Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/14—Ultrafiltration; Microfiltration
  • B01D61/147—Microfiltration
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23L—FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES, NOT OTHERWISE PROVIDED FOR; PREPARATION OR TREATMENT THEREOF
  • A23L27/00—Spices; Flavouring agents or condiments; Artificial sweetening agents; Table salts; Dietetic salt substitutes; Preparation or treatment thereof
  • A23L27/10—Natural spices, flavouring agents or condiments; Extracts thereof
  • A23L27/12—Natural spices, flavouring agents or condiments; Extracts thereof from fruit, e.g. essential oils
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/14—Ultrafiltration; Microfiltration
  • B01D61/145—Ultrafiltration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2311/00—Details relating to membrane separation process operations and control
  • B01D2311/26—Further operations combined with membrane separation processes
  • B01D2311/2688—Biological processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2315/00—Details relating to the membrane module operation
  • B01D2315/10—Cross-flow filtration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2315/00—Details relating to the membrane module operation
  • B01D2315/16—Diafiltration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2317/00—Membrane module arrangements within a plant or an apparatus
  • B01D2317/02—Elements in series
  • B01D2317/025—Permeate series

Definitions

• the present invention is in the field of industrial processes for the extraction and purification of molecules of commercial interest, concerning the production of extracts containing carotenoids and other substances of interest from cashew processing residues by techniques involving pressing, optionally enzymatic maceration and filtration (micro or ultrafiltration) as well as diafiltration.
• the process proposed by the developed technology allows the production of a yellow dye extract, a product that can be obtained from the industrial residue of large-scale cashew juice production.
• this concentrated and purified cashew carotenoid extract represents an added value to a by-product that the entire food sector " needs to meet the worldwide demands for natural colorings.
• yellow colorants used in Brazil are of synthetic origin and The available natural yellows have an orange color, unlike that obtained by the present technology, which is light bright yellow due to their predominant light yellow colorant xanthophyll composition.
• Patent document PI 0002359-0 discusses a process of high vacuum evaporation and distillation for the extraction and concentration of fat-soluble vitamins and provitamins, including carotenoids, from materials originating as by-products of the industrialization of plant and animal products.
• This prior art document describes a process for the concentration of unsaponifiable substances containing fat-soluble vitamins and provitamins, growth factors and plant and animal hormones, known as "value products", obtained from products of animal or vegetable origin, or residues from the industrialization of these products, without the need for solvents.
• the process comprises the extraction and concentration of so-called products by evaporation / distillation, and also the production of fatty acids and other high quality organic acids by hydrolysis of the residues obtained from distillation / evaporation.
• Patent Document PI 0507797-4 describes a process and equipment for diafiltration of thickened fruit juices.
• the product to be filtered is subjected to a filtration process.
• a first flow of a wash fluid (water) and a second flow of a product permeate (flow driven back by the filter media used) are added, thus the product flow, before entering the membrane system. is diluted by the first and second streams.
• WO 2004094350 also describes a method for extracting carotenoids from plant materials using supercritical fluid extraction.
• the extraction with supercritical fluid is done in two steps.
• the first extract includes obtaining ⁇ -carotene;
• the second extract may have a controlled concentration of ⁇ -carotene and also includes substantial amounts of lutein.
• This process (WO 2004094350) has significant differences from the process presented by the present invention, which does not include any heating or cryogenic steps, as well as a mass of fibrous industrial waste from the pressing of cashew stalks. however, no crushing and / or enzymatic inactivation.
• the presented process deals with a sequence of operations and unit processes which together aim at the concentration and purification of a carotenoid enriched extract under mild conditions and which maximize the yield and purity of the final product.
• the patent application under consideration deals with obtaining a purified carotenoid extract from carrot and other ground and heat-treated vegetables and fruits for blanching.
• a set of operations and processes for obtaining a carotenoid-enriched mass, especially beta-carotene is claimed and initially heated for enzymatic inactivation (bleaching), followed by successive grinding on different meshes to obtain a fine particle mass to be further treated by enzymatic liquefaction and release of carotenoids in aqueous medium.
• this mass is membrane treated to a preconcentration and then filtered with one or two volumes and water to remove water soluble compounds.
• the resulting mass is frozen and immediately thawed to the final carotenoid concentration and the final mass is treated by flash pasteurization to acquire microbiological and biochemical stability.
• patent document PI 0605425-0 describes a process of extracting and purifying serially active and dye-capable substances from solid matrices using supercritical CO 2 extraction for the production of dyes from annatto bixin.
• Said process uses extraction and purification steps using the elution and adsorption columns with series and fraction mounted extractor and fractionator.
• r / BR 2013 / O 0 0 1 3 0must be used in series or in batches.
• This process uses aqueous solution as solvent, which at the end of the process is evaporated at temperatures between 30 and 700 ° C in order not to degrade bixin.
• WO 98/28082 Recovery of mixed carotenoids from microalgae (Dunaliella salina) is described in WO 98/28082.
• a process is presented where harvested cells are disrupted by circulating the algal suspension at high pressures through vigorous pumping.
• the cells may be dehydrated by separation bubble absorption techniques, including a flotation circuit, which has a thinning zone and a concentration zone. If a higher concentration of carotenoids is required, the algae concentrate can be filtered in a tangential flow microfiltration unit in the absence of flocculating agents without permeate carotenoid losses.
• the patent document PI 0006126-3 shows a carotenoid extraction process and other antioxidants from previously crushed plant tissue is "incubated.
• the molecules of interest are recovered by precipitation and thermal treatment, especially cooling followed by heating operations fast, thus a carotenoid-containing extract is recovered as a precipitate.
• Patent document PI 0416795-3 relates to an integrated process for the extraction and purification of tocopherols, carotenoids and sterols from vegetable oils through the use of alcohol esterification processes.
• the report of said patent reports as one of the advantages of using this process to obtain an enriched and purified product, with no substantial decomposition factors of these components of interest, such as sugars that are eliminated in dialysis.
• patent document PI 0103885-0 has as its object the production of a pigment-rich cashew apple extract obtained by a process comprising the humidification of the residual cashew apple juice extraction, the pressing of the mixture. resultant separation of the extract from the solids and concentration thereof by centrifugation and filtration operations.
• the present application for protection represents a development of the technique presented in PI 0103885-0, of common ownership and authorship, adding it with essential steps to obtain a higher quality product and employing technologies that allow continuous optimization in your processing.
• the present development seeks to complement the production of a raw extract obtained from cashew residues with new processing technologies that involve the joining of pressing, enzymatic maceration and processing techniques. filtration employing membranes in specific sequential steps for the production of a concentrated and purified final extract suitable for industrial use and from which various substances of commercial interest, from dyes to food supplements, are isolated.
• the prior art does not provide an equivalent solution for processing raw cashew residue extracts and fails to describe a synergistic process such as that provided by the present invention wherein the fruit extract or residue is pre-processed.
• -Integrated treatments such as enzymatic pressing and maceration to optimize the attainment of end-of-process compounds of interest associated with the final filtration and diafiltration processes that generate a high purity product.
• the present invention describes a process for concentrating and purifying carotenoid extracts from cashew stalk fibers for use as a natural yellow dye using microfiltration and diafiltration membranes.
• the proposed process occurs under controlled conditions without the use of any organic solvent, optionally involving the pre-maceration of cashew fibers using cell structure disaggregating enzymes (pectinases, amylases, cellulases and hemicellulases), which act on fibrous tissues. in combination with controlled presses in successive aqueous extraction cycles. Concentration of the crude extract obtained by maceration / pressing is carried out at room temperature. using tangential flow micro and / or ultrafiltration ceramic membranes.
• the concentrated product is then treated by membrane diafiltration techniques, eliminating much of the undesirable components that favor its deterioration.
• the final concentrated product has the potential of application as a colorant for food and feed, being applicable in the areas of juices and beverages ready for consumption due to the considerable solubility in water. It is estimated, based on the properties of some carotenoids present in the concentrated and purified final extract, that this material has a potential applicability in the area of food supplements such as provitamin A and antioxidants for the food, pharmaceutical and cosmetic industries.
• Figure 1 Schematically presents the general process steps in a flowchart.
• the alphanumeric symbols arranged therein have the following correspondence:
• E0 residual fibers from cashew apple processing
• Figure 2 Schematically presents the general process steps in a flowchart with an emphasis on the optimized pressing step.
• the alphanumeric symbols arranged therein have the following correspondence:
• MO cashew fiber mass for juice production
• AO pressing for juice production
• E0 residual fibers from cashew apple processing
• M Enzymatic maceration (optional)
• F1; F2; F3; F4; F5 and F6 residual fibers from each press cycle
• Figure 3 Schematic representation of a helical press.
• the alphanumeric symbols arranged therein have the following correspondence:
• E0 residual fibers from cashew apple processing
• R residual fiber outputs from each pressing cycle
• V rotation speed control
• FIG. 4 shows a schematic of the membrane diafiltration pilot operating unit.
• the alphanumeric symbols arranged therein have the following correspondence:
• 5A; 5B; 5C and 5D membrane system units
• 3A; 3B; 3C and 3D permeate outputs
• FIG. 4B permeate pickup tank.
• Figure 5 shows a diagram of the membrane diafiltration pilot operating unit with details for its component equipment. The alphanumeric symbols arranged therein have the following correspondence:
• 5A; 5B; 5C and 5D membrane system units; 6A: heat exchanger fluid inlet;
• thermometer 8: thermometer
• FIG. 6 Graph of permeate flow (Lh “1 .m “ 2 ) as a function of volumetric reduction factor for different transmembrane pressures (Ptm).
• Figure 7 Graph of permeate flow (Lh “ .m “ 2 ) as a function of concentration factor for two different situations - with and without the addition of pectinases - throughout the concentration step (filtration on porous micro and / or ultrafiltration and dialysis).
• Figure 8 presents four graphs, (8-I) evolution of volumetric reduction factor (FRV), (8-II) reduced diavolume (DR), (8-III) permeate flow density (FP) and (8-IV) the soluble solids content (TSS), respectively, as a function of time, in the process of extract concentration E2 for two different situations - with and without the addition of pectinases.
• FRV volumetric reduction factor
• DR reduced diavolume
• FP permeate flow density
• TSS soluble solids content
• the present patent application differs from the state of the art by proposing a process which combines concentration and purification procedures by diafiltration with the usual techniques of obtaining purified extract from raw cashew fiber extracts.
• the present process permits the industrial-scale production of a viscous yellow-colored liquid for various uses, such as dye and natural antioxidant in the food, cosmetic and pharmaceutical industries.
• the process object of this patent application consists of a set of operations aimed at obtaining a concentrate of carotenes and xanthophylls, highlighting auroxanthin in useful and trans form, ⁇ -cryptoxanthin, mutatoxanthin and zeaxanthin.
• the ⁇ -carotene and lutein are next to be of major importance, yet have a composition rich in several other carotenoids.
• the proposed process comprises the following steps, corresponding to the indications in Figure 1:
• A) Obtaining a crude aqueous extract of carotenoids, E1, from the waste fibers from cashew apple stalk processing, E0, by pressing.
• enzymatic treatment is optional; it may occur by the addition of cell structure disaggregating enzymes (pectinases, amylases, cellulases and hemicellulases) (M1);
• the first step of the process (A) for obtaining the crude extract is based on the optimization of the process proposed by Brazilian patent document PI 0103885-0.
• the technological development described here involves the use of this extract for the concentration / purification operation / process to obtain a product with high carotenoid concentrations.
• the cashews Prior to the start of the process, the cashews are harvested and taken to a processing unit receiving area, and the nuts are immediately removed, separating the peduncle that is selected and washed to remove dirt and undesirable components for processing. of juice.
• the peduncles are directly pressed in expeller or helical presses, typical of cashew and cashew apple juice processing in processing units in Northeastern Brazil.
• this step * About 80% of whole juice and 20% of residual fibers are generated; as described in PI 0103885-0.
• These fibers (E0) are then humidified in the ratio of one to two parts of fibers for each part of water to be pressed.
• step (A) refers to the series of presses under E0 to obtain the intermediate extract (E2).
• step (E2) commercial enzymes with pectinolytic, amylolytic and cellulolytic activities may or may not be added to increase the pressing yield if necessary.
• the addition of enzymes can be up to 0.5% on the fiber mass, usually the value used is 0.2%.
• step (B) After obtaining an E2 crude extract, it is taken to step (B), where it is treated in 0.1 to 1.0 mm hole screens for an initial standardization to avoid problems of excessive viscosity increase in the phases. end of membrane processing.
• step (C) proceeds in distinct phases: a first phase (C1) in which the volume of the feed tank (1A) is kept constant until the crude extract concentration reaches FRV (volumetric reduction factor) values. 2 to 30 or until the volume of crude extract to be added has been exhausted, a concentration phase (C2) is then initiated with maximum reduction of the concentrated extract volume within the recirculation system, hereinafter retained, until minimum recirculation limit in the membrane assembly.
• a first phase in which the volume of the feed tank (1A) is kept constant until the crude extract concentration reaches FRV (volumetric reduction factor) values. 2 to 30 or until the volume of crude extract to be added has been exhausted
• FRV volume reduction factor
• the aerate of the retainer should be avoided by maintaining a volume that does not allow aeration by the recirculation pump.
• cold preconcentration is promoted using aluminum oxide microporous membrane filtration technology, or simply alumina, and other materials may eventually be employed.
• These membranes possu- in total retention capacity of carotenoids and other hypertensive ⁇ drofóbicas molecules and due to this characteristic of carotenoids are employed as retaining meitr contained in the extract.
• the retentate at the end of (C2) is diafiltered (C3) with the added volume of pure water (diavolume) until a desired soluble solids content (° Brix) is achieved.
• the entire operation is performed under temperature conditions between 10 and 50 ° C aiming at maintaining the functional properties of carotenoids that will be obtained as a concentrated solution and purified by diafiltration at the end of the process.
• the product obtained can be stored at refrigerated temperatures. for later use.
• the final product may additionally be heat treated to provide greater durability, but the use of heat is avoided throughout the process, as it deteriorates the carotenoid content, modifying its molecule profile and consequently its pro- vitaminic activity. antioxidant.
• heat treated the final product has high coloring power for food and pharmaceutical uses.
• the obtained carotenoid concentrate (E3) has the characteristics of being an aqueous extract, in the form of a bright yellow-colored emulsion capable of coloring yellow and orange-yellow juices for use in foods and drinks.
• the product can be used as a natural yellow food coloring; natural antioxidant in capsule form (nutraceutical); provitamin A and fractionation is also possible to isolate groups of carotenoids with specific functions. ⁇ ⁇ "
• step (C) it is important to characterize the tangential microfiltration pilot unit, shown schematically by Figures 4 and 5, where the solvent employed is water.
• the microfiltration unit has a set of four membranes, preferably aluminum oxide (Membralox ® ), and other membrane types may optionally be employed, and the embodiment of the invention is not limited thereto.
• Its feed tank (4A) has a capacity of 3L to 10L with four modules arranged in series, each containing a ceramic membrane with a filtration area of 0.0001 to 0.0900 m 2 , preferably at least 0.0055 m 2 and a pore diameter from 0.01 pm to 0.5 pm, ideally 0.2 pm.
• the tangential velocity is set at a value of 1 ms " to 10 ms " 1 and the hold is continuously circulated in the filtration system.
• the system dead volume is calculated to be 1, 3 L for a 3 L capacity feed tank distributed over the building elements (pumps, tubes, membranes and tray).
• the microfiltration unit allows the control of a number of parameters, including: transmembrane pressure, overall system temperature, tangential velocity and, as shown, the phase involving diafiltration itself follows a three-phase model, equivalent to steps C1, C2 and C3 described above: (1) preconcentration at constant volume (C1); (2) variable volume concentration (C2) and (3) constant volume diafiltration / purification (C3).
• the general processing conditions for purification of carotenoid from the residual fibers of cashew stalk processing involved controls of various operating parameters.
• the temperature was controlled by means of a heat exchanger (10), as indicated in Figure 5, installed in the recirculation circuit of the retained feed using a jacket outside the stainless steel pipes with cold or hot water in order to obtain a stabilization of the temperature.
• temperature in the required range, which is 38 to 42 ° C.
• this temperature can be further increased to a range from 10 to 85 ° C, depending on the purpose of the desired end product.
• Based on metabolic pathways of carotenoid degradation there may also be interest in certain molecules that are degradation products and have more intense dye activity than in their natural state and, in other cases, the need to maintain their integrity. molecule.
• Tangential speed was fixed by controlling the motor rotation of the pump used (11), also shown in Figure 5, and can be controlled by using frequency inverters to increase or decrease this speed depending on the nature of the material worked. (more viscous or less viscous).
• transmembrane pressure is controlled by a pilot system (9A) inlet (9A) end pressure control valve, shown in Figure 5.
• a pilot system (9A) inlet (9A) end pressure control valve shown in Figure 5.
• an average transmembrane pressure in the system of 1 to 5 bar is recommended, preferably 2.7 bar due to the characteristics of the system and the pump used as a driving force promoter, but this pressure can be adjusted to other values as required.
• production system need / capacity, ' ⁇ '
• Example 1 Obtaining purified carotenoid extract.
• the subsequent concentration step (C) employ tangential microfiltration techniques.
• the system pressure was 2.75 bar and the temperature was controlled at 40 ° C ( ⁇ 2 ° C).
• the process was conducted under a concentration factor of 13.
• Concentration by microfiltration techniques on microporous membranes was performed in three phases: a first phase in which the volume of the feed tank is kept constant until the exhaustion of the volume of crude extract, at which time a concentration phase starting with maximum reduction of the volume of concentrated extract within the recirculation system, herein referred to as retained or retained, to the minimum recirculation limit in the membrane assembly; and the third phase where diafiltration occurs in microfiltration microporous membranes with the volume of pure water added until a soluble solids content of between 20 and 30 ° Brix is reached.
• the yield of the operation from 1000 kg cashew stalks is about 30 to 40 kg diafiltered concentrate (E3).
• Example 2 Comparison between extraction with and without the use of enzymes.
• the preconcentration was initially performed with the volume of the constant feed tank, where the concentration factor reached values of about 5 and a second concentration phase was carried out with a decrease in the tank volume to a minimum volume. "possible when the concentration factor reaches its maximum value but without damaging the carotenoid content. After reaching the maximum concentration factor in the microfiltration system, a final phase of retinal diaphiltration purification is performed at the limit condition. of the circulating volume, which is about 1, 3 to 1, 5 L in the microfiltration pilot unit.
• step (C) the treatment parameter of step (C) is explained.
• the methodology used consisted of an initial preconcentration phase, increasing the concentration factor to a recirculation in the system at the minimum limit of the microfiltration pilot unit feed tank followed by the concentrated extract purification phase by performing diafiltration. on microfiltration membranes as shown above.
• every 10 minutes samples were collected for analysis of overall process performance by collecting permeate aliquots and measuring volumes in precision graduated beakers by subjecting them to physicochemical analysis.
• diafiltration phase in each permeate sample an equivalent volume of distilled water was fed back to maintain the total soluble solids content near zero at the end of the process so that an increase in the purity of the carotenoids present in the concentrate can be promoted.
• Final the methodology used consisted of an initial preconcentration phase, increasing the concentration factor to a recirculation in the system at the minimum limit of the microfiltration pilot unit feed tank followed by the concentrated extract purification phase by performing diafiltration. on microfiltration membranes as shown above.
• every 10 minutes samples
• the permeate fluxes were in the range of 130 Lh “1 .m “ 2 for enzyme treatments and 80 Lh ⁇ 1 .m “2 for treatments without enzyme.
• Table 2 presents an overall average of all parameters observed in the process of concentration and purification by diafiltration of the carotenoid rich aqueous extract obtained from the cashew stalk residual fibers from the whole juice processing for (I) and (II).
• Table 2 Global average of all parameters observed in the process of concentration and purification by diafiltration.
• Example 3 Application of the purified extract as a dye.
• FIGS 4 and 5 show a detail of the diafiltration operation - step (C), where the solvent is water. Diafiltration, as shown in Figure 2, was performed in three phases:
• Second phase interruption in the re-feeding of raw extract occurs.
• the volume of the tank drops to the maximum concentration point.
• Permeate sampling was performed only by measuring the permeate flux decay. From the beginning of the diafiltration phase, a digital ATAGO refractometer was used to measure the total soluble solids content (° Brix), monitoring it to keep it close to zero. All soluble materials present in the permeate were discarded, leaving only the water insoluble portion of the extract within the recirculation system and enriched with carotenoids.
• the concentration stage itself (prior to the promotion of diafiltration) is divided into two phases: the constant volume preconcentration of the tank, with feedback of the crude extract and a second stage, with the continuous decline in volume of the extract. to the minimum limit of the pilot unit's supply tank.
• the system typically operates diafiltration by considering the input of cashew fibers in the extract, yielding a volume of about 1,500 mL at the end of the concentration step. A volume of slightly more than the minimum limit of 1,000 mL was employed in the pilot unit to prevent unwanted contact with air. For each of the steps it is important to establish the volume reduction factor as explained below.
• Preconcentration step To calculate the corresponding volumetric reduction factor, the ratio between the volume of the " fed " extract in the circuit and the volume of the retained was used. During this phase, the volume of ' “feeding the crude extract (V) is equal to the permeate volume (V P) throughout the process. The volume of retentate (VR) corresponds to the volume of the tank (V B). The FRV is therefore calculated as follows at this stage:
• V P volume of permeate extracted with each sample collection
• V B feed tank volume (ml).
• the volume of the tank is fixed at 3,000 ml throughout the preconcentration phase.
• Concentration step During this phase, the volume of the tank varies and the volume of permeate is continuously extracted every 10 minutes, but this extraction is not compensated for by adding extract to the feed tank. Thus, the volume of circulating product decreases more rapidly and concentrates in a nonlinear manner.
• the calculation of changes in FRV changes with respect to the preconcentration step and is calculated considering that the circulating volume decreases by the same proportion.
• the permeate volume is collected. This means that the circulating volume represents the initial volume minus the accumulated collected volume at each permeate collection during this phase.
• the calculation formula for each permeate collection in this step is:
• V PC Permeate accumulated volume throughout the process
• V B feed tank volume (mL).
• V P accumulated volume of permeate accumulated in the concentration phase (mL).
• Purification (diafiltration) step During this phase, there is no concentration and the tank volume remains constant until the end of diafiltration, with a soluble solids content of 0 to 10.0 g.kg "1 , measured by a refractometer at diavolumes each sampling during diafiltration. at the end of this step, the manipulation should be retained and finalisada samples " 'finarcoletadas for control analysis and modeling.
• the sample subjected to enzyme pretreatment had an average stabilization at 130 Lh "1 .m " 2 and without pretreatment indicates a value below 80 Lh "1 .m " 2 and indicating good performance and industrial applicability of the proposed process even for the sample without pectinase.
• Figure 8 presents four graphs: (8-I) the evolution of the volumetric reduction factor, (8-II) the reduced diavolume, (8-III) the permeate flow density and (8-IV) the soluble solids content, respectively, as a function of time, in the concentration process of extract E2.
• the curve for the enzyme pretreatment process shows an increasing concentration rate due to the higher permeate flux during all phases of the enzyme. compared to assays without enzyme pretreatment. This fact can be attributed to the action of pectinase as a factor reducing viscosity and decreasing the average particle size in the product.
• Reduced diavolume is a value that corresponds to a ratio between the volume of water added and the volume recirculated in the system. This value is usually used for system resizing, for staggering industrial units. It should be noted, therefore, in Figure 8-11 that there is a linear growth behavior of this parameter over time, indicating good diafiltration performance.
• Diafiltration in this example was performed with a circulating volume of 1.45 L (calculated by summing the extracted permeates) and with the addition of 5.9 L of distilled water for pectinase treatment.
• the circulating volume calculated for diafiltration when no pectinase was added at the previous pressing stage was 1.2 L and 5.6 L of distilled water added to reach soluble solids content close to zero.

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• 2012
  • 2012-04-26 BR BRBR102012009761-3A patent/BR102012009761A2/pt not_active Application Discontinuation
• 2013
  • 2013-04-19 AU AU2013252503A patent/AU2013252503A1/en not_active Abandoned
  • 2013-04-19 IN IN9662DEN2014 patent/IN2014DN09662A/en unknown
  • 2013-04-19 WO PCT/BR2013/000130 patent/WO2013159167A1/pt not_active Ceased
• 2016
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• 2018
  • 2018-05-03 AU AU2018203088A patent/AU2018203088A1/en not_active Abandoned
• 2019
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