EP0655507A2 - Verfahren zur Herstellung von Kristallzucker aus einem wässrigen Zuckersaft, z.B. Zuckerrohr-oder Zuckerrübesaft - Google Patents

Verfahren zur Herstellung von Kristallzucker aus einem wässrigen Zuckersaft, z.B. Zuckerrohr-oder Zuckerrübesaft Download PDF

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Publication number
EP0655507A2
EP0655507A2 EP94402540A EP94402540A EP0655507A2 EP 0655507 A2 EP0655507 A2 EP 0655507A2 EP 94402540 A EP94402540 A EP 94402540A EP 94402540 A EP94402540 A EP 94402540A EP 0655507 A2 EP0655507 A2 EP 0655507A2
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EP
European Patent Office
Prior art keywords
sugar
juice
tangential
crystallization
sugars
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.)
Granted
Application number
EP94402540A
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English (en)
French (fr)
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EP0655507B1 (de
EP0655507A3 (de
Inventor
Robert J. Kwok
Xavier Lancrenon
Marc-André Theoleyre
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Applexion SAS
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Applexion SAS
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Publication date
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Publication of EP0655507A2 publication Critical patent/EP0655507A2/de
Publication of EP0655507A3 publication Critical patent/EP0655507A3/de
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Publication of EP0655507B1 publication Critical patent/EP0655507B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • 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
    • C13B20/02—Purification of sugar juices using alkaline earth metal compounds
    • 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
    • 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
    • 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
    • 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

  • the object of the present invention is to remedy the aforementioned drawbacks of the previously known methods and, to do this, it proposes a method for manufacturing crystallized sugar, as defined in the first paragraph of this description, which is characterized in that it further comprises an operation (c) of tangential microfiltration, tangential ultrafiltration or tangential nanofiltration, this operation being carried out before operation (a).
  • this operation (c) it is possible to eliminate the colloidal materials present in the clarified sugar juice and, insofar as such materials are precursors of dyes developing during crystallization, d '' thus obtain at the end of the process a crystallized sugar of lower coloring.
  • the starting aqueous sweet juice is constituted by a juice of the sugar cane juice type
  • the method according to the invention then makes it possible to obtain a brown sugar of a coloration less than 400 ICUMSA units, while conventional methods lead to the production of brown sugar with a coloration of 800 to 4000 ICUMSA units.
  • tangential microfiltration By using tangential microfiltration, tangential ultrafiltration or tangential nanofiltration techniques, it is possible to substantially reduce the turbidity of the clarified juice. It will be recalled for all practical purposes that the amount of colloids present in a liquid is estimated by its turbidity (expressed in NTU / Brix) that they generate within said liquid. Thus, it will be indicated, by way of example, that the tangential ultrafiltration of a clarified sugary cane juice makes it possible to reduce the turbidity of this juice from approximately 15 to 60 NTU / Brix to a value as low as 0.1 at 0.2 NTU / Brix.
  • the method according to the invention may also comprise an operation (d) of softening, this operation being carried out before operation (a) and on the sweet juice having undergone the operation (c ) microfiltration, ultrafiltration or tangential nanofiltration.
  • the softening operation (d) will advantageously be carried out by bringing the sweet juice having undergone said microfiltration, ultrafiltration or tangential nanofiltration operation into contact with a cation exchange resin, and in particular a strong cationic resin. preferably in the form of Na+ and / or K+.
  • the operation (b) of crystallization may be followed by an operation (e) of chromatography of said molasses to obtain a first liquid effluent depleted in sugars and a second liquid effluent enriched in sugars; such an operation (e) fits perfectly into the process according to the invention since the prior microfiltration, ultrafiltration or tangential nanofiltration (c) and softening (d) operations allow substantial removal of colloidal materials and Ca2+ and / or Mg2+ ions usually responsible for the relatively rapid decrease in the separation power of the chromatography.
  • the method according to the invention can also comprise an operation (f) for regenerating the cation exchange resin used in operation (d), by bringing this resin into contact with the molasses resulting from the crystallization operation (b) or with the first liquid effluent depleted in sugars resulting from the chromatography operation (e).
  • this regeneration operation makes clever use of one of the effluents generated during the process, so that there is no supply of external regeneration reagent and, consequently, economy compared to the regeneration systems. previously known in the art.
  • the operation (c) of micro-, ultra- or tangential nanofiltration allows not only to eliminate the colloidal matter present in the starting sugar juice, but also to clarify this juice, that is to say to remove suspended solids.
  • this operation (g) preferably comprising a flocculation step followed by a decantation step.
  • the implementation of the method according to the invention leads to a significant improvement in the overall balance of the candy with, moreover in the case where the starting sugar juice is of the sugarcane juice type, a gain in purity of the brown sugar obtained which goes from 98-99.4% (conventional process) to 99.7%.
  • This improvement is obtained by the implementation of a microfiltration, ultrafiltration or tangential nanofiltration operation and a softening operation, well known techniques, simple, flexible, high efficiency, fast, well controlled and d '' a low operating cost.
  • the implementation of the microfiltration, ultrafiltration or nanofiltration tangential operation possibly combined with the simple clarification operation. (g) advantageously makes it possible to eliminate the complex and expensive purification operations mentioned above.
  • the refining used in the process according to the invention for manufacturing white crystallized sugar is freed from the refining and purification operations (carbonation or phosphating). and filtration and this, thanks to the fact that the implementation of operations (a) to (d) and possibly (e) and (f) described above makes it possible to obtain a purer, less colored brown sugar and no longer containing colloidal materials in comparison with that obtained by conventional techniques.
  • the elimination of refining, carbonation or phosphating and filtration operations is of obvious interest when we know the tedious and expensive nature of the crystallization operations of the refining sewer and the sewers of low products. .
  • the advantage provided by the process according to the invention for the production of white crystallized sugar is therefore manifest from the economic point of view.
  • 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 Ca2+ and / or Mg2+ 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 at by means of an indirect heat exchanger 4.
  • this tank 3 it is mixed under 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 duct 7.
  • the reservoir 5 can 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 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 may be of the organic type or of the mineral type (for example made of TiO2 or ZrO2) and have a cutoff threshold corresponding to a molecular weight of at least 1000, good results being obtained with a membrane of 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 of ultrafiltration having a cutoff threshold corresponding to a molecular weight of 300,000
  • a microfiltration membrane having a pore diameter of 0.1 ⁇ m.
  • KERASEP® membrane available from the French company TECH-SEP or the FIMTEC® GR 90 PP membrane from 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.
  • the permeate from unit 11 which has a turbidity of the order of 0.1 to 0.2 NTU / Brix, is then conveyed by a conduit 12 into a storage tank 13 from which it is withdrawn by a pump 14 to be brought to the head of a softening column 15 filled with a cation exchange resin, in particular a strong cationic resin, in the Na+ and / or K+ form, for example C26® resin from Rohm and Haas.
  • a cation exchange resin in particular a strong cationic resin, in the Na+ and / or K+ form, for example C26® resin from Rohm and Haas.
  • This column is provided, at its upper part, with a permeate inlet 16 connected to the discharge of the pump 14 and, at its lower part, with a conduit 17 for softened permeate outlet (content of Ca2+ ions and / or Mg2+ of the order of 150 to 700 ppm), the Ca2+ and / or Mg2+ ions present in the permeate brought to the head of the column (content of Ca2+ and / or Mg2+ ions 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 the conduit 17 then arrives in a tank 18 from which it is withdrawn 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 at the outlet of 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 by FIG. 1) to deliver to each crystallization stage a brown sugar and molasses.
  • the yield of extraction of sugars from the baked mass is of the order of 65% at the level of the first crystallization stage, that the degree of coloration of the brown sugar obtained in this first stage is not greater than 300 ICUMSA units 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 to its dissolution in water. preferably hot at 80 ° C.
  • the resulting syrup is then brought into a bleaching column 25 packed with an adsorbent material such as animal black, activated carbon or a bleaching resin, for example a strong anionic resin in the form of chloride, such as IRA® 900 resin from Rohm and Haas).
  • the bleaching is preferably carried out hot, for example at 80 ° C. It will be noted that the bleaching of the syrup can alternatively be carried out by ultrafiltration or tangential nanofiltration of said syrup.
  • the syrup thus discolored is then treated in a crystallization unit 26 to deliver white sugar crystallized at 27 and a crystallization drain at 28.
  • the latter is preferably recycled by mixing it with the syrup from the concentration unit 20; it can also be used for the above-mentioned recasting operation.
  • the brown sugar obtained in the second and third crystallization stages of the crystallization unit 22 can, if desired, be remelted and then brought 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 Ca2+ and / or Mg2+ 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 DOWEX® C356 resin from DOW or LES® resin 999301 from Rohm and Haas, the elution liquid being water brought to the top 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 a conduit 35 for extracting a second liquid effluent enriched in sugars, depleted in Na and / or K salts and eluted in the second place.
  • 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)
  • Biochemistry (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Water Supply & Treatment (AREA)
  • Inorganic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Non-Alcoholic Beverages (AREA)
  • Saccharide Compounds (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Fats And Perfumes (AREA)
  • Seasonings (AREA)
EP94402540A 1993-11-12 1994-11-09 Verfahren zur Herstellung von Kristallzucker aus einem wässrigen Zuckersaft, z.B. Zuckerrohr- oder Zuckerrübensaft Expired - Lifetime EP0655507B1 (de)

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 1993-11-12

Publications (3)

Publication Number Publication Date
EP0655507A2 true EP0655507A2 (de) 1995-05-31
EP0655507A3 EP0655507A3 (de) 1996-03-20
EP0655507B1 EP0655507B1 (de) 2002-07-17

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EP94402540A Expired - Lifetime EP0655507B1 (de) 1993-11-12 1994-11-09 Verfahren zur Herstellung von Kristallzucker aus einem wässrigen Zuckersaft, z.B. Zuckerrohr- oder Zuckerrübensaft

Country Status (14)

Country Link
US (2) US5554227A (de)
EP (1) EP0655507B1 (de)
CN (1) CN1105705A (de)
AT (1) ATE220727T1 (de)
AU (1) AU698506B2 (de)
BR (1) BR9404350A (de)
CO (1) CO4370065A1 (de)
CU (1) CU22541A3 (de)
DE (1) DE69430978T2 (de)
DK (1) DK0655507T3 (de)
EG (1) EG20282A (de)
ES (1) ES2177569T3 (de)
GT (1) GT199900088A (de)
ZA (1) ZA948722B (de)

Cited By (11)

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FR2732358A1 (fr) * 1995-03-27 1996-10-04 Resindion Srl Procede pour le traitement par une resine echangeuse d'ions cationique d'une solution sucree issue de la betterave
FR2753456A1 (fr) * 1996-09-18 1998-03-20 Generale Sucriere Sa Procede de regeneration de resines echangeuses d'ions dans le processus de decalcification des jus de sucrerie
US5759283A (en) * 1996-05-14 1998-06-02 The Western Sugar Company Method for processing sugar beets to produce a purified beet juice product
EP0826781A3 (de) * 1996-07-31 2000-01-12 Mitsui Sugar Co., Ltd. Zusammensetzung eines nichtzentrifugierten Zuckers und Verfahren zur Herstellung eines Zuckerproduktes
WO2000060128A1 (en) * 1999-04-07 2000-10-12 Aeci Limited Treatment of sugar juice
EP1046718A1 (de) * 1999-04-21 2000-10-25 ERIDANIA S.p.A. Reinigungsverfahren für rohen Zuckerrübensaft
WO2001014595A3 (en) * 1999-08-19 2001-12-06 Tate & Lyle Inc Sugar cane membrane filtration process
WO2001014594A3 (en) * 1999-08-19 2001-12-06 Tate & Lyle Inc Sugar beet membrane filtration process
US6375751B2 (en) 1999-08-19 2002-04-23 Tate & Lyle, Inc. Process for production of purified cane juice for sugar manufacture
US6387186B1 (en) 1999-08-19 2002-05-14 Tate & Lyle, Inc. Process for production of purified beet juice for sugar manufacture
FR2838751A1 (fr) * 2002-04-17 2003-10-24 Applexion Ste Nouvelle De Rech Procede et installation de fabrication de sucre raffine a partir de jus sucre

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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
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
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
US6406547B1 (en) 2000-07-18 2002-06-18 Tate & Lyle Industries, Limited Sugar beet membrane filtration process
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
US6174378B1 (en) 1999-08-19 2001-01-16 Tate Life Industries, Limited Process for production of extra low color cane sugar
US6355110B1 (en) 1999-11-17 2002-03-12 Tate & Lyle Industries, Limited Process for purification of low grade sugar syrups using nanofiltration
US20040231663A1 (en) * 2001-08-24 2004-11-25 Carter Melvin Paul Process for the preparation of white and brown sugar from sugar beets
WO2004041003A1 (en) * 2002-11-06 2004-05-21 Danisco Sugar Oy Edible flavor improver, process for its production and use
BRPI0406483B1 (pt) * 2003-01-23 2014-04-22 Prayas Goel Método para clarificação e descoloração do caldo de cana-de-açúcar de forma simultânea, sem o uso de quaisquer produtos químicos para qualquer finalidade, por meio do uso de módulo de membranas planas de ultrafiltração
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 (en) * 2004-10-29 2006-05-11 Board of Supervisor of Louisiana State University and Agricultural and Mechanical College Direct production of white sugar from sugarcane juice or sugar beet juice
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
EP2947163A4 (de) * 2013-01-21 2016-05-11 Mitsubishi Rayon Co Verfahren zur metallkonzentration, verfahren zur metallgewinnung, vorrichtung zur metallkonzentration und vorrichtung zur metallgewinnung
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 (en) * 2016-08-08 2018-02-15 Rhodia Poliamida E Especialidades S.A. New components to clarify sugar cane juice in a process for producing crystal or raw sugar
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

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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

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US4432806A (en) 1981-01-14 1984-02-21 Aktieselskabet De Danske Sukkerfabrikker Method of purifying sugar juice prepared by extraction of a sugar beet material

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2732358A1 (fr) * 1995-03-27 1996-10-04 Resindion Srl Procede pour le traitement par une resine echangeuse d'ions cationique d'une solution sucree issue de la betterave
US5759283A (en) * 1996-05-14 1998-06-02 The Western Sugar Company Method for processing sugar beets to produce a purified beet juice product
EP0826781A3 (de) * 1996-07-31 2000-01-12 Mitsui Sugar Co., Ltd. Zusammensetzung eines nichtzentrifugierten Zuckers und Verfahren zur Herstellung eines Zuckerproduktes
FR2753456A1 (fr) * 1996-09-18 1998-03-20 Generale Sucriere Sa Procede de regeneration de resines echangeuses d'ions dans le processus de decalcification des jus de sucrerie
WO1998012356A1 (fr) * 1996-09-18 1998-03-26 Saint Louis Sucre Procede de regeneration de resines echangeuses d'ions dans le processus de decalcification des jus de sucrerie
EP0832986A1 (de) * 1996-09-18 1998-04-01 Generale Sucriere, S.A. Verfahren zur Regenerierung von Ionaustauschharzen im Verfahren zur Entfernung des Kalzium aus Zuckersaften
WO2000060128A1 (en) * 1999-04-07 2000-10-12 Aeci Limited Treatment of sugar juice
EP1046718A1 (de) * 1999-04-21 2000-10-25 ERIDANIA S.p.A. Reinigungsverfahren für rohen Zuckerrübensaft
WO2001014595A3 (en) * 1999-08-19 2001-12-06 Tate & Lyle Inc Sugar cane membrane filtration process
WO2001014594A3 (en) * 1999-08-19 2001-12-06 Tate & Lyle Inc Sugar beet membrane filtration process
US6375751B2 (en) 1999-08-19 2002-04-23 Tate & Lyle, Inc. Process for production of purified cane juice for sugar manufacture
US6387186B1 (en) 1999-08-19 2002-05-14 Tate & Lyle, Inc. Process for production of purified beet juice for sugar manufacture
FR2838751A1 (fr) * 2002-04-17 2003-10-24 Applexion Ste Nouvelle De Rech Procede et installation de fabrication de sucre raffine a partir de jus sucre
EP1354965A3 (de) * 2002-04-17 2004-02-11 Applexion Verfahren und Vorrichtung zur Herstellung von Raffinadezucker von Zuckersaft

Also Published As

Publication number Publication date
ATE220727T1 (de) 2002-08-15
AU698506B2 (en) 1998-10-29
DK0655507T3 (da) 2002-10-28
EG20282A (en) 1998-07-30
AU7776394A (en) 1995-05-18
US5554227A (en) 1996-09-10
US5902409A (en) 1999-05-11
DE69430978D1 (de) 2002-08-22
EP0655507B1 (de) 2002-07-17
ES2177569T3 (es) 2002-12-16
BR9404350A (pt) 1995-07-04
ZA948722B (en) 1995-07-03
EP0655507A3 (de) 1996-03-20
CN1105705A (zh) 1995-07-26
CO4370065A1 (es) 1996-10-07
DE69430978T2 (de) 2002-11-21
CU22541A3 (es) 1999-03-31
GT199900088A (es) 1999-06-17

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