US3642534A - Sugar-crystallizing method and apparatus - Google Patents

Sugar-crystallizing method and apparatus Download PDF

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Publication number
US3642534A
US3642534A US882604A US3642534DA US3642534A US 3642534 A US3642534 A US 3642534A US 882604 A US882604 A US 882604A US 3642534D A US3642534D A US 3642534DA US 3642534 A US3642534 A US 3642534A
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United States
Prior art keywords
massecuite
magma
sugar
syrup
comminuting
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Expired - Lifetime
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US882604A
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English (en)
Inventor
Jacques De Cremoux
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Fives Lille Cail
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Fives Lille Cail
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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
    • C13B30/022—Continuous processes, apparatus therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0036—Crystallisation on to a bed of product crystals; Seeding
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0063—Control or regulation

Definitions

  • This invention relates to the continuous crystallization of raw sugar from concentrated syrup, and particularly to a method of seeding the syrup and to apparatus for performing the method.
  • a principal object of the invention is a simpler and more economical method of preparing a magma of seed crystals. Another object is the provision of apparatus for performing the method.
  • a useful magma may be prepared by comminuting the particulate crystalline sugar ofmassecuite to the desired size while the crystalline sugar is immersed in the mother liquor of the massecuite.
  • the wet grinding of the crystalline sugar does not produce the tines which are undesirable in the seed crystals and unavoidable in dry crushing or grinding.
  • the equipment required for the method consists solely of a comminuting device, such as a ball mill, and the invention thus reduces the initial cost and the operating expense of a sugar crystallization plant.
  • magma may be prepared according to the method of the invention either in batches or continuously, but continuous magma preparation normally is better adapted to use with continuously operating crystallizing equipment.
  • FIG. 1 is a flow diagram of apparatus for performing the method of the invention
  • FIG. 2 illustrates a ball mill for use in the method of FIG. 1 in elevational section on the axis of rotation of the mill
  • FIG. 3 shows a modification of the apparatus of FIG. 1.
  • FIG. 1 there is shown a vacuum crystallizer of a conventional type, not shown in detail, to which concentrated syrup is fed by a feed line 12.
  • a separate feedline 14 supplies magma to the crystallizer vessel, and massecuite is withdrawn continuously by a rotary slurry pump 16, most of the withdrawn material being pumped into a mixer 18 for further processing, not relevant to this invention.
  • Metered amounts of the withdrawn massecuite are continuously transferred by a positive displacement pump 20 to a crusher 24, together with dilute syrup admitted through a control valve 22, and the magma of comminuted crystals suspended in the mother liquor of the massecuite is fed to the crystallizer 10 through the feedline 14 which connects the crusher to the crystallizer vessel and is equipped with a storage and settling tank 26 and a control valve 28, the setting of the valve being coordinated with the operation of the pump 20 to maintain steady operating conditions in the crusher 24 and to maintain an adequate magma level in the storage tank 26, which prevents air from being entrained with the magma fed to the crystallizer 10 in which a vacuum is maintained for rapid evaporation of water from the syrup, as is conventional.
  • FIG. 2 A ball mill modified for the purpose of the invention has been found advantageous in apparatus of the type shown in FIG. 1, and a suitable ball mill is illustrated in FIG. 2. It has a cylindrical shell 30 which is rotated about a horizontal axis in the usual manner, not shown. The interior ofthe shell 30 is axially divided into three compartments by two upright screens 32, 34 of an aperture size sufficient to retain the grinding balls 36 which partly fill the shell. An additional screen 38 prevents discharge of the balls 36 through an annular aperture 40 in one radial end wall of the shell. Massecuite somewhat reduced in viscosity by the admixture of syrup is fed to the shell 30 continuously through a central aperture 42 in the other radial end wall. The material is still viscous enough to maintain in the shell 30 a surface 44 which slopes obliquely downwardly in the direction ofthe mill axis.
  • the particle size distribution of the comminuted sugar crystals discharged from the aperture 40 together with mother liquor depends mainly on the dwell time of the material in the shell, on the rotary speed of the shell, and on the size, weight and shape of the grinding bodies 36 in a manner well known to those skilled in the art. Suitable comminuting conditions must be established experimentally for each piece of comminuting equipment.
  • a continuous crystallizer having an hourly capacity of 30 metric tons of massecuite was equipped with a metering pump capable of transferring 150 to 300 kg. of the withdrawn massecuite per hour to a ball mill of the type shown in FIG. 2.
  • a control valve could be set for delivering 75 to 150 kg./hour syrup or hot water to the mill, approximately one half of the liquid being added to the massecuite prior to grinding, and the other half being added to the treated massecuite to form a magma which was returned to the crystallizer.
  • the grown crystals in the massecuite had an average particle size of 0.7 mm.
  • the magma contained 20 to 25 percent seed crystals by weight, depending on the specific diluting conditions chosen, and the particle size on the seed crystals was practically entirely within the range from 20 to microns.
  • the ball mill employed had an axial length of one meter, a diameter of 0.4 meter, and it was rotated at a speed of 44 rpm.
  • FIG. 3 Another crystallizing arrangement is shown in FIG. 3. It includes a vacuum crystallizer 10' from which massecuite is withdrawn by a slurry pump 16 and largely flows into a mixer 18'. A portion of the massecuite is transferred from the intake of the pump 16' to a crusher 24 by a metering pump 20.
  • a calibrated control valve 22 delivers syrup to two branch lines respectively equipped with valves 46, 48 for feeding respective portions of the syrup to the intake of the crusher 24 and to an open storage tank 26' equipped with a nonillustrated agitator to which the treated massecuite from the crusher 24' is also transferred.
  • the mixture of treated massecuite and diluting syrup is held long enough in the tank 26' to permit escape of entrapped air before the mixture flows to a pump 50 which discharges the magma'into the feedline 12' delivering concentrated syrup to the crystallizer 10.
  • a bypass 52 connects the intake and discharge conduits of the pump 50 and is controlled by a motor-operated valve 54.
  • the reversible valve motor is connected with a level gage 56 in the storage tank 26 to open the valve 54, and thereby to reduce the effective output of the pump 54 when the magma level in the tank 26 drops below a desired height, and to reduce the flow section of the valve 54, and thereby to increase the effective output of the pump 50 when the magma level rises above the desired height.
  • a crystallizing arrangement for sugar including a crystallizer vessel, feeding means for continuously feeding a body of syrup and a magma of sugar crystals suspended in syrup to said vessel, and withdrawing means for withdrawing massecuite from said vessel, the improvement which comprises:
  • connecting means connecting said comminuting means with said feeding means for flow ofthe treated massecuite from said comminuting means to said vessel.
  • said comminuting means including a rotary mill and grinding bodies in said mill.
  • said mill including a container mounted for rotation about a horizontally extending axis, an inlet and an outlet on said container axially spaced on said container, and a plurality of screens axially dividing the interior of said container into a plurality of compartments, the apertures of said screens being of a size to retain said grinding bodies but to pass said treated massecuite.

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  • Chemical & Material Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Biochemistry (AREA)
  • Organic Chemistry (AREA)
  • Saccharide Compounds (AREA)
  • Jellies, Jams, And Syrups (AREA)
  • Coloring Foods And Improving Nutritive Qualities (AREA)
  • Medicines Containing Plant Substances (AREA)
US882604A 1968-12-06 1969-12-05 Sugar-crystallizing method and apparatus Expired - Lifetime US3642534A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
FR176907 1968-12-06

Publications (1)

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US3642534A true US3642534A (en) 1972-02-15

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US882604A Expired - Lifetime US3642534A (en) 1968-12-06 1969-12-05 Sugar-crystallizing method and apparatus

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US (1) US3642534A (pt)
JP (1) JPS5224107B1 (pt)
BE (1) BE741840A (pt)
BR (1) BR6914773D0 (pt)
ES (1) ES373898A1 (pt)
FR (1) FR1597729A (pt)
GB (1) GB1244543A (pt)
IT (1) IT1044186B (pt)
NL (1) NL151133B (pt)
PL (1) PL80373B1 (pt)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3996018A (en) * 1974-11-11 1976-12-07 Merck & Co., Inc. Crystallization system and method using crystal fracturing external to a crystallization column
US4145230A (en) * 1976-05-21 1979-03-20 Aktieselskabet De Danske Sukkerfabrikker Method for seeding super-saturated sugar solution to effect crystallization
US4164429A (en) * 1976-12-14 1979-08-14 Fives-Cail Babcock Process and installation for the production of selected crystallization seeds for use in a sugar refinery
US4518436A (en) * 1982-09-23 1985-05-21 Csm Suiker B.V. Process for the production of graft crystals for use in seeding sugar boiling brines
FR2602153A1 (fr) * 1986-08-01 1988-02-05 Fives Cail Babcock Procede de production d'un magma d'ensemencement pour un appareil de cristallisation marche continue
EP0255786A1 (fr) * 1986-08-01 1988-02-10 FIVES-CAIL BABCOCK, Société Anonyme Procédé et installation pour la production d'un magma d'ensemencement pour un appareil de cristallisation à marche continue
US5015297A (en) * 1985-05-15 1991-05-14 Roquette Freres Method and installation for the production of anhydrous crystalline fructose
WO2000056416A1 (de) * 1999-03-20 2000-09-28 Domo Caproleuna Gmbh Verfahren zur steuerung der kristallgrösse bei der kontinuierlichen massenkristallisation
EP1993513A2 (en) * 2006-03-14 2008-11-26 Merck & Co., Inc. Processes and apparatuses for the production of crystalline organic microparticle compositions by micro-milling and crystallization on micro-seed and their use

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH98737A (de) * 1922-11-21 1923-04-16 Riser Christian Jaucherührwerk.
US1671291A (en) * 1927-03-04 1928-05-29 Ihlefeldt Johannes Multichamber mill for grinding materials of all kinds
US2091900A (en) * 1932-04-04 1937-08-31 Penick & Ford Ltd Inc Crystallizer apparatus
US3356532A (en) * 1963-01-11 1967-12-05 Andre Pierre Osmond Bizet Crystallization of sugar
FR1539106A (fr) * 1967-08-01 1968-09-13 Fives Lille Cail Installation à marche continue pour la production de cristaux à partir d'une solution du produit à cristalliser
US3506486A (en) * 1966-12-30 1970-04-14 Struthers Scient & Intern Corp Continuous crystallization

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH98737A (de) * 1922-11-21 1923-04-16 Riser Christian Jaucherührwerk.
US1671291A (en) * 1927-03-04 1928-05-29 Ihlefeldt Johannes Multichamber mill for grinding materials of all kinds
US2091900A (en) * 1932-04-04 1937-08-31 Penick & Ford Ltd Inc Crystallizer apparatus
US3356532A (en) * 1963-01-11 1967-12-05 Andre Pierre Osmond Bizet Crystallization of sugar
US3506486A (en) * 1966-12-30 1970-04-14 Struthers Scient & Intern Corp Continuous crystallization
FR1539106A (fr) * 1967-08-01 1968-09-13 Fives Lille Cail Installation à marche continue pour la production de cristaux à partir d'une solution du produit à cristalliser

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
Honig, Principles of Sugar Technology, Vol. II, pp. 279 82. Elsevier Pub. Co. 1959. *
P. Honig, Principles of Sugar Technology, Vol. II, pp. 286 296, Elsevier Pub. Co. 1959. *

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3996018A (en) * 1974-11-11 1976-12-07 Merck & Co., Inc. Crystallization system and method using crystal fracturing external to a crystallization column
US4145230A (en) * 1976-05-21 1979-03-20 Aktieselskabet De Danske Sukkerfabrikker Method for seeding super-saturated sugar solution to effect crystallization
US4164429A (en) * 1976-12-14 1979-08-14 Fives-Cail Babcock Process and installation for the production of selected crystallization seeds for use in a sugar refinery
US4518436A (en) * 1982-09-23 1985-05-21 Csm Suiker B.V. Process for the production of graft crystals for use in seeding sugar boiling brines
US5015297A (en) * 1985-05-15 1991-05-14 Roquette Freres Method and installation for the production of anhydrous crystalline fructose
FR2602153A1 (fr) * 1986-08-01 1988-02-05 Fives Cail Babcock Procede de production d'un magma d'ensemencement pour un appareil de cristallisation marche continue
EP0255786A1 (fr) * 1986-08-01 1988-02-10 FIVES-CAIL BABCOCK, Société Anonyme Procédé et installation pour la production d'un magma d'ensemencement pour un appareil de cristallisation à marche continue
AU591313B2 (en) * 1986-08-01 1989-11-30 Fives-Cail Babcock Method and equipment for production of a seeding magma for a continuous crystallization apparatus
WO2000056416A1 (de) * 1999-03-20 2000-09-28 Domo Caproleuna Gmbh Verfahren zur steuerung der kristallgrösse bei der kontinuierlichen massenkristallisation
EP1993513A2 (en) * 2006-03-14 2008-11-26 Merck & Co., Inc. Processes and apparatuses for the production of crystalline organic microparticle compositions by micro-milling and crystallization on micro-seed and their use
US20090087492A1 (en) * 2006-03-14 2009-04-02 Merck & Co., Inc. Processes and Apparatuses for the Production of Crystalline Organic Microparticle Compositions by Micro-Milling and Crystallization on Micro-Seed and Their Use
EP1993513A4 (en) * 2006-03-14 2012-06-27 Merck Sharp & Dohme METHOD AND DEVICE FOR PREPARING CRYSTALLINE ORGANIC MICROPARTICLE COMPOSITIONS USING MICROMATES AND CRYSTALLIZING MICROSAMEN AND THEIR USE

Also Published As

Publication number Publication date
IT1044186B (it) 1980-03-20
FR1597729A (pt) 1970-06-29
BE741840A (pt) 1970-05-04
DE1960646A1 (de) 1970-06-18
PL80373B1 (en) 1975-08-30
JPS5224107B1 (pt) 1977-06-29
NL6918348A (pt) 1970-06-09
DE1960646B2 (de) 1976-05-26
BR6914773D0 (pt) 1973-04-10
GB1244543A (en) 1971-09-02
NL151133B (nl) 1976-10-15
ES373898A1 (es) 1972-05-16

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