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Elsayed, Nada H.
Leaching of active ingredients from blueberries and cranberries using supercritical carbon dioxide and ethanol as an entrainer and analyzing using GC/MS
h [electronic resource] /
by Nada H. Elsayed.
[Tampa, Fla] :
b University of South Florida,
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Thesis (M.S.B.E.)--University of South Florida, 2009.
Includes bibliographical references.
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ABSTRACT: Routine consumption of blueberries and cranberries has been shown to have great health benefits. Blueberries have high amounts of anthocyanin content per serving. Anthocyanins are known to be powerful antioxidants and are linked to the reduction of heart disease and cancer. New research suggests that the berries may also play a role in slowing down age related diseases such as memory loss and tissue damage caused by Alzheimer's. In addition the berries have a variety of essential vitamins and minerals that are important for overall health. Cranberries have long been used to treat urinary tract infections due to the high composition of benzoic and other acids. Both types of berries are rich in vitamin A and retinoids which have been linked to reducing certain cancers such as colon, lung and breast cancer in addition to the benefits they encompass for maintenance of eyesight.The health benefits associated with the components in the berries make them an attractive choice for extracting desirable active ingredients. A dynamic high pressure extraction setup that consisted of an extractor and a collection vessel maintained at high pressure using back pressure regulators was built to extract active components from the berry powders using supercritical CO and an entrainer (ethanol) in order to increase the solvating power of the supercritical fluid. Experiments were done at temperatures ranging from 42C to 50C and pressures up to 197 bars; extracts were analyzed using a gas chromatograph coupled with a mass spectrometer (GC/MS). Successfully extracted desirable components included important vitamins such as vitamin A and biotin. Furthermore useful acids such as ricinoleic acid, palmitic acid, benzoic acid and the omega-9 acids oleic acid as well as octadecanoic acids were extracted.In addition to the desired active ingredients extracted, at the operating conditions chosen, some pesticides and insecticides that were present in the initial fruit powders were also extracted.
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Advisor: Aydin K. Sunol, Ph.D.
Chromatography, High Pressure Liquid.
Chromatography, Supercritical Fluid.
t USF Electronic Theses and Dissertations.
Leaching of Active Ingredients From Blueberries and Cranberries Using Supercritical Carbon Dioxide and Ethanol as an Entrainer and Analyzing Using GC/MS by Nada H. Elsayed A thesis submitted in partial fulfillment of the requirements for the degree of Master of Science in Biomedical Engineering Department of Chemical and Biomedical Engineering College of Engineering University of South Florida Major Professor: Aydin K. Sunol, Ph.D. Sermin Sunol, Ph.D. Doug Shytle, Ph.D. Date of Approval: March 26, 2009 Keywords: extraction, high pressure, co solvent, carbon dioxide, ethanol, blueberries, cranberries Copyright 2009, Nada H. Elsayed
Dedication I dedicate this work to the wonderful people in my life. To my amazing mom, Salwa who has taught me to have faith and courage and has always been my greatest supporter. To my dad, Hamdy who has always been the kindest most supportive father. Finally to the love of my life, Mostafa, who is always by my side, giving me strength, support, unconditional love and who has taught me to always be strong and stand up for my dreams. To them I truly thank from the bottom of my heart and dedicate this work.
Acknowledgments I would like to acknowledge everyone who has helped me bring this work to a completion. I would like to give my sincere gratitude to Dr. Sunol who has always provided me with support and has guided me through the duration of this project in such a great way. Dr. Sermin who always gave me directional advice in a very calm way. Dr. Shytle for helping bring the idea for this project. Brandon Smeltzer who constantly took the time to help me improve my work by providing endless positive feedback and helpful advice, thank you for always helping me. Raquel Carvallo who was always there to offer a supporting hand and help me when I was desperate; thank you for always taking the time to help me with my setup and help me figure things out. Haitao Li (Eddie), the impossible missionsÂ’ guy, who always helped me when I was stuck with equipment and pressure issues. Wade Mack and Loi Ho for kindly offering a helping hand when I needed it. Anh Tdo for always making time for my samples, running the GC/MS and helping me analyze the extracts. To the chemical engineering office staff, Carla, Cay, Sandy and Ed; thank you for constantly helping me and calming me when I thought I had missed deadlines or needed software help and was panicking.
i Table of Contents List of Tables iii List of Figures iv List of Equations vi Nomenclature xi Superscript xvi Subscript xviii Abstract xix Chapter 1: Introduction to Supercritical Fluids and Use of Berries as Raw Material for Medicinal Extracts 1 1.1 Production 5 Chapter 2: History and Background of Supercritical Fluids 10 2.1 The Critical State 10 2.2 Retrograde 12 2.3 Supercritical CO2 12 2.4 Different Methods Employing Supercritical CO2 13 2.5 Co Solvents 14 2.6 Static Setup 15 2.7 Dynamic Setup 16 Chapter 3: Review of Literature Citing Extraction of Natural Components 17 Chapter 4: Fundamentals of Mass Transfer and Phase Equilibria Relating to Supercritical Fluid Extraction 29 4.1 Mass Transfer 29 4.2 Solid Extraction Using Supercritical Fluids 30 4.3 Solid Fluid Equilibria 34 4.4 Solid Liquid Vapor Equilibrium 36 4.5 Flow 39 4.6 Mass Transfer Coefficients 41 4.7 Gibbs Free Energy 44
ii 4.8 Equations of State 49 4.9 Van Der Waals 50 4.10 Peng Robinson 51 4.11 NRTL 52 4.12 Mixing Rules 54 Chapter 5: Experimental Setups and Procedures 57 5.1 High Pressure Experimental Setup 57 5.2 Soxhlet Extraction and Experimental Setup 58 5.3 Equipment Specifications 60 5.3.1 Extraction and Collection Vessels 60 5.3.2 Temperature Controllers 60 5.3.3 Wet Test Meter 60 5.3.4 Gas Chromatograph & Mass Spectrometer 60 5.4 Experimental Procedures 61 5.4.2 Preparing the Equipment 61 5.4.3 Beginning an Experiment 62 5.4.4 Shut Down Procedure 63 5.4.5 Cleaning Procedure 64 5.4.6 Soxhlet Extraction Procedure 64 5.4.7 Soxhlet Extraction Cleaning Procedure 65 Chapter 6: Results and Discussion 66 6.1 Results 67 6.2 Discussion 84 Chapter 7: Conclusions, Recommendations and Future Directions 92 7.1 Conclusions 92 7.2 Recommendations and Future Directions 92 References 95 Appendices 99 Appendix A Tables of BB and CB Nutritional Information 100 Appendix B Sample Calculations 102 Appendix C Simplified Procedure 105
iii List of Tables Table 1: Transport Properties of Gases, Liquids and Supercritical Fluids 11 Table 2: Significant Recent Publications Discussing Supercritical Technology 18 Table 3: Velocity at Different Reynolds Values 41 Table 4: Phase Effect on Velocity and Mass Transfer Coefficient 44 Table 5: Blueberry Experimental Conditions and Corresponding Extract 67 Table 6: Cranberry Experimental Conditions and Corresponding Extract 68 Table 7: Blueberry and Cranberry Soxhlet Extraction Experimental Conditions and Results 69 Table 8: Pesticides and Insecticides Extracted 90 Table 9: Blueberry Key Nutrients 100 Table 10: Cranberry Key Nutrients 101
iv List of Figures Figure 1: Path of Carotene to the Development of Vitamin A 7 Figure 2: P x y diagram of CO2 Ethanol 15 Figure 3: Structure of a Plant Cell 31 Figure 4: Total Amount of Extract With Respect to Extraction Time 32 Figure 5: Concentration Profiles Illustrating Path of Extraction from 34 a Solid Material Figure 6: High Pressure Experimental Setup 57 Figure 7: Soxhlet Extraction setup 59 Figure 8: GC of BB Sample at 125 Bars and 41.7C 70 Figure 9: GC of BB Sample at 124 Bars and 43.3C 71 Figure 10: GC of BB Sample at 126 Bars and 45.1C 72 Figure 11: GC of BB Sample at 127 Bars and 45.4C 73 Figure 12: GC of BB Sample at 125 Bars and 46.9C 74 Figure 13: GC of BB Sample at 197 Bars and 46.8C 75 Figure 14: GC of CB Sample at 125 Bars and 46.7C 76 Figure 15: GC of CB Sample at 122 Bars and 46.8C 77
v Figure 16: GC of CB Sample at 125 Bars and 48.3C 78 Figure 17: GC of CB Sample at 123 Bars and 49.9C 79 Figure 18: GC of CB Sample at 194 Bars and 50.4C 80 Figure 19: GC of CB Sample through Soxhlet Extraction with an Ethanol Baseline 81 Figure 20: GC of BB Sample through Soxhlet Extraction with an Ethanol Baseline 82 Figure 21: GC of Ethanol 83 Figure 22: Carotene Molecule 85 Figure 23: Retinol Molecule 85 Figure 24: Benzoic Acid Molecule 87 Figure 25: Ricinoleic Acid Molecule 88 Figure 26: Stearic Acid Molecule 88 Figure 27: Oleic Acid Molecule 89
vi List of Equations Equation 1: Basic Mass Transfer 29 Equation 2: Solid Solubility in Gas Phase of Supercritical Fluid 35 Equation 3: Enhancement Factor 35 Equation 4: Fraction of Solid Dissolved at Constant Molar Volume 36 Equation 5: Modeling Solid Liquid Vapor Equilibrium from Binary Equilibrium Data 37 Equation 6: Modeling Solid Liquid Vapor Equilibrium from Liquid Vapor Equilibrium 37 Equation 7: Modeling Solid Liquid Vapor Equilibrium from Solid Liquid Equilibrium 37 Equation 8: Liquid Phase Fugacity 37 Equation 9: Solid Phase Fugacity 38 Equation 10: Fugacity in Solid Phase Using an Equation of State 38 Equation 11: Solid Vapor Equilibrium Expression 38 Equation 12: Mole Fraction Given a Solute in the Vapor Phase 38 Equation 13: Reynolds Number 39 Equation 14: Solving for Reynolds Number at a Given Velocity 41 Equation 15: Extracted Material Per Unit Time 41
vii Equation 16: Solid Phase Transportation of Extracted Substances 42 Equation 17: Fluid Phase Transportation of Extracted Substances 42 Equation 18: Total Resistance 42 Equation 19: Mean Concentration 43 Equation 20: Prandtl Number 43 Equation 21: Nusselt Number 43 Equation 22: Schmidt Number 43 Equation 23: Sherwood Number 43 Equation 24: Solving for Mass Diffusivity 44 Equation 25: Solving for Mass Transfer Coefficient 44 Equation 26: Gibbs Free Energy 45 Equation 27: Single System Differential Gibbs Free Energy 45 Equation 28: Rate of Change in Gibbs Energy with Respect to System Reaction 45 Equation 29: Gibbs Equation for an Ideal Gas at a Pressure of 1 Bar 46 Equation 30: Simplification of Gibbs Equation in the Differential Form 46 Equation 31: Defining the Energy of a System in Terms of Pressure 46 Equation 32: Fugacity in Terms of 46
viii Equation 33: Limit of Fugacity as P Approaches One 47 Equation 34: Dimensionless Ratio of Fugacity and Pressure 47 Equation 35: Defining Fugacity Coefficient 47 Equation 36: Fugacity Coefficient of Pure Components 47 Equation 37: Fugacity Coefficient for a Vapor Liquid Equilibrium of a Pure Component 47 Equation 38: Fugacity Coefficient in Vapor Phase as it Equals that of Liquid and Saturated Phases 47 Equation 39: Excess Function of Gibbs Energy 48 Equation 40: Excess Energy in Terms of Activity Coefficients and Excess Volume and Enthalpy 48 Equation 41: Excess Volume Defined in Terms of Excess Energy 48 Equation 42: Excess Enthalpy Defined in Terms of Excess Energy 48 Equation 43: Excess Entropy Defined in Terms of Excess Energy 48 Equation 44: Defines Consolute Temperature 49 Equation 45: Cubic Equation of State 50 Equation 46: Van Der Waals Equation 50 Equation 47: Defining Attraction Parameter 50 Equation 48: Defining Repulsion Parameter 50 Equation 49: Lorentz and Berthelot Mixing Rules 51
ix Equation 50: Lorentz and Berthelot Mixing Rules 51 Equation 51: Compressibility Factor 51 Equation 52: Peng Robinson Equation of State 51 Equation 53: Constant a for Peng Robinson 52 Equation 54: Constant b for Peng Robinson 52 Equation 55: Correction for a at Temperatures Other than Critical 52 Equation 56: Vapor Pressure Correlation 52 Equation 57: Peng Robinson Parameter a 52 Equation 58: Peng Robinson Parameter b 52 Equation 59: Peng Robinson Parameter 52 Equation 60: Gibbs Reaction Equation for a Binary Mixture for NRTL Equation 52 Equation 61: Gibbs Reaction Equation for a Binary Mixture for NRTL Equation 53 Equation 62: Mole Fraction of Species 2 for NRTL Equation 53 Equation 63: Mole Fraction of Species 1 for NRTL Equation 53 Equation 64: Addition of Partial Molar Fractions with Respect to Species 2 53 Equation 65: Addition of Partial Molar Fractions with Respect to Species 1 53 Equation 66: Excess Gibbs Energy Using NRTL Equation 53
x Equation 67: NRTL Independent Parameter for Species 1 53 Equation 68: NRTL Independent Parameter for Species 2 54 Equation 69: Gibbs Energy for Species 1 54 Equation 70: Gibbs Energy for Species 2 54 Equation 71: NRTL Activity Coefficient 1 54 Equation 72: NRTL Activity Coefficient 2 54 Equation 73: Van Der Waals Mixing Rule for Constant a 55 Equation 74: Van Der Waals Equation for Constant b 55 Equation 75: Geometric Mean Assumption 55 Equation 76: Constant b for Wong Sandler 56 Equation 77: Constant a for Wong Sandler 56
xi Nomenclature a Attraction Parameter for Van Der Waals Equation ai Activity of Component i Attractive Forces Between Molecule i and Molecule j b Repulsion Parameter for Van Der Waals Equation a/b Equation of State Constants c/d Equation of State Constants A Temperature Parameter Isothermal Compressibility C Equation of State Dependent Constant Cp Specific Heat at Constant Pressure Cv Specific Heat at Constant Volume Mean Concentration of Extracted Components in Solid Starting Material d Change D Diameter
xii F System Non Idealities With Respect to the Fugacity Coefficient F Degrees of Freedom f Fugacity Fugacity in Solution Partial Fugacity of a Given Component in Solution H Enthalpy of System Hvap Heat of Vaporization G Gibbs Work Energy g Pure Substance Gibbs Energies for NRTL Equation Amount of Component Extracted Mass of Solid Substrate m Number of Components in the Mixture for Van Der Waals Mixing Rules N Number of Equilibrium Equations/ Number of Species ni Number of Moles Nu Nusselt Number P Pressure PS Sublimation Pressure
xiii Pc Critical Pressure Pr Prandtl Number R Ideal Gas Constant Re Reynolds Number S Entropy Sc Schmidt Number Sh Sherwood Number T Temperature Tc Consolute Temperature Tc Critical Temperature V Average Velocity V Volume Vs Molar Volume of the Solid Molar Volume X Species Xi Mole Fraction of Component i in Liquid Phase X2 Mole Fraction of Solute in Solution
xiv xi Mole Fraction of Component i Y Mole Fraction in Vapor Phase Y Gas Phase Z Compressibility Factor Zi Mole Fraction of Component i in Solid Phase Change Excess Molar Helmholtz Energy at Infinite Pressure Thermal Expansion Coefficient Vapor Pressure Correlation for PR Natural Log Density Viscosity i Energy of System Mixture Adjustable Parameter Fugacity Coefficient Activity Coefficient Partial Differential
xv Pi Partial Fugacity Coefficient NRTL Independent Parameter Binary Interaction Parameter Wilson Adjustable Parameter Energy Produced Through Interaction Within Each Species and With Each Other in a Binary Mixture Accentric Factor Area Fraction Summation
xvi Superscript Standard State Temperature Degrees + Reference State ^ In Solution Partial Liquid Phase in Liquid Liquid Equilibrium ac Actual Liquid Phase in Liquid Liquid Equilibrium c Consolute comb Combinatorial Energy for Gibbs E Excess Function I Component i id Ideal l Liquid Phase
xvii resi Residual Energy for Gibbs s Solid s Sublimation Pressure sat Saturated v Vapor Phase x Liquid Phase
xviii Subscript 1 Cell Types in NRTL Equation 2 Cell Types in NRTL Equation 1 Supercritical Solvent 2 Liquid Solvent 2 Solute in Solution 3 Solid Solute I Number of Species c Critical l Liquid mixt Mixture s Solid tp Triple Point
xix Leaching of Active Ingredients from Blueberries and Cranberries Using Supercritical Carbon Dioxide and Ethanol as an Entrainer and Analyzing Using GC/MS Nada H. Elsayed ABSTRACT Routine consumption of blueberries and cranberries has been shown to have great health benefits. Blueberries have high amounts of anthocyanin content per serving. Anthocyanins are known to be powerful antioxidants and are linked to the reduction of heart disease and cancer. New research suggests that the berries may also play a role in slowing down age related diseases such as memory loss and tissue damage caused by AlzheimerÂ’s. In addition the berries have a variety of essential vitamins and minerals that are important for overall health. Cranberries have long been used to treat urinary tract infections due to the high composition of benzoic and other acids. Both types of berries are rich in vitamin A and retinoids which have been linked to reducing certain cancers such as colon, lung and breast cancer in addition to the benefits they encompass for maintenance of eyesight. The health benefits associated with the components in the berries make them an attractive choice for extracting desirable active ingredients. A dynamic high pressure extraction setup that consisted of an extractor and a collection vessel maintained at high pressure using back pressure regulators was built to extract active components from the berry powders using supercritical CO2 and an entrainer (ethanol) in order to increase the solvating power of the supercritical fluid. Experiments were done at
xx temperatures ranging from 42C to 50C and pressures up to 197 bars; extracts were analyzed using a gas chromatograph coupled with a mass spectrometer (GC/MS). Successfully extracted desirable components included important vitamins such as vitamin A and biotin. Furthermore useful acids such as ricinoleic acid, palmitic acid, benzoic acid and the omega 9 acids oleic acid as well as octadecanoic acids were extracted. In addition to the desired active ingredients extracted, at the operating conditions chosen, some pesticides and insecticides that were present in the initial fruit powders were also extracted.
1 Chapter 1 Introduction to Supercritical Fluids and Use of Berries as Raw Materials for Medicinal Extracts Blueberries and cranberries are gaining an appreciable amount of popularity because of the new discoveries being made that suggest all the great health benefits associated with their consumption. The berries have been found to have the highest amount of anthocyanin content per serving. Anthocyanins are known to be powerful antioxidants and are linked to the reduction of heart disease and cancer. In addition, the berries are rich in carotenoids and different vitamins such as vitamin A which has a significant role in maintaining eyesight. Recent studies suggest that blueberries may also play a role in slowing down age related diseases such as memory loss and tissue damage caused by AlzheimerÂ’s. Cranberries have also been linked to reducing instances of urinary tract infections because of the essential acids they contain. In addition the berries have a variety of essential vitamins and minerals that are important for overall health. 44 The motivation for this work was to find an effective and green way of extracting the useful, active components in blueberries and cranberries due to the recent research that suggests that blueberries and cranberries are part of the few natural foods containing high anthocyanin contents among other essential vitamins and minerals which may be linked to the reduction of heart disease and cancer with new research being done to uncover many more potential health benefits to the berries44.
2 Use of supercritical fluids in industry as solvents as opposed to organic liquid solvents has been steadily increasing. As fluids are compressed beyond their critical points, their extraction power increases dramatically. Furthermore, recovery of supercritical fluids when used as solvents have been shown to be less costly and more energy efficient than liquid solvents. Supercritical CO2 is the most widely used supercritical fluid because it posses many attractive features. Carbon dioxide, as a gas, is relatively safe to use since it is nonflammable and it has a low toxicity level. Carbon dioxide is not classified as a volatile organic chemical (VOC) and is therefore approved for many uses including food and drug applications. It is non reactive by nature and is considered a green solvent. In the supercritical phase, very small temperature and pressure changes result in relatively large changes in density which then leads to favorable changes in solvent and solvating properties. Supercritical CO2 posses low viscosity, interfacial tension and diffuses like a gas allowing for much better mass transfer within a system as opposed to regular liquid solvents. 58 Supercritical carbon dioxide is not a very effective solvent for polar solutes unless very high pressures are used. To increase the solvating power at moderately high pressures in the supercritical phase, a small amount of a co solvent or entrainer can be added. In the case of supercritical CO2, entrainers include alcohols such as methanol and ethanol58. For this work, ethanol was chosen as the co solvent in the extraction process. The rest of this chapter discusses pertinent aspects of blueberries and cranberries in greater details. Crop conditions as well as soil and fertilization techniques are highlighted. Finally, production statistics are included to stress the idea that awareness of the associated
3 health benefits and consumption are growing for the berries and are thus received by increased production. A discussion of some of the important background concepts regarding the critical state of CO2 as well as that of mixtures is provided in Chapter 2. The chapter also includes a discussion on the use of co solvents, particularly ethanol and the different methods employing the use of supercritical fluids. Relevant previously published studies that relate to this work on natural component extraction using supercritical fluid technology is included in Chapter 3. In addition, an extensive table of important publications discussing supercritical fluid technology and its uses is provided in the chapter. Finally, works that used mathematical correlations to predict solubility as well as a sampling of published material on extraction of material from natural products such as tea leaves and palm kernel oil are discussed. A discussion of the phase equilibria concepts as they relate to this work is provided in Chapter 4. Gibbs Energy and fugacity concepts are discussed in Chapter 4 as well. Mass transfer is included in this chapter as it deals with solid starting materials and particularly plant cells. Changes in mass transfer coefficient with respect to solvent phase and flow are also provided in the same chapter. A discussion of relevant equations of state and possible mixing rules that can be used to predict solubility are included in the later part of the chapter. Schematics of the experimental setups used for this work as well as specifications for each piece of equipment used to conduct the experiments are provided in Chapter 5. In addition, the detailed procedures used to conduct the experiments along with the shut down protocol followed are included in the same chapter.
4 Results obtained from the conducted experiments are discussed in Chapter 6. The corresponding gas chromatographs are included in this chapter. The detailed discussion of the findings obtained post analysis is also included in this chapter. Suggestions that can be used to improve on the results obtained as well as the experimental procedure are provided in Chapter 7. The chapter also includes a future works section that outlines possible techniques that can be used in the future to further analyze the samples and maximize on the results.
5 1.1 Production Blueberries are a member of the Plantae kingdom, family of Ericaceae in the genus Vaccinium which contains more than four hundred different berry species. Several wild types exist in North America such as highbush blueberries, rabbiteye and lowbush blueberries. They are mostly grown in the form of shrubs that are no more than a foot tall and can be found at higher elevations. Lowbush blueberries such as those used for this work are the berry choice for commerce, they grow to be about a foot in height and have a distinctly lighter blue color than other species and are mostly found in Northeastern states. Cultivation of lowbush blueberries does not require much work or time as long as weeding is done on a regular basis; then it becomes a matter of harvesting the berries. Historically, blueberry fields were burned every couple of years to control weed and insect problems but the practice is slowly being replaced with mowing techniques in order to maximize field production and life as burning caused soil oxidation. The foundation for what is now a $300 million dollar a year industry in blueberries was established in the later 1800Â’s by Frederick V. Coville who was able to bread large fruit cultivars. 44 USDA statistics for 2004 have shown that the United States was responsible for producing nearly half of all blueberries used worldwide; an estimated 275 million pounds which is more than a one hundred percent increase in production over a short ten year period, the numbers which continue to rise every year 44. Cultivated blueberries were responsible for most of the revenue for that year; an average of $276 million from a total of about 45,000 acres; 30,000 of which are for lowbush blueberries. Blueberries are a relatively expensive fruit at an average of $1.21 per pound versus other types of fruits sold per pound. This high price may be attributed to the fact that any given field must be burned down to revive plantings causing it to
6 be product able only once every other year. The top three blueberry growing states are Michigan, Maine and New Jersey which typically account for over sixty five percent of all US crop production. Blueberries are used in a variety of products, including baking goods, jams, juices, sweets and even some supplemental vitamins. 44 Blueberries are gaining an appreciable amount of popularity because of the new discoveries being made that suggest all the great health benefits associated with consumption of blueberries. The berries have high amounts of anthocyanin content per serving in addition to many useful vitamins and minerals such as vitamin A, carotene, vitamin C, various B vitamins, calcium, iron, sodium and potassium 44. In 1987, research uncovered that the body makes use of vitamin A by having specific receptors that react to precursors of the vitamin such as the retinoids 5. These receptors, once activated, act on regulating gene expression by targeting and binding to specific DNA sequences. Precursors of vitamin A include various carotenoids and retinal esters that are converted to retinol in the lumen of the intestine; both of which have very specific functions and uses in the body and essentially give rise to vitamin A under proper conditions in the body. Research suggests that carotenoids such as and carotene have been shown to have strong antioxidant functions. 5 The most common precursor of vitamin A is carotene which usually undergoes a splitting process yielding another precursor of vitamin A called retinol before vitamin A is activated as shown below in Figure 1 15.
7 Figure 1: Path of Carotene to the Development of Vitamin A 15 Carotenoids such as carotene, shown in Figure 22 are stored in the body for various functions. For instance some carotene remains un reacted in order to be used for their antioxidant functions and have also been linked to reducing chances of infections and even the development of cancer 5. In addition to the role in reducing heart disease and cancer, anthocyanins are powerful antioxidants, they may also have a potential role in slowing down age related diseases such as memory loss and tissue damage caused by AlzheimerÂ’s 44. Routine blueberry consumption has also been linked to improving vision and reducing eye sight related issues such as eye fatigue and cataracts.
8 Due to the growing awareness of the benefits of the berries, consequently statistics have shown that per capita consumption of blueberries has increased by more than two hundred and fifty percent in the past two and half decades bringing it to about 0.78 pounds per year. Consequently, production of blueberries has been rapidly and steadily increasing over the past decade. The total amount of land dedicated to the production of blueberries is estimated to be more than 60,000 acres in the United States alone with 30,000 acres producing lowbush blueberries. 44 Blueberries are grown in light acidic soil and are often fertilized with ammonium sulphate as opposed to nitrate nitrogen 44. The berry crop is strong enough to handle minor flooding conditions but need to be protected from drought and cold harsh conditions. The maturity of the fruit is determined by the final color as it turns from green to pink and finally to blue indicating full maturity. Since they are delicate fruits, blueberries have a shelf life of only about two weeks which is why so much of the crop is processed industrially and sold in frozen form. 44 Like blueberries, cranberries belong to the Plantae kingdom, family of Ericaceae in the genus Vaccinium with a subgenus of Oxycoccosv. Many cultivars exist, however the most popular include Early Black, Howes, Stevens and Searles. Cranberries like other types of berries have useful antioxidant power and many essential vitamins; however they have been used extensively as a treatment for urinary tract infections (UTIs) as they are rich in benzoic and quinic acid. Once inside the body these acids are easily converted to hippuric acid which is a strong antibacterial acid that helps with UTIs.44 The United States is responsible for producing more than seventy eight percent of the worldÂ’s cranberry production according to statistical data. In 2004, USDA statistics showed that
9 approximately 636 million pounds of cranberries were produced in just over 39,000 acres, accounting for a thirty six percent increase over the previous decade. Total production of cranberries is limited to only five states which are Wisconsin, Massachusetts, Oregon, New Jersey, and Washington. Crop revenue was down to $222 million in 2004 from a record high of $350 million in 1997 due to overproduction caused by improved fruit yield per acre from 1500 pounds per acre to 16000 pounds per acre. Due to overproduction, cranberries tend to be inexpensive at an average price of $0.35 to $0.45 per pound making it a cheap and readily available fruit. Statistics have shown that cranberry production has had an almost unfaltering increase over the past several years, making it an ideal candidate for extraction of potentially useful active ingredients. 44 In the United States alone, more than 39,000 acres are used for planting cranberries and the land dedication has been increasing steadily over the past ten years. The crop is usually flooded in order to protect the developing fruit from drought and frost. However it is a growing practice to use overhead irrigation to get the same affects as a replacement for the flooding technique. 44
10 Chapter 2 History and Background This chapter will discuss some of the important background information of supercritical fluids starting from the definition of the critical state. The chapter will continue discussing some of the relevant properties of supercritical CO2 as well as the attractive features that make it a desirable solvent to use. Co solvents, their importance when used with supercritical fluids and how ethanol is a particularly useful co solvent in this case will be included in this chapter. Finally the chapter will conclude with a discussion of the different experimental setups used with supercritical fluids. 2.1 The Critical State The critical state was discovered in 1822 by Cagniard de la Tour; it is attained at certain temperatures and pressures and is defined as a state where individual gas and liquid properties change significantly in some instances by numerous orders of magnitude and become impossible to differentiate. As the critical state is approached, the density of the liquid begins to decrease while the density of the vapor increases until a single point is reached. This point at a certain pressure and temperature is called the critical point; on a phase diagram it is the point where the phase boundary disappears. The highest temperature value in which two phases, liquid and vapor can exist is known as the critical temperature. The critical pressure of a system is defined in a similar fashion as the highest pressure where two phases can coexist, above such a pressure, only one phase exists. 56
11 The critical state is commonly approximated by getting a series of density measurements at different conditions for both the liquid and gas phases. Initial experiments were done using sealed glass tubes and heating liquids in them and observing the resulting densities. As the critical point is reached, the boundary between both phases disappears. In the case of mixtures, critical properties of the pure components are required in order to attain a possible critical state for the mixture. As the critical point is approached both Cp and Cv increase a great deal along with the thermal conductivity, isothermal compressibility ( ) and thermal expansion coefficient ( ). Meanwhile, the change in heat of vaporization ( Hvap) seems to diminish as the critical point is approached along with the sonic velocity 56. Supercritical fluids when used as solvents combine the mobility of gases along with the solvating power of liquids; Table 1 outlines the transport properties for gases, liquids and supercritical fluids. It can be seen that supercritical fluids have densities closer to those of liquids but diffusivities and viscosities closer to gases. Table 1: Transport Properties of Gases, Liquids and Supercritical Fluids 49 State Condition Property Density, g/cm3 Diffusivity, cm2/s Viscosity, g/cm s Gas 1 atm, 25C 0.6 2*10 3 1 4*10 1 1 3*10 4 Liquid 1 atm, 25C 0.6 1.6 0.2 2*10 5 0.2 3*10 2 SC Fluid Tc, Pc 0.2 0.5 0.5 4*10 3 1 3*10 4 SC Fluid Tc, Pc 0.4 0.9 0.1 1*10 3 3 9*10 4 The critical state of mixtures is defined similar to pure substances when characteristics of the vapor and liquid phases are non differentiable. Variations in the critical temperatures and
12 pressures highly depend on the substances in the mixtures. For similar substances, variations may be linear and it may be non linear for dissimilar ones. For non linear variations, there exist pressures and temperatures above the critical values of the mixture where two phases are present. 56 2.2 Retrograde At this point, it is perhaps important to mention the retrograde phenomenon. It occurs when two phases exist above the critical temperature and pressure. This phenomenon is due to a variation in the amount of condensation of vaporization in the adverse direction of normality (normal behavior) as the pressure and temperature change. 56 2.3 Supercritical CO2 The many attractive features possessed by supercritical CO2 make it a very popular choice for supercritical fluid processes. Supercritical CO2 can be used to inexpensively to fractionate, purify and isolate certain desired chemicals from starting materials. For natural products, it can also be used to remove harmful residual pesticides. Supercritical CO2 doesnÂ’t leave residual chemicals behind, as it leaves system as a gas plus it can be recycled back into the system to cut down on cost. In addition, it is a relatively less expensive method due to the low critical temperature of 31.1C and critical pressure of 73.8 bar associated with CO2 38.In addition, carbon dioxide is not classified as a volatile organic chemical (VOC) and is therefore approved for many uses including food and drug applications. It is un reactive by nature and is considered a green solvent. Supercritical CO2 posses the same attractive features as other supercritical fluids; low viscosity and interfacial tension and it has higher diffusivities similar to those of a gas allowing for much better mass transfer within a system as opposed to regular liquid solvents 58.
13 Supercritical CO2 has been used extensively in the pharmaceutical industry. It is commonly used as an antisolvent for active pharmaceutical compounds by means of re crystallization from organic solvents using such processes as gas antisolvent re crystallization (GAS), precipitation with compressed antisolvents (PCA) and supercritical antisolvent process (SAS). In pharmaceutical practices, supercritical CO2 is also used as a solvent to extract drug compounds without using traditional harmful solvents by means such as rapid expansion of supercritical solutions (RESS) 47. These techniques will be discussed in greater detail in the Different Methods Employing Supercritical Fluids section. 2.4 Different Methods Employing Supercritical Fluids In 2001, Jennifer Jung and Michel Perrut 21 published what is perhaps one of the most extensive and informative literature surveys concerning different methods for particle synthesis using supercritical fluid technology. Supercritical fluids are used as solvents for particle synthesis and encapsulation using a technique called rapid expansion of supercritical solution (RESS) which involves solubilizing the desired compound and then with the help of a nozzle, rapidly and near supersonic velocities, depressurizing the system producing very high purity particles. The limitation of the RESS method is the fact that the compound used must be soluble in the supercritical fluid due to the lack of use of other co solvents; hence it is only useful for low polarity compound. However, as a process, RESS does not involve too many intermediate steps on a small scale since only a single nozzle is necessary to get the desired particles. 21 Gas Anti solvent (GAS) is a technique using supercritical fluids for re crystallization of desired compounds through saturating an already dissolved system with a supercritical fluid thus decreasing the solvating power of the initial polar solvent and causing the particles to re crystallize and leave the solution. In such instances, the supercritical fluid is described as being
14 an anti solvent to the system and produces mostly microparticles. Supercritical fluids are used as anti solvents in another process called supercritical anti solvent process (SAS) which uses a spray nozzle technique to get the desired particles and sizes. Particle sizes can be controlled by changing the rate of anti solvent introduction to the system. The GAS and SAS methods are very promising in drug delivery especially when using supercritical CO2 as they combine the use of a stable, un reactive solvent and allow for the active control of particle size. 21 2.5 Co Solvents At certain temperatures and pressures, some substances are not soluble in supercritical fluids, for this reason the addition of a small amount of a co solvent is useful. Co solvents have the ability to improve the solubility of desired components in supercritical fluid as they provide the required interactions for solubilizing the desired compound 58. It was also discovered that not all co solvents are useful for all chemical species, alcohols; specifically ethanol was determined to be a better solubilizing agent of fatty acids in supercritical CO2 than Octane for instance 3. Methanol and ethanol are two very popular choices for co solvents as they are both soluble in supercritical CO2; for this work, ethanol was chosen as the solvent of choice due to its high solubility in CO2 and stability features at room temperature. The solubility of ethanol in CO2 was done at various temperatures and pressures ranging from 18C (291.15K) to 40C (313.15K) and 8.6 bar (0.86 MPa) to 79.2 bar (7.92 MPa) respectively by Chany Day et al 11,12 and the solubility data obtained was published as shown in Figure 2.
15 Figure 2: P x y Diagram of CO2 Ethanol 11, 12 2.6 Static Setup The solubility of components in a supercritical fluid can be determined using two main types of setups, a static setup or a dynamic setup. Each of the two systems has associated advantages and disadvantages. In a static setup, the main point is that there is a fixed amount of supercritical fluid introduced to the system at the desired operating conditions. In static setups, the holding cells usually have a viewing window where the sample can be observed. The main advantage of using a static setup is that the solubility of the desired component in a binary mixture can be determined without the need for sampling. Sampling can be done on multi component mixtures easily. The system requires a minimal amount of supercritical fluid which may be a factor in cost. If two parameters are fixed such as temperature and composition then 0 0.5 1 1.5 2 2.5 3 3.5 4 4.5 5 5.5 6 6.5 7 7.5 8 8.5 00.20.40.60.81P/MPax1, y1 T=303.12 T=308.11 T=313.14 y at T=303.12 y at T=308.11 y at T=313.14
16 the third parameter can be easily adjusted for a given mixture. However, static systems have the disadvantage of not being able to provide supercritical stripping data. 28 2.7 Dynamic Setup Dynamic setups are characterized by having a continuous flow of supercritical fluid being constantly introduced to the system. Several advantages common to dynamic setups include the ease of having a sampling method for the desired system. Dynamic setups usually do not have viewing cells; hence any type of equipment can be used and modified. Large amounts of data can be obtained using dynamic setups versus static setups. The data obtained can be easily reproduced in a relatively short amount of time. Stripping and fractionating data as well as equilibrium data can be obtained using this type of setup. There are also several disadvantages associated with dynamic setups however. The system must be designed with extreme care to avoid depleting any of the components during a trial. Phase changes and transitions can occur undetected during an experiment. Sampling is usually done on the lighter phase which leaves the solubility in the liquid phase undetermined. Flawed solubility data can be obtained if the liquid phase is pushed out of the column; a possibility that can occur as the density of the supercritical fluid rich phase increases which may become higher than that of the solute containing liquid phase.28
17 Chapter 3 Review of Literature Citing Extraction of Natural Components This chapter will sample previously published materials that are of relevance to this work. An extensive list of relevant publications that deal with supercritical fluids and the uses for the technology published in the last two decades is included at the beginning of the chapter. The chapter will then cover different uses for supercritical fluids along with some useful correlations that have been used and published to predict solid solubility in such fluids. In addition, a sampling of some studies that were published specifically on extraction and fractionation of different berries and natural materials using supercritical fluids will also be highlighted. Finally, an important review published by Abbas et al 1 will be highlighted that discusses the different mechanisms that can occur when extracting using supercritical fluids. Supercritical fluid technology has been extensively researched especially in the past two decades because of all the advantages and potential uses for the technology. As a result, an endless amount of resources and publications that discuss in great detail the technology and the potential it posses for industrial applications, neutraceuticals, food technology and more are constantly being published. An extensive list of some of the important publications and compiled studies that deal with supercritical fluids is provided in Table 2 followed by a sampling of some of the recent significant supercritical extraction studies.
18 Table 2: Significant Recent Publications Discussing the Supercritical Technology Publication Title Publication Type Author(s)/Editor(s) Year Published Key Factors Supercritical Fluid Extraction 28 Book Mark McHugh Val Krukonis 1986 Phase Diagrams for Supercritical Fluid Solute Mixtures Static and Dynamic Methods for Measuring Solubility Phase Behavior: L V, L L V, S F Supercritical Fluid Process Development Studies: 1976 1981 Processing Pharmaceuticals, Natural Products, and Specialty Chemicals in SCF High Temperature Reactions in SCF Viscosity Effects in SCF Enhanced Reaction Rates and Selectivities in SCF Supercritical Fluid Chromatography and Micro HPLC 59 Book: Compilation of Publications M. Yoshioka Simone Parvez 1989 Sub and Supercritical Eluents in Chromatography SCF and Packed Columns SCF Chromatography to Conduct Oligomar Separation Microscale SCF Extraction Applications of Supercritical Fluids in Industrial Analysis 13 Book: Compilation of Publications John R. Dean S. Hitchen 1993 Properties and Fundamentals of SCF Instruments Used for SCF Chromatography Different Depressurization Systems Extraction of Pharmaceuticals Via SCF Chromatography SCF as Related to Polymer Analysis SCF as Related to Environmental Analysis Gas Extraction An Introduction To Fundamentals Of Supercritical Fluids And The Application To Separation Book G.Brunner 1994 Properties of SCFs Principle of Corresponding States Analytical Equations of State Diffusion in Dense Fluids Phase Equilibria Heat and Mass Transfer
19 Processes 6 Methods for Precipitation Using Separation of Solvent and Dissolved Components SCF Extraction from Solid Substrates Countercurrent Extraction: Multistage Supercritical Fluids: Fundamentals for Application24 Book: Compilation of Publications Erdogan Kiran J. M. H. Levelt Sengers 1994 Fluctuation Solutions Theory as Applied to Supercritical Conditions Supercritical Fluid Transport Properties SCF Microstructures Chemistry in Supercritical Fluids Phase Behavior of Supercritical Olefins High Pressure Chemical Engineering: Proceedings of the 3rd International Symposium on High Pressure Chemical Engineering, Zrich, Switzerland, October 7 9, 199655 Book: Compilation of Relevant Work Rudolf von Rohr Ch Trepp 1996 Supercritical Reaction Media to Enhance Activity of Solid Acid Catalysts Oxidation of Organic Material in Different SCFs Enzymatically Catalyzed Reactions in a Supercritical Medium Different Zeolite Catalysts Under Supercritical Conditions High Molecular Weight Alkane Mixtures Fractionated With Supercritical Fluids Cyclic and Swing Adsorption in Supercritical Fluids Supercritical fluid technology in oil and lipid chemistry 23 Book Jerry W. King Gary R. List 1996 SCF Extraction of Lipids and Oilseeds Modeling of Oilseed Solubility and Extraction Egg Lipid Extraction Via SCF Oleochemicals Analyzed Through SCF Chromatography Supercritical Fluids: Extraction and Pollution Prevention2 Book: Compilation of Relevant Work Martin A. Abraham Aydin K. Sunol 1997 Applications of Supercritical Fluid Technology Recovery of Natural Products Using SCFs Mass Transfer in SCFs Potential Applications of SCFs for Environmental Clean Up Analytical Supercritical Fluid Book: Compilation E. D. Ramsey 1998 Diffusion and Solvation Controlled Continuous Dynamic Supercritical Fluid Extraction
20 Extraction Techniques 41 of Relevant Work Supercritical Fluid Extraction On Line and Off Line Sequential and Parallel SCF Extraction Systems Liquid Based Matrices and SCF Extraction Techniques Chemical Synthesis Using Supercritical Fluids26 Book: Compilation of Relevant Work Walter Leitner Philip G. Jessop 1999 Introduction and Phase Behavior of SCFs Different Extraction, Separation and Crystallization Techniques Which Utilize SCFs Spectroscopy of SCFs Fundamentals of Supercritical Fluids10 Book Tony Clifford 1999 Single Components as SCFs Non volatile Substance Solubility in SCFs Extraction and Transport Properties in SCFs The Solubility of Solids in Supercritical Fluids29 Journal Article Janette Mndez Santiago Amyn S. Teja 1999 Mathematical Correlations to Predict Solid Particle Solubility in Supercritical Fluids Predict Certain Conditions Where Solubility is Possible Without Using Too Many Properties Such as Those Required For Equations of State Proposed Model Uses the Clausius Clapeyron Equation to Obtain the Sublimation Pressure and Incorporates the Theory of Dilute Solutions Into A Semi Empirical Relation to Ultimately Predict Solubility Natural Extracts Using Supercritical Carbon Dioxide33 Book Mamata Mukhopadhya 2000 CO2 as a SCF Applications of SCF Technology Solubility Behavior in SCF Thermodynamic Modeling and Mixing Rules Transport Fundamentals in SCF Extraction Stages for Natural Materials Mass and Heat Transfer in SCF Fruit Extraction and Recovery in SCF SCF Extraction and Fractionation of Different Spices, Herbal Extracts and Natural Antioxidants Review: Particle Design Using Supercritical Fluids: Journal Article Jennifer Jung Michel Perrut 2001 Different Methods for Particle Synthesis Using SCFs Rapid Expansion of Supercritical Solution (RESS) Re crystallization Using Supercritical Fluids: Gas Anti
21 Literature and Patent Survey 21 Solvent (GAS) Supercritical Fluids as Anti Solvents: Supercritical Anti Solvent Process (SAS) Supercritical Fluids Molecular Interactions, Physical Properties, and New Applications3 Book Y. Arai T. Sako Y. Takebayashi 2002 Supercritical Fluids at the molecular level Static Properties Phase Equilibria Transport Properties Supercritical Fluid Extraction (Ternary Mix) Organic and Catalytic Reactions in SC CO2 Supercritical Fluid Technology in Materials Science and Engineering: Syntheses, Properties, and Applications48 Book: Compilation of Relevant Work Ya Ping Sun 2002 Catalysis in Supercritical Fluids Supercritical CO2 and In Situ Blending of Electrically Conducting Polymers Surfactants in SCFs SCFs to Produce Magnetic Nanoparticles Processing of Nanoscale Materials in SCFs Green Chemistry Using Liquid and Supercritical Carbon Dioxide14 Book: Compilation of Relevant Work Joseph M. DeSimone William Tumas 2003 Chemistry of Free Radicals in Supercritical CO2 Polymer Solubility in SC CO2 Selective Hydrogenation of Fatty Acids in SCFs Enhancement of Portland Cement Properties Using SCFs Supercritical Carbon Dioxide Extraction of Selected Medicinal Plants Effects of High Pressure and Added Ethanol on Yield of Extracted Substances 19 M. Hamburger D. Baumann S. Adler 2004 Supercritical Extraction of Chemicals From Marigold, Hawthorn and Chamomile Herbs Comparison of Composition of Extractables Obtained at Very High Pressures Using Supercritical Co2 With and Without an Ethanol Co Solvent Determining the Effect of Using Different Compositions of the Co Solvent The Experiments Were Done at Pressure of 300 to 689 Bar and Using 0 to 20% Proportions of Ethanol and a Steady Temperature of 50C Sample Analysis Using GC MS and HPLC PAD MS Supercritical fluids Book Gerd Brunner 2004 Supercritical Fluid Technology in Germany
22 as solvents and reaction media 7 Fundamentals of SCF Pre dependance of Molecular Mobility in SCF Supercritical Fluid Technology for Drug Product Development58 Book: Compilation of Publications Peter York Uday B. Kompella Boris Y. Shekunov 2004 Chemistry and Materials Design for CO2 Processing Fluid Dynamics, Mass Transfer, and Particle Formation in Supercritical Fluids Colloid and Interface Science for CO2 Based Pharmaceutical Processes Development and Potential of Critical Fluid Technology Scale Up Issues for Supercritical Fluid Processing in Compliance with GMP Supercritical Carbon Dioxide (SC CO2) Extraction and Fractionation of Palm Kernal Oil From Palm Kernal as Coca Butter Replacers Blend60 Journal Article Zaidul, I. S., N. A. Nik Norulaini, A. K. Mohd Omar, and R. L. Smith Jr. 2006 Extraction and Fractionation of Palm Kernel Oil From Palm Kernel Using Supercritical CO2 Operating Conditions Used Included Pressures That Ranged From 20.7 Mpa to 48.3 Mpa at Temperatures That Were Between 40 and 80C. High Pressure Samples Were Compared to Those Obtained Using a Traditional Soxhlet Extraction Technique Attempt to Find Alternatives to Using Cocoa Butter in The Food Industry Analysis Done Using Gas Chromatography (GC) and Pulsed Nuclear Magnetic Resonance (PNMR) to Determine the Solid Fat Content of the Extractables GC/MS Characterization of Mate Tea Leaves Extracts Obtained From High Pressure CO2 Extraction20 Journal Article R. A. Jacques J. G. Santos C. Dariva J. Vladimir Oliveira E. B. Caramo. 2007 Extractables Obtained From Mate Tea Leaves (Ilex Paraguariensis) Using Supercritical CO2 The Extracts Were Analyzed With the Assistance of Gas Chromatography Coupled With Mass Spectrometry (GC/MS) Successful Identification of 51 Different Compounds Based on the Peaks Obtained From the Chromatograms The Compounds Identified Included Several Esters,
23 Fatty Acids and Vitamins Optimization of Supercritical Carbon Dioxide Extraction of Sea Buckthorn (Hippopha thamnoides L.) Oil Using Response Surface Methodology 57 Journal Article Xiang Xu Yanxiang Gao Guangmin Liu Qi Wang Jian Zhao 2007 Optimization of SCF Extraction Conditions using response surface methodology (RSM) Analysis of Response Surfaces Experimental Results at Various Pressures and Temperatures Solubility in supercritical carbon dioxide18 Book Ram B. Gupta Jae Jin Shim 2007 A Comprehensive List of Solubility Data of Different Compounds such as Oils, Acids, Tocopherols and More Supercritical Fluid Extraction of Nutraceuticals and Bioactive Compounds27 Book: Compilation of Publications Jos Luis Martinez 2007 Supercritical Extraction of Different Plants Supercritical Extraction of Specialty Oils and Tocopherols Extraction of Active Components from Algae Using SCF SCF Extraction of Antioxidants SCF Extraction of Fish and Other Essential Oils A Review of Supercritical Fluid Extraction as New Analytical Method 1 Journal Article K. A. Abbas A. Mohamed A. S. Abdulamir H. A. Abas 2008 Advantages of Using Supercritical CO2 in The Food Industry Four Different Types of Extraction Mechanisms Simple Dissolution Extraction Mechanism Desorption and Adsorption Swelling Reactive Extraction Diffusion Coefficients of Solids in Supercritical Carbon Dioxide: Modelling of Near Critical Journal Article Isabelle Raspo Christophe Nicolas Evelyne Neau Sofiane Meradji 2008 Concentration Dependence of Diffusion Coefficients Diffusion Coefficients of Different Binary Mixtures in Supercritical CO2 Modified Darken Equation
24 Behaviour42 Extraction of Phenolic Compounds from Elder Berry and Different Grape Marc Varieties Using Organic Solvents and / or Supercritical Carbon Dioxide52 Journal Article Tnde Vatai Mojcca ÂŠkerget ÂŽeljko Knez 2008 Extract of Phenols, Flavonoids, Anthocyanins from Berries Effect of Operating Conditions on Extract Yields Use of Different Co solvents with SC CO2 Optical Spectroscopy and Other Analytical Techniques
25 In 2007, Xiang et al 57published an interesting study on optimizing extract materials from a type of berries called sea buckthorn (Hippopha thamnoides L.) under supercritical carbon dioxide using response surface methodology (RSM). Supercritical extractions were done on the seeds at pressures ranging from 12.8 to 47.2 MPa and temperatures up to 67.2C. The extract obtained according to the study included different oils, vitamin E and carotenoids. The effects of operating conditions such as temperature, pressure and flow rate were analyzed by RSM to determine the optimum conditions for extracting from the berries. The model predicted optimum conditions to be at a pressure of 27.4 Mpa coupled with a temperature of 34.5C and a flow rate of 17 L/hr. The significance of this study lies in the modeling aspect, given that the model successfully predicted optimum extraction conditions for the berries used for the study, indicates that it may be a useful tool for other natural components of interest. Supercritical extraction of natural products is a rapidly growing field; in 2008 Vatai et al52 published a study on extracting active compounds from elder berries and grape pomace using supercritical CO2 with and without entrainers. Extracts were obtained at pressures as high as 30 MPa and temperatures up to 60C. The extract contained high levels of anthocyanins, phenolic compounds, and flavonoids. The study concluded that the supercritical fluid extractions although successful, resulted in low yields; however moderate increases in temperature caused an increase in the amount of extract. In 2004, M. Hamburger et al 19 published a study involving supercritical extraction of chemicals from marigold, hawthorn and chamomile herbs. The study focused on comparing the different composition of extractables obtained at very high pressures using supercritical CO2 with and without an ethanol co solvent and determining the effect of using different compositions of the co solvent. The experiments were done at pressure of 300 to 689 bar and
26 using 0 to 20% proportions of ethanol and a steady temperature of 50C. The authors analyzed the samples using GC MS and HPLC PAD MS. The authors reported extracting lipophilic, polyphenolic and glycosidic compounds.19 Zaidul et al 60 published a study on extraction and fractionation of palm kernel oil from palm kernel using supercritical CO2 in 2006. The operating conditions used were at very high pressures that ranged from 20.7 MPa to 48.3 MPa at temperatures that were between 40 and 80C. The samples obtained at high pressure were compared to those obtained using a traditional soxhlet extraction technique. The purpose of the study was to find alternatives to using cocoa butter in the food industry. The samples were finally analyzed using gas chromatography (GC) and pulsed nuclear magnetic resonance (PNMR) to determine the solid fat content of the extractables. 60 R. A. Jacques et al 20 published a study of extractables obtained from mate tea leaves (Ilex paraguariensis) using high pressure CO2 in 2007. The experiments were done under operating conditions that had varying pressures from 100 to 250 bar and temperatures of 20 to 40C. The extracts were analyzed with the assistance of gas chromatography coupled with mass spectrometry (GC/MS). The authors were able to identify 51 different compounds based on the peaks obtained from the chromatograms. The compounds identified included several esters, fatty acids and vitamins. 20 In 1999, Mndez Santiago and Teja 29 published an important study that uses mathematical correlations to predict solid particle solubility in supercritical fluids. The authors work was motivated by the lack of experimental data available for different solid solubilities in supercritical fluids. Although equations of state can model such behavior to some extent, knowledge of many properties such as accentric factor and critical properties is usually required
27 and is seldom available for solid solutes. Hence having a mathematical model that can predict certain conditions where solubility is possible without using too many properties would be important and time saving. The authorsÂ’ proposed model uses the Clausius Clapeyron equation to obtain the sublimation pressure and incorporates the theory of dilute solutions into a semi empirical relation to ultimately predict solubility. 29 In a recent review published by Abbas et al 1, different uses for supercritical fluids, specifically supercritical CO2 as it pertains to the food industry was discussed. The review discusses the major advantages of using carbon dioxide in the supercritical phase. The authors continue to discuss the four different types of extraction mechanisms than can occur when using supercritical fluid extraction. The first type of extraction mechanism discussed was simple dissolution where the solute remains un dissolved in the solid matrix with limited interactions. The second type involves interactions between the solvent and solute and is called desorption or adsorption depending on the interaction type; an example of this type of interaction occurs in carbon regeneration processes as mentioned in the review. The third mechanism is typically viewed in pigment extraction processes and is termed swelling where the solvent interacts with the solid phase. The final mechanism discussed in the review is reactive extraction where extractables are obtained from an insoluble solute interaction with the solvent hence leading only to the soluble components.1 The mentioned four mechanisms are applied to processes such as extracting fats and lipids from different foods. This leads to the production of safe, fat free foods that are commonly sold. The technology is also used, as Abbas et al 1 mentions for fortification of different vitamins from natural sources such as vitamin E from different natural oils. To enhance vitamin E, the technique discussed involves estrifying natural triglycerides using alcohols such as methanol to methyl esters, those methyl esters are then extracted using supercritical CO2.
28 Supercritical fluids are commonly used to detect food contaminants and pesticides from tomatoes, potatoes, lettuce and apples as the review described. Supercritical CO2 is a favorable method of choice because it easily isolates pesticides that have a low polarity and it leaves the system completely in the gas phase. In addition to extracting some pesticides, supercritical fluids are also used to analyze different foods to determine the presence or lack thereof of pesticides. This helps to ensure high safety standards for consumer goods. The same concept can be applied to determine contamination in soil and water as mentioned in the review. 1
29 Chapter 4 Fundamentals of Mass Transfer and Phase Equilibria Relating to Supercritical Fluid Extraction Mass transfer principles as they relate to extraction of natural plants will be presented in this chapter. A discussion of both solid fluid and solid gas phase equilibria that can occur when dealing with supercritical fluids will also be included along with the different flow types and how they can affect mass transfer 4.1 Mass transfer Mass transfer is one of three main transport processes that govern most separation processes along with heat and momentum transfer. It occurs in different processes such as distillation, absorption, liquid liquid extraction and crystallization. Mass transfer is characterized by having at least one non stagnant component in the system despite of phase 17. However regardless of the phase involved in transport, basic principles are applicable. The basic governing equation that applies to transfer including mass is written as: (1) Mass transfer is greatly influenced by state parameters; in the case of gas extraction, one of the most influential factors is pressure 6. Different types of flow which can occur depending on experimental conditions; flow such as laminar is associated with a low Reynolds number and turbulent flow which occurs at higher solvent flow rates typically has a large Reynolds number also have an effect on mass transfer. These concepts will be described in greater detail later on in this chapter.
30 4.2 Solid Extraction Using Supercritical Fluids The starting material in this thesis is a solid and the extraction is done using supercritical CO2 Â–ethanol mixture. Typically, the operation involves a continuous stream of the solvent mixture going through the starting materials. The solid substrate generally forms a fixed bed in which the supercritical solvent mixture is allowed to flow and continuously extracts the soluble components 6. If the solvent is allowed to contact the starting solid for an adequate amount of time, the soluble materials are usually fully extracted from the starting solid in the same direction as the solvent flow. Thus, the concentration of soluble materials decreases from the region where the starting solid is contained and increases at the same rate in the region in which the solvent flows. 6 The selectivity of soluble components extracted using supercritical fluids is highly dependent on many factors such as operating conditions like temperature and pressure as previously described. On the other hand, other forces can affect if not the solubility of the components, the rate of extraction, such as gravitational and centrifugal forces. The lower the solvent flow, the higher the influence of gravity becomes and thus the greater the effect on the extraction process. 6 When working with natural products and plant materials, such as the case for this project with blueberry and cranberry powders, factors other than gravitational forces and operating conditions may play a key role in the extraction process. For plants, the mechanism of transport might differ in the same substance from sample to sample depending on the harvesting conditions, treatment methods used, harvesting period and so on 6. In addition the particle sizes may be different causing different mechanisms for the extraction such as adsorption on the outer surface or onto the surface of the pores or even through the material of
31 the plant; all of which affect the extraction process. The structure of a typical plant cell is shown below: Figure 3: Structure of a Plant Cell 6 The plant cell shown in Figure 3 is part of the solid material that is inside the extraction vessel. The intermediate structures within the tiny cells are what can affect the extraction process by having a big affect on the mass transfer within and through the cell. Essentially the extracted materials are dissolved in the cytoplasm of the cell but intermediate structures such as the semi permeable cell wall, the plasma membrane and the intercellular cavities play an important role in the extraction process by facilitating the diffusion step 6. In general the
32 process of getting extracts from a solid starting material occurs in the sequence described in the next portion of this chapter 6. When starting with a solid such as plant cells, the supercritical solvent (mix) is absorbed into the matrix of the plant causing the walls of the plant cell to swell facilitating mass transport by decreasing resistance. The soluble compounds within the cells begin dissolving as the solvating power of the solvent is maximized by the decreased resistance from the initial step. The newly dissolved components start to diffuse out of the solid surface of the plant cell. Once through the outer surface, a phase change might take place. Finally the extracted materials are removed from the surface of the cell into the solvent stream. Since the process of getting extracts from solid starting materials have been explained, perhaps it is also important to explain the steps the solvent undertakes with respect to time to extract the soluble materials. The basic form of the extraction occurs in a manner similar to the following graph: Figure 4: Total Amount of Extract With Respect to Extraction Time 6 Amount of Extract Amount of Extract in Plant cell (solid)
33 The graph shows the response curve for the total amount of extract with respect to the time of extraction as the amount of solvent increases 6. The initial linear portion of the graph describes a constant extraction rate while as time progresses, a limit is approached and the amount of extract ceases to increase as shown by the second portion of the curve 6. On the other hand, the initial amount of extract in the starting solid decreases with respect to time and amount of solvent that passes through it. From the solid starting materialÂ’s position, the level of soluble components in the solid decrease as the solvent is passed through the solid and as the duration of the extraction increases. With respect to the solvent, the extracted materials increase with time as more solvent is passed through the solid starting material. This allows for an axial concentration profile both in the gas and solid phases with respect to the solvent due to the kinetics of mass transfer 6. A graphic description of this concept using a series of concentration profiles with respect to time is illustrated in Figure 5.
34 Figure 5: Concentration Profiles Illustrating Path of Extraction from a Solid Material 6 4.3 Solid Fluid Equilibria Phase equilibria of mixtures are of particular importance in order to be able to define system properties and be able to work with them. There are several types of phase equilibria that include liquid liquid, liquid vapor, liquid liquid vapor, liquid solid vapor, solid liquid, solid liquid liquid and solid vapor; the next section will discuss some of the equilibria types relevant to this work.
35 Understanding the phase equilibria of systems involving solid fluid mixtures is as crucial as understanding basic concepts of mass transfer. Processes involving two or more phases such as extraction processes as in the case of this work which uses blueberry and cranberry powder, both solid starting materials, and a supercritical CO2 ethanol mixture as a solvent; are said to have solid fluid equilibrium 27. The solubility of the solids in the gas phase of the supercritical fluid can be obtained using the following correlation assuming the solid is a pure component 27: (2) Where E is the enhancement factor is the sublimation pressure of the solute Using operating temperature and the fugacity coefficient, an expression to solve for the enhancement factor is obtained as follows: (3) Where is the fugacity coefficient of the solid solute is the solid molar volume Temperature effects on solid fluid systems vary depending on different factors in the system that can have an effect on the density and solid volatility. For ideal systems, equations predict that an increase in temperature increases the solubility of the system overall 56. This is not always the case when there is a supercritical solvent involved in the system. On the other hand, pressure has a direct effect on the density of the fluid above the critical temperature 27. It is also noted that solubility increases in the supercritical region
36 drastically by several orders of magnitude as the density is increased due to pressure effects. This phenomenon is attributed to a drastic decrease in the soluteÂ’s fugacity coefficient. At the supercritical region, the distinction between the liquid and gas states begins to disappear as supercritical fluids display characteristics of both 58. Supercritical fluids possess low viscosities, usually between 1 to 9 10 4 g/cm s and low interfacial tension similar to those of gases. Therefore determining solubility of solids in supercritical fluids can be challenging due to the fact that supercritical fluids can be modeled as either expanded liquids or compressed gases 2. Modeling supercritical fluids as compressed gases is very similar to the liquid model. For the compressed gas model, at constant molar volume and a small vapor pressure, the fraction of solid dissolved is given by: (4) Where is the solidÂ’s vapor pressure is the solidÂ’s molar volume is the solidÂ’s fugacity coefficient in the supercritical fluid phase 4.4 Solid Liquid Vapor Equilibrium Ternary systems tend to be more complex to model; however in many cases it is very important to understand the phase behavior and equilibrium of ternary systems that have different phases especially when a supercritical solvent is involved. The equilibrium of a solid liquid vapor system can be modeled from binary equilibrium data for solid liquid equilibrium
37 and liquid vapor equilibrium according to a study done in 2005 by Mukhopadhyay et al 32. In order to obtain solid liquid vapor equilibrium, initially two operating variables must be fixed in order to decrease the degrees of freedom in the system. In such a case, only three mole fractions remain as unknowns out of a possible five where the other two are assumed to have a sum equal to one in each phase. This can be represented by the following set of equations: (5) (6) (7) Where superscripts 1 is supercritical solvent 2 is liquid solvent 3 is solid solute is the partial fugacity of a given component in solution Hence the liquid fugacity can be represented by: (8) Where is the standard state fugacity in liquid phase is the activity coefficient
38 The solid phase fugacity can be obtained using a relationship found by Dixon and Johnston obtained from the same work by Mukhopadhyay et al 32: (9) Where is the sublimation pressure is the molar volume of the solid The fugacity in the solid phase may also be obtained through equations of state; Kikic et al. obtained from a publication by Mukhopadhyay et al 32 gave the following equation: (10) Where is the triple point temperature is the heat of fusion at the triple point and is the triple point pressure If the solute in the system were to exist in the vapor phase, then the mole fraction would have to be obtained using solid vapor equilibrium expressions given as: (11) (12)
39 4.5 Flow Two different types of fluid flow can occur in a system, either laminar or turbulent flow and can be predicted by mathematical means such as calculating the Reynolds number, discussed later in this chapter. The type of flow is determined by system conditions such as velocity 17. Laminar flow occurs when fluid velocities are relatively slow causing a steady smooth pattern of flow. This type of flow can be described in a system being steady and having different layers simultaneously flowing without disrupting one another and is characterized by having a low Reynolds number. The Reynolds number of a system describes the transition state between laminar and turbulent flow with respect to the diameter of the tube in which the fluid is flowing as well as the viscosity, density and velocity of the fluid 17. This dimensionless number is given by: (13) Where: NRe is the Reynolds number D is the diameter of the pipe v is the average velocity of the fluid is the fluid density is the fluid viscosity For laminar flow inside a cylindrical pipe, the Reynolds number typically has values less than 2100. For values greater than 2100 but less than 4000, flow can either be viscous or laminar where the exact type of flow is not as easily predicted as simple laminar or turbulent; at
40 these values, flow is known to be in a transition region. Turbulent flow has a relatively high Reynolds number as previously mentioned above 4000 17. Turbulent flow is the second type of fluid flow that can occur. It is the opposite of laminar flow, as it occurs at higher velocities. In turbulent flow, almost chaotic fluid molecule movements are present where there is movement in all directions. Eddies are typically developed in this type of flow. Turbulent flow is characterized by having a high Reynolds number of over 4000 in a cylindrical pipe. This is obtained by the ratio of kinetic forces to viscous forces in a given fluid system 17. Many forces contribute to the determination of the type of flow in a system. Abnormalities or chaos in a velocity can be attributed to having layers of fluid contacting each other at different velocities or due to contacting a solid form such as a particle or a plant cell as in the case of this work. In turbulent flow, velocity tends to flow in random different directions causing turbulence in the system 17. This turbulence causes eddies to form as previously mentioned; interestingly though, although eddies are formed as a result of turbulence, flow within eddies is laminar due to the magnitude of their size 17. The intensity of the turbulence can be an important factor that affects heat and mass transfer coefficients, as well as the separation and boundary layer transitions. In addition simulations rely on the intensity to equal the Reynolds number in order to closely approximate models with turbulent flows. Calculating Re for CO2 at a pressure of 2100 psia, a temperature of 40C given a diameter D= 7.36*10 4 m, CO2 density = 780.4 kg/m3, average fluid velocity v= 0.47m/s and fluid viscosity = 67.74*10 6 kg.s/m.s2.
41 (14) Given a Reynolds number of 100, 2100, 3988, 30,000 the flow velocities are calculated using the previous equation and outlined in Table 3. Table 3: Velocity at Different Reynolds Values Re Velocity (m/s) 100 0.012 2100 0.250 3988 0.470 30,000 3.54 4.6 Mass Transfer Coefficients Mass transfer coefficients can be an important tool in determining mass transfer gradients in a given system. They can also be used to closely approximate extraction from solid starting materials since fluid residence times are relatively high due to the nature of the slow extraction processes. However, this method of approximation can be limited by the physical properties of system components and difficulty of the reaction; nonetheless it is a useful tool. The amount of extracted material per unit time can be approximated using the following equation: 2, 6 (15) Where is amount of component extracted is the mass of solid substrate is mean concentration of extracted components in solid starting material
42 The previous equation can be written in terms of mass transfer coefficients by relating the mass transfer coefficients in the solid and fluid phase to the transportation of extracted substances to the bulk of fluid as given in the following expressions 6: (16) (17) Where is the mass transfer coefficient in the solid phase is the mass transfer coefficient in the fluid phase is initial mean concentration of extracted components in solid starting material is concentration of extracted components in bulk of fluid is the mass transfer area in the system The total resistance, k, due to the forces of mass transfer is given by the addition of the inverse of both mass transfer coefficients in the solid and fluid phases as shown below 6: (18) For the previous equation, in the case where resistive forces due to mass transfer are greater in the solid phase, it can be assumed that For systems where a phase transition may occur, a second equation is used in addition to the previous equation that accounts for the interface equilibrium. The equation models the extraction process post initial extraction time by taking the total mass transfer coefficient as a constant where the following resulting equation is obtained for the mean concentration 6:
43 (19) More information on mass transfer coefficients is available in many literary sources such as the Gas Extraction book by G. Brunner 6. In order to obtain the mass transfer coefficient at a Reynolds number of 3988, the Prandtl, the Nusselt, the Schmidt and the Sherwood numbers must be calculated at first, detailed sample calculations are provided in Appendix B. The Prandtl number is a dimensionless number that relates kinematic viscosity to thermal diffusivity and can be calculated as shown given the viscosity, thermal conductivity and specific heat of CO2: (20) The Nusselt number is the ratio of convective to conductive heat transfer and can also be related to the Reynolds and the Prandtl numbers as shown below: (21) The Schmidt number is another dimensionless number that relates viscosity to mass diffusivity and is given for CO2 as 42: (22) The Sherwood number is a correlation for mass transfer under conditions of forced convection and can be calculated as shown for a Reynolds number of 3988: (23)
44 Rearranging the Schmidt correlation and solving for D at the same conditions yields: (24) Now plugging back into the Sherwood equation and solving for the mass transfer coefficient Kc: (25) At different values of Reynolds and at higher velocities, the mass transfer coefficient changes as shown in Table 4: Table 4: Phase Effect on Velocity and Mass Transfer Coefficient Reynolds Number Velocity SC phase (m/s) (150 bar and 40C) Velocity Vapor Phase (m/s) (1 bar and 25C) Velocity Liquid Phase (m/s) (71 bar and 25C) Mass Transfer Coefficient (m/s) 100 0.012 1.14e 4 5.28e 7 1.68e 6 2100 0.250 2.39e 3 1.11e 5 7.05e 6 4000 0.470 4.54e 3 2.11e 5 9.67e 6 30,000 3.54 3.42e 2 1.58e 4 2.62e 5 As shown in Table 4, with increasing Reynolds number, the volumetric flow rates increase as the turbulent region is approached and the mass transfer coefficient also increases. As the Reynolds number reaches the turbulent flow region, layers of fluid begin contacting each other at different velocities and contact the solid at different points. The increase in velocity causes soluble components to get picked up into the bulk of the fluid more rapidly and thus decreases the extraction time. 4.7 Gibbs Free Energy The Gibbs free energy equation utilizes the first and second laws of thermodynamics to complete the requirements for thermodynamic equilibrium. It is defined as the maximum work
45 obtained from a closed, reversible system as it changes from the initial to the final state. That work energy ( G) is equal to the work exchanged by the system and the surroundings minus any work done by pressure forces. In mathematical terms, the basic form is shown below 56: G= H TS (26) Where G is Gibbs work energy H is enthalpy of system T is temperature S is entropy The previous equation can be rewritten for a single phase system in the differential form: (27) Where dni is the discrepancy in number of moles in the system At constant pressure and temperature, equation (27) is simplified and becomes a representation of the rate of change in the Gibbs energy with respect to the reaction in the system and is given by 46: (28) Where Gibbs defines i at constant volume and entropy as the amount of change in energy of a system with the introduction of additional particles.
46 For an ideal gas at a sufficiently low pressure such as 1 bar or vacuum, the Gibbs equation becomes: (29) Where as obtained from the ideal gas law. And the superscript refers to the standard state. Rearranging and plugging into (29), the equation becomes: (30) Where (31) Although it is a useful characteristic for phase equilibria, the existence of depends on the values of the internal energy and entropy of a given system. Thus at the absolute values, i approaches negative infinity. In addition, since there is no equation for the molar volumes, of real gases, equation (31) can only be used for ideal gases. Using the concept of fugacity, f which is defined in units of pressure 46, can be a better alternative to the limitations exhibited by i and may be used to approximate the chemical potential of real gases. Fugacity is defined in terms of as follow: (32) For ideal gases, f =P and as P approaches zero, the limit of the fugacity function becomes:
47 (33) Whereas the dimensionless ratio (34) is defined as the fugacity coefficient, and equation (34) becomes: (35) The fugacity coefficient is applicable to any species regardless of phase (vapor, liquid or gas). For ideal gases, is equal to 1. Whereas for pure components, the fugacity coefficient is defined as46: (36) Where Z is the compressibility factor The fugacity coefficient is defined for the vapor liquid equilibrium of a pure component, i as follows: (37) Where the fugacity coefficient for component i in the vapor phase is equal to that in the liquid and in the saturated phases 46. (38) It is usually easier for explanatory purposes to assume ideal behavior of components in a given system; however that is not the case in most instances; in fact it is expected to have non
48 idealities especially in mixtures. For this reason, excess properties exist for Gibbs energy, enthalpy, volume and entropy to help reveal system non idealities. Excess function values approach zero as purity of components inside a system increases. The excess function for Gibbs is defined in the basic form as 46: (39) Where GE is the excess Gibbs function Gac is the actual Gibbs for the solution Gid is the Gibbs for the ideal solution Using the activity coefficients and rearranging in terms of excess volume and enthalpy, the excess Gibbs property can be rewritten as: (40) From equation (38), excess volume and excess enthalpy can be defined in terms of GE: (41) (42) Excess entropy is defined as: (43)
49 Non idealities in systems can be better approximated using excess functions as mentioned previously; however causes for system deviations from ideality may also be a result of temperature changes. The initial temperature at which a system begins to deviate or become non ideal is known as the consolute temperature denoted as TC and given by the following equation 38: (44) Where A is a temperature parameter The consolute temperature can be an upper or a lower temperature. More systems exhibit an upper consolute temperature than those who exhibit lower consolute temperature. The upper consolute temperature is defined as the highest temperature in which two phases can exist which can be achieved if decreases with increasing temperature. The opposite is also true, where if increases with increasing temperature, a lower consolute temperature is obtained; this is common in mixtures that form hydrogen bonding 38. 4.8 Equations of State Equations of state relate volume, pressure and temperature of a substance where two of the properties are independent 56. So many equations of state exist, but no single equation of state can approximate more important properties such as entropy, enthalpy, density of vapor or liquid phases, vapor pressure or critical properties of mixtures. Cubic equations of state are used to approximate phase equilibria of different systems. Many equations exist, however different equations also have different mathematical models for obtaining activity coefficients. Activity
50 coefficients are a useful tool for non ideal systems that have more than one component and can be used to approximate phase behavior. The basic form of cubic equations of states is 58: (45) Although many equations of state rely on the basic structure of equation (45), each equation has important variations and sub equations for obtaining the constants that make it unique. However it is also important to mention that different equations of state have different restrictions; no one equation can be deemed superior for all systems. Every proposed and accepted equation has certain limitations, some equations are valid in a particular temperature or pressure range while others are only valid for certain classes of chemicals; however overall they are decent approximates of phase equilibria 56. 4.9 Van Der Waals One of the earliest proposed equations of state is the van der Waals equation; it is given in the basic form as 56: (46) Where a is termed the attraction parameter and b is the repulsion parameter and are defined by the following equations 56: (47) (48)
51 The van der Waals parameters are given for mixtures in terms of those of a pure component using mixing rules proposed by Lorentz and Berthelot, as follows 56: (49) (50) Where the compressibility factor, z, is given by: (51) Although it is considered one of the pioneer equations of state, the van der Waals equation has severe limitations, mainly in the fact that in most systems it is very inaccurate and the equation is now considered a simple model that offers a few corrections to the ideal gas law 56. The limitations for the van der Waals equation are most obvious in the prediction of the critical z value, denoted Zc, as a value of 0.375; whereas it has been proven that most real fluids have a Zc value in the range of 0.27 30. Far more superior equations have been introduced since then. 4.10 Peng Robinson The Peng Robinson (PR) equation of state was developed in 1976 to partially cure some of the problems with earlier equations. The equation focuses on several important factors that include having parameters modeled in terms of critical temperature and pressure as well as the accentric factor. The equation aims at better approximating liquid densities and compressibility factors, Z c. Finally, the original mixing rules employed with PR contain only one binary interaction parameter that is independent of temperature and pressure 56. The basic form of the equation is given by: (52)
52 Where a and b are given at the critical temperatures and pressures by: (53) (54) However, at temperatures other than the critical temperature, a(T) is corrected by a vapor pressure correlation and denoted as given by the following two equations: (55) (56) Where Z c is given a value of 0.307 which is much closer to the true value of many substances; that is part of the reason why the PR equation of state is a better approximate of liquid densities 56. For mixtures, the PR parameters are obtained using the following set of equations: (57) (58) (59) 4.11 NRTL Nonrandom two liquid equation (NRTL) is a liquid activity model that utilizes the excess Gibbs (GE) energy to obtain the corresponding parameters. The model assumes the system to contain a binary mixture of cells of types 1 and 2 that are surrounded by a variety of the same molecules. The Gibbs reaction for the two cell types are given by: (60)
53 (61) Where and are the pure substancesÂ’ Gibbs energies 56 NRTL utilizes the following equations to obtain the mole fractions of both species in a given system: (62) (63) Where is a constant in the previous equations (62, 63) under the assumption that the total mole fraction of each species sums up to one as given by the following equations 56: (64) (65) Given the mole fractions of both species in the system the excess Gibbs energy can be obtained by 56: (66) Where the independent parameters and are given by the following equations56: (67)
54 (68) The individual component Gibbs energies, G12 and G21 are given by the following equations56: (69) (70) Defining all the variables to the previous equations, the activity coefficients using the NRTL equation can be obtained by 56: (71) (72) The NRTL equation is used quite frequently because of its capacity to very closely approximate mixture behavior using binary parameters better than other equations of state that use similar techniques. However, a discouraging feature of the NRTL equation is that it requires three parameters versus other activity coefficient models.56 4.12 Mixing Rules In order to be able to closely approximate properties of a given system with two or more components, equations of state must be coupled with the proper mixing rules. Mixing rules are essentially a relationship that describes the dependence of the constants in a given system on the composition. 38 One of the earliest mixing rules to be implemented was the van der Waals rules for constants a and b shown below:
55 (73) Where is the attractive forces between molecule i and molecule j m is the number of components in the mixture (74) The equation for constant a, equation (73), makes several assumptions that allow for its use. It assumes that the molecules in the mixture are fairly close in the size range up to moderate density values. The equation is also modeled to take the intermolecular attractive forces into account as shown by the variable Finally, the equation assumes that individual fugacities in the mixture are sensitive to the value of a 38. For simplicity purposes equation (74) makes only one assumption which is that the molecular volumes are taken as an average as opposed to finding b in terms of size proportionality of the molecules in the mixture. 38 It is useful to mention that for cases where i j, a second equation is used that was proposed by Berthelot called the geometric mean assumption. It is an empirical correlation that is commonly used for mixtures and for measuring intermolecular forces. The geometric mean assumption is given as 38: (75) The van der Waals rules are an important tool; however their dependence on density and given all the underlying assumptions cause them to be invalid for a very large range. Another useful set of mixing rules are the Wong Sandler rules which are independent of density. They have been shown to produce good results both in the high as well as the low
56 density regions for a variety of mixtures 38. Wong Sandler mixing rules are unique in that they enable close estimations of mixture properties at high pressures using low pressure vapor liquid information. The constants b and a are given by Wong Sandler as: (76) (77) Where is excess molar Helmholtz energy at infinite pressure is constant a in the mixture is constant b in the mixture C is equation of state dependent constant For Peng Robinson, C is given a value of 0.62322 and for van der Waals, it is given a value of 1 38.
57 Chapter 5 Experimental Setups, Equipment Specifications and Experimental Procedures In this chapter, both experimental setups used to conduct the experiments are discussed. The specifications for all used equipment are also highlighted. Finally, the detailed experimental procedure will be discussed along with shutdown procedures and equipment cleaning. 5.1 High Pressure Experimental Setup Figure 6: High Pressure Experimental Setup Experimental Setup Using Supercritical CO2 and Ethanol for the Extraction process is shown in Figure 6. The setup shows the two pumps used to introduce the solvent and the co
58 solvent to the system. The first pump introduces the CO2 after the temperature is decreased. The second pump introduces the ethanol and both mix in an in line mixer as shown in Figure 6 before entering the first vessel. The figure also shows how both the fractionation and extraction vessels are connected to air activated back pressure regulators (BPRs). The extraction and fractionation section of the setup is in a constant temperature air bath. The equipment specifications used in the setup are discussed later in this chapter. 5.2 Soxhlet Extraction and Experimental Setup Soxhlet extraction is used as an analytical reference technique. The technique is done in a setup composed almost entirely of glassware. The solvent is added to a round bottom flask and is placed on a burner set to the boiling point of the solvent to allow for evaporation. The top of the solvent flask is connected to a glass extractor where the evaporated solvent can easily flow. Inside the extractor, the starting sample is usually contained within another, usually disposable, semi permeable vessel called a thimble. The top of the extractor is connected to another piece of glassware where cooling water is allowed to flow constantly in order to cool the newly evaporated solvent and allow it to condense back. As the solvent condenses, it falls on the starting material in the thimble within the extractor and extracts soluble components. Once the condensate reaches a certain level, it is refluxed out of the extractor back into the solvent reservoir in the round bottom flask and the process is allowed to repeat for hours (usually between 6 to 48 hours) until all soluble components are extracted in the bulk of the solvent 36.
59 Figure 7: Soxhlet Extraction Setup The soxhlet extraction setup used is shown in Figure 7. The setup operates based on total reflux and is comprised from the bottom up of a hotplate and different pieces of glassware that help with the extraction process. The solvent which is ethanol for this case is placed in the round bottom flask and the berry powder is carefully placed in the thimble which is then placed in the extractor. Finally the cooling water enters the top portion of the setup as indicated in Figure 7 in order to allow for the ethanol to condense and help with the reflux process. The detailed experimental conditions and procedures are described later in this chapter. Thimble
60 5.3 Equipment Specifications 5.3.1 Extraction and Collection Vessels The extraction cell used is a Thar Designs model 26526 44. It has a 100ml volume and an operating pressure of up to 10,000 psi. The cell is constricted at the top and the bottom by two filters with a 5 micron pore diameter to ensure that no starting solids are transferred to the collection cell. The collection vessel used is a Thar Designs model CL1573 with a 200ml capacity that operates up to pressures reaching 1,500 psi. 5.3.2 Temperature Controllers The heater used to bring the system to temperature is an EcoLine chiller; it is made by Lauda and is designed to operate between 30C and 90C. 25 A PolyScience chiller is used to cool the CO2 pump head. It is designed to operate at temperatures between 60C and 30C when ethylene glycol is used as the cooling fluid. 37 5.3.3 Wet Test Meter A Precision wet test meter model 63135 was used to measure the amount of CO2 leaving the system. The instrument operates at a pressure range between 0.3 and 0.6 in H2O with an accuracy of 0.5%.39 5.3.4 Gas Chromatograph & Mass Spectrometer A Varian CP 3800 gas chromatograph was used to analyze the samples. The GC was coupled with a mass spectrometer from Saturn, model 2000.
61 5.4 Experimental Procedures 5.4.1 Before an Experiment Before initiating a run, both the extraction and the collection vessels are thoroughly cleaned and dried. The top and bottom screw pieces of the extraction vessel are checked to ensure that the filters are secured in place. After inspection, the bottom piece is screwed on tightly. The desired amount of powder, usually about 5 grams, is obtained from the chemical fridge and weighed carefully in a beaker. The contents of the beaker are then transferred carefully to ensure minimal loss of sample to the extraction vessel. Then, the screw top of the extraction vessel is secured tightly. The connections of the extraction vessel are then tightened connecting it to the back pressure regulator and to the coil where the solvent mix enters from the bottom. The collection vessel is then connected to the back pressure regulators and all the corresponding connections are tightened. Finally, more DI water is added to the beaker for the depressurizing step. The cover of the box is then put and fastened with tape to ensure no heat losses during an experimental run. 5.4.2 Preparing the Equipment The equipment is prepared before a run by setting the first timer of the cooling bath on and ensuring it is at the desired temperature to cool the pump head for the CO2. Then, the second timer is set to the desired times and connected to the heating bath; the heating bath is double checked to ensure proper temperature is attained. Then, the fan is plugged in to ensure proper air distribution and ensure that the entire insulated box is at the desired temperature. The temperature is recorded every ten minutes for thirty minutes to ensure that there are no major temperature fluctuations. Finally the flow meter is checked to ensure the reservoir has an
62 adequate amount of DI water; if the water level is too low in the reservoir or in the meter tube, then more water is added before the experimental run. 5.4.3 Beginning an Experiment The CO2 flow meter is turned on and the necessary gas information is inputted. The HPLC pump is turned on and left for a few seconds to do the embedded self checks; and a quick check is done to verify thereÂ’s enough ethanol in the reservoir. Meanwhile the CO2 pump is turned on and also left to do the embedded self checks. The box temperature is verified one final time before initiating the experiment. Then the depressurizing connections are retightened on the N2 tanks for safety before opening the tanks. Both N2 tanks 1 and 2 are opened and the desired pressures are set using the twist knobs on the tanks. The system is left for a few minutes to ensure the desired pressures are attained at the extraction and collection vessels. The pressures at the two back pressure regulators is checked to ensure it matches that of the N2 tank pressures and recorded. To start the experimental run, the valve is opened so that all the flow goes to the system. The flow in the HPLC pump is set to 15ml/ min for about ten seconds to build pressure and to allow the ethanol to fill the lines; then the flow rate is decreased to the desired flow that accounts for about ten molar percent of the CO2 used. The HPLC pumpÂ’s starting pressure is recorded. Next the bi directional valve is set to the desired system on the high pressure pump and the CO2 tank is opened. The pump valve is opened and the flow is set using the associated controller by selecting F2 and then option E and finally inputting a high flow rate (usually about 15 g/min) in order to rapidly build pressure in the system. Once the desired pressure is attained, the CO2 flow rate is decreased to the desired flow rate by inputting it into the controller following the previously noted procedure. The final pressure of the CO2 pump is recorded as the starting pressure of the experiment.
63 At this point, a second pressure reading is observed and recorded at the HPLC pump to verify that the pump pressure is now similar to the CO2 pumpÂ’s pressure to ensure proper flow of the co solvent. Once both pump pressures are at the desired value, the gas flow meter is initiated to record the flow; both the starting time and starting gas volume are recorded. A typical run lasts approximately three to four hours; the temperature, CO2 pump pressure, HPLC pump pressure and gas volume are all recorded every half hour during an experimental run to verify that no leaks have developed and that pressure is constant. 5.4.4 Shut Down Procedure After a run is complete the two N2 tanks are tightly closed and the shut down time is recorded. The flow rate is stopped in the CO2 pump and the CO2 tank is closed tightly. The gas flow meter is also stopped and the final gas volume and temperature is recorded. The HPLC pump is stopped by decreasing the flow rate to zero. The heating bath is turned off by switching it off or by turning off the associated timer and the fan is unplugged. The controlled environmentÂ’s cover is opened to allow the vessels to cool down so the final product can be collected. Slowly, both the depressurizing connections on the N2 tanks are loosened to allow for the slow release of pressure (takes up to 1.5 hours). Heating tape is wrapped around the back pressure regulators and turned on to ensure that the system does not develop any plugs. Once the pressure reaches zero, the heating tape is unplugged and left to cool off. Both the CO2 pump pressure and the HPLC pump pressure are observed to ensure that the pump heads have been fully depressurized. Once the pumpsÂ’ pressures are noted to be zero, both pumps are turned off. The connections to the extraction and collection vessels are slowly loosened to ensure any trapped pressure is slowly released. The extracted material which is a liquid at this stage due to the ethanol presence is taken out of the collection vessel using a
64 pipette or clean syringe and put into a pre weighed vial and wrapped with foil due to the photosensitive nature of some of the extracted compounds to ensure minimal degradation to these compounds during the collection process. The vial is then capped, weighed, labeled and immediately placed in the chemicalÂ’s fridge so as to ensure minimal degradation of any sensitive compounds. The starting material is taken out of the extraction vessel and placed in a pre weighed vial and then reweighed and the weight is recorded. The beaker is then placed in the oven for two days to ensure any remaining ethanol is evaporated from the left over material and then the contents of the beaker are weighed a third time. 5.4.5 Cleaning Procedure A medium sized beaker is filled with ethanol or isopropanol where the extraction vesselÂ’s filters are dropped in the beaker and stirred slightly to loosen any particles on the surface. Once the filters are cleaned, they are taken out of the beaker and are left to air dry. The extraction and collection vessels are immersed in water and washed thoroughly to ensure complete cleanliness. As an insurance step of cleanliness, a few ml of ethanol are placed in the vessels and swirled for several minutes. The vessels are then drained and left to air dry. Finally the filters are placed back into the extraction vessel and prepared for a new run. The lines are cleaned by attaching the extraction and collection vessels to the system and running pure CO2 and ethanol at a high pressure for a minimum of 45 minutes. 5.4.6 Soxhlet Extraction Procedure The glassware is checked to ensure that it is clean and dry before initiating an experiment. The desired amount of powder is weighed, about 10 grams and is placed into a clean thimble to prevent any powder from refluxing with the extract during an experiment. The thimble is then placed in the soxhlet extractor. In a clean round bottom flask, 300 ml of ethanol
65 are added and the extractor is placed on the round bottom flask. The flask is then placed in a hot water bath over a hot plate. A continuous cold water bath is attached to the top of the soxhlet extractor to help with the condensation process. The extraction process is done for twenty four hours at the boiling point of ethanol. 5.4.7 Soxhlet Extraction Cleaning Procedure At the end of the experimental run, the glassware is carefully disassembled. The thimble is taken out of the extractor and the leftover material is carefully scrubbed out. The extractor and the round bottom flask are immersed in warm water and rinsed out several times to ensure that no material is left behind. The glassware is then left to air dry completely before another experiment can be initiated.
66 Chapter 6 Results and Discussion This chapter will discuss the results obtained using the setups and procedures previously described in this work. Each sample was analyzed using a gas chromatograph coupled with a mass spectrometer. Results obtained from each experiment along with the experimental conditions will be reported and the corresponding GC obtained will be included. A discussion of all the findings will be discussed in greater detail at the end of the chapter. For the supercritical experiments, in order to ensure that the entering CO2 ethanol mixture was at the supercritical phase, the Peng Robinson equation of state was used with the help of van der Waals mixing rules using the operating conditions for each experimental run for verification. Blueberry (BB) experiments were done using 8 and 12 ml/min of CO2 with a steady 10 molar percent of ethanol. Operating conditions varied from 122 bars to 197 bars at temperatures ranging from 41.7 to 46.8 C. Experiments were done in a 3 hour period. Cranberry (CB) experiments were done using a CO2 flow rate of 12ml/min with a 10 molar percent of ethanol as a co solvent. Operating conditions for the CB experiments were done at temperatures ranging from 46.7 to 50.4 C and pressures of 122 to 194 bars. In addition soxhlet extractions were done at the boiling point of ethanol for 24 hours on both the blueberry and cranberry powders to determine the differences in the extract.
67 6.1 Results Blueberry extracts obtained using the supercritical solvent mixture resulted in many important active components as outlined in Table 5: Table 5: Blueberry Experimental Conditions and Corresponding Extract Blueberry Experimental Conditions Pressure (Bars) Temperature (C) CO2 flow rate (ml/min) Extract Extract GC peak time (min) 125 41.7 12 Vitamin A Vitamin B8 carotene 13.5 78.5 10.4 124 43.3 8 Vitamin A carotene 20 46 126 45.1 12 Decanoic Acid Pentanoic Acid Vitamin A 10.5 10.7 13.4 127 45.4 12 Retinol carotene 13.3 20 125 46.9 12 Biotin 64 197 46.8 12 Vitamin A Undecanoic Acid Ricinoleic Acid 10.3 30.6 74 Through supercritical extraction, the most prevelant active component extracted from the blueberries was vitamin A; it was extracted at four different temperatures and pressures. Vitamin A had strong peaks on the chromatographs that indicated that it was present in significant quantities at experimental conditions of 125 bars with a temperature of 41.7 C, 124 bars with a temperature of 43.3 C, at 126 bars with a temperature of 45.1 C and finally at 197 bars and 46.8C. The corresponding chromatographs are included later on in this chapter. Experiments were also done on cranberry powder yielded in the extraction of many active ingredients using the supercritical fluid. Among the active ingredients extracted were important acids such as benzoic, and oleic acid. Benzoic acid which is present in cranberries in large quantities according to published works 61, was extracted at three separate experimental
68 conditions at pressures of 125 bars and 48.3 C, at 123 bars and 49.9 C and finally at 125 bars coupled with a temperatures of 46.7 C. A breakdown of the extracts obtained as a result of temperature and pressure along with resulting peak times are included in Table 6. Table 6: Cranberry Experimental Conditions and Corresponding Extract Cranberry Experimental Conditions Pressure (Bars) Temperature (C) CO2 flow rate (ml/min) Extract Extract GC peak time (min) 125 46.7 12 Benzoic acid Vitamin A carotene 3.6 18 18.5 122 48.8 12 Oleic Acid Octadecanoic acid Vitamin A Retinol 8.2 12.5 17.4 18.6 125 48.3 12 Benzoic Acid Undecanoic acid Ricionleic acid Vitamin A 3.7 10.6 18.1 19 123 49.9 12 Benzoic acid carotene 16.5 20 194 50.4 12 carotene 44 Soxhlet extractions were done for a period of twenty four hours at the boiling point of ethanol on both blueberry and cranberry powders resulted in some comparable extracts. Similarly to the supercritical extractions done, vitamin A, carotene, and Biotin were also extracted from the initial blueberry powder via soxhlet extraction. In addition, there was a small presence of Palmitic acid which only appeared in the soxhlet extraction done. The soxhlet extraction done on cranberry powder yielded only ricinoleic acid and undecanoic acid in quantities significant enough to be detected by the GC/MS, no other active components were detected as outlined in Table 7.
69 Table 7: Blueberry and Cranberry Soxhlet Extraction Experimental Conditions and Results Blueberry Soxhlet Experimental Conditions Pressure (Bars) Temperature (C) Solvent Time (Hr) Extract Extract GC peak time (min) 1 78.9 Ethanol 24 Vitamin A carotene Palmitic Acid Biotin 3.8 18 28 32 71 Cranberry Soxhlet Experimental Conditions Pressure (Bars) Temperature (C) Solvent Time (Hr) Extract Extract GC peak time (min) 1 78.9 Ethanol 24 Ricinoleic acid Undecanoic acid 20 21
70 Figure 8: GC of BB Sample at 125 Bars and 41.7C The GC of a sample done using a higher flow rate of CO2 of about 12 ml/min done at a pressure of 125 bars and a temperature of 41.7 C is shown in Figure 8. The chromatograph contains lots of noise that may be attributed to several different factors. It may be due to impurities left in the column from different analyses that were not completely vaporized and thus are showing up as noise peaks on the chromatograph. The column may have also contained residual water from other samples. There were several important findings still in this chromatograph. Vitamin A was strongly present at the 13.5 minute mark. At the 78.5 minute mark, the chromatograph showed a significant presence of Biotin which is also sometimes referred to as vitamin B8 or vitamin H. carotene was also moderately present around the 10.4 minute mark. Other minor peaks are contributed to pesticides and insecticides that were in the original starting material.
71 Figure 9: GC of BB Sample at 124 Bars and 43.3C Two important components were extracted as shown in Figure 9 which is a gas chromatograph of the results obtained from an experiment done using a CO2 flow rate of 8 ml/min at operating conditions of 124 bars and 43.3C. The most significant findings in this chromatograph were reflected in two distinct peaks. At approximately 20 minutes, there is a strong peak that shows the presence of vitamin A. There also was a noticeable presence of carotene around the 46 minute mark. The significance and uses of vitamin A and carotene are discussed in greater detail later on in this chapter.
72 Figure 10: GC of BB Sample at 126 Bars and 45.1C At operating conditions of 126 bars and 45.1C, Figure 10 shows a GC of the corresponding findings. The chromatograph contains some noise that can be attributed to poor injecting into the column or residual impurities left over from previous samples. In addition, pesticides and insecticides were present in the extracted material that contributed to some of the peaks on the chromatograph. Only a few active compounds were present in significant enough concentrations to be detected. Early on at the 5 minute mark, retinol was detected. The uses and significance of retinol is discussed in detail later on in this chapter. Decanoic acid was present in the sample and showed up on the chromatograph along with pentanoic acid around the 10.5 peak. Both acids are flavor compounds and are commonly used as food additives 8. Finally, vitamin A was strongly present as seen by a strong peak at the 13.4 minute mark which closely resembles previous findings.
73 Figure 11: GC of BB Sample at 127 Bars and 45.4C GC of the extract obtained from blueberry powder at a pressure of 127 bars and a temperature of 45.4C is shown in Figure 11. Although the figure seems to have many sharp peaks, those peaks are consistent with ethanol. The only identified compounds were retinol around 13.3 minutes which is shown by a small peak and carotene around 20 minutes.
74 Figure 12: GC of BB Sample at 125 Bars and 46.9C The experimental conditions for the GC shown in Figure 12 were 125 bars and a temperature of 46.9C with a CO2 flow rate of 12 ml/min. There is minimal amount of noise in GC shown although some still exists. Only one significant finding was visible in this GC, around the 64th minute Biotin was detected. Other peaks were the result of trace amounts of pesticides and insecticides in the starting material.
75 Figure 13: GC of BB Sample at 197 Bars and 46.8C The experimental conditions for the GC shown in Figure 13 included a pressure of 197 bars and a temperature of 46.8C with a CO2 flow rate of 12 ml/min. Vitamin A was detected at 10.3 minute peak, undecanoic acid was detected around the 30.6 minute peak and finally ricinoleic acid was detected around 74 minutes as indicated by a small yet defined peak. Some pesticides were also present in the extract.
76 Figure 14: GC of CB Sample at 125 Bars and 46.7C The GC in Figure 14 shows the results obtained for cranberry extract under operating conditions of 125 bars and 46.7C with a flow rate of 12 ml/min for CO2. It can be seen from the figure that some noise is present and the detection of ethanol is also very evident; however three important compounds were identified. Benzoic acid showed a very strong presence as can be seen from the peak around 3.6 minutes. Vitamin A was identified around the 18th minute mark. And carotene was also present at around 18.5 minutes. Other minor peaks were the result of the presence of germination agents and pesticides.
77 Figure 15: GC of CB Sample at 122 Bars and 46.8C At a flow rate of 12 ml/min for CO2 with a pressure of 122 bars and a temperature of 46.8C, Figure 15 shows the GC where several important compounds were identified. Although the previous chromatograph shows many peaks, only a handful of those peaks proved useful. Oleic acid which is an omega 9 acid was strongly present at 8.2 minutes into the run. Octadecanoic acid which is another omega 9 acid was identified to have a peak around 12.5 minutes. Vitamin A was present at 17.4 minutes and retinol had a strong peak at 18.6 minutes.
78 Figure 16: GC of CB Sample at 125 Bars and 48.3C Several important compounds were extracted and identified using a CO2 flow rate of 12 ml/min and a pressure of 125 bars with a corresponding temperature of 48.3C as shown in Figure 16. Benzoic acid was strongly present as shown by the peak around 3.7 minutes. Undecanoic acid was also identified by the peak visible around 10.6 minutes. In addition, ricinoleic acid which is an omega 9 fatty acid was present around the 18.1 minute peak. Finally vitamin A was noticeably present around the 19 minute mark. The importance and uses for the identified components will be included later in the discussion portion of this chapter.
79 Figure 17: GC of CB Sample at 123 Bars and 49.9C Results obtained from an experiment done at a pressure of 123 bars and a corresponding temperature of 49.9 C with a CO2 flow rate of 12 ml/min are shown as Figure 17. Ethanol is strongly detected by well defined peaks along with some germination agents and pesticides. Benzoic acid was identified around the 16.5 minute peak. carotene was present around the 20 minute mark. The uses and importance of the active compounds will be included later on in this chapter under the discussion section.
80 Figure 18: GC of CB Sample at 194 Bars and 50.4C Extract was obtained from cranberries under a pressure of 194 bars and a temperature of 50.4C with a CO2 flow rate of 12 ml/min as shown in Figure 18. The only active ingredient that was present in a large enough quantity to be detected at 44 minutes was carotene. Other peaks were attributed to the presence of ethanol and pesticides from the starting berry powder.
81 Figure 19: GC of CB Sample by Soxhlet Extraction with an Ethanol Baseline The chromatograph of components extracted from cranberry powder using soxhlet extraction is shown in Figure 19. The extraction was done using ethanol and lasted for 24 hours. In the chromatograph, two distinct plots are shown. The first one is of the ethanol baseline as indicated on the graph and the second is of the sample. It can be seen that both lines overlap a great deal which suggests that only a few compounds were extracted under this method. Only ricinoleic acid and undecanoic acid were present in large enough quantities to be detected. Both active components showed up around the 20 to 21 minute mark. Other peaks were of pesticides that are soluble in organic solvents and were thus extracted with the ethanol. Pesticides extracted are outlined in Table 8. Ethanol
82 Figure 20: GC of BB sample by Soxhlet Extraction with an Ethanol Baseline Soxhlet extraction was done for 24 hours on blueberries using ethanol as the solvent. The GC shown in Figure 20 includes the ethanol baseline as indicated by the arrow, as well as the plot from the sample. Both plots largely overlap. Active ingredients detected included vitamin A, carotene, palmitic acid and biotin. Vitamin A was identified at the peak shown around 3.8 minutes. In addition carotene was present around the 18 minute mark. Palmitic acid was present in the peak between 28 and 32 minutes. Finally, biotin was present in a minor peak around 71 minutes. Ethanol
83 Figure 21: GC of Ethanol The GC of ethanol which was used for all the samples as the standard is shown as Figure 21.
84 6.2 Discussion As shown from the included chromatographs, many desirable active components were extracted under the different temperatures and pressure used for the experiments. In addition, residuals of pesticides, insecticides and germination agents were also extracted and are shown in Table 8. Some active components such as vitamin A and carotene were extracted under more than one of the operating conditions used which suggests that they are easier to extract than other components present in the starting powders at chosen operating conditions. The extracted components included several important acids such as oleic acid, ricinoleic acid, benzoic acid, stearic acid, palmitic acid and undecanoic acid. The advantages of the vitamins and acids extracted and their uses will be discussed in greater detail in the following section. Vitamin A and its precursors are some of the most useful and powerful vitamins that are essential for many processes in the human body. In both the blueberry and cranberry experiments, vitamin A and some of its precursors were successfully extracted as previously noted. Research is constantly uncovering new various advantages to vitamin A in the human body. Vitamin A is essential from the fetal developmental stage up until adulthood. In the developmental stage, vitamin A aids epithelial cells to differentiate and continues this process through adulthood 5. Epithelial cells and tissue are responsible for a variety of life functions including protecting sub surfaces of the body from abrasions and various injuries; secreting hormones and enzymes from glands, aiding in the absorption process of nutrients and various components from different organs such as the kidney and the lumen and even aid in sensations such as taste, vision and hearing 16. So in reality, vitamin A is partially the underlying cause for all these important bodily functions mentioned previously because a deficiency in vitamin A
85 translates to poor epithelial proliferation and thus negatively affects all the aforementioned functions. Carotenoids such as carotene, shown in Figure 22 are stored in the body for various functions. Part of the carotene is left in its current state and is used by the body for its antioxidant properties. A small portion is converted to retinoic acid. A second part of the absorbed carotene is converted to retinol as mentioned before in order to give rise to vitamin A 5. Figure 22: Carotene Molecule Research is showing a strong correlation between vitamin A, its precursors and chances of reducing the development of certain cancers such as lung, colon, prostate and breast cancers 5. This evidence stems from the fact that retinoids are responsible for regulating cell proliferation in the body as previously discussed and cancer is a disease of abnormal cell Figure 23: Retinol Molecule
86 proliferation. Hence, the theory that a deficiency in retinoids such as retinol, shown in Figure 23, may increase the chances of abnormal cell differentiation and thus development of carcinogenesis came to exist. Further studies are being conducted to back up this theory which has great potential if proven correctly. It is recommended that diets contain at least 600 to 1500 g of retinoids on a daily basis; however this recommendation is only based on the idea that retinoids aid in the development of vitamin A, if the previously mentioned idea is proved, the recommended daily intake of retinoids will most likely be increased significantly. 5 In addition to their role in cell proliferation, retinoids such as retinol have been linked to other uses in the body such as maintaining vision, aiding the immune system and proper functionality of the reproductive organs. Retinoids have been shown to have an important role in the proliferation of progenitor cells that affect the immune system. 5 In the female reproductive system, retinol helps to eliminate placental necrosis where the tissue simply dies and is fatal to the developing fetus as all nutrients are cut off. Retinol also eliminates the chances of developing a fetal resorption condition where the embryo dies and pregnancy components are resorbed 5. In males, retinol is essential in the maintenance of spermatogenesis which ultimately gives rise to spermatozoa 16. Vitamin A deficiency causes severe complications such as blindness, xerophthalmia and even mortality as the body becomes more prone to catching diseases such as measles 5. Premature births and newborns with very low birth weights (VLBW) have also been linked to a deficiency of vitamin A as the correct amount of vitamin A buildup is not reached for premature births and those who are deficient have poorly proliferated cells and thus are more likely to have VLBW. VLBW children are more likely to have ill developed organs and have a higher risk of developing disease later on in life. 5
87 It is estimated that over 100 million children are affected by vitamin A deficiency and are potentially at risk of death as a result 5. Using supercritical fluids to extract essential precursors of the vitamin is an effective and inexpensive way that can be used to turn the active compounds into supplements at an affordable cost in hopes of eliminating this deficiency which has the potential to save lives due to all the previously mentioned advantages and essentiality of the vitamin and its precursors for the body. Benzoic acid was also identified in the cranberry experiments conducted in the later part of this work. According to a study by Yuegang et al 61, cranberries contain an ample amount of benzoic antioxidants that include o hydroxybenzoic acid, 2,3 dihydroxybenzoic acid and benzoic acid; shown below in Figure 24. Figure 24: Benzoic Acid Molecule It is estimated that benzoic and phenolic antioxidants are present in quantities as much as 5.7g/Kg of cranberries; a value that surpasses many other fruits and vegetable. Although, still in its infancy, some studies suggest that benzoic antioxidants may have anti carcinogenic and anti microbial effects in vitro. In addition, benzoic acid is a commonly used food preservative.61 Among the other important acids extracted and identified is ricinoleic acid which is an omega 9 fatty acid that is present mainly in castor and in many berry plants. Similar to many other berry components, the health benefits associated with ricinoleic acid are not well
88 documented. In a study conducted by Vieira et al 53; it was shown that the acid can have very important medicinal properties. It was identified that ricinoleic acid, shown below, has great anti inflammatory properties when applied locally at the site of inflammation. Figure 25: Ricinoleic Acid Molecule In addition, it was shown that the acid did not cause any adverse hyperalgesic effects even with heat or chemical subjection. This suggests that it may prove to be superior to other, common anti inflammatory agents currently used. Due to the perceived lack of adverse side effects associated with ricinoleic acid, it may also be used as an analgesic. Studies also suggest that the acid may possess laxative properties if it enters the gastrointestinal tract.53 Stearic Acid which was present in several cranberry samples in this work is a saturated fatty acid that is also known as octadecanoic acid. Stearic acid has a very unique quality in that unlike other fatty acids, stearic acid acts to lower LDL cholesterol levels in the body.9 Figure 26: Stearic Acid Molecule The human body has two types of cholesterol, LDL and HDL. LDL cholesterol is what is typically being referred to when someone is diagnosed with high cholesterol levels. Abnormally high LDL levels can cause artery blockage which can be a serious health risk as it can lead to
89 clotting and strokes. Therefore the role that stearic acid may play in lowering LDL levels can be very important.9 Oleic Acid, shown below, was extracted under the experimental pressures and temperatures used in this work as previously noted. Oleic acid is a mono saturated fat that possesses useful qualities. It can be used as a healthier substitute for saturated fat as it can reduce the bodyÂ’s risk of developing sudden cardiac death (SCD). Studies have also shown that oleic acid can prevent lipoproteins in the body from oxidizing and consumption does not increase the risk of primary cardiac arrest like other fats.35 Figure 27: Oleic Acid Molecule Compounds were extracted from the initial solid powders using a supercritical CO2 ethanol mixture. Some components such as benzoic acid, biotin, carotene, ricinoleic acid and vitamin A were also extracted with the soxhlet extraction. Meanwhile, some acids were only extracted via the supercritical mixture such as stearic and oleic acids. While both methods were successful in extracting some components, using supercritical CO2 proved to be a superior method of extraction. Moderate changes in temperature and pressure changed some of the components extracted as shown from the GC results which can be a very helpful tool in selecting only the desired components from the starting material. However, changes in temperature proved to have a greater effect on the materials extracted as was evident from the experimental trends. Moderate changes in temperature significantly changed the outcome of the extracts
90 while maintaining the temperature and changing the pressure proved to have a minimal positive effect on increasing the selectivity of the extracted components. There are many disadvantages to using the soxhlet extraction technique, first selectivity of components extracted is limited by many factors, among which is the solubility of components in the solvent at the boiling temperature. In addition, experimental time is greatly increased; soxhlet extractions were done over 24 hours versus the typical 3 hour experiments done with supercritical fluid extractions. With supercritical fluid extraction, an increase in pressure can eliminate the use of a co solvent and the CO2 leaves the system as a gas, rendering a solvent free sample. Also, cost can be minimized by recycling the supercritical fluid back into the system. Whereas in soxhlet extractions, the solvent is saturated with the extract and must be separated and discarded before the extracted material can be used. This adds an extra step which can be very costly on an industrial scale. In addition to the active ingredients extracted from the berries, many pesticides and insecticides were also extracted as outlined in Table 8: Table 8: Pesticides and Insecticides Extracted22 Name Use Gibberelic Acid Germination Quinoline Pesticide precursor Isoquinoline Insecticide Imazalil: (1H imidazole1 methyl) Fungicide Furfural Fumigant: pesticide Methotrexate Insecticide Strychnine Pesticide Cholesteryl : (Cholest 5 en 3 ol) Inert pesticide ingredient Supercritical fluids can be an inexpensive and safe alternative for extracting useful components from solid starting materials. Although, it was shown that moderate temperature
91 and pressure changes can have a big effect on the components extracted; changes in temperature seemed to have a greater effect on the components extracted. However when dealing with natural products, selection of temperature is a key factor, higher temperatures can degrade some of the desired active components. It has been shown that supercritical fluids can be used for selective extraction of desired components. In addition, it has been shown that supercritical fluids can be used as a means of extracting potentially harmful pesticides and insecticides from plant and natural components.
92 Chapter 7 Conclusions, Recommendations and Future Directions This chapter will include all relevant conclusions to this work. In addition it will provide several recommendations and improvements on the current setup and experimental conditions. And finally it will propose additions that can be done in the future to maximize results. 7.1 Conclusions The experiments conducted yielded several important vitamins and acids that are useful for human health as previously discussed in the results section of this thesis. However there were other compounds such as pesticides and insecticides extracted in the process as well. The extraction of such potentially harmful components is another application for supercritical fluids. The Supercritical technology can also be used to extract undesirable compounds in order to purify important foods and desirable products from pesticides and insecticides. This allows for better, healthful berries in this case that can be safely used to devise vitamins and medications with a low cost margin attached. 7.2 Recommendations and Future Directions At the moderately high pressures used in the experiments conducted, only some components of the berries were extracted. It is recommended that much higher pressures be used in order to extract more components. Pressures that are double and even triple those used
93 for this work will surely improve the results by potentially extracting heavier vitamins and minerals present in the berries and may eliminate the use of a co solvent. To maximize on the time for each experiment, it is recommended that more than one collection vessel be connected to the system. This will allow for more than one sample to be collected from each individual run. Each collection vessel can also be maintained at a different pressure so that several samples at several different pressures are obtained from one experiment. A slightly different experimental procedure can be utilized by soaking the solid starting material in the co solvent or water for a couple of hours before allowing the supercritical fluid to flow. This may help to open the plant pores and thus help with the extraction process. In addition, different co solvents can be tried to determine if different components can be extracted using different co solvents. Different components in samples obtained from each experiment can be analyzed using GC/MS but can also be isolated using an HPLC setup in the future as a stepping stone to finding the concentrations of the components present in each sample. Obtaining various different component libraries for the GC/MS analysis can also be a crucial step in identifying a variety of components potentially extracted but can only be identified using certain chemical libraries. Fractionation of extract is another step that can be done after the extraction either by using an HPLC setup or by changing operating conditions on the extraction setup by gradually increasing the pressure.
94 Experimental times can be increased to more than the maximum time limit that was used for this work along with increasing the flow rate of the CO2 in hopes of extracting more compounds at the higher flow rates.
95 References 1. Abbas, K. A., A. Mohamed, A. S. Abdulamir, and H. A. Abas. "A Review of Supercritical Fluid Extraction as New Analytical Method." American Journal of Biochemistry and Biotechnology (2008): 345 53. 2. Abraham, Martin A., and Aydin K. Sunol. Supercritical Fluids : Extraction and Pollution Prevention. New York: American Chemical Society, 1998. 3. Arai, Y., T. Sakou, and Y. Takebayashi. Supercritical Fluids : Molecular Interactions, Physical Properties and New Applications. New York: Springer, 2001. 4. Balch, Phyllis A. Prescription for Dietary Wellness : Using Foods to Heal. New York: Avery, 2003. 5. Blomhoff, Rune. Vitamin A in Health and Disease. Danbury: Marcel Dekker Incorporated, 1994. 6. Brunner, Gerd. Gas Extraction : An Introduction to Fundamentals of Supercritical Fluids and the Application to Separation Processes. Dietrich Steinkopff, 1994. 7. Brunner, Gerd H. Supercritical Fluids as Solvents and Reaction Media. St. Louis: Elsevier Science, 2004. 8. C. Chandan, Ramesh, Yiu H. Hui, Stephanie Clark, Nanna Cross, Joannie C. Dobbs, William J. Hurst, Leo M. Nollet, Eyal Shimoni, Nirmal Sinha, and Erika B. Smith. Handbook of Food Products Manufacturing: Health, Meat, Milk, Poultry, Seafood, and Vegetables. Wiley Interscience, 2007. 9. Chow, Ching K. Fatty Acids in Foods and their Health Implications,Third Edition (Food Science and Technology). Null: CRC, 2007. 10. Clifford, Tony. Fundamentals of supercritical fluids. New York: Oxford UP, 1999. 11. Day, Chany Yih, Chiehming J. Chang, and Chiu Yang Chen. "Correction: Phase Equilibrium of Ethanol + CO2 and Acetone + CO2 at elevated pressures." Journal of Chemical and Engineering Data (1999): 365 65. 12. Day, Chany Yih, Chiehming J. Chang, and Chiu Yang Chen. "Phase Equilibrium of Ethanol + CO2 and Acetone + CO2 at elevated pressures." Journal of Chemical and Engineering Data (1996): 839 43. 13. Dean, John R., and S. Hitchen. Applications of supercritical fluids in industrial analysis. Springer Science & Business, 1993.
96 14. DeSimone, Joseph M., and William Tumas, eds. Green Chemistry Using Liquid and Supercritical Carbon Dioxide (Green Chemistry Series). New York: Oxford UP, USA, 2003. 15. Ganguly, Jagannath, ed. Biochemistry of Vitamin A. New York: CRC P, 1989. 16. Gartner, Leslie P., and James L. Hiatt. Color Textbook of Histology. Philadelphia: Saunders, 2006. 17. Geankoplis, Christie John. Transport Processes and Separation Process Principles (Includes Unit Operations). Upper Saddle River: Prentice Hall PTR, 2003. 18. Gupta, Ram B., and Jae Jin Shim. Solubility in Supercritical Carbon Dioxide. Null: CRC, 2006. 19. Hamburger, M., D. Baumann, and S. Adler. "Supercritical Carbon Dioxide Extraction of Selected Medicinal Plants Effects of High Pressure and Added Ethanol on Yield of Extracted Substances." Phytochemical Analysis 15 (2004): 46 54. Wiley InterScience. 20. Jacques, R. A., J. G. Santos, C. Dariva, J. Vladimir Oliveira, and E. B. Caramo. "GC/MS Characterization of Mate Tea Leaves Extracts Obtained From High Pressure CO2 Extraction." Journal of Supercritical Fluids (2007): 354 59. 21. Jung, Jennifer, and Michel Perrut. "Review: particle design using supercritical fluids: Literature and patent survey." Journal of Supercritical Fluids (2001): 179 219. 22. Kegley, S.E., Hill, B.R., Orme S., Choi A.H., PAN Pesticide Database, Pesticide Action Network, North America (San Francisco, CA, 2008), http://www.pesticideinfo.org. 23. 22King, Jerry W., and Gary R. List. Supercritical fluid technology in oil and lipid chemistry. Champaign, Ill: AOCS P, 1996. 24. 23Kiran, Erdogan, and Levelt Sengers. Supercritical fluids fundamentals for application. Dordrecht: Kluwer Academic, 1994. 25. Lauda Eco Line Manual. Brochure. Germany. 26. Leitner, Walter, and Philip G. Jessop. Chemical synthesis using supercritical fluids. Weinheim: Wiley VCH, 1999. 27. Martinez, Jose L., ed. Superficial Fluid Extraction of Nutraceuticals and Bioactive Compounds. New York: C R C P LLC, 2007. 28. McHugh, Mark, and Val Krukonis. Supercritical Fluid Extraction Principles and Practice. Stoneham: Butterworth, 1986. 29. Mndez Santiago, Janette, and Amyn S. Teja. "The Solubility of Solids in Supercritical Fluids." Fluid Phase Equilibria 158 (1999): 501 10. 30. Modell, Michael, and Jefferson W. Tester. Thermodynamics and Its Applications. Upper Saddle River: Prentice Hall, 1996.
97 31. Montas, Fernando, Tiziana Fornari, Pedro J. Martn lvarez, Antonia Montilla, Nieves Corzo, Agustin Olano, and Elena Ibez. "Selective Fractionation of Disaccharide Mixtures by Supercritical CO2 with Ethanol as Co Solvent." Journal of Supercritical Fluids (2007): 61 67. 32. Mukhopadhyay, Mamata, and Sameer V. Dalvi. "New Prediction Method for Ternary Solid Liquid Vapor Equilibrium from Binary Data." Journal of Chemical and Engineering Data (2005): 1283 289. 33. Mukhopadhyay, Mamata. Natural Extracts Using Supercritical Carbon Dioxide. Null: CRC, 2000. 34. Nyvlt, Jaroslav. Solid Liquid Phase Equilibria. St. Louis: Elsevier, 1977. 35. Perk, Joep, Peter Mathes, Helmut Gohlke, Catherine Monpere, and Irene Hellemans. Cardiovascular Prevention and Rehabilitation. New York: Springer, 2007. 36. Plattenberg, Rachel H. Environmental Pollution : New Research. New York: Nova Science, Incorporated, 2006. 37. PolyScience Digital Constant Temperature Circulators. Brochure. Illinois. 38. Prausnitz, John M., Edmundo Gomes De Azevedo, and Rudiger N. Lichtenthaler. Molecular Thermodynamics of Fluid Phase Equilibria. Upper Saddle River: Prentice Hall PTR, 1998. 39. Precision Wet Test Meter. Brochure. Texas. 40. Prior, Ronald L., Sheryl A. Lazarus, Guohua Cao, Helen Muccitelli, and John F. Hammerstone. "Identification of Procyanidins and Anthocyanins in Blueberries and Cranberries (Vaccinium Spp.) Using High Performance Liquid Chromatography/Mass Spectrometry." Journal of Agriculture and Food Chemistry (2008): 1270 276. 41. Ramsey, E. D. Analytical supercritical fluid extraction techniques. Springer, 1998. 42. Raspo, Isabelle, Christophe Nicolas, Evelyne Neau, and Sofiane Meradji. "Diffusion coefficients of solids in supercritical carbon dioxide: Modelling of near critical behaviour." Fluid Phase Equilibria (2008): 214 22. 43. Reverchon, Ernesto, and Iolanda De Marco. "Review: Supercritical Fluid Extraction and Fractionation of Natural Matter." Journal of Supercritical Fluids (2006): 146 66. 44. Rieger, Mark. Introduction to Fruit Crops. New York: Food Products P, 2006. 45. Siegel, Michael. The Encyclopedia of New Jersey. Ed. Maxine N. Lurie and Marc Mappen. New York: Rutgers UP, 2004. 46. Smith, J. M., Hendrick C. Van Ness, and Michael M. Abbott. Introduction to Chemical Engineering Thermodynamics. New York: McGraw Hill Companies, The, 2004.
98 47. Subramaniam, Bala, Roger A. Rajewski, and Kirk Snavely. "Pharmaceutical Processing with supercritical Carbon Dioxide." Journal of Pharmaceutical Sciences 86 (1997): 885 90. 48. Sun, Ya Ping. Supercritical Fluid Technology in Materials Science and Engineering: Syntheses Properties, and Applications. Null: CRC, 2002. 49. Sunol & Sunol in Wypych, George, ed. Handbook of solvents. Toronto: ChemTec, 2001. 50. United States. Department of Agriculture. Blueberry Nutritional Data. 19 Jan. 2009. 51. United States. Department of Agriculture. Cranberry Nutritional Data. 19 Jan. 2009. 52. Vatai, Tnde, Mojca ÂŠkerget, and ÂŽeljko Knez. "Extraction of Phenolic Compounds from Elder Berry and Different Grape Marc Varieties Using Organic Solvents and / or Supercritical Carbon Dioxide." Journal of Food Engineering (2009): 246 54. 53. Vieira, Celme, Stefano Evangelista, Rocco Cirillo, Annalisa Lippi, Carlos A. Maggi, and Stefano Manzini. "Effect of ricinoleic acid in acute and subchronic experimental models of inflammation." Mediators of Inflammation 9 (2000): 223 28. 54. Vitamin A Supplements : A Guide to Their Use in the Treatment and Prevention of Vitamin A Deficiency and Xerophthalmia. Chicago: World Health Organization, 1997. 55. Von Rohr, Rudolf, and Ch Trepp. High pressure chemical engineering proceedings of the 3rd International Symposium on High Pressure Chemical Engineering, Zurich, Switzerland, October 7 9, 1996. Amsterdam: Elsevier, 1996. 56. Walas, Stanley M. Phase Equilibria in Chemical Engineering. London: Butterworths Tolley Limited, 1985. 57. Xu, Xiang, Yanxiang Gao, Guangmin Liu, Qi Wang, and Jian Zhao. "Optimization of supercritical carbon dioxide extraction of sea buckthorn (Hippopha thamnoides L.) oil using response surface methodology." LWT (2008): 1223 231. 58. York, Peter, Uday B. Kompella, and Boris Y. Shekunov. Supercritical Fluid Technology for Drug Product Development. Danbury: Marcel Dekker Incorporated, 2004. 59. Yoshioka, M., and Simone Parvez. Supercritical Fluid Chromatography And Micro hplc (Progress in HPLC). New York: Brill Academic, 1989. 60. Zaidul, I. S., N. A. Nik Norulaini, A. K. Mohd Omar, and R. L. Smith Jr. "Supercritical Carbon Dioxide (SC CO2) Extraction and Fractionation of Palm Kernal Oil From Palm Kernal as Coca Butter Replacers Blend." Journal of Food Engineering (2006): 210 16. 61. Zuo, Yuegang, Chengxia Wang, and Jian Zhan. "Separation, Characterization, and Quantitation of Benzoic and Phenolic Antioxidants in American Cranberry Fruit by GC/MS." Journal of Agricultural and Food Chemistry (2002): 3789 794.
100 Appendix A: Tables of BB and CB Nutritional Information Table 9: Blueberry Key Nutrients Blueberry Key Nutrients 4, 50 Element g/100g (unless otherwise noted) Element g/100g (unless otherwise noted) Water 54.66 Protein 0.41 Fiber 2.6 Sucrose/sugars Fructose Glucose 37.75 Vitamin C 0.7mg Vitamin b1 (thiamine) 0.023mg Folate 3mcg Vitamin b2 (riboflavin) 0.034mg Iron 0.8mg Vitamin b3 (niacin) 0.091mg Manganese Na** Pantothenic acid Na** Potassium 115mg Biotin 0.029mg Calcium 27mg Vitamin E Alpha Tocopherols 0.23mg Magnesium 10mg Silicon Na** Phosphorus 12mg Fats/Lipids 0.2 Sodium 12mg Carbohydrates 44.38 Zinc 0.1mg Selenium 0.4mcg Copper 0.112mg Limonene Na** Alpha carotene Na** Myristicin Na** Beta carotene 13mcg Thymol Na** Caryophyllene Na** Pectin Na** Chlorogenic acid Na** Catechins Na** Eugenol Na** Vitamin A, RAE 1mcg Ellagic acid Na** Vitamin K 3.9mcg Tocotrienols Na** Lutein + zeaxanthin 33mcg Choline 3.8mg Palmitic Acid Na** ** Na refers to values that were unavailable at the time of data compilation
101 Appendix A: (CONTINUED) Table 10: Cranberry Key Nutrients Cranberry Key Nutrients 4, 51 Element g/100g (unless otherwise noted) Element g/100g (unless otherwise noted) Water 60.65 Citric acid Na** Energy 151 Protein 0.2 Carbohydrates 38.9 Fiber 1 Magnesium 3mg Potassium 26mg Fructose Sucrose Glucose 37.9 Calcium 4mg Benzoic acid Na** Folate 3mcg Ellagic acid Na** Eugenol Na** Manganese Na** Malic acid Na** Selenium 0.3mcg Sodium 29mg Phosphorus 6mg Vitamin b1 (thiamine) 0.015mg Chloine 3.8mg Vitamin E/ tocopherols 0.83mg Biotin 0.014mg Ferulic acid Na** Chlorogenic acid Na** iron 0.22mg Vitamin A, RAE 2mcg Copper 0.02mg Zinc 0.05mg Vitamin b3 (niacin) 0.1mg Vitamin b2 (riboflavin) 0.021mg Beta carotene 25mcg Fats/Lipids 0.15 Oleic Acid (18:1) 0.021 Linoleic Acid (18:2) 0.04 Alpha Linoleic Acid 0.026 Palmitoleic Acid (16:1) 0.001 Palmitic Acid (16:0) 0.008 Quercetin Na** Vitamin C 2mg Vitamin K 1.4 mcg Lutein +zeaxanthin 63mcg Pantothenic Acid Na** Ricinoleic Acid Na** **Na refers to values that were unavailable at the time of data compilation
102 Appendix B: Sample Calculations The following sample calculations are done to ensure the solvent mixture used is above the critical point. This is done by using the peng robinson equation of state coupled with van der Waals mixing rules. Operating Parameters: Pressure P=124 bar Gas constant R=8.314 J/mol*K Temperature T=315.928 K Critical Temp (CO2) Tc=304.3 K Critical Pressure (CO2) PC=73.8 bar Accentric factor (CO2) =0.228 Tr=1.03812 Peng Robinson Equation of State
103 Appendix B: (CONTINUED) Applying the mixing rules Mole fraction CO2 yi=0.9 Mole fraction Ethanol yj=0.1 Calculating Dimensionless Numbers Calculating ReynoldÂ’s number for CO2 at a pressure of 2100 psia, a temperature of 40C given a diameter D= 7.36*10 4 m, CO2 density = 780.4 kg/m3, average fluid velocity v= 0.47m/s and fluid viscosity = 67.74*10 6 kg.s/m.s2. Calculating the Prandtl number: Calculating the Nusselt number:
104 Appendix B: (CONTINUED) Calculating the Sherwood number: Rearranging the Schmidt correlation and solving for D at the same conditions yields: Now plugging back into the Sherwood equation and solving for the mass transfer coefficient Kc:
105 Appendix C: Simplified Procedure A step by step simplified experimental procedure, shut down and cleaning methods used is provided as follows: Before a run Make sure all cells are clean and dry Weigh desired amount of blueberries (~5g) Load them carefully in extraction cell Tighten all connections Make sure water beaker has enough water for depressurizing step Turning on the Equipment Set Timer A: (Heating) make sure heating bath's switch is turned ON and set to desired temp. Set Timer B: (Cooling CO2) make sure cooling bath's switch is turned ON. Plug fan in Make sure flow meter has enough water in reservoir and in meter tube Turn CO2 flow meter ON. Turn HPLC pump ON Turn CO2 pump ON Verify box temp
106 Appendix C: (CONTINUED) Verify depressurizing connections on N2 tanks are tightened Open N2 tanks Set to desired pressure Wait a few minutes (check pressures inside controlled environment and record) Verify there's enough ethanol in reservoir Direct 3 way valve to the system Ensure the tubing lines are filled with ethanol, if not, run ethanol for a few minutes Set ethanol flow rate to desired flow (~0.02ml/min) Note HPLC pump starting pressure Open CO2 tank Direct 3 way valve to the system Open pump valve Select F2, Then E to set flow Set Flow to 2G/min Note starting pressure on CO2 pump Note the starting time of the experiment
107 Appendix C: (CONTINUED) Once pressure begins to stabilize (about 1.5 hrs): (pressure of HPLC/ CO2 pumps reaches set pressure on tank A) Run CO2 flow meter and hit next screen till run screen and hit Enter. Note the starting time and starting gas Volume!! After 2 4 hours: Shut down Close back pressures (N2 tanks) Stop HPLC pump Stop CO2 pump Close CO2 tank Stop CO2 flow meter and note the final Volume and Gas Temp Record the time of stopping Turn off timer A (heating bath) Open controlled environmentÂ’s cover Plug back pressure heating tape in to prevent freezing during depressurization Slowly and carefully start depressurizing A & B Observe to insure stable depressurizing (takes up to 1.5 hrs depending on the set pressure) Unplug heating tape
108 Appendix C: (CONTINUED) Loosen connections slowly on extraction cell and collection cell Weigh two empty beakers and record weight Collect starting material carefully in one beaker and weigh Collect fraction carefully in another beaker or vial and weigh Release any remaining CO2 from fraction beaker (if it's fizzing, then there's CO2) Cap the extract and wrap it in foil (light sensitive) Cleaning Fill a beaker with isopropanol or ethanol Drop filters in beaker (stir slightly) Thoroughly wash extraction and collection cells with water Check there's no residue remaining Cap one end of extraction cell and run a few ml of ethanol in it Air dry Pump Pure CO2 and ethanol in the lines for a minimum of 45 minutes to clean all the lines