CN116516078A - System and method for co-producing arabinose and xylo-oligosaccharide by utilizing xylose mother liquor - Google Patents
System and method for co-producing arabinose and xylo-oligosaccharide by utilizing xylose mother liquor Download PDFInfo
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- CN116516078A CN116516078A CN202310709777.4A CN202310709777A CN116516078A CN 116516078 A CN116516078 A CN 116516078A CN 202310709777 A CN202310709777 A CN 202310709777A CN 116516078 A CN116516078 A CN 116516078A
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- Prior art keywords
- storage tank
- pipeline
- arabinose
- communicated
- mother liquor
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- PYMYPHUHKUWMLA-UHFFFAOYSA-N arabinose Natural products OCC(O)C(O)C(O)C=O PYMYPHUHKUWMLA-UHFFFAOYSA-N 0.000 title claims abstract description 215
- SRBFZHDQGSBBOR-UHFFFAOYSA-N beta-D-Pyranose-Lyxose Natural products OC1COC(O)C(O)C1O SRBFZHDQGSBBOR-UHFFFAOYSA-N 0.000 title claims abstract description 215
- 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 186
- PYMYPHUHKUWMLA-WDCZJNDASA-N arabinose Chemical compound OC[C@@H](O)[C@@H](O)[C@H](O)C=O PYMYPHUHKUWMLA-WDCZJNDASA-N 0.000 title claims abstract description 122
- HEBKCHPVOIAQTA-NGQZWQHPSA-N d-xylitol Chemical compound OC[C@H](O)C(O)[C@H](O)CO HEBKCHPVOIAQTA-NGQZWQHPSA-N 0.000 title claims abstract description 119
- 239000012452 mother liquor Substances 0.000 title claims abstract description 103
- 238000000034 method Methods 0.000 title claims abstract description 62
- 238000003860 storage Methods 0.000 claims abstract description 133
- 239000007788 liquid Substances 0.000 claims abstract description 83
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 64
- 239000012528 membrane Substances 0.000 claims abstract description 48
- 238000000926 separation method Methods 0.000 claims abstract description 46
- 238000002156 mixing Methods 0.000 claims abstract description 38
- 238000013375 chromatographic separation Methods 0.000 claims abstract description 31
- 238000002360 preparation method Methods 0.000 claims abstract description 30
- 230000008569 process Effects 0.000 claims abstract description 30
- 238000005342 ion exchange Methods 0.000 claims abstract description 25
- 238000001035 drying Methods 0.000 claims abstract description 19
- 238000002425 crystallisation Methods 0.000 claims abstract description 18
- 230000008025 crystallization Effects 0.000 claims abstract description 18
- 239000002994 raw material Substances 0.000 claims abstract description 18
- 235000000346 sugar Nutrition 0.000 claims description 75
- 238000007599 discharging Methods 0.000 claims description 48
- 238000001728 nano-filtration Methods 0.000 claims description 42
- 238000000108 ultra-filtration Methods 0.000 claims description 29
- 239000000463 material Substances 0.000 claims description 25
- 239000013078 crystal Substances 0.000 claims description 19
- 238000001704 evaporation Methods 0.000 claims description 19
- 229920001542 oligosaccharide Polymers 0.000 claims description 16
- 230000008020 evaporation Effects 0.000 claims description 13
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 238000004042 decolorization Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 239000012530 fluid Substances 0.000 claims description 9
- 238000007670 refining Methods 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 9
- 238000001914 filtration Methods 0.000 claims description 7
- 238000004587 chromatography analysis Methods 0.000 claims description 5
- 238000010790 dilution Methods 0.000 claims description 5
- 239000012895 dilution Substances 0.000 claims description 5
- 238000007865 diluting Methods 0.000 claims description 4
- LGQKSQQRKHFMLI-SJYYZXOBSA-N (2s,3r,4s,5r)-2-[(3r,4r,5r,6r)-4,5,6-trihydroxyoxan-3-yl]oxyoxane-3,4,5-triol Chemical compound O[C@@H]1[C@@H](O)[C@H](O)CO[C@H]1O[C@H]1[C@H](O)[C@@H](O)[C@H](O)OC1 LGQKSQQRKHFMLI-SJYYZXOBSA-N 0.000 claims description 3
- JCSJTDYCNQHPRJ-UHFFFAOYSA-N 20-hydroxyecdysone 2,3-acetonide Natural products OC1C(O)C(O)COC1OC1C(O)C(O)C(OC2C(C(O)C(O)OC2)O)OC1 JCSJTDYCNQHPRJ-UHFFFAOYSA-N 0.000 claims description 3
- LGQKSQQRKHFMLI-UHFFFAOYSA-N 4-O-beta-D-xylopyranosyl-beta-D-xylopyranose Natural products OC1C(O)C(O)COC1OC1C(O)C(O)C(O)OC1 LGQKSQQRKHFMLI-UHFFFAOYSA-N 0.000 claims description 3
- SQNRKWHRVIAKLP-UHFFFAOYSA-N D-xylobiose Natural products O=CC(O)C(O)C(CO)OC1OCC(O)C(O)C1O SQNRKWHRVIAKLP-UHFFFAOYSA-N 0.000 claims description 3
- JVZHSOSUTPAVII-UHFFFAOYSA-N Xylotetraose Natural products OCC(OC1OCC(OC2OCC(OC3OCC(O)C(O)C3O)C(O)C2O)C(O)C1O)C(O)C(O)C=O JVZHSOSUTPAVII-UHFFFAOYSA-N 0.000 claims description 3
- JCSJTDYCNQHPRJ-FDVJSPBESA-N beta-D-Xylp-(1->4)-beta-D-Xylp-(1->4)-D-Xylp Chemical compound O[C@@H]1[C@@H](O)[C@H](O)CO[C@H]1O[C@H]1[C@H](O)[C@@H](O)[C@H](O[C@H]2[C@@H]([C@@H](O)C(O)OC2)O)OC1 JCSJTDYCNQHPRJ-FDVJSPBESA-N 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- KPTPSLHFVHXOBZ-BIKCPUHGSA-N xylotetraose Chemical compound O[C@@H]1[C@@H](O)[C@H](O)CO[C@H]1O[C@H]1[C@H](O)[C@@H](O)[C@H](O[C@H]2[C@@H]([C@@H](O)[C@H](O[C@H]3[C@@H]([C@@H](O)C(O)OC3)O)OC2)O)OC1 KPTPSLHFVHXOBZ-BIKCPUHGSA-N 0.000 claims description 3
- ABKNGTPZXRUSOI-UHFFFAOYSA-N xylotriose Natural products OCC(OC1OCC(OC2OCC(O)C(O)C2O)C(O)C1O)C(O)C(O)C=O ABKNGTPZXRUSOI-UHFFFAOYSA-N 0.000 claims description 3
- 150000002482 oligosaccharides Chemical class 0.000 description 10
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 7
- 238000000855 fermentation Methods 0.000 description 6
- 230000004151 fermentation Effects 0.000 description 6
- 239000008103 glucose Substances 0.000 description 6
- 244000068988 Glycine max Species 0.000 description 4
- 235000010469 Glycine max Nutrition 0.000 description 4
- FTSSQIKWUOOEGC-RULYVFMPSA-N fructooligosaccharide Chemical compound OC[C@H]1O[C@@](CO)(OC[C@@]2(OC[C@@]3(OC[C@@]4(OC[C@@]5(OC[C@@]6(OC[C@@]7(OC[C@@]8(OC[C@@]9(OC[C@@]%10(OC[C@@]%11(O[C@H]%12O[C@H](CO)[C@@H](O)[C@H](O)[C@H]%12O)O[C@H](CO)[C@@H](O)[C@@H]%11O)O[C@H](CO)[C@@H](O)[C@@H]%10O)O[C@H](CO)[C@@H](O)[C@@H]9O)O[C@H](CO)[C@@H](O)[C@@H]8O)O[C@H](CO)[C@@H](O)[C@@H]7O)O[C@H](CO)[C@@H](O)[C@@H]6O)O[C@H](CO)[C@@H](O)[C@@H]5O)O[C@H](CO)[C@@H](O)[C@@H]4O)O[C@H](CO)[C@@H](O)[C@@H]3O)O[C@H](CO)[C@@H](O)[C@@H]2O)[C@@H](O)[C@@H]1O FTSSQIKWUOOEGC-RULYVFMPSA-N 0.000 description 4
- 229940107187 fructooligosaccharide Drugs 0.000 description 4
- 229930182830 galactose Natural products 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- WQZGKKKJIJFFOK-PHYPRBDBSA-N alpha-D-galactose Chemical compound OC[C@H]1O[C@H](O)[C@H](O)[C@@H](O)[C@H]1O WQZGKKKJIJFFOK-PHYPRBDBSA-N 0.000 description 3
- -1 corncob Substances 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 230000000813 microbial effect Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000012465 retentate Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 241000609240 Ambelania acida Species 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- 239000004386 Erythritol Substances 0.000 description 2
- UNXHWFMMPAWVPI-UHFFFAOYSA-N Erythritol Natural products OCC(O)C(O)CO UNXHWFMMPAWVPI-UHFFFAOYSA-N 0.000 description 2
- 229920002488 Hemicellulose Polymers 0.000 description 2
- 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 2
- 229930006000 Sucrose Natural products 0.000 description 2
- 241001052560 Thallis Species 0.000 description 2
- TVXBFESIOXBWNM-UHFFFAOYSA-N Xylitol Natural products OCCC(O)C(O)C(O)CCO TVXBFESIOXBWNM-UHFFFAOYSA-N 0.000 description 2
- 239000010905 bagasse Substances 0.000 description 2
- WQZGKKKJIJFFOK-VFUOTHLCSA-N beta-D-glucose Chemical compound OC[C@H]1O[C@@H](O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-VFUOTHLCSA-N 0.000 description 2
- 150000001720 carbohydrates Chemical class 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 235000019414 erythritol Nutrition 0.000 description 2
- 229940009714 erythritol Drugs 0.000 description 2
- UNXHWFMMPAWVPI-ZXZARUISSA-N erythritol Chemical compound OC[C@H](O)[C@H](O)CO UNXHWFMMPAWVPI-ZXZARUISSA-N 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 230000000968 intestinal effect Effects 0.000 description 2
- HEBKCHPVOIAQTA-UHFFFAOYSA-N meso ribitol Natural products OCC(O)C(O)C(O)CO HEBKCHPVOIAQTA-UHFFFAOYSA-N 0.000 description 2
- 239000010413 mother solution Substances 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000005720 sucrose Substances 0.000 description 2
- 239000000811 xylitol Substances 0.000 description 2
- 235000010447 xylitol Nutrition 0.000 description 2
- HEBKCHPVOIAQTA-SCDXWVJYSA-N xylitol Chemical compound OC[C@H](O)[C@@H](O)[C@H](O)CO HEBKCHPVOIAQTA-SCDXWVJYSA-N 0.000 description 2
- 229960002675 xylitol Drugs 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 1
- 241000186000 Bifidobacterium Species 0.000 description 1
- 241000222178 Candida tropicalis Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 235000005979 Citrus limon Nutrition 0.000 description 1
- 244000131522 Citrus pyriformis Species 0.000 description 1
- WQZGKKKJIJFFOK-QTVWNMPRSA-N D-mannopyranose Chemical compound OC[C@H]1OC(O)[C@@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-QTVWNMPRSA-N 0.000 description 1
- HMFHBZSHGGEWLO-SOOFDHNKSA-N D-ribofuranose Chemical compound OC[C@H]1OC(O)[C@H](O)[C@@H]1O HMFHBZSHGGEWLO-SOOFDHNKSA-N 0.000 description 1
- 101710121765 Endo-1,4-beta-xylanase Proteins 0.000 description 1
- 244000166124 Eucalyptus globulus Species 0.000 description 1
- 229920002527 Glycogen Polymers 0.000 description 1
- 102000004157 Hydrolases Human genes 0.000 description 1
- 108090000604 Hydrolases Proteins 0.000 description 1
- 101710184309 Probable sucrose-6-phosphate hydrolase Proteins 0.000 description 1
- 108010009736 Protein Hydrolysates Proteins 0.000 description 1
- PYMYPHUHKUWMLA-LMVFSUKVSA-N Ribose Natural products OC[C@@H](O)[C@@H](O)[C@@H](O)C=O PYMYPHUHKUWMLA-LMVFSUKVSA-N 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 102400000472 Sucrase Human genes 0.000 description 1
- 101710112652 Sucrose-6-phosphate hydrolase Proteins 0.000 description 1
- 102100033019 Tyrosine-protein phosphatase non-receptor type 11 Human genes 0.000 description 1
- 101710116241 Tyrosine-protein phosphatase non-receptor type 11 Proteins 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000005903 acid hydrolysis reaction Methods 0.000 description 1
- HMFHBZSHGGEWLO-UHFFFAOYSA-N alpha-D-Furanose-Ribose Natural products OCC1OC(O)C(O)C1O HMFHBZSHGGEWLO-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 235000013736 caramel Nutrition 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 150000004676 glycans Chemical class 0.000 description 1
- 229940096919 glycogen Drugs 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 235000013402 health food Nutrition 0.000 description 1
- 125000005842 heteroatom Chemical group 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 230000003834 intracellular effect Effects 0.000 description 1
- 235000011073 invertase Nutrition 0.000 description 1
- 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 1
- 210000004185 liver Anatomy 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229940057059 monascus purpureus Drugs 0.000 description 1
- 150000002772 monosaccharides Chemical class 0.000 description 1
- 235000013615 non-nutritive sweetener Nutrition 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 230000035764 nutrition Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000001766 physiological effect Effects 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 239000005017 polysaccharide Substances 0.000 description 1
- 230000035755 proliferation Effects 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 150000005846 sugar alcohols Chemical class 0.000 description 1
- 150000008163 sugars Chemical class 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 235000015099 wheat brans Nutrition 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K13/00—Sugars not otherwise provided for in this class
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
- B01D15/12—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to the preparation of the feed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
- B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
- B01D15/1814—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns recycling of the fraction to be distributed
- B01D15/1821—Simulated moving beds
- B01D15/185—Simulated moving beds characterized by the components to be separated
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
- B01D15/08—Selective adsorption, e.g. chromatography
- B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
- B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
- B01D15/1864—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns using two or more columns
- B01D15/1871—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns using two or more columns placed in series
- B01D15/1878—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns using two or more columns placed in series for multi-dimensional chromatography
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K13/00—Sugars not otherwise provided for in this class
- C13K13/002—Xylose
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K13/00—Sugars not otherwise provided for in this class
- C13K13/007—Separation of sugars provided for in subclass C13K
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Sustainable Development (AREA)
- Saccharide Compounds (AREA)
Abstract
The invention relates to a system and a method for co-producing arabinose and xylo-oligosaccharide by utilizing xylose mother liquor, wherein the system comprises a raw material storage tank, a process water storage tank, a blending tank, a simulated moving bed chromatographic separation system, an arabinose preparation path and a xylo-oligosaccharide preparation path, wherein the simulated moving bed chromatographic separation system is respectively provided with a moving bed liquid inlet, a moving bed water inlet, an arabinose component discharge port and a xylo-oligosaccharide component discharge port, the arabinose preparation path comprises an EX storage tank, a first decolorizing tank, a first filter, a first ion exchange system, a first evaporator, a crystallization device, a centrifugal separation system, a drying device and an arabinose storage tank which are sequentially communicated, and the xylo-oligosaccharide preparation path comprises a DX storage tank, a second decolorizing tank, a second filter, a second ion exchange system, a membrane separation system, a second evaporator and a xylo-oligosaccharide storage tank which are sequentially communicated. The invention takes xylose mother liquor as raw material, simultaneously prepares arabinose and xylo-oligosaccharide, and improves the added value of the xylose mother liquor.
Description
Technical Field
The invention belongs to the technical field of xylose mother liquor recycling, and particularly relates to a system and a method for co-producing arabinose and xylo-oligosaccharide by utilizing xylose mother liquor.
Background
Arabinose is a five-carbon sugar, also called arabinose, which is mainly present in the form of heteropolysaccharide in plant pulp, hemicellulose, etc. Arabinose is a novel low calorie sweetener which has been approved by the united states, japan, etc. for inclusion in health food additives, and its representative physiological effect is sucrase which selectively affects the digestion of sucrose in intestinal disaccharide hydrolase, restricting the conversion of sucrose and glucose into glycogen for absorption by the liver.
The xylooligosaccharide is also called xylooligosaccharide, is a functional polymeric sugar formed by combining 2-9 xylose molecules through beta-1, 4 glycosidic bonds, has a relative molecular weight of 300-2000 Da, and is mainly prepared from plant raw materials such as corncob, bagasse, wheat bran and the like in nature through hydrolytic separation and refining of xylanase. Compared with soybean oligosaccharide, fructo-oligosaccharide, isomaltooligosaccharide and the like which are commonly used by people, the soybean oligosaccharide and the fructooligosaccharide have the unique advantages that the soybean oligosaccharide and the fructooligosaccharide can selectively promote the proliferation activity of intestinal bifidobacteria, and the bifidus factor function of the soybean oligosaccharide and the fructooligosaccharide is 10-20 times that of other polysaccharides.
As saccharides with special effects, the saccharides are initially used in the nutrition and health care and food industries, and are gradually developed into non-food fields such as chemical industry, pharmacy, cosmetics, biorefinery, petroleum and the like.
In industry, agricultural and forestry wastes such as corncobs, straws, bagasse and eucalyptus are subjected to dilute acid hydrolysis or enzymolysis to obtain primary sugar solution, and xylose (or xylitol is prepared by hydrogenation) is prepared by refining, concentrating and crystallizing, so that a large amount of xylose mother liquor is generated in the process, and the xylose mother liquor has relatively complex components and contains about 25-35% of glucose, 15-25% of xylose, 25-30% of arabinose, 5-10% of oligosaccharide, 5-15% of galactose and 0-10% of mannose according to mass fraction. However, the conventional separation and purification process is difficult to achieve effective purification and application, so that the process is often sold as a byproduct for preparing caramel pigment and the like, and the added value is low. In the existing production, each substance can show technical or commercial value only after reaching higher purity, so that separation and purification are very important links in the production and manufacturing process.
Methods for treating and utilizing xylose mother liquor are common, and mainly xylose and arabinose are extracted from xylose mother liquor. In order to reduce the difficulty of extraction and separation, fermentation by bacteria or yeast is a common choice, and glucose or galactose is consumed as a carbon source for the growth of thalli, so that the extraction efficiency of xylose and arabinose is improved.
For example, the patent with publication number CN114181268A discloses a method for co-producing erythritol and arabinose from xylose mother liquor, which comprises mixing xylose mother liquor chromatographic raffinate with crystal or liquid glucose, removing and converting glucose by fermentation, and further performing a series of separation, purification and crystallization processes to realize co-production of erythritol and arabinose. Chinese patent publication No. CN111747997a discloses a method for simultaneously preparing xylose, arabinose and galactose by using batch simulated moving bed chromatography, and also adopts a microbial fermentation means to remove partial miscellaneous sugars such as glucose in the pretreatment stage of raw materials. Chinese patent (publication No. CN101555503 a) metabolizes monosaccharides other than arabinose in xylose mother liquor with specific microorganism red yeast to purify xylose mother liquor and separate arabinose. Chinese patent (publication No. CN 101497904A) inoculates specific candida tropicalis into detoxified hemicellulose hydrolysate, and converts xylose into xylitol, thereby improving the chromatographic separation efficiency and the purity of the obtained components. The Chinese patent (publication No. CN 101665523A) uses the cooperation of various specific bacteria to convert xylose hydrolysis or sugar components except xylose and arabinose in xylose mother liquor into ethanol, ribose or lemon, and extracts xylose and arabinose by chromatographic separation. However, specific microbial or fungus-transformed sugar components are present: 1) Glucose is additionally added to meet the propagation and metabolism requirements of the fermentation strain; 2) The implementation conditions are strict and the period is long; 3) Non-target sugar component resources cannot be recovered, and the self-value of the non-target sugar component resources cannot be realized; 4) Microbial intervention transformation can introduce thalli and intracellular and extracellular metabolic substances to influence the separation and extraction of high-value components.
In summary, at present, xylose mother liquor is pretreated by a fermentation method, and is refined, concentrated and crystallized to prepare crystalline xylose, crystalline arabinose or galactose, and separation of xylooligosaccharide components is not involved. The fermentation method needs specific strains and strict conditions to remove the impurity sugar, so that the operation cost of the subsequent treatment process is increased, the product yield in the subsequent crystallization process of the target product is reduced, and the resource utilization rate is reduced.
Meanwhile, the oligosaccharide component contained in the xylose mother liquor is mainly xylose polymer, and can be applied to the preparation of xylo-oligosaccharide, and a method and a process for preparing a xylo-oligosaccharide product by utilizing the xylose mother liquor are not reported in the prior literature.
Therefore, in order to further improve the utilization value of the xylose mother liquor, the invention provides a system and a method for co-producing arabinose and xylo-oligosaccharide by utilizing the xylose mother liquor, which separate and purify high-value components in the xylose mother liquor, improve the added value of the xylose mother liquor and realize comprehensive utilization of resources.
Disclosure of Invention
The invention aims to solve the technical problem of providing a system and a method for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor, which take the xylose mother liquor as a raw material and simultaneously prepare the arabinose and the xylo-oligosaccharide, so that the xylose mother liquor with complex components is utilized to the greatest extent, the added value of the xylose mother liquor is improved, and the comprehensive utilization of resources is realized.
The invention is realized by the way, the system for co-producing the arabinose and the xylo-oligosaccharide by utilizing the xylose mother liquor is provided, and comprises a raw material storage tank, a process water storage tank, a blending tank, a simulated moving bed chromatographic separation system, an arabinose preparation path and a xylo-oligosaccharide preparation path, wherein the xylose mother liquor to be treated is stored in the raw material storage tank, process water for dilution and cleaning is stored in the process water storage tank, a discharge port of the raw material storage tank is communicated with one feed port of the blending tank through a pipeline, one water outlet of the process water storage tank is communicated with the other feed port of the blending tank through a pipeline, the simulated moving bed chromatographic separation system is respectively provided with a moving bed liquid inlet, a moving bed water inlet, an arabinose component discharge port and a xylo-oligosaccharide component discharge port, the moving bed liquid inlet is communicated with the discharge port of the blending tank through a pipeline, and the moving bed water inlet is communicated with the other water outlet of the process water storage tank through a pipeline; the arabinose preparation path comprises an EX storage tank, a first decolorizing tank, a first filter, a first ion exchange system, a first evaporator, a crystallization device, a centrifugal separation system, a drying device and an arabinose storage tank which are sequentially communicated through pipelines, wherein a feed inlet of the EX storage tank is communicated with an arabinose component discharge port through a pipeline, a moisture sugar discharge end is arranged on the centrifugal separation system and is communicated with a feed end of the drying device through a pipeline, materials output from the discharge end of the drying device are prepared arabinose crystals, and the prepared arabinose storage crystals are stored in the arabinose storage tank; the xylooligosaccharide preparation path comprises a DX storage tank, a second decolorizing tank, a second filter, a second ion exchange system, a membrane separation system, a second evaporator and a xylooligosaccharide storage tank which are sequentially communicated through pipelines, wherein a feed inlet of the DX storage tank is communicated with a xylooligosaccharide component discharge port through a pipeline, the membrane separation system is provided with a xylooligosaccharide discharge end, the xylooligosaccharide discharge end is communicated with a feed end of the second evaporator through a pipeline, a material output from the discharge end of the second evaporator is prepared concentrated xylooligosaccharide liquid, and the prepared xylooligosaccharide liquid is stored in the xylooligosaccharide storage tank.
Further, the system for co-producing arabinose and xylooligosaccharide by utilizing xylose mother liquor further comprises a mixed sugar preparation path, the simulated moving bed chromatographic separation system is further provided with a mixed sugar component discharge port, the mixed sugar preparation path comprises a CX storage tank, a third evaporator and a mixed sugar storage tank which are mutually communicated through pipelines, a feed inlet of the CX storage tank is communicated with the mixed sugar component discharge port through a pipeline, a material output from a discharge end of the third evaporator is prepared concentrated mixed sugar, and the prepared mixed sugar concentrated solution is stored in the mixed sugar storage tank.
Further, the simulated moving bed chromatographic separation system comprises six chromatographic columns which are connected in series, wherein each chromatographic column is provided with a feed inlet positioned at the upper part and a discharge outlet positioned at the lower part respectively, the discharge outlet of each chromatographic column is communicated with the feed inlet of the next chromatographic column through a serial pipeline, the feed inlet of each chromatographic column is communicated with the discharge outlet of the previous chromatographic column through a serial pipeline, and a circulating pump and a serial valve are respectively arranged on each serial pipeline; each feed inlet is also respectively communicated with a liquid inlet pipeline and a water inlet pipeline, a liquid inlet valve is arranged on each liquid inlet pipeline, a water inlet valve is arranged on each water inlet pipeline, each liquid inlet pipeline is respectively communicated with a discharge port of the blending tank, and each water inlet pipeline is respectively communicated with one water outlet of the process water storage tank; each discharging port is further communicated with an arabinose component discharging pipeline, an xylooligosaccharide component discharging pipeline and a mixed sugar component discharging pipeline respectively, an arabinose discharging valve is arranged on each arabinose component discharging pipeline, an xylooligosaccharide discharging valve is arranged on each xylooligosaccharide component discharging pipeline, a mixed sugar discharging valve is arranged on each mixed sugar component discharging pipeline, each arabinose component discharging pipeline is communicated with a feeding port of an EX storage tank respectively, each xylooligosaccharide component discharging pipeline is communicated with a feeding port of the DX storage tank respectively, and each mixed sugar component discharging pipeline is communicated with a feeding port of the CX storage tank respectively.
Further, the centrifugal separation system is further provided with a liquid discharge end, the liquid discharge end is communicated with the feed end of the first mother liquor storage tank through a pipeline, and the discharge end of the first mother liquor storage tank is communicated with the other feed inlet of the blending tank through a pipeline.
Further, the membrane separation system is further provided with a mother liquor discharge end, the mother liquor discharge end is communicated with the feed end of the second mother liquor storage tank through a pipeline, and the discharge end of the second mother liquor storage tank is communicated with the other feed inlet of the blending tank through a pipeline.
Further, the membrane separation system comprises a temporary storage tank, an ultrafiltration membrane component, a nanofiltration membrane component and a trapped fluid storage tank which are sequentially communicated through pipelines, wherein a feed inlet of the temporary storage tank is communicated with a discharge outlet of the second ion exchange system through a pipeline, a discharge outlet of the trapped fluid storage tank is communicated with a feed inlet of the second evaporator through a pipeline, a first valve and a first material conveying pump are sequentially arranged on the pipeline communicated with the temporary storage tank and the ultrafiltration membrane component, and a second material conveying pump is arranged on the pipeline communicated with the ultrafiltration membrane component and the nanofiltration membrane component; an ultrafiltration passing end and an ultrafiltration interception end are respectively arranged on the ultrafiltration membrane component, the ultrafiltration interception end is communicated with a feed inlet of the temporary storage tank through a first backflow pipeline, a second valve is arranged on the first backflow pipeline, and the ultrafiltration passing end is communicated with a second feed pump through a pipeline; the nanofiltration membrane component is provided with a nanofiltration passing end and a nanofiltration intercepting end, the nanofiltration intercepting end is communicated with a feed inlet of a interception liquid storage tank through a pipeline, a third valve is arranged on the pipeline, which is communicated with the interception liquid storage tank, of the nanofiltration intercepting end, the nanofiltration intercepting end outputs materials which are nanofiltration intercepting liquid rich in xylooligosaccharide components, the nanofiltration intercepting liquid rich in xylooligosaccharide components is stored in the interception liquid storage tank, the nanofiltration intercepting end is also communicated with the ultrafiltration membrane component and a connecting pipeline between a second material conveying pump through a second backflow pipeline, a fourth valve is arranged on the second backflow pipeline, and the nanofiltration passing end is communicated with the feed inlet of a second mother liquid storage tank through a pipeline.
The invention is realized in this way, and provides a method for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor, wherein the method adopts a system for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor, and the method comprises the following steps:
step one, blending and diluting xylose mother liquor: inputting xylose mother liquor stored in a raw material storage tank into a blending tank, introducing production water stored in a process water storage tank to carry out xylose mother liquor blending dilution, ensuring the stability of blended materials, wherein the refraction of blended xylose mother liquor is 50-55%, the arabinose content is 25-28%, and the temperature of the blended xylose mother liquor is 60-65 ℃;
step two, xylose mother liquor is separated by simulated moving bed chromatography: carrying out chromatographic separation on the diluted xylose mother liquor by using a simulated moving bed chromatographic separation system to respectively obtain EX liquor rich in arabinose components (namely EX components) and DX liquor rich in xylooligosaccharide components (namely DX components), wherein the EX liquor is stored in an EX storage tank, and the DX liquor is stored in a DX storage tank;
step three, refining arabinose: inputting the EX feed liquid obtained in the step two into an arabinose preparation path, and obtaining arabinose crystals after the EX feed liquid sequentially passes through a first decolorization treatment of a first decolorization tank, a first filtration treatment of a first filter, a first ion exchange treatment of a first ion exchange system, a first evaporation treatment of a first evaporator, a cooling crystallization treatment of a crystallization device, a centrifugal separation treatment of a centrifugal separation system and a drying treatment of a drying device, wherein the arabinose crystals are stored in an arabinose storage tank;
and step four, refining xylo-oligosaccharide: inputting the DX feed liquid obtained in the step two into an xylooligosaccharide preparation path, and obtaining concentrated xylooligosaccharide liquid after the DX feed liquid sequentially passes through the second decolorization treatment of a second decolorization tank, the second filtration treatment of a second filter, the second ion exchange treatment of a second ion exchange system, the membrane separation treatment of a membrane separation system and the second evaporation treatment of a second evaporator, wherein the xylooligosaccharide liquid is stored in an xylooligosaccharide storage tank.
Further, in the second step, after the diluted xylose mother liquor is subjected to simulated moving bed chromatographic separation, CX liquor rich in a mixed sugar component (namely CX component) is also obtained, and the method further comprises the step five:
step five, concentrating the mixed sugar: and (3) inputting CX feed liquid into a mixed sugar preparation path, carrying out third evaporation concentration treatment on the CX feed liquid by a third evaporator until the refraction is 65-70%, and obtaining mixed sugar concentrated solution which is stored in a mixed sugar storage tank.
Further, in the third step, the first decoloring temperature is 60-65 ℃, the first evaporating temperature is 70-75 ℃, the first evaporating discharge density is controlled to 1288-1292 g/m, the cooling crystallization feeding temperature is 60-65 ℃, the cooling gradient is 0.5 ℃/min, the crystallization discharge temperature is 25-28 ℃, the washing time of the arabinose crystals after centrifugal separation is 30S, and the content of the arabinose crystals after drying is more than or equal to 99.8%.
Further, in the fourth step, the second decoloring temperature is 60-65 ℃, the concentration temperature of the second evaporator is 90-95 ℃, the refractive index of the second evaporation discharge is controlled to be more than 70%, and the content of xylooligosaccharide in the concentrated xylooligosaccharide solution is 70-75%, wherein the sum (XOS) of xylobiose, xylotriose and xylotetraose 2-4 ) The content is more than or equal to 50 percent, and meets the 70-type xylo-oligosaccharide standard specified by national standards.
Compared with the prior art, the system and the method for co-producing the arabinose and the xylo-oligosaccharide by utilizing the xylose mother liquor have the following characteristics:
1. and a blending tank is additionally arranged to stabilize the feeding stability of the simulated moving bed chromatographic separation system.
2. And a simulated moving bed chromatographic separation system with six columns connected in series is adopted to separate and enrich raw materials into three components of hetero sugar, xylooligosaccharide and arabinose, so that the separation efficiency and the yield of each component are improved, and the burden of a subsequent refining working section is reduced.
3. The xylose mother liquor is utilized to separate and prepare the arabinose and the xylo-oligosaccharide, and the impurity sugar component is enriched for convenient subsequent utilization.
4. Creatively extracts the xylooligosaccharide component from the xylose mother liquor, and improves the added value of the xylose mother liquor.
Drawings
FIG. 1 is a schematic diagram of the principle of a preferred embodiment of the system for co-producing arabinose and xylo-oligosaccharides using xylose mother liquor according to the present invention;
FIG. 2 is a schematic diagram of the structural principle of the simulated moving bed chromatographic separation system of FIG. 1;
FIG. 3 is an enlarged schematic view of a portion A of the membrane separation system of FIG. 1;
FIG. 4 is a schematic flow chart of steps of the method for co-producing arabinose and xylo-oligosaccharides by using xylose mother liquor of the invention;
FIG. 5 is a mirror image of arabinose prepared using the xylose mother liquor co-production system of arabinose and xylo-oligosaccharides of the present invention.
Detailed Description
In order to make the technical problems, technical schemes and beneficial effects to be solved more clear, the invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
Referring to fig. 1, a preferred embodiment of a system for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor according to the present invention comprises a raw material storage tank 1, a process water storage tank 2, a blending tank 3, a simulated moving bed chromatographic separation system 4, an arabinose preparation path 5, a xylo-oligosaccharide preparation path 6 and a miscellaneous sugar preparation path 7.
The xylose mother liquor to be treated is stored in a raw material storage tank 1, the process water for dilution and cleaning is stored in a process water storage tank 2, the discharge port of the raw material storage tank 1 is communicated with one feed inlet of a blending tank 3 through a pipeline, and one water outlet of the process water storage tank 2 is communicated with the other feed inlet of the blending tank 3 through a pipeline. The simulated moving bed chromatographic separation system 4 is respectively provided with a moving bed liquid inlet, a moving bed water inlet, an arabinose component discharge port, an xylooligosaccharide component discharge port and a mixed sugar component discharge port. The liquid inlet of the moving bed is communicated with the discharge port of the blending tank 3 through a pipeline, and the water inlet of the moving bed is communicated with the other water outlet of the process water storage tank 2 through a pipeline.
The arabinose production path 5 includes an EX tank 51, a first decolorizing tank 52, a first filter 53, a first ion exchange system 54, a first evaporator 55, a crystallization device 56, a centrifugal separation system 57, a drying device 58, and an arabinose tank 59, which are sequentially communicated through pipes. The feed inlet of the EX tank 51 is communicated with the arabinose component discharge port through a pipe. The centrifugal separation system 57 is provided with a wet sugar discharge end which communicates with the feed end of the drying device 58 through a pipe, and a liquid discharge end which communicates with the feed end of the first mother liquor tank 510 through a pipe. The material output from the feed end of the drying device 58 is prepared arabinose crystals, which are stored in an arabinose storage tank 59. The discharge end of the first mother liquor storage tank 510 is communicated with the other feed inlet of the blending tank 3 through a pipeline.
Specifically, the xylo-oligosaccharide preparation path 6 includes a DX tank 61, a second decolorizing tank 62, a second filter 63, a second ion exchange system 64, a membrane separation system 65, a second evaporator 66, and a xylo-oligosaccharide tank 67, which are sequentially connected by pipes. The feed inlet of DX reservoir 61 is in communication with the xylo-oligosaccharide component discharge outlet via a conduit. The membrane separation system 65 is provided with an xylo-oligosaccharide discharge end and a mother liquor discharge end, the xylo-oligosaccharide discharge end is communicated with the feed end of the second evaporator 66 through a pipeline, and the mother liquor discharge end is communicated with the feed end of the second mother liquor storage tank 68 through a pipeline. The material output from the discharge end of the second evaporator 66 is the prepared concentrated xylo-oligosaccharide liquid, and the prepared xylo-oligosaccharide liquid is stored in the xylo-oligosaccharide storage tank 67. The discharge end of the second mother liquor storage tank 68 is communicated with the other feed inlet of the blending tank 3 through a pipeline.
Specifically, the miscellaneous sugar preparation path 7 includes a CX tank 71, a third evaporator 72, and a miscellaneous sugar tank 73, which are communicated with each other through pipes. The feed inlet of the CX storage tank 71 is connected to the mixed sugar component discharge port via a pipe, the material output from the discharge end of the third evaporator 72 is the prepared concentrated mixed sugar, and the prepared mixed sugar concentrate is stored in the mixed sugar storage tank 73.
Specifically, valves are respectively arranged on the pipelines and the pipelines.
Referring to fig. 2, the simulated moving bed chromatographic separation system 4 includes six chromatographic columns 41-46 connected in series, each of which is provided with a feed inlet at the upper part and a discharge outlet at the lower part. The discharge port of each chromatographic column is communicated with the feed port of the next chromatographic column through a serial pipeline, and the feed port of each chromatographic column is communicated with the discharge port of the previous chromatographic column through a serial pipeline. And each serial pipeline is respectively provided with a circulating pump, namely circulating pumps SHP 1-SHP 6 and serial valves F1-F6. Each feed inlet is also respectively communicated with a liquid inlet pipeline and a water inlet pipeline, and each liquid inlet pipeline is provided with a liquid inlet valve, namely liquid inlet valves A1-A6. Each water inlet pipeline is provided with a water inlet valve, namely water inlet valves B1-B6. Each liquid inlet pipeline is a moving bed liquid inlet respectively and is communicated with a discharge port of the blending tank 3 respectively. Each water inlet pipeline is a water inlet of the moving bed, and is communicated with one water outlet of the process water storage tank 2. Each discharge port is also respectively communicated with an arabinose component discharge pipeline, an xylooligosaccharide component discharge pipeline and a mixed sugar component discharge pipeline, and an arabinose discharge valve, namely, arabinose discharge valves EX 1-EX 6, are arranged on each arabinose component discharge pipeline. And an xylo-oligosaccharide discharging valve, namely xylo-oligosaccharide discharging valves DX 1-DX 6, is arranged on the xylo-oligosaccharide component discharging pipeline. And a mixed sugar discharging valve, namely mixed sugar discharging valves CX 1-CX 6, is arranged on the mixed sugar component discharging pipeline. Each arabinose component discharging pipeline is respectively an arabinose component discharging port, and each arabinose component discharging pipeline is respectively communicated with a feeding port of the EX storage tank 51. Each xylo-oligosaccharide component discharging pipeline is respectively an xylo-oligosaccharide component discharging port, and each xylo-oligosaccharide component discharging pipeline is respectively communicated with the feeding port of the DX storage tank 61. Each of the mixed sugar component discharging pipelines is a mixed sugar component discharging port, and each of the mixed sugar component discharging pipelines is communicated with the feeding port of the CX 71. Pressure gauges, namely pressure gauges PT 1-PT 6, are also arranged on each chromatographic column respectively.
Referring to fig. 3, the membrane separation system 65 includes a temporary storage tank 651, an ultrafiltration membrane module 652, a nanofiltration membrane module 653, and a retentate storage tank 654, which are sequentially connected by pipes. The feed inlet of the temporary storage tank 651 is communicated with the discharge outlet of the second ion exchange system 64 through a pipeline. The discharge port of the retentate storage tank 654 is an xylo-oligosaccharide discharge end, and the discharge port of the retentate storage tank 654 is communicated with the feed inlet of the second evaporator 66 through a pipeline. A first valve 655 and a first material conveying pump 656 are sequentially arranged on a pipeline communicated with the temporary storage tank 651 and the ultrafiltration membrane component 652, and a second material conveying pump 657 is arranged on a pipeline communicated with the ultrafiltration membrane component 652 and the nanofiltration membrane component 653. An ultrafiltration passing end and an ultrafiltration interception end are respectively arranged on the ultrafiltration membrane component 652, the ultrafiltration interception end is communicated with a feed inlet of the temporary storage tank 651 through a first backflow pipeline, and a second valve 658 is arranged on the first backflow pipeline; the ultrafiltration permeate end is in communication with a second feed pump 657 via a conduit. The nanofiltration membrane component 653 is provided with a nanofiltration passing end and a nanofiltration interception end, the nanofiltration interception end is communicated with a feed inlet of the interception liquid storage tank 654 through a pipeline, and the nanofiltration membrane interception end is communicated with the interception liquid storage tank 654 through a pipeline, and a third valve 659 is arranged on the pipeline. The material output from the nanofiltration interception end is nanofiltration interception liquid rich in the xylo-oligosaccharide component, and the nanofiltration interception liquid rich in the xylo-oligosaccharide component is stored in an interception liquid storage tank 654. The nanofiltration interception end is also communicated with the ultrafiltration membrane component 652 and a connecting pipeline between the second material conveying pump 657 through a second backflow pipeline, a fourth valve 6510 is arranged on the second backflow pipeline, the nanofiltration permeation end is communicated with the feeding end of the second mother liquor storage tank 68 through a pipeline, and the nanofiltration permeation end is a mother liquor discharge end.
Referring to fig. 1 and fig. 4, the invention also discloses a method for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor, wherein the method adopts the system for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor, and the method comprises the following steps:
step one, blending and diluting xylose mother liquor: xylose mother liquor stored in a raw material storage tank 1 is input into a blending tank 3, production water stored in a process water storage tank 2 is introduced for blending and diluting the xylose mother liquor, stability of blended materials is guaranteed, refraction of blended xylose mother liquor is 50-55%, arabinose content is 25-28%, and feed liquor temperature is 60-65 ℃.
Step two, xylose mother liquor is separated by simulated moving bed chromatography: and (3) carrying out chromatographic separation on the diluted xylose mother liquor by using a simulated moving bed chromatographic separation system 4 to respectively obtain EX liquor rich in arabinose components (namely EX components) and DX liquor rich in xylooligosaccharide components (namely DX components), wherein the EX liquor is stored in an EX storage tank, and the DX liquor is stored in a DX storage tank.
Step three, refining arabinose: the EX feed liquid obtained in the second step is fed into the arabinose production path 5, and after passing through the first decoloring treatment in the first decoloring tank 52, the first filtering treatment in the first filter 53, the first ion exchange impurity removal treatment in the first ion exchange system 54, the first evaporation concentration treatment in the first evaporator 55, the cooling crystallization treatment in the crystallization device 56, the centrifugal separation treatment in the centrifugal separation system 57, and the drying treatment in the drying device 58, the EX feed liquid is subjected to the first ion exchange impurity removal treatment in the first ion exchange system 54, thereby obtaining arabinose crystals, and the arabinose crystals are stored in the arabinose storage tank 59.
And step four, refining xylo-oligosaccharide: and (3) inputting the DX feed liquid obtained in the step (II) into an xylooligosaccharide preparation path 6, and sequentially carrying out second decolorization treatment of a second decolorization tank 62, second filtration treatment of a second filter 63, second ion exchange treatment of a second ion exchange system 64, membrane separation treatment of a membrane separation system 65 and second evaporation treatment of a second evaporator 66 on the DX feed liquid to obtain concentrated xylooligosaccharide liquid, wherein the xylooligosaccharide liquid is stored in an xylooligosaccharide storage tank 67. The nanofiltration trapped fluid obtained after the filtration treatment of the ultrafiltration membrane component 652 and the nanofiltration membrane component 653 of the membrane separation system 65 is rich in xylooligosaccharide components, the molecular mass of the xylooligosaccharide components is 300-3000 Da, and the xylooligosaccharide fluid after concentration is obtained after the second evaporation and concentration treatment of the second evaporator 66. The ultrafiltration trapped fluid with the molecular weight of 3000Da enters the temporary storage tank 651 through the first backflow pipe to be recycled, the nanofiltration permeate with the molecular weight of 300Da is temporarily stored in the second mother liquor storage tank 68 as the second mother liquor, and flows back to the blending tank 3 for material liquid blending and recycling.
In the second step, the diluted xylose mother liquor is subjected to simulated moving bed chromatographic separation to obtain CX liquor rich in a mixed sugar component (namely CX component), and the method further comprises the step five:
step five, concentrating the mixed sugar: and (3) inputting CX feed liquid into a mixed sugar preparation path 7, and carrying out third evaporation concentration treatment on the CX feed liquid by a third evaporator 72 until the refraction is 65-70%, so as to obtain mixed sugar concentrated solution, wherein the mixed sugar concentrated solution is stored in a mixed sugar storage tank 73.
In the third step, the first decoloring temperature is 60-65 ℃, the first evaporating temperature is 70-75 ℃, the first evaporating discharge density is controlled to 1288-1292 g/m, the cooling crystallization feeding temperature is 60-65 ℃, the cooling gradient is 0.5 ℃/min, the crystallization discharge temperature is 25-28 ℃, the washing time of the arabinose crystals after centrifugal separation is 30S, and the content of the arabinose crystals after drying is more than or equal to 99.8%. The refraction of the obtained first mother solution is 50-55%, and the content of arabinose in the first mother solution is 60-65%. The obtained first mother liquor is temporarily stored in a first mother liquor storage tank 510 and is returned to the blending tank 3 through a pipeline so as to stabilize the arabinose content of the feed liquor in the blending tank.
In the fourth step, the second decolorizing temperature is 60-65deg.C, and the pressure of the ultrafiltration membrane component 652 is 2.0The pressure of the nanofiltration membrane component 653 is 2.5-2.8 Mpa, the operating temperature is 60-65 ℃, the refractive index of the nanofiltration trapped fluid discharged from 300-3000 Da is 15-20%, the concentration temperature of the second evaporator 66 is 90-95 ℃, the refractive index of the second evaporation discharged from the second evaporator is controlled to be more than 70%, the content of xylooligosaccharide in the concentrated xylooligosaccharide fluid is 70-75%, wherein the sum of xylobiose, xylotriose and xylotetraose (XOS 2-4 ) The content is more than or equal to 50 percent, and meets the 70-type xylo-oligosaccharide standard specified by national standards.
In the method, xylose mother liquor is subjected to simulated moving bed chromatographic separation treatment of a simulated moving bed chromatographic separation system, so that the content and refractive parameters of sugar alcohol components in EX feed liquor, DX feed liquor and CX feed liquor are as follows:
referring to FIG. 5, a schematic view of microscopic examination of the arabinose crystals prepared by the method of the present invention is shown.
Referring to fig. 2 again, the simulated moving bed chromatographic separation treatment method of the simulated moving bed chromatographic separation system comprises the following steps:
the simulated moving bed chromatographic separation system is controlled by a computer and runs automatically, the system running at least comprises three processes of feeding, eluting and circulating, the three processes are completed as one period, one period is divided into six steps, and six running periods are one large period. Taking the chromatographic column 41 as an example of a cycle starting from the run, one cycle comprises the following six steps:
initially: the chromatographic columns 41-46 are circularly arranged from back to front in sequence, and the running program is set according to the calculated process, and all the liquid inlet valve, the water inlet valve, the discharging valve and the circulating pump in the system are in a closed state.
Feeding: simultaneously opening a liquid inlet valve A1 and a mixed sugar discharging valve CX1 of the chromatographic column 41, and opening a feed pump to obtain xylose blending liquid with a volume of 24-28m 3 The flow of/h enters the chromatographic column 41 through the liquid inlet valve A1, the liquid outlet refraction of the mixed sugar discharging valve CX1 is measured at random, and the mixed sugar CX component is collected when the refraction is displayed, and the feeding time is about 800-900 s.
And (3) water inlet: closing the liquid inlet valve A1, opening the water inlet valve B4, the serial valve F4 and the mixed sugar discharging valve CX5, controlling the water inflow rate to be 24-28m 3 And/h, collecting the components of the mixed sugar CX when the liquid discharged by the mixed sugar discharging valve CX5 to be measured has refraction, and the water inlet time is 400-450 s.
And (3) circulation: closing each liquid inlet valve, each water inlet valve and each discharge valve in the system, opening the serial valves F1-F6, starting the circulating pumps SHP 1-SHP 6, and enabling the flow of the circulating pumps to be 24-28m 3 And/h, the cycle time is 1500-1700 s.
Eluting: simultaneously opening a water inlet valve B4 of the chromatographic column 44 and an oligosaccharide discharge valve DX2 of the chromatographic column 42, closing serial valves F2 and F3 and circulating pumps SHP2 and SHP3, and controlling the flow rate to be 24-28m 3 And (3) eluting for 1050-1200 s, and collecting the oligosaccharide DX component when the liquid discharged from the oligosaccharide discharging valve DX2 to be measured has refraction.
Eluting: closing a water inlet valve B4 of the chromatographic column 44, an oligosaccharide discharge valve DX2 of the chromatographic column 42, serial valves F1-F4 and F6, circulating pumps SHP 1-SHP 4 and SHP6, opening a water inlet valve B5 of the chromatographic column 45 and an arabinose component discharge valve EX6 of the chromatographic column 46, and controlling the flow rate to be 24-28m 3 And (3) eluting for 480-600 s, and collecting the arabinose EX component when the liquid discharged by the discharge valve EX6 to be measured has refraction.
And so on, after the end of the above-described one cycle operation, the system automatically switches to feed from column 42, with the same steps as the previous cycle operation, but all further ahead of the previous column. After six cycles of sequentially running the chromatographic columns 41-46 complete one large cycle, starting a new large cycle to run, and returning to the step (1) of the first cycle, thereby circulating. After the system runs stably, all components are collected stably.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the invention.
Claims (10)
1. A system for co-producing arabinose and xylo-oligosaccharide by utilizing xylose mother liquor is characterized by comprising a raw material storage tank, a process water storage tank, a blending tank, a simulated moving bed chromatographic separation system, an arabinose preparation path and a xylo-oligosaccharide preparation path, wherein the xylose mother liquor to be treated is stored in the raw material storage tank, process water for dilution and cleaning is stored in the process water storage tank, a discharge port of the raw material storage tank is communicated with one feed port of the blending tank through a pipeline, one water outlet of the process water storage tank is communicated with the other feed port of the blending tank through a pipeline, the simulated moving bed chromatographic separation system is respectively provided with a moving bed liquid inlet, a moving bed water inlet, an arabinose component discharge port and a xylo-oligosaccharide component discharge port, the moving bed liquid inlet is communicated with the discharge port of the blending tank through a pipeline, and the moving bed water inlet is communicated with the other water outlet of the process water storage tank through a pipeline; the arabinose preparation path comprises an EX storage tank, a first decolorizing tank, a first filter, a first ion exchange system, a first evaporator, a crystallization device, a centrifugal separation system, a drying device and an arabinose storage tank which are sequentially communicated through pipelines, wherein a feed inlet of the EX storage tank is communicated with an arabinose component discharge port through a pipeline, a moisture sugar discharge end is arranged on the centrifugal separation system and is communicated with a feed end of the drying device through a pipeline, materials output from the discharge end of the drying device are prepared arabinose crystals, and the prepared arabinose storage crystals are stored in the arabinose storage tank; the xylooligosaccharide preparation path comprises a DX storage tank, a second decolorizing tank, a second filter, a second ion exchange system, a membrane separation system, a second evaporator and a xylooligosaccharide storage tank which are sequentially communicated through pipelines, wherein a feed inlet of the DX storage tank is communicated with a xylooligosaccharide component discharge port through a pipeline, the membrane separation system is provided with a xylooligosaccharide discharge end, the xylooligosaccharide discharge end is communicated with a feed end of the second evaporator through a pipeline, a material output from the discharge end of the second evaporator is prepared concentrated xylooligosaccharide liquid, and the prepared xylooligosaccharide liquid is stored in the xylooligosaccharide storage tank.
2. The system for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor according to claim 1, wherein the system for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor further comprises a mixed sugar preparation path, the simulated moving bed chromatographic separation system is further provided with a mixed sugar component discharge port, the mixed sugar preparation path comprises a CX storage tank, a third evaporator and a mixed sugar storage tank which are mutually communicated through pipelines, a feed inlet of the CX storage tank is communicated with the mixed sugar component discharge port through a pipeline, the material output from a discharge end of the third evaporator is prepared concentrated mixed sugar, and the prepared mixed sugar concentrated solution is stored in the mixed sugar storage tank.
3. The system for co-producing arabinose and xylooligosaccharide by utilizing xylose mother liquor according to claim 2, wherein the simulated moving bed chromatographic separation system comprises six chromatographic columns which are connected in series, each chromatographic column is provided with a feed inlet positioned at the upper part and a discharge outlet positioned at the lower part, the discharge outlet of each chromatographic column is communicated with the feed inlet of the next chromatographic column through a serial pipeline, the feed inlet of each chromatographic column is communicated with the discharge outlet of the previous chromatographic column through a serial pipeline, and a circulating pump and a serial valve are respectively arranged on each serial pipeline; each feed inlet is also respectively communicated with a liquid inlet pipeline and a water inlet pipeline, a liquid inlet valve is arranged on each liquid inlet pipeline, a water inlet valve is arranged on each water inlet pipeline, each liquid inlet pipeline is respectively communicated with a discharge port of the blending tank, and each water inlet pipeline is respectively communicated with one water outlet of the process water storage tank; each discharging port is further communicated with an arabinose component discharging pipeline, an xylooligosaccharide component discharging pipeline and a mixed sugar component discharging pipeline respectively, an arabinose discharging valve is arranged on each arabinose component discharging pipeline, an xylooligosaccharide discharging valve is arranged on each xylooligosaccharide component discharging pipeline, a mixed sugar discharging valve is arranged on each mixed sugar component discharging pipeline, each arabinose component discharging pipeline is communicated with a feeding port of an EX storage tank respectively, each xylooligosaccharide component discharging pipeline is communicated with a feeding port of the DX storage tank respectively, and each mixed sugar component discharging pipeline is communicated with a feeding port of the CX storage tank respectively.
4. The system for co-producing arabinose and xylooligosaccharide by using xylose mother liquor according to claim 1, wherein the centrifugal separation system is further provided with a liquid discharge end which is communicated with the feed end of the first mother liquor storage tank through a pipeline, and the discharge end of the first mother liquor storage tank is communicated with the other feed inlet of the blending tank through a pipeline.
5. The system for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor according to claim 1, wherein the membrane separation system is further provided with a mother liquor discharge end which is communicated with the feed end of a second mother liquor storage tank through a pipeline, and the discharge end of the second mother liquor storage tank is communicated with the other feed inlet of the blending tank through a pipeline.
6. The system for co-producing arabinose and xylooligosaccharide by using xylose mother liquor according to claim 5, wherein the membrane separation system comprises a temporary storage tank, an ultrafiltration membrane component, a nanofiltration membrane component and a trapped fluid storage tank which are sequentially communicated through pipelines, wherein a feed inlet of the temporary storage tank is communicated with a discharge outlet of a second ion exchange system through a pipeline, a discharge outlet of the trapped fluid storage tank is communicated with a feed inlet of a second evaporator through a pipeline, a first valve and a first material conveying pump are sequentially arranged on the pipeline communicated with the ultrafiltration membrane component, and a second material conveying pump is arranged on the pipeline communicated with the nanofiltration membrane component; an ultrafiltration passing end and an ultrafiltration interception end are respectively arranged on the ultrafiltration membrane component, the ultrafiltration interception end is communicated with a feed inlet of the temporary storage tank through a first backflow pipeline, a second valve is arranged on the first backflow pipeline, and the ultrafiltration passing end is communicated with a second feed pump through a pipeline; the nanofiltration membrane component is provided with a nanofiltration passing end and a nanofiltration intercepting end, the nanofiltration intercepting end is communicated with a feed inlet of a interception liquid storage tank through a pipeline, a third valve is arranged on the pipeline, which is communicated with the interception liquid storage tank, of the nanofiltration intercepting end, the nanofiltration intercepting end outputs materials which are nanofiltration intercepting liquid rich in xylooligosaccharide components, the nanofiltration intercepting liquid rich in xylooligosaccharide components is stored in the interception liquid storage tank, the nanofiltration intercepting end is also communicated with the ultrafiltration membrane component and a connecting pipeline between a second material conveying pump through a second backflow pipeline, a fourth valve is arranged on the second backflow pipeline, and the nanofiltration passing end is communicated with the feed inlet of a second mother liquid storage tank through a pipeline.
7. A method for co-producing arabinose and xylo-oligosaccharides by using xylose mother liquor, which is characterized in that the method adopts the system for co-producing arabinose and xylo-oligosaccharides by using xylose mother liquor according to any one of claims 1 to 6, and the method comprises the following steps:
step one, blending and diluting xylose mother liquor: inputting xylose mother liquor stored in a raw material storage tank into a blending tank, introducing production water stored in a process water storage tank to carry out xylose mother liquor blending dilution, ensuring the stability of blended materials, wherein the refraction of blended xylose mother liquor is 50-55%, the arabinose content is 25-28%, and the temperature of the blended xylose mother liquor is 60-65 ℃;
step two, xylose mother liquor is separated by simulated moving bed chromatography: carrying out chromatographic separation on the diluted xylose mother liquor by using a simulated moving bed chromatographic separation system to respectively obtain EX liquor rich in arabinose components and DX liquor rich in xylooligosaccharide components, wherein the EX liquor is stored in an EX storage tank, and the DX liquor is stored in a DX storage tank;
step three, refining arabinose: inputting the EX feed liquid obtained in the step two into an arabinose preparation path, and obtaining arabinose crystals after the EX feed liquid sequentially passes through a first decolorization treatment of a first decolorization tank, a first filtration treatment of a first filter, a first ion exchange treatment of a first ion exchange system, a first evaporation treatment of a first evaporator, a cooling crystallization treatment of a crystallization device, a centrifugal separation treatment of a centrifugal separation system and a drying treatment of a drying device, wherein the arabinose crystals are stored in an arabinose storage tank;
and step four, refining xylo-oligosaccharide: inputting the DX feed liquid obtained in the step two into an xylooligosaccharide preparation path, and obtaining concentrated xylooligosaccharide liquid after the DX feed liquid sequentially passes through the second decolorization treatment of a second decolorization tank, the second filtration treatment of a second filter, the second ion exchange treatment of a second ion exchange system, the membrane separation treatment of a membrane separation system and the second evaporation treatment of a second evaporator, wherein the xylooligosaccharide liquid is stored in an xylooligosaccharide storage tank.
8. The method for co-producing arabinose and xylo-oligosaccharides by using xylose mother liquor according to claim 7, wherein in said step two, the diluted xylose mother liquor is subjected to simulated moving bed chromatography to obtain CX feed liquor rich in a mixed sugar component, said method further comprising the step five:
step five, concentrating the mixed sugar: and (3) inputting CX feed liquid into a mixed sugar preparation path, carrying out third evaporation concentration treatment on the CX feed liquid by a third evaporator until the refraction is 65-70%, and obtaining mixed sugar concentrated solution which is stored in a mixed sugar storage tank.
9. The method for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor according to claim 7, wherein in the third step, the first decoloring temperature is 60-65 ℃, the first evaporating temperature is 70-75 ℃, the first evaporating discharge density is controlled to 1288-1292 g/m, the cooling crystallization feeding temperature is 60-65 ℃, the cooling gradient is 0.5 ℃/min, the crystallization discharging temperature is 25-28 ℃, the washing time of arabinose crystals after centrifugal separation is 30S, and the content of arabinose crystals after drying is more than or equal to 99.8%.
10. The method for co-producing arabinose and xylo-oligosaccharide by using xylose mother liquor according to claim 7, wherein in the fourth step, the second decoloring temperature is 60-65 ℃, the concentration temperature of the second evaporator is 90-95 ℃, the refractive index of the second evaporation discharge is controlled to be more than 70%, the xylo-oligosaccharide content in the concentrated xylo-oligosaccharide solution is 70-75%, and the sum content of xylobiose, xylotriose and xylotetraose is more than or equal to 50%, which accords with the 70 xylo-oligosaccharide standard specified by national standards.
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