Patent Application
20200223886
Present invention relates to downstream processing of biologics, more specifically, to downstream processing of Insulin and its analogues. Present invention further relates to integration of crystal separation, followed by crystal washing and freeze-drying into a single continuous process for purification of insulin and its analogues.
Traditionally, preparative protein crystallization involves a series of washing (of the settled crystals) and gravity settling steps. The end product of preparative protein crystallization is further processed by vacuum assisted freeze-drying to obtain the drug substance (DS) in dry powder form. The resultant drug substance must conform to purity by residual substance (RS) analysis, moisture content (LOD-Loss on Drying), sulphated ash content (ROI) and residual solvent limits as per universal quality and regulatory specifications. The entire process of preparative crystallization, settling of the crystals in the tank and washing to meet the desired quality requirements and freeze-drying requires a minimum of 7 days at commercial scale. Evidently, the discontinuous and modular nature of this process makes it energy, cost and time intensive.
Methods of crystallization and purification of insulin or insulin analogs have been disclosed in WO2015084694, U.S. Pat. No. 8,769,841, WO1996040730, CN103512318 and U.S. Pat. No. 6,408,536.
WO2015084694 describes a method for crystallizing insulin or insulin analogues under alkaline conditions and purifying the crystals by filtering through a filter and drying the crystals captured on the filter to produce crystalline insulin or insulin analogue crystal compositions. After crystallization, the entire volume of decanted crystal suspension is then transferred to a filter apparatus. The filter apparatus described in WO2015084694 is an agitated Nutsche filter, which have a stainless steel screen with a pore size about 5 μm.
U.S. Pat. No. 8,769,841 discloses a process of freeze drying of an essentially aqueous solution comprising at least one first step having a first temperature and pressure level (i.e. primary drying phase) and at least one second step having a second temperature and pressure level following the first step (i.e. secondary drying phase).
WO1996040730 disclose a method for recovering an acylated protein, those that resist recovery by precipitation or crystallization and subsequent filtration from aqueous solutions, as a powder. Acylated proteins are certain acylated proinsulins, insulins and insulin analogues. The method comprises of combination adjusting the aqueous solution to near the isoelectric pH of the protein and providing a suitable alcohol concentration to cause precipitation of the protein in the form of filterable particles at the adjusted pH.
CN103512318 disclose a drug purification drying process that relates to a lyophilized processing of insulin wherein the process discloses a freeze-drying process for insulin. The impurity content is lower than conventional technology. This process avoids the use of organic solvents, eliminating the potential adverse effects on people and the environment, and saying the drying time of 2-3 days and improve industrial productivity.
U.S. Pat. No. 6,408,536 disclose a process for drying protein crystals from an aqueous protein crystal suspension. The process comprises of filtering off the crystals from an aqueous suspension, washing the filter cake, spin-drying the same, drying the crystals in the fluidized bed with a stream of moistened nitrogen and emptying the dried crystals using a nitrogen pressure surge into a flanged container.
Though several methods are available for crystallizing insulin and its analogues, there is a need to develop an alternative method to have simple and optimized process of crystallization, washing and separation of the crystal as well as drying the same which can be practised in the industry in a bigger scale equipment which works on the same principle.
The present invention offers an integrated simple process for separation and drying of insulin and its analogues.
The object of present invention is to integrate the discrete processes of crystallization, washing of the crystals and freeze-drying into a single continuous process using pressure filtration while achieving comparable standards of critical quality attributes and process performance attributes.
The present invention describes the integration of preparative Insulin and Insulin analogues crystallization, crystal separation and freeze-drying processes into single continuous process using pressure filtration. The process facilitates time reduction, and outlines the novel design of using multiple organic solvent washes and nitrogen gas purging for the removal of imbibed water and achieve final drug substance that meets the major quality specifications.
The term ‘crystal suspension’ refer to a volume of solution prepared by addition of Zinc Chloride (ZnCl2) to insulin or insulin analogue followed by pH adjustment in the range of 4.5-8.5 using acid/alkali. Addition of zinc improves the physical stability of insulin by multimerization.
The term ‘filter’ refer to a simple set up that is similar to a ‘Buchner funnel’ with the pore size of filter membrane used varying between ‘1-15 μm’ which does not involve any centrifugal force. The term ‘pressure filtration’ refer to a solid-liquid filtration aided by controlled pressure that pushes the solution against a filter membrane so that the solid substance (crystalline insulin and insulin analogue) is retained as a cake while the (organic solvent) mother liquor passes through as permeate. This exogenous pressure results in increased effective flow rate, high pressure gradient across the membrane and use of inert gas ensures stability to the finished product. Pressure filtration is an instantaneous process with an operating time of between 2-5 minutes on a lab scale and 45-60 minutes on an industrial scale.
The term ‘insulin’ or ‘insulin analogue’ refer to 51 amino acid peptide hormone used for treatment of diabetes. It also refers to other insulin related forms such as insulin precursor or insulin analogue precursor, intermediate insulin or insulin analogue molecules obtained during downstream processes.
Insulin and insulin analogues were expressed extracellularly using a recombinant Pichia based fermentation process. Transformed Pichia pastoris yeast strain are fermented in culture medium. The secreted Insulin or Insulin analogues were recovered by method of chromatography.
Insulin and insulin analogue was crystallized from the chromatography elution pool. It was further made into crystal suspension in presence of Zinc Chloride (ZnCl2) and at an appropriate pH (in the range of 4.5 to 8.5) by addition of acid or alkali. Profile of crystal suspension (percentage solids, purity) was determined. The resultant insulin or insulin analogue crystals had high purity. Entire volume of crystal suspension was washed with water to remove the free precipitant used for crystallization and was taken forward for further processing of freeze drying.
The crystal suspension was first processed for separation through pressure filtration process to obtain the dried cake. This separation process is devoid of gravity and centrifugal force. The dried cake had imbibed water, which is removed by steps of washing by organic solvent and purging nitrogen gas through it.
The single continuous process can be depicted in following four steps.
Similar integration of crystal separation, washing and drying can be performed at multiple preceding crystallization step during the downstream processing of insulin and insulin analogues. The raw material(s), reagent(s) and equipment(s) were used as per listed below in table 1, 2 and 3 respectively.
The trials were performed in a lab scale pressure filter set up with an approximate filter cross-sectional area of 80 cm2 to 100 cm2. It also comprises of a pressure inlet for compressed inert gas (Nitrogen), a pressure gauge and safety release valve, sample inlet and outlet ports and a water jacket (
Variable parameters were wash solvent, solvent volume, number of washes, time of nitrogen purging for each wash and an optional change of filter media, which is dependent on the size of crystals being processed. Process performance and quality attributes of the obtained drug substance were measured by analysing percentage of loss of crystals in permeate and loss on drying (LOD), purity and molecular weight (HMWP). The temperature of the set up was maintained in range of 25° C. to 35° C.
The cake formed by process of pressure filtration of insulin and insulin analogue crystal suspension, had requisite thickness and texture. However, the goal was to dry the cake to achieve acceptable standards of LOD and very importantly to integrate the crystallization-freeze drying of the conventional process into a single continuous process. To achieve sufficient displacement of imbibed residual water from filter cake, single or multiple wash strategies with different organic solvents were studied. The wash steps were also designed to enable effective removal of precipitants, and residual solvents that are present in reverse phase (chromatography) elution pool and obtain a drug substance that complies with the universal quality and regulatory specifications.
The assembly of instrument(s) for achieving the dried powder in continuous and automated manner was as follows:
Two trials were conducted. First, was preliminary screening (Trial I) and second (Trail II) was design of experiment (DOE).
Preliminary screening trials (trial 1) were performed in a lab scale prototype of industrial pressure filter (
Solvents and wash combinations yielding high percentage LOD (loss on drying) values in the above design were eliminated. Data set is presented in table 5 and table 6.
The captured data set in table 5 and table 6 suggested that the resultant insulin and insulin analogue drug substance has comparable quality attributes to the drug substance made from traditional crystallization-freeze drying process with optimal recovery of product (
Two washes of acetonitrile planned in Trail I has satisfactory outcome with respect to percentage LOD. However, to fall in-line with regulatory requirements a further reduction in LOD was desired. Parameters that were studied in this experimental setup included a) number of washes; b) drying time and c) temperature during filtration to study the probability of temperature accelerating the evaporation of the residual organic solvent trapped in filter cake. For Trail II (DOE), HMWP was also determined.
A full factorial experimental design along with the response data is presented in table 6. Fifty experiments were performed discretely as below (table 6).
The drug, substance from Trials 12, 23 and 34 had the lowest LOD values i.e. of less than 10% (table 7), while drug substance from trials 11 and 42 had LOD values less than 12%. There were no significant changes in purity and HMWP profiles, and per-step losses were found to be well within range.
The results of variability are also represented in
From the multivariate studies, it was found out that more number of washes with organic solvent (3>2>1) resulted in ample displacement of imbibed water from filter cake. Three washes including wash 1 at 10%, wash 2 at 5% or 10% and wash 3 at 5% or 10%, were found to be most effective in reducing LOD. Volume of washes can be fine-tuned further as per process requirements. Increased drying time helped in forcing out some solvent imbibed in the cake post-washing. Increasing the temperature during filtration did not reduce the LOD of the drug substance, but it did not significantly affect the profile of the drug substance either. Thus, the temperature was maintained in the range of 25° to 35° C. Based on this multivariate study further trials can be designed and executed to further reduce the LOD to <4%.
The results of this multivariate study were satisfactory and drew immediate attention to a novel process that is shorter, continuous, less resource intensive and automated.
| Number | Date | Country | Kind |
|---|---|---|---|
| 201741034158 | Sep 2017 | IN | national |
This application is a U.S. National Stage Entry of International Application No. PCT/IB2018/057204, filed Sep. 19, 2018, which claims priority to IN Application No. 201741034158, filed Sep. 26, 2017, each of which is incorporated herein by reference in its entirety.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/IB2018/057204 | 9/19/2018 | WO | 00 |
