Journal of Advanced Pharmaceutical Science and Technology
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Review Article | Open Access
  • Available online freely | Peer Reviewed
  • Supercritical Fluid Technology: A Review

    Rabinarayan Parhi 1       Padilama Suresh 1    

    1GITAM Institute of Pharmacy, GITAM University, Gandhi Nagar Campus, Rushikonda, Visakhapatnam-530045, Andhra Pradesh, India

    Abstract

    The challenges ever faced by pharmaceutical industry is mainly due to discovery of new drugs and development of new technologies. Supercritical fluid (SCF) technology is one such technique, which has become an important tool in the production of different particulate systems along with extraction and drying of protein and peptides during last couple of decade because of its specific properties such as flexibility in use, reduced environmental concern and its simplicity. In this review, we briefly describe the operating principles and parameters influencing each one of SCF processes along with their merits and perspectives. The application of SCF technology in pharmaceutical industry, including particle and crystal engineering, composite particles’ preparation, coating of solid dosage form, liposome preparation, extraction and protein and peptide drying are discussed.

    Received 10 Nov 2012; Accepted 13 Jan 2013; Published 30 Jan 2013;

    Academic Editor:Rohit Ghan, Director (Head) - Product Development OHM LABS (A SUN PHARMA COMPANY)

    Checked for plagiarism: Yes

    Review by: Single-blind

    Copyright©  2013 Rabinarayan Parhi, et al.

    License
    Creative Commons License    This is an open-access article distributed under the terms of the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original author and source are credited.

    Competing interests

    The authors have declared that no competing interests exist.

    Citation:

    Rabinarayan Parhi, Padilama Suresh (2013) Supercritical Fluid Technology: A Review. Journal of Advanced Pharmaceutical Science And Technology - 1(1):13-36.
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    DOI10.14302/issn.2328-0182.japst-12-145

    Introduction

    Although SCF technology is in use from late 19th century as a tool to understand the natural mineralization, the commercial exploitation of SCF technology has began in the 1970s. This was particularly motivated by environmental concern, capability of some SCFs for replacing toxic industrial solvent and finally, the SCF processes might be economical to liquid extraction and distillation methods 1, 2.

    A fluid is said to be supercritical, when its pressure and temperature exceed their respective critical value (Tc- critical temperature and Pc- critical pressure). In the phase diagram Figure 1 the critical point located at the right upper end and the phase area beyond of this point is the SCF region 3. Above the Tc, it is not possible to liquefy a gas by increasing the pressure. In other words, a SCF can behave as either a liquid or a gas, but is actually neither. The physicochemical properties of a SCF compared with those of liquid and gas were presented elsewhere in the literature 4.

    Figure 1. Typical diagram of supercritical region.
    Figure 1.

    However, the SCF has a unique thermo-physical property. As the pressure is raised, the density of the gas increases without significant increase in viscosity while the ability of the fluid to dissolve compounds also increases. A gas may have little to no ability to dissolve a compound under ambient condition can completely dissolve the compound in supercritical range. Therefore, SCF provide a greater avenue as its solvation power is altered by careful control of changes in temperature and/or pressure 5.

    All gases can form SCF above specific sets of Pc and Tc values, but in most of the cases, the transition to the supercritical state occurs at high temperatures not compatible with pharmaceutical compounds (e.g. SC water) (Table 1). In addition, the Pc, Tc values increase with the molecular weight or intermolecular hydrogen bonding or polarity 6. Among the number of gases tried as SCF, CO2 is considered as the best option for SCF technique because of its low critical point (31.3 ºC, 7.4 MPa), attractiveness for heat sensitive materials, it is inert, leaves no traces behind after the process, as well as being inexpensive, non-inflammable, having GRAS (generally regarded as safe) status and being easy to recycle or to dispose off. By incorporating a small amount of volatile cosolvent, often a polar or proteic compound such as acetone or ethanol, the solvation power of a particular SCF in less soluble solvent like water can be improved 7, 8.

    Table 1. Critical parameters of selected compounds 9
    Compounds Tc (ºC) Pc ( MPa ) Dc (g/ml) Solubility Parameter ( cal /cm 3 ) 1/2
    H2O 374 22 0.315 23.4
    N2 -147 3.39 1.16 --
    Xe 16.6 5.9 1.10 6.1
    SF6 45.5 3.8 0.74 5.5
    N2O 36.5 4.1 0.45 7.2
    C2H4 9.1 5.1 0.22 --
    CHF3 25.9 4.7 0.526 5.4
    CO2 31.3 7.4 0.468 7.5

    Dc density at Critical Conditions

    In this review, we present various SCF processes with their advantages and limitations. In particular, different parameters influencing the above processes are discussed. Further, pharmaceutical applications of SCF processes including particle and crystal engineering, composite particles preparation, coating of solid dosage form, liposome preparation, extraction, protein and peptide drying and supercritical fluid chromatography (SFC) are presented through some selected examples.

    Processes Using Supercritical Fluid

    SCF technology can be classified in to three broad categories depending on the way SCF-CO2 is being used.

    SCF-CO2 used as solvent for active substances and its excipients (RESS, PGSS, RESOLV, RESAS, DELOS)

    SCF-CO2 used as antisolvent for the precipitation of active substances and their excipients in organic solvent (GAS, ASES, PCA, SAS, ASAIS, SEDS)

    SCF-CO2 assisted spray drying or aerosolization based methods (CAN-BD, SAA).

    SCF as a Solvent

    Rapid Expansion of Supercritical Solutions (RESS)

    RESS process is consisting of two steps; (a) dissolving the solid substance in a SCF and (b) formation of particles due to supersaturation. In the RESS process, at first SCF-CO2 is pumped at desired pressure and temperature to extraction chamber containing solid substance(s) through heat exchanger as seen in the Figure 2. The SCF percolates and dissolves the solid substance(s) in the extractor and then the resulted solution is depressurized through a heated nozzle or capillary at supersonic speed into a low pressure chamber. The supercritical solution is expanded adiabatically in the chamber, which leads to a rapid drop in temperature and pressure and spontaneous formation of droplets/particles. During the rapid expansion of the supercritical solution, the density and solvent power decrease significantly, resulting in super saturation of the solution and consequently precipitation of desire particles free of a residual solvent. This process is also called supercritical fluid nucleation (SFN) 10.

    The parameters influencing RESS process are classified into pre-expansion and post-expansion condition. Pre-expansion condition includes equipment related parameters (temperature and pressure) and raw material related parameters like SCF, structure of solute (crystalline or amorphous, composite or pure) and cosolvent. The post-expansion condition depends on nozzle temperature, geometry, size, distance and angle of impact against the surface of the jet stream 11, 12, 13, 14, 15.

    The advantages of RESS process are that it is simple, effective when single nozzle is used and it minimizes the use of organic solvent and reuses the SCF in continuous process. The main drawback is represented by poor solubility of most of the pharmaceutical material (e.g. polymer) in SCF-CO2, which, in turn require large amount of fluid, and therefore, RESS increases the cost of production. Difficulty of scaling up the process because of particle aggregation and nozzle blockage caused by cooling due to the rapid expansion of the supercritical solution and also poor control over particle size distribution 16.

    Figure 2. RESS equipment concept
    Figure 2.

    RESS with Solid Cosolvent (RESS-SC)

    To overcome the low solubility of polar drug in SCF and the aggregation of particles in the expansion zone, the RESS process is modified to use a solid cosolvent (RESS-SC) 17. The concept is based on the solubilization of solute and solid cosolvent in the SCF followed by expansion of the resulted solution through the nozzle in the expansion vessel. Finally, the solid cosolvent is removed by sublimation.

    The solid cosolvent should have sufficient high vapour pressure for easy removal by sublimation, sufficient solubility in SCF, solid at nozzle exit point and non-reactive to SCF and the desired solute. One of such solvent is menthol which is used as solid cosolvent to phenytoin in the production of fine particles. The solubility of phenytoin in SCF is only 3 µmol/mol, but when used with menthol as solid cosolvent at 196 bar and 328 K, the solubility improved by 400 times. This improvement in solubility is attributed to the interaction between phenytoin and menthol 17. Same pattern of solubility improvement was observed for drug salicylic acid or phenanthrene when benzoic acid is used as solid cosolvent 18.

    Continuous RESS Process

    This process combines the principles of RESS and SEDS process. In this method, like RESS process, SCF is introduced into a high pressure vessel upon preheating it to desired operating temperature. After maintaining the stable temperature and pressure in the high pressure vessel, polymer solution is delivered into the same chamber through co-axial nozzle. When the spraying of polymer solution is finished, the high pressure vessel is depressurized in ambient vessel and the product is collected. The ability of this technique to prepare microparticles continuously and constantly is the advantage over individual process 19

    Pre- Filtration RESS (PF-RESS) Process

    Chiou et al. 20 developed this novel RESS technique in the intention to control the formation of fine particles and to obtained particles with narrow size distribution. The principle involved in the particle formation by PF-RESS process is to use a porous membrane with pore size less than 1 µm in order to pre-filter the SCF containing drug/polymer(s) in the extraction chamber. This can avoid the particle of large size to pass through the membrane and get into the precipitation unit. They successfully prepared microparticles of meloxicam of average size less than 2 µm with a narrow particle size distribution range between 0.5 µm and 5 µm.

    Particle Formation from Gas Saturated Solutions (PGSS)

    Many pharmaceutical materials are polar or high molecular weight substance, such as protein and peptide and due to which it is difficult to dissolve them in CO2, which has no polarity even in supercritical state. High amount of CO2 is needed to compromise this low solubility, which in turn increases operational cost. In PGSS process, the polymer(s) are first melted or suspended in solvent at a given temperature in an autoclave and then solubilizing SCF-CO2 in above melted or liquid suspended substance(s), leading to a so called gas saturated solution or suspension that is further depressurized through a nozzle with the formation of droplets or solid particles Figure 3. Unlike to RESS technique, the principle governing PGSS process involves both the pressure and temperature- and solvent-induced phase separation.

    Advantages of PGSS process are; (i) substance need not be soluble in SCF-CO2, (ii) simplicity of this process, leading to low processing cost and wide range of application, (iii) can be used with suspensions of active ingredient(s) in polymer(s) or other carrier substance leading to composite particles, (iv) can be applied to process inorganic powders to pharmaceutical compounds, and (v) low solvent gas usage and pressure than RESS process as operational condition 21. Care must be taken for thermolabile solute and moreover this technique compromises with microparticles. Insulin SLNs of size less than 500 nm were prepared by using DMSO as solvent and the lipid mixture of tristearin, phosphatidylcholine and dioctylsulfosuccinate 22.

    Figure 3. PGSS equipment concept
    Figure 3.

    Rapid Expansion of a Supercritical Solution into a Liquid Solvent (RESOLV)

    RESOLV method consists of spraying of solution (drug in SCF-CO2) into an aqueous medium from vessel maintain at given temperature and pressure. The rapid expansion of solution and followed by quenching leads to particle formation. Number of water soluble polymer (e.g. PVP) may be added to the aqueous medium to stabilize the particulate suspension. Finally, particles recovered from the suspension 23. The advantage of this method is that the possibility of stopping the particle growth in the precipitator. RESOLV method is having the same limitation as RESS. The other problem is the recovery of particle from the aqueous solvent 24.

    Rapid Expansion from Supercritical to Aqueous Solutions (RESAS)

    This is a modification of RESS technique and is developed so that the stabilization of submicron particle in the aqueous phase became feasible. In this process, the supercritical solution (SCF with polymer and drug) is expanded through a nozzle in to an aqueous solution containing stabilizers. Usually, non-ionic surfactants such as lecithin, polysorbates and poloxamer are the choice for the stabilization because of their low toxicity. Parameters that are influencing the resultant particle size are stabilizer type, concentration of stabilizer in aqueous phase, solid to surfactant ratio and finally the temperature of the stabilizer solution 25, 26.

    Nanosizing of particles, high drug payload and long term stability are making this technique attractive than RESOLV method. But there are some demerits like it is not a suitable method for the drug which are unstable in aqueous solution and broad particle size distribution 26

    Depressurization of an Expanded Liquid Organic Solution (DELOS)

    In DELOS process, the substances are first dissolved in suitable organic solvent and then it is mixed with SCF-CO2 in a vessel of particular temperature and pressure. This mixture is depressurized through a nozzle into a vessel to form fine particle 27. Here, the SCF-CO2 is used as co-solvent to the organic solvent. The main advantage of this technique in comparison to PGSS is that the thermo-sensitive material can be handled to prepare fine particle without melting it.

    SCF as an Antisolvent

    The low solubility of pharmaceuticals in SCFs limited the large scale production of micro/nano sized particles by PGSS and RESS method. Using SCFs as antisolvent was thought off by many researchers to solve the above problem. Here, the solute is insoluble in an antisolvent, whereas the antisolvent should be completely miscible with liquid solvent. This is based on the principle that when a solution sufficiently expanded by a gas, the liquid phase is no longer a good solvent for the solute and particle formation by precipitation occurs. The SCFs as antisolvent includes GAS, SAS, ASES, PCA and SEDS processes.

    Gaseous Anti Solvent (GAS)

    GAS is a batch process where the precipitator is partially filled with the solution of solute of interest and then the supercritical antisolvent is pumped into the vessel, preferably from the bottom until the fixed pressure is reached as shown on Figure 4. The particles precipitates as the gas concentration in the solution increases with pressure. After a holding time, the expanded solution is made to pass through a valve present above the precipitator to wash and clean the precipitated particles. A clear disadvantage of this technique is the lack of control on the particle formation, which prevent the formation of mono dispersed particles.

    Figure 4. GAS equipment concept
    Figure 4.

    Aerosol Solvent Extraction System (ASES), Particles by Compressed Antisolvent (PCA), Supercritical Antisolvent (SAS)

    The SCF is first pumped to the top of the high pressure vessel until the system reaches a constant temperature and pressure Figure 5. Subsequently, active substance solution is sprayed as fine droplets into above SCF bulk phase through an atomization nozzle. The large volume expansion of drug solution in vessel, resulting dissolution of SCF into liquid droplets and, subsequently, in super saturation due to reduction in solvent power leading to nucleation and formation of small and mono disperse particles. Particles are collected on a filter at the bottom of the vessel. The SCF and organic solvent mixture flow down to a depressurized tank where suitable temperature and pressure condition allow gas-liquid separation. After the collection of sufficient quantity of particles, the spraying of liquid solution has to be stopped. Furthermore, to remove residual solvent, pure SCF continues to flow through the vessel 2. The ASES can be modified with the addition of precipitation of compressed anti solvent (PCA) which was proved to be more efficient in the production of a great variety of organic and biopolymer based particles.

    Figure 5.ASES/SAS/PCA equipment concept
    Figure 5.

    Main advantage of this technique over GAS is its suitability for continuous operation, which prerequisite for large scale mass production of particles. Complex mass transfer process is one of the major limitations in SAS scale up. Complex mass transfer process is originated due to two issues. First one is the result of variety of jet dispersion patterns in the supercritical spray leading to formation of droplets of non uniform sizes. It is obvious that mass transfer within the droplets of smaller size is considerable faster than that of larger droplets owing to higher surface area of the former. Furthermore, there is more time for crystal growth in larger particles. Another problem related to mass transfer in SAS is due to residence time of particles under supercritical condition until the cycle ends. Particle may still grow, when present on the filter for separation, under above condition. To solve above problems in SAS, concentric tube antisolvent reactor (CTAR) technique was developed. In this process, particles are formed inside a small concentric tube instead of usual spraying of drug solution into SCF 28, 29. Filter is used for the harvesting of particles, which is again more problematic owing to small concentric tube in CTAR.

    Atomization of Supercritical Antisolvent Induced Suspension (ASAIS)

    This is another modification to SAS technique. In ASAIS process, antisolvent induced precipitation occurs in a small tube, where antisolvent mixed with the solution to generate a suspension. This suspension of particles is then sprayed into a precipitator at atmospheric condition for solvent separation, which eliminates the high volume and high pressure precipitator. In addition, very small to moderate antisolvent concentration is required. Contrary to both SAS and CTAR process, the particles recovery is performed by cyclone separator rather than using filter. Here, the first step (suspension formation) occurs in the small tube and next step in the precipitator and finally particle recovery in cyclone separator 30.

    Solution Enhanced Dispersion by Supercritical Fluids (SEDS)

    This is a modification of SAS process in which the SCF and drug solution are introduced simultaneously in to the precipitation vessel at particular temperature and pressure through the coaxial nozzle. The design of co-axial nozzle is such that to facilitate the dispersion of drug solution by SCF, thereby enhancing mass transfer and formation of fine particles Figure 6. In addition, the high velocity of SCF allows intense mixing with drug solution. Here, the SCF serves both as an antisolvent and as a dispersion medium 31.

    The particle formation/size by SEDS depends on the mass transfer of SCF into sprayed droplets and by the rate of solvent transfer into the SCF phase. In general, high mass transfer causes faster supersaturation and smaller particle size with less agglomeration 32. Most often two way coaxial nozzle is used where both drug solution and SCF are introduced into precipitation chamber as separate stream. Basic operational principle of GAS/SAS/ASES/PCA/SEDS is described as follows. A ternary system is produced by the introduction of SCF in to chamber containing polymer and solvent homogenous binary system. Upon change in pressure, compositional quenching takes place leading phase separation and particle formation.

    Baldyga et al.33 used coaxial two-component nozzle with a mixing chamber in nozzle to prepare paracetamol particles. The intention was to partially mix alcoholic drug solution with SCF in the nozzle chamber before introduction into precipitation chamber. Mixing in the nozzle chamber creates high supersaturation, which enables to start nucleation and growth immediately after entering into precipitation chamber.

    In order to obtained ultrafine particles with narrow size distribution, He et al. 34, 35 used SEDS with prefilming atomization (SEDS-PA) process. For the above purpose they have used twin-fluid atomizer. The principle involved in this process is to drive the liquid to be atomized along a surface as a film within the nozzle and consequently reaching at the atomizing edge. As a result, separation of liquid film takes place leading to the formation of fine droplets. The liquid to be atomized was driven along the coaxial annular passage and formed to a thin swirl liquid film by the spiral slots liquid distributor with an angle (45º) of inclination relative to the central axis of the atomizer. At the exit of the atomizer the atomizing dense gas stream impinges on the thin swirl film at 45º and followed by vigorous interaction between jet stream and annular liquid sheet resulting in the formation of fine droplets.

    To overcome the limitation of water solubility in SCF, SEDS has been further modified to in order to process water soluble compounds (e.g. protein and peptides). The above modification includes the use of three way coaxial nozzle to introduce aqueous drug solution, SCF and organic solvent (polar) in to particle formation chamber as separate stream. The organic solvent acts both as precipitating agent and a modifier, enabling the non-polar SCF to remove water 36. The use of ultrasonic nozzle is a further modification of SEDS 37. The formation of fine droplets is based on the induction of ultrasonic waves of frequency between 10-100 kHz, caused by the vibration of ultrasonic coaxial nozzle.

    Figure 6. SEDS equipment concept
    Figure 6.

    Supercritical Fluid Extraction of Emulsions (SFEE)

    This technique is based on counter-current extraction of emulsion by SCF. The process is as follows, first the o/w emulsion is introduced into the extraction chamber (at particular temperature and pressure) through the nozzle present at the top at a constant rate Figure 7. Simultaneously, SCF from the side bottom of the extraction chamber is introduced. This counter-current flow leads to the expansion of organic phase of the emulsion, consequently, the precipitation of dissolved substances into composite nano-particles 38.

    The emulsion droplet diameter is the key size control parameter, besides fraction of lipid and drug in organic solvent. The advantage of this method over traditional methods like evaporation and liquid extraction are fast and complete removal of the solvent and formation of uniform particle size. In addition, whenever lipid is used as matrix material, the thermodynamic stability is established due to plasticizing effect of lipid as the depression of lipid melting point occur in the extraction column. Furthermore, lipid is purified due to extraction of impurities present along with lipid 38.

    Figure 7. SFEE equipment concept.
    Figure 7.

    SCF-CO2 Assisted Spray Drying (Aerosolization-Based) Methods

    These techniques used SF to assist or enhance the nebulization or aerosolization of the solution of the substance to be processed, which is then rapidly dried in a drying atmosphere to form fine particles. There are two methods based on this principle.

    Carbon dioxide Assisted Nebulization with Bubble Dryer (CAN-BD)

    This process focused on the nebulization of the liquid solution rather than using dense gas (SCF) to achieve precipitation by solubility reduction for the solute to be micro- or nano-sized. At first, the solute(s), preferably in between 1% to 10%, is dissolved or suspended in aqueous or organic solvent or their mixture and then mixed intimately with near critical or SC by pumping both fluid through a near zero volume tee as shown in Figure 8 to generate emulsion. The resultant emulsion is rapidly expanded through a flow restrictor to near atmospheric pressure to form aerosol consisting of micro droplets and micro bubbles. The aerosol is formed due to sudden dispersion of the liquid solution caused by rapid expansion of compressed gas. The drying chamber is filled with heated air or nitrogen gas to maintain the desired temperature for rapid drying of aerosol droplets or micro bubbles. Dry particles are collected on a filter placed at the outlet of the drying chamber 39.

    Parameters influencing the particle formation are flow rate of solution (for lab scale 0.3-0.6 ml/min is sufficient), percentage of dissolved or suspended substance, inner diameter flow restrictor (50-175 µm and length ∽ 10 cm), temperature of the drying chamber, residence time of droplets or micro bubbles (as micro bubbles are dried faster than droplets) 39.

    Figure 8. CAN-BD equipment concept.
    Figure 8.

    Advantages of CAN-BD process are; (i) minimum decomposition of thermolabile drugs, (ii) preferred method for water soluble drug, (iii) organic solvent compatible with SCF can be substituted in part or totally for water, and (iv) very fine size of the produced particle (<3 µm diameter) 40. There is need to heat tee and restrictor to a temperature in the range 50 to 100ºC in order to avoid restrictor obstruction during expansion.

    Supercritical Fluid-Assisted Atomization (SAA)

    SAA process is based on the solubilization of SCF in aqueous solution to be dried and subsequently atomization through a thin wall nozzle at atmospheric pressure. The difference between SAA and CAN-BD is the region where the mixing is achieved 41, 42.

    Application of SCF Technology

    Particle and Crystal Engineering

    Crystalline solids that are the same compound/composition but have different crystalline forms are called polymorphs or modification 43, 44. Pseudo polymorphs (solvates and hydrates) are molecular adducts that contain solvent molecule (water in case of hydrates) in the crystal lattice.

    Traditional process such as crushing/milling, micronization, spray drying, freeze drying and crystallization used to produce particles. These processes offer limited control over the physicochemical properties of the produced particles including size, shape and crystalline purity due to numerous unintentional conversion of polymorphs, desolvation of solvates, and solvates formation occur during aforementioned processes 45. Furthermore, these methods require more manufacturing steps to produce drug particles. Regulatory authority like International Conference on Harmonization (ICH), in the guideline Q6A, emphasizes the importance of solid state and crystallographic purity of the drug and excipients 46. Similarly, FDA requires proof of crystalline form of drug along with the relationship between structure and stability of the crystal 47. In above situations, SCF technology could be used as viable means of controlling crystal formation.

    The influence of GAS technique on the polymorphism of a poorly water soluble drug, puerarin, was investigated by Li et al. 48. It was known fact that puerarin commercially available in crystal form I. At optimum conditions, a more orderly and pure form of crystal of size 30.34 µm with needle-like shape was generated. In addition to this, at 60 mg/ml of solute concentration and methanol as solvent, two new crystal forms (form III and form IV) of puerarin were produced. Puerarin in form II has the smallest particle size and fastest dissolution rate compared to other forms. This was attributed to the metastable nature of form II, while form IV exists in stable form. Of all the process parameters, the type of solvent had tremendous influence on the external shape of crystal. For instance, puerarin crystal exhibited needle-like appearance with ethanol. When the solvent changed to methanol, the crystal appeared as long column and acetone produced long needles with brushes.

    Different crystal forms of terbutalin sulphate were produced including stoichiometric monohydrate and amorphous material by SEDS technique49. One crystalline and another semicrystalline form of terbutalin sulphate were obtained at the condition of higher temperature (50 ºC), lower pressure (150 bar), and ethanol as solvent but in different volume of precipitation vessel. Particles in smaller (50 ml) volume of precipitation vessel were exposed to partially mix ethanol-rich phase resulting in lower supersaturation level, subsequently microparticles of 100% crystallinity were obtained. In contrast, the particles in the large (500 ml) precipitation vessel were growing in a well mixed CO2-rich environment which is characterized by a high level of supersaturation in the beginning and followed by relatively low supersaturation particle formation process. The last stage of particle growth is considered as particle conditioning. A more stable and less energic surface of terbutalin sulphate microparticles were obtained due to above phenomenon, which in turn improved powder flow and aerosolization performance.

    Zhiyi et al. 50 prepared microparticles of water soluble drug, cefadroxil, from water-ethanol mix solvent by SAA process. They investigated the influence of operational parameters, including mixing vessel pressure and temperature, solution concentration, and solution feed rate on particle morphology (PM), particle diameter (PD) and particle diameter distribution (PDD). Among all the operational parameters, the influence of mixing vessel pressure was significant. The PD decreases, the PDD become narrower and the average particle diameter become small with the increase of the mixing vessel pressure in the range of 6-10 MPa, when other operational conditions were fixed at: the mixing vessel temperature 60 ºC, the solution concentration 8 mg/ml and feed rate of 3 ml/min. Further increase in mixing vessel pressure resulted in smaller PD but wider PDD. The diameter of most of the particles obtained was below 1 µm in the above condition and having concave morphology. With the increase of solution concentration from 4-10 mg/ml, PD becomes larger, PDD becomes wider and PM becomes more irregular. Finally, it was concluded that the optimal operation condition for preparing microparticles of cefadroxil is: the pressure of 10 MPa and the temperature of 60 ºC in the mixing vessel, the solution concentration of 4 mg/ml and the solution feed rate of 3 ml/min.

    Nijlen et al. 51 compare different micronization process, such as mechanical grinding, Jet milling and SCF technique (RESS process) on the basis of artemisinin particle size obtained. The lowest median diameter of particle of 4.1±0.2 µm is obtained by Jet milling. The mechanical grinding and micronization by RESS process produce median particle diameter of 27.4±4.6 µm and 10.6±0.5 µm, respectively. The optimal condition for RESS technique was found to be 300 bar pressure and temperature of 80 ºC in extraction column.

    Hezave et al.52 studied various parameters such as extraction temperature, extraction pressure, nozzle length, effective nozzle diameter and spraying distance on the particle size and morphology of diclofenac particles obtained by RESS method. They found that the increase in extraction temperature, nozzle length, effective nozzle diameter and spraying distance lead to increase in mean particle size of precipitated particles. But extraction pressure had an opposite effect on particle size. This was explained on the basis of solvation power of SCF. The solvating strength of SCF increases at higher extraction pressure, subsequently the concentration of diclofenac in SCF increases. Resulting higher drug concentration leads to higher supersaturation and results in smaller size of precipitated diclofenac particles. The mean particle size of diclofenac was in the range of 10.92 to 2.23 µm in all the experimental condition as comparison to the original particle of 38.12 µm. Furthermore, the morphology of particles was changed from irregular to quasi-spherical and irregular.

    Martin et al. 53 studied the effect of various parameters such as temperature of precipitation chamber, density, drug concentration and flow rate of SCF and drug solution on the particle size and morphology of microparticle of budesonide prepared by PCA method. They found that the particle growth rate increased by increasing the chamber temperature from 35 to 45 ºC. At 40 ºC, round budesonide particle size of 1-2 µm were obtained. At lower density (0.38 g/cm3) the particles formed were fairly spherical. Increase in drug concentration and its flow rate increase the particle size, while particle size decreased by increasing SCF flow rate.

    Charpentier et al. 54 investigated various parameters such as nozzle diameter, pre-expansion pressure and pre-expansion temperature on the particle size and morphology of bechlomethasone-17,21-diapropionate (BDP) microparticles prepared by RESS process. They found that both particle diameter and width of distribution increased as the nozzle diameter increases and the morphology of BDP particles changed from spheres to elongated crystal. Increase in pre-expansion pressure from 1,900 to 4,100 psi and pre-expansion temperature from 35º C to 50º C resulted in the increase in particle size. The former was attributed to the agglomeration of particles in the capillary as it was at lower temperature and latter result was explained by the fact that higher temperature solutions have a higher cloud-point pressure leading to earlier crossing of cloud point by the solution while passing through the nozzle and consequently, nucleation to start earlier which allow more time to grow and coalsce to form larger particles.

    Kim et al. 55 used RESS process to prepare ultrafine lidocaine particles and studied the whole diameter of orifice nozzle and aspect ratio (length/diameter) of capillary tube along with extraction temperature and pressure. They observed fine particles with average particle diameter of 100-300 nm with spherical morphology. The average particles diameter increases with whole diameter of nozzle. This was explained by the fact that the increase in whole diameter causes a moderate concentration gradient of lidocaine around expansion device and consequently, premature precipitation resulting in larger particles. The increase in the aspect ratio above 200 creates concentration gradient followed by precipitation in capillary tube due to prolonged precipitation time.

    Reverchon et al. 56 prepared cromolyn sodium microparticle by SAA process and analyzed the influence of precipitation temperature, drying temperature and concentration of drug on particle size and morphology. In all the trial, they found particle size in the range 1-5 µm with spherical shape. There was an insignificant increase in particle size with the temperature from 100 to 140 ºC. An increase in drug concentration from 25 mg/ml to 115 mg/ml caused the increase in particle size. This was explained by considering the fact that viscosity and surface tension increased at higher drug concentration resulting in the formation of larger primary droplets followed by the formation of secondary droplets. The degradation of product was observed at higher temperature.

    Atila et al. 57 prepared digitoxin nanoparticle by RESS technique and investigated the effect of process parameters such as spray distance, flow rate and pre-expansion temperature on the particle size. The particle size of digitoxin particles decreases with the increase of spray distance and flow rate. The former case is the resultant of two competing phenomena. Firstly, as the spraying distance is short, residence time of droplets in expansion chamber decreases and leading to smaller particle size. In contrary, short spraying distance leads to coalescence of droplets due to decreasing angles between droplets. In the later case, the residence time of droplets inside the nozzle and in the expansion chamber decreased by increasing the flow rate. This decreases particle growth time and resulting in smaller particle size. However, particle size increases by increasing pre-expansion temperature. In all conditions, the particle size of digitoxin was decreased from 0.2-8 µm to 68-458 nm.

    Keshavarz et al. 58 studied the effect of extraction temperature, extraction pressure and spray distance on the formation of raloxifen nanoparticles prepared by RESS process. They found that by increasing extraction pressure from 10 to 18 MPa and spray distance from 5 to 10 cm, the particle size decreased. However, by increasing extraction temperature from 40 to 60 ºC particle size became smaller, but further increase in temperature to 80 ºC decreases the particle size. The later part can be explained by the fact that higher temperature causes higher level of supersaturation due to increase in solubility at higher temperature. This higher degree of supersaturation increases the number of nuclei formation which in turn increases the probability of collision and followed by large particle formation. A particle size of 14.11 nm was obtained at optimum condition of 50 ºC temperature, 17.7 MPa extraction pressure and spraying distance of 10 cm.

    Varshosaz et al. 59 investigated the effect of process parameters, such as the extraction column temperature and nozzle temperature on the amorphous nanoparticles (without additives) of cefuroxime axetil prepared by RESS technique. They tried three level of temperatures each for extraction column (60-90 ºC) and nozzle (50-70 ºC) and found that lowest particle size (158.57 nm) is obtained with nozzle temperature at 60 ºC and column temperature at 90 ºC.

    Montes et al. 60 precipitated amoxicillin nanoparticles by SAS process using N-methylpyrrolidone and CO2 as solvent and antisolvent and investigated the effect of initial drug concentration, flow rate of drug solution, temperature, pressure and nozzle diameter on particle size and size distribution. They observed that increase in the initial drug concentration leads to larger particles sizes with a wider size distribution. This result is attributed to higher condensation rate from the higher drug concentration dominates the higher super-saturation from higher drug concentration. Higher flow rate leads to smaller particles sizes due to higher degree of mixing. Other factors did not have significant effect on particle size. Spherical nanoparticles with mean size diameter of 216-505 nm were obtained by this method.

    Young et al. 61 prepared cyclosporine nanoparticles by RESAS technique and compared the effect of various stabilizes such as non-ionic surfactant (e.g. Tween 80, Pluronic F127, Myrtj 52) and phospholipid based surfactant on the particle size. Among non-ionic surfactant, Tween 80 produces smaller particle sizes ranges from 660 nm to 970 nm, whereas phospholipid based surfactant produces cyclosporine particles (200-300 nm) which was smaller than particles produced by Tween 80 at similar surfactant concentration and drug/surfactant ratio (as the drug/surfactant ratio exceeds 0.6 the particle size markedly decreases due to insufficient surface coverage by surfactant in aqueous solution). This result is attributed to the aggregation of large number of surfactant for phospholipid vesicle than that for micelle i.e. in a single vesicle the local concentration of surfactant that can coat a growing drug particle is higher than single micelle. Furthermore, the preferred curvature of the surfactant is more favorable for vesicle than micelle as the interface with water is less curved for vesicle as compared to micelle. In addition, vesicles are relatively stable, so the growth of the drug particles by collision/coagulation is minimized.

    Composite Particles

    Microparticles: Microparticles are colloidal particles ranging in size from 1 µm to 1000 µm. They can be composed of either a homogeneous polymer-drug complex (microspheres) or a central drug core surrounded by a solid polymeric shell (microcapsules). Microspheres are defined as solid, spherical particles containing active substance either in solution or crystalline form. Microcapsules are spherical particles containing drug concentrated in the center core, which encloses particles of solids, liquids or gases within the polymeric embryonic membrane 62. Polymer used to prepare microparticles can be either natural such as albumin, collagen, chitosan and alginate or synthetic (e.g. poly (lactic acid), poly (caprolactone), poly (methyl methacrylates), and poly (alkyl cyano-acrylates)).

    Brion et al.63 used PGSS technique to produce microparticle of solid dispersions containing a new chemical entity (YNS3107) and hydrophilic polymers such as PEG 400, PEG 4000 and Poloxamer 407. They found that the major parameters influencing the particle diameter are autoclave temperature and pressure. Smaller average particle diameter were obtained by increasing autoclave pressure as it increases the CO2 content within the droplets and resulting in lower solid-lipid equilibrium condition time (SLEC) (more the SLEC, the less the number of collision between droplets). Similarly, temperature close to melting point of polymer matrix reduces the droplet coalescence by shortening SLEC time. Finally, they concluded that the optimal condition is temperature (62 ºC) and pressure (177 bar) to produce smallest microparticles of mean diameter 30.4 ± 2.3 µm.

    Jordan et al. 64 prepared microsphere of human growth hormone by PGSS process (CriticalMixTM) using PLGA and PLA in different ratios for subcutaneous injection. They observed that 90 % of the particles are below 100 µm and volume mean diameter (is the diameter at the 50 % point of the entire volume diameter) is 61 µm, which indicates these particles can be injectable. The encapsulation efficiency is in the range of 97.1% to 100 %, which is nearly double the value obtained by emulsification method.

    Duarte et al. 65 compared the particle size of naproxen microparticles prepared by both solvent evaporation and SAS techniques. The polymers used were methylcellulose and ethylcellulose and solvent system composed of dichloromethane and dimethylsulfoxide for SAS method. The microparticles obtained by SAS method were of significantly smaller in diameter (16.91 µm) and narrow size distribution than that of produced by solvent evaporation method. Furthermore, the particle size was further reduced to 4.71 µm, when ethylcellulose used alone.

    Zhang et al. 66 prepared microparticles of morphine by SEDS technique and investigated the effect of flow rate of drug solution (aqueous), polymer solution Poly and antisolvent (ethanol) on particle size and morphology. They observed that by increasing the flow rate of ethanol from 0.5 to 1.5 ml/min, irregular shape, uneven size and amorphous form became converted to ellipsoidal shape, uniform size and micron and submicron particles. But, the opposite effect was seen in case of flow rate polymer solution. The morphology of microparticles changed from irregular to axiolitic form with less agglomeration as the flow rate of dichloromethane was decreased from 1.5 to 0.5 ml/min. The microparticles were formed at the appropriate flow rates ratio of ethanol to dichloromethane. By increasing this ratio, the agglomeration can be prevented as the mass transfer was faster than the separation of fine droplets. Finally, they concluded that the obtained morphine microparticles possessed ellipsoidal shape and smooth surface with mean diameter of 2.45 µm at the optimum condition (the flow rates ratio of aqueous solution, ethanol and dichloromethane is 1/7.5/2.5).

    Uzun et al. 67 used SAS process to prepare composite microparticles of cefuroxime axitel with polyvinylpyrrolidone, and obtained spherical particles of smaller size as comparison to larger and plate-like particles formed when drug or polymer was precipitated alone. This was explained by the fact that polymer inhibits particle growth of drug by blocking surface of particles and the consequence was larger surface area and smaller particle size. This was conformed by FT-IR study as there was an interaction between carboxyllic groups of polyvinylpyrrolidone with amine group of cefuroxime axitel.

    Patomchaiviwat et al. 68 prepared microparticle of rifampcin and poly (L-lactide) by SAS technique and studied the effect of polymer:drug ratio on the morphology and size of particle. By fixing the conditions, such as 2 % of drug and polymer in methylene chloride, 172 bar of pressure, 40 ºC of temperature and 0.82 of CO2 molar fraction, they found few spherical particle at 5:5 polymer:drug ratio, but as the polymer: drug ratio increased to 7:3 or more, number of spherical particle increased along with lower particle size (the particle size was 3.68 µm at 9:1 polymer:drug ratio). At low polymer content, the solution was atomized into droplet having less amount of polymer which was not sufficient enough for hardening the droplet into spherical microparticle.

    Both CO2- and N2-assisted atomization processes were used to develop ibuprofen/lipid (myristic acid and tripalmitin) composite microparticles. The average size of obtained particles was slightly larger than that of pure lipid particles in case of N2-assisted process due to the difficulty of solidification using N2. In CO2-assisted process, the mean particle size was slightly smaller than that of pure myristic acid, but slightly larger than that of pure tripalmitin particles. The morphology of composite microparticles was similar to that of pure lipid particles 69.

    Nanoparticles: Nanoparticles are carrier for drugs or other active molecules of nanometer size range (10 nm-1µm). Nanoparticles can be developed by using either non-biodegradable/biodegradable polymer (polymeric nanoparticles) or solid lipid (Solid Lipid Nanoparticles). Solid Lipid Nanoparticle (SLN) is a colloidal drug carrier system consisting of spherical solid lipid particles in the nanometer range, which are dispersed in aqueous or in water surfactant solution. The essential excipients used in SLNs are solid lipids (e.g. tristearin, stearic acid) as matrix and ampipathic material (e.g. phospholids, bile salts and poloxamer) as surface stabilizer.

    Chattopadhyaya et al.38 prepared SLN suspension of model drug indomethacin and ketoprofen by SFEE method. Stable aqueous SLNs suspensions with mean volume diameter <50 nm were produced by this method, which was less than that of produced by high pressure homogenization and microemulsion technique. No crystalline drugs were detected in the formulations and also the degree of crystallinity was reduced in case of lipids (tripalmitin, tristearin and Gelucire 50/13). At stable condition, drug present in SLN above the saturation level (10 % and 20 % for tripalmitin and Gelucire 50/13, respectively).

    Coating

    Traditional coating process involves the application of coating solution/suspension to the exterior of solid dosage form. This process associated with many disadvantages like solvent residue in the final dosage form, cost and environmental concern due to the use of organic solvent. To avoid above concern, organic solvent replaced with aqueous solvent. However, it increases drying time and a number of polymers are not soluble in aqueous solvent. The SCF technology is used to overcome the above shortcomings.

    Santos et al.70 developed coated microparticle of bovine serum albumin (BSA) using SCF coating process. The process was carried out in a simple autoclave equipped with a rotating impeller and the coating material selected are trimyristin (Dynasan® 114) and Gelucire 50/02 (mixture of glycerides and fatty acid esters) having melting point 45 ºC and 50 ºC, respectively. SCF condition used was temperature ranging between 35-45 ºC and pressure about 200 bar. Gelucire® 50/02 produces consistent and homogeneous coating over BSA particles. This can be explained by the fact that Gelucire® 50/02 consists of mixture of glycerides and fatty acid which prevent the crystallization. On the other hand, Dynasan® 114 crystallized on BSA particles in the form of micro-needle resulting in discontinuity in coating layer. Due to this, Dynasan® 114 coated microparticles exhibit a high initial burst release of 35 % over in 5 minutes and 70 % release over 30 minutes. In case of Gelucire® 50/02 coated microparticles provide prolonged release of BSA over 24 hr.

    Microparticles of red phosphorous (RP) coated with paraffin were developed by RESS technique with a newly designed nozzle. The characteristic feature of this model nozzle was the width of the aperture, which can be adjusted so that the supercritical solution expands rapidly through an exit with a controllable size. In addition, it can not easily be stopped (as seen in case of conventional nozzle) which makes the encapsulation process smooth. The obtained coated particle size of RP was 65 µm, when the raw RP particle of 45 µm size was taken. The surface of the coated microparticle shown to be perfectly smooth, indicating that the RP particles were completely and effectively encapsulated by the paraffin 71.

    Mishima et al.72 used RESS method with a non-solvent for the encapsulation of proteins (lipase and lysozyme). They have used number of polymers such as polymethylmethacrylate, polyethylene glycol (PEG), polylactic acid, polylactide-co-glycolide and PEG-PPG (polypropelene glycol)-PEG triblock co-polymer and found non-agglomerated protein containing microparticles in the entire batch.

    Extraction

    Extraction by SCF involves the dissolution of the desired component from sample of plant and animal origin under the controlled condition of temperature and pressure followed by the separation of desired component from the SCF by a significant drop in solution pressure 73.

    Conventional extraction processes require large amount of hazardous solvent (e.g. chloroform, methanol) and are generally cumbersome. Soxhlet extraction technique was developed in the intention to make extraction process continuous and was used for extraction of volatile oil and lipids. This process is associated with disadvantages such as requirement of highly pure solvents, use of hazardous and flammable liquid organic solvent, potential toxic emission during extraction, and finally, it is a time consuming process 74. Supercritical fluid extraction (SFE) is routinely used for the extraction of lipids, essential oils from plant or animal material because of its environmentally friendly nature.

    The major advantages of SFE over conventional solvent extraction process are: (i) the penetration power of SCF into porous solid materials is higher than liquid solvent due to its low viscosity and high diffusivity, (ii) a complete extraction is possible in SFE as a fresh fluid is continuously forced to flow through the samples, (iii) the solvation power of the SCF can be adjusted according to requirement by varying temperature and pressure, resulting a high selectivity, (iv) suitable for thermolabile material, (v) it can be associated with various compound detecting tool like gas chromatography and mass spectroscopy, which is useful in direct quantification in addition to extraction 75, 76, 77, 78.

    Essential oils extraction: Essential oils were traditionally extracted from seeds, roots, flowers, herbs and leaves using hydrodistillation. Thermal degradation, hydrolysis and solubility of some compounds in water may alter the flavour and sometimes fragrance of essential oils. SFE technique is used to avoid these problems. The optimum operating conditions for extraction of essential oils by SFE method are: pressure in the range of 90-100 bar and temperature ranges from 40-50 ºC, since at these conditions all the essential oil compounds are highly soluble in SCF-CO279, 80, 81, 82. For instance, linalool, a terpene is completely miscible with SCF-CO2 at temperature of 40 ºC and pressure more than about 85 bar 82.

    Seed oil extraction: Seed oils were generally extracted using hexane. The major problem associated with this method was difficulty in hexane removal after extraction and thermal degradation during the extraction, which necessitates the use of SFE technique 83, 84, 85, 86.

    Salgin et al. 87 employed SFE process for the extraction of jojoba oil and investigated the effect of process parameters such as pressure, temperature and particle size of jojoba seeds, flow rate of CO2 on efficiency of extraction. They found the performance was increased (from 45.8 to 47.3 %) with the increase in temperature from 70 to 80º C and for pressure, the performance increased by increasing pressure from 200 to 600 bar. By increasing the CO2 flow rate from 0.5 to 2 ml/min and reducing the particle size to half (i.e. 2.18 to 1.09 mm), the significant increase in performance was observed.

    Preparation of Liposomes

    Liposomes are simple microscopic vesicles in which an aqueous volume is entirely enclosed by a membrane composed of lipid molecules (e.g. phosphotidylcholine, cholesterol) 88. Several methods are commonly used to prepare liposomes, like micro-emulsification, sonication, french pressure cell, membrane extrusion, organic solvent injection and reverse phase evaporation 89. All the aforementioned methods are associated with problems, such as need of large amount of organic solvent, many steps involved and high energy consumption, which limit their wide application. SCF technique is used to solve above problems.

    Frederiksen et al.90 prepared liposomes by using modified RESS process. They have dissolved phospholipids and cholesterol in SCF under high pressure followed by depressurization in a low pressure chamber and simultaneously mixed with water containing dextran and fluoroscein isothiocyanate to produce liposomes. In this method, the diameter of obtained liposomes was 200 nm and the organic solvent required was 15 times less than ethanol injection method 91. Till date many scientist used SCF principle to prepare liposomes 92, 93, 94.

    More recently the concept of pro-liposomes was developed in the view of the shortcomings such as oxidation, fusion, aggregation, and phospholipid hydrolysis resulting in physico-chemical instability associated with liposomes 95, 96. Pro-liposomes can be defined as dry and free flowing particulate system with loaded drugs, which upon dispersion in water converted in to liposome suspension.

    Feix et al.97 prepared pro-liposomes of vitamin-D3 (VD) composed of hydrogenated phosphotidylcholine by SAS method and studied the effect of operational conditions such as temperature, pressure and composition on the loading of VD in pro-liposome. They found temperature of 45 ºC, pressure of 8 MPa and mass ratio of 15 % between VD and lipid provide the optimum condition. The loading efficiency was found to be 12.89 %. In addition, they compared the encapsulation efficiency of pro-liposomes prepared by SAS method and ultrasonic dispersion method and found 100 % of encapsulation in case of SAS method upon dispersion in buffer which was more than that obtained by ultrasonic dispersion method.

    Drying of Proteins and Peptides

    The number of protein such as cyclosporine, insulin, protein hydrolysate are introduced to the market, which is the result of genetic engineering 98. The important aspect about protein and peptide is the stabilization as they are unstable in liquid formulation because of chemical and physical degradation reaction, which necessitates to store in dry form 99. Many traditional drying techniques, such as freeze drying, spray drying, vacuum drying and spray freezing drying, have been used for a long time to stabilize above compounds. But all the above techniques are having drawbacks. For instance, freeze drying is an expensive process due to high energy and time consumption and not providing complete recovery of the intact protein due to process induced degradation (during freezing and drying phase). SCF process is an alternative method to above due to its mild process conditions, cost effectiveness and possible sterilizing properties 100.

    Bouchard et al.101 dried lysozyme particles by using SEDS technique and investigated the particle morphology and molecular integrity. They used ethanol along with SCF to increase solubilization power of CO2 in aqueous solution. They observed three types of particles: (a) agglomerated nanoparticles (200-300 nm) with spherical shape, which agglomerated in to spheroid cluster (5-50 µm), (b) microparticles with ellipsoids to spheroid shape, and (c) microspheres. The agglomerated nanoparticles are formed at highest ethanol concentration because the mass transfer rate of ethanol in to the droplets exceeds the mass transfer of water to extractant phase. The microparticles were produced under competitive rate of antisolvent precipitation and water extraction. The microsphere formation can be explained by the fact that water extraction exceeds antisolvent effect of the ethanol.

    Impregnation

    Impregnation is generally used to incorporate active ingredients in the polymeric matrix. Traditionally, impregnation was carried out by two steps; (1) active ingredients is first dispersed or dissolved in a suitable solvent, and (2) the polymer is soaked in the so formed dispersion or solution 102. The presence of residual solvent in the final substrate can lead to some toxic effects, which was the major concern associated with traditional method. In addition to its nontoxic nature, supercritical impregnation is having swelling and/ or plasticizing effect on the polymer. Impregnation of polymer can be achieved either by deposition or molecular dispersion phenomenon 103, 104

    Masmoodi et al.105 carried out supercritical impregnation of Intraocular lenses (IOLs) made up of polymethylmethacrylate with cefuroxime sodium through batch process (a high pressure impregnation step followed by a depressurization step) and investigated various experimental conditions, such as pressure, temperature, impregnation duration and cosolvent on the impregnation yield. They observed that impregnation yield vary between 0.001-0.029 mgdrug/ mgIOLs and this is enhanced by using the cosolvent (ethanol). The mechanism of impregnation is deposition and in-vitro drug release show a burst release followed by slow release.

    Supercritical Fluid Chromatography and its Application

    Supercritical fluid chromatography (SFC) uses CO2 as mobile phase to dissolve compounds. Unfortunately, CO2 is not a good solvent for polar compounds. But, this problem can be corrected by adding moderate amount of organic solvent, called as modifier 106. The popularity of SFC lies on its advantage over HPLC

    such as (a) faster and more efficient separation of compounds due to lower viscosity and higher diffusivity of CO2, (b) most of the pharmaceutical ingredients used for the synthesis purpose are as soluble or more soluble in mixture of CO2 and organic modifier, (c) recovery of purified compounds from the collected fractions is easier and economical as solubility in CO2 decreases rapidly with decrease in pressure, (d) moreover, mobile phase, CO2, is cheaper, greener and safer as compared to organic solvent 106, 107, 108. There are, generally, two types of SFC, namely packed column and preparative scale.

    The application of SFC includes: (a) chiral (enantiomer) separation e.g., separation of chiral sulfoxide belonging to the family of substituted benzimidazoles by using Chiralpak AD and methanol as stationary phase and modifier, respectively 109. Separation of 44 paires of enantiomers (β-blockers, β-agonist, benzdiazepines, non-steroidal anti-inflammatory drugs, barbiturates, free and derivatized amino acids) were carried out by using common stationary phase (Chiralcel OD and AD, Chirobiotc V and T), CO2 modified with 5-30 % of methanol 110. Liu et al. 111 performed the enantiomeric separation of macrocyclic glycopeptide (teicoplanin) and some of its common derivatives, (b) Separation of achiral compounds such as the separation of mixture of estrogen metabolites 112 and separation of phosphatidylcholine, phosphatidylethanolamine, phosphatidylinositol and phosphatidylserine by SFC coupled with light scattering and mass spectrometric detection 113, (c) analysis of peptides- among the peptides separated and analyzed by SFC are cyclosporin 114, actinomycin D and vancomycin 108, gramycidin A, B, and C 115, (d) Coupling of SFC with mass spectroscopy, which helps to obtained good peak shape and signal in chromatogram 116. A large number of drugs and materials used for various SCF techniques are listed in Table 2.

    Table 2. Active ingredients and materials used for different SCF techniques with their applications
    Sl.no SCF Technique Active Ingredient Material Application Ref.
    1 RESS ArtemisininDiclofenacBechlomethasone-17,21-diapropionateLidocaineDigitoxinRaloxifenCefuroxime axetilRed phosphorousLipase and lysozyme   Dextran and fluoroscein isothiocyanate         ParaffinPolymethylmethacrylate, PEG, polylactic acid (PLA), polylactide-co-glycolide (PLGA) and PEG-PPG (polypropelene glycol)-PEG  Phospholipids and cholesterol MicronizationMicronizationParticle morphology Particle MorphologyMicronizationMicronizationNanonizationCoatingCoating   Liposomes 515254 555758597172   90
    2 PGSS YNS3107 Human growth hormone PEG 400, PEG 4000 and Poloxamer 407 PLGA and PLA Micronize solid dispersion Microparticles 63 64
    3 RESAS Cyclosporine Phospholipid Nanoparticles 61
    4 GAS Puerarin   Polymorphs 48
    5 PCA Budesonde Polylactic acid Microparticles 53
    6 SAS AmoxicillinNaproxen Cefuroxime axitelRifampcinVitamin-D3  Methyl cellulose and ethyl cellulose Polyvinylpyrrolidone-K30Poly (L-lactide)Phosphotidylcholine MicronizationMicrospheres MicroparticlesMicroparticlesPro-liposome 6065 676897
    7 ASAIS Theophylline   Polymorphs 30
    8 SEDS Terbutalin sulphateMorphineLysozyme  PLA Polymorphs MicroparticlesDrying of proteins and peptides 4966101
    9 SFEE Indomethacin and ketoprofen Tripalmitin, tristearin and Gelucire 50/13 Solid lipid nanoparticles 38
    10 SFE Jojoba oil   Extraction 87
    11 CAN-BD Ibuprofen Myristic acid and tripalmitin Solid lipid microparticles 69
    12 SAA CefadroxilCromolyn sodium   MicronizationMicronization 5056

    Conclusions

    A large number of SCF based processes were developed in recent years. There are still possibilities to improve the existing SCF processes by optimizing operational conditions (physical and chemical parameters). Furthermore, many new processes can be developed by understanding the properties of SCFs, nature of solute and their interaction. Of course, SCF based techniques are superior over existing and well established techniques such as milling/crushing for size reduction, soxhlet extraction, spray coating, impregnation by soaking, etc. However, extensive research is required to make it feasible in industrial scale.

    For instance, a commercial operation under the trade name of HIPLEX process is used for the processing of soybean at SafeSoy technologies in Ellsworth, Iowa. This CO2-assisted process resulting in between 80-90% vegetable oil recovery for soybeans and over 90% recovery for canola oil 117. Another extraction process in commercial scale using SCF technology is being carried out at Proderma Biotech (Indo Dutch Joint Venture company created between FeyeCon B.V of Holland and by Indian Promoters of Chemcaps for promoting the Super Critical Fluid technology in India) 118.

    References

    1.Marre S, Roig Y, Aymonier C. (2011) Supercritical microfluidics: Opportunities in flow-through chemistry and materials science. , J. Supercrit. Fluids, Inpress
    2.I M Al-fagih, F K Alanazi, G A Hutcheon, I Y Saleem. (2011) Recent Advances Using Supercritical Fluid Techniques for Pulmonary Administration of Macromolecules via Dry Powder Formulations. Drug Deliv. Letters. 1, 128-134.
    3.J F Brennecke, C A Eckert. (1989) Phase Equilibria for Supercritical Fluid Process Design,&quot;. , Am. Inst. Chem. Eng. J 35, 1409-1427.
    4.Yasuji T, Takeuchi H, Kawashima Y. (2008) Particle design of poorly water-soluble drug substances using supercritical fluid technologies. Adv. Drug Deliv. Rev. 60, 388-398.
    5.P J Sinko.Martin’s physical pharmacy and pharmaceutical sciences; physical chemical and biopharmaceutical principles. in the pharmaceutical sciences, 5th ed.; Lippincott Williams and Wilkins: 351 West Camden , street Baltimore, MD .
    6.Vasukumar K, K A Bansal. (2003) Supercritical fluid technology in pharmaceutical research. , Curr. Res. Infor. Pharm. Sci 4, 8-12.
    7.W J Schmitt, Reid R C. (1986) The use of entrainers in modifying the solubility of phenanthrene and benzoic acid in supercritical carbon dioxide and ethane. Fluid Phase Equilibria. 32, 77-99.
    8.Brunner E J Chem Thermochim. (1985) . 17, 672-679.
    9.Pasquali I, Bettini R, Giordano F. (2008) Supercritical fluid technologies: An innovative approach for manipulating the solid-state of pharmaceuticals. , Adv. Drug Deliv. Rev 60, 399-410.
    10.Reverchon E, Adami R. (2006) Nanomaterials and supercritical fluids. , J. Supercrit. Fluids 37, 1-22.
    11.E M Phillips, V J Stella. (1993) Rapid expansion from supercritical solutions: application to pharmaceutical processes. , Int. J. Pharm 94, 1-10.
    12.Kayrak D, Akman U, Hortacsu O. (2003) . , Micronisation of ibuprofen by RESS.J. Supercrit. Fluids 26, 17-31.
    13.Jung J, Perrut M. (2001) Particle design using supercritical fluids: literature and patent survey. , J. Supercrit. Fluids 20, 179-219.
    14.Date A A, Patravale V B. (2004) Current strategies for engineering drug nanoparticles. , Curr. Opin. Colloid Interface Sci 9, 222-235.
    15.Reverchon E, Pallado P. (1996) Hydrodynamic modeling of the RESS process. , J. Supercrit. Fluids 9, 216-221.
    16.York P. (1999) Strategies for particle design using supercritical fluid technologies. Pharm. Sci. Technolo. Today 2, 430-440.
    17.Thakur R, R B Gupta. (2006) Formation of phenytoin nanoparticles using rapid expansion of supercritical solution with solid cosolvent (RESS-SC) process. , Int. J. Pharm.308,(190-199)
    18.Domingo C, F E Wubbolts, Rodríguez-Clemente R, Rosmalen G M V. (1999) Solid crystallization by rapid expansion of supercritical ternary mixtures. , J. Cryst. Growth,198 760-766.
    19.Chen A-Z, Zhao Z, Wanga S-B, Li Y, Zhao C et al. (2011) A continuous RESS process to prepare PLA–PEG–PLA microparticles. , J. Supercrit. Fluids 59, 92-97.
    20.A H-J Chiou, Yeh M-K, Chen C-Y, Wang D-P. (2007) Micronization of meloxicam using a supercritical fluids process. , J. Supercrit. Fluids 42, 120-128.
    21.Weidner E, Petermann M, Knez Z. (2003) Multifunctional composites by high-pressure spray processes. , Curr. Opin. Solid State Mater. Sci 7, 385-390.
    22.Almeida A J, Souto E. (2007) Solid lipid nanoparticles as a drug delivery system for peptides and proteins. Adv. Drug Deliv. Rev. 59, 478-490.
    23.M J, Pathak P, Beacham F, L F Allard, Sun Y-P. (2005) Nanoparticle formation in rapid expansion of water-in-supercritical carbon dioxide microemulsion into liquid solution. , J. Supercrit. Fluids 34, 91-97.
    24.Reverchon E, Adami R. (2006) Nanomaterials and supercritical fluids. , J. Supercrit. Fluids 37, 1-22.
    25.Huang J, Moriyoshi T. (2008) Preparation of stabilized lidocaine particles by a combination of supercritical CO2 technique and particle surface control. , J. Mater. Sci 43, 2323-2327.
    26.Turk M, Lietzow R. (2004) Stabilized Nanoparticles of Phytosterol by Rapid Expansion From Supercritical Solution Into Aqueous Solution. AAPS PharmSciTech. 5, 1-10.
    27.Ventosa N, Sala S, J DELOS Veciana. (2003) process: A crystallization technique using compressed fluids 1. Comparison to the GAS crystallization method. , J. Supercrit. Fluids 26, 33-45.
    28.Boutin O, Maruejouls C, Charbit G. (2007) A new system for particle formation using the principle of the SAS process: the concentric tube antisolvent reactor(CTAR). , J. Supercrit. Fluids 40, 443-451.
    29.Boutin O. (2009) Modeling of griseofulvin recrystallization conducted in a super-critical antisolvent process. , Cryst. Growth Design 9, 4438-4444.
    30.M A Rodrigues, Padrela L, Geraldes V, Santos J, H A Matos et al. (2011) Theophylline polymorphs by atomization of supercritical antisolvent induced Suspensions. , J. Supercrit. Fluids 58, 303-312.
    31.Yeo S-D, Kiran E. (2005) Formation of polymer particles with supercritical fluids: A review. , J. Supercrit. Fluids 34, 287-308.
    32.Palakodaty S, York P, Pritchard J. (1998) Supercritical fluid processing of materials from aqueous solutions: the application of SEDS to lactose as a model substance. , Pharm. Res 15, 1835-1843.
    33.Bałdyga J, Czarnocki R, B Y Shekunov, K B Smith. (2010) Particle formation in supercritical fluids-Scale-up problem. , Chem. Engg. Res. Design 88, 331-341.
    34.W Z He, Q L Suo, Z H Jiang, Shan A, H L. (2004) Precipitation of ephedrine by SEDS process using a specially designed prefilming atomizer. , J. Supercrit. Fluids 31, 101-110.
    35.He W, Suo Q, Hong H, Shan A, Li C et al. (2007) Production of natural carotene-dispersed polymer microparticles by SEDS-PA co-precipitation. , J. Mater. Sci 42, 3495-3501.
    36.Moshashaee S, Bisrat M, R T Forbes, Nyqvist H, York P. (2000) Supercritical fluid processing of proteins. I. Lysozime precipitation from organic solution. , Eur. J. Pharm. Sci 11, 29-41.
    37.M H Hanna, York P. (1999) Methods and apparatus for particle formation. European Patent WO 9959710 .
    38.Chattopadhyay P, B Y Shekunov, Yim D, Cipolla D, Boyd B et al. (2007) Production of solid lipid nanoparticle suspensions using supercritical fluid extraction of emulsions (SFEE) for pulmonary delivery using the AERx system. Adv. Drug Deliv. Rev. 59, 444-453.
    39.R E Sievers, Karst U, P D Milewski, S P, B A Miles et al. (1999) Formation of aqueous small droplet aerosol assisted by supercritical carbon dioxide. Aerosol Sci. Technol 30, 3-15.
    40.Charbit G, Badens E, Boutin O. (2004) In: Methods of particle production;. P. York, U.B. Kompella, B.Y. Shekunov, eds.;Marcel Dekker , Inc.,New York, USA
    41.Reverchon E. (2002) Supercritical-assisted atomization to produce micro- and/or nanoparticles of controlled size and distribution. , Ind. Eng. Chem. Res 41, 2405-2411.
    42.Reverchon E.Process for the production of micro and/or nano particles. , WO A 1(2003004142), 20030116.
    43.Rodriguez-Spong B, C P Price, Jayasankar A, A J Matzger, Rodriguez-Hornedo N. (2004) General principles of pharmaceutical solid polymorphism: a supramolecular perspective. Adv. Drug Deliv. Rev. 56, 241-274.
    44.Kawakami K. (2007) Reversibility of enantiotropically-related polymorphic transformations from a practical viewpoint: thermal analysis of kinetically reversible/-irreversible polymorphic transformations. , J. Pharm. Sci 96, 982-989.
    45.Zhang G G Z, Law D, E A Schmitt, Qiu Y. (2004) Phase transformation considerations during process development and manufacture of solid oral dosage forms. Adv. Drug Deliv. Rev. 56, 371-390.
    46.Pasquali I, Bettini Ruggero, Giordano R, F. (2008) Supercritical fluid technologies: An innovative approach for manipulating the solid-state of pharmaceuticals. , Adv. Drug Deliv. Rev 60, 399-410.
    47.York P. (2000) Particle design: a ‘Supercritical’ issue for the pharma industry. Pharm.Visions. 28-30.
    48.Li Y, D J Yang, Zhou W, S B Chen, S L Chen. (2012) Recrystallization of puerarin using the supercritical fluid antisolvent process. , J. Cryst. Growth 340, 142-148.
    49.Rehman M, B Y Shekunov, York P, Lechuga-Ballesteros D, D P Miller et al. (2004) Optimisation of powders for pulmonary delivery using supercritical fluid technology. , Eur. J. Pharm. Sci 22, 1-17.
    50.Zhiyi L, Jingzhi J, Xuewu L, Huihua T, Wei W. (2009) Experimental investigation on the micronization of aqueous cefadroxil by supercritical fluid technology. , J. Supercrit. Fluids 48, 247-252.
    51.T V Nijlen, Brennan K, G V Mooter, Blaton N, Kinget R et al. (2003) Improvement of the dissolution rate of artemisinin by means of supercritical fluid technology and solid dispersions. , Int. J. Pharm 254, 173-181.
    52.A Z Hezave, Esmaeilzadeh F. (2011) The effects of RESS parameters on the diclofenac particle size. Adv. Powder Technol 22, 587-595.
    53.T M Martin, Bandi N, Shulz R, C B Roberts, U B Kompella. (2002) . Preparation of Budesonide and Budesonide-PLA Microparticles Using Supercritical Fluid Precipitation Technology. AAPS PharmSciTech 3, 1-11.
    54.P A Charpentier, Jia M, R A Lucky. (2008) Study of the RESS Process for Producing Beclomethasone-17,21-Dipropionate Particles Suitable for Pulmonary Delivery. AAPS PharmSciTech. 9, 39-46.
    55.Kim J-T, Kim H-L, Ju C-S. (2010) Micronization and characterization of drug substances by RESS with supercritical CO2. , Korean J. Chem. Eng 27, 1139-1144.
    56.Reverchon E, Adami R, Caputo G. (2007) Production of Cromolyn Sodium Microparticles for Aerosol Delivery by Supercritical Assisted Atomization. AAPS PharmSciTech. 8,E1-E9
    57.Atila C, Yildiz N, Caliml A. (2010) Particle size design of digitoxin in supercritical fluids. , J. Supercrit. Fluids 51, 404-411.
    58.Keshavarz A, Karimi-Sabet J, Fattahi A, A, Rafiee-Tehrani M et al. (2012) Preparation and characterization of raloxifene nanoparticles using Rapid Expansion of Supercritical Solution(RESS). , J. Supercrit. Fluids, Inpress
    59.Varshosaz J, Hassanzadeh F, Mahmoudzadeh M, Sadeghi A. (2009) Preparation of cefuroxime axetil nanoparticles by rapid expansion of supercritical fluid technology. Powder Technol. 189, 97-102.
    60.Montes A, Tenorio A, Gordillo Pereyra, Ossa E J M C. (2010) Screening design of experiment applied to supercritical antisolvent precipitation of amoxicillin: Exploring new miscible conditions. , J. Supercrit. Fluids 51, 399-403.
    61.T J Young, K P Johnston, G W Pace, A K Mishra. (2003) Phospholipid-Stabilized Nanoparticles of Cyclosporine A by Rapid Expansion from Supercritical to Aqueous Solution. AAPS PharmSciTech. 5, 1-16.
    62.Vyas S P, Khar R P. (2005) Controlled drug delivery, concepts and advances. Vallabh Prakashan: Delhi, 1st ed.;pp 175 .
    63.Brion M, Jaspart S, Perrone L, Piel G, Evrard B. (2009) The supercritical micronization of solid dispersions by Particles from Gas Saturated Solutions using experimental design. , J. Supercrit. Fluids 51, 50-56.
    64.Jordan F, Naylor A, C A Kelly, S M Howdle, Lewis A et al. (2010) Sustained release hGH microsphere formulation produced by a novel supercritical fluid technology: In vivo studies. , J. Control. Rel 141, 153-160.
    65.Duarte A R C, M S Costa, A L Simplicio, M, Duarte C M M. (2006) Preparation of controlled release microspheres using supercritical fluid technology for delivery of anti-inflammatory drugs. , Int. J. Pharm 308, 168-174.
    66.Zhang Y-Z, Liao X-M, Yin G-F, Yuan P, Huang Z-B et al. (2012) Preparation of water soluble drugs-loaded microparticles using modified solution enhanced dispersion by supercritical CO2. Powder Technol. In press
    67.I N Uzun, Sipahigil O, Dincer S. (2011) Coprecipitation of Cefuroxime Axetil-PVP composite microparticles by batch supercritical antisolvent process. , J. Supercrit. Fluids 55, 1059-1069.
    68.Patomchaiviwat V, Paeratakul O, Kulvanich P. (2008) Formation of Inhalable Rifampicin-Poly(L-lactide) Microparticles by Supercritical Anti-solvent Process. AAPS PharmSciTech. 9, 1119-1129.
    69.Wang X, Chen H, Guo Y, Su Y, Wang H et al. (2008) Preparation of ibuprofen/lipid composite microparticles by supercritical fluid technique. , China, Front. Chem. Eng 2, 361-367.
    70.Santos I R D, Pech J R B, Thies C, J P Benoit. (2002) Microencapsulation of protein particles within lipids using a novel supercritical fluid process. , Int. J. Pharm 242, 69-78.
    71.Liu Y, Li X, Zhang F, Sun Y, Zhao G. (2009) Design and characteristic analysis of a new nozzle for preparing microencapsulated particles byRESS. , J. Coat. Technol. Res 6, 377-382.
    72.Mishima K, Matsuyama K, Tanabe D, Yamauchi S, T J Young et al. (2000) Microencapsulation of proteins by rapid expansion of supercritical solution with a nonsolvent. AIChE J. 46, 857-865.
    73.Nielsen S S. (1998) Food analysis: crude fat analysis, 2nd ed.;Purdue University. , West Lafayette, Indiana
    74.Naude Y, Beer W H J De, Jooste S, Merwe L Van der, Rensburg S J Van. (1998) Comparison of supercritical fluid extraction and Soxhlet extraction for the determination of DDT. DDD and DDE in sediment. Water SA 24, 205-214.
    75.J A Henning, R J Core, J L Gardea-Torresdey. (1994) Extracting volatile compounds from single plants using supercritical fluid extraction. Crop Sci. 34, 1120-1122.
    76.Stashenko E E, M A Puertas, M Y Combariza. (1996) Volatile secondary metabolites from Spilanthes americana obtained by simultaneous steam distillation-solvent extraction and supercritical fluid extraction. , J. Chromatography A 752, 223-232.
    77.K M Song, S W Park, W H Hong, Lee H, S et al. (1992) Isolation of vindoline by supercritical fluid extraction. , Biotechnol. Progress 8, 583-586.
    78.W K Modey, D A Mulholland, M W Raynor. (1996) Review: analytical supercritical fluid extraction of natural products. , Phytochem. Analysis 7, 1-15.
    79.Iwai Y, Morotomi T, Sakamoto K, Koga Y, Arai Y. (1996) High-pressure vapor–liquid equilibria for carbon dioxide +. , Limonene. J. Chem. Eng. Data 41, 951-952.
    80.Marteau P, Obriot J, Tufeu R. (1995) Experimental determination of vapor–liquid equilibria of CO2. , Limonene and CO2 + citral mixtures. J. Supercrit. Fluids 8, 20-24.
    81.Reverchon E, I D Marco. (2006) Supercritical fluid extraction and fractionation of natural matter. , J. Supercrit. Fluids 38, 146-166.
    82.Akgun M, N A Akgun, Dincer S. (1999) Phase behaviour of essential oil components in supercritical carbon dioxide. , J. Supercrit. Fluids 15, 117-125.
    83.Illes V, H G Daood, Perneczki S, Szokonya L, Then M. (2000) Extraction of coriander seed oil by CO2 and propane at super- and subcritical conditions. , J. Supercrit. Fluids 17, 177-186.
    84.Molero A, E G Omez, Ossa M. (2002) Quality of borage seed oil extracted by liquid and supercritical carbon dioxide. , Chem. Eng. J 88, 103-109.
    85.Szentmihalyi K, Vinkler P, Lakatos B, Illes V, Then M. (2002) Rose hip (Rosacanina L.) oil obtained fromwaste hip seeds by different extraction methods. Biores. Technol 82, 195-201.
    86.J M Valle, Rivera O, Mattea M, Ruetsch L, Baghero J et al. (2004) Supercritical CO2 processing of pretreated rosehip seeds: effect of process scale on oil extraction kinetics. , J. Supercrit. Fluids 31, 159-174.
    87.Salgina U, Calimli A, B Z Uysal. (2004) Supercritical Fluid Extraction of Jojoba Oil. , J. Ame. Oil Chemist’s Society 81, 293-296.
    88.A D Bangham, Standish M M, J C Watkins. (1965) Diffusion of univalent ions across the lamellae of swollen phospholipids. , J. Molecular Bio 13, 238-252.
    89.Jain S K, N K Jain. (2011) . In: Controlled and Novel drug delivery; Jain, N.K, 1st ed.; CBS publishers and Distributors,New Delhi,pp 304-352.
    90.Frederiksen L, Anton K, Hoogevest V A N, Keller P, Leuenberger H R H. (1997) Preparation of liposomes encapsulating water-soluble compounds using supercritical carbon dioxide. , J. Pharm. Sci 86, 921-928.
    91.Batzri S, E D Korn. (1973) Single bilayer liposomes prepared without sonication. , Biochim. Biophys. Acta: Biomembr 298, 1015-1019.
    92.T P Castor. (2005) Phospholipids nanosomes. , Curr. Drug Deliv 2, 329-340.
    93.Otake K, Imura T, Sakai H, Abe M. (2001) Development of a new preparation method of liposomes using supercritical carbon dioxide. Langmuir. 17, 3898-3901.
    94.Otake K, Shimomura T, Goto T, Imura T, Furuya T et al. (2006) One-step preparation of chitosan-coated cationic liposomes by an improved supercritical reverse-phase evaporation method. Langmuir. 22, 4054-4059.
    95.L D Mayer, M B Baly, K J Hope, P R Cullis. (1986) Techniques for encapsulating bioactive agents into liposomes. , Chem. Phys. Lipids 40, 333-345.
    96.Xiao Y Y, Y M Song, C Z Peng, Q N Ping. (2006) Preparation of silymarin proliposome: A new way to increase oral bioavailability of silymarin in beagle dogs. , Int. J. Pharm.,319 162-168.
    97.Fei X, Heyang J, Yaping Z, Xinqiu G. (2011) Supercritical Antisolvent-based Technology for Preparation of Vitamin D3 Proliposome and Its Characteristics. Chinese. 19, 1039-1046.
    98.G K Jain. (2001) . In:Advances in Controlled and Novel drug delivery; Jain, N.K,1sted;pp 232-267.
    99.Manning, M C Patel, Borchardt K, T R. (1989) Stability of protein pharmaceuticals. , Pharm. Res 6, 903-918.
    100.A K Dillow, Dehghani F, J S Hrkach, N R Foster, Langer R. (1999) Bacterial inactivation by using near- and supercritical carbon dioxide. Proc. Natl. Acad. Sci 96, 10344-10348.
    101.Bouchard A, Jovanovic N, Jiskoot W, Mendes E, Witkamp G-J et al. (2007) Lysozyme particle formation during supercritical fluid drying: Particle morphology and molecular. 40, 293-307.
    102.Lopez-Periago A, Argemi A, J M Andanson, Fernandez V, C A Garcia-Gonzalez et al. (2009) Impregnation of a biocompatible polymer aided by supercritical CO2: evaluation of drug stability and drug–matrix interactions. , J. Supercrit. Fluids 48, 56-63.
    103.Kikic I, Vecchione F. (2003) Supercritical impregnation of polymers. , Curr. Opinion Solid State Mate. Sci 7, 399-405.
    104.V P Costa, Braga M E M, J P Guerra, Duarte A R C, Duarte C M M et al. (2010) Development of therapeutic contact lenses using a supercritical solvent impregnation method. , J. Supercrit Fluids 52, 306-316.
    105.Masmoudi Y, L B Azzouk, Forzano O, Andre J-M, Badens E. (2011) Supercritical impregnation of intraocular lenses. , J. Supercrit. Fluids 60, 98-105.
    106.Guiochon G, Tarafder A. (2011) Fundamental challenges and opportunities for preparative supercritical fluid Chromatography. , J Chromatogra. A 1218, 1037-1114.
    107.Rajendran A. (2012) Design of preparative-supercritical fluid chromatography. , J Chromatogra. A 1250, 227-249.
    108.L T Taylor. (2009) Supercritical fluid chromatography for the 21st century. , J. Supercrit. Fluids 47, 566-573.
    109.Toribio L, Alonso C, M J Nozal, J L Bernal, J. (2006) Enantiomeric separation of chiral sulfoxides by supercritical fluid chromatography. , J. Sep. Sci 29, 1363-1372.
    110.Medvedovici A, Sandra P, Toribio L, David F. (1997) Chiral Packed Column Subcritical Fluid Chromatography on Polysaccharide and Macrocyclic Antibiotic Chiral Stationary Phases. , J Chromatogra. A 785, 159-171.
    111.Berthod A, T L Xiao, Liu Y, W S Jenks, D W Armstrong. (2002) Separation of chiral sulfoxides by liquid chromatography using macrocyclic glycopeptide chiral stationary phases. , J Chromatogra. A, 955, 53 – 69.
    112.J M Roman, Abbott E, Xu X, S D Fox, T D Veenstra et al. (2007) Optimization of experimental parameters for packed column supercritical fluid chromatography. , J. Liq. Chromatogr. Rel. Technol 30, 2037-2044.
    113.Yip H S H, Ashraf-Khorassani M, L T Taylor. (2007) Feasibility of phospholipids separation by packed column SFC with mass spectrometric and light scattering detection. , Chromatographia 65, 655-665.
    114.Aaltonen O, Aikio M, Lundel J, Ruohonen S, Parvinen L et al. (1998) . Polypeptide Purification with Industrial-Scale Supercritical Fluid Chromatography Pharma Tech. Eur. 10, A 42-A 54.
    115.K B Thurbide, Zhang J. (2005) Separation of linear gramicidins using carbon dioxide-containing mobile phases. , Anal. Bioanal. Chem 382-1227.
    116.Zhang X, M H Towle, C E Felice, J H Flament, W K Goetzinger. (2006) Development of a mass-directed preparative supercritical fluid chromatography purification system. , J. Comb. Chem 8, 705-714.
    117.J W King, Srinivas K. (2009) Multiple unit processing using sub- and supercritical fluids. , J. Supercrit Fluids 47, 598-610.
    118.Biotech Proderna. (2012) . http://proderna.com/english/procedure_eng.htm (Accessed on 18.

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