The coupling of innovative technologies has emerged as a smart alternative for the process intensification of bioactive compound extraction from plant matrices. In this regard, the development of ...hybridized techniques based on the low-frequency and high-power ultrasound and high-pressure technologies, such as supercritical fluid extraction, pressurized liquids extraction, and gas-expanded liquids extraction, can enhance the recovery yields of phytochemicals due to their different action mechanisms. Therefore, this paper reviewed and discussed the current scenario in this field where ultrasound-related technologies are coupled with high-pressure techniques. The main findings, gaps, challenges, advances in knowledge, innovations, and future perspectives were highlighted.
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IZUM, KILJ, NUK, PILJ, PNG, SAZU, UL, UM, UPUK
Supercritical carbon dioxide (CO
) extraction techniques meet all-new consumer market demands for health-promoting phytochemical compound-rich extracts produced from green and sustainable technology. ...In this regard, this review is dedicated to discussing is the promise of integrating high-pressure CO
technologies into the
L. processing chain to valorize its valuable pharmaceutical properties and food biomass. To do this, the cannabis plant, cannabinoids, and endocannabinoid system were reviewed to understand their therapeutic and side effects. The supercritical fluid extraction (SFE) technique was presented as a smart alternative to producing cannabis bioproducts. The impact of SFE operating conditions on cannabis compound extraction was examined for aerial parts (inflorescences, stems, and leaves), seeds, and byproducts. Furthermore, the opportunities of using non-thermal supercritical CO
processing on cannabis biomass were addressed for industrial hemp valorization, focusing on its biorefinery to simultaneously produce cannabidiol and new ingredients for food applications as plant-based products.
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•Economic evaluation of sequential multi-stage and single-stage extractions was provided.•Tocols, fatty acids, carotenoids, and phenolics compose the extract fractions.•The cost of ...manufacturing decreased as the production scale increased.•Production scale and sale price played a vital role in the sensitive study.•The extraction processes are feasible alternatives and attractive for investments.
This work presents the economic evaluation of two processes to obtain: i) four extract fractions from passion fruit bagasse by sequential multi-stage process comprising three steps of supercritical fluid extraction (SFE) and one step of pressurized liquid extraction (PLE); ii) one extract from passion fruit rinds by single-stage PLE process. The economic simulation and sensitivity study were performed for plants containing two extraction vessels of 1, 5, 50 and 500L. The scale-up led to a decrease in the cost of manufacturing (COM). COMs of extracts from sequential multi-stage and single-stage processes decreased from US$ 220.51/kg to US$ 26.33/kg and US$ 71.03/kg to US$ 11.96/kg, respectively, when the system capacity increased from 2×1L to 2×500L. Itemized costs related to materials, facilities, labor and utilities are also presented. Both processes are economically promising, especially when the extracts are produced in large scale and sold by the current market price.
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GEOZS, IJS, IMTLJ, KILJ, KISLJ, NUK, OILJ, PNG, SAZU, SBCE, SBJE, UL, UM, UPCLJ, UPUK, ZRSKP
•Economic assessment of SFE+PLE-US hybridization is the first time reported•Economic assessment for obtaining piceatannol-rich extract was provided•Scale-up increased productivity and reduced the ...cost of manufacturing•Scale-up and extract's selling price played a fundamental role in the feasibility•The SFE+PLE showed feasibility, and SFE+PLE-US presented infeasibility at tested conditions
Low-frequency ultrasound has been efficiently applied to intensify high-pressure extraction processes. However, large-scale hybridization still is challenging. This work aims to present an economic feasibility study of two different extraction processes to produce a piceatannol-rich extract from yellow passion fruit bagasse – process A (supercritical fluid extraction + pressurized liquid extraction – SFE+PLE) and process B (SFE+PLE assisted by ultrasound – SFE+PLE-US). The SuperPro Designer software was employed to estimate the manufacturing cost (COM), productivity, and economic return rates, calculated for each overall extraction curve and different scales (50, 200, and 500 L). Process A showed economically viable, while process B showed infeasible at a 20% minimum acceptable rate of return. The lowest COM and better economic return were obtained with process A at 75 °C, 500 L, and 90 min. In addition, a sensitivity study was carried out, indicating the possibility of selling the extract below the market price, representing a competitive differential to implement the extraction process at large scales. It is noteworthy that up to now, the economic feasibility of PLE-US on a large scale has not yet been performed, so this work represents a starting point for studies of PLE-US hybridization on large scales.
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GEOZS, IJS, IMTLJ, KILJ, KISLJ, NLZOH, NUK, OILJ, PNG, SAZU, SBCE, SBJE, UILJ, UL, UM, UPCLJ, UPUK, ZAGLJ, ZRSKP
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•Tahiti lime pomace was used to obtain phenolic compounds extracts with high antioxidant capacity.•PLE and UAE were evaluated to obtain extracts from Tahiti lime pomace.•PLE achieved ...the highest yields and antioxidant capacity but it spent more time.•UAE produced the second higher yields but in a very short extraction time.•This work is the first to provide technical evaluation of PLE and UAE on Tahiti lime pomace.
This work evaluated two emerging techniques in extracting phenolic compounds from Tahiti lime pomace – pressurized liquid extraction (PLE) and ultrasound-assisted extraction (UAE). PLE was performed at different temperatures (60 – 110 °C) and times (5 – 40 min), and UAE was carried out varying ultrasound power (160 – 792 W), time (2 – 10 min), and solvent to feed mass ratio (20 – 40 kg solvent/kg dried pomace). Both used ethanol and water (3:1, wt.) as the solvent. The effects of these variables were evaluated on global extraction yield, polyphenols, hesperidin, narirutin yields, and antioxidant capacity. PLE was strongly affected by temperature and extraction time, and the highest temperature (110 °C) provided the best results for global yield, total phenolic, and ORAC, except for hesperidin and narirutin, which were not significative affected by temperature. UAE revealed a weak dependency on power, S/F, and time; however, the lowest power level significantly increased the yields compared to no power application. Thus, P = 480 W, t = 6 min, and S/F = 30 was chosen as the best condition in the UAE in terms of overall extraction yield, total phenolics, specific phenolics, antioxidant capacities, and solvent and energy expenditures. UAE mechanisms were investigated by comparing with heated and stirred maceration, and scanning electron microscopy suggested that total phenolic yield was influenced by mechanisms that only ultrasound can provide. Micrographics confirmed the cavitation effect on Tahiti lime pomace particles' surface. To sum up, PLE resulted in the highest yields and antioxidant capacity, followed by UAE.
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GEOZS, IJS, IMTLJ, KILJ, KISLJ, NLZOH, NUK, OILJ, PNG, SAZU, SBCE, SBJE, UILJ, UL, UM, UPCLJ, UPUK, ZAGLJ, ZRSKP
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•Developing a model for aerogel production using supercritical fluid drying.•Evaluating the model using fresh experimental data.•Optimizing the process in terms of short drying time ...and low CO2 consumption.
Alginate-based aerogel particles were produced by dripping alginate solution (2%, w/w) into CaCl2 solution (100 mM) followed by solvent exchange and supercritical drying (SCD). Hydrogel particles were first produced by the dripping method. Beads were separated from the CaCl2 cross-linking solution by filtration. Then, the solvent exchange was performed at room temperature by the immersion of the particles into ethanol/water mixtures. Next, the obtained alcogels were submitted to a SCD process at 12 MPa, 40 °C, and CO2 flow rate from 0.27 to 0.84 kg/h, and the recovered ethanol was gravimetrically measured. Finally, a comprehensive mathematical model was employed to describe the SCD process using the law of conservation of mass. The model, which resulted in two partial differential equations for the fluid and solid phases, was numerically solved using the finite difference method, successfully validated by the experimental data and employed in the sensitivity analysis and optimization.
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•The sequential high-pressure extraction process of biquinho pepper was investigated.•Capsiate and phenolics compounds composed the SFE and PLE extracts, respectively.•Economic ...evaluation of the sequential process (SFE + PLE) was provided.•The COM of SFE and PLE extracts were US$ 5,291.02/kg and 25.39/kg, respectively.•The proposed extraction process is a feasible alternative and attractive investment.
The economic evaluation of single stages of supercritical fluid extraction (SFE) and pressurized liquid extraction (PLE) and sequential high-pressure extraction (SFE + PLE) was performed for the obtention of capsiate-rich oleoresin and phenolics from biquinho pepper. SuperPro Designer was used to estimate the cost of manufacturing (COM), which was calculated for each kinetic yield point to define the end of the extraction to be used in the evaluation of the sequential process. Extractor volumes of 5, 50, and 500 L were considered. The evaluation of single stages (50 L and 500 L scales) showed the lowest COM for capsiate and phenolic compounds at the solvent to feed mass ratios of 4.9 and 10, respectively. For both cases, the scale-up reduced the COM. The COM values obtained for the sequential process were lower than the commercialization price of the extracts, which suggests that producing biquinho derived products is economically attractive.
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GEOZS, IJS, IMTLJ, KILJ, KISLJ, NUK, OILJ, PNG, SAZU, SBCE, SBJE, UL, UM, UPCLJ, UPUK, ZRSKP
Acai is one of the leading Brazilian Amazon fruits, which pulp is consumed throughout the country and exported to several others. Acai by-product represents 80–90% berry mass. In order to reuse the ...by-product, pressurized liquid extraction (PLE) was applied. Solvent composition and temperature were studied through their effect on the global extraction, total phenolic, reducing sugars yields, and antioxidant capacity. High temperature (115 ºC) and ethanol+water (75 wt%) favored obtaining antioxidant extracts. These PLE conditions were kinetically studied and economically evaluated. The end of the first theoretical extraction period (tCER) resulted in the extracts’ minimum cost of manufacturing (COM). Regardless of the extraction time, scale-up reduced the COM, advising the process at large scales. A sensitivity study was carried out considering different extract selling prices as scenarios. All the estimated selling prices showed encouraging economic indexes. PLE proved to be technically and economically feasible to obtain acai by-product extracts with confirmed antioxidant capacity.
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•PLE produced phenolic extracts from acai by-products.•115 ºC and 75% wt% ethanol resulted in higher antioxidant capacity.•PLE was evaluated from an economic perspective.•Minimum cost of manufacture was identified regarding scale and extraction time.•Economic indexes encourage the obtention of phenolic extract from acai by-product.
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GEOZS, IJS, IMTLJ, KILJ, KISLJ, NLZOH, NUK, OILJ, PNG, SAZU, SBCE, SBJE, UILJ, UL, UM, UPCLJ, UPUK, ZAGLJ, ZRSKP
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•Subcritical water hydrolysis was performed in a single and two sequential reactors.•Sugars, organic acids, and amino acids were recovered from brewer’s spent grains.•The highest ...sugar concentration was obtained using a single reactor at 180 °C.•Arabinose and xylose were the main monosaccharides released into the hydrolysate.•Valine, tryptophan, and lysine were the main amino acids produced.
This study evaluated the subcritical water hydrolysis (SWH) of brewer's spent grains (BSG) to obtain sugars and amino acids. The experimental conditions investigated the hydrolysis of BSG in a single flow-through reactor and in two sequential reactors operated in semi-continuous mode. The hydrolysis experiments were carried out for 120 min at 15 MPa, 5 mL water min−1, at different temperatures (80 – 180 °C) and using an S/F of 20 and 10 g solvent g−1 BSG, for the single and two sequential reactors, respectively. The highest monosaccharide yields were obtained at 180 °C in a single reactor (47.76 mg g−1 carbohydrates). With these operational conditions, the hydrolysate presented xylose (0.477 mg mL−1) and arabinose (1.039 mg mL−1) as main sugars, while low contents of furfural (310.7 µg mL−1), 5-hydroxymethylfurfural (<1 mg L-1), and organic acids (0.343 mg mL−1) were obtained. The yield of proteins at 180 °C in a process with a single reactor was 43.62 mg amino acids g−1 proteins, where tryptophan (215.55 µg mL−1), aspartic acid (123.35 µg mL−1), valine (64.35 µg mL−1), lysine (16.55 µg mL−1), and glycine (16.1 µg mL−1) were the main amino acids recovered in the hydrolysate. In conclusion, SWH pretreatment is a promising technology to recover bio-based compounds from BSG; however, further studies are still needed to increase the yield of bioproducts from lignocellulosic biomass to explore two sequential reactors.
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GEOZS, IJS, IMTLJ, KILJ, KISLJ, NLZOH, NUK, OILJ, PNG, SAZU, SBCE, SBJE, UILJ, UL, UM, UPCLJ, UPUK, ZAGLJ, ZRSKP
Carrying lipophilic compounds protection within alginate microgels is a challenge, mainly due to the necessary oil-core matrix. Based on this demand, this study aimed to evaluate the use of glass ...microfluidic devices to produce emulsion-filled alginate microgels and understand the effect of process variables on microgels size and polydispersity. Firstly, stable and monodisperse size-distributed oil microdroplets were formed by preparing an oil-in-water (O/W) emulsion using high shear followed by ultrasound. The continuous aqueous phase was composed of Na-alginate, cellulose nanocrystals and ultrafine calcium carbonate. Sunflower oil composed the emulsion oil phase (10%, w/w). Secondly, oil-in-water-in-oil (O/W/O) emulsions were formed within microfluidics devices to obtain emulsion-filled hydrogel particles. The previously produced O/W emulsion was introduced as the dispersed phase into a continuous phase containing sunflower oil, PGPR and acetic acid. The aqueous phase was gelled by internal gelation, promoting the alginate network. Monodisperse particle size distribution was observed, with a coefficient of variation lower than 6% and mean size ranging from 259 to 526 μm. Microgels size was influenced by the viscosity of O/W emulsion and the phases flow rates. Our results show the potential of microfluidic processes for producing microgels and filled microgels to encapsulate lipophilic compounds.
•Emulsion filled alginate microgels was formulated in microfluidic devices.•Phases' composition was studied before being used in microchannels.•O/W emulsion composed the dispersed phase, and sunflower oil, PGPR, and acetic acid the continuous phase.•Dispersed phase viscosity and both phase flow rates affected the microgels size.•Higher Qc/Qd produced smaller alginate microgels size and emulsion filled alginate microgels particles.
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GEOZS, IJS, IMTLJ, KILJ, KISLJ, NLZOH, NUK, OILJ, PNG, SAZU, SBCE, SBJE, UILJ, UL, UM, UPCLJ, UPUK, ZAGLJ, ZRSKP
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