CN104311391A - Membrane concentration technology for producing xylitol by using viscose fiber pressed liquor as raw materials - Google Patents
Membrane concentration technology for producing xylitol by using viscose fiber pressed liquor as raw materials Download PDFInfo
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- CN104311391A CN104311391A CN201410622101.2A CN201410622101A CN104311391A CN 104311391 A CN104311391 A CN 104311391A CN 201410622101 A CN201410622101 A CN 201410622101A CN 104311391 A CN104311391 A CN 104311391A
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- liquor
- viscose fiber
- raw material
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- 239000012528 membrane Substances 0.000 title claims abstract description 232
- TVXBFESIOXBWNM-UHFFFAOYSA-N Xylitol Natural products OCCC(O)C(O)C(O)CCO TVXBFESIOXBWNM-UHFFFAOYSA-N 0.000 title claims abstract description 47
- 239000000835 fiber Substances 0.000 title claims abstract description 47
- HEBKCHPVOIAQTA-UHFFFAOYSA-N meso ribitol Natural products OCC(O)C(O)C(O)CO HEBKCHPVOIAQTA-UHFFFAOYSA-N 0.000 title claims abstract description 47
- 239000000811 xylitol Substances 0.000 title claims abstract description 47
- HEBKCHPVOIAQTA-SCDXWVJYSA-N xylitol Chemical compound OC[C@H](O)[C@@H](O)[C@H](O)CO HEBKCHPVOIAQTA-SCDXWVJYSA-N 0.000 title claims abstract description 47
- 229960002675 xylitol Drugs 0.000 title claims abstract description 47
- 235000010447 xylitol Nutrition 0.000 title claims abstract description 47
- 229920000297 Rayon Polymers 0.000 title claims abstract description 37
- 239000002994 raw material Substances 0.000 title claims abstract description 27
- 238000005516 engineering process Methods 0.000 title claims abstract description 10
- 239000000919 ceramic Substances 0.000 claims abstract description 80
- 238000001914 filtration Methods 0.000 claims abstract description 54
- 239000003513 alkali Substances 0.000 claims abstract description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000002253 acid Substances 0.000 claims abstract description 19
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical class OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 17
- 235000011149 sulphuric acid Nutrition 0.000 claims abstract description 17
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 15
- 239000012535 impurity Substances 0.000 claims abstract description 14
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 13
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 11
- 230000007062 hydrolysis Effects 0.000 claims abstract description 10
- 238000000605 extraction Methods 0.000 claims abstract description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 6
- 239000001257 hydrogen Substances 0.000 claims abstract description 6
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 6
- 238000001728 nano-filtration Methods 0.000 claims description 98
- 239000007788 liquid Substances 0.000 claims description 80
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Substances [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 55
- 238000000034 method Methods 0.000 claims description 41
- 238000001471 micro-filtration Methods 0.000 claims description 35
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 32
- 238000006386 neutralization reaction Methods 0.000 claims description 31
- 238000004519 manufacturing process Methods 0.000 claims description 29
- 229960003487 xylose Drugs 0.000 claims description 28
- SRBFZHDQGSBBOR-LECHCGJUSA-N alpha-D-xylose Chemical compound O[C@@H]1CO[C@H](O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-LECHCGJUSA-N 0.000 claims description 27
- 239000012466 permeate Substances 0.000 claims description 17
- 239000001117 sulphuric acid Substances 0.000 claims description 16
- 238000010612 desalination reaction Methods 0.000 claims description 10
- 230000008569 process Effects 0.000 claims description 9
- 239000012141 concentrate Substances 0.000 claims description 8
- SRBFZHDQGSBBOR-IOVATXLUSA-N D-xylopyranose Chemical compound O[C@@H]1COC(O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-IOVATXLUSA-N 0.000 abstract description 4
- PYMYPHUHKUWMLA-UHFFFAOYSA-N arabinose Natural products OCC(O)C(O)C(O)C=O PYMYPHUHKUWMLA-UHFFFAOYSA-N 0.000 abstract description 2
- SRBFZHDQGSBBOR-UHFFFAOYSA-N beta-D-Pyranose-Lyxose Natural products OC1COC(O)C(O)C1O SRBFZHDQGSBBOR-UHFFFAOYSA-N 0.000 abstract description 2
- 238000000746 purification Methods 0.000 abstract description 2
- 229910052799 carbon Inorganic materials 0.000 abstract 1
- 238000006555 catalytic reaction Methods 0.000 abstract 1
- 239000002245 particle Substances 0.000 abstract 1
- 238000011045 prefiltration Methods 0.000 abstract 1
- 229920002488 Hemicellulose Polymers 0.000 description 15
- 150000003839 salts Chemical class 0.000 description 9
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 description 4
- 229920002678 cellulose Polymers 0.000 description 4
- 235000010980 cellulose Nutrition 0.000 description 4
- 238000005374 membrane filtration Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000001913 cellulose Substances 0.000 description 3
- HEBKCHPVOIAQTA-NGQZWQHPSA-N d-xylitol Chemical compound OC[C@H](O)C(O)[C@H](O)CO HEBKCHPVOIAQTA-NGQZWQHPSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 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 2
- 229920001131 Pulp (paper) Polymers 0.000 description 2
- 150000001413 amino acids Chemical class 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 229910017053 inorganic salt Inorganic materials 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000011112 process operation Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- 235000014676 Phragmites communis Nutrition 0.000 description 1
- 229930006000 Sucrose Natural products 0.000 description 1
- 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 1
- 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 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 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 1
- 210000004369 blood Anatomy 0.000 description 1
- 239000008280 blood Substances 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000004042 decolorization Methods 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- -1 far below 100 Chemical compound 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 230000002440 hepatic effect Effects 0.000 description 1
- 208000006454 hepatitis Diseases 0.000 description 1
- 231100000283 hepatitis Toxicity 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 230000008720 membrane thickening Effects 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 230000035764 nutrition Effects 0.000 description 1
- 210000002381 plasma Anatomy 0.000 description 1
- 229920002647 polyamide Polymers 0.000 description 1
- 238000004094 preconcentration Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 239000005720 sucrose Substances 0.000 description 1
- 230000001225 therapeutic effect Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/14—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group
- C07C29/141—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group with hydrogen or hydrogen-containing gases
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
- C07H1/00—Processes for the preparation of sugar derivatives
- C07H1/06—Separation; Purification
-
- C—CHEMISTRY; METALLURGY
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Biotechnology (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Molecular Biology (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention provides a membrane concentration technology for producing xylitol by using viscose fiber pressed liquor as raw materials. The technology comprises the following specific steps: A, membrane concentration: the pressed liquor produced by viscose fibers is firstly processed in a pre-filter manner to remove impurities with large particles to enter a micro-filter membrane to be processed, the penetrated liquor is concentrated two to four times in a circulating manner through a nano filter film, the final concentrated liquor is diluted by adding the water to be sent into a ceramic membrane to be filtered, and the obtained concentrated liquor is the concentrated liquor of the pressed alkali liquor; the nano filter membrane is concentrated two to four times in a circulating manner, and before filtration each time, the material liquor is diluted by adding the water to enter the nano filter film; B, semi fiber extraction: the acid is added into the concentrated liquor of the pressed alkali liquor to neutralize to obtain semi fiber liquor; C, hydrolysis: dilute sulphuric acids are added into the semi fiber liquor to carry out the hydrolysis; D, purification: the hydrolysis liquor is filtered through the ceramic membrane, the penetrated liquor enters the nano filter membrane to be desalted, and the concentrated liquor is decolored through active carbon to obtain the purified liquor; E, hydrogenation: the hydrogen is communicated into the purified liquor of xylose, and the hydrogenation is carried out on the basis of the catalysis of nickel to obtain the xylitol.
Description
Technical field
The present invention relates to Xylitol preparation field, the membrane concentration technique that to be specifically related to viscose fiber pressed liquor be raw material production Xylitol.
Background technology
The sugariness of Xylitol is equivalent to sucrose, and heat is equivalent to glucose, and Xylitol can adjust glycometabolic exception, is nutrition agent and the therapeutical agent of diabetics.Xylitol has stronger anti-ketoboidies effect, can in order to rescue ketoboidies patient.Xylitol can slow down and produce the speed of lipid acid in blood plasma, but blood sugar can not be made to increase, and is also the hepatic of hepatitis patient.Xylitol Heat stability is good, heats and does not produce chemical reaction together with amino acid, can prepare various preparation, as nutrient drug with amino acid.Xylitol also has special preventing decayed tooth function as food.But Xylitol is one of polyvalent alcohol of price, production cost is too high is the major obstacle promoting its application.Annual agroforestry are produced and all can be produced a large amount of waste material containing hemicellulose (about 20% ~ 40%).The xylose utilizing hydrolysis of hemicellulose to obtain produces Xylitol, not only has good economic benefit, also has important environment protection significance.
With chemical pulp plant celluloses such as () wood pulp, cotton pulp, straw pulp, reed pulps in the production process of viscose fiber of raw material, adopting alkali lye to process (dipping, squeezing) to Mierocrystalline cellulose is the first step manufacturing viscose fiber.Hemicellulose concentration is high, extremely adverse influence is produced to cellulose viscose manufacturing technique and final product quality, therefore must in impregnation technology with alkali lye by hemicellulose stripping, the Mierocrystalline cellulose of high strength could be obtained, so a large amount of high concentration alkali pressed liquors being rich in hemicellulose can be produced in above process.
Main component in alkali pressed liquor is sodium hydroxide and hemicellulose.Hemicellulose is therefrom separated by treatment process many employings nanofiltration of existing press lye, obtains comparatively pure alkali lye.Through purification alkali lye can direct reuse in technique, but part alkali only can be realized reuse by nanofiltration membrane, still containing a large amount of alkali in the concentrated solution that the hemicellulose in its trapped fluid obtains after concentrated.During at present this part feed liquid is used for as salkali waste and technique, hemicellulose enters wastewater treatment, or adopts calcination to reclaim sodium hydroxide, and hemicellulose is burned.From above existing technique, hemicellulose is not fully used.
201210104647.X, the patent of invention that name is called " a kind of utilize in production process of viscose fiber the method for squeezing waste lye and preparing wood sugar ".By membrane filtration prepare hemicellulose solution, the extraction of hemicellulose, hemicellulose hydrolysis, in depickling, pre-concentration, decolouring, ion-exchange and Conventional concentration, crystallization, be separated, drying process obtains wood sugar finished product.This patent adopts industrial alcohol to extract hemicellulose, and cost is high.
Document " the membrane separation concentration technical study of xylo-oligosaccharide " (" foodstuffs industry ", 09 phase in 2012), pilot plant test device is adopted to carry out pilot plant test to the separation of lower concentration xylo-oligosaccharide solution is concentrated, the effect of the polyamide-based nanofiltration of comparative studies and reverse osmosis two kinds of membrane techniquies, determines the optimised process operational condition that nanofiltration membrane separation concentrates xylo-oligosaccharide solution.This technique nanofiltration membrane thickening temperature is low, and membrane filtration efficiency is lower.
Summary of the invention
For above-mentioned technical problem, the membrane concentration technique that to the invention provides with viscose fiber pressed liquor be raw material production Xylitol.The Xylitol salinity obtained is low, and purity is high, and process operation efficiency is high, is adapted to scale operation.
For achieving the above object, the present invention adopts following technical scheme:
With the membrane concentration technique that viscose fiber pressed liquor is raw material production Xylitol, it is characterized in that: concrete technology step is as follows:
A, membrane concentration
The press lye produced by viscose fiber is first through pre-filtering removing large granular impurity, enter microfiltration membrane process, permeate is through concentrated 2-4 time of nanofiltration membrane circulation, and send after last concentrated solution thin up into ceramic membrane filter, gained concentrated solution is the concentrated solution of press lye; Concentrated 2-4 time of described nanofiltration membrane circulation, before each filtration, feed liquid all enters nanofiltration membrane after thin up.
B, extraction half fibre
By the concentrated solution acid neutralization of press lye, obtain half fine liquid.
C, hydrolysis
In half fine liquid, add dilute sulphuric acid, hydrolysis reaction occurs;
D, purifying
Hydrolyzed solution is through ceramic membrane filter, and permeate enters nanofiltration membrane desalination, and concentrated solution, through activated carbon decolorizing, obtains the refined solution of wood sugar;
E, hydrogenation
Pass into hydrogen in the refined solution of wood sugar, hydrogenation occurs in the katalysis of nickel, obtains Xylitol.
Step A of the present invention, described microfiltration membrane aperture is 5 microns, and the molecular weight cut-off of described nanofiltration membrane is 200-400, and the molecular weight cut-off of ceramic membrane is 800-1500.
Micro-filtrate membrane filtration amount is large, is conducive to improving filtration efficiency; The molecular weight cut-off of 200-400, makes alkali separate from permeate, progressively lowers alkali dense, promotes half fine concentration, retain a part of monose simultaneously; The molecular weight cut-off of ceramic membrane is 800-1500, can retain half fibre, improve the purity of product.
Step A of the present invention, before each nanofiltration membrane, the amount of thin up is 1 times of stock liquid volume, filters the concentrated solution volume obtained identical with stock liquid volume.While ensureing filtration efficiency, little to the damage of nanofiltration membrane.
Preferably, described permeate, containing alkali 200-300g/l, containing half fine 40-80 g/l, after nanofiltration membrane circulation is concentrated, obtains concentrated solution containing alkali 12-75g/l, containing half fine 40-80g/l.Under lowering the dense prerequisite of alkali, ensure the filtration efficiency of film.
Step A of the present invention, feed liquid first enters ceramic membrane device through thin up, and add water to feed liquid gradation in working cycle, total amount of water is 5 times of material liquid volume, and gained concentrated solution volume is identical with stock liquid volume.While ensureing filtration efficiency, little to the damage of ceramic membrane.
Preferably, containing alkali 2-4g/l in the concentrated solution of described ceramic membrane filter, containing half fine 40-80 g/l.Be down to minimum by dense for alkali, ensure that the purity of half fibre.
Pre-filtering of the present invention refers to, press lye filters and Plate Filtration removing large granular impurity through rotary drum successively.Pre-filtering makes press lye not containing the solid impurity of more than 5 microns, and protection film is not below damaged by solid impurity.
Step A of the present invention, the temperature of micro-filtration is 40-50 DEG C, and the temperature of nanofiltration membrane is 40-60 DEG C, and the temperature of ceramic membrane filter is 60-80 DEG C, and filtration temperature is high, and liquid viscosity is lower, is conducive to filtration efficiency and improves.
Step A of the present invention, the mistake mould difference of micro-filtration is 1-2bar, and the mistake mould difference of nanofiltration membrane is 3-4bar, and the mistake mould difference of ceramic membrane is 5-6bar.For the feature that viscose glue press lye viscosity is higher, adopt higher pressure reduction to filter, can ensure that half fine concentration in alkali lye reaches processing requirement.
Step A of the present invention, feed liquid is 20-40 m at the flow of microfiltration membrane
3/ h, the flow in nanofiltration membrane is 25-40m
3/ h, the flow in ceramic membrane is 200-250m
3/ h.The surface velocity that bonding props up film is higher, film is not easy contaminated.
Step A of the present invention, it is 1m that the list of microfiltration membrane props up filtration area
2, it is 26.8m that the list of nanofiltration membrane props up filtration area
2, it is 0.6m that the list of ceramic membrane props up filtration area
2, single film has larger filtration area under the prerequisite taking less space.
Step B of the present invention, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization.The advantage adding hydrochloric acid is that the molecules of salt amount formed is lower, is conducive to the desalination in later stage.
Step C of the present invention, the concentration of dilute sulphuric acid is 12%, and make pH value be 0, wood sugar is fully hydrolyzed under this condition.
D step of the present invention, the molecular weight cut-off of described nanofiltration membrane is 100-200.Owing to adopting hydrochloric acid neutralization, the salt of generation is sodium-chlor, and the molecular weight of sodium-chlor is smaller, and far below 100, and wood sugar molecular weight is much larger than 100, effectively can realize being separated of salt and wood sugar.
Preferably, described nanofiltration membrane desalination, crossing mould difference is 3-4bar, and temperature is 30-40 DEG C, and single filtration area is 26.8 m
2, adapt to the change of low catching molecular, guarantee salt is separated with wood sugar.
Preferably, the material liquid volume before described nanofiltration membrane concentrates is 10-15 times of concentrated solution volume, is conducive to reducing the salt content in wood sugar.
The decolouring of D step of the present invention refers to: adjusted to ph is 4-5, adds gac, at 50-60 DEG C, adsorb 0.5-1h.
Preferably, described gac is LY-T-ac gac, and consumption is 3-5%.Best to the decolorizing effect of liquid glucose, percent of decolourization is 70%, and the rate of loss of sugar is minimum.
Beneficial effect of the present invention is:
1, the present invention adopts microfiltration membrane, nanofiltration membrane and ceramic membrane to combine filtering and concentrating half fibre, because the filtration efficiency of micro-filtration and nanofiltration is higher than ceramic membrane, first with the macro-molecular protein in micro-filtrate membrane filtration removal alkali lye and bacterium, adopt repeatedly nanofiltration membrane that alkali concn is progressively dropped to certain degree again, concentrated half fibre simultaneously, reduce the damage to film, then adopt ceramic membrane filter; The feed liquid that ceramic membrane is applicable to filter the dense height of later stage low alkali half fine is run, and is the powerful guarantee that low alkali is dense.Nanofiltration membrane and ceramic membrane cooperatively interact, and have complementary advantages, and make containing alkali 2-4g/l in final concentrated solution, containing half fine 40-80 g/l, achieve low alkali dense, height half is fine; And process operation efficiency is high, little to the damage of film, cost is low.
2, the amount of nanofiltration membrane thin up of the present invention is 1 times of stock liquid volume, filters the concentrated solution volume obtained identical with stock liquid volume at every turn; Ceramic membrane filter, feed liquid first enters ceramic membrane device through thin up, and add water to feed liquid gradation in working cycle, total amount of water is 5 times of material liquid volume, and gained concentrated solution volume is identical with stock liquid volume.This technique can realize nanofiltration membrane water 10m excessively per hour
3left and right, ceramic membrane is per hour crosses water 45m
3left and right, ensure that filtration efficiency; Meanwhile, little to the damage of film, the 2-3 that can reach its quality guarantee period work-ing life doubly, reduces cost to a great extent, is adapted to industrialization scale operation.
3, the present invention adds hydrochloric acid neutralization to the concentrated solution obtained, then adopts molecular weight cut-off to be the nanofiltration membrane desalination of 100-200.In hydrochloric acid and the salt generated be sodium-chlor, the molecular weight of sodium-chlor, far below 100, and wood sugar molecular weight is much larger than 100, effectively can realize being separated of salt and wood sugar.Be conducive to the desalination in later stage, further increase the purity of wood sugar.
4, hydrolyzed solution is entered nanofiltration membrane desalination by the present invention, thus have effectively achieved being separated of salt and wood sugar, ensure that the purity of wood sugar, after wood sugar hydrogenation, be converted into Xylitol, the specific conductivity finally obtaining wood sugar is 8000-10000 μ s/cm, and ignition residue is 5-10%.Ignition residue is the direct indicator weighing inorganic salt, and the massfraction described in wood sugar shared by inorganic salt is only 5-10%; Specific conductivity is the electrolytical degree existed in reaction liquid, and the main electrolyte of wood sugar is exactly inorganic salts, so this index also can reflect the number of salinity in product.It is low that low conductivity and ignition residue describe the wood sugar salinity adopting the inventive method to obtain, high purity more than 85%.
Embodiment
Below in conjunction with embodiment, essentiality content of the present invention is described in further detail.
Embodiment 1
With the membrane concentration technique that viscose fiber pressed liquor is raw material production Xylitol, concrete technology step is as follows:
A, membrane concentration
The press lye produced by viscose fiber is first through pre-filtering removing large granular impurity, enter microfiltration membrane process, permeate is through concentrated 2 times of nanofiltration membrane circulation, and send after last concentrated solution thin up into ceramic membrane filter, gained concentrated solution is the concentrated solution of press lye; Concentrated 2 times of described nanofiltration membrane circulation, before each filtration, feed liquid all enters nanofiltration membrane after thin up.
B, extraction half fibre
By the concentrated solution acid neutralization of press lye, obtain half fine liquid.
C, hydrolysis
In half fine liquid, add dilute sulphuric acid, hydrolysis reaction occurs;
D, purifying
Hydrolyzed solution is through ceramic membrane filter, and permeate enters nanofiltration membrane desalination, and concentrated solution, through activated carbon decolorizing, obtains the refined solution of wood sugar;
E, hydrogenation
Pass into hydrogen in the refined solution of wood sugar, hydrogenation occurs in the katalysis of nickel, obtains Xylitol.
Embodiment 2
With the membrane concentration technique that viscose fiber pressed liquor is raw material production Xylitol, concrete technology step is as follows:
A, membrane concentration
The press lye produced by viscose fiber is first through pre-filtering removing large granular impurity, enter microfiltration membrane process, permeate is through concentrated 3 times of nanofiltration membrane circulation, and send after last concentrated solution thin up into ceramic membrane filter, gained concentrated solution is the concentrated solution of press lye; Concentrated 3 times of described nanofiltration membrane circulation, before each filtration, feed liquid all enters nanofiltration membrane after thin up.
B, extraction half fibre
By the concentrated solution acid neutralization of press lye, obtain half fine liquid.
C, hydrolysis
In half fine liquid, add dilute sulphuric acid, hydrolysis reaction occurs;
D, purifying
Hydrolyzed solution is through ceramic membrane filter, and permeate enters nanofiltration membrane desalination, and concentrated solution, through activated carbon decolorizing, obtains the refined solution of wood sugar;
E, hydrogenation
Pass into hydrogen in the refined solution of wood sugar, hydrogenation occurs in the katalysis of nickel, obtains Xylitol.
Embodiment 3
With the membrane concentration technique that viscose fiber pressed liquor is raw material production Xylitol, concrete technology step is as follows:
A, membrane concentration
The press lye produced by viscose fiber is first through pre-filtering removing large granular impurity, enter microfiltration membrane process, permeate is through concentrated 4 times of nanofiltration membrane circulation, and send after last concentrated solution thin up into ceramic membrane filter, gained concentrated solution is the concentrated solution of press lye; Concentrated 4 times of described nanofiltration membrane circulation, before each filtration, feed liquid all enters nanofiltration membrane after thin up.
B, extraction half fibre
By the concentrated solution acid neutralization of press lye, obtain half fine liquid.
C, hydrolysis
In half fine liquid, add dilute sulphuric acid, hydrolysis reaction occurs;
D, purifying
Hydrolyzed solution is through ceramic membrane filter, and permeate enters nanofiltration membrane desalination, and concentrated solution, through activated carbon decolorizing, obtains the refined solution of wood sugar;
E, hydrogenation
Pass into hydrogen in the refined solution of wood sugar, hydrogenation occurs in the katalysis of nickel, obtains Xylitol.
Embodiment 4
The present embodiment is substantially the same manner as Example 1, on this basis:
Described step A, microfiltration membrane aperture is 5 microns, and the molecular weight cut-off of nanofiltration membrane is 200, and the molecular weight cut-off of ceramic membrane is 800.
The nanofiltration membrane circulation of described step A is concentrated, and the amount of thin up is 1 times of stock liquid volume, filters the concentrated solution volume obtained identical with stock liquid volume at every turn.
Embodiment 5
The present embodiment is substantially the same manner as Example 2, on this basis:
Described step A, microfiltration membrane aperture is 5 microns, and the molecular weight cut-off of nanofiltration membrane is 400, and the molecular weight cut-off of ceramic membrane is 1500.
The nanofiltration membrane circulation of described step A is concentrated, and the amount of thin up is 1 times of stock liquid volume, filters the concentrated solution volume obtained identical with stock liquid volume at every turn.
Embodiment 6
The present embodiment is substantially the same manner as Example 3, on this basis:
Described step A, microfiltration membrane aperture is 5 microns, and the molecular weight cut-off of nanofiltration membrane is 300, and the molecular weight cut-off of ceramic membrane is 1000.
The nanofiltration membrane circulation of described step A is concentrated, and the amount of thin up is 1 times of stock liquid volume, filters the concentrated solution volume obtained identical with stock liquid volume at every turn.
Embodiment 7
The present embodiment is substantially the same manner as Example 1, on this basis:
Described step A, microfiltration membrane aperture is 5 microns, and the molecular weight cut-off of nanofiltration membrane is 250, and the molecular weight cut-off of ceramic membrane is 900.
The nanofiltration membrane circulation of described step A is concentrated, and the amount of thin up is 1 times of stock liquid volume, filters the concentrated solution volume obtained identical with stock liquid volume at every turn.
Embodiment 8
The present embodiment is substantially the same manner as Example 4, on this basis:
Described step A, permeate, containing alkali 300g/l, containing half fine 80g/l, after nanofiltration membrane circulation is concentrated, obtains concentrated solution containing alkali 75g/l, containing half fine 80g/l.
Embodiment 9
The present embodiment is substantially the same manner as Example 5, on this basis:
Described step A, permeate, containing alkali 260g/l, containing half fine 70g/l, after nanofiltration membrane circulation is concentrated, obtains concentrated solution containing alkali 32.5g/l, containing half fine 80g/l.
Embodiment 10
The present embodiment is substantially the same manner as Example 6, on this basis:
Described step A, permeate, containing alkali 200g/l, containing half fine 40g/l, after nanofiltration membrane circulation is concentrated, obtains concentrated solution containing alkali 12.5g/l, containing half fine 40g/l.
Embodiment 11
The present embodiment is substantially the same manner as Example 7, on this basis:
Described step A, permeate, containing alkali 220g/l, containing half fine 60g/l, after nanofiltration membrane circulation is concentrated, obtains concentrated solution containing alkali 55g/l, containing half fine 60g/l.
Embodiment 12
The present embodiment is substantially the same manner as Example 8, on this basis:
The ceramic membrane filter of described step A, feed liquid first enters ceramic membrane device through thin up, and add water to feed liquid gradation in working cycle, total amount of water is 5 times of material liquid volume, and gained concentrated solution volume is identical with stock liquid volume.
Described step A, containing alkali 2g/l in the concentrated solution of ceramic membrane filter, containing half fine 40g/l.
Embodiment 13
The present embodiment is substantially the same manner as Example 9, on this basis:
The ceramic membrane filter of described step A, feed liquid first enters ceramic membrane device through thin up, and add water to feed liquid gradation in working cycle, total amount of water is 5 times of material liquid volume, and gained concentrated solution volume is identical with stock liquid volume.
Described step A, containing alkali 4g/l in the concentrated solution of ceramic membrane filter, containing half fine 80 g/l.
Described pre-filtering refers to, pressed liquor filters and Plate Filtration removing large granular impurity through rotary drum successively.
Described step A, the temperature of micro-filtration is 40 DEG C, and the temperature of nanofiltration membrane is 40 DEG C, and the temperature of ceramic membrane filter is 60 DEG C.
Embodiment 14
The present embodiment is substantially the same manner as Example 10, on this basis:
The ceramic membrane filter of described step A, feed liquid first enters ceramic membrane device through thin up, and add water to feed liquid gradation in working cycle, total amount of water is 5 times of material liquid volume, and gained concentrated solution volume is identical with stock liquid volume.
Described step A, containing alkali 3g/l in the concentrated solution of ceramic membrane filter, containing half fine 50g/l.
Described pre-filtering refers to, pressed liquor filters and Plate Filtration removing large granular impurity through rotary drum successively.
Described step A, the temperature of micro-filtration is 50 DEG C, and the temperature of nanofiltration membrane is 60 DEG C, and the temperature of ceramic membrane filter is 80 DEG C.
Described step A, the mistake mould difference of micro-filtration is 1bar, and the mistake mould difference of nanofiltration membrane is 4bar, and the mistake mould difference of ceramic membrane is 6bar.
Embodiment 15
The present embodiment is substantially the same manner as Example 11, on this basis:
The ceramic membrane filter of described step A, feed liquid first enters ceramic membrane device through thin up, and add water to feed liquid gradation in working cycle, total amount of water is 5 times of material liquid volume, and gained concentrated solution volume is identical with stock liquid volume.
Described step A, containing alkali 2.5g/l in the concentrated solution of ceramic membrane filter, containing half fine 60g/l.
Described pre-filtering refers to, pressed liquor filters and Plate Filtration removing large granular impurity through rotary drum successively.
Described step A, the temperature of micro-filtration is 45 DEG C, and the temperature of nanofiltration membrane is 45 DEG C, and the temperature of ceramic membrane filter is 65 DEG C.
Described step A, the mistake mould difference of micro-filtration is 2bar, and the mistake mould difference of nanofiltration membrane is 3bar, and the mistake mould difference of ceramic membrane is 5bar.
Described step A, feed liquid is 20m at the flow of microfiltration membrane
3/ h, the flow in nanofiltration membrane is 25m
3/ h, the flow in ceramic membrane is 200m
3/ h.
Embodiment 16
The present embodiment is substantially the same manner as Example 11, on this basis:
The ceramic membrane filter of described step A, feed liquid first enters ceramic membrane device through thin up, and add water to feed liquid gradation in working cycle, total amount of water is 5 times of material liquid volume, and gained concentrated solution volume is identical with stock liquid volume.
Described step A, containing alkali 3.5g/l in the concentrated solution of ceramic membrane filter, containing half fine 70g/l.
Described pre-filtering refers to, pressed liquor filters and Plate Filtration removing large granular impurity through rotary drum successively.
Described step A, the temperature of micro-filtration is 46 DEG C, and the temperature of nanofiltration membrane is 55 DEG C, and the temperature of ceramic membrane filter is 75 DEG C.
The mistake mould difference of described micro-filtration is 1.5bar, and the mistake mould difference of nanofiltration membrane is 3.6bar, and the mistake mould difference of ceramic membrane is 5.6bar.
Described step A, feed liquid is 40m at the flow of microfiltration membrane
3/ h, the flow in nanofiltration membrane is 40m
3/ h, the flow in ceramic membrane is 250m
3/ h.
Described step A, it is 1m that the list of microfiltration membrane props up filtration area
2, it is 26.8m that the list of nanofiltration membrane props up filtration area
2, it is 0.6m that the list of ceramic membrane props up filtration area
2.
Embodiment 17
The present embodiment is substantially the same manner as Example 11, on this basis:
The ceramic membrane filter of described step A, feed liquid first enters ceramic membrane device through thin up, and add water to feed liquid gradation in working cycle, total amount of water is 5 times of material liquid volume, and gained concentrated solution volume is identical with stock liquid volume.
Described step A, containing alkali 3.8g/l in the concentrated solution of ceramic membrane filter, containing half fine 65g/l.
Described pre-filtering refers to, pressed liquor filters and Plate Filtration removing large granular impurity through rotary drum successively.
Described step A, the temperature of micro-filtration is 42 DEG C, and the temperature of nanofiltration membrane is 55 DEG C, and the temperature of ceramic membrane filter is 72 DEG C.
Described step A, the mistake mould difference of micro-filtration is 1.2bar, and the mistake mould difference of nanofiltration membrane is 3.6bar, and the mistake mould difference of ceramic membrane is 5.2bar.
Described step A, feed liquid is 30m at the flow of microfiltration membrane
3/ h, the flow in nanofiltration membrane is 30m
3/ h, the flow in ceramic membrane is 220m
3/ h.
Described step A, it is 1m that the list of microfiltration membrane props up filtration area
2, it is 26.8m that the list of nanofiltration membrane props up filtration area
2, it is 0.6m that the list of ceramic membrane props up filtration area
2.
Embodiment 18
The present embodiment is substantially the same manner as Example 8, on this basis:
Described step B, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization, make pH value be 4.
Embodiment 19
The present embodiment is substantially the same manner as Example 9, on this basis:
Described step B, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization, make pH value be 5.
Described step C, the concentration of dilute sulphuric acid is 12%, makes pH value be 0.
Embodiment 20
The present embodiment is substantially the same manner as Example 10, on this basis:
Described step B, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization.
Described step C, the concentration of dilute sulphuric acid is 12%, makes pH value be 0.
Described D step, the molecular weight cut-off of ceramic membrane is 800.
Embodiment 21
The present embodiment is substantially the same manner as Example 11, on this basis:
Described step B, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization.
Described step C, the concentration of dilute sulphuric acid is 12%, makes pH value be 0.
Described D step, the molecular weight cut-off of ceramic membrane is 1500.
Described D step, the molecular weight cut-off of nanofiltration membrane is 200.
Embodiment 22
The present embodiment is substantially the same manner as Example 16, on this basis:
Described step B, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization.
Described step C, the concentration of dilute sulphuric acid is 12%, makes pH value be 0.
Described D step, the molecular weight cut-off of ceramic membrane is 1000.
Described D step, the molecular weight cut-off of nanofiltration membrane is 100.
The mistake mould difference of described nanofiltration membrane is 3bar, and temperature is 30 DEG C, and single filtration area is 26.8 m
2.
Embodiment 23
The present embodiment is substantially the same manner as Example 17, on this basis:
Described step B, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization.
Described step C, the concentration of dilute sulphuric acid is 12%, makes pH value be 0.
Described D step, the molecular weight cut-off of ceramic membrane is 900.
Described D step, the molecular weight cut-off of nanofiltration membrane is 120.
The mistake mould difference of described nanofiltration membrane is 4bar, and temperature is 40 DEG C, and single filtration area is 26.8 m
2.
Described D step, the material liquid volume before nanofiltration membrane concentrates is 10 times of concentrated solution volume.
Embodiment 24
The present embodiment is substantially the same manner as Example 17, on this basis:
Described step B, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization.
Described step C, the concentration of dilute sulphuric acid is 12%, makes pH value be 0.
Described D step, the molecular weight cut-off of ceramic membrane is 950.
Described D step, the molecular weight cut-off of nanofiltration membrane is 150.
The mistake mould difference of described nanofiltration membrane is 3.5bar, and temperature is 32 DEG C, and single filtration area is 26.8 m
2.
Described D step, the material liquid volume before nanofiltration membrane concentrates is 15 times of concentrated solution volume.
The decolouring of described D step refers to: adjusted to ph is 4, adds gac, at 50 DEG C, adsorb 1h.
The specific conductivity obtaining Xylitol is 8500 μ s/cm, and ignition residue is 4%.
Embodiment 25
The present embodiment is substantially the same manner as Example 17, on this basis:
Described step B, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization.
Described step C, the concentration of dilute sulphuric acid is 12%, makes pH value be 0.
Described D step, the molecular weight cut-off of ceramic membrane is 1200.
Described D step, the molecular weight cut-off of nanofiltration membrane is 180.
The mistake mould difference of described nanofiltration membrane is 3.6bar, and temperature is 35 DEG C, and single filtration area is 26.8 m
2.
Described D step, the material liquid volume before nanofiltration membrane concentrates is 12 times of concentrated solution volume.
The decolouring of described D step refers to: adjusted to ph is 5, adds gac, at 60 DEG C, adsorb 0.5h.
Described gac is LY-T-ac gac, and consumption is 3%.
The specific conductivity obtaining Xylitol is 9000 μ s/cm, and ignition residue is 5%.
Embodiment 26
The present embodiment is substantially the same manner as Example 17, on this basis:
Described step B, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization.
Described step C, the concentration of dilute sulphuric acid is 12%, makes pH value be 0.
Described D step, the molecular weight cut-off of ceramic membrane is 800.
Described D step, the molecular weight cut-off of nanofiltration membrane is 105.
The mistake mould difference of described nanofiltration membrane is 3.6bar, and temperature is 36 DEG C, and single filtration area is 26.8 m
2.
Described D step, the material liquid volume before nanofiltration membrane concentrates is 13 times of concentrated solution volume.
The decolouring of described D step refers to: adjusted to ph is 4.5, adds gac, at 52 DEG C, adsorb 0.6h.
Described gac is LY-T-ac gac, and consumption is 5%.
The specific conductivity obtaining Xylitol is 10000 μ s/cm, and ignition residue is 6%.
Embodiment 27
The present embodiment is substantially the same manner as Example 17, on this basis:
Described step B, concentrated solution acid neutralization, refers to and adds hydrochloric acid neutralization.
Described step C, the concentration of dilute sulphuric acid is 12%, makes pH value be 0.
Described D step, the molecular weight cut-off of ceramic membrane is 1000.
Described D step, the molecular weight cut-off of nanofiltration membrane is 120.
The mistake mould difference of described nanofiltration membrane is 3bar, and temperature is 32 DEG C, and single filtration area is 26.8 m
2.
Described D step, the material liquid volume before nanofiltration membrane concentrates is 12 times of concentrated solution volume.
The decolouring of described D step refers to: adjusted to ph is 4.5, adds gac, at 53 DEG C, adsorb 0.6h.
Described gac is LY-T-ac gac, and consumption is 4%.
The specific conductivity obtaining Xylitol is 8000 μ s/cm, and ignition residue is 3%.
Claims (17)
1. with the membrane concentration technique that viscose fiber pressed liquor is raw material production Xylitol, it is characterized in that: concrete technology step is as follows:
A, membrane concentration
The press lye produced by viscose fiber is first through pre-filtering removing large granular impurity, enter microfiltration membrane process, permeate is through concentrated 2-4 time of nanofiltration membrane circulation, and send after last concentrated solution thin up into ceramic membrane filter, gained concentrated solution is the concentrated solution of press lye; Concentrated 2-4 time of described nanofiltration membrane circulation, before each filtration, feed liquid all enters nanofiltration membrane after thin up;
B, extraction half fibre
By the concentrated solution acid neutralization of press lye, obtain half fine liquid;
C, hydrolysis
In half fine liquid, add dilute sulphuric acid, hydrolysis reaction occurs;
D, purifying
Hydrolyzed solution is through ceramic membrane filter, and permeate enters nanofiltration membrane desalination, and concentrated solution, through activated carbon decolorizing, obtains the refined solution of wood sugar;
E, hydrogenation
Pass into hydrogen in the refined solution of wood sugar, hydrogenation occurs in the katalysis of nickel, obtains Xylitol.
2. the membrane concentration technique that is raw material production Xylitol with viscose fiber pressed liquor according to claim 1, it is characterized in that: described step A, the aperture of microfiltration membrane is 5 microns, and the molecular weight cut-off of nanofiltration membrane is 200-400, and the molecular weight cut-off of ceramic membrane is 800-1500.
3. the membrane concentration technique that is raw material production Xylitol with viscose fiber pressed liquor according to claim 1, it is characterized in that: described step A, before each nanofiltration membrane, the amount of thin up is 1 times of stock liquid volume, filters the concentrated solution volume obtained identical with stock liquid volume.
4. the membrane concentration technique that is raw material production Xylitol with viscose fiber pressed liquor according to claim 3, it is characterized in that: described permeate contains alkali 200-300g/l, containing half fine 40-80 g/l, after nanofiltration membrane circulation is concentrated, obtain concentrated solution containing alkali 12-75g/l, containing half fine 40-80g/l.
5. the membrane concentration technique that is raw material production Xylitol with viscose fiber pressed liquor according to claim 1, it is characterized in that: described step A, feed liquid first enters ceramic membrane device through thin up, add water to feed liquid gradation in working cycle, total amount of water is 5 times of material liquid volume, and gained concentrated solution volume is identical with stock liquid volume.
6. the membrane concentration technique that is raw material production Xylitol with viscose fiber pressed liquor according to claim 5, is characterized in that: containing alkali 2-4g/l in the concentrated solution of described ceramic membrane filter, containing half fine 40-80 g/l.
7. the membrane concentration technique that is raw material production Xylitol with viscose fiber pressed liquor according to claim 1, it is characterized in that: described step A, the temperature of micro-filtration is 40-50 DEG C, and the temperature of nanofiltration membrane is 40-60 DEG C, and the temperature of ceramic membrane filter is 60-80 DEG C.
8. the membrane concentration technique that is raw material production Xylitol with viscose fiber pressed liquor according to claim 1, it is characterized in that: described step A, the mistake mould difference of micro-filtration is 1-2bar, and the mistake mould difference of nanofiltration membrane is 3-4bar, and the mistake mould difference of ceramic membrane is 5-6bar.
9. the membrane concentration technique that is raw material production Xylitol with viscose fiber pressed liquor according to claim 1, it is characterized in that: described step A, feed liquid is 20-40m at the flow of microfiltration membrane
3/ h, the flow in nanofiltration membrane is 25-40m
3/ h, the flow in ceramic membrane is 200-250m
3/ h.
10. the membrane concentration technique that is raw material production Xylitol with viscose fiber pressed liquor according to claim 1, it is characterized in that: described step A, it is 1m that the list of microfiltration membrane props up filtration area
2, it is 26.8m that the list of nanofiltration membrane props up filtration area
2, it is 0.6m that the list of ceramic membrane props up filtration area
2.
The 11. membrane concentration techniques that are raw material production Xylitol with viscose fiber pressed liquor according to claim 1, is characterized in that: described step B, concentrated solution acid neutralization, refer to and add hydrochloric acid neutralization.
The 12. membrane concentration techniques that are raw material production Xylitol with viscose fiber pressed liquor according to claim 1, it is characterized in that: described step C, the concentration of dilute sulphuric acid is 12%, makes pH value be 0.
The 13. membrane concentration techniques that are raw material production Xylitol with viscose fiber pressed liquor according to claim 1, it is characterized in that: described D step, the molecular weight cut-off of nanofiltration membrane is 100-200.
The 14. membrane concentration techniques that are raw material production Xylitol with viscose fiber pressed liquor according to claim 13, is characterized in that: the mistake mould difference of described nanofiltration membrane is 3-4bar, and temperature is 30-40 DEG C, and single filtration area is 26.8 m
2.
The 15. membrane concentration techniques that are raw material production Xylitol with viscose fiber pressed liquor according to claim 1, is characterized in that: described D step, the material liquid volume before nanofiltration membrane concentrates be the 10-15 of concentrated solution volume doubly.
The 16. membrane concentration techniques that are raw material production Xylitol with viscose fiber pressed liquor according to claim 1, is characterized in that: the decolouring of described D step refers to: adjusted to ph is 4-5, adds gac, at 50-60 DEG C, adsorb 0.5-1h.
The 17. membrane concentration techniques that are raw material production Xylitol with viscose fiber pressed liquor according to claim 16, it is characterized in that: described gac is LY-T-ac gac, consumption is 3-5%.
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| CN105420292A (en) * | 2015-12-15 | 2016-03-23 | 宜宾雅泰生物科技有限公司 | Method for preparing xylitol through viscose squeezed alkali liquid |
| CN105969916A (en) * | 2016-07-20 | 2016-09-28 | 宜宾雅泰生物科技有限公司 | Method for preparing xylose by taking squeezed alkali liquid obtained in production of viscose as raw material |
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| CN113582814A (en) * | 2021-07-16 | 2021-11-02 | 吉林省石油化工设计研究院 | Full-process differential pressure type sugar alcohol production method |
| CN113582814B (en) * | 2021-07-16 | 2023-05-09 | 吉林省石油化工设计研究院 | Full-flow differential pressure type sugar alcohol production method |
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