WO2022219094A1 - Verfahren zur herstellung von 1,1-gpm- und/oder von 1,6-gps-angereicherten isomalt-zusammensetzungen - Google Patents
Verfahren zur herstellung von 1,1-gpm- und/oder von 1,6-gps-angereicherten isomalt-zusammensetzungen Download PDFInfo
- Publication number
- WO2022219094A1 WO2022219094A1 PCT/EP2022/059965 EP2022059965W WO2022219094A1 WO 2022219094 A1 WO2022219094 A1 WO 2022219094A1 EP 2022059965 W EP2022059965 W EP 2022059965W WO 2022219094 A1 WO2022219094 A1 WO 2022219094A1
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- WIPO (PCT)
- Prior art keywords
- isomalt
- weight
- gpm
- gps
- enriched
- Prior art date
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- SERLAGPUMNYUCK-DCUALPFSSA-N 1-O-alpha-D-glucopyranosyl-D-mannitol Chemical compound OC[C@@H](O)[C@@H](O)[C@H](O)[C@H](O)CO[C@H]1O[C@H](CO)[C@@H](O)[C@H](O)[C@H]1O SERLAGPUMNYUCK-DCUALPFSSA-N 0.000 title claims abstract description 573
- 238000000034 method Methods 0.000 title claims abstract description 385
- 235000010439 isomalt Nutrition 0.000 title claims abstract description 316
- 239000000905 isomalt Substances 0.000 title claims abstract description 315
- HPIGCVXMBGOWTF-UHFFFAOYSA-N isomaltol Natural products CC(=O)C=1OC=CC=1O HPIGCVXMBGOWTF-UHFFFAOYSA-N 0.000 title claims abstract description 315
- 239000000203 mixture Substances 0.000 title claims abstract description 151
- 230000008569 process Effects 0.000 title claims abstract description 60
- SERLAGPUMNYUCK-YJOKQAJESA-N 6-O-alpha-D-glucopyranosyl-D-glucitol Chemical compound OC[C@H](O)[C@@H](O)[C@H](O)[C@H](O)CO[C@H]1O[C@H](CO)[C@@H](O)[C@H](O)[C@H]1O SERLAGPUMNYUCK-YJOKQAJESA-N 0.000 claims abstract description 245
- 239000013078 crystal Substances 0.000 claims description 138
- 239000012071 phase Substances 0.000 claims description 128
- 238000002425 crystallisation Methods 0.000 claims description 95
- 230000008025 crystallization Effects 0.000 claims description 95
- 239000007791 liquid phase Substances 0.000 claims description 82
- 239000000725 suspension Substances 0.000 claims description 79
- 238000001704 evaporation Methods 0.000 claims description 52
- 230000008020 evaporation Effects 0.000 claims description 50
- 239000000126 substance Substances 0.000 claims description 39
- 238000010899 nucleation Methods 0.000 claims description 27
- 238000001816 cooling Methods 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 19
- 230000006911 nucleation Effects 0.000 claims description 19
- 238000004519 manufacturing process Methods 0.000 claims description 18
- 239000007787 solid Substances 0.000 claims description 13
- 238000005984 hydrogenation reaction Methods 0.000 claims description 11
- FBPFZTCFMRRESA-FSIIMWSLSA-N D-Glucitol Natural products OC[C@H](O)[C@H](O)[C@@H](O)[C@H](O)CO FBPFZTCFMRRESA-FSIIMWSLSA-N 0.000 claims description 10
- FBPFZTCFMRRESA-JGWLITMVSA-N D-glucitol Chemical compound OC[C@H](O)[C@@H](O)[C@H](O)[C@H](O)CO FBPFZTCFMRRESA-JGWLITMVSA-N 0.000 claims description 10
- 239000000600 sorbitol Substances 0.000 claims description 10
- FBPFZTCFMRRESA-KVTDHHQDSA-N D-Mannitol Chemical compound OC[C@@H](O)[C@@H](O)[C@H](O)[C@H](O)CO FBPFZTCFMRRESA-KVTDHHQDSA-N 0.000 claims description 9
- 229930195725 Mannitol Natural products 0.000 claims description 9
- 239000000594 mannitol Substances 0.000 claims description 9
- 235000010355 mannitol Nutrition 0.000 claims description 9
- 238000013019 agitation Methods 0.000 claims description 6
- 238000001223 reverse osmosis Methods 0.000 claims description 6
- 229920001542 oligosaccharide Polymers 0.000 claims description 5
- 150000002482 oligosaccharides Chemical class 0.000 claims description 5
- 150000004043 trisaccharides Chemical class 0.000 claims description 5
- 150000002016 disaccharides Chemical class 0.000 claims description 4
- 150000002772 monosaccharides Chemical class 0.000 claims description 4
- 241001465754 Metazoa Species 0.000 claims description 3
- 150000004676 glycans Chemical class 0.000 claims description 2
- 229920001282 polysaccharide Polymers 0.000 claims description 2
- 239000005017 polysaccharide Substances 0.000 claims description 2
- 238000011081 inoculation Methods 0.000 claims 1
- SERLAGPUMNYUCK-BLEZHGCXSA-N (2xi)-6-O-alpha-D-glucopyranosyl-D-arabino-hexitol Chemical compound OCC(O)[C@@H](O)[C@H](O)[C@H](O)CO[C@H]1O[C@H](CO)[C@@H](O)[C@H](O)[C@H]1O SERLAGPUMNYUCK-BLEZHGCXSA-N 0.000 abstract description 5
- 239000000243 solution Substances 0.000 description 154
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 56
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 36
- 239000000047 product Substances 0.000 description 19
- 238000004458 analytical method Methods 0.000 description 15
- 230000015572 biosynthetic process Effects 0.000 description 15
- 239000002904 solvent Substances 0.000 description 15
- 230000001965 increasing effect Effects 0.000 description 13
- 239000002245 particle Substances 0.000 description 12
- 238000000926 separation method Methods 0.000 description 12
- 239000012065 filter cake Substances 0.000 description 11
- 229960002920 sorbitol Drugs 0.000 description 11
- 238000009826 distribution Methods 0.000 description 10
- 239000000706 filtrate Substances 0.000 description 10
- 238000010008 shearing Methods 0.000 description 10
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 8
- 150000001298 alcohols Chemical class 0.000 description 7
- 238000005119 centrifugation Methods 0.000 description 7
- 239000007864 aqueous solution Substances 0.000 description 6
- 235000013305 food Nutrition 0.000 description 6
- 230000009467 reduction Effects 0.000 description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 5
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 5
- 229930006000 Sucrose Natural products 0.000 description 5
- 238000009825 accumulation Methods 0.000 description 5
- 230000007423 decrease Effects 0.000 description 5
- 239000008367 deionised water Substances 0.000 description 5
- 229910021641 deionized water Inorganic materials 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- 239000007790 solid phase Substances 0.000 description 5
- 238000003756 stirring Methods 0.000 description 5
- 239000005720 sucrose Substances 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- AYRXSINWFIIFAE-SCLMCMATSA-N Isomaltose Natural products OC[C@H]1O[C@H](OC[C@@H](O)[C@@H](O)[C@H](O)[C@@H](O)C=O)[C@@H](O)[C@@H](O)[C@@H]1O AYRXSINWFIIFAE-SCLMCMATSA-N 0.000 description 4
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- ZXEKIIBDNHEJCQ-UHFFFAOYSA-N isobutanol Chemical compound CC(C)CO ZXEKIIBDNHEJCQ-UHFFFAOYSA-N 0.000 description 4
- DLRVVLDZNNYCBX-RTPHMHGBSA-N isomaltose Chemical compound O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@@H]1OC[C@@H]1[C@@H](O)[C@H](O)[C@@H](O)C(O)O1 DLRVVLDZNNYCBX-RTPHMHGBSA-N 0.000 description 4
- 230000033001 locomotion Effects 0.000 description 4
- 238000002360 preparation method Methods 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- PVXPPJIGRGXGCY-TZLCEDOOSA-N 6-O-alpha-D-glucopyranosyl-D-fructofuranose Chemical compound O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@@H]1OC[C@@H]1[C@@H](O)[C@H](O)C(O)(CO)O1 PVXPPJIGRGXGCY-TZLCEDOOSA-N 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 3
- 238000004220 aggregation Methods 0.000 description 3
- 230000002776 aggregation Effects 0.000 description 3
- 230000001419 dependent effect Effects 0.000 description 3
- 238000010790 dilution Methods 0.000 description 3
- 239000012895 dilution Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000012047 saturated solution Substances 0.000 description 3
- 239000003765 sweetening agent Substances 0.000 description 3
- BTKQLFSKIFGYOF-MASOBFGXSA-N 1-O-alpha-D-glucopyranosyl-D-mannitol dihydrate Chemical compound O.O.OC[C@@H](O)[C@@H](O)[C@H](O)[C@H](O)CO[C@H]1O[C@H](CO)[C@@H](O)[C@H](O)[C@H]1O BTKQLFSKIFGYOF-MASOBFGXSA-N 0.000 description 2
- MIDXCONKKJTLDX-UHFFFAOYSA-N 3,5-dimethylcyclopentane-1,2-dione Chemical compound CC1CC(C)C(=O)C1=O MIDXCONKKJTLDX-UHFFFAOYSA-N 0.000 description 2
- 239000004698 Polyethylene Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 235000013736 caramel Nutrition 0.000 description 2
- 230000001427 coherent effect Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 235000009508 confectionery Nutrition 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 235000013399 edible fruits Nutrition 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000001000 micrograph Methods 0.000 description 2
- 239000008267 milk Substances 0.000 description 2
- 235000013336 milk Nutrition 0.000 description 2
- 210000004080 milk Anatomy 0.000 description 2
- 239000012452 mother liquor Substances 0.000 description 2
- 238000013021 overheating Methods 0.000 description 2
- -1 polyethylene Polymers 0.000 description 2
- 229920000573 polyethylene Polymers 0.000 description 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 2
- 238000010591 solubility diagram Methods 0.000 description 2
- 235000021092 sugar substitutes Nutrition 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- YLZOPXRUQYQQID-UHFFFAOYSA-N 3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)-1-[4-[2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidin-5-yl]piperazin-1-yl]propan-1-one Chemical compound N1N=NC=2CN(CCC=21)CCC(=O)N1CCN(CC1)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F YLZOPXRUQYQQID-UHFFFAOYSA-N 0.000 description 1
- 229920000084 Gum arabic Polymers 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- 241000978776 Senegalia senegal Species 0.000 description 1
- 239000000205 acacia gum Substances 0.000 description 1
- 235000010489 acacia gum Nutrition 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000013361 beverage Nutrition 0.000 description 1
- 230000002902 bimodal effect Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 229940112822 chewing gum Drugs 0.000 description 1
- 235000015218 chewing gum Nutrition 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 235000008504 concentrate Nutrition 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 206010012601 diabetes mellitus Diseases 0.000 description 1
- 150000004683 dihydrates Chemical class 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 235000003599 food sweetener Nutrition 0.000 description 1
- 235000015203 fruit juice Nutrition 0.000 description 1
- 125000005640 glucopyranosyl group Chemical group 0.000 description 1
- 238000004128 high performance liquid chromatography Methods 0.000 description 1
- 238000000265 homogenisation Methods 0.000 description 1
- 235000015243 ice cream Nutrition 0.000 description 1
- 238000010191 image analysis Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011534 incubation Methods 0.000 description 1
- 230000001939 inductive effect Effects 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- 235000015110 jellies Nutrition 0.000 description 1
- 239000008274 jelly Substances 0.000 description 1
- 239000002075 main ingredient Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 150000002939 palatinoses Chemical class 0.000 description 1
- 235000014594 pastries Nutrition 0.000 description 1
- 239000000825 pharmaceutical preparation Substances 0.000 description 1
- 229940127557 pharmaceutical product Drugs 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 229910001925 ruthenium oxide Inorganic materials 0.000 description 1
- WOCIAKWEIIZHES-UHFFFAOYSA-N ruthenium(iv) oxide Chemical compound O=[Ru]=O WOCIAKWEIIZHES-UHFFFAOYSA-N 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 235000013570 smoothie Nutrition 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 239000006188 syrup Substances 0.000 description 1
- 235000020357 syrup Nutrition 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 235000013618 yogurt Nutrition 0.000 description 1
Classifications
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L29/00—Foods or foodstuffs containing additives; Preparation or treatment thereof
- A23L29/30—Foods or foodstuffs containing additives; Preparation or treatment thereof containing carbohydrate syrups; containing sugars; containing sugar alcohols, e.g. xylitol; containing starch hydrolysates, e.g. dextrin
- A23L29/37—Sugar alcohols
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L27/00—Spices; Flavouring agents or condiments; Artificial sweetening agents; Table salts; Dietetic salt substitutes; Preparation or treatment thereof
- A23L27/30—Artificial sweetening agents
- A23L27/33—Artificial sweetening agents containing sugars or derivatives
- A23L27/34—Sugar alcohols
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
- C07H1/00—Processes for the preparation of sugar derivatives
- C07H1/06—Separation; Purification
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
- C07H15/00—Compounds containing hydrocarbon or substituted hydrocarbon radicals directly attached to hetero atoms of saccharide radicals
- C07H15/02—Acyclic radicals, not substituted by cyclic structures
- C07H15/04—Acyclic radicals, not substituted by cyclic structures attached to an oxygen atom of the saccharide radical
Definitions
- the present invention relates to a process for the production of 1-O-a-D-glucopyranosyl-D-mannitol- (hereinafter referred to as 1,1-GPM) and/or 6-O-a-D-glucopyranosyl-D-sorbitol- (hereinafter 1,6- called GPS) enriched isomalt compositions from isomalt-containing solutions, i.e. solutions containing hydrogenated isomaltulose, 1,1-GPM and/or 1,6-GPS-enriched isomalt compositions from isomalt-containing solutions produced by the process according to the invention , as well as the use of these 1,1-GPM and/or 1,6-GPS-enriched isomalt compositions.
- 1,1-GPM 1-O-a-D-glucopyranosyl-D-mannitol-
- GPS 6-O-a-D-glucopyranosyl-D-sorbitol-
- Isomalt Hydrogenated Palatinose
- 1,1-GPM and 1,6-GPS as its main ingredients and is beneficial for its acariogenicity, low calorific value and diabetic suitability.
- 1,1-GPM and/or 1,6-GPS-enriched isomalt compositions from an isomalt-containing solution are better suited for a variety of applications than products containing a nearly equimolar ratio of 1,1-GPM to 1, 6-GPS.
- DE 25 20 173 A1 relates to a process for the production of 1,6-GPS and 1,1-GPM from isomaltulose and its use as a sugar substitute.
- EP 0625578 A1 discloses the production of isomalt and its use as a sweetener in luxury and food products.
- EP 0 859 006 B2 and WO 1997/008958 A1 relate to processes for the production of 1,6-GPS-enriched and 1,1-GPM-enriched mixtures, 1,6-GPS and 1,1-GPM in pure form and the use from that.
- compositions of this type are used in many products, for example in the luxury and food sectors.
- the potentially very wide range of applications of such compositions requires, depending on the end product, compositions that are different Shares of 1.1 GPM and 1.6 GPS have, especially those that are enriched with 1.1 GPM or 1.6 GPS.
- the invention is therefore based on the technical problem of providing a crystallization process for the production of 1,1-GPM and/or 1,6-GPS-enriched isomalt compositions from an isomalt-containing solution that is simple and safe to carry out and in high yield and reproducible leads to 1,1-GPM and/or 1,6-GPS-enriched isomalt compositions from an isomalt-containing solution.
- the present invention solves the technical problem by providing a process for the production of 1,1-GPM and/or 1,6-GPS-enriched isomalt compositions from an isomalt-containing solution, characterized in that a) an isomalt -containing solution is provided, wherein the isomalt-containing solution has 65 to 90% by weight, in particular 70 to 85% by weight, isomalt (in each case based on the total weight of the isomalt-containing solution); b) the isomalt-containing solution provided in process step a) is subjected to flash evaporation in a reactor for crystal nucleation to obtain a first isomalt-containing suspension comprising a first crystalline phase and a first liquid phase; c) the first isomalt-containing suspension obtained in process step b) is subjected to a crystallization process, whereby a second isomalt-containing suspension comprising a second crystalline phase and a second liquid phase is obtained, the second crystalline phase containing 1,1-GPM is
- the invention is therefore based on an isomalt-containing solution as the starting solution, which is provided in process step a) and is subjected to a process that uses process steps b), c), d) and e) in particular to provide two different phases, namely a second crystalline and a second liquid phase, the second crystalline phase having a higher 1,1-GPM content than the isomalt-containing solution used in process step a) and the second liquid phase having a higher 1,6-GPM GPS content than the isomalt-containing solution used in process step a).
- the present invention therefore enables the isomalt-containing solution to be separated into two phases with phase-specific enrichment of the components 1,1-GPM in the second crystalline phase and 1,6-GPS in the second liquid phase in the isomalt-containing solution used as starting solution Phase and according to the invention provides 1,1-GPM and 1,6-GPS-enriched phases and compositions ready, in terms of 1,1-GPM and 1,6-GPS content compared to the respective 1,1-GPM and 1,6-GPS content in the starting solution are specifically enriched and are particularly suitable for certain applications.
- 1,1-GPM and 1,6-GPS-enriched isomalt-containing compositions are obtained, ie a composition which differs from the isomalt-containing solution provided in process step a). characterized by a higher content of 1,1-GPM and also a further composition which is characterized by a higher content of 1,6-GPM compared to the isomalt-containing solution provided in process step a).
- the invention accordingly provides a method for producing 1,1-GPM and/or 1,6-GPS-enriched isomalt compositions from an isomalt-containing solution, wherein an isomalt-containing solution, ie a solution containing an isomalt -containing mixture, in a process step a) is provided and in a process step b) by Llash evaporation in a reactor, in particular nucleator, an induced crystal nucleation is effected, in the context of which a crystal nucleus and these crystal nuclei beginning crystallization to obtain a first Isomalt-containing suspension takes place and in a method step c) by subsequent crystallization in a reactor, in particular the same or another reactor, in particular crystallizer, a second crystalline phase and a second liquid phase comprehensive second isomalt-containing suspension is obtained, wherein the second crystalline phase is enriched in 1,1-GPM and the second liquid phase is enriched with 1,6-GPS, and in a method step d) then the 1,1-
- the method according to the invention results in a simple and efficient, in particular cost-efficient, process control.
- the interval-based, continuous addition of highly pure crystal nuclei which is time-consuming and costly to produce, can be dispensed with.
- the process according to the invention results in a particularly homogeneous crystal nucleation, since local steps initiating the crystallization, in particular seeding, are dispensed with, since in-operando, i.e. during the process according to the invention, i.e. during ongoing operation of the reactor, Crystal nuclei continuously arise independently.
- the method according to the invention results in the avoidance of common technical problems, since the independent crystal nucleation takes place in the entire isomalt-containing solution used, whereas in common crystal nucleation reactors, in particular slurry reactors, the homogenization of the suspension used comprises seed crystals, solids and Solvent is often problematic, since the addition of seed crystals requires rapid mixing to avoid local concentration gradients and thus homogeneous crystal growth to guarantee, which often leads to the destruction of crystals that have already formed.
- the invention assumes that the solubility of 1,1-GPM and 1,6-GPS differs in a solution, in particular in an aqueous solution, i.e.
- both components have different solubility equilibria, and consequently the two components during the Llash - Evaporation and subsequent crystallization to varying degrees in the crystalline and liquid phases correspondingly enrich or deplete.
- the solubility equilibria are temperature-dependent, with preference being given to controlling the shearing and/or the process parameters, in particular pressure and/or temperature and/or the concentration of the components 1,1-GPM and/or 1,1-GPS in the liquid phase, the degree of enrichment of the both components can be specifically adjusted.
- the flash evaporation is preferably carried out at a pressure which is reduced relative to atmospheric pressure, the lowering of the absolute pressure leading to overheating of the liquid.
- the reduced absolute pressure when the reduced absolute pressure is set, the pressure drop spreads with a defined wave propagation in the reactor used for crystal nucleation, in particular the nucleator, with this wave propagation occurring faster than the temperature adaptation of the liquid, which is slowed down by heat and mass transfers at the phase boundaries media. This leads to a thermodynamic imbalance and the overheating induced by the reduction in pressure is reduced by energy transfer, in particular to boiling nuclei and/or to existing vapor bubbles.
- the reduction of the absolute pressure thus leads to the evaporation of a defined part of the solvent used, in particular water, as a result of which energy is withdrawn from the isomalt-containing solution used, ie the system cools down in a defined manner.
- the temperature dependence of the solubility equilibria of 1,1-GPM and 1,6-GPS allows, under the given process parameters and conditions, a defined crystal nucleation and a crystallization starting in a defined manner on the formed crystal nuclei, with the resulting crystal nuclei and crystals being enriched with 1,1-GPM and 1,6-GPS is enriched in the remaining liquid.
- the different solubility products of 1,1-GPM and/or 1,6-GPS are thus utilized through targeted pressure reduction and temperature control in order to achieve an enrichment of the corresponding substances in crystalline and liquid form.
- the Llash evaporation carried out in process step b) accordingly leads to the formation of a first isomalt-containing suspension, comprising a first crystalline and a first liquid phase, wherein 1,1-GPM is enriched in the first crystalline phase and 1,6-GPS in the first liquid phase.
- the flash evaporation is preferably carried out until there is a sufficient accumulation of 1,1-GPM and/or 1,6-GPS in the obtained first crystalline and first liquid phase, in particular in the first crystalline phase and crystal nuclei and grown thereon and from crystals formed from these, comprising, in particular consisting of, 1,1-GPM are present in order to enable an efficient crystallization process and homogeneous crystal growth.
- the present invention also solves the technical problem on which it is based by providing intermediates obtained in the course of carrying out the process and the 1,1-GPM and 1,6-GPS-enriched compositions obtained.
- the present invention therefore also provides first and second crystalline and liquid phases as well as compositions enriched in 1,1-GPM and 1,6-GPS.
- the crystals contained according to the invention in the second crystalline phase and in the 1,1-GPM-enriched isomalt composition are distinguished by an advantageous morphology, in particular an advantageous length-to-width ratio of the crystals, in particular in comparison to conventionally crystallized products a small length-to-width ratio.
- the 1,1-GPM-enriched isomalt composition according to the invention like the second crystalline phase obtained in process step c), has a length-to-width ratio of the crystals contained in them of 7.0 to 10 .5, in particular from 7.5 to 10.0, in particular from 7.5 to 9.0, in particular from 7.5 to 8.5, in particular from 8.0 (each mean value).
- the 1,1-GPM-enriched isomalt composition according to the invention like the second crystalline phase obtained in process step c), has a length-to-width ratio of the crystals contained in them of 6.5 to 10 .0, in particular from 7.0 to 9.5, in particular from 7.5 to 9.0, in particular from 7.5 to 8.5, in particular from 7.8 (each median).
- the 1,1-GPM-enriched isomalt compositions obtained according to the invention are due to the special length-to-width ratio of the crystals contained in them advantageously easily separable from liquid components.
- the length-to-width ratio according to the invention reduces the formation of crystal fractures and leads to a more homogeneous particle size distribution. This is advantageous because it is known that crystal breakage can lead to broader inhomogeneous particle size distributions, possibly even bimodal particle size distributions, and to clogging of the void volume in the crystal cake, which impairs the separability of the crystals, including the drainage of the crystal cake, and thus reduces the product yield.
- the reduction in broken crystals made possible according to the invention also has the advantage that the products obtained show little or no formation of dust after drying.
- the comparatively small and thus more spherical length-to-width ratio according to the invention also brings about improved, in particular faster, sedimentation behavior in centrifuges provided for separating the crystals and better screening with improved selectivity for the dried products preferably obtained.
- the length-to-width ratio according to the invention also reduces the formation of clumps, ie the formation of crystal bodies characterized by a large length-to-width ratio, which clog separating screens due to their slim structure and thus also reduce production efficiency.
- the method according to the invention advantageously results in a particularly simple and effective crystal nucleation and/or enrichment of 1,1-GPM in a first crystalline phase and of 1,6-GPS in a first liquid phase.
- the present invention provides that the flash evaporation in process step b) takes place in a reactor, in particular a nucleator.
- the present invention provides that the crystallization process in process step c) takes place in a reactor, in particular a crystallizer.
- the present invention provides that the flash evaporation in process step b) takes place in a reactor, in particular a nucleator, and the crystallization process in process step c) takes place in a reactor, in particular that the crystallization process in process step c) takes place in the same Reactor as the flash evaporation in process step b) takes place, in particular in the same nucleator.
- the present invention provides that the reactor used in process step b) is in particular a nucleator in which optional Method step c) can be carried out, whereby the nucleator is a crystallizer at the same time.
- the present invention provides that the flash evaporation in process step b) takes place in a reactor, in particular a nucleator, and the crystallization process in process step c) takes place in a reactor, in particular that the crystallization process in process step c) takes place in another reactor as the flash evaporation in process step b) takes place, in particular in a crystallizer.
- the present invention provides that process step b) and process step c) take place in the same reactor, in particular nucleator.
- process step b) and process step c) each take place in a different reactor, namely process step b) in particular in a nucleator and process step c) in particular in a crystallizer.
- the present invention provides that the flash evaporation in process step b) takes place in a reactor, in particular a nucleator, with the reactor, in particular the nucleator, having at least one agitator.
- mechanical agitation is carried out during process step b), ie movement, in particular stirring, of the isomalt-containing solution provided in process step a) is preferably carried out during the flash evaporation.
- the mechanical agitation in process step b) is carried out by means of at least one stirrer present in the reactor, in particular the nucleator.
- the agitator preferably present in the nucleator advantageously and preferably ensures mechanical agitation, in particular particularly homogeneous mixing over the entire reactor contents of the isomalt-containing solution used according to the invention in process step b) for flash evaporation.
- This preferred homogeneous mixing caused by the agitator is achieved by shearing the in Method step a) provided and used in method step b) isomalt-containing solution achieved.
- the control of the shearing in method step b) contributes in connection with a control of the process parameters, in particular pressure and/or temperature and/or the concentration of the components 1,1-GPM and/or 1,6-GPS, in particular lowering the temperature and increasing the dry matter content contributes to inducing an advantageous rapid and homogeneous crystal nucleation, in particular at the preferably present rotor blade tips of the agitator, in order to distribute the crystal nuclei thus produced quickly and homogeneously over the entire reactor content, which results in an even growth of the crystal nuclei and a controlled reduction in supersaturation throughout the isomalt -containing solution guaranteed.
- a control of the process parameters in particular pressure and/or temperature and/or the concentration of the components 1,1-GPM and/or 1,6-GPS, in particular lowering the temperature and increasing the dry matter content contributes to inducing an advantageous rapid and homogeneous crystal nucleation, in particular at the preferably present rotor blade tips of the agitator, in order to distribute the crystal
- the preferably provided control of the shearing and/or the process parameters, in particular pressure and/or temperature leads to a homogeneous crystal nucleation which is advantageous according to the invention
- the shearing caused by the preferably provided agitator advantageously an uncontrolled crystal nucleation which only occurs with high and local supersaturation avoided, which spreads disadvantageously slowly and inhomogeneously from the point of origin over the rest of the isomalt-containing solution due to the lack of mixing.
- the shear caused by the preferably used agitator of the nucleator used in process step b) can be adjusted by selecting various stirring parameters of the agitator, in particular selected from the stirring parameters rotational speed, in particular the blade tip speed, agitator geometry, in particular the extent of cavitation generated thereby at the rotor blade tips and number and/or shape and/or angle of the individual stirring blades, in particular rotor blades.
- various stirring parameters of the agitator in particular selected from the stirring parameters rotational speed, in particular the blade tip speed, agitator geometry, in particular the extent of cavitation generated thereby at the rotor blade tips and number and/or shape and/or angle of the individual stirring blades, in particular rotor blades.
- the size and particle size distribution of the crystals that form, in particular 1,1-GPM crystals can be influenced in a targeted manner. It is thus possible according to the invention, in process step c), to subject the first isomalt-containing suspension obtained in process step b) comprising a first crystalline phase and a first liquid phase to a crystallization process, whereby a second crystalline phase and a second liquid phase comprise second isomalt-containing suspension is obtained, in particular a second isomalt-containing suspension comprising a homogeneous second crystalline phase and a second liquid phase, and wherein by controlling the shearing and/or the process parameters the number and size distribution of the 1, 1 GPM crystals.
- the at least one agitator is a rotor-stator system.
- the present invention particularly preferably provides that the rotor-stator system comprises a rotor and a stator, in particular consists of a rotor and a stator.
- the present invention particularly preferably provides that the rotor of the rotor-stator system is preferably a propeller stirrer, in particular a propeller stirrer with at least two rotor blades.
- the present invention particularly preferably provides that the stator of the rotor-stator system is preferably a central tube.
- the present invention particularly preferably provides that the rotor, in particular the propeller stirrer, is present in the stator, in particular the central tube, in particular in such a way that the rotor can rotate freely.
- the present invention particularly preferably provides that the rotor is present in the stator, in particular in such a way that the isomalt-containing solution provided according to the invention in method step a) is permanently supplied to the side of the rotor blades by the mechanical agitation preferably provided in method step b) and can be discharged on the opposite side of the rotor blades in order to ensure complete mixing of the reactor contents.
- the present invention particularly preferably provides that the rotor blades of the propeller stirrer have a specific shape, in particular a rectangular shape, a trapezoidal shape, a double trapezoidal shape or a rectangular trapezoidal shape.
- the present invention particularly preferably provides that the rotor of the rotor-stator system is a propeller stirrer, having at least 2 rotor blades, in particular 3, in particular 4, in particular 5, preferably 3 rotor blades.
- the present invention particularly preferably provides that the rotor blades of the propeller stirrer, each starting from a central attachment point, are at an angle of 36 to 180°, in particular 45 to 120°, in particular 72 to 90°, preferably 72 ° (calculated from the center one rotor blade tip to the next) to the adjacent rotor blade.
- the present invention particularly preferably provides that the rotor of the rotor-stator system is a propeller stirrer, having at least 2 rotor blades, in particular 3, in particular 4, in particular 5, preferably 3 rotor blades, each starting from a central attachment point at an angle of 36 to 180°, in particular 45 to 120°, in particular 72 to 90°, preferably 72 ° (calculated from the center of one rotor blade tip to the next) to the adjacent rotor blade.
- a propeller stirrer having at least 2 rotor blades, in particular 3, in particular 4, in particular 5, preferably 3 rotor blades, each starting from a central attachment point at an angle of 36 to 180°, in particular 45 to 120°, in particular 72 to 90°, preferably 72 ° (calculated from the center of one rotor blade tip to the next) to the adjacent rotor blade.
- the present invention particularly preferably provides that the rotor blades of the propeller stirrer rotate about their longitudinal axis by 0 °, in particular 1°, in particular 5°, in particular 10°, in particular 20°, in particular 30°, in particular 40°, in particular 45° (starting from rotor blades lying in one plane) are inclined.
- the rotor of the rotor-stator system is a propeller stirrer having at least 2 rotor blades, in particular 3, in particular 4, in particular 5, preferably 3 rotor blades, each at an angle of 36 to 180 °, in particular 45 to 120°, in particular 72 to 90°, preferably 72° (calculated from the center of one rotor blade tip to the next) to the adjacent rotor blade and around the longitudinal axis of the rotor blade by 0 °, in particular 1°, in particular 5°, in particular 10° , in particular 20°, in particular 30°, in particular 40°, in particular 45 ° (starting from rotor blades lying in one plane) are inclined.
- the rotor of the rotor-stator system is a propeller stirrer having at least 2 rotor blades, in particular 3, in particular 4, in particular 5 rotor blades, preferably 3 rotor blades, each at an angle of 36 to 180 ° , in particular 45 to 120°, in particular 72 to 90°, preferably 72° (calculated from the center of one rotor blade tip to the next) to the adjacent rotor blade, which is about the longitudinal axis of the rotor blade by 0 °, in particular 1°, in particular 5°, in particular 10°, in particular 20°, in particular 30°, in particular 40°, in particular 45 ° (starting from rotor blades lying in one plane) and which have a specific shape have, in particular a rectangular shape, a trapezoidal shape, double trapezoidal shape or rectangular trapezoidal shape.
- the procedure according to the invention leads to crystal nuclei of 1,1-GPM dihydrate forming in the nucleator, in particular forming selectively, ie with at least partial, in particular complete exclusion of 1,6-GPM.
- the procedure according to the invention makes it possible to provide a first isomalt-containing suspension in process step b) in which predominantly, in particular only, crystal nuclei are present which consist of 1,1-GPM, in particular 1,1-GPM dihydrate , exist.
- the procedure according to the invention therefore provides a particularly homogeneously structured first isomalt-containing suspension, which in a preferred embodiment is characterized in that all the crystal nuclei contained in it consist of 1,1-GPM, in particular
- 1,1-GPM crystal nuclei in particular a first crystalline phase containing only 1,1-GPM crystal nuclei, is particularly suitable for the crystallization which follows in process step c).
- the method according to the invention advantageously and particularly preferably results in increased occupational safety, since no dispersing medium, in particular alcohols, in particular isopropanol, is used in the flash evaporation, in particular by targeted control of the shearing and/or process parameters compared to conventional crystal nucleation reactors, in particular slurry reactors which, in addition to increased work safety due to the reduced risk of explosion, also results in a reduction in operating costs.
- no slurry has to be provided and added in an upstream work step.
- the method according to the invention in particular and in a preferred embodiment, by controlling the shearing and/or the process parameters, in particular supersaturation, temperature and pressure, can generate homogeneous crystal nuclei comprising 1,1-GPM, in particular consisting of this, the first liquid phase of the first isomalt-containing suspension contains dissolved 1,6-GPS in addition to solvent, whereby in the subsequent crystallization process particularly pure crystals, comprising, in particular consisting of, 1,1-GPM or 1,6-GPS or 1,1-GPM and 1.6 GPS, can be obtained.
- the method according to the invention results in a particularly uniform crystal size distribution, in particular a crystal size distribution that can be set by controlling the shearing and/or the process parameters, in the 1,1-GPM and/or 1,6-GPS-enriched phases, so that these are efficient can be separated from other phases, in particular liquid phases.
- the invention thus provides a particularly simple and efficient method for the production of
- 1-GPM and 1,6-GPS makes use of and two separate phases are obtained, each compared to the 1,1-GPM content or 1,6-GPS content of the isomalt-containing solution according to process step a). have an increased, i.e. enriched, 1.1 GPM or 1.6 GPS content.
- the procedure according to the invention makes it possible, in a single process, to obtain both a 1,1-GPM and a 1,6-GPS-enriched isomalt composition.
- According to the invention can also be provided to perform the inventive method to only one
- 1.1 GPM-enriched isomalt composition to obtain.
- it can also be provided to carry out the method according to the invention in order to provide only a 1,6-GPS-enriched isomalt composition.
- the invention provides in particular that in process step a) an isomalt-containing solution is provided which has an isomalt content of 65 to 90% by weight (based on the total weight of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) contains 70 to 85% by weight, in particular 70 to 80% by weight, of isomalt, preferably 72 to 80% by weight, preferably 74 to 80% by weight %, preferably 76 to 80% by weight, preferably 70 to 78% by weight, preferably 74 to 76% by weight, preferably 70 to 74% by weight, preferably 70 to 75% by weight 70 to 76% by weight, preferably 72 to 76% by weight, preferably 74 to 76% by weight, preferably 75 to 80% by weight, or preferably 76 to 80% by weight (in each case based on the total weight the solution containing isomalt).
- the isomalt-containing solution provided in process step a) is a saturated solution, particularly preferably a supersaturated solution.
- the isomalt-containing solution provided in process step a) has a 1,1-GPM content of 35 to 61% by weight, preferably 46 to 56% by weight, preferably 48 to 55% by weight. %, preferably 49 to 54% by weight, preferably 50 to 53% by weight (in each case based on the total weight of the dry substance of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) has a 1,6-GPS content of 39 to 65% by weight, preferably 44 to 54% by weight, preferably 45 to 52% by weight. %, preferably 46 to 51% by weight, preferably 47 to 50% by weight (in each case based on the total weight of the dry matter of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) has a 1,1-GPM content of 35 to 61% by weight, preferably 46 to 56% by weight, preferably 48 to 55% by weight. %, preferably 49 to 54% by weight, preferably 50 to 53% by weight, of 1,1-GPM and a 1,6-GPS content of 39 to 65% by weight, preferably 44 to 54% by weight , preferably 45 to 52% by weight, preferably 46 to 51% by weight, preferably 47 to 50% by weight of 1,6-GPS (in each case based on the total weight of the dry substance of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) has a 1,1-GPM content of 35 to 44% by weight and a 1,6-GPS content of 56 to 65% by weight (in each case based on the total weight of the dry matter of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) has a 1,1-GPM content of 35 to 50% by weight, preferably 37 to 48% by weight, preferably 39 to 46% by weight. %, preferably 39 to 44% by weight, preferably 39 to 42% by weight (in each case based on the total weight of the dry matter of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) has a 1,6-GPS content of 50 to 65% by weight, preferably
- the isomalt-containing solution provided in process step a) has a 1,1-GPM content of 35 to 50% by weight, preferably 37 to 48% by weight, preferably 39 to 46% by weight. %, preferably 41 to 44% by weight, preferably 41 to 42% by weight, of 1,1-GPM and a 1,6-GPS content of 50 to 65% by weight, preferably 52 to 63% by weight , preferably 54 to 61% by weight, preferably 56 to 59% by weight, preferably 58 to 59% by weight of 1,6-GPS (in each case based on the total weight of the dry substance of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) has a 1,1-GPM content of 35 to 50% by weight and a 1,6-GPS content of 50 to 65% by weight. (in each case based on the total weight of the dry substance of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) has a 1,1-GPM content of 45 to 57% by weight, preferably 47 to 56% by weight, preferably 48 to 55% by weight. %, preferably 49 to 54% by weight, preferably 50 to
- the isomalt-containing solution provided in process step a) has a 1,6-GPS content of 43 to 55% by weight, preferably 44 to 53% by weight, preferably 45 to 52% by weight. %, preferably 46 to 51% by weight, preferably 47 to 50% by weight (based on the total weight of the dry matter of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) has a 1,1-GPM content of 45 to 57% by weight, preferably 47 to 56% by weight, preferably 48 to 55% by weight. %, preferably 49 to 54% by weight, preferably 50 to 53% by weight, of 1,1-GPM and a 1,6-GPS content of 43 to 55% by weight, preferably 44 to 53% by weight , preferably 45 to 52% by weight, preferably 46 to 51% by weight, preferably 47 to 50% by weight of 1,6-GPS (in each case based on the total weight of the dry substance of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) has a 1,1-GPM content of 45 to 57% by weight and a 1,6-GPS content of 43 to 55% by weight. (in each case based on the total weight of the dry substance of the isomalt-containing solution).
- the isomalt-containing solution provided in process step a) has a temperature of 50 to 90° C., preferably 60 to 90° C., preferably 61 to 85° C., preferably 64 to 85° C., preferably 50 to 80°C, preferably 60 to 80°C, preferably 60 to 75°C, preferably 64 to 75°C, preferably 64 to 75°C, or preferably 64 to 70°C.
- the isomalt-containing solution is adjusted to one of the aforementioned temperatures in process step a).
- the isomalt-containing solution provided in process step a) has 1,1-GPM, 1,6-GPS and at least one substance selected from the group consisting of 1,1-GPS and other deoxydisaccharide alcohols , polysaccharides, oligosaccharides, trisaccharides, monosaccharides, disaccharides, sorbitol, mannitol and isomelezitose.
- the isomalt-containing solution provided in process step a) has 1,1-GPM, 1,6-GPS and at least one substance selected from the group consisting of 1,1-GPS and other deoxydisaccharide alcohols , oligosaccharides, trisaccharides, monosaccharides, disaccharides, sorbitol, mannitol and isomelezitose.
- the isomalt-containing solution provided in process step a) and further processed in process steps b) and c) has selected water, 1,1-GPM, 1,6-GPS and the at least one substance from the group consisting of 1,1-GPS, other deoxy-disaccharide alcohols, oligosaccharides, trisaccharides, monosaccharides, disaccharides, sorbitol, mannitol and isomelezitose, no other substances.
- the isomalt-containing solution provided in process step a) and further processed in process steps b) and c) contains no gum arabic.
- the isomalt-containing solution provided in process step a) and further processed in process steps b) and c) contains no further substances apart from water and 1,1-GPM and 1,6-GPS .
- the isomalt-containing solution provided in process step a) is a solution of isomalt in a solvent, in particular water, ethanol, propanol, isopropanol, butanol, isobutanol or mixtures thereof.
- the isomalt-containing solution provided in process step a) is an aqueous solution with small amounts of ethanol, propanol, isopropanol, butanol and/or isobutanol, in particular 0.1 to 5% by volume of the alcohols based on the entire aqueous solution.
- a solvent in particular water, ethanol, propanol, isopropanol, butanol, isobutanol or mixtures thereof.
- the isomalt-containing solution provided in process step a) is an aqueous solution with small amounts of ethanol, propanol, isopropanol, butanol and/or isobutanol, in particular 0.1 to 5% by volume of the alcohol
- the solvent of the isomalt-containing solution provided in process step a) is water, in particular deionized water.
- the isomalt-containing solution provided in process step a) preferably comprises no organic solvents.
- the isomalt-containing solution provided in process step a) is an aqueous solution, in particular an aqueous solution which has a pH range of 3.0 to 8.0, preferably 3.5 to 7.5 4.0 to 7.0, preferably 4.3 to 6.5, preferably 4.6 to 6.0, preferably 4.8 to 5.5, or preferably 4.9 to 5.5, preferably a pH of 4.9, preferably 6.0, preferably 8.0, preferably 4.5, preferably 4.0, preferably 3.5, preferably 3.0.
- an isomalt-containing solution is produced directly from isomalt and water, optionally from isomalt, water and other components listed above.
- the isomalt-containing solution provided in process step a) is obtained in a process step a1) taking place before process step a) from an isomalt-containing starting solution or suspension by evaporation or reverse osmosis.
- the isomalt-containing solution provided according to the invention in method step a) is obtained from a starting solution or suspension of isomalt in water by increasing the temperature of the solution or suspension, in particular at a pressure reduced compared to atmospheric pressure.
- the isomalt-containing solution provided according to the invention in method step a) is prepared from a starting solution or suspension of isomalt in water by reverse osmosis, in particular at a pressure higher than atmospheric pressure, in process step a1).
- the isomalt-containing solution provided according to the invention in method step a) is prepared in method step a) by adding crystalline isomalt to water, in particular deionized water.
- the isomalt-containing solution provided according to the invention in method step a) is prepared in method step a) by adding crystalline isomalt to a less concentrated starting solution or suspension containing isomalt.
- the isomalt-containing solution provided in step a) is prepared from a starting solution or suspension which has isomalt by concentrating the starting solution, preferably by evaporation, in particular at a pressure reduced relative to atmospheric pressure, reverse osmosis , in particular at elevated pressure relative to atmospheric pressure and/or addition of crystalline isomalt, or by diluting the starting solution or suspension, preferably by adding water, and the isomalt-containing solution provided in step a) is thus obtained.
- the isomalt-containing starting solution or suspension used for process step a1) is obtained by selective hydrogenation, in particular 1,6-GPS-selective hydrogenation.
- the isomalt-containing starting solution used for process step a1) is obtained by selective hydrogenation, in particular by selective hydrogenation using a hydrogenation catalyst, in particular a hydrogenation catalyst comprising, in particular consisting of, ruthenium or ruthenium oxide and a catalyst support.
- the isomalt-containing starting solution used for process step a1) is obtained by selective hydrogenation, in particular by selective hydrogenation using a hydrogenation catalyst comprising, in particular consisting of, nickel, Raney nickel or supported nickel.
- the isomalt-containing starting solution obtained in process step a) has a temperature of 50 to 95° C., in particular 55 to 90° C., in particular 60 to 85° C., in particular 65 to 80° C., preferably 65 to 70°C
- the isomalt-containing starting solution obtained in process step al) has a temperature that is at least 10 °C higher, preferably at least 8 °C, preferably at least 5 °C, or preferably at least 3 °C, compared to in Method step a) provided isomalt-containing solution.
- the isomalt-containing solution obtained in process step a) is preferably cooled to a temperature to be used preferably in process step a).
- process step a1) takes place in an evaporator.
- the process according to the invention comprises nucleation by means of flash evaporation.
- the temperature of the isomalt-containing solution is set after process step a) and before process step b).
- the temperature of the isomalt-containing solution fed in is adjusted to 50 to 90.degree. C., preferably to 55 to 80.degree. C., particularly preferably to 60 to 75.degree.
- the isomalt-containing solution provided in process step a) preferably has a temperature of 50 to 90.degree. C., preferably 55 to 80.degree. C., particularly preferably 60 to 75.degree.
- the flash evaporation according to process step b) is carried out continuously.
- the flash evaporation according to process step b) is carried out batchwise.
- the absolute pressure is reduced by at least 5%, preferably by at least 10%, preferably by at least 50%, preferably by at least 70, during the flash evaporation according to process step b) after process step a) and before process step c). %, or preferably by at least 90% (in each case based on the originally prevailing absolute atmospheric pressure).
- Process steps a1), a), c), d) and e) preferably take place at a pressure which is higher than process step b).
- Process steps a), c), d) and e) preferably take place at a pressure which is higher than process step b).
- Process steps a1), a), d) and e) preferably take place at a pressure which is higher than process step b).
- Process steps a), d) and e) preferably take place at a pressure which is higher than process step b).
- Process steps a1), a), c), d) and e) preferably take place at atmospheric pressure.
- Process steps a), c), d) and e) preferably take place at atmospheric pressure.
- Process steps a1), a), d) and e) preferably take place at atmospheric pressure.
- Process steps a), d) and e) preferably take place at atmospheric pressure.
- process step c) is carried out under atmospheric pressure if process step c) is carried out in the form of cooling crystallization or isothermal crystallization. If process step c) is carried out as an evaporative crystallization, process step c) preferably takes place at a pressure which is reduced relative to atmospheric pressure, in particular a vacuum.
- the absolute pressure is reduced in the flash evaporation according to process step b) after process step a) and before process step c), preferably to 10 to 500 mbar, preferably to 20 to 400 mbar, preferably 30 to 300 mbar, preferably 50 to 200 mbar, preferably 90 to 110 mbar, in particular 90 to 100 mbar.
- the absolute pressure is at most 500 mbar, preferably at most 400 mbar, preferably at most 300 mbar, preferably at most 200 mbar, preferably at most 150 mbar, preferably at most 100 mbar, preferably at most 80 mbar, preferably at most 50 mbar, preferably at most 20 mbar, preferably at most 10 mbar.
- the flash evaporation according to process step b) is carried out after process step a) and before process step c) at a temperature in the range from 30 to 70.degree. C., preferably 35 to 65.degree. C., preferably 30 to 60.degree , preferably 40 to 60 ° C, preferably 45 to 55 ° C, preferably 50 to 55 ° C performed.
- the flash evaporation according to process step b) is carried out after process step a) and before process step c) at a temperature in the range from 30 to 70.degree. C., preferably 35 to 65.degree. C., preferably 40 to 60.degree , preferably 30 to 60 ° C, preferably 45 to 55 ° C, preferably 50 to 55 ° C and at reduced absolute pressure, preferably at 10 to 500 mbar, preferably at 20 to 400 mbar, preferably 30 to 300 mbar, preferably 50 to 200 mbar, preferably 90 to 110 mbar, in particular at 90 to 100 mbar and 50 to 55 ° C.
- the isomalt-containing solution provided in process step a) is exposed to a reduced absolute pressure of up to 10 to 50%, in particular 15 to 40%, in particular 20 to 30% of the amount of dissolved 1,1-GPM contained in the isomalt-containing solution provided by method step a) has passed into the first crystalline phase and thus an accumulation of 1,1-GPM in the first crystalline phase and an enrichment of 1,6-GPS in the first liquid phase is achieved.
- Process step b) can preferably for a period of 2 minutes to 12 hours, 3 minutes to 10 hours, preferably 4 minutes to 9 hours, preferably 1 to 12 hours, preferably 2 to 8 hours, preferably 3 to 7 hours, preferably 4 to 6 hours, preferably 1 to 5 hours, preferably 2 to 5 hours, preferably 3 to 5 hours, preferably 4 to 5 hours, preferably for 5 hours.
- process step b) is carried out in such a way that during process step b) 20 to 30% of the dissolved 1,1-GPM present in process step a) pass into the first crystalline phase (based on the total weight of the dry substance (TS ) of 1,1-GPM in the process step a) provided solution).
- the flash evaporation according to process step b) is carried out after process step a) and before process step c) in such a way that during process step b) the dry substance content of the isomalt-containing solution provided in process step a) is reduced by 1 to 10 wt. %, preferably 1 to 8 wt. %, preferably 1 to 6 wt.
- the first crystalline phase of the first isomalt-containing suspension obtained after the flash evaporation according to process step b) has a 1,1-GPM content of 57 to 100% by weight, preferably 60 to 100% by weight %, preferably 62 to 99% by weight, preferably 65 to 99% by weight, preferably 67 to 95% by weight of 1,1-GPM and a 1,6-GPS content of 0 to 43% by weight.
- the first liquid phase of the first isomalt-containing suspension obtained after the flash evaporation according to process step b) has a 1,1-GPM content of 25 to 35% by weight, preferably 28 to 34% by weight %, preferably 29 to 33% by weight, preferably 30 to 32% by weight, preferably 31% by weight 1,1-GPM, and a 1,6-GPS content of 65 to 75% by weight %, preferably 66 to 72% by weight, preferably 67 to 71% by weight, preferably 68 to 70% by weight, preferably 68% by weight of 1,6-GPS (in each case based on the total weight of the process step b) dry matter remaining in the first liquid phase.
- 1,1-GPM content of 25 to 35% by weight, preferably 28 to 34% by weight %, preferably 29 to 33% by weight, preferably 30 to 32% by weight, preferably 31% by weight 1,1-GPM, and a 1,6-GPS content of 65 to 75% by weight %, preferably 66 to
- the first liquid phase of the first isomalt-containing suspension obtained after the flash evaporation according to process step b) has a dry matter content of 56 to 80% by weight, preferably 69 to 74% by weight, preferably 70 to 73% by weight, preferably 71 to 72% by weight (based on the total weight of the first suspension present after process step b)).
- no seeding with seed crystals in particular isomalt, 1,1-GPM and/or 1,6-GPS, takes place during process step b).
- the crystallization process according to process step c) is carried out in a crystallizer.
- the first isomalt-containing suspension is preferably exposed to conditions which do not allow isomalt to be completely soluble in the first liquid phase used, so that isomalt, preferably 1,1-GPM, crystallizes further, in particular the first the crystalline phase is further enriched in 1,1-GPM and the first liquid phase is further enriched in 1,6-GPS to obtain a second suspension comprising a second crystalline phase and a second liquid phase, the second crystalline phase preferably enriched with 1,1-GPM and the second liquid phase is preferably enriched with 1,6-GPS.
- 1,6-GPS and 1,1-GPM are partly dissolved and partly undissolved.
- the crystallization according to process step c) can be carried out continuously. In an embodiment preferred according to the invention, the crystallization according to process step c) can be carried out batchwise.
- the crystallization in process step c) is isothermal crystallization, cooling crystallization and/or evaporative crystallization, in particular multi-stage evaporative crystallization.
- the first isomalt-containing suspension obtained from process step b) is subjected to a crystallization, preferably an isothermal crystallization, in process step c).
- the temperature of the first isomalt-containing suspension is preferably adjusted to 50 to 60° C., preferably 52 to 60° C., preferably 54 to 60° C., preferably 51 to 59° C., preferably 52 to 59° C, preferably 53 to 59 °C, preferably 54 to 59 °C, preferably 52 to 58 °C, preferably 53 to 57 °C, preferably 53 to 58 °C, preferably 54 to 58 °C, preferably 54 to 58 °C, preferably 54 to 57 °C , preferably 54 to 57 °C, or preferably 54 to 56 °C.
- the temperature of the isothermal crystallization in process step c) is 50 to 60° C., preferably 51 to 60° C., preferably 52 to 60° C., preferably 53 to 59° C., preferably 50 to 59° C. preferably 51 to 59°C, preferably 52 to 58°C, preferably 53 to 58°C, preferably 54 to 60°C, preferably 54 to 58°C, preferably 54 to 56°C, preferably 53 to 57°C, preferably 53 to 56°C, or preferably 54 to 56°C.
- the isothermal crystallization carried out in step c) takes place at the temperature set in step c), with the crystallization energy released being continuously removed.
- the isothermal crystallization of the isomalt-containing suspension in process step c) is carried out over a period of 10 to 100 hours, preferably 20 to 100 hours, preferably 20 to 80 hours, preferably 20 to 60 hours, preferably 20 to 52 hours, preferably 20 to 40 hours, preferably 30 to 80 hours, preferably 30 to 70 hours, preferably 30 to 60 hours, preferably 30 to 50 hours or preferably 30 to 40 hours.
- step c) of the process by means of isothermal crystallization results in a homogeneous crystal size distribution, since, without being bound by theory, the steady decrease in supersaturation as the course of crystallization progresses Minimizes the risk of fine particle formation later in the process. Furthermore, this mode of operation leads to an increase in the service life of the reactor used for the crystallization, because reduced deposit formation and/or reduced incrustations compared to other crystallizations, in particular cooling crystallizations using a cooling ramp, can be observed. Without being bound to theory, the reduced deposit formation and/or incrustations are based on only small temperature differences between the cooling elements used and the isomalt-containing suspension (magma) used.
- the first isomalt-containing suspension obtained from process step b) is subjected to crystallization, preferably cooling crystallization, in process step c).
- the temperature of the cooling crystallization in process step c) is preferably gradually increased by at most 2 K/h, preferably at most 1 K/h, preferably at most 0.8 K/h, preferably at most 0.6 K/h, preferably at most 0.4 K/h, preferably at most 0.2 K/h, particularly preferably at most 0.1 K/h, in order to additionally increase the yield of crystals enriched with 1,1-GPM.
- a cooling rate of 0.8 to 1.5 K/h is preferred, preferably starting at a temperature of 65° C. and ending at 37° C.
- the cooling crystallization of the isomalt-containing suspension in process step c) is carried out over a period of 10 to 100 hours, preferably 20 to 100 hours, preferably 20 to 80 hours, preferably 20 to 60 hours, preferably 20 to 52 Hours, preferably 20 to 40 hours, preferably 30 to 80 hours, preferably 30 to 70 hours, preferably 30 to 60 hours, preferably 30 to 50 hours or preferably 30 to 40 hours.
- the crystallization in particular evaporative crystallization, in particular multi-stage evaporative crystallization, is effected by increasing the concentration of the first isomalt-containing suspension obtained from process step b) in process step c), in particular the concentration of the isomalt in the liquid phase of the first suspension containing isomalt, in particular increased by a multiple-effect evaporator.
- the multiple-effect evaporator has at least two reactors, preferably at least 3 reactors, preferably at least 4 reactors, preferably at least 5 reactors, preferably at least 6 reactors at least 7, preferably at most 3 reactors, preferably at most 4 reactors, preferably at most 5 reactors, preferably at most 6 reactors, preferably at most 7 reactors.
- At least one solvent is completely or partially removed by the multiple-effect evaporator, preferably one solvent, preferably several solvents, particularly preferably water and at least one alcohol.
- concentration of isomalt in the liquid phase of the second isomalt-containing suspension in process step c) is preferably adjusted according to the invention such that the amount of solvent is not sufficient to dissolve the entire amount of isomalt at a given temperature.
- the pressure in the multiple-effect evaporator in process step c) is from 0.01 to 2 bar, preferably from 0.01 to 1 bar, preferably from 0.01 to 0.5 bar, preferably from 0.1 to 1 bar, preferably 0.1 to 0.5 bar.
- the evaporative crystallization in process step c) in the respective reactors of the multiple-effect evaporator is isothermal crystallization in each case, ie per reactor.
- the pressure in a subsequent reactor in the multiple-effect evaporator in process step c) is reduced by at least 5%, preferably by at least 10%, preferably by at least 12%, preferably by at least 5%, compared to a preceding reactor 15%, or preferably by at least 20%.
- the temperature in a subsequent reactor in the multiple-effect evaporator in process step c) is reduced by at least 5%, preferably by at least 10%, preferably by at least 12%, preferably by at least 5% compared to a preceding reactor 15%, or preferably by at least 20%.
- the proportion of 1,1-GPM and 1,6-GPS in the 1,1-GPM-enriched second crystalline phase and in the 1,6-GPS-enriched second liquid phase can be varied by temperature and/or pressure , In particular, the temperature profile and / or the pressure profile in the individual reactors in the multiple-effect evaporator can be adjusted.
- the evaporative crystallization of the isomalt-containing suspension in process step c) is carried out over a period of 1 minute to 14 hours, in particular using a multiple-effect evaporator.
- no seeding with seed crystals in particular isomalt, 1,1-GPM and/or 1,6-GPS, takes place during the crystallization in process step c).
- no seeding with seed crystals takes place during the process, in particular during an isothermal crystallization preferred according to the invention in process step c).
- no seeding with seed crystals in particular isomalt, 1,1-GPM and/or 1,6-GPS, takes place during process steps b) and c).
- crystalline isomalt, 1,1-GPM or 1,6-GPS is added in pure or almost pure form as a seed crystal in process step c). After introducing seed crystals into the isomalt-containing solution, the more soluble 1,6-GPS crystals dissolve, while the less soluble 1,1-GPM crystals remain as crystallization nuclei.
- the second crystalline phase enriched with 1,1-GPM in process step c) contains a mixture of 1,1-GPM and 1,6-GPS with 57 to 99% by weight of 1,1-GPM and 43 to 1 wt% 1,6-GPS, preferably from 60 to 80 wt% 1,1-GPM and 20 to 40 wt% 1,6-GPS, preferably 60 to 75 wt% 1,1-GPM and 25 to 40% by weight of 1,6-GPS, preferably 65 to 75% by weight of 1,1-GPM and 25 to 35% by weight of 1,6-GPS (each based on the total weight of dry matter (TS) of the second crystalline phase).
- TS dry matter
- the second liquid phase enriched with 1,6-GPM in process step c) contains a mixture of 1,1-GPM and 1,6-GPS with 43 to 1% by weight of 1,1-GPM and 57 to 99% by weight of 1,6-GPS, preferably 20 to 25% by weight of 1,1-GPM and 80 to 75% by weight of 1,6-GPS (in each case based on the total weight of the dry substance (DS ) the second liquid phase).
- the second crystalline phase separated in process step d) has at least 60% by weight of 1,1-GPM, preferably at least 67% by weight, preferably at least 75% by weight, preferably at least 80% by weight. -%, preferably at least 85% by weight, preferably at least 90% by weight, or preferably at least 95% by weight (in each case based on the total weight (TS) of the second crystalline phase).
- the second crystalline phase separated off in process step d) has at least 99% by weight, in particular 100% by weight, of 1,1-GPM (based on the total weight (TS) of the second crystalline phase).
- the second crystalline phase separated in process step d) has at most 40% by weight of 1,6-GPS, preferably at most 32% by weight, preferably at most 25% by weight, preferably at most 20% by weight. -%, preferably at most 15% by weight, preferably at most 10% by weight, or preferably at most 5% by weight (in each case based on the total weight (TS) of the second crystalline phase).
- the second crystalline phase separated off in process step d) contains at most 1% by weight, in particular 0% by weight, of 1,6-GPS (based on the total weight (TS) of the second crystalline phase).
- the crystalline phase separated off in process step d) has no or almost no 1,6-GPS.
- the second crystalline phase separated off in process step d) has 60 to 75% by weight of 1,1-GPM, in particular 60 to 72% by weight
- 1,1-GPM preferably 65 to 71% by weight, preferably 66 to 70% by weight, 67 to 69% by weight, preferably 68% by weight (in each case based on the total weight of the second crystalline phase)
- the second crystalline phase separated off in process step d) has 60 to 75% by weight of 1,1-GPM, in particular 65 to 71% by weight,
- 1,1-GPM (each based on the total weight of the second crystalline phase) and 25 to 40 % by weight, in particular 29 to 35% by weight, of 1,6-GPS (in each case based on the total weight (TS) of the second crystalline phase).
- the second crystalline phase separated off in process step d) has a length-to-width ratio of the crystals contained in it of from 7.0 to 10.5, in particular from 7.5 to 10.0, in particular from 7.5 to 9.0, in particular from 7.5 to 8.5, in particular from 8.0 (each mean value).
- the second crystalline phase separated off in process step d) has a length-to-width ratio of the crystals contained in it of 6.5 to 10.0, in particular 7.0 to 9.5, in particular 7.5 to 9.0, in particular from 7.5 to 8.5, in particular from 7.8 (each median).
- the second liquid phase separated in process step d) has 15 to 32% by weight of 1,1-GPM, preferably 17 to 30% by weight, preferably 19 to 28% by weight, 20 to 26% by weight, preferably 21 to 24% by weight (in each case based on the total weight of the dry substance (TS) of the second liquid phase).
- the second liquid phase separated off in process step d) has at least 72% by weight of 1,6-GPS, preferably at least 75% by weight, preferably at least 80% by weight, preferably at least 85% by weight. -%, or preferably at least 90% by weight (in each case based on the total weight of the dry substance (TS) of the second liquid phase).
- the second liquid phase separated in process step d) has 68 to 85% by weight of 1,6-GPS, preferably 70 to 83% by weight, preferably 72 to 81% by weight, 74 to 80% by weight, preferably 76 to 79% by weight (in each case based on the total weight of the dry matter (TS) of the second liquid phase).
- the second liquid phase separated in process step d) has 15 to 32% by weight of 1,1-GPM, preferably 17 to 30% by weight, preferably 19 to 28% by weight, preferably 20 to 26% by weight, preferably 21 to 24% by weight (in each case based on the total weight of the dry matter (TS) of the second liquid phase) 1,1-GPM and 68 to 85% by weight 1,6-GPS , preferably 70 to 83% by weight, preferably 72 to 81% by weight, preferably 74 to 80% by weight, preferably 76 to 79% by weight, of 1,6-GPS (in each case based on the total weight of the dry matter (TS) of the second liquid phase).
- 1,1-GPM preferably 17 to 30% by weight, preferably 19 to 28% by weight, preferably 20 to 26% by weight, preferably 21 to 24% by weight (in each case based on the total weight of the dry matter (TS) of the second liquid phase) 1,1-GPM and 68 to 85% by weight 1,6-GPS ,
- the second liquid phase separated in process step d) has 15 to 32% by weight 1,1-GPM (based on the total weight of the dry substance (TS) of the second liquid phase) and 68 to 85% by weight. % 1,6-GPS on (based on the total weight of the dry substance (TS) of the second liquid phase).
- the separated second crystalline phase enriched with 1,1-GPM contains at most 20% by weight of water, preferably at most 18% by weight of water, preferably at most 15% by weight of water, preferably at most 13% by weight.
- -% water preferably 5 to 20% by weight water, preferably 8 to 18% by weight water, preferably 10 to 15% by weight water, or preferably 11 to 13% by weight water (in each case based on the total weight the second crystalline phase enriched in 1,1-GPM).
- the 1,1-GPM-enriched second crystalline phase in process step d) is separated from the 1,6-GPS-enriched second liquid phase by decanting, filtering, sedimenting or centrifuging, particularly preferably by centrifuging .
- a separation provided according to the invention, in particular centrifugation, leads to a separation of the second liquid phase from the second crystalline phase, which is enriched with 1,1-GPM, while the second liquid phase is enriched with 1,6-GPS.
- the separated 1,1-GPM-enriched second crystalline phase can be further purified and concentrated to a 1,1-GPM-enriched composition, in particular to crystalline 1,1-GPM with a purity of at least 95% by weight, preferably at least 96% % by weight, preferably at least 97% by weight, preferably at least 98% by weight or preferably at least 99% by weight (weight of 1,1-GPM based on the total weight (TS) of the composition) are further processed.
- the 1,1-GPM-enriched second crystalline phase is dried after process step d) and obtained in process step e) as a solid 1,1-GPM-enriched isomalt composition.
- the second liquid phase enriched with 1,6-GPS is concentrated at least once after process step d), preferably concentrated at least twice or preferably at least three times, and in process step e) as liquid 1,6-GPS enriched isomalt composition obtained.
- the second liquid phase enriched with 1,6-GPS is concentrated after process step d) to a dry matter content of at least 60% by weight, preferably at least 65% by weight, preferably at least 70% by weight, preferably at least 75% by weight, preferably at least 80% by weight, preferably at least 85% by weight, preferably at least 90% by weight, or preferably at least 95% by weight (in each case based on the total weight of the composition) and in process step e) obtained as a liquid 1,6-GPS-enriched isomalt composition.
- the 1,6-GPS-enriched second liquid phase is s in further purification and concentration steps to a 1,6-GPS-enriched isomalt composition, in particular to crystalline 1,6-GPS with a dry matter content of at least 95% by weight, preferably at least 96% by weight, preferably at least 97% by weight, preferably at least 98% by weight, or preferably at least 99% by weight (in each case based on the total weight of the dry substance (TS) the isomalt composition) further processed.
- TS dry substance
- the 1,6-GPS-enriched isomalt composition is obtained from the 1,6-GPS-enriched second liquid phase by the
- 1,6-GPS-enriched second liquid phase is concentrated and then crystallized by cooling, the cooling crystallization preferably takes place in a temperature range of 40 to 60 °C, preferably 50 to 60 °C, preferably 40 to 50 °C, or preferably 45 to 55 °C, and preferably at cooling rates of 0.1 to 0.3 K/h, preferably 0.2 to 0.3 K/h, or preferably 0.1 to 0.2 K/h.
- concentration and the cooling crystallization are optionally repeated under the same conditions until a desired amount of crystals is obtained.
- step d) with
- 1,6-GPS-enriched isomalt composition obtained.
- the second liquid phase enriched with 1,6-GPS is dried after process step d) and obtained in process step e) as a solid 1,6-GPS-enriched isomalt composition, in particular as a crystalline product.
- the dried 1,6-GPS-enriched composition preferably contains 0.05 to 6% by weight of water, preferably 2.0 to 3.0% by weight of water, preferably 0.05 to 2.5% by weight % by weight of water, preferably 0.05 to 1% by weight of water, preferably 0.1 to 0.5% by weight of water, preferably a maximum of 6.0% by weight of water, preferably a maximum of 4.0% by weight.
- -% water preferably a maximum of 2.5% by weight, preferably a maximum of 2.0% by weight water, preferably a maximum of 1.0% by weight water or preferably a maximum of 0.5% by weight water (in each case based on the Total weight of 1,6-GPS-enriched crystalline composition).
- the present invention provides 1,1-GPM and/or 1,6-GPS-enriched isomalt compositions which can be produced, in particular produced, by the process according to the invention.
- the 1,1-GPM-enriched isomalt composition has 60 to 72% by weight of 1,1-GPM, preferably 65 to 71% by weight, preferably 66 to 70% by weight 67 to 69% by weight, preferably 67 or 68% by weight (in each case based on the total weight of the dry substance (TS) of the 1,1-GPM-enriched composition).
- the 1,6-GPS-enriched isomalt composition of the present invention has 15 to 32% by weight of 1,1-GPM, preferably 17 to 30% by weight, preferably 19 to 28% by weight %, preferably 20 to 26% by weight, preferably 21 to 14% by weight of 1,1-GPM and 68 to 85% by weight, in particular 70 to 83% by weight, in particular 72 to 81% by weight -%, in particular 74 to 80% by weight, in particular 76 to 79% by weight, of 1,6-GPS (in each case based on the total weight of the dry substance (TS) of the 1,6-GPS-enriched composition).
- 1,1-GPM preferably 17 to 30% by weight, preferably 19 to 28% by weight %, preferably 20 to 26% by weight, preferably 21 to 14% by weight of 1,1-GPM and 68 to 85% by weight, in particular 70 to 83% by weight, in particular 72 to 81% by weight -%, in particular 74 to 80% by weight, in particular 76 to 79% by
- the invention relates to a 1,1-GPM-enriched isomalt composition containing 60 to 75% by weight of 1,1-GPM and 25 to 40% by weight of 1,6-GPS, which can be prepared in particular by a process according to the invention Process (in each case based on the total weight of the dry matter (TS) of the composition).
- TS dry matter
- the invention relates to a 1,1-GPM-enriched isomalt composition containing 60 to 75% by weight of 1,1-GPM and 25 to 40% by weight of 1,6-GPS (each based on the dry substance the total amount of 1,1-GPM and 1,6-GPS), in particular producible by a method according to the invention, in particular with a 1,1-GPM content of at least 60% by weight (based on the total weight of the dry matter (TS) the composition).
- 1,1-GPM-enriched isomalt composition containing 60 to 75% by weight of 1,1-GPM and 25 to 40% by weight of 1,6-GPS (each based on the dry substance the total amount of 1,1-GPM and 1,6-GPS), in particular producible by a method according to the invention, in particular with a 1,1-GPM content of at least 60% by weight (based on the total weight of the dry matter (TS) the composition).
- the invention relates to a 1,6-GPS-enriched isomalt composition containing 15 to 32% by weight of 1,1-GPM and 68 to 85% by weight of 1,6-GPS, which can be prepared in particular by a process according to the invention Process (in each case based on the total weight of the dry matter (TS) of the composition).
- TS dry matter
- the invention relates to a 1,6-GPS-enriched isomalt composition containing 15 to 32% by weight of 1,1-GPM and 68 to 85% by weight of 1,6-GPS (each based on the dry substance the total amount of 1,1-GPM and 1,6-GPS), in particular producible by a method according to the invention, in particular with a 1,6-GPS content of at least 68% by weight (based on the total weight of the dry matter (TS) the composition).
- 1,6-GPS-enriched isomalt composition containing 15 to 32% by weight of 1,1-GPM and 68 to 85% by weight of 1,6-GPS (each based on the dry substance the total amount of 1,1-GPM and 1,6-GPS), in particular producible by a method according to the invention, in particular with a 1,6-GPS content of at least 68% by weight (based on the total weight of the dry matter (TS) the composition).
- the 1,1-GPM-enriched isomalt composition obtained in process step e) has at least 61% by weight of 1,1-GPM, preferably at least 75% by weight, preferably at least 80% by weight. %, preferably at least 85% by weight, preferably at least 90% by weight, preferably at least 94% by weight, preferably at least 95% by weight, preferably at least 96% by weight, preferably at least 99% by weight, preferably 75 to 95% by weight, preferably 75 to 90% by weight, preferably 75 to 85% by weight, or preferably 80 to 99% by weight (in each case based on the total weight of the dry substance (TS) of the 1, 1 -GPM- enriched isomalt composition).
- TS dry substance
- the 1,6-GPS-enriched isomalt composition obtained in process step e) has at least 72% by weight of 1,6-GPS, preferably at least 75% by weight, preferably at least 80% by weight. -%, preferably at least 85% by weight, preferably at least 90% by weight, preferably at least 95% by weight, preferably at least 99% by weight, preferably 72 to 95% by weight, preferably 72 to 90% by weight. -%, preferably 72 to 85 wt .-%, or preferably 80 to 99 wt .-% (in each case based on the total weight of dry matter (TS) of the 1,6-GPS-enriched isomalt composition).
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition is in crystalline form.
- the inventive 1,1-GPM-enriched isomalt composition which is preferably one or more of the preferred inventive 1,1-GPM-enriched isomalt compositions characterized above, has a length-to-width ratio of crystals contained in it from 7.0 to 10.5, in particular from 7.5 to 10.0, in particular from 7.5 to 9.0, in particular from 7.5 to 8.5, in particular from 8.0 (each mean) on.
- the inventive 1,1-GPM-enriched isomalt composition which is preferably one or more of the preferred inventive 1,1-GPM-enriched isomalt compositions characterized above, has a length-to-width ratio of crystals contained in it from 6.5 to 10.0, in particular from 7.0 to 9.5, in particular from 7.5 to 9.0, in particular from 7.5 to 8.5, in particular from 7.8 (each median) up.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition is in semi-crystalline or amorphous form.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has, in addition to the components 1,1-GPM and 1,6-GPS, at least one further component selected from the Group consisting of mannitol, sorbitol, sucrose, 1,1-GPS (1-O-a-D-glucopyranosyl-D-sorbitol), glycosylglycitols, deoxy-disaccharide alcohols, GPI (glucopyranosyl-idit), isomaltose, isomaltulose and isomelezitose.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has 0.01 to 0.3% by weight of mannitol, preferably 0.01 to 0.2% by weight %, preferably 0.01 to 0.1% by weight, preferably 0.01 to 0.06% by weight, 0.02 to 0.3% by weight, preferably 0.02 to 0.2 % by weight, preferably 0.02 to 0.1% by weight, or preferably 0.02 to 0.06% by weight, preferably at most 0.3% by weight of mannitol, preferably at most 0.2% by weight.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention contains no mannitol.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has 0.01 to 0.4% by weight sorbitol, preferably 0.01 to 0.2% by weight %, preferably 0.01 to 0.1% by weight, preferably 0.01 to 0.04% by weight, preferably 0.02 to 0.4% by weight, preferably 0.02 to 0.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention contains no sorbitol.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has 0.01 to 2% by weight of sucrose, preferably 0.01 to 1% by weight, preferably 0.01 to 0.6% by weight, preferably 0.01 to 0.4% by weight, or preferably 0.01 to 0.1% by weight, preferably at most 2% by weight sucrose, preferably at most 1% by weight, preferably at most 0.6% by weight, preferably at most 0.4% by weight, or preferably at most 0.1% by weight (in each case based on the total weight (TS) of the 1, 1-GPM and/or 1,6-GPS enriched isomalt composition).
- sucrose preferably 0.01 to 1% by weight, preferably 0.01 to 0.6% by weight, preferably 0.01 to 0.4% by weight, or preferably 0.01 to 0.1% by weight, preferably at most 2% by weight sucrose, preferably at most 1% by weight, preferably at most 0.6% by weight, preferably at most 0.4% by weight, or preferably at most 0.1% by weight (in
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention contains no sucrose.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has 0.1 to 10% by weight of 1,1-GPS, preferably 0.1 to 8% by weight. -%, preferably 0.1 to 6% by weight, preferably 0.1 to 4% by weight, preferably 0.1 to 2% by weight, preferably 0.1 to 1% by weight, preferably 0, 1 to 0.6% by weight, preferably 0.1 to 0.4% by weight, preferably 0.1 to 0.2% by weight, preferably 0.2 to 10% by weight, preferably 0, 2 to 8% by weight, preferably 0.2 to 6% by weight, preferably 0.2 to 4% by weight, preferably 0.2 to 2% by weight, preferably 0.2 to 1% by weight %, preferably 0.2 to 0.6% by weight, or preferably 0.2 to 0.4% by weight, preferably at most 10% by weight of 1,1-GPS, preferably at most 8% by weight, preferably at most 6% by weight, preferably at most 4% by weight, preferably at most 10% by weight of
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention contains no 1,1-GPS.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has 0.01 to 2% by weight of glycosylglycitols, preferably 0.01 to 1% by weight, preferably 0.01 to 0.6% by weight, preferably 0.01 to 0.4% by weight, preferably 0.01 to 0.1% by weight, preferably 0.03 to 2% by weight, preferably 0.03 to 1% by weight, preferably 0.03 to 0.6% by weight, preferably 0.03 to 0.4% by weight, preferably 0.03 to 0.1% by weight, or preferably 0.03 to 0.1% by weight, preferably at most 2% by weight of glycosylglycitols, preferably at most 0.6% by weight, preferably at most 0.4% by weight, or preferably at most 0.1% by weight % (in each case based on the total weight (TS) of the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition).
- TS total weight
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention contains no glycosylglycitols.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has 0.01 to 2% by weight of deoxydisaccharide alcohols, preferably 0.01 to 1% by weight. , preferably 0.01 to 0.6% by weight, preferably 0.01 to 0.2% by weight, preferably 0.01 to 0.1% by weight, preferably 0.03 to 2% by weight , preferably 0.03 to 1% by weight, preferably 0.03 to 0.6% by weight, preferably 0.03 to 0.2% by weight, or preferably 0.03 to 0.1% by weight %, preferably at most 2% by weight of deoxydisaccharide alcohols, preferably at most 1% by weight, preferably at most 0.6% by weight, preferably at most 0.2% by weight, or preferably at most 0.1% by weight (in each case based on the total weight (TS) of the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition).
- TS total weight
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention contains no deoxydisaccharide alcohols.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has 0.01 to 2% by weight GPI, preferably 0.01 to 1% by weight, preferably 0.01 to 0.6% by weight, preferred 0.01 to 0.4% by weight, or preferably 0.01 to 0.1% by weight, preferably at most 2% by weight GPI, preferably at most 1% by weight, preferably at most 0.6% by weight %, preferably at most 0.4% by weight, or preferably at most 0.1% by weight (in each case based on the total weight (TS) of the 1,1-GPM and/or 1,6-GPS-enriched ones isomalt composition).
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention contains no GPI.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has 0.01 to 2% by weight isomaltose, preferably 0.01 to 1% by weight, preferably 0.01 to 0.6% by weight, preferably 0.01 to 0.4% by weight, or preferably 0.01 to 0.1% by weight, preferably at most 2% by weight GPI, preferably at most 1% by weight, preferably at most 0.6% by weight, preferably at most 0.4% by weight, or preferably at most 0.1% by weight (in each case based on the total weight (TS) of the 1, 1-GPM and/or 1,6-GPS enriched isomalt composition).
- isomaltose preferably 0.01 to 1% by weight, preferably 0.01 to 0.6% by weight, preferably 0.01 to 0.4% by weight, or preferably 0.01 to 0.1% by weight, preferably at most 2% by weight GPI, preferably at most 1% by weight, preferably at most 0.6% by weight, preferably at most 0.4% by weight, or preferably at
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention contains no isomaltose.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has 0.01 to 2% by weight isomelezitose, preferably 0.01 to 1% by weight, preferably 0.01 to 0.6% by weight, preferably 0.01 to 0.4% by weight, or preferably 0.01 to 0.1% by weight, preferably at most 2% by weight GPI, preferably at most 1% by weight, preferably at most 0.6% by weight, preferably at most 0.4% by weight, or preferably at most 0.1% by weight (in each case based on the total weight (TS) of the 1, 1-GPM and/or 1,6-GPS enriched isomalt composition).
- isomelezitose preferably 0.01 to 1% by weight, preferably 0.01 to 0.6% by weight, preferably 0.01 to 0.4% by weight, or preferably 0.01 to 0.1% by weight, preferably at most 2% by weight GPI, preferably at most 1% by weight, preferably at most 0.6% by weight, preferably at most 0.4% by weight, or
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention contains no isomelezitose.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has a particle size distribution according to which at least 90% of the particles have a particle size, in particular a diameter, of 100 to 1000 mhi have, preferably 100 to 800 mhi, preferably 100 to 200 mhi, preferred 100 to 500 mih, preferably 200 to 800 mih, preferably 300 to 600 mih, preferably 20 to 80 mih, preferably 40 to 80 mih, or preferably 50 to 100 mih.
- the 1,1-GPM and/or 1,6-GPS-enriched isomalt composition according to the invention has a particle size distribution according to which at least 90% of the particles have a particle size, in particular a diameter, of at most 1000 mhi , preferably at most 800 mhi, preferably at most 600 mhi, preferably at most 500 mhi, preferably at most 400 mhi, preferably at most 200 mhi, preferably at most 100 mhi, preferably at most 80 mhi, preferably at most 40 mhi, preferably at most 20 mhi.
- the present invention also provides the use of the 1,1-GPM and/or 1,6-GPS-enriched isomalt compositions produced by the process of the invention in products for human and/or animal consumption.
- the product for human or animal consumption is preferably a food or beverage or a pharmaceutical product.
- the food or luxury food is a confectionery, a filling for confectionery, a soft caramel, a hard caramel, a fondant, a yoghurt, a pastry, a chewing gum, an ice cream, milk, a milk product, a drink, fruit juice, a fruit concentrate, a fruit preparation, a jam, a jelly or a smoothie.
- the term "isomalt” or “hydrogenated isomaltulose” preferably means a mixture consisting of or comprising 1,1-GPM and 1,6-GPS, in particular a mixture consisting of or comprising 35 to 61 wt % 1,1-GPM and 65 to 39% by weight 1,6-GPS, in particular an equimolar or nearly equimolar mixture consisting of or comprising 1,1-GPM and 1,6-GPS.
- isomalt can also be understood to mean mixtures consisting of or comprising 1,1-GPM and 1,6-GPS which do not have an equimolar ratio of 1,1-GPM to 1,6-GPS, but in which a higher 1,1 - GPM greater than 1.6 GPS or greater than 1.6 GPS than 1.1 GPM.
- the isomalt has no further components apart from the two components 1,1-GPM and 1,6-GPS. In a particularly preferred embodiment, the isomalt has both components
- 1.1-GPM and 1,6-GPS additionally one or more other components, for example mannitol, sorbitol, sucrose, 1,1-GPS (1-O-a-D-glucopyranosyl-D-sorbitol), glycosylglycitols, deoxy-disaccharide alcohols, GPI (glucopyranosyl -idit), isomaltose, isomaltulose, isomelezitose, hydrogenated or non-hydrogenated oligosaccharides, in particular hydrogenated or non-hydrogenated trisaccharides, and/or other substances.
- mannitol sorbitol
- sucrose 1,1-GPS (1-O-a-D-glucopyranosyl-D-sorbitol)
- glycosylglycitols glycosylglycitols
- deoxy-disaccharide alcohols deoxy-disaccharide alcohols
- 1.1-GPM and/or 1,6-GPS-enriched isomalt composition preferably means a 1,1-GPM and/or 1,6-GPS-enriched isomalt, ie in the case of a 1,1-GPM-enriched one Isomalt composition means a composition in which a higher content of 1,1-GPM than 1,6-GPS is present and in the case of a 1,6-GPS-enriched isomalt composition, a composition in which a higher 1, 6 GPS as 1.1 GPM content is included.
- 1.1-GPM-enriched phase or a 1,1-GPM-enriched isomalt composition obtained according to the invention in particular a phase or a mixture understood in which at least 57% by weight of 1,1-GPM, preferably at least 60, in particular at least 70, in particular at least 80, in particular at least 90, in particular at least 95, in particular at least 98, in particular at least 99% by weight 1,1-GPM and at most 43% by weight 1,6-GPS, in particular at most 40, in particular no more than 30, in particular no more than 20, in particular no more than 10, in particular no more than 5, in particular no more than 2, in particular no more than 1% by weight 1,6-GPS (in each case based on the total weight of the dry substance of the amount of 1 ,6-GPS and 1.1-GPM).
- 1,1-GPM preferably at least 60, in particular at least 70, in particular at least 80, in particular at least 90, in particular at least 95, in particular at least 98, in particular at least 99% by weight 1,1-GP
- a 1,6-GPS-enriched phase obtained according to the invention or a 1,6-GPS-enriched isomalt composition obtained according to the invention is understood as meaning a phase or a mixture in which at least 57% by weight % 1,6-GPS, preferably at least 60, in particular at least 70, in particular at least 80, in particular at least 90, in particular at least 95, in particular at least 98, in particular at least 99% by weight 1,6-GPS and at most 43% by weight 1,1-GPM, in particular no more than 40, in particular no more than 30, in particular no more than 20, in particular no more than 10, in particular no more than 5, in particular no more than 2, in particular no more than 1% by weight 1,1-GPM (in each case based on the total weight of the dry matter of the amount of 1,1-GPM and 1,6-GPS present in the phase or composition).
- a 1,1-GPM and/or 1,6-GPS-enriched isomalt composition can also be a 1,1-GPM and/or 1,6-GPS-enriched phase.
- 1.1-GPM-enriched phase and a 1.1-GPM-enriched isomalt composition obtained according to the invention, in particular according to process step e), has a higher
- the 1,1-GPM content in the 1,1-GPM-enriched phase or composition is preferably increased by at least 5, at least 10, at least 15, at least 20, at least 30, at least 40, at least 50, at least 60, at least 70, at least 80, at least 90, at least 100, at least 150 and in particular at least 200% by weight (in each case based on the 1,1-GPM content in the isomalt solution provided according to process step a) ) elevated.
- the 1,6-GPS content in the 1,6-GPS-enriched phase or composition is preferably at least 5, at least 10, at least 15, at least 20, at least 30, at least 40, at least 50, at least 60, at least 70, at least 80, at least 90, at least 100, at least 150 and in particular at least 200% by weight (in each case based on the 1,6-GPS content in the isomalt solution provided according to process step a) ) elevated.
- nucleation is understood to mean crystal nucleation, ie the first sub-process that initiates a first-order phase transition.
- a new phase that is thermodynamically stable under the given conditions is formed by nuclei from an already existing, metastable phase, preferably an oversaturated phase.
- supersaturated solution or “supersaturated phase” means a metastable state of a solution containing a greater amount of a solute than the solubility of that substance at a particular temperature.
- Such a supersaturated solution preferably forms by slowly cooling a saturated solution, by evaporating part of the solvent, or by a combination of cooling the saturated solution and evaporating part of the solvent before the excess solute precipitates, in particular crystallizes.
- flash evaporation is understood to mean flash evaporation, ie the formation of vapor when the pressure is reduced in a reactor filled with liquid.
- Llash evaporation produces an increase in supersaturation of the isomalt-containing solution which, in combination with the shear forces acting on the solution, leads to nucleation.
- a Llash evaporator when the pressure drops in a reactor filled with liquid, vapor is formed, in particular since the liquid enters the reactor superheated during Llash evaporation. The energy transfer induced in this way leads to a cooling of the solution, in particular the supersaturated solution, with a simultaneous increase in the dry matter content, as a result of which nucleation occurs. Flash evaporation occurs in a reactor filled with saturated or supersaturated liquid and associated vapor phase when the pressure is reduced.
- the Llash evaporation can preferably be carried out continuously or batchwise.
- a continuous Llash evaporation which is preferably carried out according to the invention, an isomalt-containing solution is fed continuously to the reactor while the crystal syrup suspension according to the invention obtained by Llash evaporation is removed at the same time.
- isothermal crystallization means the crystallization of a solution or suspension, which is kept at a constant crystallization temperature until the crystallization is complete or until a certain amount of a component, in particular one with 1.1 - GPM-enriched crystalline phase or a 1,6-GPS-enriched crystalline phase from which solution or suspension has crystallized.
- a 1,1 GPM-enriched or a 1,6-GPS-enriched phase is referred to as a 1,1-GPM-enriched or 1,6-GPS-enriched phase.
- enriched isomalt composition understood similar physical and chemical properties, such as a liquid or crystalline phase. Accordingly, such a phase has at least one 1,1-GPM-enriched or 1,6-GPS-enriched isomalt composition, optionally together with one or more solvents.
- a “multiple effect evaporator” is understood to be an evaporator in which a solution or suspension is crystallized in several stages at low temperatures.
- a solution is brought to the boil in a series of stages, with each successive reactor being at a lower pressure than the previous one.
- the boiling point of the solvent in the series of reactors connected to one another decreases successively.
- cooling crystallization means the crystallization of a substance from a solution or suspension by lowering the temperature until crystallization is complete or until a certain amount of a component, in particular a crystalline one enriched with 1,1-GPM Phase or a 1,6-GPS-enriched crystalline phase from which solution or suspension has crystallized.
- multi-stage evaporative crystallization means the enrichment of a crystalline phase by crystallization in a plurality of reactors, each with different pressure levels and/or temperatures.
- a “phase” is understood to mean a coherent or non-coherent spatial portion of the suspension in which homogeneous, essentially identical material properties are present.
- a liquid phase is therefore that part of the suspension that is characterized by its liquid state of aggregation.
- a crystalline phase is the part of the suspension that is characterized by its crystalline and thus solid state of aggregation.
- a “crystalline phase” or a “liquid phase” is understood to mean a phase which forms in the course of the procedure according to process steps b) and c).
- a “reduced or lowered” absolute pressure is understood to be an absolute pressure that is reduced compared to the absolute ambient pressure, in particular the atmospheric pressure of 1 bar.
- the term “and/or” is understood to mean that all members of a group which are connected by the term “and/or” are represented both cumulatively with one another in any combination and alternatively to one another.
- the expression “A, B and/or C” is to be understood as meaning the following disclosure content: i) (A or B or C), or ii) (A and B), or iii) (A and C), or iv) (B and C), or v) (A and B and C).
- “shear” is understood to mean mechanical agitation, ie preferably movement, in particular stirring.
- agitator is understood to mean in particular a rotor-stator system.
- rotor-stator system is understood to mean, in particular, a homogenizer.
- rotor is understood to mean the rotating part of a homogenizer, in particular when there is a stator.
- stator is understood to mean the immovable part of a homogenizer, in particular when a rotor is present.
- the rotor is a propeller stirrer that is present in the stator, a central tube, and can rotate in the central tube.
- Rectangular shape understood a rotor blade that has a constant blade depth.
- a rotor blade with a trapezoidal shape is understood to mean a rotor blade that has a blade depth that decreases over the length.
- Double trapezoidal shape means a rotor blade that has a blade depth that increases and then decreases over the length.
- Rectangular trapezoidal shape means a rotor blade that has a blade depth that is constant over its length and then decreases.
- crystal is understood to mean a solid with building blocks, in particular molecules, arranged regularly in a crystal structure.
- reactor is understood to mean a container, in particular a container, in particular a maturing container, in which method step b) and/or method step c) is particularly preferably carried out.
- evaporation means the transition of a liquid or a liquid mixture into the gaseous state of aggregation.
- reverse osmosis is understood to mean the reverse principle of osmosis, with osmosis describing the process of equalizing the concentration of two liquids through a semi-permeable membrane.
- the reverse osmosis takes place particularly preferably at a pressure which is higher than atmospheric pressure.
- the dissolved substance, in particular isomalt remains in the starting solution or suspension and the solvent, in particular water, is discharged through the solvent-permeable, in particular water-permeable, membrane.
- seeding means the addition of seed crystals to the solution or suspension to be seeded.
- blade tip speed is also understood to mean rotor blade tip speed, which is measured at the tip, ie the outer end of the rotor blade.
- the length to width ratio of crystals is determined according to the methodology described in Example 2.
- Figure 1 Solubility diagram according to Schiweck (H. Schiweck, alimenta 19, Palatinit® - production, technological properties and analysis of palatinit-containing foods, 5-16, 1980) for 1,1-GPM (GPM, 3), 1,6-GPS ( GPS, 2) and isomalt (isomalt, 1) in water, in which the solubility limits of the above components are shown as a function of temperature,
- Figure 2A to 2D micrographs of crystallization products from example 2.1 (magnification x4)
- Figure 3A to 3D Microscopic images of crystallization products from Example 2.1 (magnification xlO),
- Figure 4A to 4D microscopic images of crystallization products from example 2.2 (magnification x10 and x20),
- FIGS. 5A to 5F Microscopic images of crystallization products from Example 2.3 (magnification x4 and x10),
- FIG. 6A to 6F Microscopic images of crystallization products from example 2.4 (magnification x4 and x10), Example 1:
- isomalt hydromaltulose
- 1,1-GPM and 1,6-GPS-enriched isomalt compositions by means of flash evaporation in process step b) and subsequent isothermal crystallization in process step c).
- the two main components of isomalt ie 1,1-GPM and 1,6-GPS, have different solubility products in aqueous solutions ( Figure 1).
- each component develops its own solubility equilibrium.
- the equilibria that develop are temperature-dependent at the same concentration of the suspension of isomalt in water. At the same temperature, the proportion of 1,6-GPS in the solution increases with the proportion of dry matter (TS) in the suspension.
- TS dry matter
- the solubility diagram of 1,1-GPM, 1,6-GPS and isomalt shows a steady increase in the solubility of the individual components with increasing temperature.
- the present invention takes advantage of this observation.
- An isomalt-containing solution obtained by customary process steps is thermally thickened to a dry matter content of 70 to 85% by weight in a process step a1).
- the isomalt-containing solution obtained in this way and provided in process step a) (isomalt content 70 to 85% by weight based on the total weight of the solution) with a 1,1-GPM content of 35 to 44% by weight, viz 40.7% by weight, and a content of 1,6-GPS from 56 to 65% by weight, namely 58.4% by weight, 0.01 to 2% by weight GPI, 0.01 to 2% by weight glycosylglycitols, 0.01 to 0.4% by weight sorbitol, 0.001 to 2% by weight deoxy-disaccharide alcohols, 0.1 to 10% by weight 1,1-GPS and/or 0.01 up to 0.3 wt subjected to flash evaporation.
- the flash evaporation is operated at an absolute pressure of 50 to 200 mbar, in particular 90 to 100 mbar, and a temperature of 50 to 55.degree.
- the reduced absolute pressure increases the vapor pressure and the induced energy dissipation means that 1,1-GPM, which is less soluble in water than 1,6-GPS (see solubility according to Schiweck, Figure 1), corresponding to its thermodynamic solubility product in a crystalline first phase passes (initial about 5% of the 1,1-GPM in the starting solution). Due to the agitator geometry used in the reactor and the shear forces continuously generated in this way, more are constantly being generated
- the first isomalt-containing suspension obtained from process step b), comprising 1,1-GPM-enriched crystal nuclei obtained from process step b), is continuously subjected to a crystallization process according to process step c), carried out in a temperature-controlled crystallizer.
- a crystallization process according to process step c) carried out in a temperature-controlled crystallizer.
- the crystal nuclei enriched with 1,1-GPM continue to grow into crystals until the residual supersaturation has largely dissipated. Maintaining isothermal conditions is ensured by the continuous dissipation of the released crystallization energy.
- the yield of crystals enriched with 1,1-GPM is additionally increased by slowly gradually lowering the temperature of the aging tank (crystallizer) (maximum 0.5 K/h, in particular maximum 0.1 K/h) to 55 °C without thereby negatively affecting the purity of these crystals.
- the second suspension obtained in this way can be worked up using suitable separation techniques according to process step d) (e.g.
- the second crystalline phase thus obtained containing 69.9% by weight of 1,1-GPM and 29.8% by weight of 1, 6-GPS (based on the total weight of the dry matter of the second crystalline phase) and the separated second liquid phase 20.2% by weight 1,1-GPM and 78.6% by weight 1,6-GPS (based on the total weight of dry substance of the second liquid phase).
- Example 2.1 the process according to the invention is compared with known crystallization processes (Examples 2.2 to 2.4).
- the experiments were carried out in a 2 liter cooling crystallizer. This is equipped with an agitator and a double jacket for heating by means of a thermostat. Crystal magmas were separated in a heated pressure filter or in a pilot plant centrifuge. A microscope was used to image the crystals in the crystal suspensions. Olympus Stream Motion software was used for image analysis.
- a diagonal line drawn through the microscopic crystal photo (crystal image) is preferably used as a random number generator and all crystals on this diagonal line that allow a clear delimitation and determination of the crystal length and width are used to determine the length-to-width ratio, with the line at least twenty crystals must be visible. Otherwise, another micrograph was taken and used.
- Table 1 below shows the 1,1-GPM and 1,6-GPS contents of the isomalt solutions used in this example in relation to TS (dry matter) and total mass of the isomalt solution).
- a second suspension (magma) obtained according to the teaching of Example 1 is partially removed from the crystallizer before centrifuging according to process step d), diluted in glycerol and crystal images are recorded. Furthermore, a separation according to process step d) of the solid phase from the liquid phase is carried out in a centrifuge at a speed of 1800 revolutions per minute for 30 minutes:
- Figures 2A to 2D show crystal images of the obtained magma dispersed in glycerol, magnification x4, and Figures 3A to 3D show crystal images of the obtained magma dispersed in glycerol, magnification x10.
- the length-to-width ratio of the crystals obtained in the magma and in the second crystalline phase obtained in process step d) was 8.0 (mean value) and 7.8 (median).
- the crystals obtained in the solid phase are particularly pure and show a high degree of uniformity in shape and size.
- the crystal suspension after the end of the crystallization shows no formation of fine grains in the crystal image.
- the length-to-width ratio of the crystals contained in the second crystalline phase obtained in process step d) is comparatively small.
- the second crystalline phase obtained was separated by centrifugation without any problems and in a very satisfactory manner, which is reflected in particular in the accumulation of 1,1-GPM in the crystalline phase after centrifugation.
- Filtrate i.e. the 1.6-GPS-enriched second liquid phase, drains very well out of the filter cake.
- an enrichment of 1,1-GPM and a depletion of 1,6-GPS is found according to the invention, while likewise in the obtained second liquid 1,6-GPS-enriched phase an enrichment of 1,6-GPS and a depletion of 1,1-GPM in each case compared to the starting composition is observed.
- Example 2.2 (not according to the invention):
- WO 1997/008958 A1 discloses processes for the production of 1,6-GPS-enriched and 1,1-GPM-enriched mixtures.
- Example 2 of this document discloses the preparation of 1,1-GPM and 1,6-GPS-enriched 1,1-GPM/1,6-GPS mixtures, Isomalt R being added to 5 kg of water (deionized) and the resulting suspension at 35° C is stirred for 1 - 20 hours depending on grain size. This suspension is then separated at 35° C. into a liquid phase and a solid phase in a heated pressure filter.
- Example 2 of WO 1997/008958 A1 the starting material used for the desired enrichments and subsequent separation of the enriched solid and liquid phase is not an isomalt-containing solution, but a suspension of isomalt in water. Therefore, within the scope of this method, no crystallization of isomalt components from a solution takes place during the approximately 20-hour incubation at 35 °C, but only partial dissolution and dissolution of undissolved isomalt components from the solid phase of the suspension into the liquid phase and vice versa.
- Figures 4A and 4B show images of the obtained magma dispersed in glycerol, magnification x10
- Figures 4C and 4D show images of the obtained magma dispersed in glycerol, magnification x20.
- the principle of enrichment implemented in this comparative example is based on releasing the more soluble 1,6-GPS component from a solid containing 1,1-GPM and 1,6-GPS and thus does not correspond to an enrichment according to the invention by crystallization from a 1.1 GPM and 1.6 GPS containing solution.
- Table 3 below shows the 1,1-GPM and 1,6-GPS contents of the phases obtained after separation.
- EP 0859 006 B2 discloses processes for the production of 1,6-GPS-enriched and 1,1-GPM-enriched mixtures.
- Example 1 of this document discloses the preparation of 1,1-GPM and 1,6-GPS-enriched 1,1-GPM/1,6-GPS mixtures using a seeding step and two different cooling rates during crystallization.
- the separation in the centrifuge could not be carried out satisfactorily.
- the amount of effluent was small.
- the filter cake had a high level of residual moisture that was clearly visible.
- Figures 5A, 5B and 5C show crystal images, magma dispersed in glycerol, magnification x4, and Figures 5D, 5E and 5F crystal images, magma dispersed in glycerol, magnification x10.
- the length-to-width ratio of the crystals in the magma 11.2 (mean) and 11.1 (median).
- Table 4 below shows the 1,1-GPM and 1,6-GPS contents of the phases obtained after separation.
- Table 4 Analysis of the enriched phases (filter cake is the solid crystalline phase, filtrate is the liquid phase), each based on the total mass
- the crystal images clearly show that significant fine grain formation occurs in the crystal suspension after crystallization is complete.
- the length-to-width ratio of the crystals is relatively large.
- the separation of the crystalline phase by means of centrifugation is not possible satisfactorily.
- the accumulation of 1,1-GPM in the crystalline phase obtained after centrifugation is minimal and the contents of 1,1-GPM and 1,6-GPS in the filter cake roughly correspond to the composition of the starting solution.
- the 1.6-GPS-enriched filtrate drains very poorly out of the filter cake.
- US Pat. No. 6,414,138 B1 also discloses methods for producing 1,6-GPS-enriched and 1,1-GPM-enriched mixtures.
- Example 1 of this document discloses the preparation of 1,1-GPM and 1,6-GPS enriched 1,1-GPM/1,6-GPS mixtures as described in Example 2.3 but using two different cooling rates during crystallization without seeding.
- Figures 6A, 6B and 6C show crystal images, magma dispersed in glycerol, magnification x4, and Figures 6D, 6E and 6F crystal images, magma dispersed in glycerol, magnification x10.
- the length-to-width ratio of the crystals in the magma was 11.3 (mean) and 10.5 (median).
Abstract
Description
Claims
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KR1020237038975A KR20230169319A (ko) | 2021-04-15 | 2022-04-13 | 1,1-gpm 및/또는 1,6-gps가 풍부한 이소말트 조성물을 제조하는 방법 |
CA3212929A CA3212929A1 (en) | 2021-04-15 | 2022-04-13 | Process for producing 1,1-gpm- and/or 1,6-gps-enriched isomalt compositions |
BR112023021244A BR112023021244A2 (pt) | 2021-04-15 | 2022-04-13 | Composições de isomalte enriquecidas em 1,1-gpm e/ou 1,6-gps, método para produzir as mesmas e uso das mesmas |
IL307693A IL307693A (en) | 2021-04-15 | 2022-04-13 | Process for the production of Isomalt preparations enriched with GPM-1,1 and/or GPS-1,6 |
AU2022257285A AU2022257285A1 (en) | 2021-04-15 | 2022-04-13 | Process for producing 1,1-gpm- and/or 1,6-gps-enriched isomalt compositions |
JP2023562845A JP2024514609A (ja) | 2021-04-15 | 2022-04-13 | 1,1-gpm及び/又は1,6-gps富化イソマルト組成物を製造する方法 |
CN202280027885.7A CN117119908A (zh) | 2021-04-15 | 2022-04-13 | 生产富含1,1-gpm和/或1,6-gps的异麦芽酮糖醇组合物的方法 |
EP22723054.7A EP4322767A1 (de) | 2021-04-15 | 2022-04-13 | Verfahren zur herstellung von 1,1-gpm- und/oder von 1,6-gps-angereicherten isomalt-zusammensetzungen |
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DE2520173A1 (de) | 1975-05-06 | 1976-12-02 | Sueddeutsche Zucker Ag | Glucopyranosido-1,6-mannit, ein verfahren zu seiner herstellung sowie seine verwendung als zuckeraustauschstoff |
EP0625578A1 (de) | 1993-05-06 | 1994-11-23 | Südzucker Aktiengesellschaft Mannheim/Ochsenfurt | Süssungsmittel, Verfahren zur Herstellung desselben sowie dessen Verwendung |
WO1997008958A1 (de) | 1995-09-02 | 1997-03-13 | Südzucker Aktiengesellschaft | Zuckerfreie dragierte produkte |
US6414138B1 (en) | 1997-02-14 | 2002-07-02 | Sudzucker Aktiengesellschaft | Process for producing mixtures rich in 1,6-GPS or 1,1-GPM |
-
2022
- 2022-04-13 KR KR1020237038975A patent/KR20230169319A/ko unknown
- 2022-04-13 AU AU2022257285A patent/AU2022257285A1/en active Pending
- 2022-04-13 IL IL307693A patent/IL307693A/en unknown
- 2022-04-13 BR BR112023021244A patent/BR112023021244A2/pt unknown
- 2022-04-13 WO PCT/EP2022/059965 patent/WO2022219094A1/de active Application Filing
- 2022-04-13 JP JP2023562845A patent/JP2024514609A/ja active Pending
- 2022-04-13 CN CN202280027885.7A patent/CN117119908A/zh active Pending
- 2022-04-13 CA CA3212929A patent/CA3212929A1/en active Pending
- 2022-04-13 EP EP22723054.7A patent/EP4322767A1/de active Pending
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DE2520173A1 (de) | 1975-05-06 | 1976-12-02 | Sueddeutsche Zucker Ag | Glucopyranosido-1,6-mannit, ein verfahren zu seiner herstellung sowie seine verwendung als zuckeraustauschstoff |
EP0625578A1 (de) | 1993-05-06 | 1994-11-23 | Südzucker Aktiengesellschaft Mannheim/Ochsenfurt | Süssungsmittel, Verfahren zur Herstellung desselben sowie dessen Verwendung |
WO1997008958A1 (de) | 1995-09-02 | 1997-03-13 | Südzucker Aktiengesellschaft | Zuckerfreie dragierte produkte |
EP1013175A1 (de) * | 1995-09-02 | 2000-06-28 | Südzucker Aktiengesellschaft Mannheim/Ochsenfurt | Zuckerfreie dragierte Produkte |
US6414138B1 (en) | 1997-02-14 | 2002-07-02 | Sudzucker Aktiengesellschaft | Process for producing mixtures rich in 1,6-GPS or 1,1-GPM |
EP0859006B2 (de) | 1997-02-14 | 2006-09-13 | Südzucker Aktiengesellschaft Mannheim/Ochsenfurt | Verfahren zur Herstellung alpha-D-Glucopyranosyl-(1-6)-D-sorbit- oder alpha-D-Glucopyranosyl-(1-6)-D-mannit-reicher Gemische aus hydrierter Isomaltulose |
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MARGARET A. CLARKE: "Carbohydrates in industrial synthesis : proceedings of the symposium of the Division of Carbohydrate Chemistry of the American Chemical Society", 1992, BARTENS, DE, ISBN: 978-3-87040-052-1, article "3.2 Production of Isomalt", pages: 48 - 55, XP009530270 * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN117186161A (zh) * | 2023-11-06 | 2023-12-08 | 山东百龙创园生物科技股份有限公司 | 一种异麦芽酮糖醇及其制备方法 |
CN117186161B (zh) * | 2023-11-06 | 2024-01-16 | 山东百龙创园生物科技股份有限公司 | 一种异麦芽酮糖醇及其制备方法 |
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IL307693A (en) | 2023-12-01 |
AU2022257285A1 (en) | 2023-09-28 |
CA3212929A1 (en) | 2022-10-20 |
BR112023021244A2 (pt) | 2023-12-19 |
KR20230169319A (ko) | 2023-12-15 |
CN117119908A (zh) | 2023-11-24 |
EP4322767A1 (de) | 2024-02-21 |
JP2024514609A (ja) | 2024-04-02 |
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