EP0655507B1 - Procédé de fabrication de sucre cristallisé, à partir de jus sucré aqueux tel qu'un jus de canne à sucre ou de betterave sucrière - Google Patents
Procédé de fabrication de sucre cristallisé, à partir de jus sucré aqueux tel qu'un jus de canne à sucre ou de betterave sucrière Download PDFInfo
- Publication number
- EP0655507B1 EP0655507B1 EP94402540A EP94402540A EP0655507B1 EP 0655507 B1 EP0655507 B1 EP 0655507B1 EP 94402540 A EP94402540 A EP 94402540A EP 94402540 A EP94402540 A EP 94402540A EP 0655507 B1 EP0655507 B1 EP 0655507B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- sugar
- juice
- crystallization
- tangential
- process according
- 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.)
- Expired - Lifetime
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Classifications
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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
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- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B20/00—Purification of sugar juices
- C13B20/02—Purification of sugar juices using alkaline earth metal compounds
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- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B20/00—Purification of sugar juices
- C13B20/12—Purification of sugar juices using adsorption agents, e.g. active carbon
- C13B20/123—Inorganic agents, e.g. active carbon
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- 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
- C13B20/144—Purification of sugar juices using ion-exchange materials using only cationic ion-exchange material
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- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B20/00—Purification of sugar juices
- C13B20/16—Purification of sugar juices by physical means, e.g. osmosis or filtration
- C13B20/165—Purification of sugar juices by physical means, e.g. osmosis or filtration using membranes, e.g. osmosis, ultrafiltration
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- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B30/00—Crystallisation; Crystallising apparatus; Separating crystals from mother liquors ; Evaporating or boiling sugar juice
- C13B30/02—Crystallisation; Crystallising apparatus
Definitions
- WO-A-92 08810 relates to a method for increasing the crystallization yield of sugar from a sweet juice. This process is based on the removal of monovalent ions before crystallization. This elimination is carried out by the use of nanofiltration which leads to a permeate which contains a substantial part of the monovalent ions, and to a retentate depleted in monovalent ions, the crystallization being performed on the retentate.
- US-A-4,115,147 has for object a process based on the implementation of tangential filtration membranes for the production of non-centrifugal nutritious sugar.
- the object of the present invention is to remedy the aforementioned drawbacks previously known methods and, to do this, it proposes a method of manufacture of granulated sugar, as defined in the appended claims.
- the process according to the invention By implementing the tangential filtration operation, it is possible to eliminate the colloidal matter present in clarified sweet juice and, to the extent that such materials are dye precursors that develop during crystallization, thus obtaining at the end of the process a crystallized sugar of lower coloring. This is particularly true in the case where the starting aqueous sweet juice is constituted by a juice of the sugar cane juice type, since the process according to the invention then allows obtaining a brown sugar with a coloration of less than 400 ICUMSA units, while conventional methods lead to the production of brown sugar with a coloring of 800 to 4000 ICUMSA units.
- the crystallization operation may be followed by a chromatography operation of said molasses to obtain a first liquid effluent depleted in sugars and a second liquid effluent enriched in sugars; such a chromatography operation fits perfectly into the process according to the invention since the prior microfiltration, ultrafiltration or nanofiltration and tangential softening operations allow substantial elimination of colloidal materials and Ca 2+ ions and / respectively or Mg 2+ usually responsible for the relatively rapid decrease in the separation power of the chromatography.
- micro-, ultra- or nanofiltration operation tangential not only eliminates the colloidal matter present in the starting sweet juice, but also to clarify this juice, i.e. to eliminate suspended matter.
- the implementation of the method according to the invention leads to a significant improvement in the overall balance of the sugar refinery with, moreover in the case where the starting sweet juice is of the sugarcane juice type, a gain in purity of the brown sugar obtained which goes from 98-99.4% (conventional process) 99.7%.
- This improvement is obtained by the implementation of an operation of microfiltration, ultrafiltration or tangential nanofiltration and an operation softening, well known techniques, simple, flexible, high yield, fast, well controlled and low operating cost.
- the implementation of the operation of microfiltration, ultrafiltration or tangential nanofiltration possibly combined with the simple clarification operation advantageously eliminates the aforementioned complex and expensive purification operations.
- the refining used in the process according to the invention for manufacturing white sugar crystallized frees itself from refining and purification operations (carbonation or phosphating) and filtration and this, thanks to the fact that the implementation of operations described above allows obtaining a brown sugar purer, less colored and containing no more colloidal matter in comparison with that obtained by conventional techniques.
- the elimination of refining operations, carbonation or phosphating and filtration is of obvious interest when you know the tedious and expensive character of the crystallization operations of the refining sewer and low product sewers.
- the advantage provided by the process according to the invention of making crystallized white sugar is therefore evident in terms of economic.
- the starting aqueous sweet juice to be treated is a juice obtained by grinding sugar cane, this juice containing sugars and organic and mineral impurities including Ca 2+ and / or Mg 2+ ions.
- this juice can beforehand, although it is not absolutely essential, be subjected to a clarification operation having the aim of eliminating the major part of the solid matters in suspension.
- it is brought by the circulation pump 1 and the conduit 2 to the upper part of a flocculation tank 3, after having been preferably heated to 70-105 ° C, for example by means of an exchanger indirect heat 4.
- this tank 3 it is mixed with vigorous stirring with a flocculating agent stored in the tank 5 and brought from the latter to the upper part of the flocculation tank 3 by a circulation pump 6 and a conduit 7.
- the tank 5 may be provided with heating means (not shown) such as an internal jacket in which a hot fluid circulates, for example hot water or steam; these heating means make it possible to bring the flocculating agent to a temperature of the order of 70 to 80 ° C.
- This agent can in particular be constituted by a slurry of slaked lime, by a cationic surfactant, in particular a compound quaternary ammonium tallow fatty acids, such as dioctadecyldimethylammonium chloride, such as NORANIUM® M2SH marketed by the French company CECA, by derivatives of the deacetylated poly-N-acetylglucosamine chitosan derived from chitin, such as PROFLOC ® 340 from the Norwegian company PROTAN BIOPOLYMER, or by a mixture of these.
- the amount of flocculating agent will usually be 0.2 to 2 g / kg of dry matter of the juice to be treated.
- the flocculation mixture is then extracted from the base of the reservoir 3 and brought by a conduit 8 into a settling tank 9 with a substantially conical base.
- the bottom of the tank 9 can be provided with a duct and an extraction pump bringing the solid deposit collected in the conical part of the tank 9 into a filtration unit (for example rotary filter), the filtrate then being brought back into the tank 9.
- the supernatant liquid (clarified juice having a turbidity of in the order of 15 to 60 NTU / Brix) in the tank 9 is extracted from the latter by a circulation pump 10 discharging into a unit 11 of tangential microfiltration, tangential ultrafiltration or tangential nanofiltration. If necessary, the supernatant thus withdrawn from the tank 9 can be reheated so that the operation in this unit 11 takes place at a temperature of the order of 70 to 99 ° C and preferably from 95 to 99 ° C.
- the membrane used in unit 11 can be of the organic type or of the mineral type (for example of TiO 2 or ZrO 2 ) and have a cut-off threshold corresponding to a molecular weight of at least 1000, good results being obtained with a membrane ultrafiltration having a cutoff threshold corresponding to a molecular weight of 300,000, as well as with a microfiltration membrane having a pore diameter of 0.1 ⁇ m.
- a membrane ultrafiltration having a cutoff threshold corresponding to a molecular weight of 300,000
- a microfiltration membrane having a pore diameter of 0.1 ⁇ m.
- use can be made for example of the KERASEP® membrane available from the French company TECH-SEP or of the FIMTEC® GR 90 PP membrane of the American company DOW.
- the tangential circulation speed of the clarified juice is adapted to the geometry of the micro-, ultra- or nanofiltration module used and may be of the order of 2 to 9 m / s, preferably 6 m / s.
- This circulation speed is regulated by the pump 10, it being specified that a portion of the filtered juice is brought back by a return line 11 a at the suction of said pump 10.
- a cation exchange resin in particular a strong cationic resin, in the Na + and / or K + form
- This column is provided, at its upper part, with a permeate inlet 16 connected to the outlet of the pump 14 and, at its lower part, with a conduit 17 for softened permeate outlet (content of Ca 2+ ions and / or Mg 2+ of the order of 150 to 700 ppm), the Ca 2+ and / or Mg 2+ ions present in the permeate brought to the head of the column (content of Ca 2+ and / or Mg 2+ ions of of the order of 7000 ppm) being retained by the resin during the progression of the permeate through the column by displacing the Na + and / or K + ions of this resin.
- the softened liquid extracted through line 17 then arrives in a reservoir 18 from where it is drawn off by a pump 19 to be brought into a concentration unit 20 which can be for example an evaporator such as a falling-stream evaporator.
- concentration unit 20 can be for example an evaporator such as a falling-stream evaporator.
- the syrup obtained from this unit 20 is then brought by a pump 21 into a crystallization unit 22 where it undergoes several successive crystallizations (three in the example illustrated in Figure 1) to deliver sugar to each stage of crystallization roux and molasses.
- the extraction yield of the sugars from the mass cooked is of the order of 65% at the level of the first crystallization stage, that the degree brown sugar obtained on this first stage is not more than 300 units ICUMSA and that this same sugar has a purity of 99.7%.
- the brown sugar produced on the first crystallization stage is subjected to a recasting operation in the reservoir 24, that is to say when it dissolves in water preferably hot at 80 ° C.
- the resulting syrup is then brought into a column of discoloration 25 filled with an adsorbent material such as animal black, charcoal active or a bleaching resin for example strong anionic resin in the form of chloride, such as IRA® 900 resin from Rohm and Haas).
- an adsorbent material such as animal black, charcoal active or a bleaching resin for example strong anionic resin in the form of chloride, such as IRA® 900 resin from Rohm and Haas.
- the discoloration is preferably carried out hot, for example at 80 ° C.
- the discoloration of the syrup can alternatively be carried out by ultrafiltration or nanofiltration tangential of said syrup.
- the syrup thus discolored is then treated in a crystallization unit 26 to deliver white sugar crystallized in 27 and a crystallization sewer in 28.
- the latter is preferably recycled by mixing it with the syrup from the concentration unit 20; he can also be used for the above-mentioned redesign operation.
- the brown sugar obtained in the second and third stages of crystallization of the crystallization unit 22 can, if desired, be remelted and then brought back to the top of this crystallization unit 22.
- the installation thus described can be completed by a circuit comprising a pump 29, the suction of which communicates by a conduit 30 with the base of the storage tank 23 and the discharge of which communicates by a conduit 31 with the upper part of the column of softening 15.
- This circuit will be implemented when it is desired to regenerate the resin filling the column 15, the molasses stored in the tank 23 serving as regeneration liquid due to its high content of Na + and / or K + ions and its low content of Ca 2+ and / or Mg 2+ ions.
- the installation represented by FIG. 2 is in all points identical to the installation represented by FIG. 1, except that the third crystallization stage of the crystallization unit 22 has been replaced by a chromatography column 32 operating at a temperature of the order of 80 ° C., where the molasses from the second crystallization stage of unit 22 is treated.
- This column is of the type comprising a fixed support constituted by a strong cationic resin, in the Na form + and / or K + , for example the resin DOWEX® C356 from the company DOW or the resin LES® 999301 from the company Rohm and Haas, the elution liquid being water brought into the upper part of the column by a conduit 33.
- This same column 32 is provided at its lower part with a conduit 34 for extracting a first liquid effluent depleted in sugars, enriched with Na and / or K salts and eluted first and with a conduit 35 extraction of a second liquid effluent e enriched in sugars, depleted in Na and / or K salts and eluted second.
- Said first effluent from line 34 is received in a storage tank 36. Due to its high content of Na + and / or K + ions, said first effluent can advantageously be used as regeneration liquid for the softening column 15 and this, in the same way as in the case of the installation of FIG. 1.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- Water Supply & Treatment (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Non-Alcoholic Beverages (AREA)
- Saccharide Compounds (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Fats And Perfumes (AREA)
- Seasonings (AREA)
Description
Claims (8)
- Procédé de fabrication de sucre cristallisé à partir d'un jus sucré aqueux contenant des sucres et des impuretés organiques et minérales dont des ions Ca2+ et/ou Mg2+, tel qu'un jus de canne à sucre ou de betterave sucrière, qui comprend les opérations :de microfiltration tangentielle, d'ultrafiltration tangentielle ou de nanofiltration tangentielle dudit jus sucré aqueux pour obtenir un perméat et un rétentat,de concentration du seul perméat, pour obtenir un sirop,de cristallisation dudit sirop, pour obtenir un sucre cristallisé et une mélasse, etde séparation du sucre cristallisé de ladite mélasse, étant précisé que ledit procédé est exempt de toute opération de purification entre l'opération de filtration tangentielle et l'opération de concentration.
- Procédé selon la revendication 1, caractérisé en ce qu'il comprend en outre une opération d'adoucissement, cette opération étant effectuée sur le perméat avant que ce dernier ne soit soumis à l'opération de concentration.
- Procédé selon la revendication 2, caractérisé en ce que l'opération d'adoucissement est réalisée par mise en contact dudit perméat, avec une résine échangeuse de cations.
- Procédé selon l'une des revendications 1 à 3, caractérisé en ce que l'opération de cristallisation est suivie d'une opération de chromatographie de ladite mélasse pour obtenir un premier effluent liquide appauvri en sucres et un second effluent liquide enrichi en sucres.
- Procédé selon l'une des revendications 3 et 4, caractérisé en ce qu'il comprend en outre une opération de régénération de la résine échangeuse de cations mise en oeuvre dans l'opération d'adoucissement, par mise en contact de cette résine avec la mélasse issue de l'opération de cristallisation ou avec le premier effluent liquide issu de l'opération de chromatographie.
- Procédé selon l'une des revendications précédentes, caractérisé en ce qu'il comprend en outre une opération préalable de clarification du jus sucré aqueux de départ pour obtenir un jus clarifié, l'opération de microfiltration, d'ultrafiltration ou de nanofiltration tangentielle étant alors mise en oeuvre sur ce jus clarifié.
- Procédé selon la revendication 6, caractérisé en ce que l'opération de clarification comprend une étape de floculation suivie d'une étape de décantation.
- Procédé de fabrication de sucre blanc cristallisé à partir d'un jus sucré aqueux du type jus de canne à sucre, contenant des sucres et des impuretés organiques et minérales dont des ions Ca2+ et/ou Mg2+, caractérisé en ce qu'il comprend le procédé selon l'une quelconque des revendications 1 à 7 qui conduit à l'obtention d'un sucre roux, suivi par les opérations :de refonte dudit sucre roux, pour obtenir un sucre de fonte,de décoloration du sucre de fonte, pour obtenir un sucre de fonte décoloré, etde cristallisation du sucre de fonte décoloré, pour obtenir du sucre blanc cristallisé.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US08/151,383 US5554227A (en) | 1993-11-12 | 1993-11-12 | Process of manufacturing crystal sugar from an aqueous sugar juice such as cane juice or sugar beet juice |
US151383 | 2002-05-20 |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0655507A2 EP0655507A2 (fr) | 1995-05-31 |
EP0655507A3 EP0655507A3 (fr) | 1996-03-20 |
EP0655507B1 true EP0655507B1 (fr) | 2002-07-17 |
Family
ID=22538521
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP94402540A Expired - Lifetime EP0655507B1 (fr) | 1993-11-12 | 1994-11-09 | Procédé de fabrication de sucre cristallisé, à partir de jus sucré aqueux tel qu'un jus de canne à sucre ou de betterave sucrière |
Country Status (14)
Country | Link |
---|---|
US (2) | US5554227A (fr) |
EP (1) | EP0655507B1 (fr) |
CN (1) | CN1105705A (fr) |
AT (1) | ATE220727T1 (fr) |
AU (1) | AU698506B2 (fr) |
BR (1) | BR9404350A (fr) |
CO (1) | CO4370065A1 (fr) |
CU (1) | CU22541A3 (fr) |
DE (1) | DE69430978T2 (fr) |
DK (1) | DK0655507T3 (fr) |
EG (1) | EG20282A (fr) |
ES (1) | ES2177569T3 (fr) |
GT (1) | GT199900088A (fr) |
ZA (1) | ZA948722B (fr) |
Families Citing this family (43)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5554227A (en) * | 1993-11-12 | 1996-09-10 | Societe Nouvelle De Recherches Et D'applications Industrielles D'echangeurs D'ions Applexion | Process of manufacturing crystal sugar from an aqueous sugar juice such as cane juice or sugar beet juice |
AUPN118095A0 (en) * | 1995-02-16 | 1995-03-09 | Csr Limited | Improved process for the refining of sugar |
IT1275974B1 (it) * | 1995-03-27 | 1997-10-24 | Resindion S R L | Procedimento di trattamento con una resina scambiatrice di ioni di una soluzione zuccherina derivata da barbabietola |
US6096136A (en) * | 1996-10-18 | 2000-08-01 | Board Of Supervisors Of Louisiana State University And Agricultural And Mechanical College | Method for producing white sugar |
US5759283A (en) * | 1996-05-14 | 1998-06-02 | The Western Sugar Company | Method for processing sugar beets to produce a purified beet juice product |
EP0826781B1 (fr) * | 1996-07-31 | 2004-11-24 | Mitsui Sugar Co., Ltd. | Composition de sucre non-centrifugé et procédé de préparation d'un produit de sucre |
FR2753456B1 (fr) * | 1996-09-18 | 1998-12-31 | Generale Sucriere Sa | Procede de regeneration de resines echangeuses d'ions dans le processus de decalcification des jus de sucrerie |
US6051075A (en) * | 1996-11-15 | 2000-04-18 | Amalgamated Research, Inc. | Process for sugar beet juice clarification |
US6037456A (en) * | 1998-03-10 | 2000-03-14 | Biosource Technologies, Inc. | Process for isolating and purifying viruses, soluble proteins and peptides from plant sources |
IT1304373B1 (it) * | 1998-05-13 | 2001-03-15 | Eridania S P A | Procedimento per la produzione di zucchero bianco commerciale apartire da sugo greggio di bietola microfiltrato o ultrafiltrato. |
US6159302A (en) * | 1999-01-13 | 2000-12-12 | Betzdearborn Inc. | Neutral phosphate pre-coagulant composition for clarification in white sugar production |
US6146465A (en) * | 1999-01-13 | 2000-11-14 | Betzdearborn Inc. | Methods for clarifying sugar solutions |
AU781362B2 (en) * | 1999-04-07 | 2005-05-19 | Ufion (Proprietary) Limited | Treatment of sugar juice |
IT1311938B1 (it) * | 1999-04-21 | 2002-03-20 | Eridania S P A | Metodo di depurazione del sugo greggio di barbabietola. |
US6375751B2 (en) | 1999-08-19 | 2002-04-23 | Tate & Lyle, Inc. | Process for production of purified cane juice for sugar manufacture |
EP1788099A2 (fr) * | 1999-08-19 | 2007-05-23 | TATE & LYLE INDUSTRIES LIMITED | Procédé de filtration sur membrane de betterave à sucre |
US6440222B1 (en) * | 2000-07-18 | 2002-08-27 | Tate & Lyle Industries, Limited | Sugar beet membrane filtration process |
US6406548B1 (en) | 2000-07-18 | 2002-06-18 | Tate & Lyle Industries, Limited | Sugar cane membrane filtration process |
WO2001014595A2 (fr) * | 1999-08-19 | 2001-03-01 | Tate & Lyle, Inc. | Procede pour filtrer sur membrane de la canne a sucre |
US6406547B1 (en) | 2000-07-18 | 2002-06-18 | Tate & Lyle Industries, Limited | Sugar beet membrane filtration process |
US6174378B1 (en) | 1999-08-19 | 2001-01-16 | Tate Life Industries, Limited | Process for production of extra low color cane sugar |
US6387186B1 (en) | 1999-08-19 | 2002-05-14 | Tate & Lyle, Inc. | Process for production of purified beet juice for sugar manufacture |
US6355110B1 (en) | 1999-11-17 | 2002-03-12 | Tate & Lyle Industries, Limited | Process for purification of low grade sugar syrups using nanofiltration |
DE60224680T2 (de) * | 2001-08-24 | 2009-01-15 | Danisco Sugar A/S | Verfahren zur herstellung von weissem und braunem zucker aus zuckerrüben |
FR2838751B1 (fr) * | 2002-04-17 | 2007-03-09 | Applexion Ste Nouvelle De Rech | Procede et installation de fabrication de sucre raffine a partir de jus sucre |
PL377399A1 (pl) * | 2002-11-06 | 2006-02-06 | Danisco Sugar Oy | Dodatek jadalny polepszający smakowość, sposób jego wytwarzania i jego zastosowanie |
WO2004073414A2 (fr) * | 2003-01-23 | 2004-09-02 | Goel Prayas | Procede de clarification et de decoloration simultanee de jus de canne a sucre ne faisant intervenir aucune substance chimique, utilisant un module d'ultrafiltration a membrane plane |
US7077953B2 (en) * | 2003-09-11 | 2006-07-18 | Harris Group, Inc. | Nanofilter system and method of use |
KR20060026616A (ko) * | 2004-09-21 | 2006-03-24 | 박상영 | 고청정 기능성 알칼리 미네랄 설탕과 그 제조방법 및 장치 |
WO2006050064A2 (fr) * | 2004-10-29 | 2006-05-11 | Board of Supervisor of Louisiana State University and Agricultural and Mechanical College | Production directe de sucre blanc a partir du jus de canne a sucre ou du jus de betterave a sucre |
FR2907687B1 (fr) * | 2006-10-30 | 2008-12-26 | Applexion | Procede de purification de sialyllactose par chromatographie |
CN100507007C (zh) * | 2006-11-21 | 2009-07-01 | 华南理工大学 | 天然有色糖品的生产方法 |
FR2925349A1 (fr) * | 2007-12-20 | 2009-06-26 | Applexion | Procede de separation sequence multicolonnes d'un derive metallique ionique |
CN102659855B (zh) * | 2012-05-16 | 2014-09-03 | 成都连接流体分离科技有限公司 | 一种节能环保的蔗糖生产工艺 |
FR2999606B1 (fr) * | 2012-12-18 | 2015-09-04 | Lesaffre & Cie | Procede de purification du jus de betteraves |
US20150315670A1 (en) * | 2013-01-21 | 2015-11-05 | Mitsubishi Rayon Co., Ltd. | Method for metal concentration, method for metal recovery, device for metal concentration, and device for metal recovery |
CN103710470B (zh) * | 2013-12-26 | 2016-03-23 | 江苏久吾高科技股份有限公司 | 一种二步法制糖的工艺及装置 |
US9757688B2 (en) | 2014-03-07 | 2017-09-12 | Sidel Systems USA Inc. | Systems and methods of capturing carbon dioxide and minimizing production of carbon dioxide |
CN104004860A (zh) * | 2014-05-29 | 2014-08-27 | 江苏久吾高科技股份有限公司 | 一种黄金糖的生产工艺及装置 |
RU2589789C1 (ru) * | 2015-01-30 | 2016-07-10 | Федеральное государственное бюджетное образовательное учреждение высшего образования "Воронежский государственный университет инженерных технологий" (ФГБОУ ВО "ВГУИТ") | Способ получения клеровки желтого сахара |
WO2018029500A1 (fr) * | 2016-08-08 | 2018-02-15 | Rhodia Poliamida E Especialidades S.A. | Nouveaux constituants pour clarifier le jus de canne à sucre dans un procédé de production de sucre cristallisé ou brut |
CN108998578A (zh) * | 2018-08-22 | 2018-12-14 | 柳州味泉食品科技有限公司 | 一种联产零添加甘蔗糖蜜和零添加砂糖的方法 |
CN110016525A (zh) * | 2019-04-10 | 2019-07-16 | 中国科学院近代物理研究所 | 一种功能性食品甜高粱糖浆及其制备方法 |
Family Cites Families (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2413844A (en) * | 1941-01-31 | 1947-01-07 | Dorr Co | Ion exchange treatment of sugar |
US3808050A (en) * | 1965-07-01 | 1974-04-30 | L Paley | Clarification and treatment of sugar juice |
GB1350261A (en) * | 1970-10-16 | 1974-04-18 | Hitachi Shipbuilding Eng Co | Sugar refining process |
US3799806A (en) * | 1972-04-20 | 1974-03-26 | Danske Sukkerfab | Process for the purification and clarification of sugar juices,involving ultrafiltration |
JPS5912278B2 (ja) * | 1976-04-01 | 1984-03-22 | 三井製糖株式会社 | 甘庶汁から栄養糖を製造する方法 |
IT1124013B (it) * | 1979-03-15 | 1986-05-07 | Assalini Giuseppe | Procedimento ed impianto per il ripristino delle resine scambiatrici i ioni nel processo alcali magnesio tramite rigenerazione con melasso proveniente da detto processo arrichito con sale rigenerante fresco |
SE441932B (sv) | 1981-01-14 | 1985-11-18 | Danske Sukkerfab | Forfarande for rening av sockersaft framstelld genom extraktion av sockerbetssnitsel |
IT1225689B (it) * | 1988-09-09 | 1990-11-22 | Isi Ind Saccarifera Italiana A | Procedimento ed impianto per la purificazione differenziata in due colonne a resine a scambio ionico di sugo zuccherino |
AU635352B2 (en) * | 1990-11-09 | 1993-03-18 | Applied Membrane Systems Pty Ltd | A method and apparatus for fractionation of sugar containing solution |
US5176832A (en) * | 1991-10-23 | 1993-01-05 | The Dow Chemical Company | Chromatographic separation of sugars using porous gel resins |
US5443650B2 (en) * | 1993-06-11 | 2000-05-30 | Univ Louisiana State | Process for softening a sugar-containing aqueous solution such as sugar juice or molasses |
FR2707997B1 (fr) * | 1993-07-19 | 1995-09-29 | Applexion Ste Nle Rech Applic | Procédé de raffinage d'un sucre brut, notamment de sucre roux provenant de l'industrie sucrière de la canne à sucre. |
US5554227A (en) * | 1993-11-12 | 1996-09-10 | Societe Nouvelle De Recherches Et D'applications Industrielles D'echangeurs D'ions Applexion | Process of manufacturing crystal sugar from an aqueous sugar juice such as cane juice or sugar beet juice |
US5468300A (en) * | 1994-04-07 | 1995-11-21 | International Food Processing Incorporated | Process for producing refined sugar directly from sugarcane |
-
1993
- 1993-11-12 US US08/151,383 patent/US5554227A/en not_active Expired - Lifetime
-
1994
- 1994-11-04 ZA ZA948722A patent/ZA948722B/xx unknown
- 1994-11-04 BR BR9404350A patent/BR9404350A/pt not_active Application Discontinuation
- 1994-11-09 EG EG71194A patent/EG20282A/xx active
- 1994-11-09 EP EP94402540A patent/EP0655507B1/fr not_active Expired - Lifetime
- 1994-11-09 DE DE69430978T patent/DE69430978T2/de not_active Expired - Fee Related
- 1994-11-09 CO CO94051192A patent/CO4370065A1/es unknown
- 1994-11-09 ES ES94402540T patent/ES2177569T3/es not_active Expired - Lifetime
- 1994-11-09 DK DK94402540T patent/DK0655507T3/da active
- 1994-11-09 AT AT94402540T patent/ATE220727T1/de not_active IP Right Cessation
- 1994-11-10 AU AU77763/94A patent/AU698506B2/en not_active Ceased
- 1994-11-11 CN CN94117930A patent/CN1105705A/zh active Pending
- 1994-11-11 CU CU1994126A patent/CU22541A3/es unknown
-
1996
- 1996-08-15 US US08/698,035 patent/US5902409A/en not_active Expired - Lifetime
-
1999
- 1999-06-17 GT GT199900088A patent/GT199900088A/es unknown
Also Published As
Publication number | Publication date |
---|---|
CU22541A3 (es) | 1999-03-31 |
AU7776394A (en) | 1995-05-18 |
DE69430978T2 (de) | 2002-11-21 |
DK0655507T3 (da) | 2002-10-28 |
BR9404350A (pt) | 1995-07-04 |
EP0655507A2 (fr) | 1995-05-31 |
US5554227A (en) | 1996-09-10 |
GT199900088A (es) | 1999-06-17 |
CO4370065A1 (es) | 1996-10-07 |
EP0655507A3 (fr) | 1996-03-20 |
EG20282A (en) | 1998-07-30 |
US5902409A (en) | 1999-05-11 |
AU698506B2 (en) | 1998-10-29 |
ATE220727T1 (de) | 2002-08-15 |
DE69430978D1 (de) | 2002-08-22 |
ZA948722B (en) | 1995-07-03 |
ES2177569T3 (es) | 2002-12-16 |
CN1105705A (zh) | 1995-07-26 |
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