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WO2022000060A1 - Procéprocédé continu de purification de xylitol biotechnologique - Google Patents

Procéprocédé continu de purification de xylitol biotechnologique Download PDF

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Publication number
WO2022000060A1
WO2022000060A1 PCT/BR2021/050281 BR2021050281W WO2022000060A1 WO 2022000060 A1 WO2022000060 A1 WO 2022000060A1 BR 2021050281 W BR2021050281 W BR 2021050281W WO 2022000060 A1 WO2022000060 A1 WO 2022000060A1
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xylitol
purification
hydrolyzate
bagasse
temperature
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Portuguese (pt)
Inventor
Marcus BRUNO SOARES FORTE
Bernardo SOARES CARDOSO
Yara PEREIRA CERCEAU ALVES
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Universidade Estadual de Campinas UNICAMP
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Universidade Estadual de Campinas UNICAMP
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/09—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis
    • 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
    • A23L27/30—Artificial sweetening agents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/18—Polyhydroxylic acyclic alcohols
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P7/00—Preparation of oxygen-containing organic compounds
    • C12P7/02—Preparation of oxygen-containing organic compounds containing a hydroxy group
    • C12P7/04—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic
    • C12P7/18—Preparation of oxygen-containing organic compounds containing a hydroxy group acyclic polyhydric
    • 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
    • A23L27/30—Artificial sweetening agents
    • A23L27/33—Artificial sweetening agents containing sugars or derivatives
    • A23L27/34—Sugar alcohols
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/09—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis
    • C07C29/095—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of esters of organic acids

Definitions

  • the present invention is a continuous process of purification of biotechnological xylitol produced by fermentation.
  • the present invention is part of the field of industrial biotechnology, more precisely in the section of production processes and purification of biotechnological xylitol.
  • Xylitol being a sweetener, has applications in foods, such as chewing gum, candies, chocolates, ice cream, gelatins and various beverages, as well as pharmaceuticals and oral hygiene and personal care products.
  • Xylitol being a five-carbon polyol (pentitol)
  • pentitol has a high sweetening power, despite having a 40% lower caloric content when compared to sucrose. Its use is related to the beneficial effects on health, such as helping to combat the formation of caries, reducing the occurrence of acute otitis media in children, participation in the fight against obesity and diabetes, reduction of gingivitis and halitosis control.
  • xylitol is mainly produced by chemical reactions.
  • pure xylose is catalytically reduced under high pressures and temperatures using expensive catalysts, usually nickel-based. Due to the operating conditions, the need for xylose purification steps and the high cost of the catalysts, the process is quite expensive. In this way, xylitol ends up becoming an expensive additive.
  • An alternative is to produce xylitol through a biochemical route using lignocellulosic biomass as agro-industrial residues from sugarcane bagasse.
  • the production of biotechnological xylitol is oriented towards obtaining hemicellulosic hydrolysates from the initial lignocellulosic raw material, its fermentation and metabolic bioconversion.
  • This alternative form of production fits into sustainable development, as it can use agro-industrial residues and can have a cheaper price when compared to the current form of production, if its technology is fully developed.
  • the proposed solution presents an alternative for the purification of biotechnological xylitol obtained from hemicellulosic hydrolyzate from lignocellulosic biomass.
  • the document BRPI0903273 entitled “BIOTECHNOLOGICAL PRODUCTION OF XYLITOL FROM ORGANIC SUGAR CANE BAGASSE” refers to a method of producing xylitol through the use of a xylose-containing hydrolyzate from sugarcane bagasse organic.
  • the methodology involves the process of acid hydrolysis (0.2-5.0%), purification of the hydrolyzate, fermentation to produce xylitol, purification of xylitol and crystallization.
  • the document reveals that the purification of biotechnologically produced xylitol occurs using anion and cationic exchange resins in columns, with three anionic and one cationic resins, and also reveals that the resins can be replaced by activated carbon. However, the document does not disclose the process of using activated carbon in fixed bed columns, according to the present invention.
  • the multiphase biotechnological xylitol purification process is analyzed, including adsorption on activated carbon, use of three ion exchange resins, vacuum concentration and crystallization.
  • the adsorption step on activated carbon which is the closest to the present invention, is carried out in batches, in which 1 to 5 g are added to 100 mL of broth containing xylitol.
  • the present invention uses a continuous process, in a fixed bed column, with procedural characteristics that are far from the state of the art of this document, since a batch process has different parameters from a continuous process.
  • the present invention is a continuous process of purification of biotechnological xylitol produced by fermentation.
  • the continuous process of purification of biotechnological xylitol comprises the following steps: a) Hydrolysis of sugarcane bagasse at room temperature (25°C) until reaching a humidity of 5 to 15% (m/m), preferably 10% (w/w); b) Pre-treatment of dried bagasse with dilute sulfuric acid, with a bagasse/liquid ratio of 5 to 20%, preferably 10% by mass in the proportion of 10 to 300 mg H 2 SO 4 /g of bagasse, preferably 100 mg H 2 SO 4 /g of bagasse, and temperature from 80 to 200°C, preferably 121°C for a period of 5 to 60 min, preferably 20 min; c)Filtering the hydrolyzate obtained on filter paper at room temperature; d) Storage of the liquid source at 4°C; e) Concentration of the hydrolyzate obtained in (d) preferably by vacuum evaporator, at a temperature of 40 to 90°C, preferably 70°C, increasing the xylose concentration from 2 to 10 times,
  • the flow rate varies (v s) from 0.8 to 1.5 cm/min, preferably from 0.64 to 1.2 mL/min, the temperature (T) varies from 40 to 70°C and the injection volume (V i) varies from 0.14 to 3.0 mL or from 12 to 25% of the empty column volume;
  • the flow is from 1.2 to 1.5 cm/min and the temperature is 70°C; and i) obtaining fractions rich in xylitol, with recovery of 70 to 83% of the injected xylitol and purity of 93.4 to 100.0% in relation to proteins (major contaminant identified in the fermentation broth).
  • Figure 1 graphically illustrates the continuous purification process in fixed bed columns of activated carbon using the pulse chromatographic mode of operation (feeding a specific volume), in which the concentrations of xylitol, xylose, arabinose, glycerol are presented and ethanol at the exit of the 3-run purification process.
  • Figure 2 graphically illustrates the continuous process of biotechnological xylitol purification in activated carbon fixed bed columns using the operation mode called step (continuous feeding), in which the relative concentrations of xylitol and contaminants are presented.
  • step continuous feeding
  • the relative concentration (C/C0) referring to the ratio between the concentration in the fraction collected after the purification and concentration in the initial sample.
  • Relative absorbance refers to the ratio between the absorbance in the fraction collected after purification and the absorbance in the initial sample.
  • the present invention is a continuous process of purification of biotechnological xylitol produced by fermentation.
  • the continuous process of purification of biotechnological xylitol comprises the following steps: j) Hydrolysis of sugarcane bagasse at room temperature (25°C) until reaching a humidity of 5 to 15% (m/m), preferably 10% (w/w); k) Pre-treatment of dried bagasse with dilute sulfuric acid, with a bagasse/liquid ratio of 5 to 20%, preferably 10% by mass in the proportion of 10 to 300 mg H 2 SO 4 /g of bagasse, preferably 100 mg H 2 SO 4 /g of bagasse, and temperature from 80 to 200°C, preferably 121°C for a period of 5 to 60 min, preferably 20 min; l) Filtration of the hydrolyzate obtained on filter paper at room temperature; m) Storage of the liquid source at 4°C; n) Concentration of the hydrolyzate obtained in (d) preferably by vacuum evaporator, at a temperature of 40 to 90°C, preferably 70°C, increasing the xylose concentration from 2 to 10 times,
  • the flow rate varies (v s ) from 0.8 to 1.5 cm/min, preferably from 0.64 to 1.2 mL/min, the temperature (T) varies from 40 to 70°C and the injection volume (V i ) varies from 0.14 to 3.0 mL or from 12 to 25% of the empty column volume;
  • the flow is from 1.2 to 1.5 cm/min and the temperature is 70°C; and r) obtaining fractions rich in xylitol, with recovery of 70 to 83% of the injected xylitol and purity of 93.4 to 100.0% in relation to proteins (major contaminant identified in the fermentation broth).
  • the column is filled with activated carbon from coconut husk.
  • Activated carbon comprising a diameter of 0.03 to 1.00 mm or a ratio between particle diameter and bed diameter between 0.3 and 10%, ash content ranging from 1 to 40%, is placed slowly through a funnel. Intense and intermittent vibration is applied to the column so that the adsorbent settles properly and does not form preferential paths.
  • a fixed bed of activated carbon 1 cm in diameter and 15 cm in height is formed in the inside the column, filling it completely.
  • Activated carbons from other sources can be selected from any residual plant material, such as stems, leaves and biomass and provided the plant material is dehydrated, followed by carbonization and activation.
  • step feeding the broth is continuously fed into the column with a controlled flow rate (v s) and temperature (T) until saturation of the column occurs.
  • the broth containing xylitol is fed into a column with a flow rate (expressed in terms of surface velocity) controlled by a peristaltic pump and temperature controlled in the column jacket by a thermostatic bath.
  • a flow rate expressed in terms of surface velocity
  • the flow varies (v s ) from 0.8 to 1.5 cm/min (or from 0.64 to 1.2 mL/min)
  • the temperature (T) varies from 40 to 70°C
  • the injection volume (Vi ) ranges from 0.14 to 3.0 mL (or from 12 to 25% of the empty column volume).
  • the flow rate is 1.5 cm/min (or 1.2 mL/min) and the temperature is 70°C.
  • the fermented broth passes through the activated carbon bed and at the exit of the system is collected by a fraction collector and the fractions collected have from 0.5 to 10 ml, preferably 5 ml, or from 1 to 100% of the liquid volume of the column.
  • biotech xylitol to be purified it needs to be produced by fermenting the strain of the microorganism using the hemicellulose hydrolyzate as the substrate medium.
  • the hydrolyzate is obtained from the hydrolysis of sugarcane bagasse.
  • the obtaining of the complex broth containing xylitol obtained by fermentation occurs so that the biotechnological xylitol is purified. Thus, it needs to be produced by fermenting the strain of the microorganism using the hemicellulose hydrolyzate as the substrate medium.
  • the hydrolyzate is obtained from the hydrolysis of sugarcane bagasse.
  • the bagasse is dried in the open air until it reaches about 10% (m/m) humidity. Then, the dried bagasse is subjected to a pre-treatment with diluted sulfuric acid, in the proportion of 100 mg H 2 SO 4 /g of bagasse, and temperature of 121°C for 20 min.
  • the hydrolyzate obtained is filtered and the liquid source resulting from the process is stored at 4°C.
  • the hydrolyzate obtained is concentrated in a vacuum evaporator with a volume capacity of 32 L, at 70°C, raising the xylose concentration from 15 g/L to 45 g/L, corresponding to a concentration factor equal to 3.
  • the hydrolyzate obtained after pre-treatment and concentrate goes through the detoxification process.
  • the detoxification of the hydrolyzate is initiated with the liming technique, which consists of two phases; at first, the pH of the hydrolyzate is raised from 0.8 to 7.0 with 12 M sodium hydroxide, then centrifuged at 3000 rpm/15 min and vacuum filtered through common filter paper; in a second moment the pH is reduced to 5.5 by the addition of phosphoric acid (analytical grade), being centrifuged again and filtered. With the change in pH, there is the removal of insoluble compounds, which varies according to the pH of the medium. After liming, active carbon is added to the hydrolyzate at a rate of 2.5% (m/v), maintained at 200 rpm, 30°C for 1 h. At the end of this time, the hydrolyzate is centrifuged and filtered under the same conditions as in the previous detoxification steps.
  • the pH of the hydrolyzate is raised from 0.8 to 7.0 with 12 M sodium hydroxide, then centrifuged at 3000 rpm/15 min and vacuum filtered
  • the obtaining of xylitol by the fermentation of yeast from the hydrolyzate is basically composed by the stages of strain activation, inoculum and fermentation. After fermentation, the complex broth containing the xylitol is purified.
  • the yeast used for biotechnological production of xylitol refers to a strain of Candida tropicalis found naturally in sugarcane bagasse.
  • the strain was isolated from sugarcane bagasse in the municipality of Guararu (SE), provided by LGE/IB/UNICAMP and stored in a culture medium containing 30% glycerol (v/v) at -80°C.
  • Strain activation is performed in a specific culture medium (YEPD) in a petri dish, containing yeast extract (10 g/L), peptone (20 g/L) and dextrose
  • the inoculum consists of a volume (about 10% of the fermentation volume) of culture medium similar in composition to the fermentation medium so that the yeast adapts to the medium and so that the yeast growth is accelerated for the next step. next fermentation.
  • the inoculum medium is not prepared with the hydrolyzate, but in a synthetic medium (to accelerate yeast growth), which is composed of xylose as a carbon source (30 g/L), in addition to peptone (20 g/L). L) and yeast extract (10 g/L) as sources of nitrogen and other nutrients necessary for yeast growth and multiplication.
  • composition of the medium are used stock solutions of 200 g/L for xylose, 200 g/L for peptone and 100 g/L for yeast extract, which were sterilized in an autoclave at 121°C for 15 min.
  • the inoculums are made in Erlenemeyer flasks (125 mL), in a rotating incubator, under agitation of 200 rpm, temperature of 30°C for a time of 48 h. After this period, the yeasts are recovered by centrifugation at 3000 rpm for 5 min, washed with sterile distilled water, centrifuged again under the same conditions and finally resuspended in a small volume of sterile water.
  • the volume necessary for the fermentation process to start with an optical density equivalent to 1.0 is calculated, since it is expected that at this optical density the microorganism is in its exponential growth phase.
  • the fermentations of the hydrolysates are carried out in 1L Erlenmeyer flasks.
  • the hydrolyzate used as a carbon source, is composed of 41 g/L of xylose.
  • the medium is supplemented with yeast extract (10 g/L), potassium monophosphate (KH2PO4, 5 g/L) and magnesium sulfate heptahydrate (MgSCd.7H2O, 0.4 g/L).
  • yeast extract (10 g/L)
  • KH2PO4, 5 g/L potassium monophosphate
  • MgSCd.7H2O magnesium sulfate heptahydrate
  • composition of the fermented broth used for purification by the present invention may vary depending on the lignocellulosic material and the microorganism used, however, it may contain, in addition to xylitol, residual sugars (xylose, arabinose, cellobiose and oligomers), ethanol, arabitol, furfural, acetic acid, phenols, glycerol, uronic acids, proteins and ash. and other components.
  • xylitol from 1.0 to 100.0 g/L, preferably 15.0 g/L, xylose from 0.0 to 20.0 g/L, preferably 1.4 g/L, glucose from 0.0 to 20.0 g/L, preferably 0.0 g/L, arabinose from 0.0 to 20.0 g/L, preferably 3.4 g/L, glycerol from 0.0 to 20 g/L L, preferably 1.7 g/L, acetic acid from 0.0 to 20 g/L, preferably 0.0 g/L, ethanol from 0.0 to 20 g/L, preferably 5.0 g/L, proteins totals from 0.0 to 30.0 g/L, preferably 19.2 g/L, absorbance at 420 nm from 0.1 to 30.0, preferably 15.7 and absorbance at 560 nm from 0.1 to 10, 0, preferably 3.5.
  • the broth containing xylitol is fed into the jacketed column at a constant flow rate of 0.1 to 5.0 cm.
  • System temperature is controlled by the column jacket keeping from 20 to 80°C and kept constant.
  • the product at the outlet of the system is collected by a fraction collector and the fractions collected have from 0.5 to 10 ml, preferably 5 ml or from 1 to 100% of the liquid volume of the column.
  • Fraction analysis [0034] In a first run, the fractions collected are analyzed for color, protein content, total solids content and concentrations of other contaminants in order to identify which fractions have the purest xylitol.
  • concentrations of residual sugars, xylose and glucose, xylitol, ethanol, glycerol and acetic acid are determined by High Performance Liquid Chromatography (HPLC), with Aminex HPX-87H column using 5.0 N sulfuric acid as phase mobile, flow rate of 0.6 mL/min, column temperature of 45°C and injection volume of 20 pL.
  • HPLC High Performance Liquid Chromatography
  • Aminex HPX-87H column using 5.0 N sulfuric acid as phase mobile flow rate of 0.6 mL/min, column temperature of 45°C and injection volume of 20 pL.
  • a calibration curve is constructed for each compound by correlating different known concentrations of said compound (from standard solutions) with the peak areas obtained in the equipment with the injection of the solutions in the respective concentrations.
  • the samples obtained in the experiment are then injected into the equipment using the same conditions and the respective concentrations are determined using the previously constructed calibration curves.
  • the total solids content is determined using an oven at 100°C until constant weight, and then the weight difference between the initial and final sample is calculated. Color was determined by reading the absorbance in a spectrophotometer at wavelengths of 420 nm and 560 nm, as established by the International Commission for the Unification of the Methods of Sugar Analysis (ICUMSA). Reading at 420 nm is used to compare white sugars and light colored products and reading at 560 nm is used to compare darker products. The pH values were determined by potentiometry in a pH meter.
  • the total protein content was determined according to the Lowry method, which is based on the reduction of the Folin-Ciocateau reagent when reacting with proteins, in the presence of a copper (II) catalyst, producing a compound with maximum absorption at 750 nm.
  • Folin-Ciocateau reagent is a mixture containing molybdate, tungstate and phosphoric acid.
  • distilled water was used for the blank.
  • the calibration curve was constructed from standard bovine albumin and both samples and points on the standard curve were analyzed in triplicate.
  • Total purity of a compound in a solution is the ratio between the mass of said compound and the total mass of the solution.
  • Partial purity of a compound with respect to specific contaminants in a solution is the ratio between the mass of said compound and the sum of the masses of specific contaminants in the solution.
  • the purification process can be evaluated through a coefficient called Purification Factor.
  • Purification Factor is the ratio between the purity of the purified samples and the initial and pre-purification purity.
  • FP > 1 means that the sample obtained after purification has higher purity than initially;
  • FP ⁇ 1 means that the sample obtained after purification is of lower purity than initially.
  • the fraction has sufficient xylitol purity when the FP of xylitol in relation to contaminants is greater than 2 for the fraction. This value can be changed in order to select only fractions with more isolated xylitol, or to accommodate fractions containing more contaminants. After this identification, the process can be repeated, but interrupted when the fractions are no longer adequate according to the criterion presented.
  • Another measured response for evaluating the purification process is the Retention Coefficient (CR) of the compounds alone, which represents the mass percentage of said compound retained in the column during the purification process.
  • CR Retention Coefficient
  • the purification process is also evaluated for the xylitol recovery yield (g xylitol ) which represents the mass percentage of injected xylitol that is recovered in the pool (union) of samples after the purification process.
  • g xylitol xylitol recovery yield
  • the first batch of experiments called DCCR was carried out using the pulse feeding method, a number of 17 tests were performed at 5 different temperatures (T) (20, 28, 40, 52 and 60°C), 5 different injection volumes (V i ) (0.80, 1.05, 1.40, 1.75 and 2.00 mL) and 5 different superficial velocities (v s ) (0.40, 0.56, 0 .80, 1.04 and 1.20 cm/min). The results obtained with these tests are shown in Table 1.
  • Table 1 Conditions used, temperature (T), injection volume (V i ) and feed rate in terms of surface velocity (v s ) and responses obtained for the batch of experiments called DCCR using pulse feed.
  • T temperature
  • V i injection volume
  • v s surface velocity
  • FP Retention Coefficient
  • p xylitol xylitol recovery yield
  • p xylitol xylitol mass obtained in the pool of samples obtained after the purification process.
  • the pool of samples refers to the union of samples that individually presented PF
  • Table 2 Pulse feeding. Conditions used, temperature (T), injection volume (V i ) and feed flow in terms of surface velocity (v s ) and responses obtained for the tests (Central Pto, Confl and Conf2).
  • the pool of samples refers to the union of samples that individually presented PF > 2.
  • CR solids solids retention coefficient
  • CR 420 reduction in absorbance read at 420 nm
  • CR 560 absorbance reduction read at 560 nm
  • CR ethanol ethanol retention coefficient
  • FP protein protein purification factor
  • FP solids solids purification factor
  • Table 7 Feeding by step. Concentrations in g/L of xylose, arabinose, xylitol, glycerol, ethanol, total proteins and total solids in the fractions obtained.

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Abstract

La présente invention relève du domaine de la biotechnologie industrielle, notamment du secteur des procédés de production et de purification, et décrit un procédé continu de purification de xylitol produit par fermentation. Le procédé permet la réalisation d'un procédé continu et automatisé, mieux adapté à l'utilisation industrielle et à large échelle, étant donné qu'il peut être associé en série à d'autres étapes, augmentant la productivité et réduisant les pertes.
PCT/BR2021/050281 2020-06-28 2021-06-25 Procéprocédé continu de purification de xylitol biotechnologique Ceased WO2022000060A1 (fr)

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BRPI0412250A (pt) * 2003-07-25 2006-09-19 Cj Corp candida tropicalis cj-fid (kctc 10457bp) e processo de fabricação de xilitol a partir da mesma
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BR102016002700A2 (pt) * 2016-02-05 2019-04-24 Universidade Federal De Minas Gerais Processo para produção de xilitol a partir de hidrolisado hemicelulósico de torta de macaúba (acrocomia aculeata) e co-produtos de cervejaria, e uso

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BRPI0412250A (pt) * 2003-07-25 2006-09-19 Cj Corp candida tropicalis cj-fid (kctc 10457bp) e processo de fabricação de xilitol a partir da mesma
BRPI0401216A (pt) * 2004-04-12 2005-11-22 Unicamp Processo de separação do xilitol por adsorção em colunas de leito fixo de zeólitas
BRPI0903273A2 (pt) * 2009-09-01 2011-05-10 Mario Clovis Garrefa produÇço biotecnolàgica de xilitol a partir do bagaÇo de cana-de-aÇécar orgÂnico
BR102016002700A2 (pt) * 2016-02-05 2019-04-24 Universidade Federal De Minas Gerais Processo para produção de xilitol a partir de hidrolisado hemicelulósico de torta de macaúba (acrocomia aculeata) e co-produtos de cervejaria, e uso

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