Polyacrylic acid based plasma fractionation for the production of albumin and IgG: Compatibility with existing commercial downstream processes.

Commercial fractionation of human plasma into immunoglobulin- and albumin-rich fractions is often initiated with sequential cold ethanol-based precipitation methods, which have changed little over the past 70 years. The required low temperature (-4 to -8°C) and high concentrations of ethanol 8-40%) necessitate large-scale fixed processing lines, and major capital investment and operating costs. The resulting fractions are then further purified by ethanol based precipitation or chromatographic procedures to obtain the purified final product. Aqueous polyacrylic acid (PAA) based precipitation, which readily interfaces with existing downstream processing, could offer advantages with respect to cost, safety, environmental impact, and flexibility. Sequential precipitation with 7%, 12%, and 20% (w/v) solutions of PAA 8000 in the presence of a kosmotropic salt (sodium citrate) gave fibrinogen-, immunoglobulin-, and albumin-rich fractions with 80-90% yield and 64%, 55%, and 82% purity, respectively. Further purification of the IgG-rich precipitate by caprylic acid precipitation and anion exchange chromatography, achieved a target purity of >99%. This was also achieved for the downstream processing of the albumin-rich precipitate using a two-step ion exchange chromatographic procedure. This work shows that PAA precipitation can be used in place of cold ethanol precipitation to generate crude IgG and albumin fractions which can be purified to final products of acceptable purity.

Development of an intermediate chromatography step in an insulin purification process. The use of a High Throughput Process Development approach based on selectivity parameters.

Recent innovations in designing purification processes for biopharmaceutical production have enabled initial screening (optimization) of chromatographic conditions for binding to be performed in miniaturized batch format. The present report demonstrates the possibility of using this format to screen for selectivity and illustrates the need for careful adjustment of protocols when highly abundant, tightly-binding impurities are present in the sample. This batch format approach was used to choose a chromatography medium (resin) from a selection of available resins for the purification of recombinant insulin expressed in E. coli and to screen binding and elution conditions. Subsequent optimization was performed in small packed columns using a Design of Experiments (DoE) approach with statistical modeling before scaling up to a small pilot scale experiment. In this study insulin was effectively purified from the more tightly-binding C-peptide, and a reduction in insulin variants was also noted using the optimized conditions.

Purification of a synthetic oligonucleotide by anion exchange chromatography: method optimisation and scale-up.

A single-step chromatographic method for purification of a synthetic 20-mer oligonucleotide is described. Method optimisation was conducted at laboratory scale where 30 mg crude sample was purified per run with a yield of 17 mg pure oligonucleotide. The protocol was scaled-up in steps to achieve 5-, 58- and a final 230-fold scale-up. At the final scale, 7.0 g of crude material was purified with a yield of 4.1 g product. The purity of the oligonucleotide was in all scales higher than 97%. The cycle time was 110 min, which corresponds to a purification capacity of about 90 g crude oligonucleotide material per 24 h.