US3781174A - Continuous process for producing refined sugar - Google Patents

Continuous process for producing refined sugar Download PDF

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Publication number
US3781174A
US3781174A US00188851A US3781174DA US3781174A US 3781174 A US3781174 A US 3781174A US 00188851 A US00188851 A US 00188851A US 3781174D A US3781174D A US 3781174DA US 3781174 A US3781174 A US 3781174A
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Prior art keywords
juice
sugar
process according
concentrating
clarified
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US00188851A
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English (en)
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Y Nishijima
K Adachi
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Kanadevia Corp
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Hitachi Shipbuilding and Engineering Co Ltd
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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
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
    • C13B20/00—Purification of sugar juices
    • C13B20/18—Purification of sugar juices by electrical means

Definitions

  • a continuous process for producing refined sugar from juice extracted from sugarcane or other raw material comprises removing part of the impurities and part of the coloring matter in the juice by the use of a continuous carbonation process, decolorizing the juice by the use of granular active carbon, further removing the impurities and coloring matter remaining in the juice by using a combination of ion-exchange resin and ion-exchange membrane electrodialysis, concentrating the purified juice, and crystallizing the concentrated juice to form refined sugar.
  • plantation refined sugar has been produced by first producing raw sugar which is melted and processed by means of sugar refining equipment installed either in a raw-sugar plant or at a place adjacent thereto.
  • the refined sugar producing process according to the present invention applies a high degree of refinement directly to a juice extracted from sugarcane or other raw material, without requiring recrystallization as in the conventional process.
  • the juice extracted from the raw material is subjected to a fractional liming process for clarification, and the clarified juice is concentrated and crystallized to produce raw sugar.
  • the raw sugar is then remelted, decolorized by the use of granular active carbon, and purification is effected by the recrystallization process to remove the impurities (ash, organic non-sugar, etc.) contained in the juice.
  • a continuous carbonation process is applied to the extracted juice and the resulting carbonated juice is filtered.
  • the filtrate is decolorized by granular active carbon
  • the impurities in the juice are removed by the use of a combination of ion-exchange resin and ion-exchange membrane electrodialysis to provide the refined juice, which is then crystallized, thereby directly producing refined sugar.
  • the present invention is superior to the conventional process in several respects.
  • salts and organic non-sugars in the juice are removed by the chemical process occuring with the use of ionexchange resin, whereas in the conventional process such impurities are removed by the recrystallization process, i.e., physical means, and hence the conventional process necessitates the remelting of the crystallized raw sugar and then recrystallizing the same.
  • Sugar boiling, curing and purging steps are necessary for both the production of raw sugar and the refined sugar.
  • the process of the present invention is capable of directly producing refined sugar, the sugar boiling, curing and purging steps required in the conventional production of raw sugar become unnecessary; or in other words, no steps other tan those required for the production of refined sugar are necessary in the process of the invention.
  • the installation and operation costs ofa sugar refining plant can be greatly reduced, and a high yield of a product high in purity can be obtained.
  • FIG. 1 is a portion of a flow diagram illustrating an embodiment of the present invention.
  • FIG. 2 is a continuation of the flow diagram of FIG. 1, both Figures being connected together at line AA theeon.
  • sugarcane is transferred by a cane yard crane l, a cane feeding table 2 and a cane carrier 3 to cane cutters 4 and 5, where it is cut up.
  • the cane is then squeezed in a pre-extraction mill 6 and conveyed by a diffuser inlet conveyor 7 to a cane diffuser 8.
  • the juice resulting from diffusion and extraction is passed through a juice weigher 15 to a receiving tank 16 and then introduced by a pump 17 into a juice heater 18.
  • the squeezed cane discharged from the cane diffuser 8 by a diffuser outlet conveyor 9 is passed through a first dewatering mill 10 and an intermediate carrier 11 into a second dewatering mill 12. Liquid from both dewatering mills 10 and 12 is used as an additive liquid for the cane diffuser 8.
  • the juiceless remains of the sugarcane, bagasse, is taken out by a bagasse elevator 13 and carrier 14 to be used as fuel for boilers. All the steps described above are conventional and may be replaced by other conventional steps equivalent thereto.
  • the extractedjuice introduced into thejuice heater 18 is heated to about 55 C and is subjected to carbonation in a first carbonator 19, with the addition to the juice of milk of lime and carbon dioxide gas.
  • the carbonated juice is fed to a thickener 22 through a first carbonated juice tank 20 by a pump 21.
  • the carbonated juice is separated into supernatant liquid (hereinafter referred to as clarified juice) and the precipitate of calcium carbonate (hereinafter referred to as mud), the former being received in a clarified juice tank 26 and the latter in a muddy juice tank 23.
  • the mud is fed by a pump 24 from the tank 23 into a muddy juice separator 25 and separated into clarified juice and cake.
  • the clarified juice resulting from separation in the muddy juice separator is received by the same clarifiedjuice tank 26 as is the clarified juice from the thickener 22.
  • the clarified juice from both the thickener and the muddy juice separator is fed by a clarified juice pump 27 into a second carbonator 28, where the clarified juice is carbonated, and passed into a second carbonated juice tank 29.
  • a pump 30 feeds the carbonated juice from the tank 29 to a heater 31, where the juice is heated to about C to facilitate filtration, and is then passed through a check filter 32 for removal ofthe resulting calcium carbonate. In this way, the greater part of the impurities and part of the coloring matter are removed from the juice by the use of a continuous carbonation process.
  • Filtered juice from the filter 32 is received in a filtrate juice tank 33 and is fed by a pump 34 into decolorizing equipment 35, where the juice is decolorized by granular active carbon, and the decolorized juice is received in a tank 36.
  • Decolorized juice from the tank 36 is fed by a pump 37 through an ion-exchange membrane 38 and into a purification tank 39 having a cation tower 39a and an anion tower 39b. Removal of the impurities decoloration and dechlorination refinement is effected by a combination of the ion-exchange membrane 38 and ion-exchange membrane electrodialysis, and the resulting refined juice is received in a tank 40. In commercial practice, small amounts of salts may pass through this purification equipment, and so the juice is fed to a monobed ion exchange tower 42 by a pump 41 in order to apply complete dechlorination thereto and the pH is adjusted in order to prevent inversion from taking place in the concentration and crystallization steps.
  • the sequence of these juice purification processes by the ion exchange method is reversible; that is, the decolorized juice from the tank 36 may be first fed to the ion exchange resin towers 39a and 39b, then through the monobed ion exchange tower 42, and finally through the ion exchange membrane apparatus 38 to a tank 43 (FIG. 2).
  • the refined juice, received in the tank 43, is introduced by a pump 44 into a pre-heater 45 and the heated juice is evaporated and concentrated by multieffect evaporators 46a46d to form a refined juice of high purity.
  • this concentrating step may be performed by arranging the first three evaporators 46a, 46b, and 460 immediately after the decolorized juice tank 36 of FIG. 1. In other words, a portion of the concentrating step may be performed prior to the purifying step with results comparable to those obtained by the arrangement illustrated.
  • the refined juice derived from the last evaporator 46d is received by a vacuum pan 47 and the massecuite cured therein is collected in a tank 48 and introduced into a centrifugal machine 49, where the massecuite is fractionated into sugar and molasses.
  • the molasses is stored in a molasses tank 54, while the sugar is dried and cooled by a sugar dryer and cooler 50 to crystallize the sugar. Thereafter, the sugar is passed through a sugar sieve 51 for adjutment of grain size and then delivered through a sugar bin 52 into sugar bagging equipment, where the sugar is bagged to provide bagged products 55.
  • the resin tower is planned to eliminate 5 percent 60 percent of the ash from the juice and the remainder of the purification is accomplished by the combination of the ion exchange resin tower and the ion exchange membrane apparatus.
  • the sequence of these processes is reversible, that is, the juice from the granular carbon tower is first fed to the ion exchange membrane apparatus where about percent percent of the minerals in the juice are eliminated, and as the following stage, this predemineralized juice is treated in the continuous ion exchange resin towers. With either sequence, percent 98 percent ofjuice purity is expected.
  • strong anion resin type II DIAlON SA-20, Amberlite IRA-41 l, etc.
  • week anion resin Amberlite C-SO, etc.
  • the sugar juice having a substantial amount of nonsugar matter (ash and organic non-sugar) thus removed therefrom may be used in this state to produce white sugar of good quality, and if the resin towers are designed to reduce the ash to 20 percent or less or the original ash content, it is possible to expect 95 percent or more of purified juice purity. But, in this invention, considering the running cost for regeneration and com- Note: 1 ln this experiment, substantially the same results will be obtained even if the order of the ionexchange and electro dialysis processes is reversed, but the apparatus for electrodialysis shall be a larger scale than the other.
  • the amount of mineral matter removed by the electrodialysis is about -200 equivalent per 1 KWl-l of electrical consumption.
  • a continuous process for refining sugar from the juice extracted from a raw material such as sugarcane comprising the steps of:
  • step (a) of removing part of the impurities and part of the coloring matter from the juice is carried out by adding milk of lime and carbon dioxide gas to the juice, separating the carbonated juice into clarified juice and cake, carbonating the clarified juice, and filtering the carbonated clarified juice.
  • step c) of further purifying the juice includes the employment of a dechlorination treatment.
  • step (c) of further purifying the juice is carried out by passing the juice through an ion-exchange membrane, a cation tower and a anion tower.
  • a process according to claim 5 wehrein the purified juice from the cation and anion towers is dechlorinated, by using an anion exchange resin treatment.
  • step (d) of concentrating the juice is carried out by passing the juice through a multi-effect evaporator.

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Biochemistry (AREA)
  • Organic Chemistry (AREA)
  • Non-Alcoholic Beverages (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
US00188851A 1970-10-16 1971-10-13 Continuous process for producing refined sugar Expired - Lifetime US3781174A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP9105370 1970-10-16

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US3781174A true US3781174A (en) 1973-12-25

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US (1) US3781174A (enExample)
BR (1) BR7106173D0 (enExample)
DE (1) DE2151341C3 (enExample)
FR (1) FR2109613A5 (enExample)
GB (1) GB1350261A (enExample)

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3887391A (en) * 1974-02-19 1975-06-03 Amalgamated Sugar Co Process for the decalcification sugar beet juice
US3962077A (en) * 1973-06-15 1976-06-08 Tecneco S.P.A. Process for the purification of waste waters
US4299677A (en) * 1980-11-03 1981-11-10 The Hubinger Co. Process for the preferential separation of fructose from glucose
US4376023A (en) * 1980-11-03 1983-03-08 The Hubinger Company Process for the preferential separation of dextrose from oligosaccharides
US4880647A (en) * 1989-03-10 1989-11-14 Fmc Corporation Process for mild heat treatment of concentrated fluids from membranes
US4936962A (en) * 1989-03-01 1990-06-26 Fmc Corporation Process for adjusting the pH of an aqueous flowable fluid
US4938856A (en) * 1989-03-01 1990-07-03 Fmc Corporation Process for mild heat treatment of a flowable fluid
US5051236A (en) * 1988-12-19 1991-09-24 Fmc Corporation Process for reducing the concentration of viable cells in a flowable fluid
US5454875A (en) * 1994-07-01 1995-10-03 Board Of Supervisors Of Louisiana State University And Agricultural And Mechanical College Softening and purification of molasses or syrup
WO1995027798A1 (en) * 1994-04-07 1995-10-19 International Food Processing, Incorporated Process for producing sugar directly from sugarcane
WO1996004406A1 (en) * 1994-08-03 1996-02-15 International Food Processing, Incorporated Process for producing refined sugar
US5851372A (en) * 1994-05-09 1998-12-22 Societe Anonyme Francaise D'ingenierie Et De Recherche Process for demineralizing a liquid containing organic matter and salts in solution
US5865899A (en) * 1993-07-19 1999-02-02 Applexion Process for refining a raw sugar, particulary raw sugar from the sugar cane sugar industry
US5902409A (en) * 1993-11-12 1999-05-11 Societe Nouvelle De Recherches Et D'applications Industrielles D-Exchangeurs D'ions Applexion Process of manufacturing crystal sugar from an aqueous sugar juice such as cane juice or sugar beet juice
EP0916620A3 (en) * 1997-11-12 1999-08-04 Archer-Daniels-Midland Company Desalting aqueous streams via filled cell electrodialysis
US6372049B1 (en) * 1997-06-02 2002-04-16 Centre for the Advancement of New Technologies “CANTEC” Method of producing sugar syrup from sugar-containing raw materials
US20030049813A1 (en) * 1998-03-10 2003-03-13 Garger Stephen J. Process for isolating and purifying proteins and peptides from plant sources
US20070169772A1 (en) * 2005-12-21 2007-07-26 Danisco Sugar A/S Process for the recovery of sucrose and/or non-sucrose components
US20070256936A1 (en) * 2006-05-04 2007-11-08 Robert Jansen Method for Deashing Syrup by Electrodialysis
CN101508707B (zh) * 2009-03-25 2011-09-28 湖南尔康制药股份有限公司 药用蔗糖的生产工艺
CN109825651A (zh) * 2019-04-08 2019-05-31 中国科学院过程工程研究所 一种膜法制糖工艺中多联产的方法

Cited By (29)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3962077A (en) * 1973-06-15 1976-06-08 Tecneco S.P.A. Process for the purification of waste waters
US3887391A (en) * 1974-02-19 1975-06-03 Amalgamated Sugar Co Process for the decalcification sugar beet juice
US4299677A (en) * 1980-11-03 1981-11-10 The Hubinger Co. Process for the preferential separation of fructose from glucose
US4376023A (en) * 1980-11-03 1983-03-08 The Hubinger Company Process for the preferential separation of dextrose from oligosaccharides
US5051236A (en) * 1988-12-19 1991-09-24 Fmc Corporation Process for reducing the concentration of viable cells in a flowable fluid
US4936962A (en) * 1989-03-01 1990-06-26 Fmc Corporation Process for adjusting the pH of an aqueous flowable fluid
US4938856A (en) * 1989-03-01 1990-07-03 Fmc Corporation Process for mild heat treatment of a flowable fluid
US4880647A (en) * 1989-03-10 1989-11-14 Fmc Corporation Process for mild heat treatment of concentrated fluids from membranes
US5865899A (en) * 1993-07-19 1999-02-02 Applexion Process for refining a raw sugar, particulary raw sugar from the sugar cane sugar industry
US5902409A (en) * 1993-11-12 1999-05-11 Societe Nouvelle De Recherches Et D'applications Industrielles D-Exchangeurs D'ions Applexion Process of manufacturing crystal sugar from an aqueous sugar juice such as cane juice or sugar beet juice
WO1995027798A1 (en) * 1994-04-07 1995-10-19 International Food Processing, Incorporated Process for producing sugar directly from sugarcane
US5468301A (en) * 1994-04-07 1995-11-21 International Food Processing Incorporated Process for producing refined sugar
US5468300A (en) * 1994-04-07 1995-11-21 International Food Processing Incorporated Process for producing refined sugar directly from sugarcane
US5851372A (en) * 1994-05-09 1998-12-22 Societe Anonyme Francaise D'ingenierie Et De Recherche Process for demineralizing a liquid containing organic matter and salts in solution
US5454875A (en) * 1994-07-01 1995-10-03 Board Of Supervisors Of Louisiana State University And Agricultural And Mechanical College Softening and purification of molasses or syrup
WO1996004406A1 (en) * 1994-08-03 1996-02-15 International Food Processing, Incorporated Process for producing refined sugar
US6372049B1 (en) * 1997-06-02 2002-04-16 Centre for the Advancement of New Technologies “CANTEC” Method of producing sugar syrup from sugar-containing raw materials
EP0916620A3 (en) * 1997-11-12 1999-08-04 Archer-Daniels-Midland Company Desalting aqueous streams via filled cell electrodialysis
EP1233004A1 (en) * 1997-11-12 2002-08-21 Archer-Daniels-Midland Company Desalting aqueous streams via filled cell electrodialysis
US20030049813A1 (en) * 1998-03-10 2003-03-13 Garger Stephen J. Process for isolating and purifying proteins and peptides from plant sources
US6740740B2 (en) 1998-03-10 2004-05-25 Large Scale Biology Corporation Process for isolating and purifying proteins and peptides from plant sources
US20070169772A1 (en) * 2005-12-21 2007-07-26 Danisco Sugar A/S Process for the recovery of sucrose and/or non-sucrose components
WO2007071729A3 (en) * 2005-12-21 2007-09-13 Danisco Sugar As A process for the recovery of a brown food-grade sugar product from a sugar beet solution
WO2007071727A3 (en) * 2005-12-21 2007-09-13 Danisco Sugar As Process for the recovery of sucrose and/or non-sucrose components
US20080299287A1 (en) * 2005-12-21 2008-12-04 Danisco Sugar A/S Process For The Recovery Of A Brown Food-Grade Sugar Product From A Sugar Beet Solution
US7763116B2 (en) 2005-12-21 2010-07-27 Danisco A/S Process for the recovery of sucrose and/or non-sucrose components
US20070256936A1 (en) * 2006-05-04 2007-11-08 Robert Jansen Method for Deashing Syrup by Electrodialysis
CN101508707B (zh) * 2009-03-25 2011-09-28 湖南尔康制药股份有限公司 药用蔗糖的生产工艺
CN109825651A (zh) * 2019-04-08 2019-05-31 中国科学院过程工程研究所 一种膜法制糖工艺中多联产的方法

Also Published As

Publication number Publication date
DE2151341C3 (de) 1978-07-13
BR7106173D0 (pt) 1973-03-29
DE2151341A1 (de) 1972-04-20
DE2151341B2 (de) 1977-10-27
GB1350261A (en) 1974-04-18
FR2109613A5 (enExample) 1972-05-26

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