Residence-time distribution model for twin-screw extruders

Prediction of the physical stability of amorphous solid dispersions: relationship of aging and phase separation with the thermodynamic and kinetic models along with characterization techniques

Introduction: Solid dispersion has been considered to be one of the most promising methods for improving the solubility and bioavailability of insoluble drugs. However, the physical stability of solid dispersions (SDs), including its aging and recrystallization, or phase separation, has always been one of the most challenging problems in the process of formulation development and storage.Areas covered: The high energy state of SDs is one of the primary reasons for the poor physical stability. The factors affecting the physical stability of SDs have been described from the perspective of thermodynamics and kinetics, and the corresponding theoretical model is put forward. We briefly summarize several commonly used techniques to characterize the thermodynamic and kinetic properties of SDs. Specific measures to improve the physical stability of SDs have been proposed from the perspective of prescription screening, process parameters, and storage conditions.Expert opinion: The separation of the drug from the polymer, the formation, and migration of drug crystals will cause the SDs to shift toward the direction of energy reduction, which is the intrinsic cause of instability. Furthermore, computational simulation can be used for efficient and rapid screening suitable for the excipients to improve the physical stability of SDs.

Validation of Model-Based Melt Viscosity in Hot-Melt Extrusion Numerical Simulation

A validation for the use of model-based melt viscosity in hot-melt extrusion numerical simulations was presented. Here, the melt viscosity of an amorphous solid dispersion (ASD) was calculated by using its glass transition temperature (T_g) and the rheological flow profile of the pure polymeric matrix. All further required physical properties were taken from the pure polymer. For forming the ASDs, four active pharmaceutical ingredients (APIs), that had not been considered in first place to establish the correlation between T_g and melt viscosity were examined. The ASDs were characterized in terms of density, specific heat capacity, melt rheology, API solubility in the polymeric matrix, and deviation from the Couchman⁻Karasz fit to, identify the influencing factors of the accuracy of the simulation using model-based melt viscosity. Furthermore, the energy consumption of the hot-melt extrusion (HME) experiments, conventional simulation, and simulation using model-based melt viscosity were compared. It was shown, with few exceptions, that the use of model-based melt viscosity in terms of the HME simulation did not reduce the accuracy of the computation outcome. The commercial one-dimensional (1D) simulation software Ludovic^® was used to conduct all of the numerical computation. As model excipients, vinylpyrrolidone-vinyl acetate copolymer (COP) in combination with four APIs (celecoxib, loratadine, naproxen, and praziquantel) were investigated to form the ASDs.

Inline Determination of Residence Time Distribution in Hot-Melt-Extrusion

In the framework of Quality-by-Design (QbD), the inline determination of process parameters or quality attributes of a product using sufficient process analytical technology (PAT) is a center piece for the establishment of continuous processes as a standard pharmaceutical technology. In this context, Twin-Screw-Extrusion (TSE) processes, such as Hot-Melt-Extrusion (HME), are one key aspect of current research. The main benefit of this process technology is the combination of different unit operations. Several of these sub-processes are linked to the Residence Time Distribution (RTD) of the material within the apparatus. In this study a UV/Vis spectrophotometer from ColVisTec was tested regarding the suitability for the inline determination of the RTD of an HME process. Two different measuring positions within a co-rotating Twin-Screw-Extruder were compared to an offline HPLC-UV as reference method. The obtained results were overall in good agreement and therefore the inline UV/Vis spectrophotometer is suitable for the determination of the RTD in TSE. An influence of the measuring position on repeatability was found and has to be taken into consideration for the implementation of PATs. An effect of the required amount of marker on process rheology is not likely due to the low Limit-of-Quantification (LoQ).

NANEX: Process design and optimization

Previously, we introduced a one-step nano-extrusion (NANEX) process for transferring aqueous nano-suspensions into solid formulations directly in the liquid phase. Nano-suspensions were fed into molten polymers via a side-feeding device and excess water was eliminated via devolatilization. However, the drug content in nano-suspensions is restricted to 30 % (w/w), and obtaining sufficiently high drug loadings in the final formulation requires the processing of high water amounts and thus a fundamental process understanding. To this end, we investigated four polymers with different physicochemical characteristics (Kollidon(®) VA64, Eudragit(®) E PO, HPMCAS and PEG 20000) in terms of their maximum water uptake/removal capacity. Process parameters as throughput and screw speed were adapted and their effect on the mean residence time and filling degree was studied. Additionally, one-dimensional discretization modeling was performed to examine the complex interactions between the screw geometry and the process parameters during water addition/removal. It was established that polymers with a certain water miscibility/solubility can be manufactured via NANEX. Long residence times of the molten polymer in the extruder and low filling degrees in the degassing zone favored the addition/removal of significant amounts of water. The residual moisture content in the final extrudates was comparable to that of extrudates manufactured without water.

Residence Time Distribution in a High Shear Twin Screw Extruder

The residence time distributions (RTD) of a high shear twin screw extruder were measured by an on–line UV fluorescence device. First, by increasing throughput (Q) and screw speed (N), a decrease of the complex viscosity of the studied polypropylene (PP) was observed, revealing chain scissions. It was associated to high viscous dissipation taking place during extrusion, and more particularly under high shear conditions. Then the impact of these experimental conditions on the RTD was carried out. As expected, an increase of usual throughputs and screw speeds decrease mostly the RTD characteristic data. In this study industrial rate have been studied: throughput varied from 1.5 up to 22 kg h−1 and screw speed varied from 200 min−1 up to 1 200 min−1. However, by increasing the screw speed over usual values (from 500 up to 1 200 min−1), the variation of some experimental RTD characteristics were unexpected. Indeed, the slope of the shape of the experimental RTD function E(t) changed significantly. This phenomenon will be called lag or delay time. This result was only observed at low throughputs and high screw rotation speeds. To finish, a modeling software of twin screw extrusion process was used to compare experimental and calculated results. For usual processing conditions (up to 700 min−1), the simulation predicts nicely the experimental RTDs. However, at high screw speed (N > 800 min−1) and moderate throughput (Q = 4 kg h−1), the simulation fails to predict the RDT delay time. Hence, some side effects apparently occurred during high shear extrusion at low throughputs.

Determination of the Residence Time Distribution in Twin Screw Extruders via Free Radical Modification of PE

The main objective of the present work was to introduce an inline method for measuring the residence time distribution (RTD) of twin screw extruders on the basis of information obtained from the melt free radical modification of polyethylene in a modular intermeshing co-rotating twin screw extruder. The trend of increasing rate of the extruder total torque resulted from replacing the neat polyethylene feed by a mixture of polyethylene and reactants which are chemically capable of creating chainbranching and/or crosslinking reactions was considered as the main information source for evaluating the RTD of the extruder. The RTD results were compared with those obtained from the tracer pulse input method, and good agreement was found. It was also demonstrated that, the present in-line RTD measuring technique has reliability of following the effect of feeding rate, screw speed and reactant concentration on the RTD of the twin screw extruders. It was found that, increasing the feeding rate results in decreasing the minimum residence time, and results in a narrower RTD. At constant feeding rate increasing the screw speed decreased the minimum residence time and broadened the RTD. The results also showed that, reactant concentration and variation of the viscosity along the screw have not appreciable effect on the twin screw extruders RTD.

Determinação da Distribuição de Tempos de Residência em Tempo Real no Processamento Reativo de Blendas Poliméricas

Determinou-se por transmissão de luz a distribuição de tempos de residência (DTR) em tempo real em uma extrusora com rosca dupla co-rotativa e autolimpante onde o sinal do detetor é sensível à presença da segunda fase dispersa, usada como traçador. Vários traçadores foram utilizados em diferentes concentrações: dois pigmentos (TiO2 e ftalocianina) e dois polímeros (poliestireno PS e poliamida-6 PA6) sendo adicionados na forma de um pulso em um fluxo de polipropileno (PP). Os parâmetros temporais (tempos de residência inicial, t i e médio t n e a variância normalizada <FONT FACE=Symbol>s q</FONT>²) medidos nas mesmas condições de processamento são muito próximos, dentro do erro experimental, indicando que a dispersão axial neste tipo de extrusora é independente do traçador. Por outro lado curvas de DTR medidas usando-se um polímero traçador (PS) disperso em um polímero de fluxo (PP) ficam deslocadas no tempo quando a situação é invertida, ou seja, usando-se PP como traçador em um fluxo de PS. Os parâmetros temporais são dependentes das características reológicas do polímero de fluxo, assim diferentes tipos de um mesmo polímero apresentam DTR com formas diferentes e deslocadas no tempo. A intensidade do sinal produzido pelo detetor é dependente não só da concentração mas também das características ópticas do par polímero/traçador, ou polímero/fase dispersa. Misturas poliméricas reativas (PP/PA6/PP-g-AA) e não reativas (PP/PA6) apresentaram diferenças na intensidade do sinal da DTR, devido à ocorrência da reação de graftização com conseqüente mudança na morfologia e no comportamento reológico. Estes resultados foram corroborados com medidas "off-line" por espectroscopia no infravermelho.