CN109369731A - A kind of method of glucose during removing xylose production - Google Patents
A kind of method of glucose during removing xylose production Download PDFInfo
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- C07H—SUGARS; DERIVATIVES THEREOF; NUCLEOSIDES; NUCLEOTIDES; NUCLEIC ACIDS
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Abstract
The invention discloses a kind of methods of glucose during removing xylose production, specifically comprise the following steps: that (1) is preprocessed to solid content 20-50% by xylose first extract；(2) pH to 3-9 is adjusted；(3) glucose is digested；(4) it is pumped into the recycling of macromolecular ultrafiltration system enzyme；(5) above-mentioned enzymolysis liquid is pumped into chromatographic separation device chromatographic isolation；(6) the B material rich in xylose and arabinose ingredient is refined；(7) refined liquid is concentrated by evaporation, drying and packaging obtains finished product xylose crystals after centrifuge separation.Utilize oxydasis glucose, then pass through chromatographic purification, effectively remove glucose, improve xylose purity 6-15%, crystallization yield of xylose 5-15% is improved, xylose crystalline temperature fall time is effectively reduced, solves easy microbiological contamination during xylose production in traditional xylose process, the drawbacks such as crystallization is difficult, and crystallization yield is low.
Description
Technical field
The invention belongs to the purification technique fields of xylose production, and in particular to Portugal during a kind of removing xylose production
The method of grape sugar.
Background technique
Xylose is a kind of using very extensive high valuable chemicals, is widely used in food, medicine and other fields, mainly
For producing xylitol.Xylose mainly passes through plant material (corncob, bagasse, the slurrying that dilute acid hydrolysis is rich in hemicellulose
Paper waste, birch-bark etc.) it obtains, currently used catalyst is the dilute sulfuric acid of mass fraction 0.5-2%.China be xylose,
The production of xylitol and big export country.Currently, the xylose production process of comparative maturity are as follows: dilute acid hydrolysis-neutralization-decoloration-ion
Exchange-concentration-crystallization-finished product.Wherein, on the main chain xylosyl of the hemicellulose of the raw materials such as corncob, it is connected with 4-O- methyl
Glucuronic acid base or glucuronic acid base branch, every 100g xylan 4-O- containing 0.7g methyl glucose uronic acid base and 0.4g
In addition glucuronic acid base is also connected with aralino branch on main chain glycosyl.The ratio of xylosyl, aralino is
10:1~20:1.Therefore, hydrolysis of hemicellulose product, other than D- xylose that pentosan hydrolyzes, L-arabinose,
Also inevitably there is part glucose.In addition, xylose is produced by raw material of bagasse, because the sucrose hydrolysis of remaining can also produce Portugal
Grape sugar, to increase the content of glucose impurity.The presence of glucose causes strong influence to xylose production, as main
Impurity, the presence of glucose directly reduce xylose purity, increase feed liquid viscosity, cause to seriously affect to the crystallization of xylose massecuite,
Reduce xylose yield.On the other hand, glucose is the monosaccharide easily utilized by microbial metabolism, under appropriate conditions, largely
Microorganism growth, very big influence is caused to subsequent production, if breeding object enters downstream process, final crystallized centrifugation
Step is easy to be mixed into xylose crystals product, influences product purity, causes production accident, a kind of patent " micro- life in inhibition Xylose
The device and method of object growth " it (number of patent application: is expressly mentioned in 201310485500.4) a kind of by control temperature, pH etc.
The method that condition suppresses growth of microorganism.So effectively removing the glucose in xylose production, fundamentally avoid microorganism raw
It is long, it is not only advantageous to normally produce, while crystallization difficulty can be reduced, greatly improves crystallization yield of xylose.
Currently, the effective means of removal glucose includes yeast degradation, glucose oxidase enzymatic hydrolysis, chromatographic isolation, film point
From etc., wherein yeast degradation is using relatively broad, wherein patent " a method of improve purity of xylose solution " (number of patent application:
200710116111.9) and patent " a method of utilize biological treatment improve crystalline xylose yield " (number of patent application:
201310333481.3) method for having all referred to glucose in the yeast fermentation method removal Xylose under different condition, but yeast
Fermentation method introduces other a large amount of metabolic derivatives, impacts to subsequent separation process while removing glucose, while by
In the presence of the main components such as xylose, Yeast Growth environmental requirement is harsh, and quantity-produced unstability risk is high.Xylose,
The separation of monosaccharide, but the separation of glucose and xylose can be realized in arabinose production process with chromatographic separation technology
It is relatively low, it, can be with the separating effect of significant increase glucose and xylose if gluconic acid can be converted glucose into.With enzyme
The development of engineering technology converts glucose into gluconic acid technology day by day by glucose oxidase (EC.1.1.3.4, GOD)
Maturation, patent " a method of improve xylose hydrolysis fluid in xylose purity " (number of patent application: 201611079111-1) are related to
Gluconic acid is obtained using glucose oxidase enzymatic hydrolysis glucose, thus the method for improving xylose purity, the method can realize grape
Sugared Efficient Conversion, but fundamentally do not remove the impurity such as gluconic acid from Xylose, still there is a fixing to xylose crystalline
It rings.Enzyme preparation higher cost not only influences the processing capacity of downstream separation process such as without effectively recycling, and causes big
Amount waste.The method of enzyme recycling has many methods, and such as the methods of flocculation, air bearing, extraction, these method rate of recovery are all relatively low, and
Influence enzymatic activity.
Summary of the invention
For glucose in the prior art as major impurity, lead to easy microbiological contamination during xylose production, crystallizes difficulty
Technical problem, the purpose of the present invention is to provide a kind of method of glucose during removing xylose production, this method operation letters
Single efficient, process does not introduce the pollutants such as heavy metal.Glucose during xylose production can be played and significantly to be removed
Effect, improves crystallization yield of xylose conscientiously.
The invention is realized by the following technical scheme, a method of glucose during removing xylose production, feature
It is, converts glucose into gluconic acid or gluconate using enzyme process, utilizes the enzyme system of membrane technology separation and recovery addition
Agent efficiently separates gluconic acid (salt) and xylose using chromatographic separation technology.
The technical scheme adopted by the invention is as follows:
The method of glucose, specifically comprises the following steps: during a kind of removing xylose production
(1) it pre-processes: xylose first extract is removed into solid residue, powder activity carbon decoloring, ion exchange through mechanical filter
Resin or electrodialysis desalination depickling are concentrated by evaporation to solid content 20-50%；
(2) it adjusts pH: under airflow stirring or mechanical rapid mixing conditions, adding suitable inorganic acid or alkali adjusts pH to 3-
9；
(3) digest glucose: the feed liquid after pH will be adjusted and be added in reactor tank, using air stirring, be added enzyme preparation into
Row enzyme digestion reaction, enzyme preparation additive amount are the 0.5-3% of raw material solid quality, persistently convey air, 25-55 DEG C of temperature control, instead
1-48h between seasonable controls pH by adding appropriate inorganic base；
(4) enzyme recycles: above-mentioned enzymatic hydrolysis completion liquid pump is entered macromolecular ultrafiltration system, operating pressure 0.1-1.0MPa, control
Through retention ratio, trapped fluid is collected and returns to next group enzyme digestion reaction tank, permeate enters chromatographic isolation head tank；
(5) chromatographic isolation: above-mentioned enzymolysis liquid is pumped into chromatographic separation device, pure water is eluant, eluent, system temperature 35-80
DEG C, system pressure 0.1-0.5MPa, the B material for separating rich in xylose and arabinose ingredient is rich in inorganic salts, gluconic acid
The C of (salt), glycan impurity expects；It collects to obtain B material, the solid content 12-25% that B expects, wherein xylose purity 65-85%, grape
Sugared purity is lower than 5%.
(6) it refines: above-mentioned B being expected to carry out active carbon decoloring, anion-cation exchange resin desalting refinement, promotes light transmission extremely
50% or more, conductance 0.5mS/cm or less；
(7) finished product: refined liquid is concentrated by evaporation to solid content 70-85%, using gradient cooling crystallization, centrifugation
Drying and packaging obtains finished product xylose crystals after separation.
Further, xylose first extract is plant fiber through dilute acid hydrolysis, steam blasting or biology hair in the step (1)
What ferment obtained is rich in xylose, and the feed liquid containing impurity glucose, plant fiber includes but is not limited to birch-bark, corncob, sugarcane
Slag.
Further, mechanical filter is in belt filter press, plate and frame filter press or diaphragm filter press in the step (1)
Any one；Ion exchange resin includes cation exchange resin and anion exchange resin, and wherein cation exchange resin is excellent
For model 001*7 resin；Anion exchange resin is model D301 and 300C resin；Electrodialysis include but is not limited to homogeneous membrane,
Heterogeneous membrane, bipolar membrane electrodialysis.
Further, inorganic acid is dilute sulfuric acid or dilute hydrochloric acid in the step (2)；The inorganic base be sodium hydroxide,
Sodium carbonate or calcium carbonate.
Preferred embodiment is sodium carbonate, and compared to sodium hydroxide, sodium carbonate liquor pH is low under same concentrations, does not easily cause neutralization
The local pH of process liquid glucose is excessively high, to reduce the loss of sugar caused by partial over-alkali, compared to calcium carbonate etc., sodium ion is to enzyme
Activity influence is minimum.Therefore the factors such as comprehensive economy, it is preferable that sodium carbonate.
Further, the air gas velocity of air stirring is controlled in 2-50BV per hour, i.e. charge volume in the step (3)
It is (2-50) with the ratio between liquid volume: 1.
Further, enzyme preparation is glucose oxidase (E.C.1.1.3.4) and peroxidase in the step (3)
The complex enzyme that (EC 1.11.1.7 or EC1.11.1.6) is mixed according to weight ratio 7:3, additive amount are raw material solid quality
1%, the reaction time is for 24 hours.
PH control is in 3-9 in the step (3), it is preferable that pH4-5.
Further, macromolecular ultrafiltration system is in ceramic membrane, organic rolled film or hollow-fibre membrane in the step (4)
Any one, retaining molecular weight 1,000-150,000Da, membranous system material rejection 5-10%, preferably retention molecule
The ceramic membrane of 100,000Da is measured, it is best to retain ratio 8%.
Further, the macromolecular ultrafiltration system cycle of operation is 180 minutes in the step (4), wherein being successively normal
Operation 170 minutes, pure water is just being washed 5 minutes, and pure water backwash 5 minutes, for eliminating enzyme preparation in the enrichment of film surface.It is small every 48
Shi Yici is respectively cleaned 1 hour with 0.5% sodium hydroxide of quality and 0.1% protease, to eliminate pollution of the film in membranous system.
Further, the chromatographic isolation resin of chromatographic separation device is Hydrogen, sodium form, potassium type or calcium in the step (5)
Any one in type resin, it is preferable that sodium form resin.
Further, step (6) ion exchange resin includes cation exchange resin and anion exchange resin,
Wherein cation exchange resin is model 001*7 resin；Anion exchange resin is model D301 and 300C resin.
The invention has the benefit that
The method of glucose has following compared with traditional production technique during a kind of removing xylose production of the invention
Advantage: utilizing oxydasis glucose, then by chromatographic purification, effectively removes glucose, improves xylose purity 6-15%,
Crystallization yield of xylose 5-15% is improved, xylose crystalline temperature fall time is effectively reduced, solves xylose production in traditional xylose process
Easy microbiological contamination in the process, the drawbacks such as crystallization is difficult, and crystallization yield is low.
Glucose oxidase molecules amount about 140KDa, catalase (EC1.11.1.6, CAT) molecular weight about 240KDa,
It selects the ultrafiltration membrane of appropriate molecular cut off (MWCO) to recycle above-mentioned enzyme preparation, any chemistry can be not added under normal temperature conditions
High efficiente callback is realized in the case where auxiliary agent, the enzyme preparation rate of recovery is more than 95%, thermal sensitivity caused by will not thus increasing because of temperature
Enzyme preparation or loss of material, or side reaction occurs, do not introduce the risk that other chemical reagent generate product quality yet.
Specific embodiment
The present invention is further illustrated below with reference to embodiment.
Embodiment 1:
Corncob 1.0% dilute sulfuric acid of mass fraction after mechanical grading, washed with impurities hydrolyzes 2.5 hours, keeps the temperature 125 DEG C,
Liquid-solid ratio 8:1 (over dry), after hydrolysis after diaphragm filter press is separated by solid-liquid separation, the Powdered Activated Carbon of addition amount of dry matter 0.5% is de-
Color, light transmittance 76%.It is concentrated by evaporation after sun-male-female ion exchange resin treatment, concentrate solid content 31%,
PH2.30, positive resin select 001*7, and negative resin selects 300C.
The sodium carbonate liquor that mass fraction is 8% is prepared, refining and concentrating liquid is slowly added under compressed air stirring, adjusts
PH to 4.5.
The above-mentioned feed liquid of 500L is taken, compressed air stirring is passed through, tolerance is controlled in 5m31.0Kg enzyme preparation is added in/h, wherein
Glucose oxidase 0.8Kg, peroxidase 0.2Kg, reaction time for 24 hours, control temperature at 35 DEG C, by the way that 8% carbonic acid is added dropwise
Sodium solution controls pH.
Hollow fibre membrane systems after opening cleaning, retaining molecular weight 100,000Da, control system pressure 0.2MPa,
Obtain dialyzate 460L, solid content 30%.Remaining about 40L trapped fluid reserves for other use.
The Simulation moving bed for loading sodium form resin is selected, 60 DEG C of system temperature, system pressure 0.1-.02MPa, single batch feeds
Volume 1.5L, pure water 7.1L, extraction B expect 3.5L, solid content 12%, xylose purity 81.5%, glucose purity 0.3%；C
Expect 5.1L, xylose purity 5.3%, glucose purity 1.5%.
B to be expected to add active carbon decoloring, sun-male-female ion exchange resin combines desalting refinement, and positive resin selects 001*7,
Negative resin selects 300C, permeate light transmission 95%, conductivity 0.32mS/cm.It is concentrated by evaporation to solid content 80%, is transferred to
In crystallizer, gradient cooling is to 35 DEG C, 2 DEG C/h of cooling rate.Xylose crystals are obtained after centrifugation drying.
Table 1: the various middle control point constituent contents of embodiment 1 and the ultrafiltration system enzyme rate of recovery
Note: 1. xyloses, glucose purity detection use liquid chromatography, referring to xylose national standard GB/T 23532-2009；
2. enzyme rate of recovery detection method is dying method with coomassie brilliant blue.
Embodiment 2:
Birch-bark 0.5% dilute hydrochloric acid of mass fraction after mechanical grading, washed with impurities hydrolyzes 2 hours, keeps the temperature 125 DEG C, liquid
Gu after hydrolysis after belt filter press is separated by solid-liquid separation, the powder activity carbon decoloring of amount of dry matter 0.5% is added than 8:1 (over dry),
Light transmittance 79%.It is concentrated by evaporation after sun-male-female ion exchange resin treatment, concentrate solid content 33%, pH2.15,
Positive resin selects 001*7, and negative resin selects 300C.
The sodium carbonate liquor that mass fraction is 8% is prepared, refining and concentrating liquid is slowly added under compressed air stirring, adjusts
PH to 5.0.
The above-mentioned feed liquid of 500L is taken, compressed air stirring is passed through, tolerance is controlled in 6m31.5Kg enzyme preparation is added in/h, wherein
Glucose oxidase 1.05Kg, peroxidase 0.45Kg, reaction time 12h control temperature at 35 DEG C, by the way that 8% carbon is added dropwise
Acid sodium solution controls pH.
Hollow fibre membrane systems after opening cleaning, retaining molecular weight 50,000Da, control system pressure 0.23MPa,
Obtain dialyzate 450L, solid content 30.5%.Remaining about 50L trapped fluid reserves for other use.
The Simulation moving bed for loading sodium form resin is selected, 60 DEG C of system temperature, system pressure 0.1-.02MPa, single batch feeds
Volume 1.5L, pure water 7.1L, extraction B expect 3.5L, solid content 12%, xylose purity 82.4%, glucose purity 0.2%；C
Expect 5.1L, xylose purity 5.8%, glucose purity 1.5%.
B to be expected to add active carbon decoloring, sun-male-female ion exchange resin combines desalting refinement, and positive resin selects 001*7,
Negative resin selects 300C, permeate light transmission 95%, conductivity 0.28mS/cm.It is concentrated by evaporation to solid content 80%, is transferred to
In crystallizer, gradient cooling is to 35 DEG C, 2 DEG C/h of cooling rate.Xylose crystals are obtained after centrifugation drying.
Table 2: the various middle control point constituent contents of embodiment 2 and the ultrafiltration system enzyme rate of recovery
Embodiment 3:
Bagasse 0.5% dilute hydrochloric acid of mass fraction after washed with impurities hydrolyzes 2 hours, keeps the temperature 125 DEG C, liquid-solid ratio 10:1
(over dry) adds the powder activity carbon decoloring of amount of dry matter 0.5%, light transmittance after hydrolysis after plate and frame filter press is separated by solid-liquid separation
76%.It is concentrated by evaporation after sun-male-female ion exchange resin treatment, concentrate solid content 32%, pH2.17, positive resin
001*7 is selected, negative resin selects D301.
The sodium carbonate liquor that mass fraction is 8% is prepared, refining and concentrating liquid is slowly added under compressed air stirring, adjusts
PH to 5.0.
The above-mentioned feed liquid of 500L is taken, compressed air stirring is passed through, tolerance is controlled in 6m31.5Kg enzyme preparation is added in/h, wherein
Glucose oxidase 1.05Kg, peroxidase 0.45Kg, reaction time for 24 hours, control temperature at 35 DEG C, by the way that 8% carbon is added dropwise
Acid sodium solution controls pH.
Hollow fibre membrane systems after opening cleaning, retaining molecular weight 100,000Da, control system pressure 0.23MPa,
Obtain dialyzate 460L, solid content 30.6%.Remaining about 40L trapped fluid reserves for other use.
The Simulation moving bed for loading sodium form resin is selected, 60 DEG C of system temperature, system pressure 0.1-.02MPa, single batch feeds
Volume 1.6L, pure water 7.0L, extraction B expect 3.6L, solid content 12%, xylose purity 80.4%, glucose purity 0.2%；C
Expect 5.0L, xylose purity 5.4%, glucose purity 2.6%.
B to be expected to add active carbon decoloring, sun-male-female ion exchange resin combines desalting refinement, and positive resin selects 001*7,
Negative resin selects D301, permeate light transmission 97%, conductivity 0.29mS/cm.It is concentrated by evaporation to solid content 82%, is transferred to
In crystallizer, gradient cooling is to 35 DEG C, 2 DEG C/h of cooling rate.Xylose crystals are obtained after centrifugation drying.
Table 3: the various middle control point constituent contents of embodiment 3 and the ultrafiltration system enzyme rate of recovery
Embodiment 4:
Bagasse 0.5% dilute hydrochloric acid of mass fraction after washed with impurities hydrolyzes 2.5 hours, keeps the temperature 125 DEG C, liquid-solid ratio 12:1
(over dry) adds the powder activity carbon decoloring of amount of dry matter 0.5%, light transmittance after hydrolysis after diaphragm filter press is separated by solid-liquid separation
76%.It is concentrated by evaporation after sun-male-female ion exchange resin treatment, concentrate solid content 30%, pH2.27, positive resin
001*7 is selected, negative resin selects D301.
The sodium carbonate liquor that mass fraction is 8% is prepared, refining and concentrating liquid is slowly added under compressed air stirring, adjusts
PH to 4.5.
The above-mentioned feed liquid of 500L is taken, compressed air stirring is passed through, tolerance is controlled in 6m31.0Kg enzyme preparation is added in/h, wherein
Glucose oxidase 0.8Kg, peroxidase 0.2Kg, reaction time 36h control temperature at 35 DEG C, by the way that 8% carbonic acid is added dropwise
Sodium solution controls pH.
Ceramic membranous system after opening cleaning, retaining molecular weight 50,000Da, control system pressure 0.2MPa are obtained saturating
Analyse liquid 460L, solid content 30.5%.Remaining about 40L trapped fluid reserves for other use.
The Simulation moving bed for loading calcium type resin is selected, 60 DEG C of system temperature, system pressure 0.1-.02MPa, single batch feeds
Volume 1.6L, pure water 7.0L, extraction B expect 3.6L, solid content 12%, xylose purity 80.3%, glucose purity 0.9%；C
Expect 5.0L, xylose purity 3.4%, glucose purity 2.8%.
B to be expected to add active carbon decoloring, sun-male-female ion exchange resin combines desalting refinement, and positive resin selects 001*7,
Negative resin selects D301, permeate light transmission 97%, conductivity 0.29mS/cm.It is concentrated by evaporation to solid content 79%, is transferred to
In crystallizer, gradient cooling is to 35 DEG C, 2 DEG C/h of cooling rate.Xylose crystals are obtained after centrifugation drying.
Table 4: the various middle control point constituent contents of embodiment 5 and the ultrafiltration system enzyme rate of recovery
On above-mentioned working foundation, the Experiment on Microbiology of refined liquid and blank assay in each embodiment of across comparison, and
Final crystallization yield finished product, purity.Wherein blank assay is that the identical feed liquid of implementation case 1 is directly entered step 6 from step 2, no
It is handled by intermediate process.Refined liquid Experiment on Microbiology operating condition is as follows, takes refined liquid 100mL in triangular flask, opening is set
In 35 DEG C of constant temperature oscillation casees, revolving speed 180rpm continues 48 hours observation micro-organisms situations.As a result it see the table below:
Table 5: each embodiment influences to compare on subsequent handling
Note: crystal purity and light transmittance detection method are referring to xylose national standard GB/T 23532-2009
The above is not limitation of the present invention, it should be pointed out that: those skilled in the art are come
It says, under the premise of not departing from essential scope of the present invention, several variations, modifications, additions or substitutions can also be made, these improvement
It also should be regarded as protection scope of the present invention with retouching.
Claims (9)
1. a kind of method of glucose during removing xylose production, which is characterized in that specifically comprise the following steps:
(1) it pre-processes: xylose first extract is removed into solid residue, powder activity carbon decoloring, ion exchange resin through mechanical filter
Or electrodialysis desalination depickling, evaporation and concentration to solid content 20-50%；
(2) it adjusts pH: under airflow stirring or mechanical rapid mixing conditions, adding suitable inorganic acid or alkali adjusts pH to 3-9；
(3) it digests glucose: the feed liquid after adjusting pH being added in reactor tank, air stirring is utilized, enzyme preparation is added and carries out enzyme
Solution reaction, enzyme preparation additive amount are the 0.5-3% of raw material solid quality, persistently convey air, 25-55 DEG C of temperature control, when reaction
Between 1-48h, pass through the appropriate inorganic base of addition and control pH；
(4) enzyme recycles: above-mentioned enzymatic hydrolysis completion liquid pump being entered macromolecular ultrafiltration system, operating pressure 0.1-1.0MPa, control penetrates
Ratio is retained, trapped fluid is collected and returns to next group enzyme digestion reaction tank, permeate enters chromatographic isolation head tank；
(5) chromatographic isolation: above-mentioned enzymolysis liquid is pumped into chromatographic separation device, pure water makees eluant, eluent, 35-80 DEG C of system temperature, is
Unite pressure 0.1-0.5MPa, and the B material for separating rich in xylose and arabinose ingredient rich in inorganic salts, gluconic acid (salt), gathers
The C of sugared impurity expects；
(6) it refines: above-mentioned B being expected to carry out active carbon decoloring, ion exchange resin desalting refinement, promote light transmission to 50% or more,
Conductance 0.5mS/cm or less；
(7) finished product: refined liquid is concentrated by evaporation to solid content 70-85%, using gradient cooling crystallization, centrifuge separation
Drying and packaging obtains finished product xylose crystals afterwards.
2. according to claim 1 it is a kind of removing xylose production during glucose method, which is characterized in that the step
(1) to be plant fiber be rich in xylose through what dilute acid hydrolysis, steam blasting or biofermentation obtained to xylose first extract in, contains impurity
The feed liquid of glucose.
3. according to claim 1 it is a kind of removing xylose production during glucose method, which is characterized in that the step
(1) or step (6) ion exchange resin includes cation exchange resin and anion exchange resin, wherein cation exchange tree
Excellent rouge is model 001*7 resin；Anion exchange resin is model D301 and 300C resin.
4. according to claim 1 it is a kind of removing xylose production during glucose method, which is characterized in that the step
(2) inorganic acid is dilute sulfuric acid or dilute hydrochloric acid in；The inorganic base is sodium hydroxide, sodium carbonate or calcium carbonate.
5. according to claim 1 it is a kind of removing xylose production during glucose method, which is characterized in that the step
(3) the air gas velocity control of air stirring is (2-50) in 2-50BV per hour, i.e. the ratio between charge volume and liquid volume in: 1.
6. according to claim 1 it is a kind of removing xylose production during glucose method, which is characterized in that the step
(3) enzyme preparation is the complex enzyme that glucose oxidase and peroxidase are mixed according to weight ratio 7:3 in, and additive amount is raw material
The 1% of solid quality, the reaction time is for 24 hours.
7. according to claim 1 it is a kind of removing xylose production during glucose method, which is characterized in that the step
(4) in macromolecular ultrafiltration system be ceramic membrane, organic rolled film or hollow-fibre membrane in any one, retaining molecular weight 1,
000-150,000Da, membranous system material rejection 5-10%.
8. according to claim 1 it is a kind of removing xylose production during glucose method, which is characterized in that the step
(4) the macromolecular ultrafiltration system cycle of operation is 180 minutes in, wherein being successively up 170 minutes, pure water is just being washed 5 minutes,
Pure water backwash 5 minutes；It was successively respectively cleaned 1 hour with 0.5% sodium hydroxide of quality and 0.1% protease every 48 hours.
9. according to claim 1 it is a kind of removing xylose production during glucose method, which is characterized in that the step
(5) the chromatographic isolation resin of chromatographic separation device is any one in Hydrogen, sodium form, potassium type or calcium type resin in.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110229195A (en) * | 2019-06-14 | 2019-09-13 | 广西福仪生物技术有限公司 | A method of extracting rhamnose from bagasse |
| CN113004346A (en) * | 2021-02-07 | 2021-06-22 | 济南茂腾生物科技有限公司 | Method for preparing xylose by negative pressure coupling normal pressure crystallization |
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| CN110229195B (en) * | 2019-06-14 | 2022-11-04 | 广西福仪生物技术有限公司 | Method for extracting rhamnose from bagasse |
| CN113004346A (en) * | 2021-02-07 | 2021-06-22 | 济南茂腾生物科技有限公司 | Method for preparing xylose by negative pressure coupling normal pressure crystallization |
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