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The objective of this research was to study the atypical secondary drying dynamics observed during the freeze-drying of a formulation consisting of mannitol, disaccharide, and sodium chloride, where "bursts" of water vapor release were observed during secondary drying as detected by comparative pressure measurement. "Thief" samples were removed at the end of primary drying and during secondary drying as the shelf temperature was increased in a stepwise fashion. These samples were examined by X-ray powder diffraction and thermal analysis. From the X-ray powder diffraction data, we determined that mannitol crystallized predominantly as its hemihydrate. The physical state of mannitol changed from the hemihydrate form to anhydrous forms during secondary drying. Investigation of the effect of excipients on mannitol crystallization demonstrated that sodium chloride (at 225 mM, 1.3% w/v) had the greatest influence on hemihydrate crystallization, followed by trehalose and sucrose. However, only negligible hemihydrate formation was observed when mannitol was freeze-dried either by itself or in the presence of 150 mM sodium chloride and no hemihydrate in the presence of 75 mM sodium chloride. In general, a combination of a disaccharide and sodium chloride promoted the hemihydrate formation to a greater extent than the individual components. Comparative pressure measurement was demonstrated to be an effective tool to monitor mannitol hemihydrate dehydration during secondary drying., (Copyright © 2017 American Pharmacists Association®. Published by Elsevier Inc. All rights reserved.)

The purpose of this study was to investigate the effect of sucrose-glycine excipient systems on the stability of selected model proteins during lyophilization. Recovery of protein activity after freeze-drying was examined for the model proteins lactate dehydrogenase and glucose 6-phosphate dehydrogenase in a sucrose-glycine-based excipient system in which the formulation composition was systematically varied. In a sucrose-only excipient system, activity recovery of both model proteins is about 80% and is independent of sucrose concentration over a range from 1 to 40 mg/mL. When both sucrose and glycine are used and the ratio of the 2 excipients is varied, however, activity recovery decreases in a pattern that is consistent with the inhibition of activity recovery by glycine crystals, despite the presence of an adequate amount of sucrose to afford protection. Annealing of sucrose-glycine formulations causes a small but significant decrease in activity recovery relative to unannealed controls, whereas no annealing effect is observed with sucrose-only formulations. Addition of 0.01% polysorbate 80 to the formulation resulted in complete recovery of activity, irrespective of the sucrose-glycine ratio or annealing. Addition of the same concentration of polysorbate 80 to the reconstitution medium caused an increase in activity recovery for each formulation, but the overall pattern remained unchanged. The data are consistent with an interfacial model for lyophilization-associated loss of protein activity involving denaturation at a solid/freeze-concentrate interface.

Given the increasing importance of reducing development time for new pharmaceutical products, formulation and process development scientists must continually look for ways to "work smarter, not harder." Within the product development arena, this means reducing the amount of trial and error empiricism in arriving at a formulation and identification of processing conditions which will result in a quality final dosage form. Characterization of the freezing behavior of the intended formulation is necessary for developing processing conditions which will result in the shortest drying time while maintaining all critical quality attributes of the freeze-dried product. Analysis of frozen systems was discussed in detail, particularly with respect to the glass transition as the physical event underlying collapse during freeze-drying, eutectic mixture formation, and crystallization events upon warming of frozen systems. Experiments to determine how freezing and freeze-drying behavior is affected by changes in the composition of the formulation are often useful in establishing the "robustness" of a formulation. It is not uncommon for seemingly subtle changes in composition of the formulation, such as a change in formulation pH, buffer salt, drug concentration, or an additional excipient, to result in striking differences in freezing and freeze-drying behavior. With regard to selecting a formulation, it is wise to keep the formulation as simple as possible. If a buffer is needed, a minimum concentration should be used. The same principle applies to added salts: If used at all, the concentration should be kept to a minimum. For many proteins a combination of an amorphous excipient, such as a disaccharide, and a crystallizing excipient, such as glycine, will result in a suitable combination of chemical stability and physical stability of the freeze-dried solid. Concepts of heat and mass transfer are valuable in rational design of processing conditions. Heat transfer by conduction--the dominant mechanism of heat transfer in freeze-drying--is inefficient at the pressures used in freeze-drying. Steps should be taken to improve the thermal contact between the product and the shelf of the freeze dryer, such as eliminating metal trays from the drying process. Quantitation of the heat transfer coefficient for the geometry used is a useful way of assessing the impact of changes in the system such as elimination of product trays and changes in the vial. Because heat transfer by conduction through the vapor increases with increasing pressure, the commonly held point of view that "the lower the pressure, the better" is not true with respect to process efficiency. The optimum pressure for a given product is a function of the temperature at which freeze-drying is carried out, and lower pressures are needed at low product temperatures. The controlling resistance to mass transfer is almost always the resistance of the partially dried solids above the submination interface. This resistance can be minimized by avoiding fill volumes of more than about half the volume of the container. The development scientist should also recognize that very high concentrations of solute may not be appropriate for optimum freeze-drying, particularly if the resistance of the dried product layer increases sharply with concentration. Although the last 10 years has seen the publication of a significant body of literature of great value in allowing development scientists and engineers to "work smarter," there is still much work needed in both the science and the technology of freeze-drying. Scientific development is needed for improving analytical methodology for characterization of frozen systems and freeze-dried solids. A better understanding of the relationship between molecular mobility and reactivity is needed to allow accurate prediction of product stability at the intended storage temperature based on accelerated stability at higher temperatures. This requires that the temperature dependence of glass transition-associated mobility, particularly at temperatures below the glass transition, be studied in greater depth. The relevance of the concept of strong and fragile glasses to frozen systems and freeze-dried solids has only begun to be explored. The list of pharmaceutically acceptable protective solutes is very short, and more imagination--and work--is needed in order to develop pharmaceutically acceptable alternative stabilizers. There is a need for technology development in process monitoring, particularly in developing a way to measure the status of the product during freezing and freeze-drying without placing temperature measurement probes in individual vials of product. The current practice of placing thermocouples in vials is uncertain with respect to reliability of the data, inconsistent with elimination of personnel in close proximity to open vials of product in an aseptic environment, and incompatible with technology for automatic material handling in freeze-drying. In addition, a method for controlling the degree of supercooling during freezing would allow better control of freezing rate and would, in many cases, result in more consistent product quality.

The objective of this research was to gain a better understanding of the degree to which recovery of activity of model proteins after freeze-drying can be maximized by manipulation of freeze-dry process conditions in the absence of protective solutes. Catalase, beta-galactosidase and lactate dehydrogenase (LDH) were used as model proteins. All of the three proteins exhibited a concentration-dependent loss of activity after freezing, with significantly higher recovery at higher concentration. The freezing method and the type of buffer were also important, with sodium phosphate buffer and freezing by immersion of vials in liquid nitrogen associated with the lowest recovery of activity. Differential scanning calorimetry was predictive of the onset of collapse during freeze-drying only for beta-galactosidase. For the other proteins, either no Tg' transition was observed, or the apparent glass transition did not correlate with the microscopically-observed collapse temperature. The time course of activity loss for beta-galactosidase and LDH was compared during freeze-drying under conditions which produced collapse of the dried matrix and conditions which produced retention of microstructure in the dried solid. Recovery of activity decreased continuously during primary drying, with no sharp drop in recovery of activity associated with the onset of collapse. The most important drying process variable affecting recovery of activity was residual moisture level, with a dramatic drop in activity recovery associated with residual moisture levels less than about 10%.

Freeze drying provides a valuable tool to the formulation scientist by permitting dehydration of heat-sensitive drugs and biologicals at low temperature. The final product is quickly and easily reconstituted, and the process is compatible with aseptic operations. Freezing is a critical step, since the microstructure established by the freezing process usually represents the microstructure of the dried product. The product must be frozen to a low enough temperature to be completely solidified. If the solute crystallizes during freezing, this temperature is the eutectic temperature. If the solute remains substantially amorphous with freezing, the relevant temperature is the collapse temperature. Understanding the physical form of the solute--crystalline or amorphous--after freezing can be important from the standpoint of drying characteristics, appearance of the final product, and even product stability during storage. Supercooling is a significant factor in freezing of formulations intended for freeze drying--prior to both primary and secondary (eutectic) crystallization. The driving force for freeze drying is the difference in vapor pressure of ice between the sublimation zone and the condenser. Because the vapor pressure of ice increases sharply with increased product temperature, it is important from the standpoint of process efficiency to maintain product temperature as high as possible during primary drying without damaging the product. The upper limit of product temperature during primary drying again depends on the physical form of the solute. Exceeding either the eutectic temperature (crystalline solute) or the collapse temperature (amorphous solute) results in loss of the desirable properties of a freeze dried product. Freeze drying is a coupled heat and mass transfer process, where either heat transfer or mass transfer may be rate limiting with respect to the overall drying rate. Heat transfer is often the rate-limiting transfer operation because of the high heat of sublimation of ice and the inefficiency of heat transfer. Conduction is the primary mechanism of heat transfer, as opposed to convection or thermal radiation. The rate-limiting resistance to heat transfer is usually the interfacial, or contact, resistance caused by poor contact between materials--the heated shelf, metal trays, and the bottom surface of glass vials. Since the thermal conductivity of a gas is directly proportional to pressure in the free molecular flow regime, the chamber pressure during primary drying is an important determinant of the overall heat transfer rate. As a result, the drying rate for a heat transfer-limited process increases sharply with chamber pressure up to a pressure where free molecular flow conditions no longer apply.(ABSTRACT TRUNCATED AT 400 WORDS)