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The purification of human chymotrypsinogen B (hCTRB) after expression and secretion by the yeast Pichia pastoris is described based on two different approaches using integrated initial recovery. Extraction employing aqueous two-phase systems (ATPS) from poly(ethylene glycol) and sodium sulfate allows direct processing of cell containing yeast suspensions of 50% wet weight. The target protein is obtained partially purified in the top phase while cells and cell debris are partitioned to the bottom phase of the system. hCTRB is further purified by adsorption from the top phase to the cation exchanger SP Sepharose Big Beads and elution in a salt step. The single step isolation of hCTRB is possible by expanded bed adsorption (EBA) using a fluidized cation exchanger (Streamline SP XL). A design strategy is shown taking both target protein binding and stable fluidization of the stationary phase in cell containing suspensions into consideration. For the example of hCTRB isolation from cell containing P. pastoris suspensions, a successful use of this strategy is demonstrated. Both initial recovery strategies deliver a product that can be further purified and formulated by ultrafiltration/diafiltration followed by lyophilization, resulting in a homogeneous product. Scale-up to 30-90 L of culture suspension was shown for both methods, resulting in a product of similar quality. Comparing both strategies reveals that the two-step ATPS route is better suited for high cell density cultures, while the single step EBA method is preferred for cultures of moderate cell density. This is due to the fact that application of EBA is restricted to suspensions of 10-12.5% wet weight cell concentration, thus necessitating dilution of the original broth prior to sample application. The data presented show that integrated recovery operations are a valuable alternative to traditional processing for systems that are problematic during initial solid-liquid separation.

To achive the coarse purification of a monoclonal antibody from whole hybridoma fermentation broth a fluidized bed cation exchange process was used. The procedure consisted of application of the crude sample and washing of the bed in a fluidized mode and elution in a fixed bed mode. A completely clarified eluate was obtained with purification factors between 4 and 8 and a concentration of the desired product (monoclonal antibody) by a factor of more than 3 was achived. Thus, a combination of the three early steps of the downstream process clarification, concentration and coarse purification was possible. Two different materials were tested: a commercially available agarose-based matrix (Stream-line-SP), and a self-derivatized material based on controlled-pore glass (Bioran). Initial experiments were performed to describe the fluidization of the glass material. Comparison with the agarose material showed several differences, the agarose matrix allowing liquid flow closer to plug flow than the glass material. Increased backmixing in the liquid phase was detected when fluidizing the glass adsorbent compared with the agarose-based matrix. Despite this fact, comparison of the two materials with respect to antibody binding and elution demonstrated a similar performance. (c) 1995 John Wiley & Sons, Inc.

Cyclohexadiene-trans-5,6-diols such as (S,S)-2,3-dihydroxy-2,3-dihydrobenzoic acid (2,3-trans-CHD) have been shown to be of importance as chiral starting materials for the syntheses of bioactive substances, especially for the syntheses of carbasugars. By using methods of metabolic-pathway engineering, the Escherichia coli genes entB and entC, which encode isochorismatase and isochorismate synthase, were cloned and over-expressed in E. coli strains with a deficiency of entA, which encodes 2,3-dihydroxybenzoate synthase. A 30-fold increase in the corresponding EntB/EntC enzyme activities affects the accumulation of 2,3-trans-CHD in the cultivation medium. Although the strains did not contain deletions in chorismate-utilising pathways towards aromatic amino acids, neither chorismate nor any other metabolic intermediates were found as by-products. Fermentation of these strains in a 30 L pH-controlled stirred tank reactor showed that 2,3-trans-CHD could be obtained in concentrations of up to 4.6 g L(-1). This demonstrates that post-chorismate metabolites are accessible on a preparative scale by using techniques of metabolic-pathway engineering. Isolation and separation from fermentation salts could be performed economically in one step through anion-exchange chromatography or, alternatively, by reactive extraction. Starting from 2,3-trans-CHD as an example, we established short syntheses towards new carbasugar derivatives.