The process comprises: dissolving the raw sugar to a raw syrup (sucrose solution) with 65° Brix to 68° Brix, containing amide and dextran; chemically treating the raw syrup with acidulating and neutralizing agents and with flocculating agents, and by injecting air or carbonic gas in the raw syrup, for providing its flotation and production of a clarified syrup; filtering the clarified syrup; regenerating the clarified syrup by making it pass through a column for the immobilization of contaminant enzymes present in the raw syrup, and through ionic cationic and ionic anionic exchange columns disposed downstream and in series with the enzyme immobilization column; and filtering for final polishing of the clarified and regenerated syrup, with the removal of the undesirable residual color, turbidity, odor and flavor.
B01D 15/36 - Adsorption sélective, p. ex. chromatographie caractérisée par le mécanisme de séparation impliquant une interaction ionique, p. ex. échange d'ions, paire d'ions, suppression d'ions ou exclusion d'ions
2.
PROCESS AND EQUIPMENT FOR THE DRY CLEANING OF SUGARCANE HARVESTED IN BILLETS AND CONTAINING STRAW AND OTHER IMPURITIES
The process comprises the steps of: distributing a sugarcane load, with mineral and vegetable impurities, on a conveyor belt (12), forming thereon a sugarcane and impurity mattress; submitting the mattress to a dosing and spreading operation, forming a thin and dispersed curtain in gravitational displacement in a first chamber portion (15); submitting the sugarcane and impurity curtain to a transversal and ascending forced air flow, displacing the impurities outwards from the curtain to the interior of a first collecting compartment (21) and of a second and a third chamber portion (22 and 27); deflecting the fraction of forced air flow, received in the third chamber portion (27), obtusely in a plurality of adjustable "Persian blinds" (28), decompressing the air flow; discharging the clean sugarcane load and the impurities through a clean sugarcane lower outlet (19) and through impurity outlets (21a, 23a and 26a).
A23N 12/00 - Machines à nettoyer, blanchir, sécher, griller ou torréfier les fruits ou les légumes, p. ex. le café, le cacao, les noix
B07B 13/00 - Classement ou triage des matériaux solides par voie sèche non prévu ailleursTriage autrement que par des dispositifs commandés indirectement
3.
PROCESS FOR PRODUCING ETHANOL FROM THE FERMENTATION OF SUGAR SOURCES IN A FERMENTATION MEDIUM WITH HIGH ETHANOL CONTENT
The fermentation process comprises the steps of: (i) preparing a must to feed the fermentation medium containing a high sugar content, containing between 16% to 30% of TRS; (ii) cooling the must to temperatures between 8°C and 30°C; (iii) feeding the yeast cream of Saccharomyces cerevisiae, into the fermenter, so as to maintain a concentration from 5% to 15%; (iv) gradually feeding the cooled must, at increasing flow rates to the fermenter containing the yeast, accompanying the progressive increase of the metabolic activity of the microorganism; (v) starting the cooling process of the fermenter, at the stage in which the temperature of the fermentation system surpasses from 28°C - 30°C; (vi) maintaining the fermentation and must feeding; (vii) maintaining the fermentation until the TRS value is substantially zero; (viii) separating the wine and yeast in a centrifugation system; (ix) re-using the separated yeast in the process; and (x) distilling the centrifuged wine to distillation.
A process is proposed for recovery of water in the sugar cane processing in production mills of sugar and alcohol or only alcohol (ethanol). In the process, the thermal energy available in the exhausted steam from the electric energy generation turbines is transferred to the different mixed juice processing phases, with the reuse of the exhausted steam condensates in the boilers and of the other condensates, after using thermal energy, for imbibition, in the juice extraction phase, for cooling in the process, after passing through cooling towers, for other industrial uses and for possible treatment or use in the irrigation out of the productive system in the mill.
The tanks to be formed comprise cylindrical rings (1) with the lower edge (1a) seated and welded onto the upper edge (1b) of the ring immediately below. Each jack (M) comprises: a base (10) to be seated onto a bearing surface; a vertical column (20) attached on the base (10); a driving device (DA) mounted in the base (10) or in the vertical column (20); a head (30) operatively associated with the driving device (DA) so as to be vertically displaced thereby, between lowered and elevated positions spaced from each other by the height of the metal sheet strip (2) which forms the cylindrical rings (1); and a train of guide rollers (40), which are pivotedly mounted in the head (30), side-by-side and according to a horizontal alignment in circle arc with the radius of the tank (T) to be formed.
UNIVERSIDADE ESTADUAL DE CAMPINAS - UNICAMP (Brésil)
DEDINI S.A. INDÚSTRIAS DE BASE (Brésil)
Inventeur(s)
Andrietta, Silvio Roberto
Andrietta, Maria De Graça Stupiello
Abrégé
'Process of fermentation for production of bioethanol', it refers to a process of alcoholic fermentation that uses strains of flocculant yeasts, in bioreactor of fixed tower kind, expanded bed or fluidized, with an unit of regeneration of biocatalytic coupled, using vegetable products that contain saccharose, glucose and fructose as raw material; the developed process is applied in the unit of fermentation of sugary materials containing saccharose, glucose and fructose, coming from vegetable sources of direct way or after hydrolysis, in the industries of production of alcoholic drunk, fuel alcohol, industrial alcohol and anhydrous alcohol; such process comprehends the following stages: 1) Preparation of the must, 2) Alimentation of the bioreactor, 3) Process of conversion, 4) Degassing of the fermented material, 5) Recovery of the biocatalytic, 6) Treatment of the biocatalytic, 7) Return of the biocatalytic to fermenter, and 8) Recovery of ethanol.
A process is proposed for recovery of water in the sugar cane processing in production mills of sugar and alcohol or only alcohol (ethanol). In the process, the thermal energy available in the exhausted steam from the electric energy generation turbines is transferred to the different mixed juice processing phases, with the reuse of the exhausted steam condensates in the boilers and of the other condensates, after using thermal energy, for imbibition, in the juice extraction phase, for cooling in the process, after passing through cooling towers, for other industrial uses and for possible treatment or use in the irrigation out of the productive system in the mill.
C13B 25/06 - Évaporateurs ou bassins de cuisson spécialement adaptés aux jus sucrésÉvaporation ou ébullition des jus sucrés combinés à des instruments de mesure pour la surveillance de l'opération
C12P 7/06 - Éthanol en tant que produit chimique et non en tant que boisson alcoolique
C13B 10/12 - Détails des appareils d'extraction, p. ex. agencement des conduits et des robinets
C13B 25/02 - Détails, p. ex. pour empêcher la formation d'écume ou pour la prise de jus
8.
PROCESS FOR PRODUCING AN ORGANO-MINERAL FERTILIZER
The invention relates to a process for producing an organo-mineral fertilizer from vinasse, filter cake and generally boiler ashes, as byproducts of the sugar and/or alcohol manufacture and, optionally, complemented with fertilizer sources composed of macronutrients (primary and secondary) and micronutrients. The process comprises, in a preferred form of the invention, the steps of : concentrating the vinasse until about 65% of solids (p/p); mixing and dissolving the fertilizer elements in the concentrated vinasse; mixing and drying the filter cake and ashes in a hot gas stream obtained by burning bagasse or fine straw; impregnating this dry mixture with the concentrated vinasse mixture and the added fertilizer agents; and, finally, drying and granulating the final formulated mixture. The end product is a granular solid containing N, P, K, Ca, S, Mg and micronutrients, according to the previously programmed formulation. In the other form of the invention, the same process is effected, but without adding the fertilizer elements.
A process is proposed for crystallizing, by progressively cooling, in multiple stages arranged in series in a crystallization vessel (10), a descending continuous flow of a saturated sucrose solution at a temperature from about 78° to about 120°C, each stage maintaining the sucrose solution being crystallized at a predetermined temperature, until reaching a temperature from about 25 to 40°C, obtaining substantially pure sucrose crystals. A suspension containing sugar seeds is introduced in the crystallizing equipment, in the first stage, jointly with the saturated sucrose solution of 1.05-1.15. In another embodiment of the invention, the saturated solution is fed and its temperature is controlled, already in the first stage of the vessel (10), to obtain a supersaturation between 1.05 and 1.15, inducing the formation of small crystals used as crystallization seeds.
The present invention relates to a pressure swing adsorption process, also known as PSA process, which is modified with a view to utilizing the heat from the post-adsorption stream coming from the molecular sieves to heat/vaporize the pre-adsorption stream containing the hydrated product or the mixture component(s) to be adsorbed in said sieves. The present invention provides alternative arrangements for the heat exchanger system in order to use the thermal potential of the post- adsorption stream with the elimination or minimization of the risk of a slug flow regime in the exchangers, the so-called 'gush,' which would be a natural result from the periodic oscillation characteristic of PSA processes. With this, the vapor consumption with the modified process according to the present invention is considerably reduced.
The present invention relates to a process and a system for producing alcohol by distillation with energy optimization using split-feed technology. The process of the present invention comprises the steps of: a) splitting a stream of wine (1) to feed two depuration columns (2, 3), the depuration column (2) generating a stream of phlegma (4) and the depuration column (3) generating a stream of phlegma (5) and a stream of vinasse (6); b) feeding the stream of phlegma (4) into at least one rectification column (7) generating a top flow (8) and a stream of hydrated alcohol (9); c) effecting the heat exchange between the top flow (8) from at least one rectification column (7) and the stream of vinasse (6) from the depuration column (3) in at least one heat exchanger (10); and d) feeding the stream of phlegma (5) into a rectification column (11 ) generating a stream of hydrated alcohol (12). The present invention further relates to hydrated alcohol produced by the process described above and to a process for producing anhydrous alcohol.
Improvements in a process for rapid acid hydrolysis of lignocellulosic material and in a hydrolysis reactor, said lignocellulosic material being fed in different levels of a reactor (10) and contacted with flows of lignin organic solvent, water and an extremely dilute solution of a strong inorganic acid, for obtaining a liquid phase of hydrolysis extract and a solid phase of non-reacted and non-dissolved material. A controlled steam flow is injected into the different levels of the reactor (10), so as to provide adequate temperatures of organic solvent and strong inorganic acid and forming the desired products (sugars). A flow of the liquid phase is recirculated in different levels of the reactor (10), the remainder thereof being withdrawn from the reactor (10), abruptly cooled with the solvent submitted to evaporation to obtain a concentrate. The lignin is transferred by decantation and the concentrate is transferred to subsequent process steps.
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