SK279610B6 - Method of crystalline alpha,alpha-trehalose isolation - Google Patents
Method of crystalline alpha,alpha-trehalose isolation Download PDFInfo
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- SK279610B6 SK279610B6 SK697-95A SK69795A SK279610B6 SK 279610 B6 SK279610 B6 SK 279610B6 SK 69795 A SK69795 A SK 69795A SK 279610 B6 SK279610 B6 SK 279610B6
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- HDTRYLNUVZCQOY-UHFFFAOYSA-N α-D-glucopyranosyl-α-D-glucopyranoside Natural products OC1C(O)C(O)C(CO)OC1OC1C(O)C(O)C(O)C(CO)O1 HDTRYLNUVZCQOY-UHFFFAOYSA-N 0.000 title claims abstract description 34
- HDTRYLNUVZCQOY-LIZSDCNHSA-N alpha,alpha-trehalose Chemical compound O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@@H]1O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 HDTRYLNUVZCQOY-LIZSDCNHSA-N 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000002955 isolation Methods 0.000 title claims abstract description 11
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 44
- 239000012528 membrane Substances 0.000 claims abstract description 20
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims abstract description 14
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 claims abstract description 14
- 238000001471 micro-filtration Methods 0.000 claims abstract description 12
- 239000011148 porous material Substances 0.000 claims abstract description 8
- 229920001577 copolymer Polymers 0.000 claims abstract description 6
- 150000001450 anions Chemical class 0.000 claims abstract description 4
- UEEJHVSXFDXPFK-UHFFFAOYSA-N N-dimethylaminoethanol Chemical group CN(C)CCO UEEJHVSXFDXPFK-UHFFFAOYSA-N 0.000 claims abstract description 3
- 230000002378 acidificating effect Effects 0.000 claims abstract description 3
- 238000005115 demineralization Methods 0.000 claims abstract description 3
- 239000000469 ethanolic extract Substances 0.000 claims abstract description 3
- 150000001768 cations Chemical class 0.000 claims abstract 2
- 238000000108 ultra-filtration Methods 0.000 claims description 15
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 238000000605 extraction Methods 0.000 claims description 3
- 150000002500 ions Chemical class 0.000 claims description 3
- 238000004042 decolorization Methods 0.000 claims description 2
- 238000005374 membrane filtration Methods 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 125000000020 sulfo group Chemical group O=S(=O)([*])O[H] 0.000 claims description 2
- 238000002425 crystallisation Methods 0.000 abstract description 5
- 230000008025 crystallization Effects 0.000 abstract description 5
- 150000002016 disaccharides Chemical class 0.000 abstract description 4
- 238000001953 recrystallisation Methods 0.000 abstract description 2
- 230000002328 demineralizing effect Effects 0.000 abstract 1
- 239000000284 extract Substances 0.000 abstract 1
- 238000002360 preparation method Methods 0.000 abstract 1
- 238000000926 separation method Methods 0.000 abstract 1
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 10
- 239000000243 solution Substances 0.000 description 10
- 238000001914 filtration Methods 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 239000012065 filter cake Substances 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000000706 filtrate Substances 0.000 description 4
- 235000013305 food Nutrition 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 239000006188 syrup Substances 0.000 description 4
- 235000020357 syrup Nutrition 0.000 description 4
- 239000007864 aqueous solution Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000003544 deproteinization Effects 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- -1 α, α-trehalose disaccharide Chemical class 0.000 description 2
- 241000611223 Selaginella lepidophylla Species 0.000 description 1
- 230000001476 alcoholic effect Effects 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- RQPZNWPYLFFXCP-UHFFFAOYSA-L barium dihydroxide Chemical compound [OH-].[OH-].[Ba+2] RQPZNWPYLFFXCP-UHFFFAOYSA-L 0.000 description 1
- 229910001863 barium hydroxide Inorganic materials 0.000 description 1
- 229940041514 candida albicans extract Drugs 0.000 description 1
- 238000005341 cation exchange Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000002242 deionisation method Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000005445 natural material Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000003828 vacuum filtration Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000012138 yeast extract Substances 0.000 description 1
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 description 1
- 229960001763 zinc sulfate Drugs 0.000 description 1
- 229910000368 zinc sulfate Inorganic materials 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/12—Disaccharides
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- Engineering & Computer Science (AREA)
- Zoology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Microbiology (AREA)
- General Chemical & Material Sciences (AREA)
- Biotechnology (AREA)
- Health & Medical Sciences (AREA)
- Biochemistry (AREA)
- Bioinformatics & Cheminformatics (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Pharmaceuticals Containing Other Organic And Inorganic Compounds (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
Oblasť technikyTechnical field
Vynález sa týka spôsobu izolácie disacharidu α,α-trehalózy (α-D-glukopyranozyl-a-D-glukopyranozidu), ktorý je dôležitou surovinou resp. medziproduktom v potravinárskom priemysle, farmácii a biochémii.The present invention relates to a process for the isolation of α, α-trehalose disaccharide (α-D-glucopyranosyl-α-D-glucopyranoside), which is an important raw material and / or compound. intermediate in the food industry, pharmacy and biochemistry.
Doterajší stav techniky α,α-Trehalóza sa dá získať izoláciou zo širokého radu prírodných látok, najmä z plavúnky schúlivej (Selaginella lepidophylla), pôvodom z juhozápadu USA, teraz pestovanej v krajinách Blízkeho východu. V súčasnej dobe sú najvhodnejším zdrojom tohto disacharidu pekárenské kvasnice, najmä kvôli svojej dostupnosti, nízkej cene a relatívne vysokému obsahu α,α-trehalózy.BACKGROUND OF THE INVENTION α, α-Trehalose can be obtained by isolation from a wide variety of natural substances, particularly Selaginella lepidophylla, native to the southwest of the United States, now grown in the Middle East. At present, the most suitable source of this disaccharide is baker's yeast, mainly because of its availability, low price and relatively high α, α-trehalose content.
Izolácia α,α-trehalózy z pekárenských kvasníc bola prvýkrát opísaná už v roku 1936 (Myrback, K., Ortenblad, B.: Biochem. Z. 288, 329 /1936/) a jej modifikovaná forma (Stewart Z. C., Richtmyer N.K., Hudson C. S.: J. Am. Chem. Soc. 72, 2059 /1950/) je využívaná na prípravu α,α-trehalózy dodnes. Okrem toho JP 04360692 a 05091890 opisujú spôsob izolácie α,α-trehalózy z pekárenských kvasníc extrakciou alkoholom, resp. organickým rozpúšťadlom.The isolation of α, α-trehalose from baker's yeast was first described in 1936 (Myrback, K., Ortenblad, B .: Biochem. Z. 288, 329/1936 /) and its modified form (Stewart ZC, Richtmyer NK, Hudson CS: J. Am Chem Soc., 72, 2059 (1950)) has been used to prepare α, α-trehalose to this day. In addition, JP 04360692 and 05091890 describe a process for the isolation of α, α-trehalose from baker's yeast by alcohol extraction, respectively. an organic solvent.
Podstatnou nevýhodou týchto postupov, ktorá obmedzuje predovšetkým ich priemyselnú aplikáciu, je spôsob uskutočnenia deproteinizácie pridaním vodného roztoku síranu zinočnatého k zahustenému alkoholickému extraktu kvasníc a nasledujúce vyzrážanie síranových aniónov roztokom hydroxidu bárnatého. Tento spôsob deproteinizácie vyvoláva nielen značné nároky na purifikáciu produktu, ktorého požadovaná vysoká čistota je daná farmaceutickými alebo potravinárskymi aplikáciami, ale taktiež veľké množstvo tuhého organického odpadu, ktorého likvidácia vyžaduje značné finančné nároky na investície, energiu a suroviny.A major disadvantage of these processes, which limits their industrial application in particular, is the method of effecting deproteinization by adding an aqueous zinc sulfate solution to the concentrated alcoholic yeast extract and subsequently precipitating the sulfate anions with a barium hydroxide solution. This method of deproteinization not only imposes considerable demands on the purification of a product whose desired high purity is due to pharmaceutical or food applications, but also a large amount of solid organic waste, the disposal of which requires considerable financial demands on investment, energy and raw materials.
Uvedené nevýhody v podstatnej miere odstraňuje spôsob izolácie kryštalickej α,α-trehalózy podľa predloženého vynálezu, kde využitím moderných membránových procesov sa získal postup, ktorý sa vyznačuje vysokou kvalitou produktu, nízkymi investičnými nákladmi, nízkym ekologickým zaťažením, dostupnými surovinami a relatívne vysokým výťažkom.These disadvantages are substantially eliminated by the process of isolating the crystalline α, α-trehalose of the present invention, where the use of modern membrane processes yields a process characterized by high product quality, low investment costs, low environmental burden, available raw materials and relatively high yield.
Podstata vynálezuSUMMARY OF THE INVENTION
Predmetom predloženého vynálezu je spôsob izolácie kryštalickej α,α-trehalózy izoláciou z pekárenských kvasníc, pri ktorom sa pekárenské kvasnice extrahujú etanolom s koncentráciou 70 až 96 % obj., získaný etanolový extrakt sa po odfiltrovaní tuhého podielu vákuovo zahustí na koncentráciu α,α-trehalózy 2 až 30 % hmotn., ktorého podstata spočíva v tom, že potom nasleduje membránový filtračný proces, pozostávajúci z ultrafiltrácie cez ultrafiltračnú membránu s deliacou hranicou molekulových hmotností vyššou ako 500, a získaný číry roztok sa po odfarbení aktívnym uhlím privedie do styku s ionomeničom v H+ cykle, potom v OH' cykle. Získaný demineralizovaný roztok sa vákuovo zahustí na koncentráciu 40 až 85 % hmotn. a po pridaní etanolu v množstve 0,5 až 1,5 : 1,0, vztiahnuté na obsah α,α-trehalózy, sa nechá kryštalizovať pri teplote od -5 °C do +25 °C a vykryštalizovaná α,α-trehalóza sa izoluje alebo prekryštalizuje z etanolu po opätovnej demineralizácii.SUMMARY OF THE INVENTION The present invention relates to a process for the isolation of crystalline α, α-trehalose by isolation from baker's yeast, wherein the baker's yeast is extracted with ethanol at a concentration of 70-96% by volume, the ethanol extract obtained is concentrated by vacuum filtration to α, α-trehalose 2 to 30% by weight, followed by a membrane filtration process consisting of ultrafiltration through an ultrafiltration membrane having a molecular weight cut-off greater than 500, and the clear solution obtained after contacting with the charcoal is decolorized in an activated carbon H + cycle, then in the OH 'cycle. The demineralized solution obtained is concentrated in vacuo to a concentration of 40 to 85% by weight. and after addition of ethanol in an amount of 0.5 to 1.5: 1.0, based on the α, α-trehalose content, it is allowed to crystallize at a temperature of -5 ° C to +25 ° C and the crystallized α, α-trehalose is crystallized. isolated or recrystallized from ethanol after re-demineralization.
Spôsob izolácie podľa vynálezu sa dá uskutočniť tak, že sa pred ultrafiltráciu prípadne predradí mikrofiltrácia cez mikrofiltračnú membránu so stredným priemerom pórov od 0,05 do 5 pm, najlepšie 0,05 až 0,15 pm.The isolation process according to the invention can be carried out by optionally pre-microfiltrating through a microfiltration membrane with an average pore diameter of from 0.05 to 5 µm, preferably 0.05 to 0.15 µm, before ultrafiltration.
Ďalším znakom spôsobu podľa vynálezu je, že sa uskutočňuje kontinuálnou ultrafiltráciou cez ultrafiltračnú membránu s deliacou hranicou molekulových hmotností vyššou ako 500, s pripadne predradenou mikrofiltráciou cez mikrofiltračnú membránu so stredným priemerom pórov od 0,05 do 5 pm, najlepšie 0,05 až 0,15 pm.A further feature of the process according to the invention is that it is carried out by continuous ultrafiltration through an ultrafiltration membrane with a molecular weight cut-off greater than 500, optionally with an upstream microfiltration through a microfiltration membrane with a mean pore diameter of 0.05 to 5 µm, preferably 0.05 to 0. 15 pm.
Pri vykonávaní spôsobu podľa vynálezu sa na extrakciu použije etanol s koncentráciou výhodne 85 až 96 % objemových.In carrying out the process according to the invention, ethanol with a concentration of preferably 85 to 96% by volume is used for the extraction.
Ďalej sa pri vy konávaní spôsobu podľa vynálezu sa s výhodu ako katex používa styréndivinylbenzénový kopolymér so silne kyslými sulfoskupinami a ako anex styréndivinylbenzénový kopolymér s kvartémymi dimetylhydroxyetylamóniovými výmennými skupinami.Furthermore, in carrying out the process according to the invention, it is advantageous to use a styrene-divinylbenzene copolymer with strongly acidic sulfo groups and an anion exchanger of a styrene-divinylbenzene copolymer with quaternary dimethylhydroxyethylammonium exchange groups.
Podľa vynálezu sa dá postupovať tak, že sa pekárenské kvasnice extrahujú v 96 % etanole, denaturovanom izopropanolom, pri normálnej teplote, vyextrahované kvasnice sa odfiltrujú a z filtrátu sa vákuovo oddestiluje etanol. Získaný vodný alebo vodno-alkoholický roztok s koncentráciou α,α-trehalózy 10 až 40 % hmotn. sa podrobí ultrafiltrácii ultrafiltračnou membránou s deliacou hranicou molekulových hmotností vyššou ako 500 alebo je možné vodný roztok po oddestilovaní etanolu najskôr vystaviť mikrofiltrácii mikrofiltračnou membránou so stredným priemerom pórov od 0,05 do 5 pm a potom ultrafiltráciou ultrafiltračnou membránou s deliacou hranicou molekulových hmotností vyššou ako 500. Číry vodný roztok je po odfarbení aktívnym uhlím deionizovaný na stĺpcoch katexu a anexu a zahustený na vákuovej odparke na vodný sirup s koncentráciou 50 až 70 % hmotn. α,α-trehalózy. Z tohto sirupu sa disacharid kryštalizuje po pridaní etanolu v množstve cca 1 : 1, vzhľadom na obsah α,α-trehalózy pri normálnej alebo zníženej teplote. Filtráciou izolovaná kryštalická α,α-trehalóza sa suší pri 40 až 60 °C pri zníženom tlaku. Za predpokladu produkcie kryštalickej α,α-trchalózy s čistotou vyššou ako 99 % hmotn. je nutné vykonať rekryštalizáciu tejto surovej substancie z etanolu po deionizácii obdobným postupom.According to the invention, the yeast is extracted in 96% ethanol, denatured with isopropanol at normal temperature, the extracted yeast is filtered off and ethanol is distilled off in a vacuum. The aqueous or aqueous-alcoholic solution obtained having an α, α-trehalose concentration of 10 to 40% by weight. subjected to ultrafiltration with an ultrafiltration membrane having a molecular weight cut-off greater than 500, or the aqueous solution after distillation of ethanol may first be subjected to microfiltration with a microfiltration membrane with a mean pore diameter of 0.05 to 5 µm and then ultrafiltration with an ultrafiltration membrane with a molecular weight cutoff The clear aqueous solution is deionized on cation exchange and anion exchange columns after decolourisation with activated carbon and concentrated in a vacuum evaporator to an aqueous syrup having a concentration of 50 to 70% by weight. α, α-trehalose. From this syrup, the disaccharide crystallizes when ethanol is added in an amount of about 1: 1, with respect to the α, α-trehalose content at normal or reduced temperature. The crystallized α, α-trehalose is isolated by filtration and dried at 40 to 60 ° C under reduced pressure. Assuming production of crystalline α, α-trchalose with a purity greater than 99% by weight. it is necessary to recrystallize this crude substance from ethanol after deionization in a similar manner.
Spôsobom podľa vynálezu sa pripraví α,α-trehalóza s uspokojivým výťažkom a vysokou kvalitou, čo umožňuje jej ďalšie priame použitie napríklad vo farmácii alebo v potravinárstve. Okrem extrahovaných kvasníc, ktoré sa dajú ďalej zužitkovať, nie sú produkované žiadne významné odpady, čoho výsledkom je podstatne menší ekologický dopad tejto technológie v porovnaní so súčasnými výrobami α,αtrehalózy'. Táto skutočnosť sa taktiež významne pozitívne prejavuje v nižších investičných a prevádzkových nákladoch výroby podľa predloženého vynálezu.The process according to the invention produces α, α-trehalose with a satisfactory yield and high quality, allowing its further direct use, for example, in pharmacy or in the food industry. With the exception of extracted yeast, which can be further utilized, no significant waste is produced, resulting in a considerably less ecological impact of this technology compared to the current production of α 'αtrehalose'. This also has a significant positive effect on the lower investment and operating costs of the production according to the present invention.
Príklady uskutočnenia vynálezuDETAILED DESCRIPTION OF THE INVENTION
Príklad 1Example 1
1000 g pekárenských kvasníc sa za intenzívneho miešania extrahuje pri normálnej teplote 3000 ml 96% etanolu, denaturovaného 6 % izopropanolu, počas 45 minút. Suspenzia sa sfiltruje a filtračný koláč sa premyje 250 ml etanolu. Získaný filtrát sa na vákuovej odparke (20 torr, teplota kúpeľa 60 °C) zahustí na objem 400 ml a vpraví sa do filtračnej komôrky s objemom 450 ml s účinným miešaním filtrovanej kvapaliny a s mikrofiltračnou membránou Synpor® so stredným priemerom pórov 0,12 pm. Nad filtrovanou kvapalinou a membránou je pretlak 0,08 MPa, získaný1000 g of baker's yeast are extracted with vigorous stirring at normal temperature with 3000 ml of 96% ethanol, denatured with 6% isopropanol, for 45 minutes. The suspension is filtered and the filter cake is washed with 250 ml of ethanol. The filtrate was concentrated to 400 ml on a vacuum evaporator (20 torr, bath temperature 60 ° C) and introduced into a 450 ml filter chamber with efficient stirring of the filtered liquid and a Synpor ® microfiltration membrane with a mean pore diameter of 0.12 µm. Above the filtered liquid and the membrane, an overpressure of 0.08 MPa is obtained
SK 278610 B6 pomocou dusíka, privedeného z tlakovej fľaše. Prefiltruje sa 380 ml kvapaliny. Tento filtrát sa podrobí ultrafiltrácii v rovnakej komôrke, ale vybavenej ultrafiltračnou membránou z polysulfónu s deliacou hranicou molekulových hmotností 2000. Nad filtrovanou kvapalinou a membránou je teraz pretlak 0,25 MPa. Získa sa 360 ml filtrátu.With the aid of nitrogen supplied from the cylinder. Filter with 380 ml of liquid. This filtrate is subjected to ultrafiltration in the same chamber, but equipped with a polysulfone ultrafiltration membrane having a molecular weight cutoff of 2000. The pressure of 0.25 MPa is now above the filtered liquid and the membrane. 360 ml of filtrate are obtained.
360 ml číreho vodného roztoku sa odfarbí pridaním 10 g aktívneho uhlia a po jeho odfiltrovaní sa vykoná deionizácia na stĺpci 300 ml Wofatitu KPS v H+ cykle a na stĺpci 215 ml Wofatitu SBK v OH' cykle. Po premytí ionexov 1500 ml vody sa spojené roztoky vákuovo odparia (20 torr) na vodný sirup s koncentráciou α,α-trehalózy 71 % hmotn. Po pridaní 50 ml etanolu prebieha kryštalizácia pri normálnej teplote počas 16 hodín. Vykryštalizovaná α,α-trehalóza sa izoluje filtráciou na frite G-2. Po premytí filtračného koláča 50 ml etanolu a sušení za vákua (50 °C, 15 torr) sa získa 31,5 g kryštalickej α,α-trehalózy s čistotou 97,1 %. Zahustením materských roztokov a kryštalizáciou pri uvedených podmienkach sa získalo ďalších 2,7 g kryštalického produktu.360 ml of a clear aqueous solution is decolorized by addition of 10 g of activated carbon and after filtration it is deionized on a 300 ml column of Wofatit KPS in an H + cycle and on a 215 ml column of Wofatit SBK in an OH 'cycle. After washing the ion exchangers with 1500 ml of water, the combined solutions are vacuum evaporated (20 torr) to an aqueous syrup with a concentration of α, α-trehalose of 71% by weight. After addition of 50 ml of ethanol, crystallization is carried out at normal temperature for 16 hours. Crystallized α, α-trehalose is isolated by filtration on frit G-2. After washing the filter cake with 50 ml of ethanol and drying under vacuum (50 ° C, 15 torr), 31.5 g of crystalline α, α-trehalose with a purity of 97.1% are obtained. Concentration of the mother liquors and crystallization under the above conditions yielded an additional 2.7 g of crystalline product.
Príklad 2Example 2
250 g sušených pekárenských kvasníc sa rozmieša pri laboratórnej teplote s 580 ml demineralizovanej vody na pastu, ktorá sa ďalej extrahuje počas 30 minút 2000 ml 96% etanolu, denaturovaného 7 % izopropanolu. Suspenzia sa sfiltruje a filtračný koláč sa premyje 2150 ml 70% etanolu, denaturovaného izopropanolom. Získaný filtrát sa na vákuovej odparke (20 torr, teplota vodného kúpeľa 60 °C) zahustí na objem 400 ml, vpraví sa do filtračnej komôrky s objemom 450 ml s kontinuálnym tokom filtrovanej kvapaliny nad membránou a s ultrafiltračnou membránou z acetátu celulózy s deliacou hranicou molekulových hmotností 5000. Nad filtrovanou kvapalinou je pretlak 0,2 MPa. Prefiltruje sa 350 ml roztoku, ktorý sa odfarbí pridaním 13 g aktívneho uhlia a po jeho odfiltrovaní sa vykoná deionizácia na stĺpci 280 ml Wofatitu KPS v H+ cykle a pridaním do roztoku 250 ml Wofatitu SBK v OH' cykle (pH deionizovaného roztoku dosiahne hodnoty 4,2). Po odfiltrovaní anexu a premytí obidvoch ionexov 900 ml vody sa spojené roztoky vákuovo odparia (20 torr) na vodný sirup s koncentráciou α,α-trchalózy 79 % hmotn.. Po pridaní 80 ml etanolu prebieha kryštalizácia pri teplote 5 “C počas 12 hodín. Po filtrácii a premytí filtračného koláča 40 ml etanolu sa získa 42,1 g surovej α,α-trehalózy s čistotou 98,2 %, ktorá sa sušila pri laboratórnej teplote. Zahustením materských roztokov a rekryštalizáciou pri uvedených podmienkach sa získali ďalšie 3,2 g produktu.250 g of dried baker's yeast are mixed at room temperature with 580 ml of demineralized water to a paste which is further extracted over 30 minutes with 2000 ml of 96% ethanol denatured with 7% isopropanol. The suspension is filtered and the filter cake is washed with 2150 ml of 70% ethanol, denatured with isopropanol. The filtrate is concentrated to a volume of 400 ml on a vacuum evaporator (20 torr, 60 ° C water bath temperature), introduced into a 450 ml filter chamber with a continuous flow of filtered liquid over the membrane and a molecular weight cut-off ultrafiltration membrane. The pressure over the filtered liquid is 0.2 MPa. Filter 350 ml of the solution, which is decolorized by adding 13 g of activated carbon and de-ionizing on a 280 ml column of Wofatit KPS in an H + cycle and adding 250 ml of Wofatit SBK in an OH 'cycle (pH of the deionized solution reaches 4). , 2). After filtering the anion exchanger and washing both ion exchangers with 900 ml of water, the combined solutions are evaporated in vacuo (20 torr) to an aqueous α, α-trchalose concentration of 79% by weight. After addition of 80 ml of ethanol, crystallization is carried out at 5 ° C for 12 hours. After filtration and washing of the filter cake with 40 ml of ethanol, 42.1 g of crude α, α-trehalose having a purity of 98.2% are obtained, which is dried at room temperature. Concentration of the mother liquors and recrystallization under the above conditions gave an additional 3.2 g of product.
45,3 g kryštalickej surovej α,α-trehalózy sa rozpustilo v 190 ml demineralizovanej vody s teplotou 40 °C a uskutočnila sa deionizácia na stĺpci, obsahujúcom 5 ml Wofatitu KPS v H+ cykle a 10 ml Wofatitu SBK v OH“ cykle. Získaný deionizovaný roztok sa vákuovo odparil (20 torr) na vodný sirup s koncentráciou 68 % (hmotn.) α,α-trchalózy. Po pridaní 40 ml 96% etanolu, denaturovaného 5 % izopropanolu, prebieha kryštalizácia počas 10 hodín pri teplote 5 °C. Vykryštalizovaná α,α-trehalóza sa izoluje filtráciou. Po premytí filtračného koláča 25 ml etanolu a sušení za vákua (50 °C, 15 torr) sa získa 41,4 g α,α-trehalózy s čistotou 99,7 %.45.3 g of crystalline crude α, α-trehalose was dissolved in 190 ml of demineralized water at 40 ° C and deionized on a column containing 5 ml of Wofatit KPS in an H + cycle and 10 ml of Wofatit SBK in an OH-cycle. The deionized solution obtained was evaporated in vacuo (20 torr) to an aqueous syrup having a concentration of 68% (w / w) α, α-trchalose. After addition of 40 ml of 96% ethanol, denatured with 5% isopropanol, crystallization is carried out for 10 hours at 5 ° C. Crystallized α, α-trehalose is isolated by filtration. After washing the filter cake with 25 ml of ethanol and drying under vacuum (50 ° C, 15 torr), 41.4 g of α, α-trehalose with a purity of 99.7% are obtained.
Priemyselná využiteľnosťIndustrial usability
Disacharid α,α-trehalóza, vyrobený spôsobom podľa vynálezu, je dôležitou surovinou alebo medziproduktom vo farmácii, potravinárskom priemysle alebo biochemickom výskume.The disaccharide α, α-trehalose produced by the process of the invention is an important raw material or intermediate in pharmacy, food industry or biochemical research.
Claims (5)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CZ932025A CZ281723B6 (en) | 1993-09-28 | 1993-09-28 | Process of isolating crystalline alpha, alpha-thehalose |
| PCT/CZ1994/000022 WO1995009243A1 (en) | 1993-09-28 | 1994-09-23 | METHOD OF PRODUCING α,α-TREHALOSE |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| SK69795A3 SK69795A3 (en) | 1996-05-08 |
| SK279610B6 true SK279610B6 (en) | 1999-01-11 |
Family
ID=5464225
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| SK697-95A SK279610B6 (en) | 1993-09-28 | 1994-09-23 | Method of crystalline alpha,alpha-trehalose isolation |
Country Status (6)
| Country | Link |
|---|---|
| EP (1) | EP0674717A1 (en) |
| JP (1) | JPH08506248A (en) |
| CA (1) | CA2150256A1 (en) |
| CZ (1) | CZ281723B6 (en) |
| SK (1) | SK279610B6 (en) |
| WO (1) | WO1995009243A1 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1053670C (en) * | 1997-09-18 | 2000-06-21 | 大连理工大学 | Seaweed sugar producing process |
| CN107446007A (en) | 2011-09-21 | 2017-12-08 | 株式会社林原 | Contain α, the preparation method of the powder of alpha trehalose dihydrochloride dihydrate crystal |
| CN102504040A (en) * | 2011-11-16 | 2012-06-20 | 华南理工大学 | Method for extracting trehalose from waste yeast after sterol production |
| EP3744853A1 (en) * | 2019-05-29 | 2020-12-02 | Ohly GmbH | Trehalose-rich yeast hydrolysate |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04360692A (en) * | 1991-06-07 | 1992-12-14 | Kanegafuchi Chem Ind Co Ltd | Production of trehalose |
| JPH0591890A (en) * | 1991-08-27 | 1993-04-16 | Kanji Matsumoto | Production of trehalose |
| JPH05292986A (en) * | 1992-02-21 | 1993-11-09 | Takeda Chem Ind Ltd | Production of trehalose |
| JPH06145186A (en) * | 1992-11-05 | 1994-05-24 | Nippon Shokuhin Kako Co Ltd | Method for producing α, α-trehalose |
| BR9400368A (en) * | 1993-02-02 | 1994-08-23 | Ajinomoto Kk | Process for isolation and purification of trehalose |
-
1993
- 1993-09-28 CZ CZ932025A patent/CZ281723B6/en not_active IP Right Cessation
-
1994
- 1994-09-23 SK SK697-95A patent/SK279610B6/en unknown
- 1994-09-23 CA CA 2150256 patent/CA2150256A1/en not_active Abandoned
- 1994-09-23 WO PCT/CZ1994/000022 patent/WO1995009243A1/en not_active Ceased
- 1994-09-23 EP EP94926769A patent/EP0674717A1/en not_active Withdrawn
- 1994-09-23 JP JP7510039A patent/JPH08506248A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| CZ281723B6 (en) | 1996-12-11 |
| CA2150256A1 (en) | 1995-04-06 |
| CZ202593A3 (en) | 1996-10-16 |
| JPH08506248A (en) | 1996-07-09 |
| WO1995009243A1 (en) | 1995-04-06 |
| EP0674717A1 (en) | 1995-10-04 |
| SK69795A3 (en) | 1996-05-08 |
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