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EP2292803B1 - Trennungsverfahren - Google Patents

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Publication number
EP2292803B1
EP2292803B1 EP20090164728 EP09164728A EP2292803B1 EP 2292803 B1 EP2292803 B1 EP 2292803B1 EP 20090164728 EP20090164728 EP 20090164728 EP 09164728 A EP09164728 A EP 09164728A EP 2292803 B1 EP2292803 B1 EP 2292803B1
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Prior art keywords
fructose
crystallization
fraction
glucose
cation exchange
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English (en)
French (fr)
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EP2292803A1 (de
Inventor
Heikki Heikkilä
Jari Lewandowski
Juha Nurmi
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DuPont Nutrition Biosciences ApS
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DuPont Nutrition Biosciences ApS
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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
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
    • C13B35/00—Extraction of sucrose from molasses
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K11/00—Fructose

Definitions

  • the present invention relates to an improved process of producing crystalline fructose.
  • the process is based on chromatographic fractionation of fructose crystallization run-offs with cation exchange resins in two different ion forms and introduction of the fructose fractions thus obtained into further crystallization for the production of crystalline fructose.
  • US Patent 3 692 582 Melaja, A.J. (publ. 19 September 1972) discloses a chromatographic process of separating fructose from an invert sugar solution with a cation exchange resin in an alkaline earth metal salt form, such as a calcium form.
  • a glucose-rich fraction, a fraction containing glucose and fructose as well as a fructose-rich fraction are recovered.
  • the fraction containing glucose and fructose may be returned to the feed for diluting the invert sugar feed solution.
  • the purity of the fructose fraction may be 95-97%.
  • the fructose fraction may be evaporated and fructose crystallized therefrom.
  • US Patent 3 883 365, Suomen Sokeri Osakeyhtiö, Forsberg, H. et al. (publ. 13 May 1975) relates to a method of crystallizing fructose at a pH in the range of 4.5 to 5.5 from an aqueous solution containing glucose as an impurity.
  • the solution to be crystallized contains at least about 90% dry substance, the fructose content of the dry substance being at least about 90% by weight.
  • the crystallization may be carried in two or more steps. It is also recited in the reference that difructoses and difructose anhydrides are believed to be actual crystallization inhibitors.
  • US Patent 3 928 062 Daiichi Kogyo Seiayku Co., Ltd (publ. 23 December 1975) discloses a process for obtaining anhydrous fructose crystals without the formation of fructose hemihydrate or fructose dihydrate crystals from an aqueous fructose solution, whereby it is essential that the crystallization is carried out within a certain range of fructose concentration and temperature.
  • the starting fructose solutions include those obtained from the inversion of sucrose or from the isomerization of glucose, optionally pretreated by concentration, dilution, heating or cooling. It is recited that the starting fructose solution may also be a mother liquor from a previous crystallization cycle.
  • US Patent 4 634 472 discloses a process for manufacturing an enriched fructose syrup.
  • dextrose is crystallized from a relatively high solids feed syrup (a dry solids content between about 75 and 89 percent) containing fructose and dextrose.
  • a relatively high solids feed syrup a dry solids content between about 75 and 89 percent
  • another relatively dilute (or low solids) fructose containing diluent syrup is added to enhance separation of the dextrose crystals from the mother liquor.
  • US Patent 5 230 742 , A.E. Staley Manufacturing Co. (publ. 27 July 1993) and US Patent 5 234 503 , A.E. Staley Manufacturing Co. (publ. 10 August 1993) disclose an integrated process for producing crystalline fructose and high-fructose liquid-phase sweetener (such as a high fructose corn syrup) from a feed stream comprising dextrose. A portion of the dextrose in the feed stream is isomerized to fructose and the resulting dextrose/fructose stream is fractionated to produce a high fructose stream.
  • high-fructose liquid-phase sweetener such as a high fructose corn syrup
  • a portion of the fructose in the high fructose stream is crystallized out and the mother liquor remaining after crystallization is blended with dextrose-containing streams to produce the liquid-phase sweetener. It is recited that the fractionation may be carried out in a chromatographic column with a polystyrene sulfonate cation resin using calcium as the preferred salt form.
  • US 4 938 804 Suomen Sokeri Oy, Heikkilä et al. (publ. 3 July 1990) relates to a process of producing crystalline fructose by adding ethanol to a concentrated fructose syrup to form an ethanol-water azeotrope, supersaturating the solution, seeding the solution with fructose seed crystals and removing the ethanol-water azeotrope under reduced pressure to crystallize fructose.
  • the crystalline fructose is separated from the crystallization mother liquor.
  • the spent mother liquor is recovered and distilled to recover ethanol.
  • the hydrolysis is carried out by an invertase enzyme immobilized on a solid carrier, followed by separating a glucose fraction and a fructose fraction from the hydrolysis product by chromatographic simulated moving-bed process.
  • the chromatographic separation is typically carried out with a strongly acid cation exchange resin, which is preferably in calcium form. Fructose and glucose may then be crystallized from the fructose and glucose fractions obtained from the separation.
  • US Patent 6 206 977 B1 Danisco Finland Oy, Heikkilä et al. (publ. 27 March 2001) relates to a method of crystallizing anhydrous fructose from water by a cooling crystallization process, where the temperature difference between the solution and the cooling elements is maintained at a value of less than about 10°C and the supersaturation of the solution with respect to saturated fructose is maintained at a ratio between 1.1. and 1.25.
  • the crystallization is carried out from an aqueous solution containing at least about 90% dry substance, which has a fructose content of at least about 90% by weight.
  • US Patent 6 607 603 B1 discloses a process for manufacturing crystallized fructose by preparing a pure fructose syrup by melting fructose dihydrate crystals, concentrating the melt to a dry matter content above 96% by weight, seeding the concentrated syrup with fructose seed crystals and solidifying the seeded syrup.
  • the crystallization mother liquor may be submitted to a new crystallization stage.
  • US 6 924 371 B2 relates to a chromatographic process of separating hydrophilic carbohydrates from hydrophobic carbohydrates with a weak acid cation exchange resin.
  • Example 7 of the reference discloses chromatographic separation of a fructose crystallization run-off with a weak acid cation exchange resin in Na + -form. It is recited in the reference that the resin separates well fructose and oligosaccharides formed in thermal acid breakdown of fructose. It is also recited that oligosaccharides are eluted from the column faster than fructose.
  • US 7 150 794 B2 Getec Guanabara Quimica Industrial S.A. (published 25 November 2004) discloses a process for the production of crystalline fructose, comprising (a) hydrolysis of an aqueous solution of sucrose to produce a solution of fructose and glucose, (b) chromatographing the solution of fructose and glucose to yield a solution having a fructose content between 84% and 90% and concentrating the solution to a dry solids concentration of at least 92% by weight, (c) rapidly cooling the syrup thus obtained and seeding the syrup with fructose seed crystals to obtain a massecuite, (d) subjecting the massecuite to controlled slow cooling, (e) adding absolute ethanol, (f) subjecting the massecuite to slow cooling and (g) separating the fructose crystals.
  • the chromatographic separation step is carried out with a cation exchange resin.
  • the ethanol-containing crystallization mother liquor is subjected to evaporation, until complete removal of ethanol is achieved.
  • the mother liquor thus obtained is a valuable fructose-containing by-product and can be used for example as a fructose-rich syrup or for the production of mannitol and sorbitol.
  • US Patent 7 314 528 discloses a process of removing crystallization inhibitors from a solution comprising one or more reducing sugars, such as fructose, by subjecting the solution to one or more purification steps selected from nanofiltration, hydrolysis and chromatography. After the purification, the solution is subjected to crystallization. It is recited in the reference that the starting solution may also be a mother liquor obtained from the crystallization of fructose. Furthermore, Example 5 discloses the purification of a fructose run-off by nanofiltration to provide a purified fructose-rich nanofiltration permeate, followed by crystallization of fructose from the purified nanofiltration permeate.
  • US 5 730 877 , Xyrofin Oy (publ. 24 March 1998) discloses a method for fractionating a solution by a simulated moving bed chromatographic separation system comprising at least two packing material beds in different ionic forms.
  • One of the ion forms may be a divalent cation, such as Ca 2+
  • the other may a monovalent cation, such as Na + .
  • Example 6 discloses two-phase separation of maltose, glucose and fructose with a five-column system where the first column is in Na + form and the next four columns are in Ca 2+ form. A maltose fraction was withdrawn from the first column and a glucose fraction and a fructose fraction were withdrawn from the third and fifth column. Crystallization of the fructose fraction is not disclosed.
  • US 6 896 811 B2 discloses a chromatographic SMB fractionation process, where the separation profile passes more than once or less than once through the separation loop during each separation cycle.
  • the solution to be separated may be a fructose syrup, for example.
  • Example 4 of the US patent discloses separation of fructose syryp by a separation system, which comprised two columns containing a strong acid cation exchange resin in a Ca 2+ form as the column filling material. One fructose-containing fraction was drawn from both columns. Crystallization of the fructose fractions is not disclosed.
  • One of the problems associated with conventional fructose crystallization methods relates to the presence of crystallization inhibitors, especially dimeric sugars of fructose, in the crystallization.
  • the formation of dimeric sugars is especially accelerated in prolonged heating of a concentrated fructose solution in an acidic environment.
  • Dimeric sugars having an inhibiting effect on the crystallization of fructose are formed in the enzymatic or acid inversion of sucrose to a mixture of fructose and glucose, in the enzymatic isomerization of glucose to fructose and in the crystallization process itself especially during evaporation.
  • the presence of dimeric sugars and other impurities in the crystallization of fructose leads to lower process yields.
  • the presence and formation of dimeric sugars in the crystallization of fructose is discussed for example in the Example at columns 17 and 18 of US 5 234 503 (see especially Table III).
  • Another problem associated with conventional fructose crystallization methods relates to a low overall yield of crystalline fructose from the fructose feed solution for the reason that fructose has not as a rule been recovered by crystallization from crystallization run-offs because of a low yield due to dimeric crystallization inhibitors such as difructose dianhydrides, which are concentrated into the run-offs. Instead, the run-offs have conventionally been used for preparing liquid fructose syrups, for example.
  • the object of the invention is achieved by a process which is characterized by what is stated in the independent claim.
  • the preferred embodiments of the invention are disclosed in the dependent claims.
  • the invention is based on the treatment of fructose crystallization run-offs by a chromatographic fractionation with cation exchange resins in two different ion forms and introduction of the fructose fractions thus obtained into further crystallization for the production of further crystalline fructose.
  • the process of the invention provides an improved overall yield of crystalline fructose calculated on the basis of the fructose source as well as on the basis of fructose in the crystallization batch.
  • the present invention relates to a process of producing crystalline fructose with a high overall yield of crystalline fructose from the starting material of a fructose process and from the crystallization feed.
  • the process of the invention comprises, as characteristic elements, the following steps:
  • the crystallization as such is carried out by conventional methods known in the art for the crystallization of fructose, advantageously by cooling crystallization or by other methods such as boiling crystallization, or precipitation crystallization, or a combination thereof. Seeding of the crystallization mass may be used, if desired.
  • the crystallization may be carried out in water, but an alcohol, such as ethanol, or a mixture of water and alcohol, can also be used.
  • the crystallization is preferably carried out at a pH in the range of 4.5 to 5.5.
  • the crystals are separated from the crystallization massecuite for instance by centrifugation or filtering to provide crystalline fructose and a fructose run-off.
  • Said one or more crystallization steps provide crystalline fructose and a fructose run-off, which can be crystallized to provide further crystalline fructose and a further fructose run-off.
  • the crystallization run-offs contain high amounts of fructose as well as reasonable amounts of glucose and disaccharides.
  • the crystallization run-offs may contain 88 to 96% of fructose, 2 to 5% of disaccharides and 1 to 8% of glucose, based on the dry substance content (DS) of the run-offs.
  • Disaccharides especially fructose dimers, act as crystallization inhibitors in the crystallization of fructose, whereby they should be removed as efficiently as possible from the crystallization run-offs before subsequent recovery of fructose by further crystallization.
  • a separation system which comprises two or more cation exchange resin beds, whereby at least one of said cation exchange resin beds is in a Ca 2+ form and at least one of said cation exchange resin beds is in a monovalent cation form.
  • the resin in a monovalent cation form may be in a Na + form or K + form, for example.
  • the chromatographic fractionation by the separation system described above provides from the fructose run-off a fructose fraction, which contains 94 to 98% of fructose, less than 3%, preferably less than 2% of disaccharides and less than 1.5%, preferably less than 1.0% of glucose on DS.
  • Said disaccharides existing in the fructose run-offs may be fructose dimers, degradation products of starch, such as maltose or isomaltose or a residue of raw material such as saccharose.
  • said disaccharides are especially selected from disaccharides A and disaccharides B, which are mainly composed of fructose dimers, such as difructose dianhydrides.
  • Fructose dimers have been formed in acidic conditions, in a concentrated fructose solution in enzymatic conversions (inversion, isomerization), in acidic inversion of saccharose and during the crystallization process of fructose.
  • Fructose dimers such as difructose dianhydrides include various difructose anhydrides and various diheterolevulosans, which have been formed from the polymerization of fructose during a prolonged treatment of fructose in a concentrated form in acid or alkaline conditions.
  • Disaccharides may be analyzed by HPLC with a Na + -form resin using water as an eluant.
  • the elution order of disaccharides in the HPLC-diagram is saccharose (similar retention time also for maltose and isomaltose), disaccharides B, disaccharides A, glucose and fructose.
  • Disaccharides A and B show two separate peaks in the HPLC diagram.
  • HPLC-peaks for disaccharides A and B mainly consist of different difructose dianhydrides, which are considered to be more harmful crystallization inhibitors than the other type of disaccharides such as saccharose, maltose or isomaltose.
  • the disaccharide A type of difructose dianhydrides is more difficult to remove from a fructose run-off solution by chromatographic separation than disaccharides B.
  • Inventors have surprisingly discovered that the disaccharide A type of difructose dianhydrides can be efficiently separated from fructose solution using a cation exchange resin in a monovalent form in the chromatographic separation.
  • the cation exchange resin may be a strong or weak cation exchange resin.
  • Especially advantageous removal of disaccharides A, disaccharides B and glucose and low loss of fructose can been achieved when using cation exchange resin beds in Ca 2+ - form and Na + -form consecutively.
  • the fructose fraction obtained from the chromatographic fractionation of the invention typically comprises less than 1.5%, preferably less than 1.0% of disaccharides A and less than 1.5%, preferably less than 0.8% of disaccharides B on DS.
  • a typical range for disaccharides A is 0.5 to 1% on DS and for disaccharides B 0.5 to 0.8% on DS.
  • Said at least one other fraction in the chromatographic fractionation of fructose run-off may be a residue fraction enriched in fructose dimers. Consequently, in addition to the fructose fraction, which is depleted in fructose dimers (disaccharides A and B), a residue fraction can be obtained, which is enriched in fructose dimers (disaccharides A and B).
  • the fructose fraction depleted in fructose dimers (disaccharides A and B) typically comprises less than 1.5%, preferably less than 1.0% disaccharides A and less than 1.5%, preferably less than 0.8% disaccharides B on DS.
  • the residue fraction enriched in fructose dimers typically contains 2 to 8%, preferably 4 to 8% disaccharides A and 3 to 10%, preferably 8 to 10% disaccharides B on DS.
  • the chromatographic separation system used in the process of the present invention comprises two or more cation exchange resin beds, whereby at least one of the resin beds in a Ca 2+ form and at least one of the resin beds is in a monovalent cation form.
  • At least 20% of the total length of the resin beds of the separation system is in a Ca 2+ form. In another embodiment of the invention, at least 20% of the total length of the resin beds of the separation system is in a monovalent cation form.
  • the relation between the length of the Ca 2+ resin bed/beds and the other resin bed/beds may be adjusted depending on the content of disaccharides A and B and glucose in the fructose crystallization run-off used as the feed for the chromatographic fractionation. Consequently, in a further embodiment of the invention, when the feed contains less than 2% disaccharides A and B on DS and more than 3% glucose on DS, 60 to 80% of the total length of the resin beds of the separation system may be in a Ca 2+ form. In another embodiment of the invention, when the feed contains more than 3% disaccharides on DS and less than 2% glucose on DS, 60 to 80% of the total length of the resin beds may be in a monovalent cation form.
  • Said two or more cation exchange resin beds of the separation system are preferably composed of strongly acid cation exchange resins.
  • the resins have typically a styrene skeleton, which is preferably cross-linked with divinylbenzene.
  • Said two or more cation exchange resin beds may also comprise a weakly acid cation exchange resin.
  • the weakly acid cation exchange resin may be in a free acid form, for example.
  • Said two or more cation exchange resin beds may be arranged in series or in parallel.
  • the chromatographic fractionation in accordance with the present invention may be carried out with a batch process or a simulated moving bed process (SMB process).
  • the simulated moving bed process may be continuous or sequential.
  • the temperature of the chromatographic fractionation is typically in the range of 20 to 90°C, preferably 40 to 65°C.
  • the pH of the solution to be fractionated is typically in the range of pH 3 to pH 6, preferably in the range of pH 4 to pH 5 to minimize further formation of fructose-based disaccharides.
  • the chromatographic fractionation provides the fructose fraction with a fructose yield of more than 80%, preferably more than 90% and with an especially preferred fructose yield of more than 95% based on fructose in the fructose crystallization run-off used as the feed in the chromatographic fractionation.
  • the amount of disaccharides A is reduced to a level of less than 60% and the amount of disaccharides B is reduced to a level less of than 40% based on the disaccharide A or B content in the fructose run-off.
  • the fructose fraction obtained from the chromatographic fractionation has a typical fructose purity of more than 93%, preferably more than 95% and more preferably more than 97%, based on dissolved dry substance (DS).
  • the removal of disaccharides B is as a rule more efficient than the removal of disaccharides A.
  • the residue fraction obtained from the chromatographic fractionation of the fructose crystallization run-off with the process of the invention contains fructose in an amount of 45 to 65% on DS, glucose in an amount of 10 to 30% on DS, preferably 20 to 30% on DS, disaccharides A in an amount of 2 to 8% on DS, preferably 4 to 8% on DS, disaccharides B in an amount of 3 to 10% on DS, preferably 8 to 10% on DS.
  • the dry substance yield to the residue fraction represents 5 to 15 weight-%, preferably 5 to 8 weight-% of the run-off.
  • Typical yield of crystalline fructose in a single pass (no previous crystallizations) in the crystallization of a solution containing over 95% fructose on DS is in the range of 40-55%, normally about 45% of the fructose in the feed.
  • the yield of crystalline fructose in a second pass is less than 90% of the yield of the first pass. Also a much longer time is required for the crystallization of the second pass due to the crystallization inhibitors.
  • the efficient removal of the crystallization inhibitors with the method of the invention facilitates the overall crystallization yield of the crystalline fructose to be more than 90%, preferably more than 93% and most preferably over 95%, based on the fructose in the crystallization feed.
  • the fructose fraction depleted in fructose dimers, obtained from the fractionation of the fructose run-off is then introduced into at least one of said one or more crystallization steps for the production of crystalline fructose. This step may be realized in different ways.
  • the process may comprise the following steps:
  • the process may comprise the following steps:
  • fructose sources for obtaining fructose are as a rule mixtures of glucose and fructose, such as solutions of inverted sucrose, solutions of isomerized glucose (starch based) and mixtures thereof.
  • the fructose source may also be a fructose solution obtained by hydrolysing inulin.
  • the solution of inverted sucrose is typically obtained by enzymatic or acidic inversion of sucrose to a mixture of fructose and glucose.
  • One process for enzymatic inversion is described in WO 92/07057 (EP 553 126 B1 ).
  • Small amounts of dimeric sugars are formed in the inversion process, especially at lower pH values.
  • the acidic inversion processes catalyze the formation of dimers, leading into small amounts of dimeric sugars.
  • dimeric sugars comprise for example difructose anhydrides, fructose dianhydrides, and diheterolevulosans. These inversion by-products act as crystallization inhibitors in the subsequent crystallization of fructose.
  • the solution of isomerized glucose is obtained from starch-based glucose syrup, which is isomerized with an isomerase enzyme to a mixture of glucose and fructose.
  • the enzymatic isomerization is preferably carried out at the optimum pH range for the enzyme, i.e. at a pH of about 8.
  • One process for the isomerization is disclosed in US 4 411 996 .
  • the isomerization is carried out at a higher pH than the inversion of glucose. Consequently, the fructose solution from isomerized glucose includes less fructose dimers than the fructose solution from inverted sucrose.
  • ion exchange is as a rule used for removing ions.
  • the first step in the fructose process typically comprises separation of these mixtures of glucose and fructose into a glucose fraction and a fructose fraction.
  • the crystallization inhibitors such as dimeric sugars formed either in the inversion or isomerization process or during the crystallization, should be removed as efficiently as possible by various separation techniques.
  • the process may thus also comprise, as a preceding step, chromatographic fractionation of a solution containing glucose and fructose to obtain a glucose fraction and a fructose fraction for producing crystalline fructose.
  • the process may also comprise the following steps:
  • the chromatographic separation of glucose and fructose is typically carried out with a cation exchange resin, preferably with a strongly acid cation exchange resin.
  • the resin is preferably in a divalent cation form, whereby the divalent cation is typically selected from Ca 2+ , Mg 2+ or Sr 2+ , especially Ca 2+ .
  • the resin has typically a styrene skeleton, which is preferably cross-linked with divinylbenzene.
  • the starting solution containing glucose and fructose is selected from inverted sucrose, converted and isomerized starch and isomerized glucose.
  • the process may com-comprise the following steps:
  • the process may comprise the following steps:
  • One further embodiment of the process of the invention comprises, as characteristic elements, the following steps:
  • steps (e) to (i) comprise the following:
  • the fructose fraction obtained from the chromatographic fractionation of a fructose crystallization run-off in accordance with the present invention is as a rule subjected to decolorization before the next crystallization.
  • Figure 1 shows one preferred embodiment of carrying out the present invention.
  • a fructose fraction (1) obtained from chromatographic fractionation of a glucose/fructose solution is introduced into a first crystallization (crystallization 1), which provides fructose crystals (a first batch of crystalline fructose) and a first fructose run-off (run-off 1).
  • the first fructose run-off is introduced into a second crystallization (crystallization 2), which provides fructose crystals (a second batch of crystalline fructose) and a second run-off (run-off 2).
  • the second run-off is introduced into chromatographic fractionation, which is carried out with a combination of a Ca 2+ form resin and a Na + form resin.
  • the chromatographic fractionation provides a fructose fraction (2), which is returned to crystallization 2, and a residual fraction containing most of the crystallization inhibitors (disaccharides A and B).
  • the embodiment is especially efficient, if the source of glucose/fructose solution is sucrose, because the feed to the second crystallization is a mixture of fructose run-off (1) and fructose fraction (2) containing a low amount of crystallization inhibitors and a high amount of fructose to facilitate an overall yield of crystalline fructose of up to 98% of the sucrose.
  • the process schema is also advantageous in respect to the required chromatographic system, because the volume of the fructose run-off (2) to be separated is significantly lower (30-40%) than if the total volume of run-off (1) would be separated.
  • fructose and glucose were measured as follows: Liquid chromatography HPLC, Na + form cation exchange column at a temperature of 85°C with a flow rate of 0.8 ml/min using water as the eluent.
  • disaccharides A and disaccharides B were measured by HPLC (liquid chromatography) in the following conditions:
  • the process equipment included four columns connected in series, feed pump, recycling pumps, eluent water pump, heat exchangers, flow control means for the out-coming liquids as well as inlet and product valves for the various process streams.
  • the height of each column was 4.0 m and each column had a diameter of 3.1 m.
  • the columns were packed with a strong acid gel type cation exchange resin (manufactured by Finex) in Ca 2+ -form.
  • the divinylbenzene content of the resin was 5.5% and the mean bead size of the resin was 0.36 mm.
  • the liquor concentration was 67.5 g/100 ml and the pH was 4.1.
  • the fructose syrup was composed as set forth below, whereby the percentages are given on a dry substance weight basis.
  • the fractionation was performed by way of a 12-step SMB sequence as set forth below.
  • the feed and the eluent were used at a temperature of 65°C and water was used as an eluent.
  • Step 1 3.5 m 3 of feed solution were pumped into the first column at a flow rate of 25 m 3 /h and a glucose fraction was collected from the same column. Simultaneously 4.45 m 3 of water were pumped into the third column at a flow rate of 35 m 3 /h and fructose fraction was collected from the same column.
  • Step 2 2.85 m 3 of water were pumped into the third column at a flow rate of 28 m 3 /h and glucose fraction was collected from the first column.
  • Step 3 15.6 m 3 were circulated in the column set loop, formed with all columns, at a flow rate of 30 m 3 /h.
  • Step 4 3.5 m 3 of feed solution were pumped into the second column at a flow rate of 25 m 3 /h and a glucose fraction was collected from the same column. Simultaneously 4.45 m 3 of water were pumped into the fourth column at a flow rate of 35 m 3 /h and fructose fraction was collected from the same column.
  • Step 5 2.85 m 3 of water were pumped into the fourth column at a flow rate of 28 m 3 /h and glucose fraction was collected from the second column.
  • Step 6 15.6 m 3 were circulated in the column set loop, formed with all columns, at a flow rate of 30 m 3 /h.
  • Step 7 3.5 m 3 of feed solution were pumped into the third column at a flow rate of 25 m 3 /h and a glucose fraction was collected from the same column. Simultaneously 4.45 m 3 of water were pumped into the first column at a flow rate of 35 m 3 /h and fructose fraction was collected from the same column.
  • Step 8 2.85 m 3 of water were pumped into the first column at a flow rate of 28 m 3 /h and glucose fraction was collected from the third column.
  • Step 9 15.6 m 3 were circulated in the column set loop, formed with all columns, at a flow rate of 30 m 3 /h.
  • Step 10 3.5 m 3 of feed solution were pumped into the fourth column at a flow rate of 25 m 3 /h and a glucose fraction was collected from the same column. Simultaneously 4.45 m 3 of water were pumped into the second column at a flow rate of 35 m 3 /h and fructose fraction was collected from the same column.
  • Step 11 2.85 m 3 of water were pumped into the second column at a flow rate of 28 m 3 /h and glucose fraction was collected from the fourth column.
  • Step 12 15.6 m 3 were circulated in the column set loop, formed with all columns, at a flow rate of 30 m 3 /h.
  • the process equipment included four columns connected in series, feed pump, recycling pumps, eluent water pump, heat exchangers, flow control means for the out-coming liquids as well as inlet and product valves for the various process streams.
  • the height of each column was 4.0 m and each column had a diameter of 0.2 m.
  • the columns were packed with a strong acid gel type cation exchange resin (manufactured by Finex) in Ca 2+ -form.
  • the divinylbenzene content of the resin was 5.5% and the mean bead size of the resin was 0.36 mm.
  • an enzymatically isomerized glucose solution ( US 4 411 996 ) was used and the aim was to separate glucose and fructose to different fractions.
  • the liquor concentration was 64.2 g/100 ml and the pH was 4.0.
  • the fructose syrup was composed as set forth below, whereby the percentages are given on a dry substance weight basis.
  • the fractionation was performed by way of a 12-step SMB sequence as set forth below.
  • the feed and the eluent were used at a temperature of 65°C and water was used as an eluent.
  • Step 1 17.9 l of feed solution were pumped into the first column at a flow rate of 110 l/h and a glucose fraction was collected from the same column. Simultaneously 17.4 l of water were pumped into the third column at a flow rate of 110 l/h and fructose fraction was collected from the same column.
  • Step 2 17.4 l of water were pumped into the third column at a flow rate of 120 l/h and glucose fraction was collected from the first column.
  • Step 3 59.5 l were circulated in the column set loop, formed with all columns, at a flow rate of 125 l/h.
  • Step 4 17.9 l of feed solution were pumped into the second column at a flow rate of 110 l/h and a glucose fraction was collected from the same column. Simultaneously 17.4 l of water were pumped into the fourth column at a flow rate of 110 l/h and fructose fraction was collected from the same column.
  • Step 5 17.4 l of water were pumped into the fourth column at a flow rate of 120 l/h and glucose fraction was collected from the second column.
  • Step 6 59.5 l were circulated in the column set loop, formed with all columns, at a flow rate of 125 l/h.
  • Step 7 17.9 l of feed solution were pumped into the third column at a flow rate of 110 l/h and a glucose fraction was collected from the same column. Simultaneously 17.4 l of water were pumped into the first column at a flow rate of 110 l/h and fructose fraction was collected from the same column.
  • Step 8 17.4 l of water were pumped into the first column at a flow rate of 120 l/h and glucose fraction was collected from the third column.
  • Step 9 59.5 l were circulated in the column set loop, formed with all columns, at a flow rate of 125 l/h.
  • Step 10 17.9 l of feed solution were pumped into the fourth column at a flow rate of 110 l/h and a glucose fraction was collected from the same column. Simultaneously 17.4 l of water were pumped into the second column at a flow rate of 110 l/h and fructose fraction was collected from the same column.
  • Step 11 17.4 l of water were pumped into the second column at a flow rate of 120 l/h and glucose fraction was collected from the fourth column.
  • Step 12 59.5 l were circulated in the column set loop, formed with all columns, at a flow rate of 125 l/h.
  • the process equipment included a separation column, feed pump, eluent water pump, heat exchangers, flow control means for the out-coming liquid as well as inlet and product valves for the various process streams.
  • the height of the column was 3.3 m and column had a diameter of 2.76 m.
  • the column was packed with a strong acid gel type cation exchange resin (manufactured by Finex) in Na + -form.
  • the divinylbenzene content of the resin was 5.5% and the mean bead size of the resin was 0.35 mm.
  • the feed and the eluent were used at a temperature of 65°C and water was used as the eluent.
  • the feed volume was 2.6 m 3 and the flow rate for the feed and elution was 3.2 m 3 /h.
  • Feed interval for the separation was 9.0 m 3 .
  • the overall fructose yield calculated from these fractions was 94.7%.
  • the glucose content was reduced to 43.8%, the content of disaccharides A to 56.3% and the content of disaccharides B content to 50.0% compared to the content in the feed.
  • the process equipment included a separation column, feed pump, eluent water pump, heat exchangers, flow control means for the out-coming liquid as well as inlet and product valves for the various process streams.
  • the height of the column was 3.7 m and column had a diameter of 2.76 m.
  • the column was packed with a strong acid gel type cation exchange resin (manufactured by Finex) in Ca 2+ -form.
  • the divinylbenzene content of the resin was 5.5% and the mean bead size of the resin was 0.35 mm.
  • a fructose crystallization run-off was used as a feed and the aim was to separate fructose contained therein.
  • the feed and the eluent were used at a temperature of 65°C and water was used as the eluent.
  • the feed volume was 2.5 m 3 and the flow rate for the feed and elution was 3.2 m 3 /h.
  • Feed interval for the separation was 9.0 m 3 .
  • the overall fructose yield calculated from these fractions was 94.8%.
  • the glucose content was reduced to 18.8%, the content of disaccharides A to 75.0% and the content of disaccharides B to 35.0% compared to the content in the feed.
  • the process equipment included two columns connected in series, feed pump, recycling pumps, eluent water pump, heat exchangers, flow control means for the out-coming liquids as well as inlet and product valves for the various process streams.
  • the height of both columns was 4.3 m and both columns had a diameter of 2.76 m.
  • the columns were packed with a strong acid gel type cation exchange resin (manufactured by Finex) in Ca 2+ -form.
  • the divinylbenzene content of the resin was 5.5% and the mean bead size of the resin was 0.36 mm.
  • a fructose crystallization run-off was used as a feed and the aim was to separate the fructose contained therein.
  • the fractionation was performed by way of a 16-step SMB sequence as set forth below.
  • the feed and the eluent were used at a temperature of 65°C and water was used as an eluent.
  • Step 1 1.8 m 3 of feed solution were pumped into the first column at a flow rate of 9 m 3 /h and a recycle fraction was collected from the second column.
  • Step 2 0.2 m 3 of feed solution were pumped into the first column at a flow rate of 9 m 3 /h and a fructose fraction was collected from the second column.
  • Step 3 4,8 m 3 of feed solution were pumped into the first column at a flow rate of 9,5 m 3 /h and a residual fraction was collected from the same column. Simultaneously 12,3 m 3 of water were pumped into the second column at a flow rate of 20 m 3 /h and fructose fraction was collected from the same column.
  • Step 4 12.5 m 3 were circulated in the column set loop, formed with all columns, at a flow rate of 12 m 3 /h.
  • Step 5 5.7 m 3 of water were pumped into the first column at a flow rate of 12 m 3 /h and a residual fraction was collected from the second column.
  • Step 6 12.5 m 3 were circulated in the column set loop, formed with all columns, at a flow rate of 12 m 3 /h.
  • Step 7 5.7 m 3 of water were pumped into the second column at a flow rate of 12 m 3 /h and a residual fraction was collected from the first column.
  • Step 8 9.4 m 3 were circulated in the column set loop, formed with all columns, at a flow rate of 12 m 3 /h.
  • Step 9 1.8 m 3 of feed solution were pumped into the second column at a flow rate of 9 m 3 /h and a recycle fraction was collected from the first column.
  • Step 10 0.2 m 3 of feed solution were pumped into the second column at a flow rate of 9 m 3 /h and a fructose fraction was collected from the first column.
  • Step 11 4.8 m 3 of feed solution were pumped into the second column at a flow rate of 9.5 m 3 /h and a residual fraction was collected from the same column. Simultaneously 12.3 m 3 of water were pumped into the first column at a flow rate of 20 m 3 /h and fructose fraction was collected from the same column.
  • Step 12 12.5 m 3 were circulated in the column set loop, formed with all columns, at a flow rate of 12 m 3 /h.
  • Step 13 5.7 m 3 of water were pumped into the second column at a flow rate of 12 m 3 /h and a residual fraction was collected from the first column.
  • Step 14 12.5 m 3 were circulated in the column set loop, formed with all columns, at a flow rate of 12 m 3 /h.
  • Step 15 5.7 m 3 of water were pumped into the first column at a flow rate of 12 m 3 /h and a residual fraction was collected from the second column.
  • Step 16 9.4 m 3 were circulated in the column set loop, formed with all columns, at a flow rate of 12 m 3 /h.
  • the overall fructose yield calculated from these fractions was 95.5%.
  • the glucose content was reduced to 17.9%, the content of disaccharides A to 84.6% and the content of disaccharides B to 40.0% compared to the content in the feed.
  • the process equipment included two columns connected in series, feed pump, recycling pumps, eluent water pump, heat exchangers, flow control means for the out-coming liquids as well as inlet and product valves for the various process streams.
  • the height of both columns was 3.95 m and both columns had a diameter of 0.2 m.
  • the columns were packed with a strong acid gel type cation exchange resin (manufactured by Finex) in Na + -form.
  • the divinylbenzene content of the resin was 5.5% and the mean bead size of the resin was 0.36 mm.
  • a fructose crystallization run-off was used as a feed and the aim was to separate the fructose contained therein.
  • the fractionation was performed by way of a 14-step SMB sequence as set forth below.
  • the feed and the eluent were used at a temperature of 65°C and water was used as an eluent.
  • Step 1 13 l of feed solution were pumped into the first column at a flow rate of 90 l/h and a recycle fraction was collected from the second column.
  • Step 2 22 l of feed solution were pumped into the first column at a flow rate of 90 l/h and a residual fraction was collected from the same column. Simultaneously 47 l of water were pumped into the second column at a flow rate of 190 l/h and fructose fraction was collected from the same column.
  • Step 3 54 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 4 28 l of water were pumped into the first column at a flow rate of 90 l/h and a residual fraction was collected from the second column.
  • Step 5 57 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 6 25 l of water were pumped into the second column at a flow rate of 90 l/h and a residual fraction was collected from the first column.
  • Step 7 44 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 8 13 l of feed solution were pumped into the second column at a flow rate of 90 l/h and a recycle fraction was collected from the first column.
  • Step 9 22 l of feed solution were pumped into the second column at a flow rate of 90 l/h and a residual fraction was collected from the same column. Simultaneously 47 l of water were pumped into the first column at a flow rate of 190 l/h and fructose fraction was collected from the same column.
  • Step 10 54 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 11 28 l of water were pumped into the second column at a flow rate of 90 l/h and a residual fraction was collected from the first column.
  • Step 12 57 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 13 25 l of water were pumped into the first column at a flow rate of 90 l/h and a residual fraction was collected from the second column.
  • Step 14 44 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • the overall fructose yield calculated from these fractions was 96.1%.
  • the glucose content was reduced to 48.1%, the content of disaccharides A to 36.1% and the content of disaccharides B to 41.2% compared to the content in the feed.
  • the process equipment included two columns connected in series, feed pump, recycling pumps, eluent water pump, heat exchangers, flow control means for the out-coming liquids as well as inlet and product valves for the various process streams.
  • the height of both columns was 3.9 m and both columns had a diameter of 0.2 m.
  • the columns were packed with a weakly acid gel type cation exchange resin (manufactured by Finex).
  • the divinylbenzene content of the resin was 8% and the mean bead size of the resin was 0.31 mm.
  • the resin was balanced to pH 4.5 with 5-% Na-acetate solution and HCl by circulating solution through the resin bed until the outflow pH was 4.5.
  • fructose crystallization run-off was used as a feed and the aim was to separate the fructose contained therein.
  • the fractionation was performed by way of a 16-step SMB sequence as set forth below.
  • the feed and the eluent were used at a temperature of 65°C and water was used as an eluent.
  • Step1 8 l of feed solution were pumped into the first column at a flow rate of 90 l/h and a recycle fraction was collected from the second column.
  • Step 2 22 l of feed solution were pumped into the first column at a flow rate of 90 l/h and a residual fraction was collected from the same column. Simultaneously 37 l of water were pumped into the second column at a flow rate of 143 l/h and first 3 l of recycle fraction and then 34 l of fructose fraction were collected from the same column.
  • Step 3 5 l of feed solution were pumped into the first column at a flow rate of 90 l/h and a fructose fraction was collected from the second column.
  • Step 4 50 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 5 24 l of water were pumped into the first column at a flow rate of 90 l/h and a residual fraction was collected from the second column.
  • Step 6 55 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 7 24 l of water were pumped into the second column at a flow rate of 90 l/h and a residual fraction was collected from the first column.
  • Step 8 48 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 9 8 l of feed solution were pumped into the second column at a flow rate of 90 l/h and a recycle fraction was collected from the first column.
  • Step 10 22 l of feed solution were pumped into the second column at a flow rate of 90 l/h and a residual fraction was collected from the same column. Simultaneously 37 l of water were pumped into the first column at a flow rate of 143 l/h and first 3 l of recycle fraction and the 34 l of fructose fraction were collected from the same column.
  • Step 11 5 l of feed solution were pumped into the second column at a flow rate of 90 l/h and a fructose fraction was collected from the first column.
  • Step 12 50 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 13 24 l of water were pumped into the second column at a flow rate of 90 l/h and a residual fraction was collected from the first column.
  • Step 14 55 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 15 24 l of water were pumped into the first column at a flow rate of 90 l/h and a residual fraction was collected from the second column.
  • Step 16 48 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • the overall fructose yield calculated from these fractions was 94.2%.
  • the glucose content was reduced to 48.0%, the content of disaccharides A to 31.3% and the content of disaccharides B to 25.0% compared to the content in the feed.
  • the process equipment included two columns connected in series, feed pump, recycling pumps, eluent water pump, heat exchangers, flow control means for the out-coming liquids as well as inlet and product valves for the various process streams.
  • the height of both columns was 3.95 m and both columns had a diameter of 0.2 m.
  • the columns were packed with a strong acid gel type cation exchange resin (manufactured by Finex) and first column was in Na + -ion form and second column in Ca 2+ -ion form.
  • the divinylbenzene content of the resin was 5.5% and the mean bead size of the resin was 0.36 mm.
  • a fructose crystallization run-off was used as a feed and the aim was to separate the fructose contained therein.
  • the fractionation was performed by way of a 14-step SMB sequence as set forth below.
  • the feed and the eluent were used at a temperature of 65°C and water was used as an eluent.
  • Step 1 10 l of feed solution were pumped into the first column at a flow rate of 90 l/h and a recycle fraction was collected from the second column.
  • Step 2 25 l of feed solution were pumped into the first column at a flow rate of 90 l/h and a residual fraction was collected from the same column. Simultaneously 45 l of water were pumped into the second column at a flow rate of 190 l/h and fructose fraction was collected from the same column.
  • Step 3 58 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 4 30.5 l of water were pumped into the first column at a flow rate of 90 l/h and a residual fraction was collected from the second column.
  • Step 5 55 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 6 27.5 l of water were pumped into the second column at a flow rate of 90 l/h and a residual fraction was collected from the first column.
  • Step 7 48 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 8 13 l of feed solution were pumped into the second column at a flow rate of 90 l/h and a recycle fraction was collected from the first column.
  • Step 9 22 l of feed solution were pumped into the second column at a flow rate of 90 l/h and a residual fraction was collected from the same column. Simultaneously 45 l of water were pumped into the first column at a flow rate of 190 l/h and fructose fraction was collected from the same column.
  • Step 10 55 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 11 28 l of water were pumped into the second column at a flow rate of 90 l/h and a residual fraction was collected from the first column.
  • Step 12 58 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • Step 13 30.5 l of water were pumped into the first column at a flow rate of 90 l/h and a residual fraction was collected from the second column.
  • Step 14 49 l were circulated in the column set loop, formed with all columns, at a flow rate of 90 l/h.
  • the overall fructose yield calculated from these fractions was 95.8%.
  • the dry substance yield to the residue fraction was 6.6%.
  • the glucose content was reduced to 22.2%, the content of disaccharides A to 55.0% and the content of disaccharides B to 38.9% compared to the content in the feed.
  • EXAMPLE 9 CRYSTALLIZATION OF FRUCTOSE FROM A PRODUCT FRACTION MIXTURE OBTAINED FROM CA 2+ -ION FORM INVERT SEPARATION OF EXAMPLE 1 AND CA 2+ -ION FORM ISOMEROSE SEPARATION OF EXAMPLE 2
  • Seed crystal magma was prepared in 10 m 3 cooling crystallizer by filling the crystallizer with evaporated 90.5% w/w feed liquid, seeding at 57.1°C temperature by adding 1.5 kg seed crystals and cooling the suspension to 40.4°C in 32 hours.
  • the average size of the seed crystals was about 0.03 mm and 90% of the crystals were between 0.02-0.08 mm as analyzed by a PMT-PAMAS particle analyzing system.
  • crystalline fructose Approximately 17.5 tn of crystalline fructose was recovered in 45.8 hours from the fructose feed liquid containing 96.7% fructose, 0.5% glucose and 1.9% disaccharides on DS. The crystallization was performed in a 30 m 3 cylindrical cooling crystallizer.
  • Seed crystal magma was prepared in a 10 m 3 cooling crystallizer by filling the crystallizer with evaporated 91.0% w/w feed liquid, seeding at 58.1°C temperature by adding 1.5 kg seed crystals and cooling the suspension to 42.2°C in 39 hours. About 9 m 3 of the seed crystal magma, which had a mean crystal size about 0.2 mm, was placed in the 30 m 3 cooling crystallizer. Next about 92 w/w % fructose syrup was added to the crystallizer and mixed with the seed magma. When the crystallizer was filled, the temperature of the mass in the crystallizer was adjusted to 56°C and a total concentration of 91.8% w/w was measured.
  • the mass was then cooled to 30.0°C over 36 hours. After cooling, the crystals were separated and washed by a conventional centrifuge, dried in a drum drier, sieved and packed.
  • the fructose yield after cooling was about 57% of the dry substance.
  • the product yield was about 43.2% of dry substance with a mean crystal size of 0.51 mm and a purity of 99.9%.
  • crystalline fructose was recovered in 54.1 hours from a fructose feed liquid containing 96.0% fructose, 1.0% glucose and 2.1% disaccharides on DS.
  • the crystallization was performed in a 30 m 3 cylindrical cooling crystallizer.
  • Seed crystal magma was prepared in 10 m 3 cooling crystallizer by filling the crystallizer with evaporated 90.5% w/w feed liquid, seeding at 56.2°C temperature by adding 1.0 kg seed crystals and cooling the suspension to 38.6°C in 47 hours. About 9 m 3 of the seed crystal magma, which had a mean crystal size about 0.2 mm, was placed in the 30 m 3 cooling crystallizer. Next about 92 w/w % fructose syrup was added to the crystallizer and mixed with the seed magma. When the crystallizer was filled, the temperature of the mass in the crystallizer was adjusted to 56°C and a total concentration of 91.7% w/w was measured. The mass was then cooled to 26.5°C over 44 hours.
  • the fructose yield after cooling was about 53% of the dry substance.
  • the product yield was about 41.4% of dry substance with a mean crystal size of 0.52 mm and a purity of 99.7%.
  • crystalline fructose was recovered in 41.4 hours from a fructose feed liquid containing 97.2% fructose, 0.5% glucose and 1.7% disaccharides on DS.
  • the crystallization was performed in a 30 m 3 cylindrical cooling crystallizer.
  • Seed crystal magma was prepared in 10 m 3 cooling crystallizer by filling the crystallizer with evaporated 91.0% w/w feed liquid, seeding at 58.6°C temperature by adding 1.5 kg seed crystals and cooling the suspension to 40.4°C in 39 hours. About 9 m 3 of the seed crystal magma, which had a mean crystal size about 0.2 mm, was placed in the 30 m 3 cooling crystallizer. Next about 92 w/w % fructose syrup was added to the crystallizer and mixed with the seed magma. When the crystallizer was filled, the temperature of the mass in the crystallizer was adjusted to 56°C and a total concentration of 91.6% w/w was measured.
  • the mass was then cooled to 28.2°C over 31 hours. After cooling, the crystals were separated and washed by a conventional centrifuge, dried in a drum drier, sieved and packed.
  • the fructose yield after cooling was about 58% of the dry substance.
  • the product yield was about 43.5% of dry substance with a mean crystal size of 0.45 mm and a purity of 99.8%.
  • Crystalline sucrose (57.0 tn/d) is first dissolved and inverted enzymatically (EP 553 126 ).
  • Inverted sucrose dry substance is adjusted and invert separation is performed with Ca 2+ -ion form strongly acidic cation exchange resin as descript in the example 1.
  • Glucose fraction is evaporated and subjected to the isomerization ( US 4 411996 ) and further to the isomerose separation.
  • Isomerose separation is performed with Ca 2+ -ion form strongly acidic cation exchange resin as described in Example 2.
  • Glucose fractions from the invert and isomerose separation are combined, evaporated and subjected back to the enzymatic isomerization and further to the isomerose separation.
  • Fructose fractions from both separations are combined, evaporated and subjected to the crystallization. Purity for the combined fraction is 97.2% on dry solids and amount 59.9 tn/d.
  • Fructose is crystallized (feed purity 97.2% and the mass amount of 59.9 tn/d) with 45.7% fructose yield as described in Example 9.
  • Total fructose process yield calculated from sucrose is 46.7% and the fructose yield calculated from fructose entering the crystallization (fructose in the crystallization feed) is 45.9%.
  • Production volume for fructose is 26.7 tn/d. In this option total mass amount to be crystallized is 59.9 tn/d and no mother liquor separation is used.
  • EXAMPLE 14 PRODUCTION OF CRYSTALLINE FRUCTOSE WITH FIRST CRYSTALLIZATION STEP, CA 2+ /NA + -ION FORM MOTHER LIQUOR SEPARATION AND SECOND CRYSTALLIZATION STEP (YIELD 70.8%)
  • Crystalline sucrose (57.0 tn/d) is first dissolved and inverted enzymatically (EP 553 126 ).
  • Inverted sucrose dry substance is adjusted and invert separation is performed with Ca 2+ -ion form strongly acidic cation exchange resin as described in Example 1.
  • Glucose fraction is evaporated and subjected to the isomerization ( US 4 411 996 ) and further to the isomerose separation.
  • Isomerose separation is performed with Ca 2+ -ion form strongly acidic cation exchange resin as described in Example 2.
  • Glucose fractions from the invert and isomerose separation are combined, evaporated and subjected back to the enzymatic isomerization and further to the isomerose separation.
  • Fructose fractions from both separations are combined, evaporated and subjected to the crystallization. Purity for the combined fraction is 97.2% on dry solids and the amount 59.9 tn/d.
  • Fructose is crystallized (feed purity 97.2% and the mass amount 59.9 tn/d) with 45.7% fructose yield as described in Example 9.
  • Mother liquor (amount 33.2 tn/d) is subjected to the chromatographic separation using Na + and Ca 2+ resins and fractionated with 94% fructose yield as described in example 8.
  • Fructose fraction from the mother liquor separation (amount 30,4 tn/d) is crystallized (feed purity 97.7% and mass amount 30.4 tn/d) with 46% fructose yield.
  • Total fructose process yield calculated from sucrose is 70.8% and the fructose yield calculated from fructose in the crystallization feed is 69.4%. Production volume is 40.4 tn/d.
  • mother liquor amount to be separated is 33.2 tn/d and the total mass amount to be crystallized is 90.3 tn/d.
  • EXAMPLE 15 PRODUCTION OF CRYSTALLINE FRUCTOSE WITH FIRST CRYSTALLIZATION STEP, CA 2+ /NA + -ION FORM MOTHER LIQUOR SEPARATION AND SECOND CRYSTALLIZATION STEP FROM WHERE THE MOTHER LIQUOR IS SUBJECTED BACK TO THE MOTHER LIQUOR SEPARATION (YIELD 95.5%)
  • Crystalline sucrose (57.0 tn/d) is first dissolved and inverted enzymatically (EP 553 126 ).
  • Inverted sucrose dry substance is adjusted and invert separation is performed with Ca 2+ -ion form strongly acidic cation exchange resin as described in Example 1.
  • Glucose fraction is evaporated and subjected to the isomerization ( US 4 411996 ) and further to the isomerose separation.
  • Isomerose separation is performed with Ca 2+ -ion form strongly acidic cation exchange resin as described in Example 2.
  • Glucose fractions from the invert and isomerose separation are combined, evaporated and subjected back to the enzymatic isomerization and further to the isomerose separation.
  • Fructose fractions from both separations are combined, evaporated and subjected to the crystallization. Purity for the combined fraction is 97.2% on dry solids and amount 59.9 tn/d.
  • Fructose is crystallized (feed purity 97.2% and mass amount 59.9 tn/d) with 45.7% fructose yield as described in Example 9.
  • Mother liquor (amount 33.2 tn/d) is subjected to the chromatographic separation using Na + and Ca 2+ resins and fractionated with 94% fructose yield as described in Example 8.
  • Fructose fraction (61.7 tn/d) from the mother liquor separation is crystallized (feed purity 97.9% and the mass amount 61.7 tn/d) with 46% fructose yield and second crystallization mother liquor (amount 33.9 tn/d) is also subjected back to the mother liquor separation.
  • Total fructose process yield calculated from sucrose is 95.5% and the fructose yield calculated from fructose in the crystallization feed is 93.6%. Production volume is 54.5 tn/d. In this option the mother liquor amount to be separated is 67.1 tn/d and total mass amount to be crystallized is 121.6 tn/d.
  • EXAMPLE 16 PRODUCTION OF CRYSTALLINE FRUCTOSE WITH FIRST CRYSTALLIZATION STEP, SECOND CRYSTALLIZATION STEP AND USING CA 2+ AND NA + -ION FORM MOTHER LIQUOR SEPARATION FROM WHERE THE FRUCTOSE FRACTION IS SUBJECTED BACK TO SECOND CRYSTALLIZATION (YIELD 98.3%).
  • Crystalline sucrose (57.0 tn/d) is first dissolved and inverted enzymatically (EP 553 126 ). Dry substance of the the inverted sucrose solution is adjusted and the separation is performed using Ca 2+ -ion form strongly acidic cation exchange resin bed as described in Example 1. Glucose fraction is evaporated and subjected to the isomerization ( US 4 411 996 ) and further to the isomerose separation. Isomerose separation is performed using a Ca 2+ -ion form strongly acidic cation exchange resin bed as described in Example 2. Glucose fractions from the invert and isomerose separation are combined, evaporated and subjected back to the enzymatic isomerization and further to the isomerose separation. Fructose fractions from both separations are combined, evaporated and subjected to the crystallization. Purity for the combined fructose fraction is 97.2% on dry solids and the amount 59.9 tn/d.
  • Fructose is crystallized (feed purity 97.2% and mass amount 59.9 tn/d) with 45.7% fructose yield as described in Example 9.
  • Mother liquor (amount 33.2 tn/d) is subjected to the second crystallization step and 43% fructose yield (feed purity 96.0% and mass amount 71 tn/d) is obtained like described in Example 11.
  • Mother liquor (purity 93.4% and amount 41.6 tn/d) from the second crystallization step is subjected to the chromatographic separation using Na + and Ca 2+ resin beds like described in Examples 5, 6 and 8.
  • Fructose fractions from the mother liquor separation are combined (purity 96.7% and amount 37.8 tn/d) and subjected back to the second crystallization step.
  • Total fructose process yield calculated from sucrose is 98.3% and the fructose yield calculated from fructose in the crystallization feed is 96.4%.
  • Production volume is 56.1 tn/d.
  • Example 16 show that a very high yield of crystalline fructose (98.3% on the basis of sucrose) is achieved by introducing a reasonably low amount of fructose mother liquor (41.6 tn/d) from the second crystallization step to chromatographic fractionation using a combination of Na + and Ca 2+ resins. Consequently, the chromatographic fractionation improves the crystallization.
  • Crystalline sucrose (57.0 tn/d) is first dissolved and inverted enzymatically (EP 553 126 ).
  • Inverted sucrose dry substance is adjusted and invert separation is performed with Ca 2+ -ion form strongly acidic cation exchange resin as described in Example 1.
  • Glucose fraction is evaporated and subjected to the isomerization ( US 4 411 996 ) and further to the isomerose separation.
  • Isomerose separation is performed with Ca 2+ -ion form strongly acidic cation exchange resin as described in Example 2.
  • Glucose fractions from the invert and isomerose separation are combined, evaporated and subjected back to the enzymatic isomerization and further to the isomerose separation.
  • Fructose fractions from both separations are combined, evaporated and subjected to the crystallization. Purity for the combined fraction is 97.2% on dry solids and the amount 59.9 tn/d.
  • Fructose is crystallized (feed purity 97.2% and the mass amount 124.8 tn/d) with 44.7% fructose yield as described in Example 12 and mother liquor (amount 70.4 tn/d) is subjected to the chromatographic separation using Ca 2+ resin with 94% fructose yield as described in Example 5.
  • Fructose fraction from the mother liquor separation (purity 97.2% and the amount 64.9 tn/d) is subjected back to crystallization.
  • Total fructose process yield calculated from sucrose is 95.2% and the fructose yield calculated from fructose in the crystallization feed is 93.3%. Production volume is 54.3 tn/d.
  • the mother liquor amount to be separated is 70.4 tn/d and the total mass amount to be crystallized is 124.8 tn/d.
  • the process of this example was modified by using a Na + form resin and the Ca 2+ form resin in the chromatographic separation in consecutive beds (columns) and by returning 50% of the mother liquor from the crystallization directly to the same crystallization step (with a the feed purity of 96.0% and a mass amount of 135.7 tn/d).
  • the need for the mother liquor separation (the amount of the mother liquor to be introduced into the chromatographic separation) can be reduced significantly (to an amount of 39.7 tn/d with a purity of 93.4%), while a relatively high crystallization yield (fructose yield of 43%) is still maintained and the total process yield was improved (the total fructose process yield from sucrose was 98.5% and the fructose yield from fructose in the crystallization feed was 96.5%.

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Claims (30)

  1. Verfahren zur Herstellung kristalliner Fructose mit verbesserter Ausbeute, dadurch gekennzeichnet, dass es umfasst:
    eine oder mehrere Kristallisationsschritte zur Herstellung kristalliner Fructose und einen oder mehrere Fructose-Kristallisationsabläufe, die 88 bis 96% Fructose, 2 bis 5% Disaccharide und 1 bis 8% Glucose bezogen auf die Trockensubstanz enthalten, wobei die Disaccharide Fructose-Dimere umfassen,
    chromatographische Fraktionierung mindestens eines Teils des einen oder der mehreren Fructose-Kristallisationsabläufe in einem Trennungssystem, das zwei oder mehr Kationenaustauscherharzbetten umfasst, wobei mindestens einer der Kationenaustauscherharzbetten in einer Ca2+-Form vorliegt und mindestens einer der Kationenaustauscherharzbetten in einer monovalenten Kationenform vorliegt, um eine an Fructose-Dimeren abgereicherte Fructose-Fraktion und gegebenenfalls mindestens eine andere Fraktion zu erzeugen, und
    Einführen der Fructose-Fraktion in mindestens eine der einen oder mehreren Kristallisationsschritte zur Herstellung kristalliner Fructose.
  2. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die aus der chromatographischen Fraktionierung erhaltene Fructose-Fraktion 94 bis 98% Fructose, weniger als 3%, vorzugsweise weniger als 2% Fructose-Dimere und weniger als 1,5%, vorzugsweise weniger als 1,0% Glucose bezogen auf die Trockensubstanz enthält.
  3. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die Fructose-Dimere aus Disacchariden A und/oder Disacchariden B ausgewählt sind.
  4. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die Fructose-Dimere DiFructose Dianhydride umfassen.
  5. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die mindestens eine andere Fraktion eine mit Fructose-Dimeren angereicherte Rückstandsfraktion ist.
  6. Verfahren gemäß Anspruch 1 und 5, dadurch gekennzeichnet, dass eine an Fructose-Dimeren abgereicherte Fructose-Fraktion und eine mit Fructose-Dimeren angereicherte Rückstandsfraktion erhalten werden.
  7. Verfahren gemäß Anspruch 4, dadurch gekennzeichnet, dass die Fructose-Fraktion weniger als 1,5%, vorzugsweise weniger als 1,0% Disaccharide A und weniger als 1,5%, vorzugsweise weniger als 0,8% Disaccharide B bezogen auf die Trockensubstanz umfasst.
  8. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die chromatographische Fraktionierung eine Fructose Ausbeute von mehr als 80%, vorzugsweise mehr als 90% und besonders bevorzugt mehr als 95% bezogen auf die Fructose in dem in der chromatographischen Fraktionierung als Zulauf verwendeten Fructose-Kristallisationsablauf bereitstellt.
  9. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass das einwertige Kation aus Na+ und K+ ausgewählt ist.
  10. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die Kationenaustauscherharze im Trennungssystem stark saure Kationenaustauscherharze sind.
  11. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass mindestens 20% der Gesamtlänge der Harzbetten des Trennungssystems in einer Ca2+-Form vorliegen.
  12. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass mindestens 20% der Gesamtlänge der Harzbetten des Trennungssystems in einer monovalenten Kationenform vorliegen.
  13. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass der als Zulauf in der chromatographischen Fraktionierung verwendete Fructose-Kristallisationsablauf Disaccharide in einer Menge von weniger als 2% bezogen auf die Trockensubstanz und Glucose in einer Menge von mehr als 3% bezogen auf die Trockensubstanz enthält, wobei 60 bis 80% der Gesamtlänge des Harzbettes des Trennungssystems in Ca2+-Form vorliegen.
  14. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass der als Zulauf in der chromatographischen Fraktionierung verwendete Fructose-Kristallisationsablauf Disaccharide in einer Menge von mehr als 3% bezogen auf die Trockensubstanz und Glucose in einer Menge von weniger als 2% bezogen auf die Trockensubstanz enthält, wobei 60 bis 80% der Gesamtlänge der Harzbetten des Trennungssystems in einer monovalenten Kationenform vorliegen.
  15. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die zwei oder mehreren Kationenaustauscherharzbetten in einer monovalenten Kationenform ein schwach saures Kationenaustauscherharz umfassen.
  16. Verfahren gemäß Anspruch 15, dadurch gekennzeichnet, dass das schwach saure Kationenaustauscherharz in einer freien Säureform vorliegt.
  17. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die zwei oder mehreren Kationenaustauscherharzbetten in Reihe oder parallel angeordnet sind.
  18. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die chromatographische Fraktionierung mit einem diskontinuierlichen Verfahren oder einem simulierten Wanderbett-Verfahren durchgeführt wird.
  19. Verfahren gemäß Anspruch 18, dadurch gekennzeichnet, dass das simulierte Wanderbett-Verfahren kontinuierlich oder sequentiell ist.
  20. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die chromatographische Fraktionierung bei einem pH von 3 bis 6, vorzugsweise bei einem pH im Bereich von 4 bis 5 durchgeführt wird.
  21. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die Fructose-Fraktion, die in die Kristallisation eingeführt werden soll, eine Fructose-Reinheit von mehr als 93%, vorzugsweise mehr als 95% und besonders bevorzugt mehr als 97%, bezogen auf die gelöste Trockensubstanz aufweist.
  22. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass das Verfahren eine Gesamtkristallisationsausbeute an kristalliner Fructose von mehr als 90%, vorzugsweise mehr als 93% und am meisten bevorzugt mehr als 95% bezogen auf die Fructose im Kristallisationszulauf bereitstellt.
  23. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass die chromatographische Fraktionierung eine Ausbeute an Fructose von mehr als 90%, bevorzugt mehr als 95% bezogen auf die Fructose in dem als Zulauf in der chromatographischen Fraktionierung verwendeten Fructose-Kristallisationsablauf bereitstellt und dass das Verfahren eine Gesamtausbeute an kristalliner Fructose von mehr als 90% und vorzugsweise mehr als 95% bezogen auf die Fructose im Kristallisationszulauf bereitstellt.
  24. Verfahren gemäß Anspruch 1, gekennzeichnet durch folgende Schritte:
    chromatographische Fraktionierung mindestens eines Teils des einen oder der mehreren Fructose-Kristallisationsabläufe in einem Trennungssystem, das zwei oder mehr Kationenaustauscherharzbetten umfasst, wobei mindestens einer der Kationenaustauscherharzbetten in einer Ca2+-Form vorliegt und mindestens einer der Kationenaustauscherharzbetten in einer monovalenten Kationenform vorliegt, um eine an Fructose-Dimeren abgereicherte Fructose-Fraktion zu erzeugen,
    Einführen der Fructose-Fraktion in die Kristallisation, um kristalline Fructose und einen weiteren Kristallisationsablauf zu erhalten, und
    Rückführen mindestens eines Teils des weiteren Kristallisationsablaufs in die chromatographische Fraktionierung.
  25. Verfahren gemäß Anspruch 1, gekennzeichnet durch folgende Schritte:
    Kristallisation eines Fructose-Kristallisationsablaufs um kristalline Fructose und einen weiteren Kristallisationsablauf zu erhalten, der 88 bis 96% Fructose, 2 bis 5% Disaccharide und 1 bis 8% Glucose bezogen auf die Trockensubstanz enthält, wobei die Disaccharide Fructose-Dimere umfassen,
    chromatographische Fraktionierung mindestens eines Teils des weiteren Kristallisationsablaufs in einem Trennungssystem, das zwei oder mehr Kationenaustauscherharzbetten umfasst, wobei mindestens einer der Kationenaustauscherharzbetten in einer Ca2+-Form vorliegt und mindestens einer der Kationenaustauscherharzbetten in einer monovalenten Kationenform vorliegt, um eine an Fructose-Dimeren abgereicherte Fructose-Fraktion zu erzeugen,
    Rückführen der Fructose-Fraktion in die Kristallisation.
  26. Verfahren gemäß Anspruch 1, dadurch gekennzeichnet, dass das Verfahren auch, als vorangehenden Schritt, eine chromatographische Fraktionierung einer Lösung umfasst, die Glucose und Fructose enthält, um eine Glucose-Fraktion und eine Fructose-Fraktion zur Herstellung kristalliner Fructose zu erhalten.
  27. Verfahren gemäß Anspruch 26, dadurch gekennzeichnet, dass die Lösung, die Glucose und Fructose enthält, ausgewählt ist aus invertierter Saccharose und isomerisierter Glucose.
  28. Verfahren gemäß Anspruch 26, dadurch gekennzeichnet, dass das Verfahren auch umfasst
    Unterwerfen der Glucose-Fraktion einer Isomerisierung, um eine Lösung zu erhalten, die Glucose und Fructose enthält, und
    Rückführen der Lösung, die Glucose und Fructose enthält, in die chromatographische Fraktionierung.
  29. Verfahren gemäß Anspruch 26, dadurch gekennzeichnet, dass es die folgenden Schritte umfasst:
    (a) Bereitstellen einer Lösung, die Glucose und Fructose enthält,
    (b) Unterwerfen der Lösung, die Glucose und Fructose enthält, der chromatographischen Fraktionierung, um eine Glucose-Fraktion und eine Fructose-Fraktion zu erhalten,
    (c) Unterwerfen der Fructose-Fraktion der Kristallisation, um kristalline Fructose und einen Fructose-Kristallisationsablauf zu erhalten, der 88 bis 96% Fructose, 2 bis 5% Disaccharide und 1 bis 8% Glucose bezogen auf die Trockensubstanz enthält, wobei die Disaccharide Fructose-Dimere umfassen,
    (d) Unterwerfen mindestens eines Teils des Fructose-Kristallisationsablaufs der chromatographischen Fraktionierung in einem Trennungssystem, das zwei oder mehr Kationenaustauscherharzbetten umfasst, wobei mindestens einer der Kationenaustauscherharzbetten in einer Ca2+-Form vorliegt und mindestens einer der Kationenaustauscherharzbetten in einer monovalenten Kationenform vorliegt, um eine weitere an Fructose-Dimeren abgereicherte Fructose-Fraktion zu erhalten,
    (e) Einführen der weiteren Fructose-Fraktion in die Kristallisation, um weitere kristalline Fructose und einen weiteren Kristallisationsablauf zu erhalten, der 88 bis 96% Fructose, 2 bis 5% Disaccharide und 1 bis 8% Glucose bezogen auf die Trockensubstanz enthält, wobei die Disaccharide Fructose-Dimere umfassen, und
    (f) Rückführen mindestens eines Teils des weiteren Kristallisationsablaufs in die chromatographische Fraktionierung des Schrittes (d).
  30. Verfahren gemäß Anspruch 26, dadurch gekennzeichnet, dass es die folgenden Schritte umfasst:
    (a) Bereitstellen einer Lösung, die Glucose und Fructose enthält,
    (b) Unterwerfen der Lösung, die Glucose und Fructose enthält, der chromatographischen Fraktionierung, um eine Glucose-Fraktion und eine Fructose-Fraktion zu erhalten,
    (c) Unterwerfen der Fructose-Fraktion der Kristallisation, um kristalline Fructose und einen Fructose-Kristallisationsablauf zu erhalten,
    (d) Unterwerfen des Fructose-Kristallisationsablaufs der Kristallisation, um weitere kristalline Fructose und einen weiteren Kristallisationsablauf zu erhalten, der 88 bis 96% Fructose, 2 bis 5% Disaccharide und 1 bis 8% Glucose bezogen auf die Trockensubstanz enthält, wobei die Disaccharide Fructose-Dimere umfassen,
    (e) Unterwerfen mindestens eines Teils des weiteren Kristallisationsablaufs der chromatographischen Fraktionierung in einem Trennungssystem, das zwei oder mehr Kationenaustauscherharzbetten umfasst, wobei mindestens einer der Kationenaustauscherharzbetten in einer Ca2+-Form vorliegt und mindestens einer der Kationenaustauscherharzbetten in einer anderen als einer Ca2+-Form vorliegt, um eine weitere an Fructose-Dimeren abgereicherte Fructose-Fraktion zu erhalten,
    (f) Rückführen der weiteren Fructose-Fraktion in die Kristallisation.
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9982284B2 (en) 2014-02-27 2018-05-29 E I Du Pont De Nemours And Company Enzymatic hydrolysis of disaccharides and oligosaccharides using alpha-glucosidase enzymes
WO2018217722A1 (en) 2017-05-23 2018-11-29 E. I. Du Pont De Nemours And Company Enzymatic production of alpha-1,3-glucan
EP3532481B1 (de) 2016-10-28 2023-06-14 Tate & Lyle Solutions USA LLC Verfahren zur herstellung von allulosekristallen

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014030030A1 (en) * 2012-08-20 2014-02-27 Naturalia Ingredients S.R.L. Method of producing a sugar product from fruit
US10266861B2 (en) 2015-12-14 2019-04-23 E. I. Du Pont De Nemours And Company Production and composition of fructose syrup
JP6820194B2 (ja) * 2016-12-19 2021-01-27 日本コーンスターチ株式会社 液状甘味料組成物、その製造方法及び飲料の製造方法
EP3561080B1 (de) * 2018-04-23 2023-08-02 Novasep Process Solutions Herstellungsverfahren von fruktose aus glukose

Family Cites Families (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3692582A (en) 1970-07-31 1972-09-19 Suomen Sokeri Oy Procedure for the separation of fructose from the glucose of invert sugar
US3883365A (en) 1972-01-04 1975-05-13 Suomen Sokeri Oy PH adjustment in fructose crystallization for increased yield
JPS5239901B2 (de) 1973-02-12 1977-10-07
US4411996A (en) 1982-06-30 1983-10-25 Nabisco Brands, Inc. Process for isomerizing glucose
US4634472A (en) 1985-08-23 1987-01-06 A. E. Staley Manufacturing Company Enrichment of fructose syrups
US5230742A (en) 1987-02-02 1993-07-27 A. E. Staley Manufacturing Co. Integrated process for producing crystalline fructose and high-fructose, liquid-phase sweetener
US5234503A (en) 1987-02-02 1993-08-10 A.E. Saley Manufacturing Co. Integrated process for producing crystalline fructose and a high-fructose, liquid-phase sweetener
FI77693C (fi) 1987-06-03 1989-04-10 Suomen Sokeri Oy Foerfarande foer kristallisering av fruktos.
FI88933C (fi) 1990-10-15 1993-07-26 Xyrofin Oy Foerfarande foer produktion av glukos och fruktos av sackaros
EP0482275B1 (de) 1990-10-22 1996-07-10 The Procter & Gamble Company Stabile, flüssige Reinigungsmittel enthaltend ein Bleichmittel
US6206977B1 (en) 1992-01-27 2001-03-27 Danisco Finland Oy Method for crystallizing anhydrous fructose from its aqueous solutions
FI98791C (fi) 1994-04-21 1997-08-25 Xyrofin Oy Menetelmä liuoksen fraktioimiseksi
ATE249524T1 (de) 1998-07-08 2003-09-15 Warcoing S A Verfahren zur herstellung von kristalfruktose
FI20002149A (fi) * 2000-09-29 2002-03-30 Xyrofin Oy Sakkaridien puhdistaminen kromatografisella erotuksella
FI20010977A (fi) * 2001-05-09 2002-11-10 Danisco Sweeteners Oy Kromatografinen erotusmenetelmä
BR0103406A (pt) 2001-08-15 2004-05-04 Getec Guanabara Quimica Ind S Processo de produção de frutose cristalina de elevada pureza utilizando xarope com baixo teor de frutose originária de sacarose, e produto obtido
FI115919B (fi) 2002-06-27 2005-08-15 Danisco Sweeteners Oy Menetelmä kiteytysinhibiittoreiden poistamiseksi monosakkaridisokeriliuoksista

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9982284B2 (en) 2014-02-27 2018-05-29 E I Du Pont De Nemours And Company Enzymatic hydrolysis of disaccharides and oligosaccharides using alpha-glucosidase enzymes
US9988657B2 (en) 2014-02-27 2018-06-05 E I Du Pont De Nemours And Company Enzymatic hydrolysis of disaccharides and oligosaccharides using alpha-glucosidase enzymes
US10472657B2 (en) 2014-02-27 2019-11-12 Dupont Industrial Biosciences Usa, Llc Enzymatic hydrolysis of disaccharides and oligosaccharides using alpha-glucosidase enzymes
EP3532481B1 (de) 2016-10-28 2023-06-14 Tate & Lyle Solutions USA LLC Verfahren zur herstellung von allulosekristallen
WO2018217722A1 (en) 2017-05-23 2018-11-29 E. I. Du Pont De Nemours And Company Enzymatic production of alpha-1,3-glucan
US10774352B2 (en) 2017-05-23 2020-09-15 Dupont Industrial Biosciences Usa, Llc Enzymatic production of alpha-1,3-glucan

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