Integrated method using solanum lycocarpum fruit

Abstract

The present invention relates to an integrated method using Solanum lycocarpum fruit as a source of raw material, providing a cost-effective method that does not generate toxic residues, requires minimal water input, and preserves the components contained in said fruit from interaction with its pigmented phenolic compounds. The present invention describes, more specifically, a biorefinery method for recovering and reusing the solvents used during the steps thereof, wherein said method comprises six stages aimed at the complete exhaustion of the fruits and the obtainment of six different final products that may be used as precursors or intermediates of new products in various industrial sectors.

Description

[0001] INTEGRATED PROCESS FROM WOLF FRUITS

[0002] FIELD OF THE INVENTION

[0003] The present invention relates to an integrated process using lobeira fruit as a raw material source. More specifically, the present invention relates to processing leading to the complete exhaustion of the raw material and the obtaining of six different end products, with the reuse of solvents throughout said process and without the generation of toxic waste.

[0004] BACKGROUND OF THE INVENTION

[0005] The lobeira, popularly known as jurubebão, juripeba, jurepeba, baba-de-boi, fruta-do-lobo or guarambá, is a plant species found in devastated areas, primary scrubland, secondary formations in high places and along roadsides throughout Brazil, more specifically in the states of Amazonas, Goiás, Maranhão, Mato Grosso, Mato Grosso do Sul, Minas Gerais, Pará, Paraná, Rio de Janeiro, São Paulo and Tocantins. Because it is a hardy plant tolerant of unfavorable environmental conditions, it is considered by ranchers to be a pasture pest, as it grows in different types of soil, such as sandy soils, poor in nutrients, acidic soils, with a pH between 4.5 and 5.5.

[0006] Furthermore, the lobeira plant is characterized by its resistance to temperatures ranging from -2°C (during frosts) to 40°C (in arid climates), fire resistance, and its ability to withstand seasonal water stress. For example, the lobeira does not require much soil moisture, growing well with a minimum of 600 to 1,200 millimeters of annual rainfall. As for fruiting, this begins between 2 and 3 years after planting, and the fruits can weigh up to 1.3 kg.

[0007] Due to its diverse components, the lobeira plant has been studied primarily for use in the food industry, for example, as a source of starch, and in the pharmaceutical industry. However, there is very little information related to the extraction of its major components, as well as its large-scale processing.

[0008] Currently, it is observed that the studies being developed are limited to obtaining a single component or a fraction of components from the fruits of the lobeira plant, employing isolated methods for the individual extraction of each component.

[0009] Patent No. PI1000753-9 discloses an extraction process for obtaining starch from wolf apple (Solatium lycocarpum St. Hil), in which the selected fruits were washed, peeled and chopped, the seeds removed, the pulp crushed, and the resulting starch filtered, decanted, washed twice with distilled water, and dried in a forced-air oven. However, after successive washing and decantation steps, two fractions are obtained (one clear and one dark at the bottom of the flask), resulting in a low-quality starch since it is contaminated with adsorbed pigmented phenolic compounds. Furthermore, the yield is low, on the order of 2.6% on a wet basis.

[0010] Patent application no. PI 0305446-2 aims to provide a water-soluble extract obtained from a plant of the genus Solanum to be used as an active component in a pharmaceutical composition, consisting essentially of at least 60% to 90% solamargine and solasonine, and which can be directly dissolved in pure water with a neutral pH value without the addition of any other solvent and / or solvent aid, thus forming a clear and transparent yellowish aqueous solution with a water solubility ranging from 2 to 20 mg / mL or more. However, it is noted that such processing is not feasible for the lobeira plant, as it would imply grinding an entire plant, according to the preferred embodiment of said application. Furthermore, said patent application aims to obtain the alkaloids solamargine and solasonine, which is not the intention of the present invention.

[0011] Pascoal, AM et al. (“Extraction and chemical characterization of starch from S. lycocarpum fruits”, Carbohydrate Polymers 98 (2013), pp. 1304-1310) report a process for the extraction and chemical characterization of starch from S. lycocarpum fruits, in which citric acid was used as an inhibitor of enzymatic browning. However, citric acid is among the least effective inhibitors for inhibiting enzymatic browning, since its action is notably as an antioxidant agent and not as an inhibitor of the polyphenol oxidase enzyme present in the pulp of lobeira fruits, having an efficacy of 24.3%. Furthermore, this efficacy is dependent on the concentration of polyphenol oxidase, which is intrinsically related to the stage of fruit maturation. Thus, the extraction process used will be effective for a very restricted range of fruits, leading to a limitation of the processing methodology on an industrial scale.Additionally, sodium hydroxide is used to neutralize citric acid and ethanol, generating a highly corrosive residue that requires treatment for its disposal.

[0012] Já Mota, RDP et al. (“Elaboration and Characterization of Biodegradable Films from Swamp Lily (Hedychium coronarium) Starch and Wolf Fruit (Solanum lycocarpum St. Hill) Starch”, Scientific Journal of the SENAI Roberto Mange Faculty of Technology (Jan / Jun 2009), pp. 44-50 - ISSN 1981-8521) report the extraction of starch from the grinding of wolf fruit pulp in the presence of sodium metabisulfite solution to prevent starch browning. However, metabisulfite and its sodium or potassium salts, as well as other sulfites derived or not, present acute toxicity category 4, cause serious eye injuries of category 1 and, when in contact with acids, release toxic gases. According to Resolution - RDC No. 8, of March 6, 2013, from the National Health Surveillance Agency, the tolerance limit for the presence of residual sulfites in foods of plant origin varies from 0.005 g to 0.03 g per 100 g or 100 mL.Another problem associated with the use of sulfites in general, for example, metabisulfite, is the final disposal of waste containing these compounds, since they are potent inhibitors of microorganism growth, which makes their disposal, for example, in biological treatment lagoons or deposition in soils, unfeasible.

[0013] SUMMARY OF THE INVENTION

[0014] The present invention aims at the complete utilization of lobeira fruits and the obtaining of their components from an integrated processing without the generation of toxic waste.

[0015] In one aspect of the present invention, an inhibitory agent for fruit browning enzymes is provided. In addition to other compounds, phenolic compounds and peroxidase enzymes are present in the lobeira fruit and, together, confer a chemical defense mechanism to the fruit, such as, for example, the rapid browning of the fruit when subjected to some type of injury. Thus, the processing of said fruits is not trivial, because after cell rupture, contact between the enzyme and the substrate leads to the formation of pigmented polyphenols. Therefore, to preserve the fruit components from interaction with the pigmented phenolic compounds, care is needed, ranging from careful fruit selection to the inhibition of enzyme activity after cell rupture during processing.

[0016] Fruit selection should consider, among other factors, phytosanitary conditions and the stage of maturation. Fruits from trees that have suffered attacks from insects, fungi, or even herbivores respond to this type of stress by inducing the synthesis of a greater number of copies of enzymes from the peroxidase family, including polyphenol oxidases and peroxidases. These enzymes are naturally produced constitutively, but the induction of synthesis in response to abiotic and biotic stresses increases their concentration, so that the browning process intensifies, leading to significant changes in the physicochemical and sensory parameters of the fruits.

[0017] Similarly, as the fruits ripen, there is an accumulation of phenolic compounds responsible for aroma and flavor, as well as an increase in the expression of enzymes responsible for the synthesis of these compounds. Furthermore, a change in texture occurs due to a reduction in cell wall thickness caused by enzymes such as lignin peroxidase.

[0018] Therefore, in order for the processing of lobeira fruits to occur without the undesirable appearance of pigmented compounds, a combination of factors is necessary, involving the selection of fruits from trees cultivated in an environment where abiotic and biotic stress agents are controlled, the choice of the ideal stage of maturation - in order to minimize the endogenous load of browning agents - and the use of inhibitors of browning enzymes during the initial stages of processing.

[0019] Another aspect of the present invention aims to provide an integrated processing method using the fruits of the lobeira plant, specifically the species Solanum lycocarpum, Solanum crinitum, or Solanum grandiflorum, where the fruits are fully utilized, from the peel to the seeds.

[0020] In yet another aspect, the present invention aims to provide an integrated process in which the components contained in the fruits of the lobeira plant are continuously extracted, with minimal water input and the generation of a product that is harmless to the environment as a final residue.

[0021] It also consists of an object of the invention, an integrated process from the fruits of the lobeira plant for obtaining a starchy compound.

[0022] In another additional aspect, the present invention aims to provide an integrated and sustainable process for the production of a starch compound, in which the by-products and / or industrial waste generated in the process are non-toxic and do not harm the environment. Furthermore, the by-products and / or industrial waste generated in the process of the present invention can be reused in the generation of other high value-added products with application in a wide range of industries, such as, for example, cosmetics, food, chemicals, agrochemicals, among others.

[0023] Brief Description of the Drawings

[0024] The present invention will now be described by way of illustration only, but not limitation, with reference to the accompanying drawings for better understanding, in which:

[0025] Figure 1 is a flowchart of the integrated process according to the present invention;

[0026] Figure 2 is a block diagram of step A of the integrated process according to the present invention;

[0027] Figure 3 is a block diagram of step B of the integrated process according to the present invention;

[0028] Figure 4 is a block diagram of step C of the integrated process according to the present invention;

[0029] Figure 5 is a block diagram of step D of the integrated process according to the present invention;

[0030] Figure 6 is a block diagram of step E of the integrated process according to the present invention;

[0031] Figure 7 is a block diagram of step F of the integrated process according to the present invention;

[0032] Figure 8 is a graph representing the classification of fruits in relation to the stage of maturation, according to the present invention;

[0033] Figure 9 shows the infrared (FTIR) spectrum profile of the hemicellulosic polymer composition obtained by the integrated process according to the present invention;

[0034] Figure 10 shows the infrared spectrum profile (FTIR) of the glycogalactosidic polymer.

[0035] DETAILED DESCRIPTION OF THE INVENTION

[0036] The present invention provides a comprehensive process using lobeira fruits as raw material, without generating toxic waste. More specifically, said lobeira fruits are used in their entirety to obtain six bioproducts, mainly a starch component, in addition to the following bioproducts: lignocellulosic fiber, phenolic extract, phenol-alkaloid-protein extract, glycogalactosidic polymer, and hemicellulosic polymer.

[0037] According to the present invention, the integrated process comprises six processing steps for obtaining each bioproduct, as well as the reuse of solvents used throughout each step of said process.

[0038] According to the present invention, the terms "a," "an," "the," and "the" include plural references unless the context clearly dictates otherwise.

[0039] The term "bioproduct" refers to any substance of interest obtained from a product of plant origin, such as, for example, whole plant biomass, roots, and fruits.

[0040] The term "raw material" refers to a base element, in its natural or processed state, to serve as a source for the integrated process, according to the present invention.

[0041] The term "byproduct" refers to a substance that is produced and / or isolated during any of the processes described herein, which may have economic and / or environmental value, is non-toxic, and does not harm the environment.

[0042] The six bioproducts generated in this integrated process are:

[0043] (1) Starchy compound or starch or powder;

[0044] (2) Glycogalactosidic composition polymer, also referred to in the present invention as “FGH”;

[0045] (3) Polymer of hemicellulosic composition, also known as “Fibromass”;

[0046] (4) Acidic phenolic extract or phenolic extract, also referred to in the present invention as “Caldo Verde”;

[0047] (5) Cellulose fiber or cellulosic fiber or lignocellulosic fiber, also referred to in the present invention as “Lignocel”;

[0048] (6) Liquid extract of phenol-alkaloid-protein nature, also referred to in the present invention as “Pepox”.

[0049] It should also be noted that the components contained in the lobeira fruits are continuously extracted in the integrated process of the present invention, with a minimum input of water, in which, in addition to the generation of the 6 bioproducts, there is also the generation of a product that is harmless to the environment as a final residue.

[0050] Although attempts have been made to be precise, the numerical values ​​and ranges described herein should be considered approximations unless the context indicates otherwise. These values ​​and ranges may vary from their stated numbers depending on the desired properties sought by this description, as well as variations resulting from the standard deviation found in the measurement techniques. Furthermore, the ranges described herein are intended and specifically contemplated to include all sub-ranges and values ​​within the indicated ranges. For example, a range of 10 to 50 is intended to include all values ​​within the range, including sub-intervals such as 10 to 40, 15 to 45, etc.

[0051] Any two numbers of the same property or parameter reported in embodiments of the present invention may define a range. These numbers may be rounded to the nearest thousandth, hundredth, whole number, ten, one hundred, or thousand to define the range.

[0052] As used herein, the term “and / or” when used in a list of two or more items means that any of the listed items may be used alone or any combination of two or more of the listed items may be used. For example, if a separation method is described as being able to be A, B and / or C, said method may be only A; B alone; C alone; A and B in combination; A and C in combination; B and C in combination; or A, B and C in combination.

[0053] In the manner used here, the terms “understanding,” “understands,” and “understand” are open transitional terms used to transition from a subject recited before the term to one or more elements mentioned after the term, where the element(s) listed after the transitional term are not necessarily the only elements that make up the subject. Similarly, the terms “includes,” “include,” and “including” have the same open meaning as “understanding,” “understands,” and “understand.”

[0054] According to the present invention, the fruits used in said integrated process are of the species Solanum lycocarpum, or Solanum crinitum, or Solanum grandiflorum.

[0055] In one embodiment of the present invention, said fruits have a diameter in the range of 4 to 11 centimeters. More preferably, the fruits have a diameter in the range of 6 to 11 cm. Even more preferably, the fruits have a diameter of 8 cm.

[0056] According to the present invention, the integrated process using lobeira fruit comprises the following steps:

[0057] • Stage A comprising:

[0058] (i) select and sanitize the fruits in a tank (2); (ii) peel the fruits by mechanical means (3) in the presence of a solution comprising organic acid and / or inorganic acid; wherein at the end of step A are obtained: the peeled fruits and a suspension of peel fragments in acidic solution;

[0059] • Stage B comprising:

[0060] (iii) separate the liquid fraction (fl) present in said suspension of shell fragments from the particulate material by means of a separation means (20);

[0061] (iv) transfer the liquid fraction (fl) to a tank (4) and adjust the hydronium ion concentration so that it is maintained between 2.1 x 10' 6 and 7.9 x 10' 4 moles per gram of fruit;

[0062] (v) repeat processes (iii) and (iv) until at the end of about 9 to about 15 peeling cycles of step A, said liquid fraction (fl) is sent to a separation medium (5) to obtain the acidic phenolic extract, which then goes to packaging;

[0063] (vi) direct the solid fraction (fs) obtained in (iii) to the drying medium (6) and packaging;

[0064] • Stage C comprising:

[0065] (vii) remove residues from fruit peels by spraying said acidic phenolic extract;

[0066] (viii) crushing the fruit in a mechanical means (17) in the presence of a solution containing organic acid, inorganic acid and / or combinations thereof; wherein the ratio of peeled fruit to acid is 1:2 (w / v);

[0067] (ix) transfer the crushed mass to a separation medium (18) and obtain two fractions, said fractions being liquid (Cliq) and solid (Csol);

[0068] • Stage D comprising:

[0069] (x) transfer the liquid fraction (Cliq), obtained in (ix), to a centrifuge (19); wherein the supernatant is sent for packaging; wherein said precipitate goes through a sequence of alternating washing (7) and centrifugation (8) operations until neutralization is achieved, wherein the first two wash waters are directed to the treatment of the solid fraction (Csol) in step E; wherein the remaining waters obtained in the washing process are directed to tank (2) of step A; wherein said precipitate is sent to an air dryer (9) until it reaches a moisture content of less than 13% for subsequent packaging;

[0070] • Stage E, including:

[0071] (xi) homogenize in a reactor (10) the solid fraction (Csol), obtained in (ix), with the wash water obtained in step D; wherein the proportion of Csol to wash water is 1:3 to 1:50 (w / v);

[0072] (xii) adjust the reaction mixture so that the hydronium ion concentration is maintained between 2.0 x10' 6 and 2.0 x10 -4 moles per gram of Csol, through the addition of a solution comprising organic acid, inorganic acid and / or combinations thereof;

[0073] (xiii) heat the reaction mixture between 40 °C and 95 °C for 30 to 90 minutes;

[0074] (xiv) separate the reaction mixture obtained in said step E in a separation medium (15);

[0075] (xv) obtaining a supernatant (Eliq) and a precipitate (Eppt); wherein said precipitate (Eppt) is dried under an air stream (11) and subsequently packaged; wherein said supernatant (Eliq) is sent to a cooling tank (12);

[0076] • Stage F comprising:

[0077] (xvi) cool the supernatant (Eliq);

[0078] (xvii) react the supernatant (Eliq) with C2-5 alcohol;

[0079] (xviii) separate the reaction material in a separation medium (16), obtaining a particulate material in the reaction medium (Fpmr) and a liquid fraction;

[0080] (xix) drying in a medium under air flow (13) said particulate material in the reaction medium (Fpmr);

[0081] (xx) distill the remaining liquid in the reactor into a medium (14), in which the C2-5 alcohol is recovered and redirected to the tank (12).

[0082] According to the present invention, the sanitization step further comprises a chemical agent, a physical agent, or combinations thereof. Suitable chemical agents are at least one compound selected from the group consisting of sodium hypochlorite, hydrogen peroxide, ozone gas, acetic acid, peracetic acid, chlorine gas, perchloric acid, hypochlorous acid, or hydrochloric acid. In one embodiment, the concentration of the chemical agent varies from 0.2% to 70% by volume per gram of fruit, depending on the chemical agent to be used. In a preferred embodiment, the chemical agent is ozone gas at a flow rate of 300 L / ha to 2000 L / h for 30 to 240 min, preferably at a flow rate of 900 L / h for 90 min.

[0083] Suitable physical agents are selected from the group consisting of ozonation, electrolysis with or without chlorine gas bubbling, UV-C radiation (180-280 nm), UV radiation (4-400 nm) or gamma radiation.

[0084] Suitable organic acids used in steps A, B, and E, according to the present invention, are selected from the group consisting of lactic acid, pyruvic acid, acetic acid, oxalic acid, citric acid, aconitic acid, succinic acid, fumaric acid, malic acid, malonic acid, ascorbic acid, erythorbic acid, phthalic acid, salicylic acid, acetylsalicylic acid, benzoic acid, cinnamic acid, ferulic acid, coumaric acid, gallic acid, pelagic acid, or their derivatives. In a preferred embodiment, the organic acid used in steps A and B is selected from citric acid, acetic acid, ascorbic acid, or lactic acid.

[0085] In one embodiment, the organic acid concentration in step A is 0.0040% to 0.020% mol, preferably 0.0042% to 0.013% mol.

[0086] Suitable inorganic acids used in steps A, B, and E, according to the present invention, are selected from the group consisting of chloric acid, hydrochloric acid, chlorous acid, hypochlorous acid, perchloric acid, phosphoric acid, phosphorous acid, polyphosphoric acid, pyrophosphoric acid, nitric acid, nitrous acid, mixtures thereof, or mixtures with their sodium salt derivatives or their potassium salt derivatives. Preferably, the inorganic acid used in steps A and B is phosphoric acid or nitric acid.

[0087] In one embodiment, the concentration of inorganic acid in step A is 0.005% to 0.5% mol, preferably 0.005% to 0.01% mol.

[0088] In a preferred embodiment in processing (ii) of step A, the hydronium ion concentration is maintained in the range of 2.1 x10 -6 a 1.6 x 10 -3 moles of hydronium ions per gram of fruit, preferably in the range of 3.2 x 10⁻¹⁵ 6 7.9 x 10 4moles of hydronium ions per gram of fruit.

[0089] In another preferred embodiment in processing (ii) of step A, the mole percentage of organic acid is in the range between 0.042% and 0.013%, where the hydronium ion concentration is in the range of 2.1x10⁻¹⁵ 6 5.3x10' 4 moles of hydronium ions per gram of fruit, preferably 6.7 x 10⁻¹⁰ 5 moles of hydronium ions per gram of fruit.

[0090] In another preferred embodiment in processing (ii) of step A, the mole percentage of inorganic acid is in the range between 0.005% and 0.01 mol%, wherein the hydronium ion concentration is maintained between 6.3 x 10⁻⁶ 6 a 1.6 x 10' 3 moles of hydronium ions per gram of fruit, preferably between 3.2 x 10 6 and 7.9 x 10' 4 moles of hydronium ions per gram of fruit.

[0091] In another preferred embodiment in processing (ii) of step A, the hydronium ion concentration is maintained between 6.3 x 10'6 a 1.6 x 10' 3 moles per gram of fruit, preferably between 3.2 x 10 6 7.9 x 10 4 moles per gram of fruit.

[0092] Suitable organic acids used in step C, according to the present invention, are those with antioxidant or copper-chelating action, selected from the group consisting of citric acid, acetic acid and its derivatives monochloroacetic acid, dichloroacetic acid, trichloroacetic acid, ascorbic acid, lactic acid, benzoic acid, pyruvic acid, aconitic acid, succinic acid, fumaric acid, malic acid, malonic acid, erythorbic acid, phthalic acid, salicylic acid, acetylsalicylic acid, cinnamic acid, ferulic acid, coumaric acid or pelagic acid. In a preferred embodiment, the organic acid used in step C is selected from coumaric acid, citric acid, acetic acid, ascorbic acid or lactic acid. In a preferred embodiment, said organic acid is in a range between 0.0042% and 0.013% by mole, preferably the minimum proportion is 8.3 x 10⁻⁶. 5 mole of organic acid per gram of fruit.

[0093] Suitable inorganic acids used in step C, according to the present invention, are selected from the group consisting of phosphoric acid, hydrochloric acid, chloric acid, chlorous acid, hypochlorous acid, perchloric acid, phosphorous acid, polyphosphoric acid, pyrophosphoric acid, nitric acid, nitrous acid, mixtures thereof, or mixtures thereof with their sodium salt derivatives or their potassium salt derivatives. In a preferred embodiment, the inorganic acid used in step C is selected from phosphoric acid, hydrochloric acid, or nitric acid. In a preferred embodiment, said inorganic acid is in a range of 0.005% to 0.01% by mole, preferably in the range of 2 x 10⁻⁵ 4 a 1 x 10' 3 mole of acid per gram of fruit.

[0094] In a preferred embodiment in processing (viii) of step C, the hydronium ion concentration is maintained between 2.1x10 -6 and 1.6 x 10' 3 .

[0095] In another embodiment of the present invention, when the solution in step C is a combination of organic and inorganic acid, one or more inhibitor compounds identified in Table 1 below, as well as their respective concentrations, may be added. TABLE 1 - INHIBITOR COMPOUNDS THAT CAN BE USED IN STEP C WHEN THE SOLUTION IS A MIXTURE OF ORGANIC AND INORGANIC ACIDS, AS WELL AS THEIR RESPECTIVE CONCENTRATIONS

[0096] Preferably, inorganic acids are used in (xii) of step E. In a preferred embodiment, the suitable inorganic acids used in (xii) of step E are selected from the group consisting of nitric acid, phosphoric acid, citric acid or hydrochloric acid.

[0097] Preferably in (xii) of step E, the hydronium ion concentration is 2.0 x 10' 5 moles per gram of Csol.

[0098] Suitable C2-5 alcohols in the present invention are selected from the group consisting of ethanol, propanol, isopropanol, butanol, sec-butanol, 3-methylbutanol, 1-pentanol, 2-methyl-1-butanol, 3-pentanol, 2-pentanol, or 3-methyl-2-butanol. Preferably, the C2-5 alcohol is ethanol.

[0099] In one embodiment according to the present invention, the ratio of supernatant (Eliq) to C2-5 alcohol is 1:1 to 1:6 (v / v).

[0100] In a preferred embodiment, the process of the present invention further comprises resting the reaction mixture obtained in step F (xvii) for a period of time between 2 h and 24 h before proceeding to processing (xviii) of said step F.

[0101] According to the present invention, the mechanical means (3) employed in step A is preferably an industrial type peeler. However, other types of means may be used provided they promote friction or abrasion or exfoliation or scraping or scouring of the shells of the lobeira fruits.

[0102] According to the present invention, preferably the tank (2) of the sanitization process included in step A is a washing tank with swirling agitation.

[0103] Suitable separation media (20, 5, 18, 15, 16) used in steps B, C, E and F, according to the present invention, may be selected from centrifuge, decanter, filter and / or combinations thereof. In a preferred embodiment of the present invention, the separation media (20) used in step B is a filter. In another preferred embodiment of the present invention, the separation media (18) used in step C is a centrifuge and the separation media (16) used in step E is a decanter.

[0104] According to the present invention, the mechanical means (17) of step C is a knife or blade crusher, grinder, crusher and / or combinations thereof, wherein the particle size of the crushed fruit is in the range between 10 and 30 mm.

[0105] In a preferred embodiment of the present invention, the grinding in step C takes place in an environment with restricted oxygen presence.

[0106] In a preferred embodiment of the present invention, the temperature range in step C is between 10 °C and 20 °C. Preferably, said temperature is 20 °C.

[0107] In another preferred embodiment of the present invention, in step E, the temperature range of the homogenization process of the solid fraction (Csol) is between 60 °C and 85 °C.

[0108] Furthermore, in another preferred embodiment according to the present invention, in step E, the ratio of wash water to the solid fraction (Csol) is between 1:3 and 1:50.

[0109] In a preferred embodiment of the present invention, the integrated process comprises the following steps:

[0110] • Stage A comprising:

[0111] (i) select and sanitize the fruits in a tank (2);

[0112] (ii) peeling the fruit by mechanical means (3) in the presence of a solution comprising: o 0.0040% to 0.020% mol of organic acid; and / or o 0.005% to 0.5% mol of inorganic acid; wherein the removal of the peel covering is 80%, preferably 90%; wherein at the end of step A are obtained: the peeled fruit and a suspension of peels in acidic solution;

[0113] • Stage B comprising:

[0114] (iii) separate the liquid fraction (fl), present in the shell fragment suspension, from the particulate material by means of a separation medium (20);

[0115] (iv) transfer the liquid fraction (fl) to a tank (4) and adjust the hydronium ion concentration to maintain it between 2.1 x 10' 6 and 7.9 x 10' 4 moles of hydronium ions per gram of fruit;

[0116] (v) repeat processes (iii) and (iv) until at the end of about 9 to about 15 peeling cycles of step A, said liquid fraction (fl) with adjusted pH is sent to a separation medium (5) to obtain the acidic phenolic extract, which is then sent for packaging;

[0117] (vi) direct the solid fraction (fs) obtained to the drying medium (6) for obtaining and packaging the lignocellulosic fiber;

[0118] • Stage C comprising:

[0119] (vii) remove residues from fruit peels by spraying with the acidic phenolic extract obtained in step B;

[0120] (viii) crushing the fruit in a mechanical means (17) in the presence of a solution containing organic acid, inorganic acid and / or combinations thereof; wherein said organic acid is in a range of 0.0042% to 0.013% by mol; wherein said inorganic acid is in a range of 0.005% to 0.01% by mol; wherein the ratio of peeled fruit to acid is 1:2 (w / v), the temperature being between 10 °C and 50 °C, preferably between 10 °C and 20 °C; wherein the browning content is below 10%;

[0121] (ix) transfer the crushed mass to a separation medium (18) and obtain two fractions, said fractions being liquid (Cliq) and solid (Csol);

[0122] • Stage D comprising:

[0123] (x) transfer the liquid fraction (Cliq) to a centrifuge (19); wherein the supernatant is a liquid extract of phenol-alkaloid-protein nature and is sent for packaging; wherein an asylaceous compound is obtained as a precipitate; wherein said precipitate undergoes a sequence of alternating washing (7) and centrifugation (8) operations until neutralization is achieved; wherein the first two wash waters are directed to the treatment of the solid fraction (Csol) in step E; wherein the remaining waters obtained in the washing process are directed to tank (2) of step A; wherein said neutralized precipitate is sent to an air dryer (9), at a temperature in the range of 25 °C to 50 °C, preferably between 30 °C and 40 °C, until it reaches a moisture content of less than 13% for subsequent packaging;

[0124] • Stage E, including:

[0125] (xi) homogenize, in a reactor (10), the solid fraction (Csol) obtained in step C with the washing water obtained in step D; wherein the proportion of Csol to washing water is 1:3 to 1:50 (w / v), preferably the proportion is 1:6 to 1:10 (w / v);

[0126] (xii) adjust the reaction mixture so that the hydronium ion concentration is maintained between 2.0 x 10 6 and 2.0 x 10' 4 moles per gram of Csol, preferably 2.0 x 10 5 moles of hydronium ions per gram of Csol, through the addition of a solution comprising organic acid, inorganic acid and / or combinations thereof;

[0127] (xiii) heat the reaction mixture to a temperature between 40 °C and 90 °C for a period of time between 30 min and 90 min, while stirring;

[0128] (xiv) separate the reaction mixture obtained in said step E in a separation medium (15);

[0129] (xv) obtaining a supernatant (Eliq) and a hemicellulosic composition polymer as a precipitate (Eppt); wherein said precipitate (Eppt) is dried under an air stream (11) and subsequently packaged; wherein said supernatant (Eliq) is sent to a cooling tank (12);

[0130] • Stage F comprising:

[0131] (xvi) cool the supernatant (Eliq) to a temperature between 4 °C and 25 °C, preferably between 6 °C and 10 °C;

[0132] (xvii) react the supernatant (Eliq) with C2-5 alcohol, in a ratio of 1:1 to 1:6 (v / v), at a temperature between 4 and 25 °C, under stirring, for about 30 min to about 1 h; wherein after (xvii) the reaction mixture is kept at rest for a period of time between 2 h and 24 h, preferably between 2 h and 6 h, preferably 3 h;

[0133] (xviii) separate the reaction material in a separation medium (16), obtaining a particulate material in the reaction medium (Fpmr) and a liquid fraction;

[0134] (xix) drying in a medium (13) said particulate material in the reaction medium (Fpmr), obtaining a polymer of glycogalactosidic composition; and

[0135] (xx) distill the remaining liquid in medium (14), in order to recover the C2-5 alcohol to be reused in the processing of the supernatant (Eliq) in tank (12).

[0136] The present invention will now be described by way of example only, but not limitation, for better understanding.

[0137] Figure 2 shows the diagram of the processes included in step A of the integrated process according to the present invention. Initially, the lobeira fruits are received on a platform coupled to a perforated mechanical conveyor belt (1) so that the fruits can be selected so that they have a diameter between 4 and 11 cm, corresponding to the maturation stage E4 to E9, as shown in the graph in Figure 8. The selected fruits then proceed to the sanitization stage, where they are transferred to a washing tank with agitation by swirling (2), preferably comprising a chemical agent, such as, for example, chlorine gas or ozone, in order to reduce the microbial load present on the fruit peels, at a flow rate of 300 to 2000 L / h for 30 to 240 min, preferably at a flow rate of 900 L / h for 90 min.Alternatively, the water used to wash the fruit can also undergo a process or treatment with a physical agent capable of producing ionizing radiation, such as, for example, UV radiation. Then, the fruit is peeled by mechanical means (3), where it is placed in contact with a solution based on organic and / or inorganic acid, such as, for example, acid solution spraying, so that the hydronium ion concentration is maintained between 2.1 x 10⁻⁵. 6 and 1.6 x 10' 3 moles of hydronium ions per gram of fruit. The fruits are kept in the mechanical medium (3) for a sufficient time to remove at least 80% of the peel covering, preferably 90% of the peel covering. At the end of step A, two by-products are obtained: (i) the peeled fruits and (ii) an acidic suspension comprising the crushed peels.

[0138] Figure 3 shows the processing diagram for step B according to the present invention. The liquid fraction (fl) obtained in step A is separated from the particulate material by means of a separation medium (20). The resulting supernatant is transferred to a tank (4) so ​​that the concentration of hydronium ions is maintained between 2.1 x 10⁻⁶ 6 and 7.9 x 10' 3mol per gram of fruit by adding a sufficient quantity (qsp) of organic acid, inorganic acid, or mixtures thereof. Preferably, the hydronium ion concentration is adjusted with a solution containing a mixture of organic and inorganic acid. Then, the supernatant with the adjusted hydronium ion concentration is directed to be used in the peeling process of step A. This process is repeated so that after about 9 to about 15 peeling cycles, said supernatant is sent to a separation medium (5) to obtain a final product such as an acidic phenolic extract, which is then sent for packaging. The solid fraction (fs) obtained in step B is directed to the drying medium (6) to obtain a lignocellulosic fiber, which is then sent for packaging.

[0139] As can be seen in Figure 4, the peeled fruits are sent via a mechanical conveyor belt (1) under spraying of the liquid extract obtained in step B, to remove the remaining peel residues, to a mechanical medium (17) such as, for example, a crusher, in the presence of a solution containing organic acid, inorganic acid and / or their combinations, in a minimum proportion of 8.3 x 10⁻¹⁰ 5 mole of organic acid per gram of fruit, for example. The grinding process takes place in a temperature range between 10 °C and 50 °C, preferably between 10 °C and 20 °C, more preferably at 20 °C in an oxygen-limited environment, until the ground fruits reach a particle size in the range between 10 and 30 mm. Subsequently, the ground mass is transferred to a separation medium (18) such as, for example, a centrifuge, obtaining two fractions, namely the liquid (Cliq) and solid (Csol) fractions.

[0140] Figure 5 illustrates step D of the integrated process according to the present invention, in which the liquid fraction (Cliq) obtained in the previous step, step C, is transferred to a centrifuge (19), obtaining a starchy compound as a precipitate and a liquid extract of phenol-alkaloid-protein nature as a supernatant, which is sent for packaging. The starchy compound undergoes a sequence of alternating washing operations (7) with water and centrifugations (8) until it is neutralized. In particular, the waters obtained in the first and second washes, called starch water, are directed to the treatment of the solid fraction (Csol) in step E. The remaining washing waters are directed to step A for use in the sanitization of the fruits.The precipitate is sent to an air dryer (9), such as, for example, heated belts or air flow dryer, for drying at a temperature in the range of 25 °C to 50 °C, preferably between 30 °C and 40 °C, obtaining a starchy compound with a moisture content of less than 13%, which is subsequently packaged.

[0141] Figure 6 illustrates step E of the integrated process according to the present invention, where the solid fraction (Csol) obtained in step C is homogenized in a reactor (10) with the washing water obtained in step D, wherein the ratio of Csol to washing water is in the range of 1:3 to 1:50 (w / v), preferably said ratio is in the range of 1:6 to 1:10 (w / v). After complete homogenization, the reaction mixture is adjusted so that the hydronium ion concentration is between 2.0 x 10 -6 and 2.0 x10 -4 moles per gram of Csol, preferably 2.0 x 10 -5moles of hydronium ions per gram of Csol a by adding a solution comprising organic acid, inorganic acid and / or combinations thereof, for example, nitric acid. The reaction mixture is then heated to a temperature between 40 °C and 90 °C, preferably between 60 and 85 °C, for a period between 30 min and 90 min, preferably 30 min, under constant stirring. Afterwards, the mixture is separated in a separation medium (15), such as, for example, a centrifuge, filter or decanter, preferably the separation medium (15) is a decanter, obtaining a supernatant (Eliq) and a hemicellulosic polymer as a precipitate (Eppt), which is dried under an air stream (11) and subsequently packaged.

[0142] Figure 7 illustrates step F of the integrated process according to the present invention, where the supernatant (Eliq), obtained in step E, is sent to a cooling tank (12), so that the temperature reaches the range between 4 °C and 25 °C, preferably between 6 °C and 10 °C. Then, C2-5 alcohol, such as, for example, ethanol, is added in a ratio between 1:1 and 1:6 (v / v), under stirring, and the reaction mixture reacts for a period of time between 30 min and about 1 h, and is then left to stand for a period of time between 2 h and 24 h, preferably between 2 h and 6 h, more preferably for a period of time of 3 h. Subsequently, the reaction material is separated in a separation medium (16), such as, for example, centrifuge, filter, decantation or combinations thereof, obtaining a particulate material in the reaction medium (Fpmr) and a liquid fraction.The said particulate matter in the reaction medium (Fpmr) is dried under an air stream (13) and a glycogalactosidic polymer is obtained. The remaining liquid in the reactor (12) is distilled in a medium (14) in order to recover the C2-5 alcohol, which is redirected to the tank (12) as a purge stream; and the other liquid obtained is a harmless residue, which is then disposed of.

[0143] According to the present invention, the acidic phenolic extract obtained in step B comprises the components listed in Table 2.

[0144] TABLE 2 - COMPONENTS INCLUDED IN THE ACIDIC PHENOLIC EXTRACT

[0145]

[0146] According to the present invention, the lignocellulosic fiber obtained in step B comprises the components listed in Table 3.

[0147] TABLE 3 - COMPONENTS COMPRISING LIGNOCELLULOSIC FIBER

[0148] According to the present invention, the hemicellulosic polymer composition obtained in step E comprises the components listed in Table 4.

[0149] TABLE 4 - COMPONENTS INCLUDED IN THE HEMICELLULOSIC COMPOSITION POLYMER phenol-alkaloid-protein obtained in step C, according to the present invention.

[0150] TABLE 5 - COMPONENTS INCLUDED IN THE LIQUID EXTRACT OF PHENOL NATURE

[0151] ALKALOID-PROTEIN

[0152] Table 6 lists the components in the form of methylated derivatives and the type of linkages between glucose and galactose residues present in the glycogalactosidic polymer composition obtained in step F, according to the present invention, whose determination was performed by gas chromatography coupled to mass spectrometry (GC / MS).

[0153] TABLE 6 - COMPONENTS INCLUDED IN THE GLYCOGALACTOSIDIDE POLYMER

Claims

1. CLAIMS 1. INTEGRATED PROCESS FROM LOBEIRA FRUITS characterized by comprising the following steps: • Stage A comprising: (i) select and sanitize the fruits in a tank (2); (ii) peeling the fruit by mechanical means (3) in the presence of a solution comprising organic acid and / or inorganic acid; wherein at the end of step A are obtained: the peeled fruit and a suspension of peel fragments in acidic solution; • Stage B comprising: (iii) separate the liquid fraction (fl) present in said suspension of shell fragments from the particulate material by means of a separation means (20); (iv) transfer the liquid fraction (fl) to a tank (4) and adjust the hydronium ion concentration so that it is maintained between 2.1 x 10' 6 and 7.9 x 10' 4 moles per gram of fruit; (v) repeat processes (iii) and (iv) until at the end of about 9 to about 15 peeling cycles of step A, said liquid fraction (fl) is sent to a separation medium (5) to obtain the acidic phenolic extract, which then goes to packaging; (vi) direct the solid fraction (fs) obtained in (iii) to the drying medium (6) and packaging; • Stage C comprising: (vii) remove residues from fruit peels by spraying said acidic phenolic extract; (viii) crushing the fruit in a mechanical means (17) in the presence of a solution containing organic acid, inorganic acid and / or combinations thereof; wherein the ratio of peeled fruit to acid is 1:2 (w / v); (ix) transfer the crushed mass to a separation medium (18) and obtain two fractions, said fractions being liquid (Cliq) and solid (Csol); • Stage D comprising: (x) transfer the liquid fraction (Cliq), obtained in (ix), to a centrifuge (19); wherein the supernatant is sent for packaging; wherein said precipitate goes through a sequence of operations alternating washes (7) and centrifugations (8) until neutralization is achieved, wherein the first two wash waters are directed to the treatment of the solid fraction (Csol) in stage E; wherein the remaining waters obtained in the washing process are directed to tank (2) of stage A; wherein said precipitate is sent to an air dryer (9) until it reaches a moisture content of less than 13% for subsequent packaging; • Stage E, including: (xi) homogenize in a reactor (10) the solid fraction (Csol), obtained in (ix), with the wash water obtained in step D; wherein the proportion of Csol to wash water is 1:3 to 1:50 (w / v); (xii) adjust the reaction mixture so that the hydronium ion concentration is maintained between 2.0 x10' 6and 2.0 x10 -4 moles per gram of Csol, through the addition of a solution comprising organic acid, inorganic acid and / or combinations thereof; (xiii) heat the reaction mixture between 40 °C and 95 °C for 30 to 90 minutes; (xiv) separate the reaction mixture obtained in said step E in a separation medium (15); (xv) obtaining a supernatant (Eliq) and a precipitate (Eppt); wherein said precipitate (Eppt) is dried under an air stream (11) and subsequently packaged; wherein said supernatant (Eliq) is sent to a cooling tank (12); • Stage F comprising: (xvi) cool the supernatant (Eliq); (xvii) react the supernatant (Eliq) with C2-5 alcohol; (xviii) separate the reaction material in a separation medium (16), obtaining a particulate material in the reaction medium (Fpmr) and a liquid fraction; (xix) drying in a medium under air flow (13) said particulate material in the reaction medium (Fpmr); (xx) distill the remaining liquid in the reactor into a medium (14), in which the C2-5 alcohol is recovered and redirected to the tank (12).

2. PROCESS, according to claim 1, characterized in that the fruits are of the species Solanum lycocarpum, or Solanum crinitum, or Solanum grandiflorum.

3. PROCESS, according to any one of claims 1 to 2, characterized in that step A comprises a platform coupled to a perforated conveyor belt (1) for sorting the fruit.

4. PROCESS, according to any one of claims 1 to 3, characterized in that the sanitization step further comprises the addition of a chemical agent, a physical agent or combinations thereof, wherein the chemical agent is selected from the group consisting of ozone gas, chlorine gas, sodium hypochlorite, hydrogen peroxide, acetic acid, peracetic acid, hydrochloric acid, perchloric acid, hypochlorous acid; wherein the physical agent is selected from the group consisting of ozonation, electrolysis with or without bubbling of chlorine gas, UV-C radiation (180-280 nm), UV radiation (4-400 nm) or gamma radiation.

5. PROCESS, according to any one of claims 1 to 4, characterized in that the concentration of the chemical agent varies from 0.2% to 70% by volume per gram of fruit.

6. PROCESS, according to any one of claims 1 to 5, characterized in that the chemical agent is ozone gas at a flow rate of 300 L / ha to 2000 L / h for 30 to 240 min, preferably at a flow rate of 900 L / h for 90 min.

7. PROCESS, according to any one of claims 1 to 6, characterized in that the tank (2) employed in step A is a washing tank with swirl agitation.

8. PROCESS, according to any one of claims 1 to 7, characterized in that the organic acid used in steps A, B and E is selected from the group consisting of lactic acid, pyruvic acid, acetic acid, oxalic acid, citric acid, aconitic acid, succinic acid, fumaric acid, malic acid, malonic acid, ascorbic acid, erythorbic acid, phthalic acid, salicylic acid, acetylsalicylic acid, benzoic acid, cinnamic acid, ferulic acid, coumaric acid, gallic acid, pelagic acid, or their derivatives, preferably selected from cinnamic acid, citric acid, acetic acid, ascorbic acid or lactic acid.

9. PROCESS, according to any one of claims 1 to 8, characterized in that the inorganic acid used in steps A, B and E is selected from the group consisting of chloric acid, hydrochloric acid, acid Chlorous acid, hypochlorous acid, perchloric acid, phosphoric acid, phosphorous acid, polyphosphoric acid, pyrophosphoric acid, nitric acid, nitrous acid, mixtures thereof or mixtures with their sodium salt derivatives or their potassium salt derivatives, preferably selected from phosphoric acid or nitric acid.

10. PROCEDURE, in accordance with any of the claims I a 9, characterized in that the concentration of organic acid in step A is from 0.0040% to 0.020% mol, preferably 0.0042% to 0.013% mol; and the concentration of inorganic acid in step A is from 0.005% to 0.5% mol, preferably 0.005% to 0.01% mol.

11. PROCESS, according to any one of claims 1 to 11, characterized in that, in processing (ii) of step A and in step C, the hydronium ion concentration is maintained in the range of 2.1 x 10⁻¹⁵ 6 a 1.6 x 10' 3 moles of hydronium ions per gram of fruit.

12. PROCESS, according to claim 11, characterized in that the concentration of organic acid is maintained at a minimum of 8.3 x 10⁻⁶ 5 moles per gram of fruit.

13. PROCESS, according to any one of claims 1 to 12, characterized in that the solid fraction (fs) obtained in step B comprises the fruit peels.

14. PROCESS, according to any one of claims 1 to 2, characterized in that said fruits have a diameter in the range of 4 to II centimeters, preferably 6 to 11 cm, preferably 8 cm.

15. PROCESS, according to claim 1, characterized in that the mechanical means (3) of step A is a peeler.

16. PROCESS, according to any one of claims 1 to 15, characterized in that in step A, the fruits are held in the mechanical medium (3) for a time sufficient to remove at least 80% of the peel covering, preferably 90% of the peel covering.

17. PROCESS, according to any one of claims 1 to 16, characterized in that in steps B, C, E and F, the separation means (20, 5, 18, 15, 16) is a centrifuge, decanter, filter or combinations thereof.

18. PROCESS, according to any one of claims 1 to 17, characterized in that in step B, the drying medium (6) is an airflow dryer.

19. PROCESS, according to any one of claims 1 to 18, characterized in that in (viii) in step C, the temperature is between 10 °C and 50 °C, preferably between 10 °C and 20 °C; wherein the browning content is below 10%.

20. PROCESS, according to any one of claims 1 to 19, characterized in that in (x) in step D, the drying temperature in the air dryer (9) is in the range of 25 °C to 50 °C, preferably between 30 °C and 40 °C.

21. PROCESS, according to any one of claims 1 to 20, characterized in that in step E, homogenization occurs under agitation.

22. PROCESS, according to any one of claims 1 to 21, characterized in that in (xi) of step E: - the acid must be selected from nitric acid, phosphoric acid, citric acid, or hydrochloric acid; and / or - the ratio of Csol to wash water should be 1:3 to 1:50 (w / v), preferably said ratio is 1:6 to 1:10 (w / v).

23. PROCESS, according to any one of claims 1 to 22, characterized in that in (xii) of step E, the hydronium ion concentration is 2.0 x10 -5 moles per gram of Csol.

24. PROCESS, according to any one of claims 1 to 23, characterized in that it further comprises resting the reaction mixture obtained in step F (xvii) for a period of time between 2 h and 24 h before proceeding to processing (xviii) of said step F.

25. PROCESS, according to any one of claims 1 to 24, characterized in that in (xvi) of step F, the supernatant (Eliq) is cooled to a temperature between 4 °C and 25 °C, preferably between 6 and 10 °C.

26. PROCESS, according to any one of claims 1 to 25, characterized in that in (xvii) of step F, the reaction of the supernatant (Eliq) with C2-5 alcohol occurs at a temperature between 4 °C and 25 °C, under stirring, for 30 min to 1 h.

27. PROCESS, according to any one of claims 1 to 26, characterized in that in (xvii) of step F, the C2-5 alcohol is selected from ethanol, propanol, isopropanol, butanol, sec-butanol, 3-methyl-butanol, 1-pentanol, 2-methyl-1-butanol, 3-pentanol, 2-pentanol, 3-methyl-2-butanol, preferably Alcohol C2-5 is ethanol.

28. PROCESS, according to any one of claims 1 to 27, characterized in that at the end of step F an innocuous residue is still obtained.

29. PROCESS, according to any one of claims 1 to 28, characterized in that the mechanical means (17) of step C is a knife or blade crusher, grinder, crusher or combinations thereof, wherein the particle size of the crushed fruit is in the range between 10 and 30 mm.

30. PROCESS, according to any one of claims 1 to 29, characterized in that when the solution in step C is an organic acid, said organic acid is selected from the group consisting of citric acid, acetic acid, and their derivatives monochloroacetic acid, dichloroacetic acid, trichloroacetic acid, ascorbic acid, lactic acid, benzoic acid, pyruvic acid, aconitic acid, succinic acid, fumaric acid, malic acid, malonic acid, erythorbic acid, phthalic acid, salicylic acid, acetylsalicylic acid, cinnamic acid, ferulic acid, coumaric acid, pelagic acid, preferably coumaric acid, citric acid, acetic acid, ascorbic acid or lactic acid; wherein the said organic acid is in a range between 0.0042% and 0.013% by mole, preferably the minimum proportion is 8.3 x 10 5 mole of organic acid per gram of fruit.

31. PROCESS, according to any one of claims 1 to 30, characterized in that when the solution in step C is an inorganic acid, said inorganic acid is selected from the group consisting of phosphoric acid, hydrochloric acid, chloric acid, chlorous acid, hypochlorous acid, perchloric acid, phosphorous acid, polyphosphoric acid, pyrophosphoric acid, nitric acid, nitrous acid, their mixtures or their mixtures with their sodium salt derivatives or their potassium salt derivatives, preferably phosphoric acid, hydrochloric acid or nitric acid; wherein said inorganic acid is in a range of 0.005% to 0.01% by mol, preferably in the range of 2 x 10⁻⁵ 4 a 1 x 10' 3 mole of acid per gram of fruit.

32. PROCESS, according to any one of claims 1 to 31, characterized in that when the solution in step C is a mixture of organic and inorganic acid, one or more inhibitory compounds selected from p-hydroxybenzyl alcohol, 3',5'-di-C-13-glucopyranosylphloretin, vitexin, baicalein, kushenol A, 7,3',4'-trihydroxyisoflavone, steppogenin, catechin, gliasperin C, (1E,6E)-1,7-bis(4-hydroxy-3-methoxyphenyl)hepta-1,6-diene-3,5-dione, trans-N-coumaroyltyramine, 2,4,2',4',6'-pentahydrochalcone, 4,6,4'- trihydroxyaurone, 3-phenylbenzoic acid, oxyresveratrol, 2-[2-methyl-5-(pronan-2-yl)phenoxyl-2-oxoethyl(2E0-3-(2,4-dihydrocyphenyl)propenoate, tanshinone HA, ((S)-(5-(benzyloxy)-1-octyl-4-oxo-1,4-dihydropyridine-2-yl)methyl 2-aminophenylpropanoate), 2-fluorophenylthiosemicarbazone, pyrosulfite acid and its salts, 5-phenyl-3[5-hydroxy-4-pyron-2-yl-methylmercapto]-4-(2,4-dihydrocyclobenzylamino)-1,2,4-triazole, arjunilic acid, hydroxyacontanoic acid, (+)-Lioniresinol.

33. PROCESS, according to claim 17, characterized in that the separation means (18) of step C is a centrifuge.

34. PROCESS, according to claim 17, characterized in that the separation means (15) of step E is a decanter.

35. PROCESS, according to any one of claims 1 to 34, characterized in that the following bioproducts are obtained: - in stage B (vi), the solid fraction (fs) is lignocellulosic fiber; - In step B, the liquid fraction is an acidic phenolic extract; - in step D (x), a starchy compound is obtained as a precipitate; - In step D, the supernatant is a liquid extract of phenolic-alkaloid-protein nature; - in step E, the precipitate (Eppt) is a hemicellulosic polymer; and - In step F, the particulate matter in the reaction medium (Fpmr) is a polymer of glycogalactosidic composition.

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