EP0357901A2 - Procédé et équipement de défécation différenciée de jus dans deux colonnes échangeuses d'ions chargées de résine - Google Patents

Procédé et équipement de défécation différenciée de jus dans deux colonnes échangeuses d'ions chargées de résine Download PDF

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Publication number
EP0357901A2
EP0357901A2 EP89112093A EP89112093A EP0357901A2 EP 0357901 A2 EP0357901 A2 EP 0357901A2 EP 89112093 A EP89112093 A EP 89112093A EP 89112093 A EP89112093 A EP 89112093A EP 0357901 A2 EP0357901 A2 EP 0357901A2
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EP
European Patent Office
Prior art keywords
juice
column
resin
sugars
columns
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP89112093A
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German (de)
English (en)
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EP0357901A3 (fr
Inventor
Giuseppe Assalini
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ISI INDUSTRIA SACCARIFERA ITALIANA AGROINDUSTRIALE SpA
Original Assignee
ISI INDUSTRIA SACCARIFERA ITALIANA AGROINDUSTRIALE SpA
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Publication date
Application filed by ISI INDUSTRIA SACCARIFERA ITALIANA AGROINDUSTRIALE SpA filed Critical ISI INDUSTRIA SACCARIFERA ITALIANA AGROINDUSTRIALE SpA
Publication of EP0357901A2 publication Critical patent/EP0357901A2/fr
Publication of EP0357901A3 publication Critical patent/EP0357901A3/fr
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
    • C13B35/00—Extraction of sucrose from molasses
    • C13B35/02—Extraction of sucrose from molasses by chemical means
    • C13B35/06—Extraction of sucrose from molasses by chemical means using ion exchange
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
    • C13B20/00—Purification of sugar juices
    • C13B20/14—Purification of sugar juices using ion-exchange materials
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K3/00—Invert sugar; Separation of glucose or fructose from invert sugar

Definitions

  • This invention covers the separation of sacharose from juice impurities (whether non-sugars or sugars other than sacharose) with the aid of resin cation and/or anion exchangers and or the separation of different sugars (such as for instance glucose and fructose) in the mixed solution.
  • Separation takes place through percolation of the juice through these resins based upon two main actions, i.e. ion exclusion and a physical action.
  • Defecation by means of ion exclusion takes advantage of the properties of ion exchanging resins, which, immersed in a polar solvent, will not permit the ions contained in the solution to permeate the resin granules, while the latter will be easily permeated by non-ionic solutions such as non dissociated organic sugars and non-sugars.
  • the physical action is achieved by taking advantage of the resin property differentially to retain the various non-­ionic molecules which are present in the juice flowing through the resin.
  • chromatography utilizes these above described two phenomena at the same time thus purifying the juice at a differentiated velocity at which the various substances in the juice to be defecated pass through the resin packing.
  • the molasses in which most non-sugars will be found will have a low sugar content and will be strongly diluted. If a sufficiently pure juice is to be obtained, such molasses will be difficult to utilize and will have a very low or no commercial value, with an average 3% - 4% content of dry substance and 20% - 30% purity.
  • a further drawback lies in the fact that the single large sized column containing the resin requires a large amount of sparge water which, when recovered and recycled, will dilute the juice to the detriment of the concentration rate, or else water discharge will cause serious pollution problems and involve considerable purifying costs.
  • the first objective is to keep the two actions, i.e. ion exclusion and the physical actions of the resins separated, so that juice defecation will yield a high purity juice and a commercial molasses having an SS ⁇ 10 value and a purity ranging between 45% and 50%.
  • this invention has the aim to reduce the amount of sparge water necessary to eliminate polluting waste, to ensure a uniform flow rate of the juice through the resin, to homogenize the defecation process over the entire column section and, more generally, to cut the cost of the equipment and to reduce the quantity of resin required for purifying.
  • the utilization of two successive columns will permit to differentiate their action.
  • the first column through which the juice flows will provide for an initial but partial defecation.
  • the juice is essentially defecated by ion exclusion and scanty physical action.
  • the juice passes through the second column having an essentially physical purifying action to ensure further separation of non-­sugars and/or of other sugars contained in the juice which will thus have a high purity.
  • the molasses may be mixed with the molasses obtained at the outlet of the first column, or else it may be recycled for preliminary dilution of the entering juice, whereas other sugars and organic substances may be either regenerated and/or recylced.
  • the resin columns are fitted at their upper end with a removable loading or filling chamber featuring numerous juice distributors, whereas the columns are fitted at their lower end with properly perforated trays, the holes of which are vertically matching the distributors.
  • the collecting vessel S receives the juice to be defecated for instance to a re­ finer's syrup having 72% - 75% purity and 80 Bx.
  • Condenser or vacuum pan water may C be added in this vessel to dilute the juice (for instance from 80 to 70 Bx) together with the additives A (fossil meal, etc.).
  • the juice may be added steam heated V to a suitable temperature.
  • the juice is filtered on filter 2 and then reaches the vessel 3 fitted with a heating system for condenser water C.
  • the latter vessel also provides for loading of the first ion exchanging resin column (4).
  • the juice is defecated in the first column (4) prevail­ingly by ion exclusion.
  • the molasses is discharged in a sugar and non-sugar mixture having an SS ⁇ 10 and 45% - 50% purity value.
  • the partially defecated juice leaves the first column with an 83% - 88% purity.
  • the molasses M is collected in vessel 5 and is then con­veyed to the heat exchanger 6 and to the concentration device 7 for hyperfiltering and/or reverse osmosis on membranes.
  • the concentrated molasses MC thus obtained can either directly be utilized for further processing or for further concentration and storage.
  • the permeated water P reaches the vessel 8 and can then be used as sparge water in the columns or for dilution of the juice to be defe­cated, as an alternative or in addition to the condenser water C in tank 9.
  • a small quantity of molasses trickles initially from column 10 to be mixed with the molasses obtained from column 4 or else to be recycled.
  • the defecated limed juice Z is collected in tank 11 and conveyed through a heat exchanger 13, to a hyperfiltering and/or reverse osmosis membrane device 14, from which defecated concentrated juice ZC is obtained .
  • the permeate is collected in tank 8.
  • the above described installation includes the pumps, valves, control and monitoring systems and whatever else is necessary for its completely automatic operation.
  • the molasses M leaves the column after an initial time t′, followed by the high-purity juice Z together with various sugars and non-sugars D.
  • the the low-purity molasses is diluted and therefore not easily marketable.
  • defecation through one single column does not allow for efficient separation between saccharose and other sugars.
  • the molasses M obtained during the initial period t′ has a fair commercial value and it is followed by the juice Z conveyed to the second column.
  • molasses separation occurs after a 't period, whereas the high-purity juice Z is separated between t′ and t ⁇ , followed by various sugars and non-­sugars D which may at least partially regenerated.
  • the optium linear percolation speed of the liquids strained through the resin layers has a well defined value. It follows that the cycle time is univocally determined by this preset velocity and volume of the liquid to be percolated (which, in our case is the juice first and the water later), provided however that the liquid is percolated in one single column.
  • the cycle time will be reduced proportionally to the liquid volume bypassing the first column and directly entering the second column and this in turn will proportionally increase the capacity of the plant (i.e. a greater number of cycles per day).
  • the columns 4 and 10 are fitted with a removable loading device 15, the bottom of which has distributor nozzles with levelled mouthpieces (16) so as to ensure uniform distribution of the liquid on the resins (17).
  • the tank 20 keeps the resins 17 flat on its bottom, preventing local accumulation and differentiated resin thickness.
  • this configuration permits elutration of the resin, thus facilitating the operations while reducing idle time.
  • the smaller grainsized resins are placed at the top where they can keep back most of the suspended impurities.
  • the method and equipment subject matter of this invention offer the following advantages as compared with single column plants: - separation of molasses having a fair commercial value; - separation of a concentrated and high purity juice - separation of various sugars and non-sugars having a high commercial value; - reduced amount of elutration water - integral recycling of soft and permeated water - elimination of pollutants discharged in the sewer system - greater capacity at equal installed resin quantities - perfect and uniform permeation of the resin bed by the percolated liquids ; - hence, considerable cutting of the installation and operating costs .
EP19890112093 1988-09-09 1989-07-03 Procédé et équipement de défécation différenciée de jus dans deux colonnes échangeuses d'ions chargées de résine Withdrawn EP0357901A3 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT8812543A IT1225689B (it) 1988-09-09 1988-09-09 Procedimento ed impianto per la purificazione differenziata in due colonne a resine a scambio ionico di sugo zuccherino
IT1254388 1988-09-09

Publications (2)

Publication Number Publication Date
EP0357901A2 true EP0357901A2 (fr) 1990-03-14
EP0357901A3 EP0357901A3 (fr) 1991-01-09

Family

ID=11141391

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19890112093 Withdrawn EP0357901A3 (fr) 1988-09-09 1989-07-03 Procédé et équipement de défécation différenciée de jus dans deux colonnes échangeuses d'ions chargées de résine

Country Status (4)

Country Link
EP (1) EP0357901A3 (fr)
BR (1) BR8904190A (fr)
DK (1) DK442389A (fr)
IT (1) IT1225689B (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0655507A3 (fr) * 1993-11-12 1996-03-20 Applexion Procédé de fabrication de sucre cristallisé, à partir de jus sucré aqueux tel qu'un jus de canne à sucre ou de betterave sucrière.
WO2003056933A2 (fr) * 2002-01-09 2003-07-17 Oladur Ltd. Procede de production de sucres de soja et produit ainsi obtenu

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2261338A1 (en) * 1974-02-20 1975-09-12 Brandoli Giuseppina Clearing syrups, e.g. molasses, and recovering sugar - by separate treatment with anionic ion-exchanger and cationic ion-exchanger
US4422881A (en) * 1980-10-29 1983-12-27 Roquette Freres Installation and process for the continuous separation of mixtures of sugars and/or of polyols by selective adsorption

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2261338A1 (en) * 1974-02-20 1975-09-12 Brandoli Giuseppina Clearing syrups, e.g. molasses, and recovering sugar - by separate treatment with anionic ion-exchanger and cationic ion-exchanger
US4422881A (en) * 1980-10-29 1983-12-27 Roquette Freres Installation and process for the continuous separation of mixtures of sugars and/or of polyols by selective adsorption

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0655507A3 (fr) * 1993-11-12 1996-03-20 Applexion Procédé de fabrication de sucre cristallisé, à partir de jus sucré aqueux tel qu'un jus de canne à sucre ou de betterave sucrière.
WO2003056933A2 (fr) * 2002-01-09 2003-07-17 Oladur Ltd. Procede de production de sucres de soja et produit ainsi obtenu
WO2003056933A3 (fr) * 2002-01-09 2003-10-23 Oladur Ltd Procede de production de sucres de soja et produit ainsi obtenu
US6913771B2 (en) 2002-01-09 2005-07-05 Oladur, Ltd Process for the production of soybean sugars and the product produced thereof

Also Published As

Publication number Publication date
DK442389D0 (da) 1989-09-07
IT8812543A0 (it) 1988-09-09
BR8904190A (pt) 1990-04-10
DK442389A (da) 1990-03-10
EP0357901A3 (fr) 1991-01-09
IT1225689B (it) 1990-11-22

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