CN102676606A - Process for clarifying and removing impurities from fermentation liquor of xylose mother liquid - Google Patents
Process for clarifying and removing impurities from fermentation liquor of xylose mother liquid Download PDFInfo
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- CN102676606A CN102676606A CN2012101684555A CN201210168455A CN102676606A CN 102676606 A CN102676606 A CN 102676606A CN 2012101684555 A CN2012101684555 A CN 2012101684555A CN 201210168455 A CN201210168455 A CN 201210168455A CN 102676606 A CN102676606 A CN 102676606A
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- ion exchange
- xylose mother
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- 239000007788 liquid Substances 0.000 title claims abstract description 82
- SRBFZHDQGSBBOR-IOVATXLUSA-N D-xylopyranose Chemical compound O[C@@H]1COC(O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-IOVATXLUSA-N 0.000 title claims abstract description 38
- PYMYPHUHKUWMLA-UHFFFAOYSA-N arabinose Natural products OCC(O)C(O)C(O)C=O PYMYPHUHKUWMLA-UHFFFAOYSA-N 0.000 title claims abstract description 23
- SRBFZHDQGSBBOR-UHFFFAOYSA-N beta-D-Pyranose-Lyxose Natural products OC1COC(O)C(O)C1O SRBFZHDQGSBBOR-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000000855 fermentation Methods 0.000 title claims abstract description 17
- 230000004151 fermentation Effects 0.000 title claims abstract description 17
- 239000012535 impurity Substances 0.000 title claims abstract description 9
- 239000012528 membrane Substances 0.000 claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 claims abstract description 17
- 238000005342 ion exchange Methods 0.000 claims abstract description 14
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 14
- 239000013078 crystal Substances 0.000 claims abstract description 11
- 238000013375 chromatographic separation Methods 0.000 claims abstract description 10
- 238000012216 screening Methods 0.000 claims abstract description 9
- 238000000926 separation method Methods 0.000 claims abstract description 5
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Chemical compound OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 claims description 26
- SRBFZHDQGSBBOR-QMKXCQHVSA-N alpha-L-arabinopyranose Chemical compound O[C@H]1CO[C@@H](O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-QMKXCQHVSA-N 0.000 claims description 21
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 14
- 240000004808 Saccharomyces cerevisiae Species 0.000 claims description 9
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 238000005352 clarification Methods 0.000 claims description 8
- 238000009413 insulation Methods 0.000 claims description 8
- 238000012856 packing Methods 0.000 claims description 8
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 6
- 239000012141 concentrate Substances 0.000 claims description 6
- 238000002425 crystallisation Methods 0.000 claims description 6
- 230000008025 crystallization Effects 0.000 claims description 6
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 5
- 239000008103 glucose Substances 0.000 claims description 5
- 239000003456 ion exchange resin Substances 0.000 claims description 5
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 4
- 239000004202 carbamide Substances 0.000 claims description 4
- 238000011033 desalting Methods 0.000 claims description 4
- 239000012452 mother liquor Substances 0.000 claims description 4
- 238000009987 spinning Methods 0.000 claims description 4
- LPQOADBMXVRBNX-UHFFFAOYSA-N ac1ldcw0 Chemical compound Cl.C1CN(C)CCN1C1=C(F)C=C2C(=O)C(C(O)=O)=CN3CCSC1=C32 LPQOADBMXVRBNX-UHFFFAOYSA-N 0.000 claims description 3
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 3
- 239000001913 cellulose Substances 0.000 claims description 2
- 229920002678 cellulose Polymers 0.000 claims description 2
- 238000001914 filtration Methods 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 4
- 238000005374 membrane filtration Methods 0.000 abstract description 4
- 238000001035 drying Methods 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 abstract description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 2
- 150000005846 sugar alcohols Chemical class 0.000 abstract description 2
- PYMYPHUHKUWMLA-WDCZJNDASA-N arabinose Chemical compound OC[C@@H](O)[C@@H](O)[C@H](O)C=O PYMYPHUHKUWMLA-WDCZJNDASA-N 0.000 abstract 4
- 239000000385 dialysis solution Substances 0.000 abstract 1
- 150000002772 monosaccharides Chemical class 0.000 abstract 1
- 238000004806 packaging method and process Methods 0.000 abstract 1
- 102000004169 proteins and genes Human genes 0.000 abstract 1
- 108090000623 proteins and genes Proteins 0.000 abstract 1
- 229920002521 macromolecule Polymers 0.000 description 3
- 238000001514 detection method Methods 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 102000004160 Phosphoric Monoester Hydrolases Human genes 0.000 description 1
- 108090000608 Phosphoric Monoester Hydrolases Proteins 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 150000002016 disaccharides Chemical class 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
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- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention discloses a process for clarifying and removing impurities from a fermentation liquor of a xylose mother liquid, and belongs to the technical field of function sugar-alcohol production. According to the production process, a membrane separation technology is adopted, and the fermentation liquor of the xylose mother liquid in an arabinose production process is processed, wherein a membrane core of a membrane system is an ultrafiltration membrane, and monosaccharide is not intercepted basically. The production process comprises the following steps: (1) fermenting; (2) clarifying and removing proteins from the fermentation liquor; (3) decoloring; (4) performing ion exchange; (5) performing multiple-effect concentration; (6) decoloring; (7) performing chromatographic separation; (8) performing ion exchange; (9) performing vacuum concentration; (10) centrifuging crystals; and (11) drying, screening and packaging crystal arabinose to obtain tabular crystal arabinose. Vacuum drum filtration is changed into membrane filtration in the arabinose production process, the consumption of kieselguhr is reduced, the quality of a dialysis fluid is stable and is influenced by raw materials a little, the efficiency of the subsequent decoloring process is improved and the cost and labor intensity are reduced.
Description
Technical field
The invention belongs to technical field of functional sugar alcohol production, be specifically related to the xylose mother liquid fermentation liquor treatment technology in the pectinose production process.
Background technology
The industrial production of pectinose is raw material with the xylose mother liquid, removes glucose by fermentation, centrifugally removes yeast, rotary drum filtration, activated carbon decolorizing, IX, chromatographic separation, concentrates, Crystallization Procedure makes.Contain a large amount of albumen in the feed liquid of back by fermentation; Eliminating albumen in the present existing pectinose production technique mainly is through carrying out activated carbon decolorizing behind the vacuum drum precoating diatomite filtration again; But because the particle of zeyssatite itself is bigger; The coating that forms can not be held back the albumen in the fermented liquid, and follow-up activated carbon decolorizing difficulty is big and concentrate the reason liquid glucose viscosity increase of back owing to impurity, influences the follow-up crystallization and the quality of product.
Membrane filtration process makes material through behind the film exactly under the higher pressure, the impurity that molecular weight is bigger is realized physical sepn with other small-molecule substances, and the general temperature of membrane filtration process is lower, and is very favourable to the separating substances of some biologically actives.Patent CN1414001 has introduced " enzyme process prepares the regulate and control method of different oligose "; Through selecting the different film mediums and the size of membrane pore size; Oligose to different polymerization degree separates immediately; Ultrafiltrated separates through the nanofiltration device again, removes micromolecular compounds such as SA monose, disaccharides and water, obtains the oligose of different polymerization degree.Contain more albumen and other macromolecular substance in the xylose mother liquid fermented liquid, feed liquid is muddy, and transparence is lower; Macromolecular substance absorption activated carbons such as albumen; Make feed liquid gac viscosity when decolouring increase, sheet frame stops up serious, and difficulty in filtration increases; Long filtration time makes the filtrating color present grey, and ensuing ion exchange resin is polluted.Select suitable aperture ultra-filtration membrane that fermented liquid is handled, could reduce the content of other macromolecular substance such as proteinochrome, improve the efficient of decolouring, reduce the pollution of diatomaceous consumption and feed liquid, reach the purpose that reduces cost resin.
Summary of the invention
In order to overcome the defective of prior art; The present invention provides the impurity removal process of the xylose mother liquid fermented liquid clarification in a kind of pectinose production technique; Filter the drawback that exists to solve the vacuum drum that uses in the xylose mother liquid fermented liquid clarification removal of impurities operation in the prior art, overcome difficult, the problems such as the zeyssatite consumption is big, energy consumption height of unstable, the follow-up decolouring of the feed liquid quality that exists in the technology.
The technical solution adopted for the present invention to solve the technical problems is to adopt membrane separation technique; Through the film system, what the film core of its film system adopted is ultra-filtration membrane with centrifugate, and it is that 100,000 dalton and molecular weight cut-off are 300,000 daltonian two kinds of films that molecular weight cut-off is arranged; Xylose mother liquid fermented liquid in the pectinose production technique is handled; Ultra-filtration membrane according to the invention can be a rolled film, also can be tubular membrane or hollow cellulose film, and ultra-filtration membrane does not exist monose basically to be held back.Its concrete production craft step is following:
(1) fermentation: xylose mother liquid is added water be assigned to Brix value 16%-20%; Add urea and phosphoric acid and regulate pH to 4.6-5.0; Add yeast, keep leavening temperature, whenever measured the fermented liquid glucose content at a distance from two hours at 33-36 ℃; To glucose content reduce to stop below 1% the fermentation, the centrifugal yeast of removing of fermented liquid;
(2) the fermented liquid clarification removes albumen: centrifugate is passed through the film system; What the film core of its film system adopted is ultra-filtration membrane, and the liquid concentrator of film system and the volume flow ratio of dialyzate are 1:12-1:30, pressure 2.7-3.1Mpa before the film; 30 ℃-50 ℃ of feed temperatures; The Brix value of dialyzate and liquid concentrator is consistent basically with stoste, changes lessly, and liquid concentrator can return in the step (1) fermentation once more;
(3) decolouring: the 4-6% that in the dialyzate of step (2) gained, presses amount of dry matter adds powdered active carbon, and 75 ℃-80 ℃ are incubated 25-35 minute, filters and obtains destainer;
(4) IX: the destainer that step (3) obtains carries out desalting treatment through ion exchange resin and obtains ion exchange liquid;
(5) multiple-effect concentrates: ion exchange liquid is concentrated into the liquid glucose of Brix value for 40-48% through multiple-effect evaporator;
(6) decolouring: the liquid glucose that step (5) is obtained gets into 75 ℃-80 ℃ insulations of powdered active carbon 25-35 minute according to the 4-6% of amount of dry matter, filters to obtain two and take off liquid;
(7) chromatographic separation: two of step (6) is taken off liquid separate, collect chromatographic separation liquid through chromatogram;
(8) IX: the pectinose component liquid of collecting in the step (7) is carried out IX;
(9) vacuum concentration: the ion exchange liquid with step (8) obtains, obtain the vacuum concentration liquid glucose that Brix is 80%-86% through vacuum concentration, vacuum tightness is 9.7*10
4Pa;
(10) crystallization is centrifugal: the vacuum concentration liquid glucose that step (9) is obtained goes to crystallizer tank, 70-80 ℃ of insulation 1-1.5 hour, then with the speed decrease temperature crystalline of 1-2 ℃/h, reduces to 38-42 ℃ and carries out spinning, obtains crystal pectinose and mother liquor;
(11) dry, screening and packing: the crystal pectinose is dry, screening, packing back warehouse-in are preserved.
Positively effect of the present invention is: the vacuum drum in the pectinose production technique is filtered change membrane filtration into; Reduced the zeyssatite consumption; It is little and stable that mass of dialysate is influenced by raw material, improved the efficient of follow-up decoloration process, helps reducing production costs and labour intensity.
Specific embodiment
Below in conjunction with specific embodiment the present invention is further specified.
Embodiment 1
(1) fermentation: get 3 tons of xylose mother liquids and add water and be assigned to Brix value 18.5%, add 10 kilograms in urea and phosphoric acid 2L, adjusting pH to 4.8; Add the active dry yeast 120 kg; Keep leavening temperature at 35 ℃, whenever measured the fermented liquid glucose content at a distance from two hours, glucose content reduces to 0.9% after 4 hours; Stop fermentation, the centrifugal yeast of removing of fermented liquid;
(2) the fermented liquid clarification removes albumen: adopt membrane separation technique; Centrifugate through the film system, is handled the xylose mother liquid fermented liquid in the pectinose production technique, centrifugate is passed through the film system; What the film core of its film system adopted is ultra-filtration membrane; The film core is 300,000 daltonian tubular ultra-filtration membranes for seeing through molecular weight, and the liquid concentrator of film system and the volume flow ratio of dialyzate are 1:20, and pressure maintains 3.1Mpa before the film; Feed temperature maintains 30-45 ℃, and the Brix value of dialyzate and liquid concentrator is respectively 17.5% and 19.5%;
(3) decolouring: in the dialyzate of step (2) gained, press 5% of amount of dry matter and add powdered active carbon, 75 ℃ are incubated 30 minutes, filter and obtain destainer;
(4) IX: the destainer that step (3) obtains carries out desalting treatment through ion exchange resin and obtains ion exchange liquid;
(5) multiple-effect concentrates: it is 44% liquid glucose that ion exchange liquid is concentrated into the Brix value through multiple-effect evaporator;
(6) decolouring: the liquid glucose that step (5) is obtained gets into 75 ℃ of insulations of powdered active carbon 30 minutes according to 5% of amount of dry matter, and filtration obtains two and takes off liquid;
(7) chromatographic separation: two of step (6) is taken off liquid separate, collect chromatographic separation liquid through chromatogram;
(8) IX: the pectinose component liquid of collecting in the step (7) is carried out IX;
(9) vacuum concentration: the ion exchange liquid that step (8) is obtained, obtaining Brix through vacuum concentration is 86% vacuum concentration liquid glucose, vacuum tightness is 9.7*10
4Pa;
(10) crystallization is centrifugal: the vacuum concentration liquid glucose that step (9) is obtained goes to crystallizer tank, 70 ℃ of insulations 1 hour, then with the speed decrease temperature crystalline of 1.5 ℃/h, reduces to 40 ℃ and carries out spinning, obtains crystal pectinose and mother liquor;
(11) drying, screening and packing: after crystal pectinose drying, screening, packing, warehouse-in is preserved.
Metal detection and quality inspection result are following:
Embodiment 2
(1) fermentation: get 2.5 tons of xylose mother liquids and add water and be assigned to Brix value 16%, add 8.3 kilograms in urea and phosphatase 11 .7L, adjusting pH to 4.8; Add the active dry yeast 120 kg; Keep leavening temperature at 35 ℃, whenever measured the fermented liquid glucose content at a distance from two hours, glucose content reduces to 0.5% after 4 hours; Stop fermentation, the centrifugal yeast of removing of fermented liquid;
(2) the fermented liquid clarification removes albumen: adopt membrane separation technique; Centrifugate through the film system, is handled the xylose mother liquid fermented liquid in the pectinose production technique, centrifugate is passed through the film system; What the film core of its film system adopted is ultra-filtration membrane; The film core is the rolling ultra-filtration membrane below 100,000 dalton for seeing through molecular weight, and the liquid concentrator of film system and the volume flow ratio of dialyzate are 1:15, pressure 2.8Mpa before the film; Feed temperature maintains 30-45 ℃, and the Brix value of dialyzate and liquid concentrator is respectively 15% and 18%;
(3) decolouring: in the dialyzate of step (2) gained, press 5% of amount of dry matter and add powdered active carbon, 80 ℃ are incubated 30 minutes, filter and obtain destainer;
(4) IX: the destainer that step (3) obtains carries out desalting treatment through ion exchange resin and obtains ion exchange liquid;
(5) multiple-effect concentrates: it is 44% liquid glucose that ion exchange liquid is concentrated into the Brix value through multiple-effect evaporator;
(6) decolouring: the liquid glucose that step (5) is obtained gets into 80 ℃ of insulations of powdered active carbon 30 minutes according to 5% of amount of dry matter, and filtration obtains two and takes off liquid;
(7) chromatographic separation: two of step (6) is taken off liquid separate, collect chromatographic separation liquid through chromatogram;
(8) IX: the pectinose component liquid of collecting in the step (7) is carried out IX;
(9) vacuum concentration: the ion exchange liquid that step (8) is obtained, obtaining Brix through vacuum concentration is 86% vacuum concentration liquid glucose, vacuum tightness is 9.7*10
4Pa;
(10) crystallization is centrifugal: the vacuum concentration liquid glucose that step (9) is obtained goes to crystallizer tank, 80 ℃ of insulations 1 hour, then with the speed decrease temperature crystalline of 1.5 ℃/h, reduces to 40 ℃ and carries out spinning, obtains crystal pectinose and mother liquor;
(11) dry, screening and packing: the crystal pectinose is dry, screening, packing back warehouse-in are preserved.
Metal detection and quality inspection result are following:
Claims (2)
1. an xylose mother liquid fermented liquid is clarified impurity removal process; It is characterized in that adopting membrane separation technique; Through the film system, what the film core of film system adopted is ultra-filtration membrane with centrifugate, and it is that 100,000 dalton and molecular weight cut-off are 300,000 daltonian two kinds of films that molecular weight cut-off is arranged; Xylose mother liquid fermented liquid in the pectinose production technique is handled, and its production craft step is following:
(1) fermentation: xylose mother liquid is added water be assigned to Brix value 16%-20%; Add urea and phosphoric acid and regulate pH to 4.6-5.0; Add yeast, keep leavening temperature, whenever measured the fermented liquid glucose content at a distance from two hours at 33-36 ℃; To glucose content reduce to stop below 1% the fermentation, the centrifugal yeast of removing of fermented liquid;
(2) the fermented liquid clarification removes albumen: centrifugate is passed through the film system; What the film core of its film system adopted is ultra-filtration membrane, and the liquid concentrator of film system and the volume flow ratio of dialyzate are 1:12-1:30, pressure 2.7-3.1Mpa before the film; Feed temperature is between 30 ℃-50 ℃; The Brix value of dialyzate and liquid concentrator is consistent basically with stoste, changes lessly, and liquid concentrator can return in the step (1) fermentation once more;
(3) decolouring: the 4-6% that in the dialyzate of step (2) gained, presses amount of dry matter adds powdered active carbon, and 75 ℃-80 ℃ are incubated about 25-35 minute, filters and obtains destainer;
(4) IX: the destainer that step (3) obtains carries out desalting treatment through ion exchange resin and obtains ion exchange liquid;
(5) multiple-effect concentrates: ion exchange liquid is concentrated into the liquid glucose of Brix value for 40-48% through multiple-effect evaporator;
(6) decolouring: the liquid glucose that step (5) is obtained gets into 75 ℃-80 ℃ insulations of powdered active carbon about 25-35 minute according to the 4-6% of amount of dry matter, filters to obtain two and take off liquid;
(7) chromatographic separation: two of step (6) is taken off liquid separate, collect chromatographic separation liquid through chromatogram;
(8) IX: the pectinose component liquid of collecting in the step (7) is carried out IX;
(9) vacuum concentration: the ion exchange liquid with step (8) obtains, obtain the vacuum concentration liquid glucose that Brix is 80%-86% through vacuum concentration, vacuum tightness is 9.7*10
4Pa;
(10) crystallization is centrifugal: the vacuum concentration liquid glucose that step (9) is obtained goes to crystallizer tank, 70-80 ℃ of insulation 1-1.5 hour, then with the speed decrease temperature crystalline of 1-2 ℃/h, reduces to 38-42 ℃ and carries out spinning, obtains crystal pectinose and mother liquor;
(11) dry, screening and packing: the crystal pectinose is dry, screening, packing back warehouse-in are preserved.
2. xylose mother liquid fermented liquid clarification impurity removal process according to claim 1 is characterized in that ultra-filtration membrane described in the present invention can be a rolled film, also can be tubular membrane or hollow cellulose film, and ultra-filtration membrane does not exist monose basically to be held back.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101684555A CN102676606A (en) | 2012-05-28 | 2012-05-28 | Process for clarifying and removing impurities from fermentation liquor of xylose mother liquid |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101684555A CN102676606A (en) | 2012-05-28 | 2012-05-28 | Process for clarifying and removing impurities from fermentation liquor of xylose mother liquid |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102943131A (en) * | 2012-11-30 | 2013-02-27 | 安徽丰原发酵技术工程研究有限公司 | Xylose preparation method |
| CN103409565A (en) * | 2013-07-26 | 2013-11-27 | 山东福田药业有限公司 | Preparation technology of xylose |
| CN106755613A (en) * | 2016-12-16 | 2017-05-31 | 广州双桥股份有限公司 | A kind of purification process of starch sugar |
| CN107778333A (en) * | 2017-12-08 | 2018-03-09 | 山东福田药业有限公司 | A kind of combination decoloration process of fermentation liquor of xylose mother liquid |
| CN109384819A (en) * | 2018-11-14 | 2019-02-26 | 浙江华康药业股份有限公司 | The minimizing technology of xylose mother liquid impurity |
| CN112029914A (en) * | 2020-09-22 | 2020-12-04 | 焦作市华康糖醇科技有限公司 | Pretreatment method of xylose mother liquor |
| CN112225762A (en) * | 2020-11-09 | 2021-01-15 | 安阳市豫鑫木糖醇科技有限公司 | Process for extracting xylose |
| CN114478191A (en) * | 2021-12-29 | 2022-05-13 | 浙江华康药业股份有限公司 | Refining treatment system and method for xylitol fermentation liquor |
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| WO2002053783A1 (en) * | 2000-12-28 | 2002-07-11 | Danisco Sweeteners Oy | Recovery of xylose |
| CN101372700A (en) * | 2008-07-24 | 2009-02-25 | 上海交通大学 | Method for extracting L-arabinose from xylose mother liquor and biomass acid hydrolyzate |
| CN101643752A (en) * | 2009-06-26 | 2010-02-10 | 安徽丰原发酵技术工程研究有限公司 | Method for producing xylitol and L-arabinose by xylose mother liquor |
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| WO2002053783A1 (en) * | 2000-12-28 | 2002-07-11 | Danisco Sweeteners Oy | Recovery of xylose |
| CN101372700A (en) * | 2008-07-24 | 2009-02-25 | 上海交通大学 | Method for extracting L-arabinose from xylose mother liquor and biomass acid hydrolyzate |
| CN101643752A (en) * | 2009-06-26 | 2010-02-10 | 安徽丰原发酵技术工程研究有限公司 | Method for producing xylitol and L-arabinose by xylose mother liquor |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102943131A (en) * | 2012-11-30 | 2013-02-27 | 安徽丰原发酵技术工程研究有限公司 | Xylose preparation method |
| CN103409565A (en) * | 2013-07-26 | 2013-11-27 | 山东福田药业有限公司 | Preparation technology of xylose |
| CN103409565B (en) * | 2013-07-26 | 2015-04-22 | 山东福田药业有限公司 | Preparation technology of xylose |
| CN106755613A (en) * | 2016-12-16 | 2017-05-31 | 广州双桥股份有限公司 | A kind of purification process of starch sugar |
| CN107778333A (en) * | 2017-12-08 | 2018-03-09 | 山东福田药业有限公司 | A kind of combination decoloration process of fermentation liquor of xylose mother liquid |
| CN109384819A (en) * | 2018-11-14 | 2019-02-26 | 浙江华康药业股份有限公司 | The minimizing technology of xylose mother liquid impurity |
| CN112029914A (en) * | 2020-09-22 | 2020-12-04 | 焦作市华康糖醇科技有限公司 | Pretreatment method of xylose mother liquor |
| CN112225762A (en) * | 2020-11-09 | 2021-01-15 | 安阳市豫鑫木糖醇科技有限公司 | Process for extracting xylose |
| CN114478191A (en) * | 2021-12-29 | 2022-05-13 | 浙江华康药业股份有限公司 | Refining treatment system and method for xylitol fermentation liquor |
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Application publication date: 20120919 |