US3909287A - Recovery of sugar from clarifier scum by countercurrent extraction - Google Patents

Recovery of sugar from clarifier scum by countercurrent extraction Download PDF

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US3909287A
US3909287A US467662A US46766274A US3909287A US 3909287 A US3909287 A US 3909287A US 467662 A US467662 A US 467662A US 46766274 A US46766274 A US 46766274A US 3909287 A US3909287 A US 3909287A
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scum
sugar
mixture
clarifier
stage
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John Trethowan Rundell
Raymond George Bennett
Colin Vesty Rich
Paul Richmond Pottage
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Tate and Lyle PLC
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Tate and Lyle PLC
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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
    • C13B20/126—Organic agents, e.g. polyelectrolytes

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  • This invention relates to a process for the recovery of sucrose from clarifier scum obtained by the phosphatation process in sugar refining.
  • the production of sugar for human consumption generally comprises two distinct operations, namely the production of raw sugar and the production of refined sugar, which are often carried out in geographically separate locations.
  • Raw sugar is manufactured from raw juice", obtained from sugar cane or sugar beet, by clarification (i.e. removal of suspended solids), evaporation to a thick syrup, and crystallization. If special processing is introduced into these stages, the crystallized product can reach a standard suitable for direct consumption, and is then known as Mill White or Plantation White” sugar; but, generally, raw sugar must be refined before it reaches anacceptable standard of purity.
  • raw sugar is first washed and centrifuged to remove adherent syrup, and the affined sugar so produced is dissolved in water as melter liquor.
  • the melter liquor is then purified in two successive steps, the first of which is termed defecation" and prepares the liquor for the second step, which is termed decolorization.
  • the liquor produced by these successive steps is termed fine liquor; and refined sugar is obtained from fine liquor by crystallization.
  • the decolorization step may be omitted altogether.
  • the defecation step may comprise simple filtration through a bed of diatomaceous earth or another suitable filter aid; but, more generally, defecation involves an inorganic precipitation reaction, whereby insoluble and colloidal impurities are removed along with the inorganic precipitate.
  • the inorganic precipitate is calcium carbonate, formed in-situ by dissolving lime in the melter liquor and introducing carbon dioxide, for example in flue gas: the precipitate, which contains various impurities, is removed by filtration, the calcium carbonate acting as its own filter aid.
  • the inorganic precipitate is calcium sulphite, formed by the introduction of sulphur dioxide into limed melter liquor: the calcium sulphite is then removed by filtration, as in the carbonatation process. Sulphitation is often used in conjunction with carbonatation; and, because of the special effect of sulphur dioxide in preventing colour formation during the subsequent processing of the sugar liquor, a separate decolorization process is seldom necessary with this particular combination of defecation treatments.
  • the inorganic precipitate may be calcium phosphate, for example formed by the addition of lime and phosphoric acid to the melter liquor, in which case the process is termed phosphatation. This precipitate can also be removed by filtra-' tion, but large quantities of filter aid are required: consequently, it is more common to remove the calcium phosphate precipitate by flotation, in association with air bubbles.
  • the flocculent calcium phosphate precipitate is aerated and rises to the top of the liquor in a clarifier vessel, carrying with it various suspended impurities.
  • the calcium phosphate is removed as a scum from the top of the clarifier, and the clarified defecated liquor is removed from the bottom.
  • Many chemical additives have been recommended to aid the flotation separation of the phosphatation precipitate, including high molecular weight anionic polymers of the poly-acrylamide type, which increase the size of the floc and the retention of air bubbles within it.
  • the mere addition of such flocculants will not necessarily give rise to the efficient flocculation which is needed in order to achieve subsequent rapid and complete clarification of the liquor.
  • dissolved anionic high molecular weight impurities including the colorant impurities, can be precipitated from melter liquor by adding a cationic surfactant, which forms an insoluble complex with the impurities, the precipitated complex then being removed by a defecation treatment, such asphosphatation-flotation, along with the inorganic precipitate.
  • a problem which arises in all phosphatation-flotation processes is that an appreciable proportion'of the sugar is retained .in the clarifier scum.'In the conventional processes, typically about 4% by weight of the input sugar is present in the calcium phosphate scum removed fromthe. clarifier, and even in the improved processes described in our U.S. Pat. No. 3,698,951 and application Ser; No. 263,784 (now U.S. Pat. No. 3,853,616) about 2% by weight of the input sugar is present in the scum. For efficient and economical refinery operation, at least some of this sugar must be recovered, by desweetening the clarifier scum.
  • Desweetening water is plain water, for example steam condensate, or a dilute sugar solution from another sugar refining operation, characterized by an impurity content low enough for returning to the process stream.
  • the invention provides a continuous process for recovering sugar from the clarifier scum produced by phosphatation-flotation in sugar refining, which process comprises: subjecting the scum to at least two consecutive stages of counter-current aqueous extraction, wherein each extraction stage comprises the successive steps of a. dispersing the scum in desweetening water, to give a homogeneous mixture, and aerating the mixture,
  • step (e) of the first extraction stage passes the flocculated scum from step (e) of each except the last extraction stage to step (a) of the next extraction stage; passing the dilute sugar solution from step (e) of each except the first extraction stage to step (a) of the immediately preceding extraction stage, for use as desweetening water therein; discharging the flocculated scum from step (e) of the last extraction stage, as desweetened scum; and recovering the dilute sugar solution from step (e) of the first extraction stage.
  • the process of the invention is a multi-stage counter-current extraction, it achieves effective desweetening of the clarifier scum without producing inconveniently large volumes of dilute sugar solution.
  • the dilute sugar solution recovered from step (e) of the first extraction stage typically has a concentration of from to 20 Brix. This solution, known as sweetwater", can be recycled to the melter, where it is used to dissolve raw sugar and produce more melter liquor.
  • the sugar concentration in the dilute sugar solution removed from step (e) of the last extraction stage is typically from 0.2 to 2 Brix.
  • the residual sugar content in the desweetened scum removed from step (e) of the last extraction stage typically represents a loss of 0.05% by weight or less on the total sugar input to the refinery; and the desweetened scum can, therefore, be discarded without filtration or any other treatment.
  • the desweetening water used for step (a) of the last extraction stage is plain water, normally in the form of steam condensate provided from elsewhere in the refinery.
  • the scum In each extraction stage, the scum is first thoroughly mixed with and'dispersed in desweetening water. This is important, to ensure that the sugar is equilibrated throughout the system and not left trapped in the flocs.
  • the homogeneous mixture thus obtained must be thoroughly aerated.
  • the dispersion and aeration can be performed independently of each other, by conventional means. However, in accordance with a particularly preferred embodiment of the invention, homogeneous dispersion of the scum and aeration of the mixture are simultaneously performed in a mixing tank provided with an external recirculation loop which includes a power-driven high-speed high-shear aerator, with the injection of compressed air.
  • the mean residence time of the mixture in the mixing tank is preferably from 2 to 10 minutes.
  • the amount of air introduced is from 1% to 5% by volume, on the basis of the mixture volume; and the recirculation rate in the loop should be from 1 to 10 times the throughput in the mixing tank.
  • the aerator should operate with a rotor speed of not less than 2,500 r.p.m., and preferably at about 3,500 r.p.m.
  • a suitable aerator is available from the TALO Products and Processes Division of Tate & Lyle Enterprises Limited, London, England.
  • an organic polymeric flocculant is added to the aerated mixture.
  • polymeric flocculants are well known per se.
  • Particularly suitable are the high molecular weight anionic polyacrylamide flocculating agents (i.e. having a molecular weight of at least 1 million), especially those containing up to 20 mole percent of acrylic acid or sodium acrylate units, such as that available under the Trade Mark TALOFLOTE.
  • the flocculant should desirably be used in the form of a dilute aqueous solution, generally having a concentration of from 0.25 to 5.0, preferably 0.5 to 2.0, grams per litre, since a high dilution of the polymer molecules allows better utilization of the full activity of the flocculant.
  • the flocculant solution should not be subjected to vigorous mechanical treatment which can rupture the polymer molecules: instead, a streamof air bubbles or a paddle rotating at notmore than 200 r.p.m. can be used to dissolve the polymer.
  • the flocculant solution should be aged for a few hours before use, to aid dissolution, but should not be kept longer than about 3 days, otherwise hydrolysis and fragmentation of the polymer molecules can occur; generally, ageing for 2 to 3 hours is satisfactory.
  • the satisfactory distribution of the polymeric flocculant in the aerated mixture is also important; On the one hand, good distribution of the flocculant cannot be achieved by merely dosing it into a volume of the mixture; whilst, on the other hand, violent blending, such as produced in some inline mixers or by passing the mixture through a centrifugal pump, is also unsatisfactory.
  • violent blending such as produced in some inline mixers or by passing the mixture through a centrifugal pump, is also unsatisfactory.
  • completely homogeneous blending is undesirable; it is theorized that, with too thorough mixing, the flocculant molecules are lost within the growing flocs and can no longer gather together suspended solid particles, to form larger fiocs.
  • the degree of disbribution of the flocculant molecules in the mixture will depend on the intensity and duration of mixing.
  • the right degree of distribution is achieved by .a degree of turbulence corresponding to Reynolds numbers ranging from 7,000 to 70,000 at a sugar concentration of 20 Brix, and from 14,000 to 140,000 at sugar concentrations below 5 Brix.
  • this satisfactory distribution can be achieved by dosing the flocculant through a metering pump into the aerated mixture flowing with a linear velocity of from 30 to 300 cm. per second, preferably about 150 cm. per second, in a pipe of appropriate bore; but the right de gree of distribution can also be obtained in other ways, such as by causing the liquor to flow through apipe containing one or two right-angle bends in it.
  • the mixture then enters a clarifier, in which the flocculated scum is allowed'to segregate by flotation.
  • the mixture should enter the clarifier at a velocity not greater than 20 cm. per second, preferably not greater than cm. per second.
  • the flocculated scum floats to the top, and the clarified sweetwater is removed from the bottom.
  • the residence time in the clarifier is generally 5-10 minutes. The size of clarifier needed will obviously depend upon the volume of scum to be treated, which in turn depends on the throughput of the refinery, usually expressed in terms of the sugar melt rate.
  • the scum clarifiers will typically be cylindrical, with a height and diameter of about 150 cm. each.
  • the scum clarifiers can all be of the same size, irrespective of the number of extraction stages.
  • the temperature of the extraction process is not critical, but it is generally convenient to operate the process at a temperature of from 50 to 90C, and preferably at about 70C.
  • the temperature used is largely dictated by the requirements of the main refining process, in that the steam condensate fed to the last extraction stage will already be hot, and the sweetwater recovered from the first extraction stage should be hot for recycling to the melter.
  • 1 is a liquor clarifier of the TALO type. It comprises a central flocculator chamber 2, into which the aerated phosphated melter liquor is fed at 3. As the liquor rises in the flocculator chamber 2, it is kept gently stirred by the stirrer 4, allowing the flocs in it to grow. The liquor then flows into the separator chamber 5 which surrounds the flocculator chamber 2. In the separator chamber, the flocs rise to the top of the liquid as a scum, which is pushed into the annular trough 6 surrounding the top of the chamber by means of the slowly rotating scum rake 7. The clarified sugar liquor is removed from the bottom of the separator chamber via the liquid outlet 8.
  • the clarifier scum in the trough 6 is diluted with sweetwater from the pipe 9, and led via the pipe 10 into the first scum mixing tank 11 which is fitted with a baffle 12, dividing it into two compartments.
  • the flocs in the scum are broken up, the scum is uniformly dispersed in the desweetening water, and the mixture is simultaneously aerated by recirculation through the external loop containing the aerator l3, fed with compressed air from the maincompressed air line 14.
  • the aerated mixture flows out of the mixing tank 11 via pipe 15 into the first scum clarifier 16.
  • the mixture flows out of the mixing tank, it is dosed via pipe 17 with a solution of an organic polymeric flocculant.
  • This solution is supplied from holding tank 41 via metering pump 42.
  • the feed line 15 to the clarifier 16 contains right-angle bends in it, so as to provide the correct degree of turbulence in the mixture for uniform distribution of the flocculant solution.
  • the scum rises to the top and is pushed into the annular trough 18 by means of the slowly rotating scum rake 19.
  • the clarified sweetwater is removed from the bottom of the first scum clarifier via outlet 20, and flows via level control box 21 and pipe 22 to the sweetwater tank 23, from where it is removed to process as required.
  • the scum in the trough 18 of the first scum clarifier is diluted with water from the condensate tank 24, via the pump 25 and pipe 26.
  • the diluted scum then flows via pipe 27 into the second scum mixing tank 28 fitted with a baffle 29.
  • the scum is there treated in exactly the same manner as in the first scum mixing tank, being simultaneously dispersed and aerated by means of the aerator 30 fed with compressed air from the line 14.
  • the aerated mixture On leaving the second scum mixing tank, again typically after a residence time of 2-l0 minutes, the aerated mixture is dosed with a solution of organic polymeric fiocculant via pipe 31 (fed from flocculant holding tank 41 via metering pump 43), and flows through the pipe 32 having right-angle bends in it, into the second scum clarifier 33.
  • the scum rises to the top and is pushed into the annular trough 34 by means of the slowly rotating scum rake 35. From the trough 34, the now desweetened scum is discharged via pipe 36 into the scum tank 37, for eventual disposal.
  • the clarified sweetwater flows from the bottom of the second scum clarifier via outlet 38 and level control box 39 to pump 40, from which it is recycled via the pipe 9 to the annular trough 6 on the main clarifier l, to dilute the scum fed to the first scum mixing tank.
  • the number of extraction stages and degree of scum dilution in each stage will depend upon the specific conditions and requirements of the particular refinery, especially the level of sugar loss which is acceptable, the quantity and quality of desweetening water available, and the quantity and quality of sweetwater which can be accommodated back in the process, for example for recycling to the melter.
  • two stages of extraction with a relatively high degree of dilution will be adequate, but three stages of extraction with a lower degree of dilution will sometimes be necessary.
  • the following typical performance data are given to illustrate how operating conditions may be chosen to suit different refinery conditions and requirements.
  • Table 1 shows how the sugar loss, expressed as a percentage of the refinery melt solids throughput, varies with the sugar concentration in the water present in the desweetened scum discarded from the last extraction stage of the process. Of course, this is precisely the I same as the sugar concentration in the clarified sweetwater removed from that stage, which is recycled for use as desweetening water to the previous extraction stage.
  • These data are based on operating results obtained from a refinery having a sugar melt solids throughput of 10 tons per hour (corresponding to 220 tons per day refined sugar production), operating at a P level of 0.03% on melt solids, producing a mean volume of 385 liters per hour of final discard scum with a water content of 75%.
  • the loss values shown are independent of the sugar content of the input scum, ob-
  • Table 1 Sugar concentration of water in discard scum Brix) Sugar loss by weight of refinery melt solids)
  • the relationship between the scum dilution ratio and the sugar concentration of the sweetwater obtained from each extraction stage is shown in Tables 2 and 3, respectively for a two-stage and a three-stage process.
  • the scum dilution ratio is the weight ratio of input desweetening water (normally steam condensate, and therefore assumed to have zero sugar concentration) to input scum (obtained from the liquor clarifier). It is assumed that the liquor present in the input scum has a sugar concentration of 65 Brix, which is a typical value.
  • Tables 2 and 3 give data for input scums containing 2% and 4% by weight of refinery melt sugar solids, representing scum obtained from liquor clarifiers oper- As an example of how these data can be used in practice, it will be assumed that the maximum acceptable sugar loss in a particular refinery is set at 0.04% by weight of total melt solids. Reference to Table 1 shows that the sugar concentration of the water in the discard scum, and hence of the sweetwater from the final extraction stage, should not exceed l.5 Brix.
  • Table 2 shows that the sugar loss target can be achieved with a two-stage desweetening process operating at a scum dilution ratio of about 4:1, while Table 3 shows that the same target can be achieved with a three-stage desweetening process operating at a scum dilution ratio of about 3:1.
  • Table 2 shows that the sugar loss target can be achieved with a two-stage desweetening process operating at a scum dilution ratio of 7:1, while Table 3 shows that the same target can also be achieved with a three-stage desweetening process operating at a scum dilution ratio of about 3.5:1.
  • Tables 2 and 3 also show the sugar concentration of the sweetwater recycled to the melter, in the columns for Extraction Stage I, and the volume of this sweetwater can be calculated. Thus, the optimum operating conditions can be selected for any particular refinery.
  • Table 4 shows the relationship between the scum dilution ratio and sweetwater sugar concentration in a desweetening process comprising a single extraction stage (and consequently outside the scope of the present invention), but otherwise operated under the same conditions as the processes of Tables 2 and 3. It will be noted that the sugar concentration in the sweetwater corresponds to unacceptably large sugar losses. In order to achieve the sugar loss target of 0.04% by weight exemplified abovej Table 4 would have to be extended to coversciim dilution ratios up to 15:1 or even 20:1, which are impractically large.
  • Table 4 Single-stage desweetening process The invention is illustrated by the following Examples, all of which make use of the two-stage desweetening process shown in the drawing. ln all of the Examples, the TALOFLOTE" flocculating agent was used in the form of an aqueous solution having a concentration of 1 gram per liter.
  • EXAMPLE 1 A phosphatation refinery having a melt solids throughput of 10 tons per hour operated at a P 9 level of 0.03% by weight on melt solids, using a single TALO liquor clarifier, with a clarified liquor sugar concentration of 65 Brix and a scum pH of 7.0-7.5.
  • the two-stage desweetening process of the invention was installed in this refinery, using 4,000 liters per hour of desweetening water.
  • the amount of air introduced at each extraction stage was 3% by volume; and the aerated mixture in each stage was closed with 1.2 parts by weight of TALOFLOTE flocculating agent per million parts by weight of melt solids throughput.
  • the last stage produced 400 liters per hour of discard scum, the water in which had a sugar concentration not exceeding 0.2 Brix, representing a sugar loss not greater than 0.006% by weight of refinery melt solids throughput.
  • the first stage produced 3,800 liters per hour of sweetwater having a sugar concentration of 8-l2 Brix, for return to the melter.
  • EXAMPLE 2 A phosphatation refinery having a melt solids throughput of 13 tons per hour operated at a P level of 0.02% by weight on melt solids, using two Williamson liquor clarifiers, with a clarified liquor sugar concentration of 65 Brix and a scum pH of 6.9-7.1.
  • the two-stage desweetening process of the invention was installed in this refinery, using 3,200 liters per hour of desweetening water.
  • the amount of air introduced at each Stage was 2% by volume; and the aerated mixture in each stage was dosed with 1.3 parts by weight ofTALOFLOTE flocculating agent per million parts by weight of melt solids throughput.
  • the first extraction stage gave 3,000 liters per hour of sweetwater having a sugar concentration of l0-15 Brix, for return to the rnelte'r; and the second stage produced 389 liters per hour of dis'card scum, the water in which'had a su'gar'concentration not greater than 0.2 Brix, representin g a sugar loss of not more than 0.006% by weight v of refinery' melt solids.
  • a phosphatation refinery had a melt solids throughputfof 36 tonsper' hour, operating at a P 0 levelof 0.02% by weight on melt solid s, using two Bulkleyljunton liquor clarifiers, with a clarified liquor sugar concentration of Brix and a scum pH of 6.8-7.2.
  • the two-stage desweetening process of the invention was installed in this refinery, with 8,000 liters per hour of desweetening water supplied to the first stage.
  • EXAMPLE 4 A phosphatation refinery had a melt solids throughput of tons per hour, operating at a P 0 level of 0.02% by weight on melt solids, using two TALO clarifiers, with a clarified liquor sugar concentration of 65 Brix and a scum pH of 6.8-7.1.
  • the two-stage desweetening process of the invention was installed in this refinery, with 16,000 liters per hour of desweetening water supplied to the first stage.
  • the amount of air introduced at each stage was 2% by volume, and in each stage the aerated mixture was dosed with 0.7 part by weight ofTALOFLOTE flocculating agent per million parts by weight of melt solids throughput.
  • the first stage produced 15,000 liters per hour of sweetwater having a sugar concentration of 8-14 Brix, for return to the melter; and the second stage produced'2,400 liters per hour of discard scum, the water in which had a sugar concentration not higher than 02 Brix, representing a sugar loss of not more than 0.006% by weight of refinery melt solids.
  • a continuous process for recovering sugar from the clarifier scum produced by phosphatation-flotation in sugar'refining comprises: subjecting the scum to at least two consecutive stages of countercurrent aqueous extraction, wherein each extraction stage comprises the successive steps of a. dispersing the scum in desweetening water, to give a homogeneous mixture, and aerating the mixture,
  • step (e) of the last extraction stage discharging the flocculated scum from step (e) of the last extraction stage, as desweetened scum; and recovering the dilute sugar solution from step (e) of the first extraction stage.
  • step (a) of at least one of the said stages of counter-current extraction the homogeneous dispersion of the scum and aeration of the mixture are simultaneously performed in a mixing tank provided with an external recirculation loop which includes a power-driven aerator, with injection of compressed air.
  • step (b) of each of the said stages of counter-current extraction there are distributed from 0.1 to 5.0 parts by weightof said flocculant permillion parts by weight of melt sugar solids throughput in the refinery.
  • step (b) of each of the said stages of counter-current extraction there are distributed from 0.5 to 2.0 parts by weight of said flocculant per million parts by weight of melt sugar solids throughput in the refinery.
  • said flocculant is an anionic polyacrylamide flocculating agent having a molecular weight of at least one million and containing up to mole percent of anionic units selected from the group consisting of acrylic acid and sodium acrylate units.

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  • Chemical & Material Sciences (AREA)
  • Electrochemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
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Cited By (19)

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US4207185A (en) * 1977-04-18 1980-06-10 Chevron Research Company Method for purifying liquids
US4234350A (en) * 1979-05-07 1980-11-18 Davies Hamakua Sugar Co., A Division Of Theo. H. Davies, Ltd. Process for the purification of evaporated sugar solutions
US4234349A (en) * 1979-04-16 1980-11-18 Davies Hamakua Sugar Co., A Division Of Theo. H. Davies, Ltd. Apparatus for the purification of evaporated sugar solutions
US4263052A (en) * 1979-10-12 1981-04-21 American Crystal Sugar Company Production of fructose and useful by-products
US4288551A (en) * 1980-03-10 1981-09-08 The Coca-Cola Company Process for the purification of sugar syrups
US4345947A (en) * 1981-04-28 1982-08-24 Tate & Lyle Limited Clarification of glucose syrups
US4382823A (en) * 1981-09-24 1983-05-10 The Coca Cola Company Process for the purification of sugar syrups
US4441993A (en) * 1975-11-03 1984-04-10 Fluor Corporation Flotation process
US4478645A (en) * 1981-09-24 1984-10-23 The Coca-Cola Company Process for the purification of sugar syrups
US5281279A (en) * 1991-11-04 1994-01-25 Gil Enrique G Process for producing refined sugar from raw juices
US6146465A (en) * 1999-01-13 2000-11-14 Betzdearborn Inc. Methods for clarifying sugar solutions
US6159302A (en) * 1999-01-13 2000-12-12 Betzdearborn Inc. Neutral phosphate pre-coagulant composition for clarification in white sugar production
US20090145426A1 (en) * 2004-11-24 2009-06-11 Fernando Cesar Boscariol Refined sugar manufacturing process
US20110108021A1 (en) * 2009-11-11 2011-05-12 Carbo-UA Limited Compositions and processes for sugar treatment
WO2011060168A1 (en) * 2009-11-11 2011-05-19 Carbo-UA Limited Compositions and processes for improving phosphatation clarification of sugar liquors and syrups
WO2011060169A1 (en) * 2009-11-11 2011-05-19 Carbo-UA Limited Compositions and processes for improving carbonatation clarification of sugar liquors and syrups
US20110174303A1 (en) * 2009-12-23 2011-07-21 Carbo-UA Limited Compositions and processes for clarification of sugar juices and syrups in sugar mills
GB2522777A (en) * 2013-12-23 2015-08-05 T & L Sugars Ltd Novel purification processes
CN108107737A (zh) * 2017-12-28 2018-06-01 广西大学 基于熵最小的蔗汁澄清过程的协同优化方法

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GB2136446B (en) * 1983-03-15 1986-09-17 Coca Cola Co Purification of sugar syrups
JPH0670844A (ja) * 1992-08-28 1994-03-15 Osaka Gokou:Kk 茹麺機
RU2728610C1 (ru) * 2020-01-16 2020-07-30 Федеральное государственное бюджетное образовательное учреждение высшего образования "Кубанский государственный аграрный университет имени И.Т. Трубилина" Клеровочный аппарат непрерывного действия
CN112237986A (zh) * 2020-11-12 2021-01-19 力上资源科技开发有限公司 矿物浮选方法

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US3166442A (en) * 1963-05-23 1965-01-19 Minerals & Chem Philipp Corp Method for treating sugar liquor
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US3698951A (en) * 1967-09-29 1972-10-17 Tate & Lyle Ltd Sugar refining
US3853616A (en) * 1971-06-22 1974-12-10 Tate & Lyle Ltd Separation of suspended solids from liquids

Cited By (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4441993A (en) * 1975-11-03 1984-04-10 Fluor Corporation Flotation process
US4207185A (en) * 1977-04-18 1980-06-10 Chevron Research Company Method for purifying liquids
US4234349A (en) * 1979-04-16 1980-11-18 Davies Hamakua Sugar Co., A Division Of Theo. H. Davies, Ltd. Apparatus for the purification of evaporated sugar solutions
US4234350A (en) * 1979-05-07 1980-11-18 Davies Hamakua Sugar Co., A Division Of Theo. H. Davies, Ltd. Process for the purification of evaporated sugar solutions
US4263052A (en) * 1979-10-12 1981-04-21 American Crystal Sugar Company Production of fructose and useful by-products
US4288551A (en) * 1980-03-10 1981-09-08 The Coca-Cola Company Process for the purification of sugar syrups
US4345947A (en) * 1981-04-28 1982-08-24 Tate & Lyle Limited Clarification of glucose syrups
US4382823A (en) * 1981-09-24 1983-05-10 The Coca Cola Company Process for the purification of sugar syrups
US4478645A (en) * 1981-09-24 1984-10-23 The Coca-Cola Company Process for the purification of sugar syrups
US5281279A (en) * 1991-11-04 1994-01-25 Gil Enrique G Process for producing refined sugar from raw juices
US6146465A (en) * 1999-01-13 2000-11-14 Betzdearborn Inc. Methods for clarifying sugar solutions
US6159302A (en) * 1999-01-13 2000-12-12 Betzdearborn Inc. Neutral phosphate pre-coagulant composition for clarification in white sugar production
US20090145426A1 (en) * 2004-11-24 2009-06-11 Fernando Cesar Boscariol Refined sugar manufacturing process
WO2011060168A1 (en) * 2009-11-11 2011-05-19 Carbo-UA Limited Compositions and processes for improving phosphatation clarification of sugar liquors and syrups
US8486474B2 (en) 2009-11-11 2013-07-16 Carbo-UA Limited Compositions and processes for improving carbonatation clarification of sugar liquors and syrups
WO2011060169A1 (en) * 2009-11-11 2011-05-19 Carbo-UA Limited Compositions and processes for improving carbonatation clarification of sugar liquors and syrups
US20110165303A1 (en) * 2009-11-11 2011-07-07 Carbo-UA Limited Compositions and processes for improving carbonatation clarification of sugar liquors and syrups
US20110165302A1 (en) * 2009-11-11 2011-07-07 Carbo-UA Limited Compositions and processes for improving phosphatation clarification of sugar liquors and syrups
US9175358B2 (en) 2009-11-11 2015-11-03 Carbo-UA Limited Compositions and processes for sugar treatment
US8486473B2 (en) 2009-11-11 2013-07-16 Carbo-UA Limited Compositions and processes for improving phosphatation clarification of sugar liquors and syrups
US20110108021A1 (en) * 2009-11-11 2011-05-12 Carbo-UA Limited Compositions and processes for sugar treatment
US9163292B2 (en) 2009-11-11 2015-10-20 Carbo-UA Limited Compositions and process for improving carbonatation clarification of sugar liquors and syrups
US9163293B2 (en) 2009-11-11 2015-10-20 Carbo-UA Limited Compositions and processes for improving phosphatation clarification of sugar liquors and syrups
US20110174303A1 (en) * 2009-12-23 2011-07-21 Carbo-UA Limited Compositions and processes for clarification of sugar juices and syrups in sugar mills
US9605324B2 (en) 2009-12-23 2017-03-28 Carbo-UA Limited Compositions and processes for clarification of sugar juices and syrups in sugar mills
GB2522777A (en) * 2013-12-23 2015-08-05 T & L Sugars Ltd Novel purification processes
US9976193B2 (en) 2013-12-23 2018-05-22 T&L Sugars Limited Purification processes
CN108107737A (zh) * 2017-12-28 2018-06-01 广西大学 基于熵最小的蔗汁澄清过程的协同优化方法

Also Published As

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DE2422889A1 (de) 1974-11-28
ZA742821B (en) 1975-05-28
JPS5029759A (es) 1975-03-25
GB1417344A (en) 1975-12-10
DE2422889B2 (de) 1978-03-23
FR2228840B1 (es) 1977-10-21
IT1020606B (it) 1977-12-30
AU6886974A (en) 1975-11-13
JPS572000B2 (es) 1982-01-13
DE2422889C3 (de) 1978-11-16
CA1009651A (en) 1977-05-03
SU656535A3 (ru) 1979-04-05
FR2228840A1 (es) 1974-12-06
AU476186B2 (en) 1976-09-16
AR198925A1 (es) 1974-07-24

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