostripain assay showed reduced activity in the amino supplemented when compared to the control fed-batch fermentation. The reduction in clostripain activity whilst still significant was not as great as the difference between animal and non-animal media. The assessment of the primary recovery step of the collagenases using ammonium sulphate precipitation was carried out on 0.2μm filtrates of the crude fermentation supernatants. The aim here was to help increase the collagenase yield and ideally decrease the quantity of clostripain that was carried through the process. Initially ammonium sulphate concentrations of 100 - 400g/L were assessed. Ammonium sulphate at 400g/L resulted in significant recovery of collagenase. A further study was carried out with a higher range of ammonium sulphate (400 - 520g/L). In addition, the effect of decreasing the pH to 6.0 and oxygenating the media prior to precipitation were also investigated. No difference was observed in either the quantity of the collagenases or clostripain recovered from the supernatant under any of these conditions. The pellet generated from 400g/L ammonium sulphate was the easiest to resuspend.
The study to compare the two strains of C. histolyticum (004 and 013) showed that the productivity of the collagenases from the animal derived media was lower than that of the optimal non-animal derived media. SDS-PAGE analysis, supported by an enzymatic assay for clostripain activity, highlighted that there were significantly lower quantities of clostripain in the material produced from the animal derived media than the non-animal media. This highlighted the fact that the feedstock produced from the non-animal derived media fermentation was a significantly different feedstock material from the fermentation using animal derived media with respect to the production of contaminating proteases. 1st set of fed-batch fermentations - DCFT24
The results from the process development work showed that the use of an enriched media (100g/L phytone peptone and 50g/L yeast extract) resulted in the expression of higher amounts of collagenases compared to the original media (50g/L phytone peptone and 8.5g/L yeast extract). In addition, it initially appeared that it reduced the amounts of clostripain produced.
Two 5L fermentations were then performed. Firstly the strategy consisted of a long batch phase/short fed-batch phase, whereas the second consisted of a short batch phase / long fed-batch phase. In both strategies at the end of the fermentation (after 2Oh) the concentrations of phytone peptone and yeast extract were 100g/L and 50g/L, respectively, as in the case of the batch fermentations. Table 1 and 2 detail the media recipes and strategies used. Table 1 Media reci e and fed-batch strate
Figure imgf000039_0001
Table 2 Media recipe and fed-batch strategy
Figure imgf000040_0001
Figure 1 shows the growth curves (ODeoonm vs time) from the two fermentations, whereas Figure 2 shows the net growth curves (Net ODβoonm vs time). It was observed that the cells from the first fermentation grew very fast and reached their maximum OD after approximately 10 hours. This was due to the fact that the media in the batch phase was very rich. During the fed-batch phase the cells did not appear to grow. The OD values decreased slightly, which could be partly attributed to the fact that the cells were dying and to the dilution effect of the feed in to the fermenter.
For the second fermentation, the fed-batch phase was started after 6 hours. At that point the OD value would have been low, as suggested by the growth curve in Figure 1. The cells continued to grow slowly up to approximately 18 hours. It was noted that the net growth curves in Figure 2 suggested that the cell densities in DCFT24b fermentation were higher than in DCFT24a fermentation. The ODόoonm of the media prior to inoculation was approximately 1.7, whereas in DCFT24b it was approximately 0.4. These differences are due to the fact when the fermenters are autoclaved a precipitate is formed. For DCFT24a, higher amounts were formed compared to DCFT24b.
SDS PAGE gels: SDS PAGE analysis (8% Tris - Glycine gels) of the supernatant samples were carried out for each for the two fermentations. The gels are shown in Figure 3 and 4. A semi - quantitative SDS PAGE gel was also produced for the harvest point sample of the second fermentation.
The SDS PAGE gel analysis in Figure 4 indicated that very low amounts of the collagenases were expressed. This could be due to the fact that the cells grew very fast during the batch phase and as a result the maximum cell concentration was reached after approximately 10. hours. In contrast, very high level of collagenase expression was observed in the second fermentation, probably due to the fact that the cells grew more slowly during the short batch phase and continued to grow during the fed-batch phase. Thus the invention relates to an improved fermentation method for C. his wherein cell growth is controlled and slow during the short batch phase and continuing growth during the fed-batch phase. Slow growth is defined to mean that the rate of growth during the short batch phase does not result in a maximum cell concentration prior to the fed-batch phase, such as within about 10 hours of the beginning of the fermentation process. In a preferred embodiment, the rate of growth is approximately that resulting from the second fermentation cycle described herein.
Estimated collagenase productivities from the semi-quantitative SDS PAGE gel at the harvest point of the second fermentation cycle (Figure 5), were 132mg/L for collagenase ABC I and 158mg/L for collagenase ABC II. Comparing these values with those previously obtained, there is approximately a 3-fold increase in the expression levels using the fed-batch strategy.
The next step was to perform an additional set of fed-batch fermentations using slightly modified fed-batch strategies and media. The aim was to improve the scalability and robustness of the fermentation process.
The media recipe for this fermentation was the same as above, with the exception that the phytone peptone and the yeast extract in the batch phase were filter sterilised instead of being autoclaved. This was done in order to avoid autoclaving the yeast extract and phytone, which can potentially affect their composition by heat and denaturation of proteins in the media. For fermentation DCFT26b, the amount of yeast extract and phytone peptone was increased. This was done so that the concentration of yeast extract and peptone in the feed was less than that in DCFT26a and thus easier to make up and filter sterilise. For both fermentations the strategy followed was the same, a 6h batch phase followed by a 14h fed-batch phase. Tables 3 and 4 present the media recipes, whereas Figure 6 the strategy used for both fermentations.
Table 3 Media recipe and fed-batch strategy for DCFT26a
Figure imgf000042_0001
Table 4 Media recipe and fed-batch strategy for DCFT26b
Figure imgf000043_0001
Figure 7 shows the growth curves (ODgoonm vs time) from the two fermentations, whereas Figure 8 shows the net growth curves (Net OD^oonm vs time).
The growth curves for DCFT26a and DCFT26b were very similar to that of DCFT24b shown in Figure 2. The cells grew slowly during the fed-batch phase and reached a final net OD6oonm of approximately 3.5.
SDS PAGE gels of fermentation samples:
SDS PAGE analysis (8% Tris - Glycine gels) of the supernatant samples was carried out for each of the two fermentations (Figure 9 and Figure 10). Tn addition, in order to have a better estimate of the amount of collagenases, a semi-quantitative SDS PAGE gel was conducted for the harvest sample point of DCFT26a (Figure 11) and DCFT26b (Figure 12).
In both fermentations the levels of collagenases were similar to those in DCFT24b (Figure 3). The semi-quantitative SDS PAGE gel shows that very similar levels to DCFT24b (between 280mg/L to 300mg/L total collagenase) were obtained for both DCFT26a and DCFT26b. The harvest point of the DCFT26a fermentation cycle (Figure 11) were ~ 142mg/L for collagenase I and ~ 132mg/L for collagenase II. The harvest point of the DCFT26b fermentation cycle (Figure 12) were ~ 147mg/L for collagenase I and ~ 158mg/L for collagenase 11. The levels of clostripain, as in the case of DCFT24b, were still high.
Study of the ammonium sulphate precipitation step:
The results from these fermentations indicated that although the levels of collagenases were high using the fed-batch strategy, the levels of clostripain were also still significantly high. Therefore a small scale experimental study was set up to investigate the effect of the ammonium sulphate concentration on the recovered amounts of clostripain and collagenases in the precipitated pellet from the filtered fermentation supernatant.
In order to evaluate the efficiency of the ammonium sulphate precipitation step, 6 x 10OmL supernatant samples were harvested from fermentation DCFT26a. These samples were precipitated with 6 different ammonium sulphate concentrations as detailed in the following table. The pellets were re-suspended in 3.3mL of WFI and dialysed against 10OmM OfK2HPO4 (pH 6.7).
Table 5 Ammonium sulphate concentrations that were used to precipitate 10OmL supernatant samples from DCFT26a.
Figure imgf000044_0001
The post-dialysed samples were then analysed by SDS PAGE analysis. Figure 13: post-dialysed harvest point sample precipitated with 15% and 22.5% Figure 14: post-dialysed harvest point sample precipitated with 30% and 37.5% Figure 15: post-dialysed harvest point sample precipitated with 45% and 60% The gels show that in the case where the ammonium sulphate used was between 15% to 45% saturation, the levels of collagenases in the post-dialysed samples were very low. The recovery in these cases seemed to be less than 5%. In the case where 60% saturation of ammonium sulphate was used (400g/L) the levels of collagenases in the post-dialysed sample were very high (Figure 15). By comparing the intensity of the bands (sample versus references) it can be estimated that approximately 70mg/L for each of the collagenases were present in the post-dialysed sample. This suggests a recovery of about 50 to 60%, since according to the semi-quantification gel for DCFT26a (Figure 11) there were approximately 130mg/L of each of the collagenases in the harvest point sample.
Thus, the invention relates to the use of the media recipe (of course, amounts set forth therein are approximated) set forth above in DCFT26b and the use of ammonium sulphate to precipitate collagenase wherein about 400 g/liter of ammonium sulfate is added to the collagenase-containing medium. 3rd set of fed-batch fermentations
Here the primary aim was to assess the reproducibility of the developed fed- batch strategy. A fed-batch fermentation was performed which was a replicate fermentation of DCFT26b. In addition, the ammonium sulphate / precipitation steps were investigated in more detail compared to the previous small-scale study. More specifically, the aim was to examine the effect of various ammonium sulphate concentrations, from 60% (400g/L) up to 80% (530g/L) on the recovery of collagenases and clostripain in the post precipitated / dialysed samples. In addition, two methods of treating the harvested supernatant samples were also assessed, i.e., shifting the pH and oxygenating the media. Growth curve:
The media and fed-batch strategy used was exactly the same as DCFT26b. Figure 16 shows the growth curve (ODβoonm vs time) and the net growth curve (Net OD6oonm vs time) from the fermentation. The growth curve was very similar to that ofDCFT26b, indicating the good reproducibility of the process.
SDS PAGE analysis (8% Tris — Glycine gels) of the supernatant samples taken throughout the fermentation indicated that the levels of collagenases and clostripain were very similar to those of DCFT26b (SDS PAGE gel not shown). A semi-quantitative SDS PAGE gel (8% Tris - Glycine gel) was performed for the harvest point sample (Figure 17). The gel suggests that there is higher than 120mg/L of each of the collagenases present, similar to the levels observed in DCFT26b.
Ammonium sulfate precipitation of fermentation harvest samples: In order to evaluate the efficiency of the ammonium sulphate precipitation step, 7 x 50OmL supernatant samples were harvested. These were precipitated using the following six methods.
In all cases, the pellets were re-suspended in 16.5mL of WFI and dialysed against 10OmM of K2HPO4 (pH 6.7), with the exception of method 4, where the pellet was re-suspended in 16.SmL of 10OmM Of K2HPO4 (pH 6) and dialysed against the same buffer. SDS PAGE gels were then performed in order to estimate the amounts of collagenases in the post-dialysed samples and evaluate the recovery of the precipitation /dialysis steps.
The methods for precipitation / dialysis followed are the following: 1 Precipitation with 400g/L of ammonium sulphate added all at once into the supernatant sample. Dialysis against 10OmM OfK2HPO4, pH 6.7.
2 Precipitation with 400g/L of ammonium sulphate added slowly (about 30min) into the supernatant sample. Dialysis against 10OmM of K2HPO4, pH 6.7.
3 Precipitation with 400g/L of ammonium sulphate added slowly (about 30min) into the supernatant sample, which was pre-oxygenated. This was done by oxygenating for approximately 10 minutes 50OmL of cell culture harvested from the fermenter. The culture was then filter sterilised. The pellet formed after ammonium sulphate precipitation was dialysed against 10OmM Of K2HPO4 pH 6.7. 4 Precipitation with 400g/L of ammonium sulphate added slowly (about 30min) into the supernatant sample, the pH of which was changed to pH 6 by adding 5N HCl. The pellet formed after was dialysed against 10OmM OfK2HPO4, pH 6. 5 Precipitation with 440g/L of ammonium sulphate added slowly (about 30min) into the supernatant sample. Dialysis against 10OmM OfK2HPO4, pH 6.7. 6 Precipitation with 480g/L of ammonium sulphate added slowly (about 30min) into the supernatant sample. Dialysis against 10OmM OfK2HPO4, pH 6.7. 7 Precipitation with 520g/L of ammonium sulphate added slowly (about 30min) into the supernatant sample. Dialysis against 10OmM OfK2HPO4, pH 6.7. The ammonium sulphate did not completely dissolve when added at 480g/L and 520g/L in the supernatant samples, whereas it completely dissolved when added at 400g/L and 440g/L. The results from the SDS PAGE indicated that the different levels of ammonium sulphate used for the precipitation step (400g/L, 440g/L, 480g/L, 520g/L) or the other methods used (oxygenation, pH shift) did not seem to have an obvious effect on the amounts of collagenases present in the post dialyzed samples. In all cases, the concentration of each of the collagenases in the post dialyzed samples ranged between 50mg/L and 60mg/L. Figure 18a shows a representative SDS PAGE gel, such as that of the post dialyzed sample precipitated with 400g/L ammonium sulphate. Since all the gels were very similar the other SDS PAGE gels are not presented in this report.
Taking into account the estimated concentrations of collagenases in the harvest point sample (Figure 17) and in the post dialyzed samples, the recovery of the collagenase after the precipitation / dialysis steps was approximately 50%. In order to investigate whether the value of 50% recovery was accurate, since the error in the estimation of collagenase concentration by SDS gel is in general high, the following SDS PAGE gels were carried out. • An SDS PAGE gel of all the supernatants after centrifugation of the ammonium sulphate precipitated samples (Figure 18a). The aim was to assess whether any amount of collagenases is lost into the supernatant.
• An SDS PAGE gel in which the harvest point supernatant sample and the post dialysed ammonium sulphate (400g/L) precipitated sample were appropriately diluted to contain equal amounts of collagenases and loaded on the same gel (Figure 19).
• An SDS PAGE gel in which the harvest point supernatant sample and the post dialysed ammonium sulphate sample (520g/L) were appropriately diluted to contain equal amounts of collagenases and loaded on the same gel (Figure 20).
It can be seen from Figure 18b that the amount of collagenases present in the supernatants after centrifugation of the ammonium sulphate precipitated samples was very low. In Figure 19 and Figure 20 that the amount of collagenases after the precipitation / dialysis steps appeared to be very similar to that in the supernatant harvest sample. It was therefore likely that the recovery value that was derived by comparing the semi-quantitative SDS PAGE gels of the supernatant and the post- dialyzed samples was actually higher.
Benchmarking fermentation experiments with animal derived TSB/Proteose:
Fermentations of C. histolyticum 013 and 004 strains in the media containing animal derived components were performed. The aim was to compare strain 013 to strain 004 and evaluate the effect of the animal components on cell growth, collagenase expression and on the levels of contaminants.
C. histolyticum 013:
The lyophilised strain was re-constituted in PBS and plated out onto
TSB/Proteose agar plates (30g/L TSB, 10g/L proteose peptone, 12g/L agar. The plates were incubated in an anaerobic jar in the presence of anaerobic gas packs.
Single colonies were picked and used to inoculate 5mL TSB/Proteose media. After
15 hours of incubation at 37°C the ODβooπm of the culture was approximately 1.0 unit. 5mL of culture was then mixed with ImL of sterile and stored below -7O0C.
PBFT58 fermentations Growth curves:
Two 5L batch fermentations were carried out, PBFT58c (strain 004) and
PBFT58d (strain 013). Table 6 presents the recipe of the TSB/Proteose media used.
Figure 21 shows the growth curves obtained (Net ODeoonm vs time).
Table 6 Recipe for TSB/Proteose media
Figure imgf000049_0001
It was seen from Figure 21 that the strain 013 grew to a higher OD than strain 004. In both cases however the final OD^oonm was higher than 2.5, indicating that the animal derived media supported good growth for both strains.
It was noted that strain 013 continued to grow slowly up to the harvest point (20 hours) whereas strain 004 grew up to a net ODβoonm of approximately 2.7 and then stopped growing. Compared to the fed-batch fermentations presented previously, using the non-animal derived media, the final OD obtained using the animal derived TSB/Proteose media was lower. SDS PAGE analysis:
The SDS PAGE gels (8% Tris-Glycine gels) of the supernatant samples taken throughout the fermentations are shown in Figure 22 and Figure 23.
There did not seem to be any clostripain in the fermentation supernatants, especially in the case of strain 013. This was a very important finding since it could explain the fact that the originator may not have had issues or reduced issues during the purification of collagenases. In contrast, significant problems with degradation of the collagenases had been previously experienced during the purification process. This could be partly attributed to the presence of clostripain in the fermentation. In order to obtain a better estimate of the amount of collagenases present in the fermentations, a semi-quantitative SDS PAGE gel was conduced for the harvest point samples (Figure 24 and Figure 25). The gels suggest that lower amount of collagenases was produced in the batch fermentations with the TSB/Proteose media (PBFT58c) compared to the fed-batch fermentation with the vegetable media (PBFT57). This could be attributed to the fact that higher cell densities were obtained in the latter case (OD^oonm ~ 4 to ODβoonm ~ 2.7). Table 7 summarizes the results from the semi-quantitative gels.
Table 7. Results from semi-quantitative SDS PAGE gels for PBFT57 and PBFT58c,d
Figure imgf000050_0001
Ammonium sulphate precipitation of fermentation harvest samples:
For each fermentation, 2 x 50OmL harvest point samples were precipitated with 400g/L (60%) and 520g/L (80%) ammonium sulphate. The pellets were re- suspended in 16.5mL of WFI and dialyzed against 10OmM of K2HPO4 (pH 6.7). SDS PAGE analysis (8% Tris-Glycine gels) of the post-dialyzed samples was then performed (Figure 26 and Figure 27).
The results from these gels indicated that the levels of clostripain, even in the very concentrated post-dialyzed samples (lanes 6 and 7 of Figures 26 and 27) were extremely low. This is more evident in the case of strain 013 compared to strain 004.
Thus the invention relates to collagenase compositions which are free of clostripain, such as those produced by the fermentation processes described herein. Measurement of clostripain activity:
In order to investigate further the role of clostripain an enzymatic assay was set up to measure the clostripain activity of post dialyzed samples. The following method was used: Enzymatic assay of clostripain:
Figure imgf000051_0001
BAEE = N-a-Benzoyl-L-Arginine Ethyl Ester Conditions: T = 25°C, pH = 7.6, A25311nI, Light path = 1 cm Method: Continuous Spectrophotometry Rate Determination
Unit definition: One unit will hydrolyze 1.0 μmole of BAEE per minute at pH 7.6 at 25°C in the presence of 2.5 mM DTT. Analysis of post dialvsed samples for clostripain activity:
The clostripain activity assay was used to analyze the post-dialyzed samples from the fermentations with the TSB/Proteose (PBFT58) and the vegetable based fed- batch fermentation (PBFT57). Table 8 summarizes the results. The results demonstrate that there was very low clostripain activity in the case of TSB/Proteose fermentations. In contrast the clostripain activity in the case of the fed-batch PBFT58 was very high.
Table 8 Enzymatic activities of post-dialyzed samples
Figure imgf000051_0002
* Clostripain activity determined in the post precipitated / dialyzed sample
Investigation of alternative peptones Screening experiments in shake flask:
In this work various vegetable peptones were used as alternatives to the phytone peptone. The aim was to evaluate their effect on the levels of expression of the collagenases and clostripain. All the peptones tested are derived from vegetable sources and are marketed by Sigma.
The experimental procedure used is described in Figure 28. The media recipes are detailed in Table 9, whereas a list of the peptones used is shown in Table 10. A control shake flask was also conducted, containing phytone peptone. In all cases, 50g/L of yeast extract and lOOg/L of each peptone were used in an effort to mimic the concentrations of these components at the harvest point of the developed fed-batch fermentation (see Table 4).
Table 9 Composition of media used in shake flask experiment. All media were filter sterilised.
Figure imgf000052_0001
The shake flasks were incubated for 18 hours. The cultures were analysed for ODeoonm and viable cell ocunts. The cultures were filtered and the supernatants analysed by SDS PAGE. The results from the ODβoonm measurements and viable cell counts are summarised in Table 10.
Most of the vegetable peptones resulted in higher net OD values compared to the phytone peptone. However the OD values did not correlate to the viable cell counts. This could be partly attributed to the variability of the viable cell count method or to the fact that the cells had already started to lyse before the pre-selected harvest point (18 hours).
Interestingly, the SDS-PAGE gel indicated that there was no expression of collagenase (gel not shown) in all the flasks, including that of the control (phytone peptone). A possible reason for this could be the fact that the concentrations of the phytone peptone and yeast extract used were very high and as a result they repressed the expression of collagenases.
Table 10 Results from 1st screening experiment
Figure imgf000053_0001
Fed-batch fermentations using alternative peptones - DCFT27a,b:
Based on information from the previous shake flasks experiments that no expression of collagenases was observed, it was decided to evaluate the alternative peptones using the developed fed-batch strategy.
Two fed-batch fermentations were conducted, DCFT27a (vegetable extract
2) and DCFT27b (vegetable hydrolyzate 2). In both fermentations the fed-batch strategy that was developed for the media containing phytone peptone was used.
Table 11 describes the media recipes, whereas Figure 29 the strategy used.
Table 11 Media recipe for fed-batch fermentations DCFT27a and DCFT27b
Figure imgf000054_0001
Growth curves:
The growth curves (Net OD6oonm vs. time) for DCFT27a and DCFT27b are depicted in Figure 30. In both fermentations, the cells grew to a slightly higher ODβoonm compared to the media containing phytone peptone (fermentation PBFT57, Figure
16). This was in accordance with the viable cell counts (approximately 2 x 109
CFU/mL for DCFT27a,b compared to 1.5 x 109CFUAnL for PBFT57).
SDS PAGE gels: As with the shake flask experiments the SDS PAGE analysis indicated that there was no expression of collagenases in both DCFT27a and DCFT27b (gels not shown).
This could be attributed to the fact that the media, which consists of high amounts of peptone, supports the expression of collagenases when phytone peptone is used, but is too rich when an alternative peptone is used and thus represses the expression of any metabolite, including collagenase and clostripain. It seems that the cells experience luxurious growth conditions in the media containing the alternative peptones and do not need to produce any proteases. Batch fermentations using alternative peptones — PBFT59a.b,c:
The results from DCFT27a and DCFT27b fed-batch fermentations, led to further work to investigate three additional alternative peptones, however using lower concentrations than previously used.
Three 5L batch fermentations were conducted, PBFT59a (vegetable tryptone), PBFT59b (vegetable extract) and PBFT59c (vegetable extract no.l). The fermentations were harvested after 18 hours.
All peptones were used at concentrations of 50g/L in an effort to mimic the concentration of the proteose peptone in the animal media (Proteose / Peptone) and the concentration of phytone peptone that was used previously. The media recipe is shown in Table 12.
Table 12 Media recipe and fermentation strategy for 5L fermentations PBFT59a,b,c
Figure imgf000055_0001
Growth curves:
The growth curves obtained from PBFT59a,b,c fermentations are depicted in Figure 31. In all cases the cells grew to a lower ODeoonm (between 1.8 and 2.8) compared to the DCFT27 fed-batch fermentations. This was also in accordance with the viable cell counts (between 0.7 x 109CFUAnL to 1.2 x 109 CFU/mL for PBFT59a,b,c compared to 2 x 109 CFU/mL for DCFT27a,b). In the media containing tryptone the cells demonstrated the slowest growth rate and achieved the lowest cell density after 18 hours. SDS PAGE gels: As for the shake flask experiment and the DCFT27a,b fed-batch fermentations no collagenase expression was seen in the SDS PAGE gels (gels not shown).
These results show that the alternative peptones, although they support the cell growth, they do not allow the expression of collagenases. As suggested before this could be due to the fact these peptones are very rich in nutrients, e.g., free amino acids, small peptides. 4th set of fed-batch fermentations - DCFT27d
As the results from the experiments using the alternative vegetable peptones were not successful the next aim of this work was to investigate the possibility of decreasing the levels of clostripain in the developed fed-batch fermentation using the phytone peptone media. As described previously, the clostripain was probably causing the degradation of collagenases during the purification process.
A fed-batch fermentation was carried out using the standard phytone peptone media supplemented with three amino acids, i.e., glutamine, tryptophan and asparagine. This fermentation was performed as the concentrations of these particular amino acids were lower in the phytone peptone compared to the animal TSB/Proteose media, based on the amino acid composition of these components, provided by the manufacturers. The aim here was to investigate whether addition of these amino acids could reduce any nutrient limitation that may be a contributing factor for the expression of clostripain. The media recipe is shown in Table 13. The fermentation strategy used was the standard fed-batch strategy used for DCFT26 and PBFT57 fermentations (see Figure 6).
Table 13 Media recipe for fed-batch fermentation DCFT27d
Figure imgf000057_0001
Growth curve:
The growth curve obtained from DCFT27d fermentation is depicted in Figure 32. The growth profile obtained was very similar to that obtained for the standard fed-batch fermentation in the absence of amino acids (DCFT26b and PBFT57) shown previously. SDS PAGE gel:
Figure 33a shows the SDS PAGE gel of the supernatant samples taken throughout the fermentation. The level of collagenases is similar to that seen for the standard fed-batch fermentation (see Figure 10 for SDS PAGE gel from DCFT26b). Although clostripain is still present in the fermentation, it did seem that its level was lower than that in DCFT26b.
In order to investigate this further, the clostripain activity of the post- dialysed harvest point sample was estimated using the clostripain activity assay. In addition, the clostripain activity of the post-dialysed harvest point sample taken from the 2OL lyophilization batch was also estimated. Since this particular batch was purified without showing significant collagenase degradation, knowledge of its clostripain activity would be informative. Table 14 summarizes the enzymatic activities of the post-dialyzed samples. It also includes the enzymatic activities for the standard fed-batch fermentation PBFT57 and the animal TSB/Proteose peptone presented in Table 8, for comparative purposes.
Table 14 Enzymatic activities of post-dialyzed samples
Figure imgf000058_0001
The results from DCFT27d indicate that the addition of the amino acids reduces the activity of clostripain produced by the strain. The ratio of clostripain to collagenase is approximately four fold lower in the amino acid supplemented fermentation compared to the control fed-batch fermentation. The ratio of clostripain to collagenase in the animal-derived fermentation was ten fold lower than the amino acid supplemented fed-batch fermentation. It is possible that the reduction of clostripain activity may result in significant reduction on the degradation of collagenases during purification.
A series of 5L fermentations were conducted to assess several fed-batch fermentation strategies. The strategies were assessed based on their yield of collagenase, quantity of contaminants and scalability. Based on these results an optimum fed-batch strategy was identified that resulted in a productivity of total collagenases of approximately 280 mg/L. The fermentation strategy was modified by slightly increasing the batch media concentration and reducing the fed-batch media concentration to improve its scalability. This change to the fermentation strategy had no effect on the productivity or levels of contaminants.
The second objective was to optimize the primary recovery step of the collagenases. Optimization of this step involved improvement in the yield of the process step or a reduction in the quantity of contaminants recovered or an increase in scalability. A range of ammonium sulphate concentrations from 100 to 520 g/L were assessed. The effect of lowering the pH to 6.0 and oxygenating the media were also assessed. All ammonium sulphate concentrations below 400g/L showed very low recoveries of collagenase. No difference in the recovery of collagenase or clostripain was observed in any of the ammonium sulphate concentrations between 400 and 520 g/L. The pellet from the 400 g/L precipitation was the easiest to re- suspend and this concentration was therefore defined as the optimum level.
A benchmarking experiment was carried out in order to determine and compare the growth and production of collagenases and clostripain in an animal- derived media with C. histolyticum strains 013 and 004. The animal-derived media recipe was taken from the Process 1 fermentation media, utilizing TSB and protease peptone. This experiment also allowed a comparison of strain 004 grown in animal and non-animal media. The results from SDS-PAGE analysis showed that much lower quantities of clostripain from C. histolyticum grown in the animal -derived media. These results were confirmed using an enzymatic assay for clostripain activity. The assay demonstrated a significant reduction in the activity of clostripain in fermentations using the animal-derived media. When the two strains were compared 004 showed a higher clostripain activity than 013.
Selections of alternative nitrogen sources were assessed for their ability to replace the Phytone peptone in the fed-batch fermentation strategy. These peptones were Vegetable Extract No.2 (Sigma, 49869) and Vegetable Hydrolysate No. 2 (Sigma, 07436). The C. histolyticum grew extremely well on the vegetable peptones reaching optical densities (600nm) of 4 to 5 units. SDS-PAGE analysis of these fermentations showed no expression of either collagenase or clostripain. Due to the luxuriant cell growth observed on these peptones it was thought that the concentration of complex nitrogen source was too high resulting in an inhibition of protease expression. A second set of fermentations was therefore carried out using the alternative peptones at 50 g/L in a batch strategy. Vegetable Tryptone (Sigma, 16922) Vegetable Extract (Sigma, 05138) and Vegetable Extract No. 1 (Sigma, 04316) were used as alternative peptones for these experiments. When the fermentations were analyzed by SDS-PAGE no expression of collagenase or clostripain was seen. A fed-batch fermentation using Phytone peptone was supplemented with three amino acids, glutamine, tryptophan and asparagine. These amino acids were identified as being present in lower amounts in the non-animal media. The growth profile of the fermentation was very similar to that of the fed- batch fermentation without amino acid supplementation. SDS-PAGE analysis showed a similar yield of collagenase but a slightly lower level of clostripain. The clostripain assay showed reduced activity in the amino supplemented when compared to the control fed-batch fermentation. The reduction in clostripain activity whilst still significant was not as great as the difference between animal and non- animal media. Materials and Methods:
Inoculum media for fermentations using vegetable media
Throughout this development work the following recipes for the inoculum media were used. Inoculum media - Vegetable
Figure imgf000060_0001
The media was filter sterilized Inoculation procedure
A vial from the internal cell bank was thawed and 0.025mL was used to inoculate 5mL of the inoculum media in a 3OmL universal. The 5mL culture was incubated at 37°C in an anaerobic jar in the presence of anaerobic gas generators. After approximately 13 to 15 hours of incubation, 4mL of the culture was used to inoculate 20OmL of the inoculum media in a 50OmL flask. As previously the flask was placed in an anaerobic jar in the presence of anaerobic gas generators. After approximately 13 to 15 hours of incubation at 370C and 75rpm, the whole content of the flask was used to inoculate the fermenter. The pH and the temperature of the fermenters were controlled at 7.0 and 370C, respectively. The nitrogen flow rate was set at lL/min (~ 0.2vvm) and the stirrer speed at lOOrpm. The fermenter was sampled at regular time intervals for ODβoonm measurements and viable cell counts. Samples were filtered through a 0.22μm filter. The filtrates were stored at -200C and were frozen at -200C for SDS PAGE analysis. Figure 33b depicts a schematic diagram the inoculation procedure.
A preferred recipe for the fed-batch fermentation is set forth below.
Figure imgf000061_0001
It is also desirable to scale-up the fermentation process further without detracting from the quality or yields of the collagenase products. Thus, the invention further relates to an approximately 200 liter fed batch process as described in the flow chart in Figure 33c. Viable cell counting method
Samples taken from the shake flasks were diluted by a factor of 10"4 to 10'7 and plated out onto TB agar plates. Plates were incubated at 37°C for approximately 48 hours in a Genbox Jar. An Anaerobic Gas Generator Pack was used in order to create anaerobic conditions within the Jar. The number of colonies was then counted. Ammonium Sulphate Precipitation; Materials: Sorvall Evolution centrifuge
Chemicals: Ammonium Sulphate, GPR grade (BDH)
Supernatant samples (10OmL to 50OmL) were filtered through a 0.22μm filter. Depending on the experiment various amounts of ammonium sulphate were added (from 15% to 80% saturation). The solution was mixed slowly in a magnetic stirrer for approximately 15 minutes, until all the ammonium sulphate had dissolved. It was then held without mixing for —3.5 hours at +2-80C. Following the hold step, significant amount of precipitate was formed. The solution was then centrifuged at 7,200 x g for 20 minutes at 40C. The supernatant was decanted and the pellet stored at -2O0C. Dialysis
Materials: 1OkDa MWCO SnakeSkin Dialysis Tubing (68100, Pierce) Magnetic Stirrer
Chemicals: Potassium Dihydrogen Orthophosphate AnalaR (BDH) Water for Injection (WFI) The pellets obtained from a 10OmL ammonium sulphate sample were re- suspended in 3.3mL of WFI. The re-constituted pellet was transferred into a pre- wetted 1OkDa MWCO SnakeSkin dialysis tubing and dialyzed against 10OmM of K2HPO4 (pH 6.7) for -12 to 16 hours at 2-80C. The WFI was then changed and dialysis continued for 2 to 4 hours. The dialyzed material was recovered and the volume determined. The post-dialyzed sample was stored at -2O0C. SDS-PAGE Analysis (8% Tris-Glvcine eels') Materials: Xcell SureLock Mini-Cell Chemicals:
SDS-PAGE Standards High Molecular Weight (161-0303, Bio Rad) Novex 8% Tris-Glycine gels, 1.5mm, 10 well (EC6018BOX, Invitrogen) Novex 8% Tris-Glycine gels, 1.5mm, 15 well (EC60185BOX, Invitrogen) Novex Tris-Glycine SDS Running Buffer ( 1 Ox) (LC2675, Invitrogen) Novex Tris-Glycine SDS Sample Buffer (2x) (LC2676, Invitrogen) NuPAGE Sample Reducing Agent (1 Ox) (NP0009, Invitrogen) Collodial Blue Staining kit (LC6025, Invitrogen) Ethylenediaminetetra-acetic acid disodium salt Analar R (BDH) Samples were prepared for reducing SDS-PAGE by adding 1 Oμl of sample to lOμl sample Buffer (2x), 2.5μl reducing agent (1 Ox) and 2μl of 0. IM EDTA (to achieve final concentration of 1OmM). The high molecular weight (HMW) marker was prepared by adding lOμl of concentrated stock to 80μl reducing agent (1 Ox), 31 Oμl WFI and 400μl sample buffer (2x). The diluted HMW standard was then heated at 950C for 5 minutes before aliquoting and storage at -2O0C for use in subsequent gels. Samples (15μl) containing collagenases were run directly (i.e. with no prior heat treatment) on 8% Tris-Glycine gels using Tris-Glycine running buffer at 130V for -lhour 50mϊns. After electrophoresis, the gels were stained with colloidal blue stain reagent as per the manufacturer's instructions. Purification Process
Method summary for 5L process of purification:
Step 1. Ammonium sulfate precipitation of culture media supernatant
(secreted protein).
Reconstitution and dialysis into 0.1 M potassium phosphate, 0.1M arginine pH6.7.
Step 2. Hvdroxyapatite chromatography (in presence of 200μM leupeptin)
Elute with 0-100% gradient of 0.264M potassium phosphate pH6.7 over 4 CV.
Pool 2 Iate-eluting peaks where A2so > A26o, load straight onto TMAE Step 3. Fractogel TMAE ion exchange (in presence of 200μM leupeptin)
Nucleic acid removal (a Pall Mustang Q filter can also be used) Collect and pool unbound flowthrough. Step 4. Dialysis into 1OmM Tris pH8.0
Step 5. O Sepharose HP ion exchange (in presence of 200μM leupeptirO
Separates AUXI from AUXII
Elute with 0-40% gradient of 1OmM Tris, 3mM CaCl2, 36OmM NaCl pH8.0 over 20 CV
2 peaks collected: Peak 1 = AUXII Peak 2 = AUXI
Arginine added to 0.1 M to AUXI and AUXII containing fractions Step 6. AUXI and AUXII pools concentrated by pressurized stirred-cell Step 7. Superdex 75 Gel Filtration
Removal of clostripain and gelatinase from AUXI and AUXII AUXI and AUXII run individually on separate columns. Samples loaded at 5% CV
Buffer: 1OmM Tris, 3mM CaCl2, 15OmM NaCl, 0.1 M Arginine pH8 Step8. The AUXI and AUXII are pooled and concentrated individually, diafiltered into water and then pooled to form the final drug product.
Column details:
Table 15. Column s ecifications for 5L rocess
Figure imgf000064_0001
Column Packing
• Columns were packed as manufacturer's instructions where possible.
• TMAE column - no issues were encountered.
• Q Sepharose and Superdex 75 - difficulties were encountered in packing to correct pressure due to size of the column. However, the columns could be run at the recommended pressure.
• HA — packed as a 50% slurry and run at 1 OmL/min. Yields / recoveries from 5L process:
Figure imgf000065_0001
Table 17: Purification from Q-Sepharose IEX to post Superdex 75 GPC.
Figure imgf000066_0001
Yields from a 5L process are approximately 60-75mg each of ABCI and ABCII
For the scale up, depending on fermentation, yields of 250-300mg for 2OL and 2500-
3000mg for 200L could be expected.
Individual Chromatography steps of 5L scale process:
Hydroxyapatite chromatography
Column size: 2 x 30OmL in XK50/30 (15cm bed height each) Buffer A: 0. IM potassium phosphate, 200μM leupeptin, pH6.7 Buffer B: 0.264M potassium phosphate, 200μM leupeptin, pH6.7 Sample: ~350mL (in 0.1 M potassium phosphate, 0.1 M Arginine pH6.7) loaded at <1.0mg/mL media*
Flow rate: 9.8 mL/min Elution: 0-100% B over 4 CV Figure 34 shows a chromatogram after hydroxyapatite with a loading of 1.0 mg/L media, wherein a considerable loss of resolution and target degradation occurs. Fractogel TMAE anion exchange
Column size: 58mL in XK26/20 (10cm bed height) Buffer A: 1OmM Potassium Phosphate, 0.2M NaCl, 200μM leupeptin, pH6.7
Buffer B: 1OmM Potassium Phosphate, 2M NaCl, pH6.7
Sample: ~650mL @ 0.5mg/mL (in Potassium Phosphate pH6.7, straight from HA column) loaded at ~5.5mg/mL media Flow rate: 8.8 mL/min
Elution: (100% B to elute nucleic acid)
Figure 35 illustrates a chromatogram after Fractogel TMAE anion exchange. The unbound fraction pooled to give ~650mL at 0.5mg/mL. Dialysed into 1OmM Tris at pH8. Figure 36 shows a SDS-PAGE gel of Pre HA, Post HA and Post TMAE material from 5L scale process. The gel is stained wth Colloidal blue. O Sepharose HP anion exchange with original elution gradient Column size: 10OmL in XK50/20 (5.0cm bed height)
Buffer A: 1 OmM Tris, 3mM CaCl2, 200μM leupeptin, pH8.0 Buffer B: 1OmM Tris, 3mM CaCl2, 36OmM NaCl, 200μM leupeptin, pH8.0 Sample: ~650mL at 0.5mg/mL (in 1OmM Tris, pH8.0 + 200μM leupeptin) loaded at ~3.0mg/mL media Flow rate: 18.0 mL/min Elution: 0-40% B over 20 CV
Figure 37 illustrates a chromatogram after Q Sepharose HP anion exchange with original elution gradient. Arginine is added to 0.1 M to ABCI and ABCII containing fractions. Peak 1 fraction (ABCII) pooled to give ~220mL at 0.55mg/mL which was concentrated by stirred-cell to give ~45mL at 2.8mg/mL. Peak 2 fractions (ABCI5 excluding gelatinase shoulder) pooled to give ~19OmL at
O^mg/mL, which was concentrated by stirred-cell to give ~42mL at 2mg/mL. Figure 38 shows a SDS-PAGE gel of Q Sepharose IEX chromatography of post TMAE material run in the presence of leupeptin for Peak 1 (ABCII). The gel is stained wth Colloidal blue.
Figure 39 shows a SDS-PAGE gel of Q Sepharose IEX chromatography of post TMAE material run in the presence of leupeptin for Peak 2 (ABCl). The gel is stained wth Colloidal blue.
O Sepharose HP anion exchange with modified gradient
Small scale test of NaCl addition to Buffer A and using a steeper/faster gradient. Sample was from a 1/3 5L process, post TMAE, previously frozen (-200C). Column size: ImL
Buffer A: 1 OmM Tris, 3OmM NaCl, 3mM CaCl2, 200μM leupeptin, pH8.0 Buffer B: 1 OmM Tris, 3mM CaCl2, 36OmM NaCl, 200μM leupeptin, ρH8.0 Sample: 3mg post TMAE, post dialysis into 1 OmM Tris, 3OmM NaCl,
200μM leupeptin, pH 8.0. Loaded at 3mg/mL media
Gradient: 0-25% B over 2CV, 25% B for 2CV, 25-40% B over 7.5CV
Figure 40 illustrates a chromatogram after Q Sepharose HP anion exchange with modified elution gradient. Good separation of ABCI and ABCII is observed. The second part of the gradient can be made steeper to sharpen ABCI peak.
Improvement of the peak can also be made using 5mL CV loaded at 3 and 1 Omg/mL media.
Superdex 75 Gel Permeation chromatography of ABCII (Peak 1 from IEX) Column size: 88OmL in XK50/60 (54cm bed height) Buffer; 1OmM Tris, 3mM CaCl2, 15OmM NaCl, 0.1 M arginine, pH8.0
Sample: ~44mL (5% CV) at 2.5mg/mL (in 1OmM Tris, 3mM CaCl2,
~60mM NaCl, 0.1M arginine, pH8.0) Flow rate: 8.8 mL/min
Figure 41 illustrates a chromatogram after superdex 75 gel permeation chromatography of ABCII (Peak 1 from IEX). Peak pooled to give ~60rnL ABC II at 1.2mg/mL. Figure 42 shows a SDS-PAGE gel of superdex 75 gel permeation chromatography of concentrated ABC II run in the presence of arginine. The gel is stained wth Colloidal blue.
Superdex 75 Gel Permeation chromatography of ABCI (Peak 2 from IEX): Column size: 88OmL in XK50/60 (54cm bed height)
Buffer: 1OmM Tris, 3mM CaCl2, 15OmM NaCl, 0.1 M arginine, pH8.0
Sample: ~42mL (5% CV) at 2.0mg/mL (in 1OmM Tris, 3mM CaCl2,
~60mM NaCl, 0.1M arginine, pH8.0) Flow rate: 8.8 mL/min
Figure 43 illustrates a chromatogram after superdex 75 gel permeation chromatography of ABCI (Peak 2 from IEX). Peak pooled to give ~60mL ABC I at l.lmg/mL.
Figure 44 shows a SDS-PAGE gel of superdex 75 gel permeation chromatography of concentrated ABC I run in the presence of arginine. The gel is stained wth Colloidal blue. Scale up column sizing
Table 18
Figure imgf000069_0001
Figure imgf000070_0001
* Column type and resulting bed height to be further optimized. Media volumes are linear scale up from 5L scale.
Figure 44b illustrate a 5L purification process flow scheme.
In yet other embodiments of the invention, the dialysis steps of the purification process described above can be substituted with ultrafiltration/diafϊltratϊon (UF/DF) operations using dialysis and stirred cells will be replaced by TFF, tangential flow filtration. The TMAE step discussed above is optional.
The invention includes the collagenase products that are produced by (or can be produced by) the above purification processes. Such collagenase products possess exceptional high degrees of purity and retained enzymatic activity. For example, the compositions are free of clostripain (e.g., possess negligible or undetectable levels of clostripain). Optimization of the Manufacturing Process:
In order to support clinical studies and provide a commercial-scale process, optimization of the manufacturing process earlier developed was completed. The process changes are described briefly below, and are outlined in Table 19. Table 19: Summary of Process Changes between BTC (Process 1) and Auxilium Supplies (Process 2 and 3)
Figure imgf000071_0001
Fermentation Optimization
Removal of the bovine-derived raw materials from the original cell bank and fermentation process was carried out. Strain 004 of Clostridium histolyticum was propagated for use as the master cell bank based on passage viability required for scale-up. The specifications and analytical results for the master cell bank are captured in Table 20. In order to increase bϊomass and production of collagenase, a fed-batch fermentation strategy was developed utilizing animal-free raw materials in the growth medium at a 20 Liter fermentation scale. Further fermentation scale-up to 200 Liter was observed to require the use of a porcine-derived media component (i.e., Proteose Peptone #3, infra) to assure consistent cell growth, collagenase expression, and an improved impurity profile. Subsequent changes were made to increase the yield and purity of collagenase over the downstream process. These changes include the addition of new separation and filtration strategies, as well as scale-up of the production equipment to support the 200 Liter batch fermentation scale. Figure 45 depicts a flow chart of the fermentation for process 3.
Table 20: Analytical Specifications and Test Results for Master Cell Bank
Figure imgf000072_0001
Primary Recovery and Purification Optimization
Further development to optimize the primary recovery and downstream purification process is being undertaken. Substitution of the ammonium sulfate precipitation with phenyl sepharose fast flow low sub column chromatography to capture the collagenases has been implemented to improve yields, eliminate the use of bulk ammonium sulfate and to improve aseptic processing.
With regards to purification, the Pall Mustang Q filter has been implemented for residual DNA and impurity clearance to further enhance yields and simplify the production process train and validation requirements. The Quaternary Amine Sepharose High Performance (Q HP) operating parameters have been optimized to eliminate the Gel Permeation Chromatography (GPC) step. In addition to the process changes cited above, the drug substance formulation has been modified to include 10 mM Tris, 60 mM Sucrose, pH 8.0, improving both product solubility and drug substance and drug product stability. The optimization process took place in two stages. The initial process
(Process 2) utilizes an animal-free medium for all cell banking and fermentation stages with the fed-batch fermentation performed at the 20 Liter scale. The downstream process has been adapted from Process 1 to include Mustang Q filtration for residual DNA removal and Superdex 75 GPC for additional host cell contaminant clearance. Leupeptin has also been added to the chromatography buffer systems to prevent proteolytic degradation. Process 2 material has been bridged analytically with Process 1 material (Table 21 A), and was tested in a side-by-side pre-clinical study outlined herein. Process 2 material has been proposed for use in the early stage of the Phase 3 clinical program. The specifications for Process 2 intermediates and drug substance are detailed in Tables 22 and 23 respectively.
Further process, formulation and lyophilization development provided an optimized manufacturing process (Process 3). These changes include the addition of new separation and filtration strategies, as well as scale-up of the production equipment to support the 200 Liter batch fermentation scale as outlined in Table 19. Figure 46 depicts a flow chart of the purification for process 3.
Declaration of dose: The initial in vitro potency assay was a bovine collagenase assay and did not differentiate collagenase types I and II. This assay was utilized for the material used in the open label, DUPYlOl and DUPY 202 clinical studies only, with the 0.58 mg dose typically resulting in a potency of 10,000 Units. Analysis of Process 1 material utilizing the current separate in vitro potency assays for type I collagenase and type II collagenase typically results in 1,700 to 3,500 Units/dose (0.58 mg dose) for type I collagenase and 43,000 to 69,000 Units/dose (0.58 mg dose) for type II collagenase. Analysis of Process 2 material utilizing the current in vitro potency assays has confirmed that similar relative potency values compared to Process 1 material are typically achieved. Demonstration of analytical comparability between Process 1 and Process 2: In order to support the changes between Process 1 and Process 2, comparability data have been submitted in the form of release testing and analytical characterization. These data are presented in Table 21.
Comparison of the intermediates, described as AUX-I and AUX-II, and drug substance from the previous process (Process 1; Reference) with a process of the invention (Process 2). This analytical comparison shows that material manufactured from Process 2 is comparable to that made with Process 1 (Table 21). In particular, the identity, potency and purity between these materials are comparable.
The purity level of Process 2 intermediates is shown in Fig. 47, a reduced SDS-PAGE Coomasie stained gel. The gel shows a single band for each intermediate with no other minor bands evident. AUX-I has an apparent MW of 1 15 IeDa and compares with the reference (ABC I), while AUX-II has an apparent MW of 110 IeDa and compares with the reference (ABC II). Fig. 48 shows a reduced SDS-PAGE Coomasie stained gel depicting drug substance. As with the intermediates, drug substance manufactured by Process 2 compares with the reference (Process 1). A silver stained SDS-PAGE gel is depicted in Fig. 49 further substantiating the high purity level of the Process 2 drug substance. In summary, the release testing and analytical characterization for the intermediates (AUX-I and AUX-II) and drug substance manufactured using Process 2 clearly demonstrates comparability with Process 1 (Reference) materials. Additionally, further release testing was performed on Process 2 material and is listed in Table 2 IB. In conclusion, the direct analytical comparison between Process 1 and Process 2 materials (Table 21), and the further intermediate and release testing (Table 22) indicate that Process 2 material is suitable for use in the human studies. Tables 23 and 24 further list the analytical specifications resulting from Process 2 manufacturing process.
Table 21: Analytical comparability between (Process 1) and Auxilium (Process 2) intermediates and drug substance.
Figure imgf000075_0001
Figure imgf000076_0001
* Process 1 preliminary specifications not included here
**Drug Substance not available for these tests, limited supplies on hand
***N-terminal sequencing completed for AUX-I (identical to reference), but further development required for AUX-II as N-terminus appears to be blocked.
Table 22: Analytical results for Process 2 intermediates and drug substance
Figure imgf000076_0002
♦Result is at the LOQ of the previous residual DNA method Table 23: Analytical Specifications for Process 2 AUX-I and AUX-II Intermediates
Figure imgf000076_0003
Figure imgf000077_0001
Table 24: Analytical Specifications for Process 2 Drug Substance
Figure imgf000077_0002
Figure imgf000078_0001
DETAILED EXPERIMENTAL FORPROCESS 3: PROCESS 3 FERMENTATION: The fermentation process using Phytone peptone employed during Process 2 had shown significant variability during both supplies for DSP development and GMP manufacture.
During previous work an animal derived Proteose Peptone had been shown to support the growth of C. histolyticum very well. The animal derived Proteose Peptone culture produced significantly less clostripain than observed during Process 2 and expressed AUXI and AUXII at a 1:1 ratio. As a result a regulatory acceptable animal derived peptone, Proteose Peptone #3 from Becton Dickinson (PP3), was evaluated in 5L fermenters. Initial comparison to the existing Phytone based process (Process 2) showed that using the PP3 at 50g/L generated a high biomass concentration with a rapid exponential growth rate. The fermentation resulted in a higher product yield of >350mg/L total collagenase opposed to ~230mg/L from Process 2 (by semi quantitative SDS-PAGE analysis). Further fermentations using PP3 demonstrated that significantly less clostripain was produced using the animal derived fermentation medium. The first three fermentations (using one batch of PP3) demonstrated very consistent growth profiles. When the product was analysed by SDS-PAGE the yield and purity of collagenase was found to be very reproducible between the three fermentations.
To supply DSP with material for process development several fermentations were conducted using PP3. For this supply material three different batches of PP3 were used. It was noted that when two of these batches were used the growth profiles of the cultivations were not consistent with previous PP3 fermentations and demonstrated variability in the growth profile between fermentations. A small scale investigation showed that batch to batch variability in the PP3 caused this variation. The small scale study also demonstrated that an increase in the PP3 concentration to 100g/L would prevent this variation.
Two 5L fermentations were conducted with 100g/L PP3 using two batches of the peptone, one that resulted in the typical growth profile and one which did not (as demonstrated during the small scale experiment). The experiment showed that the increase in concentration ensured that the two fermentations with different batches of PP3 were reproducible. The growth profiles were highly similar and the product was expressed at a similar yield and purity.
The optimized fermentation process utilizing 100g/L PP3 was finally scaled to 200L. The 200L growth profile was very similar to that seen at 5L scale. SDS- PAGE analysis of the fermentation filtrate showed a high yield from the 200L fermentation, ~320mg/L total collagenase (by quantitative densitometry analysis). The purity of the collagenase product (post fermentation) was similar at both 5L and 200L scale.2OL of the 200L fermentation filtrate was processed by the DSP group to represent a partial scale-up for the downstream process {infra).
The Proteose Peptone #3 fermentation process (Process 3) generated collagenase with a higher yield and with less clostripain than the existing Phytone process. At lOOg/L PP3 was shown to yield C. histofyticum cultivations with reproducible growth curves despite using various batches of PP3. Both the yield and purity of collagenase were also shown to be reproducible when using various lots of PP3. Evaluation of Proteose Peptone #3 as a raw material for production of collagenase from Clostridium histofyticum.
Due to the variability observed in fermentations utilising Phytone peptone as a complex nitrogen source the suitability of Proteose Peptone #3 (Becton Dickinson, 212230) (PP3) was evaluated in 5L fermentations. A simple batch strategy with 50g/L PP3 was used. The exact medium composition can be found in the materials and methods section. Figure 51 compares the growth curve of the 50g/L PP3 (a lower . concentration than the Phytone concentration in Process 2) fermentation to the Phytone fed-batch fermentation. The PP3 cultivation demonstrates a very rapid specific growth rate during exponential growth before entering stationary phase approximately 8 hours after inoculation. The PP3 fermentation reached a maximum optical density (600nm) of 4.7 units. The culture was left for a further 12 hours in stationary phase to monitor product formation / degradation.
Figure 52 shows SDS-PAGE semi-quantitative analysis of the concentration of the collagenase products from the 20 hour point of the PP3 cultivation. Figure 53 shows the same analysis for the Phytone fed-batch process. It can be observed that the PP3 fermentation generates more product than the Phytone based process (an increase from 230mg/L to 360mg/L total collagenase, based on the semi-quantitative analysis in figures 52 and 53). The PP3 culture also expressed AUXI and AUXII at a 1 :1 ratio, whereas the Process 2 produced the two proteins at a 1:1.6 ratio. Reproducibility of Proteose Peptone #3 batch fermentation.
The reproducibility of the PP3 batch process was further examined using lot # 5354796 of Proteose Peptone #3. All three runs illustrated in figure 54 demonstrate consistent growth profiles with a maximal optical density (600nm) of approximately 4.5 obtained after 8 hours. Semi-quantitative SDS-PAGE analysis of the harvest points of the fermentation showed that yield of total collagenase to be ~ 350 — 400mg/L.
The harvest point of the fermentation was also evaluated during this study. The fermentations were harvested at 8, 11 and 20 hours. Figure 55 and 56 show SDS-PAGE analysis of the time course of PP3 fermentation GCFT05d (harvested at 11 hours). The gel depicted in figure 55 has been stained with colloidal blue and the gel in figure 56 has been silver stained. A third higher molecular weight band can be observed above the two collagenase bands on the gels in figures 55 and 56. It is thought that this band corresponds to an AUXI precursor protein reported in the literature. The precursor band is present during the exponential growth phase. At the end of exponential growth the precursor band decreases in intensity and is not present after 11 hours (in GCFT05d). The main lower molecular weight contaminants can be seen on the silver stained gel at approximately 90, 60, 55, 45 and 40 kDa. It must be noted that these contaminants are present at a low level and are only clearly detected on the silver stained gel. The optimal harvest point for the fermentation was determined to be ~ 11 hours at this stage of development. Figure 57 shows SDS-PAGE analysis of samples from the time course of a standard Phytone fed-batch fermentation. A 40 kDa contaminant can be observed on the gel in figure 57. This 40 kDa contaminant band from the Phytone fed-batch process was identified as the protease clostripain. By comparing the gels in figure 55 and 57 it is possible to determine that the quantity of clostripain produced using the PP3 fermentation process is significantly lower than the Phytone based fermentation. Generation of supply material for Downstream Process Development
To support downstream process (DSP) development several fermentations were conducted using 50g/L PP3. During these fermentations two different lots of PP3 were used (5332398 and 5325635). Figure 58 depicts the growth curves of these fermentations (shown in diamond) compared to a fermentation (shown in square) using lot # 5354796 (GCFT05d). The fermentations with the new batches of PP3 display highly varied growth profiles. Although the initial growth rates of the cultures are all very similar, the point at which they enter stationary phase and therefore the maximum biomass concentrations differ considerably. The optical densities (600nm) in the inoculum cultures showed very little variation (OD600 of 5mL stage; 2.9 - 3.6 units, OD600 of 20OmL stage; 4.5 - 5.9 units) and no reduction from previous inocula using PP3 lot # 5354796. The variation and reduced optical density (600nm) only manifested itself in the final (fermentation) stage of the cultivation. This suggests that reason for the variation was a nutrient limitation in the PP3 and the quantity of the limiting nutrient varied between batches of PP3. Although these fermentations were successfully used for DSP development and SDS-PAGE analysis showed that there was not a huge variation in the quantity of collagenase produced (350 - 400 mg/L total collagenase based on semiquantitative SDS-PAGE analysis, data not shown) it was decided that it was still critical to investigate the reason for the variation. The variation in the growth profile would make it very difficult to predict a harvest point of the fermentation. There were also concerns that nutrient limitation may induce expression of other proteases as seen with the Phytone fed-batch process and specifically the protease, clostripain. Investigation into the variation between batches of Proteose Peptone #3.
Initial work with PP3 had demonstrated a highly robust process with a higher product yield and lower levels of the protease clostripain. When new batches of PP3 were employed it was observed that the process robustness decreased significantly with highly variable growth profiles. A shake flask experiment was conducted to directly compare the three batches of PP3 used so far (lots 5354796, 5325635 and 5332398). The experiment replicated the two stage inoculum process from the 5L process but replaced the final fermentation phase with another 20OmL culture. Having this third stage was critical, as the variation was only observed in the final fermentation stage of the process in previous experiments. The optical densities
(600nm) of the cultures were measured at each transfer stage and the cultures were used to inoculate the next stage. Media was prepared using the three batches of PP3 at 50g/L. One of the two batches that had resulted in lower biomass concentrations of C. histolyticum during 5L experiments (lot# 5332398) was also prepared at 100g/L.
Figure 59 shows the results from the small scale experiment. It can be observed that lot 5325635 and 5332398 showed reduced optical densities (600nm) in the third stage of approximately 2.5 units, these were deemed to be "poor" batches of PP3. Lot 5354796 maintains an optical density (600nm) of 5 units in the third stage of cultivation, this was deemed to be a "good" batch of PP3. Interestingly when the concentration of a "poor" batch of PP3 (5332398) was increased to 100g/L the same optical density (600nm) was achieved in the second and third stage of the cultivation. This data does support the theory that the deviations in growth profiles are caused by variation in the quantity of a limiting nutrient between batches of PP3. It was not possible to identify this nutrient by analytical testing of the batches of PP3. Evaluation of Proteose Peptone #3 at lOOg/L in 5L fermentation
The results of the small scale study demonstrated that increasing the concentration of PP3 from 50 to 100g/L removed the issue of batch to batch variability. This process change was tested at 5L scale using a "good" and "poor" batch of PP3 (lot 5354796 and 5325635, respectively) as determined during the small scale investigation into PP3 variability. Figure 60 shows the growth profiles of the two fermentations. The two cultures show identical specific growth rates during the exponential phase. The fermentation enter stationary phase and reach very similar maximal optical densities (600nm) of approximately 6.5 units. This data demonstrates that increasing the concentration of PP3 alleviates the issue of batch to batch variability of the PP3. Due to the higher biomass concentration achieved and longer exponential phase in the fermentation harvest point was extended to 12 hours.
Figures 61 and 62 show SDS-PAGE analysis of the two fermentations utilising lOOg/L PP3. The gels demonstrate consistent expression of collagenase in both fermentations. The samples from both fermentations appear to contain similar levels of contaminant described in figure 56, although PBFT70d appears contain slightly more of the 4OkDa band (clostripain). It is possible that these small differences are due to staining or loading differences. Again the quantity of clostripain produced using the PP3 process is significantly lower than the Phytone process. The precursor band appears to persist longer into the time course of the fermentation. It was recommended that future fermentations at 100g/L should be extended to a 14 hour harvest.
The presence of the precursor band highlights the importance of the harvest point definition and its qualification during process validation.
Figure 63 displays data from densitometry analysis of the gel in figure 61. The chart compares product and precursor formation (densitometry peak area) to cell growth (OD600). Product formation appears to be consistent with cell growth and the rate of production decreases as the cultivation enters stationary phase. The precursor band decreases in intensity as exponential growth ends but is still present at the harvest point of the fermentation. Scale-up of lOθg/L Proteose Peptone #3 fermentation to 200L.
Following the increase in the PP3 concentration to 100g/L the process was scaled to 200L. To generate the required quantity of inoculum for the 200L vessel a third inoculum stage was introduced using a 15L working volume fermenter. 3 x 20OmL cultures were used to inoculate the 15L fermenter and following 12 hours of growth 8L of the 15L were inoculated into the 200L vessel. Figure 64 compares the growth curve of the 200L fermentation to the two 5L fermentation using 100g/L PP3. As recommended the growth profile was extended to 14 hours to ensure that the precursor band had completely disappeared before processing began. The growth profile of the 200L fermentation is very similar to the fermentation at 5L scale, demonstrating successful scale up of the cultivation.
Figure 65 shows SDS-PAGE analysis of the time course of the 200L fermentation. The gel shows product formation during the course of the fermentation. The material at the 14 hour harvest point contains no detectable precursor and very low levels of contaminants. The product generated from the 200L fermentation appears very similar to that produced from the 5L process, indicating that the increased generation number of the 200L process has not had a detrimental effect. Figure 66 displays data from densitometry analysis of the gel in figure 64.
The chart compares product and precursor formation (densitometry peak area) to cell growth (OD600). Product formation appears to be consistent with cell growth and the rate of production decreases as the cultivation enters stationary phase. The precursor band decreases in intensity as exponential growth ends. The precursor band decreases in intensity more rapidly in the 200L fermentation than the 5L cultivation, PBFT70c (figure 63). Figure 67 shows SDS-PAGE analysis using a 4- 12% Bis-Tris gel on the 200L fermentation time course. The approximate molecular weights of the detected contaminants are annotated on the gel.
The harvest process (clarification by filtration) developed for Process 2 was evaluated during the 200L scale up fermentation. The cell culture was successfully clarified using the existing process with no blockage of the filter train. The harvest process is described in the materials and methods section.2OL of filtrate from the 200L fermentation was processed by DSP to demonstrate a partial scale up of the downstream Process 3 (infra). Quantification of product yield by Densitometry analysis
A more accurate and quantifiable method was required to determine product concentration during the upstream process step than the semi-quantitative SDS- PAGE analysis (figures 62 and 63). The fermentation filtrate has a high quantity of pigment and peptides from the growth medium that makes standard protein quantification techniques such as UV and the Bradford assay unusable. The semiquantitative analysis carried out previously was modified and updated by carrying out densitometry analysis of the Coomassie stained gels. The method involved loading a range of quantities (0.2 - 1.2μg / lane) of mixed AUXI and AUXII reference material and dilutions of the sample to be quantified onto a Tris Glycine gel. The scanned image was then analysed and the peak area for estimated for the standards and the samples. A standard curve was then constructed (total collagenase) and used to quantify the amount of total collagenase in the sample dilutions. Figure 68 shows an example of a collagenase standard curve and highlights the linearity of the quantification method within the anticipated range of the samples. The Tris Glycine gels did not completely resolve AUXI and AUXII therefore the total collagenase was quantified rather than attempting to separately quantitate the two proteins.
The quantity of collagenase was analysed for PBFT70c, PBFT70d and the 200L scale-up fermentations. The quantity was found to be —280 — 350 mg/L total collagenase for all three fermentations. Materials and Methods Media preparation: 1 L media preparation
The phosphates for the inoculum preparation (table 25) were autoclaved in a IL bottle at 1210C for 20 minutes. The bulk media (table 26) was initially heated in a microwave to 600C to fully dissolve components before autoclaving in a IL bottle at 121°C for 20 minutes. The PSA 1 (table 27) was filtered through a 0.2 μm Sartopore 2 150cm2 filter into a 25OmL sterile bottle. The 30OmL autoclaved phosphates, 60OmL autoclaved bulk media and 10OmL sterile filtered PSA 1 were pooled before aliquoting into 3OmL gamma irradiated universale (8*5rnL) and 50OmL Erlenmeyer flasks (4χ200mL). Table 25: Phosphate composition for inoculum preparation
Figure imgf000085_0001
Table 26: Bulk medium composition for inoculum preparation
Figure imgf000086_0001
"Medium recipe includes PP3 at 50 and lOOg/L.
Table 27: PSA 1 Magnesium/Glucose composition for inoculum preparation
Figure imgf000086_0002
Table 28: Vitamin solution for inoculum preparation
Figure imgf000086_0003
5L media preparation The phosphate solution for the 5L scale (table 29) was autoclaved in a IL bottle at 1210C for 20 minutes. The bulk medium (table 30) was added directly to the 5 L vessel and autoclaved at 1210C for 20 minutes. The PSA 1 (table 31) was filtered through a 0.2 μm Sartopore 2 150cm2 filter into a 50OmL sterile bottle. The 25OmL phosphate solution and 20OmL PSA 1 was separately pumped into the 5L vessel on completion of autoclaving and cooling of the vessel.
Table 29: Phosphate composition for 5L fermentation
Figure imgf000086_0004
Table 30: Bulk medium composition for 5L fermentation
Figure imgf000087_0001
*Mediτuu recipe includes PP3 at 50 and lOOg/L.
Table 31: PSA 1 Magnesium/Glucose composition for 5L fermentation
Figure imgf000087_0002
Table 32: Vitamin solution for 5L fermentation
Figure imgf000087_0003
15L media preparation The phosphate solution (table 33) was filtered through a 0.2μm Sartopore 2
300cm2 filter into a sterile 2L bottle. The bulk medium (table 34) was added directly to the 2OL vessel prior to Steam -In -Place (SIP) sterilisation of the vessel. The PSA 1 (table 35) was filtered through a 0.2μm Sartopore 2 300cm2 filter into a IL sterile bottle. The 75OmL phosphates and 60OmL PSA 1 were separately pumped into the 2OL vessel on completion of SIP and cooling of the vessel.
Table 33: Phosphate composition for 15L fermentation
Figure imgf000087_0004
Table 34: Bulk medium composition for 15L fermentation
Figure imgf000088_0003
Table 35: PSA 1 Magnesium/Glucose composition for 15L fermentation
Figure imgf000088_0001
Table 36: Vitamin solution for 15L fermentation
Figure imgf000088_0002
200L media preparation
The phosphate solution (table 37) was filtered through a 0.2 μm Sartopore 2 300cm2 filter into a Gammasart Biosystem SAlO 1OL bag. The bulk media (table 38) was added directly to the 200L vessel prior to SIP sterilisation of the vessel. The PSA 1 solution (table 39) was filtered through a 0.2μm 300cm2 filter into a Gammasart Biosystem SAlO 1OL bag. The 1OL phosphates and 8L PSA 1 were separately pumped into the 200L vessel on completion of SIP and cooling of the vessel. Table 37: Phosphate composition for 200L fermentation
Figure imgf000089_0001
Table 38: Bulk medium composition for 200L fermentation
Figure imgf000089_0002
Table 39: PSA 1 Magnesium/Glucose composition for 200L fermentation
Figure imgf000089_0003
Table 40: Vitamin solution for 200L fermentation
Figure imgf000089_0004
Fermentation
Figure 69 illustrates overviews of the process flows for the Phytone and PP3 fermentation processes at 5 and 200L scale. 5L scale fermentation
A vial of the WCB (2005#1019D) was thawed and 50μL aliquots were used to binoculate 8x5mL of inoculum media in 3OmL gamma irradiated universals. The 5mL cultures were incubated at 37°C in an anaerobic jar in the presence of 3 anaerobic gas packs. After approximately 12 hours of incubation (OD600 3.0-4.0) 2χ5mL cultures were selected and used to inoculate 2x200mL inoculum media in 50OmL Erlenmeyer flasks. The two flasks were placed together in an anaerobic jar with 3 gas packs and were incubated at 37°C in a shaking incubator (70 rpm) for 12 hours. After 12 hours of incubation (OD600 6.0-7.0) each 20OmL inoculum was used to inoculate a 5L vessel.
The working volume of the 5/7L vessels FT Applikon vessels was 5L of which 4% (v/v) was inoculum from the 200 mL stage. The agitation rate was set at 100 rpm. The pH, dO2 and temperature were controlled at 7.00 units, 0% of saturation and 37°C respectively. The pH was controlled with additions of either HCl (5M) or NaOH (5M). The dO2 concentration was maintained at 0% by continuous sparging of nitrogen, with a flowrate of 1 L/min. Samples were taken during the fermentation and filtered through 0.2μm filters before storing at -200C for analytical purposes. The fermentations began to enter stationary phase at an OD600 of 6.0-7.0. After 12 hours the fermenter was cooled to 10-200C before commencing harvest recovery. 200L scale fermentation
A vial of the WCB (2005#1019D) was thawed and 50μL aliquots were used to inoculate 8><5mL of inoculum media in 3OmL gamma irradiated universale. The 5mL cultures were incubated at 37°C in an anaerobic jar in the presence of 3 anaerobic gas packs. After approximately 12 hours of incubation (OD600 3.0-4.0), 4x5mL cultures were selected and used to inoculate 4χ200mL inoculum media in 50OmL Erlenmeyer flasks. Two flasks were placed together in anaerobic gas jars with 3 gas packs and left to incubate at 37°C in a shaking incubator (70 rpm) for 12 hours. After 12 hours of incubation (OD600 6.0-7.0) three of the four flasks were pooled together and used to inoculate the 20 L vessel.
The working volume of the 2OL vessels was 15L of which 4% (v/v) was inoculum from the 20OmL stage. The agitation rate was set at 100 rpm. The pH, dO2 and temperature were set at 7.00 units, 0% and 37°C respectively. The pH was controlled with additions of either HCl (5M) or NaOH (5M). The dO2 concentration was maintained at 0% by continuous headspace sparging of nitrogen, with a flowrate of 20 L/min. After 12 hours of growth in the 2OL vessel (OD600 6.0-7.0), 8L of culture were used to inoculate the 200L vessel. The running conditions were identical to the 2OL scale. The final optical density (600nm) at harvest was 6.0-7.0. After 14 hours the fermenter was cooled to 10-200C before commencing harvest recovery. Harvest 5 L Harvest
The 5 L cultures were pumped with a flow rate of 5 L/h through a Millistak+ 10" Opticap depth filter (Miϊlipore, KC0HC10FF1) and 0.2μm Sartopore 2 300cm2 filter into sterile 25OmL bio-containers. The processed material was either stored at -200C or stored at 4°C overnight before processing by DSP. 200L Harvest
The 200L harvest was performed using a filtration harvest train. The culture was pumped with a flow rate of 200 L/h through a Milistak+ (MCOHCl OFSl) disposable depth filter with a filtration area of 4x1 m2 followed by two 0.2μm Express Opticap XL 10 filters, 2*0.49m2 (Millipore, KHGESIOTTI). The process time for primary clarification was 1 hour. An additional 10 min was allowed at the end of the harvest to retrieve residual product held up in the filters. The clarified supernatant was collected in a 200L Stedim Palletank with the filtrate weight recorded. 2OL of filtrate was passed through a Mustang Q high affinity DNA column with a flowrate ~6 L/min and collected into two sterile 20 L stedim bags, prior to storage at 4°C overnight. Analysis
Optical Density measurements The spectrophotometer was blanked using PBS at wavelength 600 nm. Fermentation samples were diluted by factors of 10, 20 or 100 (dependent on cell density) using PBS.
ImL of each diluted sample was transferred into a ImL cuvette; the top was sealed and inverted 5 times before recording triplicate optical density readings at a wavelength of 600nm. Tris-Glycine Gels
Fermentation samples were filtered through 0.2μm filters before preparing them for SDS-PAGE analysis. lOμl of filtered sample was added to 1 Oμl sample buffer (2x), 2.5 μl reducing agent (1Ox) and 2μl of 0.1 M EDTA (to achieve final concentration of 1OmM). The high molecular weight (HMW) marker was prepared by adding lOμl of concentrated stock to 80μl reducing agent (1Ox)5 31 Oμl WFI and 400μl sample buffer (2x). The diluted HMW standard was then heated to 95oC for 5 minutes before aliquoting and storage at-20oC for use in subsequent gels. 15μL of fermentation sample and lOμL of HMW marker were run on 8% Tris-Glycine gel using pre-cooled (4°C) Tris-Glycine running buffer at 130V, 400mA and 100 W for ~1 hour and 50 minutes. After electrophoresis, the gels were immersed in 100 mL colloidal blue stain reagent (55mL WFI, 2OmL methanol, 5mL stainer A, 2OmL stainer B) and left to stain for 5 h on an orbital shaker at 60 rpm. Gels were de- stained with 20OmL WFI. The gel was left in WFI for 15-20 h until excess stain was removed after which the gel was scanned and dried according to the manufactures instructions. Bis-Tris Gels
The fermentation samples were prepared for SDS-PAGE analysis by adding lOμl of 0.2μm filtered sample to 4μl sample buffer (4x), 1.5μl reducing agent (1Ox) and 1.7μl of 0.1M EDTA (to achieve final concentration of 1OmM). 15μL of fermentation sample and lOμL of Mark 12 marker were run on a 4-12% Bis-Tris gel and run using MES running buffer at 200V, 400mA and IOOW for ~40mins. After electrophoresis, the gels were immersed in a 10OmL fixing solution (4OmL dH2O, 5OmL methanol, 1OmL acetic acid) for 10 minutes before replacing with a 95mL staining solution (55 mL dH2O, 2OmL methanol, 2OmL stainer A) for a further 10 minutes. 5mL of stainer B was added to the staining solution and the gels were left to stain for 5 h on an orbital shaker at 60 rpm before de-staining with 20OmL WFI. The gel was left in WFI for 15-20 h until excess stain was removed after which the gel was scanned and dried according to the manufactures instructions. PROCESS 3 PURIFICATION:
The first 2OL scale run-through of a newly developed process (Process 3) for the purification of collagenases from Clostridium histolyticum, which was modified from Process 2 performed to GMP at 2OL scale. Significant process changes were introduced in the development of Process 3 in order to make the. purification more robust and more amendable to scale up and subsequent process validation. One significant factor in facilitating this process change was in the choice of fermentation component. Process 2 had been based on the requirement to maintain a phytone based fermentation media whereas for process 3 proteose peptone No. 3 was use. The process run-through is split into the key steps of the down stream purification and the collagenases AUXI and AUXII. These include the treatment of the fermentation filtrate using a Mustang Q capsule, hydrophobic interaction chromatography, tangential flow filtration step 1 (denoted TFFl), anion exchange chromatography and tangential flow filtration step 2 (denoted TFF2). AUXI and AUXII co-purify in the initial steps of the purification and are only separated during the anion exchange chromatography step (performed using Q-Sepharose HP media). AUXI and AUXII are then processed separately and formulated. The intermediates are then mixed in a 1:1 ratio (based on protein content determined by UV) and filtered to form the drug substance. In developing process 3, key steps associated with process 2 were removed. Notably the ammonium sulphate precipitation step, two chromatography steps (hydroxyapaptite and gel permeation chromatography) and all -200C hold steps were eliminated. The use of un-scaleable steps such as stirred cells and dialysis were also removed and replaced with tangential flow filtration (TFF). The issue of product instability, which was evident in process 2 (and eliminated the use of TFF), was not apparent in the 2OL scale run of process 3. The contaminant profile associated with process 3 was however different to process 2 in which clostripain and gelatinase had been major components. Most notably a 4OkDa, 55kDa and two 9OkDa contaminants (one co-purifying with AUXI and the other with AUXII) were detected by SDS-PAGE. As a result of these new contaminants, some of the QC assays (such as RPHPLC and SEC-HPLC) were of limited use since they did not resolve all process 3 impurities. The inability to utilize established QC assays for in-process purity determination, resulted in the need to define a method for establishing which material form the QSepharose column was suitable for further purification. This was required since the contaminants were not clearly resolved from the AUXI and AUXII products on the QSepharose column and it was therefore necessary to collect eluted material in discrete fractions, which could be analyzed retrospectively. Analysis was performed by SDS PAGE and the pooling decision for the 2OL run-through was based on experience of the relative staining intensity of impurity to product using a standardized lμg load.
Retrospective densitometry analysis of SDS-PAGE enabled the pooling criteria to be described based on relative per cent product purity. Further densitometry analysis using material from the 200L demonstration run enabled a standardised method to be established as well as an approximation of assay variation. This led to an agreed procedure for the pooling of in-process fractions to be implemented in the first GMP campaign.
In addition to the process description, preliminary work describing a buffer stability and in-process sample stability study is presented along with initial characterization of some of the impurities associated with Process 3. Process 3 differed from process 2 in three main areas. Firstly, the ammonium sulphate precipitation step and hydroxyapatite chromatography steps were removed; secondly, the gel permeation chromatography (GPC) step was eliminated and thirdly, all buffer exchange steps were performed by tangential flow filtration. The precipitation step was replaced by the use of hydrophobic interaction chromatography (HIC) at the client's recommendation. Development of this step resulted in the successful implementation of HIC for (i) product capture (thereby serving as a concentration step) and (ii) some protein and pigment contaminant removal. The HIC step was also subsequently shown to reduce levels of dsDNA. As a result of the process development program, the introduction of HIC and inclusion of a Mustang Q step removed the need for both the ammonium sulphate precipitation step and the hydroxyapatite chromatography step. The overall effect was to simplify the up front capture of product and to remove a potential hold step associated with Process 2. This latter point had significance in that previously the fermentation could be assessed prior to down stream purification since the pellets resulting from the precipitation step could be held at -200C prior to processing.
Following the HIC step, product was buffer exchanged using tangential flow filtration (TFF). This was performed using 3OkDa molecular weight cut off (MWCO) membranes and replaced the dialysis procedure used for Process 2. Aggregate contamination, which when present was detected as AUXII-derived, appeared to be removed during the anion exchange chromatography step (IEX). As a result, the GPC step was eliminated since both AUXI and AUXII intermediates were within specification for aggregates following IEX. Finally, the final concentration and formulation of the AUXI and AUXII intermediates was performed using TFF instead of the previous method of utilising stirred cells.
Overall, Process 3 represented a simpler process that was more amenable to scale up and validation than Process 2. In addition, the reduction in consumable cost was apparent by the elimination of the need for hydroxyapaptite and gel permeation media and by the reduced number of steps requiring leupeptin. An overview of the purification scheme for Process 3 is given in figure 46. Non-GMP demonstration run at 2OL scale
Process 3 was performed at 2OL scale in the process development laboratories in order to demonstrate if material of suitable quality could be generated using this modified process at 2OL scale. A key requirement for processing was the ability to limit potential protease activity by performing steps chilled wherever possible and by the inclusion of the cysteine protease inhibitor leupeptin at key stages in the procedure. A full 2OL of fermentation filtrate was processed since the feedstock was generated from 200L fermentation PP3. Details of the fermentation and subsequent harvest and filtration are documented in a separate report. Mustang Q treatment of fermentation filtrate
Following 0.2μm filtration, approximately 22L of fermentation supernatant was loaded onto a Mustang Q chromatography capsule as described previously. Some visible pigment contamination (green/brown) appeared to be removed by the Mustang Q capsule during the filtration of the first 1OL since the contents of the first 1OL Stedim bag appeared visibly less pigmented than the second. The ability of the Mustang Q capsule to remove dsDNA was monitored across this step by pico green analysis of pre and post Mustang Q samples (Table 41). In process analysis indicated that unlike previous data generated at small-scale, bulk nucleic acid removal was not evident at the Mustang Q step. The robustness and application of this step therefore requires further investigation. Table 41
Figure imgf000096_0001
Hydrophobic interaction chromatography (HIC)
The use of HIC served three functions in the purification. Firstly, the product was reduced in volume since conditions were identified in which collagenases bound to the resin. Secondly, some pigment and protein contaminant was removed at this stage and thirdly, pico green analysis from this run indicated reduction of dsDNA. The HIC step was performed using supernatant processed directly from the fermentation (after Mustang Q treatment) and, as a result a hold step, (evident in Process 2 as the ammonium sulphate pellet) was no longer present for Process 3. In order to provide conditions for collagenases to bind to the HIC column, product (20L) from the Mustang Q step was diluted with a 3M-ammonium sulphate solution to a final concentration of IM. After filtration, product was loaded onto the column and eluted using a 2-step isocratic elution.
The protein concentration of the HIC load material was difficult to determine accurately and was estimated in two ways. Firstly, a Bradford assay was performed on the material prior to ammonium sulphate addition. This was performed with undiluted material in order to standardise the contribution from pigment present in the fermentation media, which was known to interfere with the assay. Secondly, the estimate was based on volume of fermentation media loaded per mL of column resin. The column load was estimated to be 5.9mg of total protein/mL resin by Bradford assay or alternatively ~13mL of fermentation media per mL of resin. An estimate of the total amount of target protein eluted from the column was determined as 3.4g using UV (see Table 42). Assuming that the total protein present in the HIC load was 9g (Bradford assay), this equated to a 38% recovery. This value was only regarded as a relative measure, however, due to the inaccuracy of the assay for the samples containing fermentation media components. An alternative method for estimating the HIC load concentration was determined using densitometry although it was recognised that this estimation would give a collagenase content rather than estimate of total protein (which could vary between fermentations). Using this approach, the total collagenases were estimated as 360mg/L with an approximate ratio of AUXI to AUXII estimated as 40:60. Using this data, the total collagenase expected in the HIC load would be 7.2g giving a step yield of 47%.
The chromatogram resulting from the HIC step is shown in figure 70. Visible pigment was apparent in the flow-through as well as bound to the column. After washing the column with equilibration buffer to remove the flow-through contamination, peak 1 was eluted using an intermediate concentration ammonium sulphate solution (0.3M).
This peak was shown to contain protein contaminants although some AUXII was also eluted at this stage (figure 71). This loss in product was expected and had been noted previously. In order to minimise the amount of product lost, without compromising purity, the elution volume for peak 1 removal was set at 5 column volumes. Peak 2, containing the majority of the product, was then eluted using buffer with no ammonium sulphate. Peak 2 was collected as a single pool with the chromatography method programmed so that collection began after V* of a column volume of elution buffer had been applied to the column. Collection was then terminated after a total of 4 column volumes had been collected. In order to minimise potential proteolysis in the product at this stage in the process, leupeptin was added to the post HIC eluate and the material held at 2-8°C. The hold time for the post HIC eluate was of 2 day duration. Tangential flow filtration 1 (TFFl)
TFF using 3OkDa membranes was introduced following the HIC in order to reduce the volume of product (5-fold) and to exchange the buffer into conditions suitable for binding to the anion exchange column. Of particular importance was the sufficient reduction in ammonium sulphate such that the conductivity of the IEX load sample was <1.8mS. The diafiltration buffer was chilled and leupeptin added prior to use to reduce the likelihood of proteolysis. No loss in protein was estimated over the course of this step (>100% recovery) although this may reflect the inaccuracy in protein concentration estimation at this stage in the process due to the presence of pigment in the pre TFFl material. Approximately 97.5% of the total protein (3325mg) was recovered in the retentate with an additional 204.8mg recovered in the first membrane rinse {infra). Filtration of the total protein from the combined retentate and rinse was performed at the end of the TFF step prior to holding the material overnight at 2-80C. SDS-PAGE analysis indicated no significant differences were detected before and after the TFF step (figure 71). Q-Sepharose chromatography
The Q-Sepharose column was loaded at a maximum capacity of 5mg total protein per mL resin. As a result, not all of the available material from the TFF step was utilized in this step (see Table 421). The Q-Sepharose column resolved AUXI and AUXII collagenases as expected (figure 72). The start of AUXII elution began at approximately 13.6% B (where buffer A = 1OmM Tris, 0.2mM leupeptin pH 8 and buffer B = Buffer A + 36OmM NaCl) which equated to a post column conductivity of 5.7mS. Fractions (10OmL) were collected throughout the elution of AUXII until the absorbance value dropped to 25% of the peak height (55OmAU). A small peak was eluted at approximately 8mS (20.3% B) following AUXII elution. In-process analysis of this peak from previous small-scale experiments indicated this to be AUXIIderived aggregate material. The start of AUXI elution was at approximately 27% B (which equated to 10.4mS). As before, 10OmL fractions were collected until the absorbance dropped to the required 25% value (19OmAU).
Each AUXI and AUXII fraction collected was analysed by SDS-PAGE and subjected to densitometry (figures 73-76). Densitometry was performed retrospectively, so the decision on fraction pooling was based on experience of the levels of contaminant visible by Colloidal blue staining. In consultation with
Auxilϊum, fractions 6-12 were pooled for the AUXII product and fractions 19-26 pooled for AUXI. The step yields and protein concentrations present in the material pooled from the Q-Sepharose run are included in table 42.
SDS-PAGE analysis of the post IEX AUXI and AUXII products from the 20L demonstration run (figure 77 and 78) showed few contaminants visible by SDSPAGE. In addition, the contaminants detected were in accordance with previous small-scale experiments although there were noted differences in the resolution of the contaminants, which appeared to be more defined (i.e. separate peaks or shoulders) in the small-scale model. These contaminants were also different to those identified for Process 2 in which clostripain and gelatinase had been major components. As a result, the QC protocols developed for Process 2 were not optimised for the detection of the new contaminants associated with Process 3.
Retrospective densitometry of the pooled material estimated the purity at 95.1% for AUXI and 99.4% for AUXII. Currently, however the purity specification of >97% is specified by RP-HPLC and no final product specification has been established using densitometry. Concentration and buffer exchange of A UXI and A UXII
The separated AUXI and AUXII products from the Q Sepharose column were processed separately by TFF using a 3OkDa membrane. This step was required to; (i) remove/reduce leupeptin in the final product (ii) formulate the intermediates into the correct buffer (1 OmM Tris, 6OmM sucrose pH 8) and (iii) to achieve the required target protein concentration of 0.9-1.lmg/mL. A total of 799mg (~683mL at 1.17mg/mL) of AUXII and 860mg (796mL at 1.08mg/mL) of AUXI was concentrated to a target concentration of 1.75mg/mL. This theoretical concentration was based on the calculated reduction in volume required assuming no loss of product during the concentration step. Diafiltration was then performed into the required formulation buffer, the membranes washed with the minimum volume of the TFF system (~250mL) and the full amount combined with the concentrate to achieve the required target concentration of 0.9-1. lmg/mL. A total of 819.5mg AUXII (at 1.03mg/mL) and 797.0mg of AUXI (at 1.09mg/mL) were available after filtration. In both cases, the majority of product was recovered in the retentate and was estimated as 95.4% (762mg) for AUXII and 83.1 % (715mg) for AUXI. The additional material provided by the membrane rinse was estimated as 153mg and 89.6mg for AUXII and AUXI respectively. Mixing of intermediates to drug substance
Approximately 200mg of each intermediate was combined to give 400mg of the drug substance. This was then filtered and approximately 26mg provided to QC for testing. The QC results for AUXI, AUXII intermediates and the drug substance are provided in Table 43. All tests on the drug substance and AUXII intermediate passed the required specification. The test for potency of the intermediate AUXI however, was not within the specified range although all other tests passed. With the exception of the AUXI potency result, these data indicated that Process 3 was capable of generating material of the required specification when purified at the 2OL scale.
As well as QC testing, material from the 2OL demonstration run was utilized for method validation at KBI BioPharma, Inc. At the client's request, 200mg of drug substance was shipped on dry ice to KBI for drug substance and drug product methods validation. The latter testing was performed after lyophilisation of the drug substance at KBI. In addition, 25mg of each intermediate was supplied to KBI for validation of analytical methods.
The individual step yields for the 20L demonstration run are given in table 42. An extrapolation of the data in which all the available material had been loaded onto the Q-Sepharose column indicated that the maximum total amount of available drug substance from this process run-through was 1.6g (assuming no loss of material through retains). This equates to an approximate overall process yield of 17.8% based on the initial estimate of 9g (using the Bradford assay) for the amount of total protein available to load onto the HIC column. With the limitation on the load for the Q-Sepharose column, a maximum of 1.4g of drug substance was available from the current run-through if all the available intermediate had been mixed to form the drug substance.
Figure imgf000101_0001
Table 43
Figure imgf000102_0001
Figure imgf000102_0002
Sample stability study
During the 20L demonstration run, samples were taken at key process points. As the demonstration run was performed as a continuous process (with no hold steps) an attempt was made to assess the stability of in-process material during the hold times anticipated for GMP batches. The extended run duration expected for GMP was recognised due to the requirement to obtain equipment clearance data between process steps. In-process material was held at 2-8°C for approximately the duration expected for the GMP manufacture. In addition samples were held for an extended time representing twice that expected for the GMP campaign. A description of the samples taken, along with the respective hold times is given in table 44. The processing times for the 2OL demonstration run are represented in table 45. All samples were submitted to QC for SDS-PAGE, RP-HPLC, SEC-HPLC and UV analysis (Figures 79-83).
Overall, the results showed no detectable deterioration in the product over the first hold point with respect to purity (as determined by RP-HPLC), degradation (as detected by 8% Tris-Glycine SDS-PAGE) and aggregation (as determined by SECHPLC). Some of the assays, however, were recognised to be limiting since low molecular mass components would not be detected by 8% SDS-PAGE and the RPHPLC assay had not been developed to detect the 4OkDa, 55kDa and 9OkDa contaminants associated with Process 3. Some assays were also less relevant for crude samples such as the use of UV and SEC-HPLC in the fermentation samples. Despite these limitations, the only detected change in product profile was identified for the second hold point (day 12) for the AUXIl in-process sample taken from the Q-Sepharose column. This showed an increase in aggregate level between day 5 and day 12 although this increase was only from 0 to 0.62%.
A second stability study was performed on the in-process retains which were taken at the point of manufacture during the 2OL demonstration run and stored at — 200C. In this study, samples were thawed and incubated at room temperature and at 37°C and monitored by 4-12% SDS-PAGE analysis to allow the full molecular mass range of contaminants to be evaluated (figures 84-88). These data demonstrated that the samples prior to Q-Sepharose anion exchange were vulnerable to degradation. Following separation of the collagenases AUXI and AUXII (by the Q-Sepharose column), the samples appeared to be relatively stable and looked comparable to the time zero samples by SDS-PAGE.
Taken together, both studies indicate that providing the temperature is maintained between 2-8°C, in-process material is not expected to deteriorate during processing over the hold times investigated. This gives a level of confidence that the use of leupeptin and temperature control is sufficient to restrict levels of product degradation during processing over the durations anticipated in GMP.
Table 44
Figure imgf000104_0001
Table 45
Figure imgf000104_0002
Buffer stability study
Buffer samples illustrated in table 46 were reserved from the 2OL demonstration and retested after storage at 2-8°C. The pH, conductivity, temperature and appearance of the buffers were noted at the time of completion and after 12-13 days storage. The results of this study are given in table 47. Small differences were observed in the values for pH and conductivity but this may be due to differences in temperature between the original buffers and the tested retains. In particular, the HIC buffers showed the largest variation in conductivity and temperature. As a result, future studies on buffer stability should include specification of an accepted temperature range for recording all parameters. In all cases, the buffer retains were clear in appearance at time zero and after the required hold time.
Table 46
Figure imgf000105_0001
Table 47
Figure imgf000106_0001
Contaminant identification by N-terminal sequencing
Three main impurities were detected for Process 3 by SDS-PAGE analysis. These appeared to be co eluted with the AUXI and AUXIl collagenases and were only resolved by fractionation of the peaks eluted from the Q-Sepharose column. The contaminants were assigned by their apparent molecular mass on SDS-PAGE as 4OkDa, 55kDa and 9OkDa contaminants. Fractions with elevated levels of a particular contaminant were submitted for N-terminal sequencing after excision of the band from SDS-PAGE. Sequence analysis was successful for both the 55kDa and 4OkDa contaminant isolated from the 2OL demonstration run. The N-terminus of the 55kDa contaminant band associated with AUXI (Lanes 1-5; figure 89) was shown to match a region of the Col G sequence for collagenase AUXI whereas the 4OkDa contaminant band from AUXII (Lanes 6-10; figure 89) was identical to a region of the Col H sequence for collagenase AUXII. A previous attempt was made to sequence the 9OkDa band associated with both the AUXI and AUXII products (figure 90). Sequencing of the 9OkDa contaminant associated with the AUXI product was successful in that identity was correlated with the N-terminus of the AUXI sequence. In contrast, it was not possible to obtain a complete sequence for the 9OkDa contaminant associated with AUXII5 which suggested that the two 9OkDa contaminants were different products.
The main contaminants associated with Process 3 appeared to be product related and were either identified as N-terminally cleaved products of AUXI (55kDa) and AUXII (4OkDa) or a C-terminally cleaved product of AUXI (9OkDa). As these contaminants were different to those identified in Process 2, the QC assays utilized for the specification of the intermediates and drug substance did not resolve the new contaminants as the assay development had originated around Process 2. In particular, the standard purity assay (RP-HPLC) could not be used to detect levels of the 4OkDa and 55kDa contaminants. Densitometry analysis 2OL demonstration run
The 4OkDa, 55kDa and 9OkDa contaminants associated with Process 3 were identified and resolved by SDS-PAGE. These contaminants were clearly detected in fractions eluted from the Q-Sepharose column and appeared to elute at the leading and trailing edges of the peak profile (see figures 72-76). The decision for which fractions were included or excluded for further purification was based on experience of the relative intensity of staining for contaminants and product on Colloidal blue stained gels. In order to make this a less subjective estimation, densitometry was utilized to determine specific pooling criteria for fractions following the Q- Sepharose step. Densitometry was used in preference to the current QC assay for purity (RP-HPLC) since this assay could not resolve the new contaminants associated with Process 3. Densitometry data from post Q fractions from the 2OL demonstration run
The densitometry values from 2 separate analyses of the post-IEX fractions were averaged and are shown in table 48. Fractions 1-12 and the last 25% (tail) of peak 1 contain AUXTI and the associated contaminating proteins of 40, 75 and 9OkDa. Fractions 13-27 and the last 25% (tail) of peak 2 contain AUXI and the associated contaminants of 55 and 9OkDa. The pools of the fractions selected, based on SDS-PAGE without densitometric analysis, are highlighted.
Table 48
Figure imgf000108_0001
Densitometry summary documents from post Q fractions from the 200L demonstration run
Summary of Densitometry Analysis
Post IEX fractions from the 200L engineering run have been analysed multiple times to establish a pooling criteria that can be documented in the IEX
BMR for the GMP campaign. This pooling criterion is based on the assumption that (i) the quality of material generated from the engineering run is appropriate for the GMP material and (ii) the approximation of the densitometry method is acceptable. If the aim is to generate material of higher quality in the GMP campaign, the specification for pooling criteria will need to be revised. Specification for pooling from the IEX
In total, the samples from the 200L engineering run have been analyzed 6 times (2 operators and 3 repeats of each gel) and the average data presented in table 49. The fractions that were pooled for the engineering run are highlighted in red. From this analysis, the following pooling criteria can be established: (i) Any fraction of purity greater than or equal to 88.5% can be pooled (ii) Any fraction with a single impurity greater or equal to 10% cannot be pooled (iii) Fractions to be pooled must be from consecutive fractions, (iv) The calculated theoretical purity of the pool should be: Greater than or equal to 93% theoretical purity for AUXI Greater than or equal to 96% theoretical purity for AUXII
This last point was based on the estimates from the 200L engineering run in which the total protein in available fractions was estimated (although one limitation was that not all fractions were present for UV analysis for the AUXI). The data from this analysis is presented in table 50.
**NOTE: from these criteria, fraction 7 for AUXII peak would now be excluded. Assay variation
From the data of the post IEX fractions from the 200L engineering run, the following level of accuracy has been estimated: (i) for the product (AUXI and AUXII) the % CV had been calculated as 2.1 %
(AUXI) and 2.3% (AUXII). Therefore the purity specification of 88.6% for pooling could be in the range 86.3-90.9%. (ii) for the impurities, the % CV is much greater and the range has been estimated as 18.5%-33.7% depending on the impurity. Consequently, the purity specification of excluding fractions with a single impurity of no greater than 10% could be for fractions with an actual impurity range of 6.63 - 13.37 %. Therefore the value for the purity of the product (and not the impurities) is the most reliable value for pooling specification. Estimated purity of final material by densitometry
Densitometry analysis of the final material (DS and intermediates) for the 200L engineering run has also been determined by densitometry and is as follows: AUXI = 96.0% (3.1% of 9OkDa contaminant)
AUXII = 98.7% (1.2% of 9OkDa contaminant)
DS = 97.6% (2.1% of 9OkDa contaminant)
(Note: This is the range determined for a single SDS-PAGE analysed 3 times by 3 different operators.) Standardisation of the method
Over the course of the repeat analysis, the densitometry method has been standardized to minimise error between operators and variation between gels and will be documented in an SOP. Most notably:
(i) The standard loading of total protein in each lane of the gel will be lμg. (ii) A maximum of 16 fractions will be selected for analysis from each of the product peaks (AUXI and AUXII). This will limit the number of gels for densitometry analysis to 4.
(iii) The 16 fractions selected will start at the last fraction to be collected for each peak and work forward consecutively. This is to ensure accuracy in the figure calculated for the average purity (since all fractions to be pooled are likely to be included). Table 49: Average relative quantities of product and impurities in the post IEX fractions from the 200L Engineering run, as determined by densitometry analysis. The fractions pooled are highlighted in red.
Figure imgf000111_0001
Table 50: Theoretical relative amounts of product and impurities in the post IEX pools from the 200L Engineering run, as determined by densitometry analysis. The fractions pooled are highlighted in red. The theoretical average product purity is calculated as 92.3% and 95.8% for the AUXI and AUXII intermediates respectively.
Figure imgf000112_0001
GMP Pooling Criteria for Post Q-Sepharose Fractions Detail to be specified in the ion exchange BMR
A. The following pooling criteria is to be specified for fractions from both the AUXI and AUXII peaks which have been analysed by densitometry:
(i) A maximum of 16 fractions will be selected for analysis from each of the product peaks (AUXI and AUXII). This will limit the number of gels for densitometry analysis to 4.
(ii) Any fraction of purity greater than or equal to 90.00% (reported to 2 decimal places) can be pooled. (iii) Any fraction with a single impurity greater than or equal to 9.00% (to 2 dp) cannot be pooled.
(iv) Fractions to be pooled must be from consecutive fractions. B. The following pooling criteria is to be specified for fractions from the AUXII peak which have been analysed by SEC-HPLC:
(i) The maximum number of samples to be submitted for SEC-HPLC is 10 and must be from the last fraction collected for this peak and consecutive fractions forward.
(ii) Any fraction with greater than or equal to 2.00% (to 2dp) aggregate cannot be pooled. Details to be recorded for information only
A. The estimated theoretical purity of the pool should be calculated for information only and is expected to be:
Greater than or equal to 93.00% theoretical purity for AUXI Greater than or equal to 97.00% theoretical purity for AUXII
B. The minimum quantity of protein in each pool should be noted to establish if criteria for excluding fractions with less than 0.5g could be used in the future.
C. Fractions for the AUXI peak will be submitted for RP-HPLC but will be analysed retrospectively and for information only. These data will NOT be considered as part of the pooling criteria.
Expected impact on pooling
The following has been calculated from the average data set presented in table 51 to reflect the effect on yield and fraction selection following the new pooling criteria:
Table 51
Figure imgf000113_0001
Table 52: Average relative quantities of product and impurities in the post IEX fractions from the 200L Engineering run, as determined by densitometry analysis.
Figure imgf000114_0001
Table 53: Theoretical relative amounts of product and impurities in the post IEX pools from the 200L Engineering run, as determined by densitometry analysis. The fractions pooled are highlighted in red. The theoretical average product purity is calculated as 92.3% and 95.8% for the AUXI and AUXII intermediates respectively.
Figure imgf000115_0001
A comparison of 2 data sets (i.e. the same in-process samples run on different gels by different operators) allowed the following retrospective pooling criteria to be noted for the average data set although one additional fraction (fraction 27 from AUXI) would be included from those actually pooled in the 2OL run: • AUXI Pool all fractions with a purity of >87% but which do not have a single impurity of
>10%.
• AUXII
Pool all fractions with a purity of >94% but which do not have a single impurity of >4%.
QC data from the analysis of the final material from the 2OL demonstration run showed that the AUXII intermediate was 99.4% pure, the AUXI intermediate was 99.1% pure and the drug substance was 99.9% collagenase by RP-HPLC.
Therefore, the criteria specified for the pooling process would be expected to result in material that passes the release specifications for the final material.
200L demonstration run
The criteria established for the 2OL demonstration run previously mentioned was different to that implemented for the 200L engineering run. In this case, pooling was specified for both the AUXI and AUXII products as fractions with a purity of >86.5% but which did not have a single impurity contaminant of >10%. AUXII samples with an impurity level >2% detected by SEC-HPLC for were also excluded.
The resulting AUXI/AUXII intermediates and drug substance were also analyzed by densitometry, using a standardized method, and shown to have the following estimated purity based on analysis of a single gel 3 times (3 different operators): AUXI = 96.0% (3.1% of 9OkDa contaminant); AUXII = 98.7% (1.2% of 9OkDa contaminant); DS = 97.6% (2.1% of 9OkDa contaminant).
In addition, the QC determined purity of the intermediates and drug substance was show to pass specification by the RP-HPLC assay (AUXI = 98.2%;
AUXII = 98.1%; drug substance = 99.4%). Consequently, the pooling criteria followed for the 200L engineering run was successful in delivering product of suitable purity based on the current available analytical methods.
Materials and Methods
Mustang O Chromatography (2OL scale run*)
Equipment: Mustang Q Chromatography Capsule, 6OmL (CL3MSTGQP1 , Pall)
Conductivity and pH Meter 4330 (Jenway) Chemicals:
Sodium chloride (USP grade, Merck)
Sodium hydroxide solution (volumetric 4M) (AnalaR, BDH)
Tris (hydroxymethyl) methylamine (USP grade, Merck) Ammonium sulphate (Extra Pure, Merck)
Hyclone Water for Injection - Quality Water (WFI-QW)
A 6OmL bed volume Mustang Q chromatography capsule was sanitised with
IM NaOH at a flow rate of 30mL/min for 30minutes. The capsule was then preconditioned for the same time and flow-rate using IM NaCl. The capsule was equilibrated with 2L of Mustang Q Equilibration buffer (1OmM Tris, IM ammonium sulphate, pH 8), at a flow rate of 60mL/min. The outlet flow was checked to ensure the pH was <8. Supernatant (22L) from 200L fermentation PP3 (which had been
0.2μm filtered) was loaded onto the capsule at a flow rate of 540mL/min
(approximately 40 min. duration). The maximum recommended operating flow rate for the capsule was 600mL/min. The filtered material was stored in 2 x 1OL Stedim bags at 2-8°C overnight.
Hydrophobic interaction chromatography T20L scale run)
Equipment:
AKTA Pilot installed with Unicorn V 5.01 software (GE Healthcare) Vantage S130 column (cross sectional area 125cm2, Millipore)
Conductivity and pH Meter 4330 (Jenway)
Sartopore 2 0.8+0.45μm filter capsule (Sartorius)
Medical Refrigeration Unit MPl 50 (Electrolux)
Chemicals: Phenyl Sepharose 6 FF low sub (GE Healthcare)
Sodium hydroxide solution (volumetric 4M) (AnalaR, BDH)
Sodium chloride (USP grade, Merck)
Tris(hydroxymethyl)methylamine (USP grade, Merck)
Ammonium sulphate (Extra Pure, Merck) Leupeptin (MP Biomedicals, Inc)
Hyclone Water For Injection - Quality Water (WFI -QW) HIC column packing
240OmL of Phenyl Sepharose 6 FF Low Sub (Lot# 312089) slurry was settled for 3 hours and the ethanol removed and replaced with 180OmL WFI. The media was reslurried (50%), settled and washed once with WFI and twice with 180OmL 20OmM NaCl, with settling overnight between washes. The media was reslurried with 180OmL 20OmM NaCI, poured into the column and allowed to settle for Ih. The adaptor was brought down to ~lcm above the resin bed (removing all air bubbles) and the media packed in 20OmM NaCI at a flow rate of 400mL/min (192cm/hr) for lOmins. This packing flow rate was utilized as equivalent to the maximum operating flow rate for the K-prime system available in GMP. The adaptor was brought down to the top of the bed and the column packed at 192cm/hr for 1 Omins before screwing the adaptor into the top of the resin and packing at 192cm/hr for a further 1 Omins, during which no compression of the resin was observed. The pack test was carried out using the AKTA Pilot method: HIC 150OmL Pack Test. For this, the column was equilibrated with 1 column volume (CV) of 20OmM NaCl in WFI and pack tested with 15mL (1% CV) of IM NaCl in WFI at a flow rate of 313mL/min (150cm/hr). The column was flushed with 2CV WFI and stored with 2CV 1OmM NaOH. The packed column had an asymmetry of 1.2, a plate count of 2659 plates/meter, a CV of 1525mL and bed height of 12.2cm. Column sanitisation and equilibration
The Phenyl Sepharose 6 FF (low sub) column was sanitised with 0.5M NaOH for 60 minutes, washed with 2 column volumes (CV) WFI and equilibrated with 5CV 1OmM Tris, pH 8 (HIC Buffer B) followed by 5CV 1OmM Tris, LOM ammonium sulphate, pH 8 (HIC Buffer A). Preparation of the HIC load
13.48kg (11.05L) of 3.0M ammonium sulphate, 1OmM Tris, pH 8 was added to 22.1kg fermentation filtrate after the Mustang Q treatment (section 3.1). The filtrate was mixed for 5 minutes before filtering through a 0.05m2 filter capsule (0.8+0.45μm). The filtered material (denoted the HIC load material) was stored on ice (approximately 30 minutes duration) until use. HIC column run
The HIC run was performed at a constant linear flow rate of 150cm/hour using chilled buffers maintained at 2-8°C. 30L feedstock (equivalent to 2OL post- Mustang Q filtrate) was loaded onto the 1525mL Phenyl Sepharose 6 FF (low sub) column previously equilibrated with 2CV 1 OmM Tris, 1.0M ammonium sulphate, pH 8 (HIC Buffer A). Unbound material was washed off the column with lOCV HIC Buffer A. The column was then washed with 5CV 1OmM Tris, 0.3M ammonium sulphate, pH 8 (HIC Buffer A2) and bound proteins eluted with lOCV 1OmM Tris, pH 8 (HIC Buffer B). The first 0.67 CV (IL) of the elution buffer was discarded and a post-HIC pool of 4CV was collected. Leupeptin was added
(126.4mL) to the post-HIC pool (6191.3g) to a final concentration of 200μM from a stock solution of 1OmM leupeptin, 1OmM Tris, pH 8. The mixed solution (6.3kg) was stored at 2-8°C for 2 days before further processing by tangential flow filtration. Tangential Flow Filtration step 1 (TFFl 2OL scale run) Equipment:
ProFlux Ml 2 TFF system (Millipore)
Conductivity and pH meter 4330 (Jenways)
Sartopore 2 0.8+0.45μm filter capsule (Sartorius)
PelHcon 2 "Mini" Filter 0.1 im 3OkDa MWCO PES membranes (Millipore) Medical Refrigeration Unit MP 150 (Electrolux) Materials/Chemicals:
Sodium hydroxide solution (volumetric 4M) (AnalaR, BDH) Tris(hydroxymethyl)methylamine (USP grade, Merck) Leupeptin (MP Biomedicals, Inc) Hyclone Water For Injection Quality Water (WFI-QW) System step up
The ProFlux Ml 2 TFF system was set up according to the manufacturer's instructions with two PelHcon 2 "Mini" Filter 3OkDa MWCO PES membranes, sanitised with 0.5M NaOH for 60 minutes and stored in 0.1 M NaOH until use. The system was drained and flushed with 14L WFI and the normal water permeability (NWP) measured as 23L/m2/hr/psi at 25°C at a trans-membrane pressure (TMP) of 15psig (inlet pressure of 20psig and outlet pressure of 10 psig). The system was flushed with 0.5L 1OmM Tris, pH 8 (diafiltration buffer) and equilibrated with IL of the same buffer for 10 minutes. The conductivity and pH of the permeate was determined and checked against that of the diafiltration buffer to ensure the membranes were equilibrated prior to use. Concentration and diafiltration
The concentration and diafiltration steps were performed with chilled dialfiltration buffer (1OmM Tris, pH 8) containing 200μM leupeptin. The TFF system was flushed with IL chilled buffer just before use. 2L of the post-HIC material (6.3L total volume) was pumped into the TFF system reservoir and recirculated for 10 minutes without back-pressure to condition the membrane. The level sensor on the reservoir was set to 1.2L and the post-HIC material concentrated at a TMP of 15psig (inlet pressure of 20psig and outlet pressure of lOpsig) until all the material had entered the system. The permeate was collected and stored at 2-8°C for analysis. The inlet tubing was connected to the diafiltration buffer and diafiltration of the material was performed at a TMP of 15psig (inlet pressure of 20psig and outlet pressure of lOpsig) for approximately 8.5 turnover volumes (TOV), maintaining the volume of material in the reservoir at 1.2L. The conductivity and pH of the permeate was determined after 5, 7 and 8.5 TOV and checked against that of the diafiltration buffer. The retentate was drained from the system and stored at 2-8°C. 25OmL diafiltration buffer was pumped into the reservoir, recirculated around the system for 10 minutes without backpressure to rinse the system, drained, the rinse repeated and both rinses were stored separately at 2-8°C. The protein concentration of the retentate and rinses were determined (by UV) and the first rinse (204.8g weight) added to the retentate (1231.4g weight). This post TFFl material (1.4kg) was then filtered through a Sartopore 2 0.8+0.45μm filter capsule and stored at 2-80C overnight until further processing by Q Sepharose ion exchange chromatography.
Ion Exchange Chromatography (2OL scale run*) Equipment: AKTA Pilot installed with Unicorn 5.01 software (GE Healthcare) Conductivity and pH Meter 4330 (Jenway) Vantage S90 Column (cross sectional area 62cm2, Millipore) Medical Refrigeration Unit MPl 50 (Electrolux)
Chemicals:
Sodium hydroxide solution (volumetric 4M) (AnalaR, BDH)
Sodium chloride (USP grade, Merck) Tris(hydroxymethyl)rnethylamine (USP grade, Merck)
Calcium chloride 2-hydrate (USP grade, Merck)
Leupeptin (MP Biomedicals, Inc.)
Q Sepharose HP (GE Healthcare)
Hyclone Water For Injection - Quality Water (WFI-QW) Column packing and preparation
A Vantage S90 column was packed using an AKTA Pilot chromatography system with Q Sepharose HP media in WFI to give a packed column with a 10cm bed height, therefore a column volume (CV) of 62OmL. The packing was performed in accordance to the manufacturers instruction but with the pressure limit of the Vantage column imposed (0.3MPa) which equated to a packing flow rate of
210cm/hr and pressure limit of 0.28MPa. After packing, the column was equilibrated with 2CV of 0.2M NaCl and pack tested with 1% CV (6.2mL) IM NaCl at a flow rate of lOOcm/hr (103mL/min). The packed column had an asymmetry of
1.6 and a plate count of 12605 plates/meter, which was within specification for the media (asymmetry between 0.8 and 1.8, with a plate count >10,000). The column was stored in 1OmM NaOH until required.
Prior to use, the Q Sepharose column was washed with 1.5 column volumes
(CV) of WFI to remove the storage buffer, sanitised with 0.5M NaOH for 60mins at
40cm/hr before flushing again with 1.5CV WFI. The column was then charged and equilibrated in accordance to the manufacturers instructions with 2CV 1OmM Tris,
3mM calcium chloride, pH 8 followed by 2CV 1OmM Tris, 3mM CaCb, 36OmM
NaCl, pH 8 and finally 5CV 1OmM Tris, 3mM CaCl2, pH 8.
Column run
Immediately prior to the sample being loaded onto the column, the column was reequilibrated with chilled 1OmM Tris, 3mM CaCb, 200μM leupeptin pH 8
(IEX Buffer A). 1216mL of chilled post TFF 1 material at a concentration of
2.55mg/mL (determined by UV) was loaded onto the column at a flow rate of lOOcm/hr (103mL/min). This equated to a column load of 5mg total protein per mL of media. Following loading of the product, the column was washed with 3 column volumes (CV) of IEX Buffer A and the protein eluted with 1OmM Tris, 3mM CaCh, 36OmMNaCl, 200μM leupeptin, pH 8 (IEX Buffer B) with a gradient of 0-40% elution buffer (A to B), over 20CV at a flow rate of 70.2ml/min (68cm/hr). Elution was monitored at 280nm and 260nm and 10OmL fractions collected across the two product peaks containing AUX II and AUX I. Fraction collection was started from the breakthrough of the peak and continued until 25% of the peak height on the trailing edge. A total of 12 fractions were collected across the AUX II peak and 15 fractions across the AUX I peak. The Q Sepharose HP chromatography was carried out at a standard laboratory temperature of 18-230C, although the buffers used were pre-chilled. Fractions were stored at 2-80C until a result was obtained from the SDSPAGE analysis. Fractions 6 to 12 (peak 1) were pooled as AUX II collagenase with the volume determined as 683g (after sampling) and the concentration by UV analysis measured as 1.17mg/mL. Fractions 19 to 26 (peak 2) were pooled as AUX I collagenase with the volume determined as 796g (after sampling) and the concentration by UV measured as 1.08mg/mL. Tangential Flow Filtration step 2 (TFF2 2OL scale run) Equipment: ProFlux M12 TFF system (Millipore)
Conductivity and pH meter 4330 (Jenways)
Pellicon 2 "Mini" Filter 0.1m230kDa MWCO PES membrane (Millipore)
90mm Filter Unit (IL) 0.2μm PES membrane (Nalgene)
Medical Refrigeration Unit MP150 (Electrolux) Materials/Chemicals:
Sodium hydroxide solution (volumetric 4M) (AnalaR, BDH) Tris(hydroxymethyl)methylamine (USP grade, Merck) Sucrose (BP grade, Merck) Leupeptin (MP Biomedicals, Inc.) Hyclone Water For Injection - Quality Water (WFI-QW) Frensius Kabi Water For Injection (WFI) System set up
The ProFIux M 12 TFF system was set up according to the manufacturer's instructions with one Pellicon 2 "Mini" Filter 3OkDa MWCO PES membrane, sanitised with 0.5M NaOH for 60 minutes and stored in 0.1 M NaOH until use. The system was drained and flushed with 14L WFI and the normal water permeability (NWP) measured as 19.5L/m2/hr/psi for the membrane used for AUXI and as 14.5L/rri2/hr/psi at 25°C for the membrane used for AUXII at 25°C and at a transmembrane pressure (TMP) of 15psig (inlet pressure of 20psig and outlet pressure of lOpsig). The system was flushed with 0.5L 1OmM Tris, 6OmM sucrose, pH8 (formulation buffer), and equilibrated with IL of the same buffer for 10 minutes. The conductivity and pH of the permeate was determined and checked against that of the formulation buffer. Concentration and formulation
The concentration and diafiltration steps were performed separately on each of the post IEX pools of AUXI and AUXII. All steps were performed using chilled formulation buffer (1OmM Tris, 6OmM sucrose, pH 8) maintained at 2-8°C. The TFF system was flushed with IL chilled buffer just before use. The post-IEX pool (683g weight of AUXIl and 796g weight of AUXI) was pumped into the TFF system reservoir and recirculated at 10% pump speed for 10 minutes without backpressure to condition the membrane. The level sensor on the reservoir was set to approximately 40OmL and the AUXI or AUXII pool concentrated at a TMP of 15psig (inlet pressure of 20psig and outlet pressure of lOpsig) until the volume in the reservoir had been reduced to approximately 360-39OmL (this assumed a system hold up volume of 10OmL). The target volume reduction was based on achieving a theoretical concentration of 1.75mg/mL for the product assuming no loss in protein during the concentration operation. The permeate was collected and stored at 2-8°C for analysis. For the diafiltration operation the inlet tubing was connected to the formulation buffer and diafiltration performed at a TMP of 15psig (inlet pressure of 20psig and outlet pressure of lOpsig). Approximately 12 turnover volumes (TOV) were performed for AUXII and 8.5 TOVs for AUXI, maintaining the volume of material in the reservoir at ~400mL. The conductivity and pH of the permeate was determined after 12 TOV for AUXII and after 6, 7, and 8.5 TOVs for AUXI and checked against that of the formulation buffer. The retentate was drained from the system and stored at 2-8°C.
25OmL formulation buffer was used to wash residual product from the membranes by re-circulated around the system for 10 minutes (without backpressure). After draining the rinse solution, a second wash was performed and both rinse 1 and rinse
2 were stored at 2-8°C. After UV protein content determination of the retentate and rinses, the first rinse was added to the retentate, mixed and a UV protein concentration of the mix determined. For AUXII, 122g of the second rinse was also added to the retentate plus rinse 1 to give a theoretical AUXII concentration of 1.1 mg/mL. For AUXI, 94g of the second rinse was added to the material to give a theoretical AUXI concentration of 1.1 mg/mL. Both the AUXI and AUXII material were filtered through a IL Nalgene 0.2μm filter unit in a Class II hood and the post filtered protein concentration determined. The AUXI and AUXII intermediates were stored at 2-8°C. Protein concentration determination
Absorbance
Equipment:
DU800 Spectrophotometer (Beckman)
In process samples were analysed by UV spectrophotometry by performing a UV scan of samples between 220 and 330nm. The appropriate buffer was used as a blank and a scan of the buffer blank performed before scanning the samples. If necessary, samples were diluted with the same buffer to ensure the A280 < 1.0 AU.
Protein concentrations (mg/mL) were determined according to the Beer-Lambert law, c = A/b.ε, where A is the absorbance (A280- A330), b is the pathlength (1.0cm) and ε is the extinction coefficient of the protein. Extinction coefficients of 1.48mg- lcm-imL for AUXI, 1.576mg-icm-imL for AUXII and 1.428mg-icm-imL for an
AUXI/AUXII mix were used.
Bradford Assay
Materials: Lyophilised BSA (hydrated to 1.4mg/mL)
Chemicals:
Protein Assay Dye Reagent Concentrate (500-0006, Bio-Rad) A BSA standard curve was prepared by diluting the BSA with water, to known concentrations. The Bio-Rad protein assay dye reagent was prepared by diluting one part concentrate with four parts water. Test samples were prepared by diluting with water. 50μL of test sample either neat or diluted was added to a cuvette and 2.5mL diluted regent added. Samples were prepared in duplicate. The samples were incubated for lOminutes before reading the OD. The standard curve of ODs95nm vs. protein concentration was obtained by measuring the ODs95nm of BSA solutions of known concentration. The test samples were then assayed and the protein concentration determined from the standard protein assay curve. Samples from the post Mustang Q step were always analysed without dilution in order to standardise the contribution from the pigment. In this case, 50μL of the undiluted post Mustang Q material was utilised in the assay. SDS-PAGE Analysis Equipment: Xcell SureLock Mini-Cell Electrophoresis System (Invitrogen)
Electrophoresis Power Supply EPS 601, (Amersham Pharmacia Biotech)
Rocky shaker platform, (Scientific Laboratory Supplies)
Chemicals:
SDS-PAGE Standards High Molecular Weight (161-0303, Bio Rad) Markl2 Unstained Standard (LC5677, Invitrogen)
Novex 8% Tris-Glycine gels, 1.5mm, 10 well (EC6018BOX, Invitrogen) NuPAGE Novex 4-12% Bis-Tris gels, 1.0mm, 12 well (NP0322BOX, Invitrogen) Novex Tris-Glycine SDS Running Buffer (1Ox) (LC2675, Invitrogen) NuPAGE MES SDS Running Buffer (2Ox) (NP0002, Invitrogen) Novex Tris-Glycine SDS Sample Buffer (2x) (LC2676, Invitrogen) NuPAGE LDS Sample Buffer (4x) (NP0007, Invitrogen) NuPAGE Sample Reducing Agent (1Ox) (NP0009, Invitrogen) Colloidal Blue Staining kit (LC6025, Invitrogen) Ethylenediaminetetra-acetic acid disodium salt AnalaR R (BDH) Tris-Glycine Gels
Samples were prepared for reducing SDS-PAGE by adding 12μl of sample to 20μl sample Buffer (2x), 4μl reducing agent (1Ox) and 4μl of 0.1M EDTA (to achieve final concentration of 1OmM). The high molecular weight (HMW) marker was prepared by adding lOμl of concentrated stock to 80μl reducing agent (1Ox)3 310μl WFI and 400μl sample buffer (2x). The diluted HMW standard was then heated at 95oC for 5 minutes before aliquoting and storage at — 20oC for use in subsequent gels. Samples (20μl load volume) containing collagenases were run directly (i.e. with no prior heat treatment) on 8% Tris-Glycine gels using Tris- Glycine running buffer at 130V for ~2hours. After electrophoresis, the gels were stained with colloidal blue stain reagent as per the manufacturers instructions. Bis-Tris Gels Samples were prepared for reducing SDS-PAGE by adding 16.5μl of sample to 7.5μl sample buffer (4x), 3μl reducing agent (1Ox) and 3μl of 0.1M EDTA (to achieve final concentration of 1OmM). MARK 12 marker loaded neat (lOμl). Samples (15μl load volume) containing collagenases were run directly (i.e. with no prior heat treatment) on 4-12% Bis-Tris gels using either MES running buffer at 200V for ~40mins. After electrophoresis, the gels were stained with either colloidal blue stain reagent as per the manufacturers instructions or silver stained using a standard procedure (GE Healthcare). Densitometry analysis of post-IEX fractions Equipment: Xcell SureLock Mini-Cell Electrophoresis System (Invitrogen)
Electrophoresis Power Supply EPS 601, (Amersham Pharmacia Biotech)
Rocky shaker platform, (Scientific Laboratory Supplies) Flatbed scanner (Hewlett
Packard)
Materials/Chemicals: NuPAGE Novex 4-12% Bis-Tris gels, 1.0mm, 12 well (NP0322BOX, Invitrogen) NuPAGE MES SDS Running Buffer (2Ox) (NP0002, Invitrogen) NuPAGE LDS Sample Buffer (4x) (NP0007, Invitrogen) NuPAGE Sample Reducing Agent (1Ox) (NP0009, Invitrogen) Mark 12 Unstained Standard (LC5677, Invitrogen) Colloidal Blue Staining kit (LC6025, Invitrogen)
Ethylenediaminetetra-acetic acid disodium salt (EDTA) (AnalaR, BDH) Purified water Reducing SDS-PAGE
The post-IEX samples were run on 4-12% Bis-Tris gels using MES running buffer at lμg/Iane loading. Samples were prepared by adding 20μL of diluted post- IEX material to 8μL Sample Buffer (4x), 3μL Reducing Agent (1Ox) and 3.4μL of 0.1M EDTA. 15μL of each sample was loaded into the well directly after mixing (i.e. with no heat treatment) and run at 200V for 40mins. After electrophoresis, the gels were stained with Colloidal Blue stain reagent according to the manufacturers instructions but with a fixed staining duration to reduce staining variation (10 minute fix, 5 hours stain, 15-20 hours destain with purified water). Gel scanning and densitometry
Gels were placed between 2 sheets of acetate ensuring removal of all air bubbles, scanned on a flat-bed scanner at 600dpi resolution and the image cropped, resized and colour corrected with HP Image zone software. The image was converted to an 8-bit greyscale TIFF image with Alpha EaseFC software and the protein bands were analysed using QuantityOne gel documentation software
(BioRad). After background substitution, the intensity peak areas of selected bands were converted to relative percentage values of product (AUXI or AUXII) and impurity(s) in each lane. Buffer stability Equipment:
Peristaltic Pump (Watson Marlow) 125ml PETG biotainers (Cellon) Watson Marlow Tubing for peristaltic pump Conductivity and pH Meter 4330 (Jenway) Sartopore 2 300 (0.45/0.2μm) filter capsule (Sartorius)
Buffers for the 2OL demonstration run were filtered after preparation through a 0.45/0.2μm filter capsule into 10 or 2OL Stedim bags for storage at 2-8°C prior to use- When the majority of the buffer had been filtered, approximately 75mls of the remaining buffer was collected into pre-labelled 125ml PETG biotainers and stored at 2-8oC. The pH, conductivity, temperature and date of buffer preparation were recorded. On completion of the 2OL demonstration run, the buffer samples were retrieved from cold storage and retested for pH, conductivity, and appearance. The temperature of the buffer at the time of testing was also recorded. Preparation of samples for N-terminal sequencinfi analysis Equipment: Electrophoresis Power Supply EPS 601, (Amersham Pharmacia Biotech) Xcell SureLock Mini-Cell Electrophoresis System, (Invitrogen) Rocky shaker platform, (Scientific Laboratory Supplies) Chemicals: Novex 8% Tris-Glycine Gel, 1.5mm, 10 well, (Invitrogen) High Molecular Weight Marker, (BioRad)
NuPAGE Sample Reducing Agent (1Ox), (Invitrogen) Novex Tris-Glycine SDS Running Buffer (1Ox), (Invitrogen) Novex Tris-Glycine SDS Sample Buffer (2x), (Invitrogen) Colloidal Blue Staining Kit, (Invitrogen) Ethylenediaminetetra-acetic acid disodium salt (EDTA) (AnalaR, BDH) Methanol, AnalaR (BDH) Acetic Acid, AnalaR (BDH) Water for injection (WFI) Purified Water Samples for N-terminal sequencing were prepared and separated on 8% Tris-
Glycine gels as outlined previously. Samples identified as enriched for the 4OkDa contaminant (fraction 2 from the post IEX AUXII peak, CTL2006#0610H;) and 55kDa contaminant (fraction 16 from the post IEX AUXI peak, CTL2006#061 IH) were each loaded in 5 lanes of the gel to provide enough material for sequencing (figure 89). Post IEX fractions from a previous 2OL fermentation (2OL PP3), which were enriched for the 9OkDa contaminants associated with both AUXI (fraction B7 R2, CTL2006#0581P) and AUXII (fraction Dl, CTL2006#0582P) were also loaded in multiple lanes (figure 90). After electrophoresis, the gels were stained with colloidal blue stain reagent according to the manufacturers instructions and the contaminant bands excised and submitted to Alta Bioscience (Birmingham University, UK) for N-terminal sequencing. The 9OkDa AUXI associated contaminant (CTL2006#0612H) from the 2OL demonstration run was also submitted for sequencing but no data was obtained.
SUMMARY OF THE MANUFACTURING OF PROCESS 3
Fermentation
The Phytone fed-batch fermentation process (Process 2) for production of collagenase from Clostridium histolyticum had been shown to be highly variable due to batch-to-batch variability in the Phytone peptone. For this reason Proteose Peptone #3 (PP3) was evaluated in 5L fermentations. The evaluation demonstrated that when one specific batch of PP3 was used at 50g/L the fermentation process was robust and reproducible. However when other batches of PP3 were employed at 50g/L large variations were seen in the growth profiles of the cultivations. The maximum biomass concentration the various batches of PP3 would support were assessed in a small scale evaluation. These batches were deemed "good" or "poor" based on their ability to support high or low biomass concentrations of C. histolyticum respectively. When two fermentations were carried out at 5L scale with "ppor" and "good" batches of PP3 at 100g/L both demonstrated highly similar growth profiles and product yields. This experiment showed that increasing the concentration of PP3 to 100g/L alleviated the problem associated to batch to batch variation in the peptone.
A scale up fermentation was carried out at 200L. The fermentation used the optimized concentration of PP3 (100g/L). The fermentation was successful and replicated both the growth profile and product yield/quality observed at 5L scale. The harvest process (clarification by filtration) developed for Process 2 was evaluated during the 200L scale up fermentation. The cell culture was successfully clarified using the existing process with no blockage of the filtration train.
The quantification of collagenase concentration in crude fermentation samples was improved using densitometry analysis of Coomassie stained Tris Glycine gels. A standard curve of mixed AUXI and AUXII was loaded with dilutions of fermentation samples. The relationship between collagenase concentration and densitometry peak area was shown to be linear within the range of the sample dilutions. The concentrations of collagenase in the samples were then extrapolated using their peak area and the standard curve. This method estimated the yield of collagenase to be 280 - 350mg/L from the 100g/L PP3 process at 5 and 200L scale.
The optimised PP3 fermentation process generated a higher biomass concentration (OD600 7 units) and increased product yield (280 - 350mg/L total collagenase, by quantitative densitometry) when compared to the Phytone fed-batch process. The fermentation filtrate contained significantly less clostripain than the Phytone process. The ratio of AUXI: AUXII was closer to 1 compared to that observed during evaluation of Process 2. In summary the PP3 process increased the product yield, purity (post-fermentation) and reproducibility of the fermentation. Purification
Process 3 was developed in an accelerated time frame in order to improve the processes previously developed at Cobra (Process 2) and run at 2OL scale in GMP. Major improvements to the process were made in order to simplify the purification procedure, facilitate robustness as well as make the process more amenable to scale up to 200L. These improvements were also considered key to assisting process validation.
Process 3 was performed using material from a 200L fermentation of Clostridium histolyticum in which a full 2OL of fermentation was purified. Material was processed directly from the fermentation and no hold steps were implemented. Following filtration, product was passed through a Mustang Q filter since small- scale experiments demonstrated reduction of dsDNA (as detected by pico green analysis) using this procedure. Analysis of in-process samples from the 20L demonstration run however, showed no reduction in dsDNA suggesting that the robustness and application of this step required further investigation. A comparison of the parameters used for the 2OL run-through and previous small-scale experiments demonstrated dsDNA removal when the capsule was oversized by a factor of 1000 (based on the DNA binding capabilities of 15-25mg DNA/mL capsule described by the manufacturer). In comparison, the capsule used in the 2OL run-through was oversized by a factor of approximately 177-296. Material from the Mustang Q capsule was held overnight at 2-8°C. An off-line stability study on sample material taken at this stage in the process indicated that maintaining a low temperature was key to the product stability at this point in the process since samples incubated at RT and 37°C were susceptible to degradation as indicated by SDS-PAGE analysis.
Product from the Mustang Q capsule was prepared for hydrophobic interaction chromatography (HIC) by the addition and mixing of an ammonium sulphate solution (3M) to achieve a final concentration of IM. This provided conditions suitable for collagenase binding to Phenyl Sepharose FF (low sub) media. A proportion of protein contaminants and pigment were then eluted from the HIC column using a step elution of 0.3M ammonium sulphate followed by collagenase product elution with a solution containing no ammonium sulphate. Criteria for collection of the product peak were established as a fixed volume of 4 column volumes (although this was later extended to 5 column volumes for the 200L scale demonstration run). Leupeptin was then added immediately following elution and the material held for a period of 2 days at 2- 8°C. The yield from this step was difficult to determine accurately due to the complex nature of the feedstock. The process step yield was estimated as (i) 38% based on Bradford assay of the load and UV of the eluted material or (ii) 47% based on collagenase content in the load estimated by densitometry and UV of the eluted material. Alternatively, 0.17g of total protein was eluted from the HIC column for the equivalent of every IL of fermentation filtrate applied. The post HIC pool was prepared for Q-Sepharose purification by concentration (5- fold) and buffer exchange using tangential flow filtration (TFFl) using 2 x 0.1 m2 3OkDa membranes. No loss was detected over this step and the reported increase in protein recovered may reflect the inaccuracy of UV at this point in the process. Inaccuracy could be attributed to pigment contamination or the use of the extinction coefficient for collagenases, which will be less accurate for material earlier in the purification when a complex of proteins are likely to be present. The TFF step was completed by a product filtration step before holding the material at 2- 8°C over night.
As with Process 2, the Q-Sepharose column was a key purification step in Process 3 and resulted in the separation of the AUXI and AUXII collagenases. The contaminants associated with process 3, however, were different to those in process 2 and appeared to closely co-purify with the AUXI and AUXII products. It was possible however, to remove the contaminants from the products by fractionation of the product peaks since the contaminants appeared to elute at either the leading or tail edges of both peaks. The contaminants were denoted by their relative molecular mass on reducing SDS-PAGE. Those associated with the AUXII product (the first peak eluted from the Q-Sepharose column) were identified as (i) 4OkDa (associated with the leading edge of the peak) and (ii) 75kDa and 9OkDa (associated with the trailing edge of the peak). N-terminal amino acid sequencing indicated that the 4OkDa was AUXII related since the sequence matched identity with a region of the Col H sequence. In comparison, no identity could be confirmed for the 9OkDa contaminant due to issues of low signal. Contaminants associated with AUXI product (the second peak eluted form the Q-Sepharose column) were (i) 55kDa (associated with the leading edge of the peak) and (ii) 9OkDa (associated with the trailing edge of the peak). N-terminal sequencing showed both the 55kDa and 9OkDa contaminants to be identified as AUXI-related where the 55kDa contaminant showed sequence identity with a mid region in the Col G sequence and the 9OkDa showed identical N-terminal match to AUXI. Consequently, the major impurities identified at this stage in the process were all product related and either identified as internal cleavage products of AUXI (55kDa) and AUXII (4OkDa) or a C-terminally cleaved product of AUXI (9OkDa). Following the Q-Sepharose column, a key process step was in the decision as to which fractions should go forward for further purification. For the 2OL demonstration run this criteria was based on the relative staining intensities of contaminants to product when analysed by 4-12% SDS-PAGE and stained with Colloidal Blue stain. The decision was subjective and based on the collective experience of the process development group as well as requests from the client. In order to establish defined criteria that described the pooling procedure, densitometry was performed on SDSPAGE. From this, the pooling was described as including fractions that were >87% pure (with no single impurity >10%) for AUXI and >94% pure (with no single impurity >4%) for AUXII. This resulted in a step yield based on UV estimation of 27.7% and 25.8% for AUXI and AUXTI respectively. Further refinement and standardization of the densitometry method was achieved from data acquired from the 200L scale demonstration run which resulted in definition of modified criteria for the subsequent GMP run.
Fractions containing AUXl or AUXII product from the Q-Sepharose column were formulated separately by TFF (denoted TFF2) using 1 x 0.1 m2 3OkDa membrane for each collagenase. The formulation buffer of 1OmM Tris, 6OmM sucrose pH 8, had been established by KBI BioPharma Inc. Product was filtered following the TFF2 step and the overall step yields for TFF and filtration estimated as 97.5% for AUXI and 92.2% for AUXII. At this stage samples were referred to as intermediates and were retained at 2-8°C for QC analysis and prior to mixing of the drug substance. A retrospective stability study indicated the intermediates were stable over a period of at least 5 days at 2-8°C as determined by SDS-PAGE, UV, RP-FIPLC and SEC-FIPLC analysis. The only detected deterioration in intermediates was identified in the AUXII intermediate after a 12 day hold in which aggregate levels increased from 0 to 0.62%. The AUXI and AUXII intermediates were mixed in equal ratio (as determined by UV) to generate the drug substance before performing a final product filtration. Only 400mg of drug substance was prepared of which 200mg was shipped to KBI BioPharma Inc. along with 25mg of each intermediate. The overall process yield was estimated for the 2OL demonstration run in which all available material from the 2OL of fermentation feedstock had been processed and assuming all material had been mixed as drug substance. This gave a predicted yield of 1.6g drug substance for the 2OL scale purification. This equated to a process recovery of 17.8% based on then assumption that the initial estimate of 9g (using the Bradford assay) for the amount of total protein available to load onto the HIC column was accurate. Alternatively, if the total available protein was related to the collagenase content in the HIC load (as estimated by densitometry) the overall process yield was calculated as 22%.
In addition to the process run-through, some preliminary studies were preformed on sample and buffer retains taken from the process to assess stability. These data indicated that for the product, low temperature was a key factor in controlling degradation and samples taken early in the purification (prior to the Q- Sepharose column) were more susceptible to proteolysis. A product hold study showed however, that the combination of leupeptin and temperature control (2-8°C) was successful in maintaining the product quality over the time courses anticipated for the GMP process.
Tables 54 and 55 detailed the analytical specifications AUX-I and AUX-II intermediates and also for Drug Substance for Process 3.
Table 54: Analytical Specifications for Process 3 AUX-I and AUX-II Intermediates
Figure imgf000134_0001
*Tests required for provisional release of intermediates for further manufacturing Table 55: Analytical Specifications for Process 3 Drug Substance
Figure imgf000135_0001
Tests required for provisional release of Drug Substance for further manufacturing.
The patent and scientific literature referred to herein establishes the knowledge that is available to those with skill in the art. All United States patents and published or unpublished United States patent applications cited herein are incorporated by reference. AU published foreign patents and patent applications cited herein are hereby incorporated by reference. All other published references, documents, manuscripts and scientific literature cited herein are hereby incorporated by reference.
While this invention has been particularly shown and described with references to preferred embodiments thereof, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the scope of the invention encompassed by the appended claims.

Claims

What is claimed is:
1. A drug product consisting of collagenase I and collagenase II having the sequence of Clostridium histolyticum collagenase I and collagenase II, respectively, having a mass ratio of about 1 to 1 with a purity of at least 95% by area.
2. The drug product of claim 1, wherein the drug product has a SRC assay activity for collagenase I of about 13,000 to about 23,000 fSRC units/mg, and a GPA assay activity for collagenase II of about 200,000 to about 380,000 fGPA units/mg, when the drug product is in 1OmM Tris buffer and 6OmM sucrose at a pH of about 8.
3. The drug product of claim 1, wherein the drug product contains less than about 2% by area aggregated protein.
4. The drug product of claim 3, wherein the drug product contains less than about 1% by area of clostripain.
5. The drug product of claim 4, wherein the drug product contains less than about 1% by area of gelatinase.
6. The drug product of claim 5, wherein the drug product contains less than about 1% ug/mg (w/w) of leupeptin.
7. The drug product of claim 6, wherein having a bioburdeπ less than 1 cfu/ml, and wherein the drug product sterilized.
8. The drug product of claim 7, containing less than 10 EU/ml of endotoxin.
9. The drug product of claim 7, containing less than 5 EU/mg of endotoxin.
10. The drug product of claim 1, wherein the collagenase I and II have a purity of a least about 97% by area.
11. The drug product of claim 1, further comprising a pharmaceutically acceptable excipient.
12. The drug product of claim 1, wherein the drug product is a sterile lyophilized powder is stored at a temperature of about 5°C.
13. The drug product of claim 11, wherein the drug product is a lyophilized injectable composition formulated with Sucrose, Tris and with a pH level of about 8.0.
14. The drug product of claim 13, wherein the drug product is a lyophilized injectable composition formulation comprising about 0.9 mg of the said drug product, about 18.5 mg of sucrose and about 1.1 mg of Tris, and wherein the targeting a vial fill volume is about 0.9 mL.
15. The drug product of claim 13, wherein the drug product is a lyophilized injectable composition formulation comprising about 0.58 mg of the said drug product, about 12.0 mg of sucrose and about 0.7 mg of Tris.
16. A kit comprising a vial for providing the drug product according to claim 11 and instructions explaining how to deliver said drug product with said device.
17. The drug product of claim 1, wherein the drug product is used to treat a subject suffering from a collagen-mediated disease.
18. A drug product consisting of collagenase I and collagenase II having the sequence of Clostridium histolyticum collagenase I and collagenase II, respectively, having a mass ratio of about 1 to 1 with a purity of at least 95% by area, wherein the preparation of the drug product comprising the steps of: a) fermenting Clostridium histolyticum; b) harvesting a crude fermentation comprising collagenase I and collagenase II; c) purifying collagenase I and collagenase II from the crude harvest via filtration and column chromatography; and d) combining the collagenase I and collagenase II purified from step (c) at a ratio of about 1 to 1.
19. The drug product of claim 18, wherein the drug product has a SRC assay activity for collagenase I of about 13,000 to about 23,000 fSRC units/mg, and a GPA assay activity for collagenase II of about 200,000 to about 380,000 fGPA units/mg.
20. The drug product of claim 18, wherein the purity is at least 97% by area.
21. The drug product of claim 18, wherein the purity is at least 98% by area.
22. The drug product of claim 18, wherein cell bank preparations are conducted in the presence of phytone peptone or vegetable peptone.
23. The drug product of claim 18, wherein the fermentation step comprises the steps of: a) inoculating the medium in a first stage with Clostridium histolyticum and agitating the mixture; b) incubating the mixture from step (a) to obtain an aliquot; c) inoculating the medium in a second stage with aliquots resulting from step (b) and agitating the mixture; d) incubating mixtures from step (c); e) inoculating the medium in a third stage with aliquots resulting from step (d) and agitating; f) incubating mixtures from step (e); g) inoculating the medium in a fourth stage with an aliquot resulting from step (f) and agitating; h) incubating mixtures from step (g); and i) harvesting culture resulting from step (h) by filtration.
24. The drug product of claim 18, wherein the purification step comprises the steps of: a) filtering the crude harvest through a Mustang Q column; b) adding ammonium sulphate; c) filtering the crude harvest; d) subjecting the filtrate through a HIC column; e) adding leupeptin to the filtrate; f) removing the ammonium sulfate and maintaining leupeptin for correct binding of collagenase I and collagenase II with buffer exchange by TFF; g) filtering the mixture of step (f); h) separating collagenase I and collagenase II using Q-Sepharose HP i) preparing TFF concentration and formulation for collagenase I and collagenase II separately; and j) filtering through a 0.2 μm filtration system.
25. The drug product of claim 18, wherein the drug product is stored at a temperature of about -700C.
26. The drug product of claim 18, further comprising a pharmaceutically acceptable excipient.
27. The drug product of claim 18, wherein the drug product is a sterile lyophilized powder and is stored at a temperature of about 50C.
28. The drug product of claim 26, wherein the drug product is a lyophilized injectable composition formulated with Sucrose, Tris and with a pH level of about 8.0.
29. The drug product of claim 28, wherein the drug product is a lyophilized injectable composition formulation comprising about 0.9 mg of the said drug product, about 18.5 mg of sucrose and about 1.1 mg of Tris, and wherein the targeting a vial fill volume is about 0.9 mL.
30. The drug product of claim 28, wherein the drug product is a lyophilized injectable composition formulation comprising about 0.58 mg of the said drug product, about 12.0 mg of sucrose and about 0.7 mg of Tris.
31. A kit comprising a vial for providing the drug product according to claim 26 and instructions explaining how to deliver said drug product with said device.
32. The drug product of claim 18, wherein the drug product is used to treat a subject suffering from a collagen-mediated disease.
33. A process for producing a drug product according to Claim 1, comprising the steps of: a) fermenting Clostridium histolyticum; b) harvesting a crude fermentation comprising collagenase I and collagenase II; c) purifying collagenase I and collagenase 11 from the crude harvest via filtration and column chromatography; and d) combining the collagenase I and collagenase II purified from step (c) at a ratio of about 1 to 1.
34. The process of claim 33, wherein the drug product has a SRC assay activity for collagenase I of about 13,000 to about 23,000 fSRC units/mg, and a GPA assay activity for collagenase II of about 200,000 to about 380,000 fGPA units/mg.
35. The drug product of claim 33, wherein the drug product has a purity of at least 97% by area.
36. The drug product of claim 33, wherein the drug product has a purity of at least 98% by area.
37. The process of claim 33, wherein cell bank preparations are conducted in the presence of phytone peptone or vegetable peptone.
38. The process of claim 33, wherein the fermentation step comprises the steps of a) inoculating the medium in a first stage with Clostridium histolyticum and agitating the mixture; b) incubating the mixture from step (a) to obtain an aliquot; c) inoculating the medium in a second stage with aliquots resulting from step (b) and agitating the mixture; d) incubating mixtures from step (c); e) inoculating the medium in a third stage with aliquots resulting from step (d) and agitating; f) incubating mixtures from step (e); g) inoculating the medium in a fourth stage with an aliquot resulting from step (f) and agitating; h) incubating mixtures from step (g); and i) harvesting culture resulting from step (h) by filtration.
39. The process of claim 33, wherein the purification step comprises the steps of: a) filtering the crude harvest through a Mustang Q column; b) adding ammonium sulphate; c) filtering the crude harvest; d) subjecting the filtrate through a HIC column; e) adding leupeptin to the filtrate; f) removing the ammonium sulfate and maintaining leupeptin for correct binding of collagenase I and collagenase II with buffer exchange by TFF; g) filtering the mixture of step (f); h) separating collagenase I and collagenase II using Q-Sepharose HP i) preparing TFF concentration and formulation for collagenase I and collagenase II separately; and j) filtering through a 0.2 μm filtration system.
40. The process of claim 33, wherein the drug product is stored at a temperature of about -700C.
41. The drug product of claim 33, further comprising a pharmaceutically acceptable excipient.
42. The drug product of claim 33, wherein the drug product is a sterile lyophilized powder is stored at a temperature of about 5°C.
43. The drug product of claim 33, wherein the drug product is a lyophilized injectable composition formulated with Sucrose, Tris and with a pH level of about 8.0.
44. The drug product of claim 43, wherein the drug product is a lyophilized injectable composition formulation comprising about 0.9 mg of the said drug product, about 18.5 mg of sucrose and about 1.1 mg of Tris, and wherein the targeting a vial fill volume is about 0.9 mL.
45. The drug product of claim 43, wherein the drug product is a lyophilized injectable composition formulation comprising about 0.58 mg of the said drug product, about 12.0 mg of sucrose and about 0.7 mg of Tris.
46. A kit comprising a vial for providing the drug product according to claim 41 and instructions explaining how to deliver said drug product with said device.
47. The process of claim 33, wherein the drug product is used to treat a subject suffering from a collagen-mediated disease.
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DK07762860.0T DK1987141T3 (en) 2006-01-30 2007-01-30 COMPOSITIONS SUITABLE FOR TREATING COLLAGEN-CONDUCTED DISEASES
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NZ569882A NZ569882A (en) 2006-01-30 2007-01-30 Treating collagen-mediated diseases with Clostidium histolyticum collagenase I and II
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BRPI0708017-4A BRPI0708017A2 (en) 2006-01-30 2007-01-30 medicated product, process for its production and kit comprising a vial to provide such medicated product
CN200780008746.5A CN101400788B (en) 2006-01-30 2007-01-30 The compositions of the disease that treatment is mediated by ossein and Therapeutic Method
AU2007211313A AU2007211313C1 (en) 2006-01-30 2007-01-30 Compositions and methods for treating collagen-mediated diseases
EP18209918.4A EP3508571B1 (en) 2006-01-30 2007-01-30 Compositions suitable for treating collagen-mediated diseases
EP07762860.0A EP1987141B8 (en) 2006-01-30 2007-01-30 Compositions suitable for treating collagen-mediated diseases
EP12155233.5A EP2474321B1 (en) 2006-01-30 2007-01-30 Compositions suitable for treating collagen-mediated diseases
ES07762860T ES2709202T3 (en) 2006-01-30 2007-01-30 Suitable compositions for the treatment of collagen-mediated diseases
CA2637262A CA2637262C (en) 2006-01-30 2007-01-30 Compositions and methods for treating collagen-mediated diseases
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IL192878A IL192878A (en) 2006-01-30 2008-07-17 Clostridium histolyticum collagenase i and collagenase ii, drug comprising the same and process for producing said drug
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