Soft sensor for viable cell counting by measuring dynamic oxygen uptake rate.

Regulatory authorities in biopharmaceutical industry emphasize process design by process understanding but applicable tools that are easy to implement are still missing. Soft sensors are a promising tool for the implementation of the Quality by Design (QbD) approach and Process Analytical Technology (PAT). In particular, the correlation between viable cell counting and oxygen consumption was investigated, but problems remained: Either the process had to be modified for excluding CO2 in pH control, or complex kLa models had to be set up for specific processes. In this work, a non-invasive soft sensor for simplified on-line cell counting based on dynamic oxygen uptake rate was developed with no need of special equipment. The dynamic oxygen uptake rates were determined by automated and periodic interruptions of gas supply in DASGIP® bioreactor systems, realized by a programmed Visual Basic script in the DASware® control software. With off-line cell counting, the two parameters were correlated based on linear regression and led to a robust model with a correlation coefficient of 0.92. Avoidance of oxygen starvation was achieved by gas flow reactivation at a certain minimum dissolved oxygen concentration. The soft sensor model was established in the exponential growth phase of a Chinese Hamster Ovary fed-batch process. Control studies showed no impact on cell growth by the discontinuous gas supply. This soft sensor is the first to be presented that does not require any specialized additional equipment as the methodology relies solely on the direct measurement of oxygen consumed by the cells in the bioreactor.

A step closer to continuous buffer preparation from solids: Predicting powder compaction and how to prevent it.

The preparation of buffer solutions used in the biopharmaceutical industry is typically performed manually by the addition of one or multiple buffering reagents to water. Recently, the adaptation of powder feeders for continuous solid feeding was demonstrated for continuous buffer preparation. However, the intrinsic characteristics of powders can change the stability of the process, due to the hygroscopic nature of some substances and humidity-induced caking and compaction behavior, but there is no simple and easy methodology available for predicting this behavior for buffer species. To predict which buffering reagents are suitable without special precautions and investigate their behavior, force displacement measurements were conducted with a customized rheometer over 18 h. While most of the eight investigated buffering reagents indicated uniform compaction, especially sodium acetate and dipotassium hydrogen phosphate (K2HPO4) showed a significant increase in yield stress after 2 h. Experiments conducted with a 3D printed miniaturized screw conveyor confirmed the increased yield stress measurements by visible compaction and failure of the feeding. By taking additional precautions and adjusting the design of the hopper, we demonstrated a highly linear profile of all buffering reagents over a duration of 12 and 24 h. We showed that force displacement measurements accurately predict the behavior of buffer components in continuous feeding devices for continuous buffer preparation and are a valuable tool to identify buffer components that need special precautions. Stable, precise feeding of all tested buffer components was demonstrated, highlighting the importance of identifying buffers that need a specialized setup with a rapid methodology.

In-situ gradient formation by direct solid addition of buffer components.

Buffer preparation and storage requires a significant facility footprint in large scale bioprocessing and together with the costs of supply chain management can have a substantial economic impact. In-line buffer mixing in chromatography is commonly performed by blending different buffer solutions using at least two pumps and a static or dynamic mixer. We developed a device for an in-line gradient delivery of buffering agents directly from solids to be applied for chromatographic separation processes. A solid feeding device with a screw conveyor and a hold tank for the solids was designed and a miniaturized system was 3D printed. The coefficient of variation for the precision of the solid feeding of 5 different buffering agents was below 5% even for very small solid flow rates necessary for lab-scale chromatography. Stability was demonstrated by a constant linear solid feed at a very low dosing rate of 0.05 g.min-1 over 24 hours. We demonstrated the suitability for chromatography by directly connecting the system to a standard chromatography workstation for protein chromatography. The solids were fed into a miniaturized continuously stirred tank reactor connected to an ÄKTA purification system. The performance of the in-line gradient delivery of buffering agents directly from solids was compared to conventional in-line buffer mixing. We were able to achieve highly linear gradients for elution using only one pump of a chromatographic system, generating the gradient by the direct addition of solids avoiding the necessity of additional pumps and hold tanks. By direct conditioning of buffers and the addition of solids a simple, just in time, at site preparation of buffers was possible. The design of the feeding unit for solid addition for buffer preparation is easily scalable and adaptable to work with or as a replacement for already existing in-line dilution or conditioning units.

Economics and ecology: Modelling of continuous primary recovery and capture scenarios for recombinant antibody production.

With the maturation of antibody production technologies, both economic optimization and ecological aspects have become important. Continuous downstream processing is a way to reduce the environmental footprint and improve process economics. We compared different primary recovery, capture, and fermentation methods for two output-based antibody production scales: 50 kg/year and 1000 kg/year. In addition, a fixed fermentation volume case of 1000 L was analysed in terms of total cost of goods and process mass intensity as a measure of the environmental footprint. In our scenario, a significant amount of water can be saved in downstream processing when single use equipment is utilized. The overall economic and ecological impact is governed by the product titre in our perfusion (1 g/L) and fed-batch (4 g/L). A low titre in fermentation with similar downstream purification leads to higher process mass intensity and cost of goods due to the higher media demand upstream. The economic perspective for continuous integrated biomanufacturing is very attractive, but environmental consequences should not be neglected. Here, we have shown that perfusion has a higher environmental footprint in the form of water consumption compared to fed-batch. As general guidance to improve process economics, we recommend reducing water consumption.