Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07K—PEPTIDES
  • C07K14/00—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof
  • C07K14/435—Peptides having more than 20 amino acids; Gastrins; Somatostatins; Melanotropins; Derivatives thereof from animals; from humans
  • C07K14/52—Cytokines; Lymphokines; Interferons
  • C07K14/555—Interferons [IFN]
  • C07K14/57—IFN-gamma

Definitions

• the invention relates to a process for producing purified, biologically active, 'free form' of recombinant human interferon gamma (HIG) by cytoplasmic expression in Escherichia Coli, as bacterial host.
• HOG human interferon gamma
• Interferons are a group of proteins produced by the cells of most of the vertebrates and characterized by their ability to inhibit the growth of viruses exposed to these proteins. Interferon proteins have been classified into three types - alpha, beta and gamma based on physiological functions, antigenicity and structural differences. Interferon gamma has number of characteristics that differentiate it from alpha and beta forms of interferons. Among these differences are antigenic distinctiveness and greater activity with regard to immunoregulation and antitumor effects. Human interferon gamma may be produced by T-lymphocytes, stimulated by mutagens or by antigens to which they are sensitized. It may also be obtained through cloning and expression techniques well known to the art.
• the lymphocyte route for the production of human interferon gamma involves costly chemicals (viz. fetal calf serum, micronutrients), fermenter design, and a quality check on the lymphocyte cell lines used (without any mycoplasma/viruses which need to be checked for every batch and stock).
• the quantity (yield) of HIG produced is very low, fermentation cycle is more than 15 days to harvest the broth for purifying the HIG.
• the infrastructure facility required for the production of HIG through the lymphocyte route is also cumbersome. Recombinant DNA technology has permitted the expression of exogenous or foreign proteins in bacteria and other host cells.
• the cultures were grown in fermenter with sufficient agitation and aeration to achieve a growth rate of 60 to 90 min per cell division; glucose was fed to the cultures to maintain growth, but did not exceed 50 g per liter during the fermentation, and the pH of the cultures was controlled at 6.8-7.2 by NaOH or (NH OH.
• IAA indole acrylic acid
• IPA indole propionic acid
• Gray et.al. (US Patent Nos.5,574,137, 5,595,888, 5,690,925) also discloses production of recombinant human interferon gamma in a fermenter with a working volume of about 10 to 1000 lit.
• the fermentation is carried out at 25°C to 40°C under conditions of agitation (100 to 1000 rpm) and aeration (0.5 to 1.5 wm) at a pH between 6,5 to 7.5.
• an expression and purification scheme for biologically active interferon gamma which allows correct folding in vivo, is highly desirable.
• the subject invention surprisingly finds that expression by a combination of reduced temperature and low inducer concentration results in more than 15% 'free-form' of biologically active interferon gamma.
• interferon gamma containing cells so obtained are liberated from the host cells by various means such as osmotic shock, ultrasonic vibration, grinding or by high shear disruption and then processed to isolate the interferon gamma. The insoluble debris is separated by centrifugation and the interferon gamma containing supernatant is collected for purification.
• free-form as used in description and claims of the instant application means the state of the protein namely human interferon gamma which exists in a non-aggregate, soluble form inside the cell in the cytosol.
• the invention provides a sequence of bioprocess steps for the production and purification of recombinant human interferon gamma in biologically active form.
• the first object of the invention is to produce biologically active "free form" human interferon gamma in high yield and quality by using recombinant DNA technology.
• the other object of the invention is to produce human interferon gamma in active form which allows correct folding in vivo.
• Yet another object of the invention is to provide a purification scheme with least degradation or aggregation of the molecules of human interferon gamma so produced and recovery of the interferon gamma in high purity and activity.
• the invention establishes conditions at which proteins are synthesized in Escherichia coli cells and fold in vivo into the correct conformation with improved yield and quality (homogenous structure) of the protein with very low antigenicity.
• Lower expression rates induced by a combination of a low incubation temperature and inducer concentration besides other operational parameters in the fermenter allow a correct in vivo folding of the protein.
• More than 15% of the interferon gamma remains in soluble/free-form in the cytoplasm of the bacterial cell.
• the advantage of this system is a higher yield after purification and the recovery of active, structurally homogeneous population of the protein.
• the present invention provides for a process for producing purified, biologically active, 'free form' of recombinant human interferon gamma (HIG) by cytoplasmic expression in Escherichia coli (E. coli) as bacterial host, comprising the steps of : a) Growing a culture of E.
• HOG human interferon gamma
• Fig 1 Bioprocess flow diagram of interferon gamma purification process of the present invention.
• Fig 2 Bioprocess flow diagram of a preferred embodiment of the present invention.
• Fig 3 Shows the results of SDS-PAGE (Sodium Dodecyl Sulphate -
• the present invention provides a process for the biosynthesis and purification of the recombinant human interferon gamma.
• interferon gamma is produced at a lower temperature and inducer concentration in Escherichia coli cells transformed with a plasmid carrying the gene for interferon gamma, grown in a culture, and expressing the gene in the form of interferon gamma protein.
• Such cells generally show a degree of expression of interferon gamma ranging from 10 to 40% of total cellular protein content. This controlled expression leads to the formation of recombinant human interferon gamma in "free form' within the cells.
• the production of recombinant human interferon gamma using Escherichia coli is carried in batches ranging from volume of 100 ml to 5000 ml. After fermentation, the interferon containing Escherichia coli cells are recovered from the broth for isolation and purification. The following is the description for the fermentation and cell recovery process. Preparation and maintenance of stock cultures
• a stock culture is prepared jn sterile culture flasks containing 10 to 50 ml of sterile Luria Broth medium.
• This medium is then inoculated with primary culture of Escherichia coli.
• the inoculated flask is then incubated on a shaker at 25°C to 37°C, until the absorbance at 600 nm reaches approximately 0.6 to 1.0 OD.
• This culture is added to a glycerol mixture in 1:1 ratio.
• the inoculum is prepared in sterile medium having the following composition :
• the inoculum is incubated in shake flasks at about 37°C for approximately 8 to 10 hours.
• the inoculum is transferred to a fermentor.
• the volume of the inoculum is between 2 to 10% of the volume of the fermentor. Fermentation :
• Recombinant human interferon gamma fermentation is carried out in fermentors with
• the fermentation medium is composed of
• Ingredients in the medium are sterilized by heat treatment or filtration prior to use in
• the fermentation is carried out at 22 °C to 30°C.
• Other operating conditions are as follows:
• the other inducers which can be used includes IAA (Indole Acrylic Acid), IPA (Indole Propionic Acid), Lactose, etc. Purification :
• the cells are inactivated by one of the standard methods e.g. by addition of a chemical killing agent such as 0.25% benzyl alcohol.
• a chemical killing agent such as 0.25% benzyl alcohol.
• concentrated Escherichia coli cells are in a medium containing salts in appropriate buffer (after the buffer exchange in the primary clarification step) in the pH range of 6.0 to 9.0 preferably 8.
• Recombinant human interferon gamma is extracted by cell disruption of the cell suspension in a high-pressure homogenizer such as APN Gaulin-30 CD. The homogenization is carried out in three passes of 600 bar each. The temperature of the homogenate was maintained below 25 °C by chilled jacket. Then the final homogenate is centrifuged using the Beckman Avanti J 30-1 centrifuge at 20,000 g for 20 minutes at 4°C. The resulting supernatant contains the 'free form' interferon gamma to the concentration of 15% and above.
• step gradient with buffer (0.4 M ⁇ aCl, 20 mM sodium phosphate buffer, pH 8.0), 2 column volumes at flow rate of 2-4 ml/min, and c) a linear gradient with buffer (0.4 M to 0.8 M ⁇ aCl, 20 njM sodium phosphate buffer, pH 8.0) five column volumes, at 2-4 ml min flow rate.
• interferon gamma is eluted at 0.4 to 0.6 M NaCl concentration in the linear gradient step (steps).
• the eluants off the column are monitored by SDS-PAGE and the fractions containing pure interferon gamma are pooled for dialysis (against 2-10 mM succinic acid with 0.9% NaCl at pH of 5.0 to 5,5 for 36 to 50 hours at 4°C to 8 °C or gel-filtration using SG-75 ® matrix (Amersham Pharmacia).
• the dialyzed solution is then centrifuged at 20,000 g for 10 minutes.
• the resulting supernatant is then diluted with the same buffer as used for SDS-PAGE monitoring to a final protein concentration of 0.4 to 0.8 mg/ml.
• the solution of purified interferon gamma is
• the procedure results in a pure, biologically active recombinant human interferon gamma.
• the novel procedure has consistently produced interferon gamma, having purity above 95% and yield in excess of 5% of total cell protein.
• This purified, homogeneous recombinant human interferon gamma produced according to the invention may be utilized in the therapeutic treatment of viral infection, tumor or cancer as well as in immuno modulation application methods.

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• 2000
  • 2000-02-01 IN IN49CA2000 patent/IN187900B/en unknown
  • 2000-03-20 BR BR0007186-2A patent/BR0007186A/pt not_active IP Right Cessation
  • 2000-03-20 AU AU31854/00A patent/AU3185400A/en not_active Abandoned
  • 2000-03-20 EP EP00909574A patent/EP1171603A1/en not_active Withdrawn
  • 2000-03-20 WO PCT/IB2000/000318 patent/WO2001057218A1/en not_active Application Discontinuation

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