CN105039458A - Method for realizing clean separation of carbohydrate from lignin components in corncob residue - Google Patents
Method for realizing clean separation of carbohydrate from lignin components in corncob residue Download PDFInfo
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Abstract
The invention relates to a method for realizing clean separation of carbohydrate from lignin components in corncob residue. The method comprises the following steps: conducting chemical method pretreatment and mechanical method pretreatment on corncob residue respectively; conducting biological enzyme treatment; separating biological enzyme hydrolysate from residues; conducting extraction treatment; filtering; conducting rotary evaporation; filtering, washing, freeze drying, washing and vacuum-drying so as to obtain purified lignin. According to the method, effective utilization of crop wastes such as corncob residue is fully realized, not only is agricultural waste resource effectively utilized, but also pressure on environmental protection is relieved, and the method benefits the nation and the people, conforms to the strategy of sustainable development of the nation, is extremely urgent, and has important significances on national economy development, cleaning production and environmental protection of China.
Description
Technical field
The invention belongs to the technical field that biomass resource and agricultural waste material utilize, especially a kind of method realizing carbohydrate and lignin components clean separation in corn cob residue.
Background technology
The mineral fuel such as coal, oil, Sweet natural gas are the core energy of industrial society, but non-renewable and reserves are limited.Along with the develop rapidly of human social economy, energy consumption speed is aggravated, simultaneously, utilize to high strength mineral fuel that unnecessary energy and carbon element are discharged in a large number, natural energy and carbon balance are broken, cause the catastrophic effects such as depletion of the ozone layer, global warming, acid rain, cause the very big worry in the whole world.
In this context, take biomass energy as the green of representative, clean, renewable energy source becomes the focus of world attention.Biomass energy is the photosynthesis by green plants, sun power is stored in a kind of form of energy in tellurian matter with chemical energy form, being a kind of inexhaustible, nexhaustible renewable energy source, is the fourth-largest energy earth being only second to coal, oil and natural gas resource.
China is large agricultural country, the aboundresources of agricultural crop straw residuum, and wherein the annual production of corn reaches more than one hundred million ton, occupy in the world the second, account for 1/5th of Gross World Product, the crop residue such as corn cob, stalk aboundresources and cheap, but its effective rate of utilization is low.Improving comprehensive utilization scope and the utilization ratio of the residuum resources such as agricultural crop straw, not only effectively can utilize agricultural wastes resource, also can alleviate the pressure to environment protection, is benefit the nation and the people, meet National Sustainable Development Strategies and extremely urgent movement.If the carbohydrate components in corn cob residue is separated with lignin by suitable pretreatment technology; then the industrial chemicals such as carbohydrate components fermentative production of ethanol, acetone, furfural, lactic acid, L-glutamic acid are utilized further; lignin is further purified the exploitation for follow-up lignin base product simultaneously; to be conducive to the efficient of biomass resource and higher value application, this development to Chinese national economy, cleaner production and environment protection are all significant.
At present, a kind of method that can realize carbohydrate and lignin components clean separation in corn cob residue is not still had.
By retrieval, not yet find the patent publication us relevant to patent application of the present invention.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art part, a kind of method realizing carbohydrate and lignin components clean separation in corn cob residue is provided, the method can realize effective utilization of this agricultural waste material of corn cob residue, to supply raw materials basis for follow-up processing and utilization or production have high value added product.
The technical solution adopted for the present invention to solve the technical problems is:
Realize a method for carbohydrate and lignin components clean separation in corn cob residue, step is as follows:
(1) first, the corn cob residue chosen is carried out electroplating effluent recycling and or mechanical preparation respectively:
1. electroplating effluent recycling and: corn cob residuum feedstocks is placed in reactor, add the NaOH of 0.1%-5.0% (relative to raw material absolute dry mass), reaction vessel is incubated 10-60min at the temperature of 60-90 DEG C, and constantly stir in reaction process, fully react to make corn cob residuum feedstocks and liquid, after reaction terminates, filter so that pretreatment fluid is separated with solid residue, reacted corn cob solid residue is washed to neutrality, and stores after air-dry equilibrium water content for follow-up cellulase treatment;
2. mechanical preparation: corn cob residue is put into shredder and added water and grinds, ensure that grinding concentration maintains in the scope of 1%-30%, rotating speed is 300-2000rpm, milling time is 10-60min, the corn cob solid residue after grinding through collecting, after equilibrium water content for follow-up cellulase treatment;
(2) cellulase treatment: carry out cellulase treatment to pretreated corn cob solid residue, before being processed, carries out high-temperature sterilization process to container used;
(3) aseptically, acetate-sodium acetate buffer is added in pretreated corn cob solid residue, the absolute dry mass of corn cob solid residue and acetate-sodium acetate buffer volume ratio are 1:5kg:L, biological enzyme mixed solution is added after abundant stirring, then adding distilled water makes the mass concentration of corn cob residue be 1% – 10%, carry out biological enzyme constant temperature culture enzymolysis processing under aseptic condition, namely obtain the residue after enzymic hydrolysis and biological enzyme hydrolysis liquid subsequently;
Wherein, the condition of described biological enzyme constant temperature culture enzymolysis processing is: temperature of reaction 40 – 55 DEG C, reaction times 10 – 80h, rotating speed 100 – 180rpm, and biological enzyme consumption used is 10 – 70FPU/g substrates;
(4) after cellulase treatment, separating bio enzyme hydrolyzate and residue, collection of biological enzyme hydrolyzate, must comprise the saccharified liquid of carbohydrate, store for future use;
Residue is the thick lignin of enzymolysis, and thick for enzymic hydrolysis lignin being washed till pH value is after 6 – 7, air-dry, store, for subsequent use after equilibrium water content;
(5) get the thick lignin of enzymolysis, make it be dissolved in comprising concentration is in the weakly acidic dioxane-water mixed liquid of 0.01mol/LHCl, wherein the volume ratio of dioxane and water is 85:15, the mass concentration of the thick lignin of enzymolysis is 5%, at 90-100 DEG C of temperature, extracting process is carried out to the thick lignin of enzymolysis, will ensure during extracting process to reflux under the protection of nitrogen, timing from during first time backflow, extracting 2-4h, obtains mixture;
(6) after extracting process terminates, filtered by mixture, the residue mixed solution that fresh dioxane and water form washs, and washing until filtrate clarification, is collected filtrate and is used for subsequent disposal for several times;
(7) sodium bicarbonate particle being added collected filtrate carrying out neutralizes until filtrate is in neutral, then rotary evaporation devices is utilized to carry out evaporation concentration process, temperature is 30 – 35 DEG C, concentration ratio is 1:15-40, the concentrated solution of gained is dropwise added in a large amount of acid deionized waters, in the process dropwise added, keeps uniform stirring to promote stripping, the precipitation of lignin;
(8) stripping, the lignin that is precipitated out are carried out filtration treatment with isolated lignin, the solid filtering gained fully washs through acid deionized water, after washing terminates, lignin is transferred to collection, lyophilize 20-28h in container, dried lignin n-hexane is to remove other impurity component, then through continuing to carry out vacuum-drying 6-10h under 30 DEG C of conditions, the lignin after final acquisition purifying.
And described step (1) middle corn cob residue is the residuum of corn cob raw material after acidic process extracts the wood sugar in corn cob.
And main ingredient and the mass percent of described corn cob residue are as follows: dextran 63.68%, xylan 4.17%, Klason lignin 17.03%, ethanol extractum 10.64%, ash content 2.93%.
And, described step (2) in the condition of high-temperature sterilization process be 121 DEG C of sterilizing 60min.
And, described step (3) in the pH of acetate-sodium acetate buffer be 4.5 – 5.0, its compound method is: take sodium acetate, adding distil water dissolves, add glacial acetic acid again, it is 0.5mol/L that adding distil water is diluted to sodium acetate concentration, and the volumetric concentration of glacial acetic acid is 2.5%, and adjust ph to 4.5 – 5.0.
And described step (3) middle biological enzyme is complex cellulase.
And, described step (4) in utilize strainer to realize being separated of biological enzyme hydrolysis liquid and residue.
And, described step (6) in the volume ratio of dioxane and water be 85:15.
And described step (7) middle stirring velocity is 50-200rpm; Or, described step (7) in the concentration ratio of evaporation concentration process be 1:20.
And, described step (8) in the pH=2.0 of acid deionized water.
The advantage that the present invention obtains and beneficial effect are:
1, the inventive method adequately achieves effective utilization of this agricultural waste material of corn cob residue; not only can effectively utilize agricultural wastes resource; also mitigate the pressure to environment protection; benefit the nation and the people, meet National Sustainable Development Strategies and extremely urgent method, all significant to the development of Chinese national economy, cleaner production and environment protection.
2, the inventive method realizes the clean separation of its Main chemical component (carbohydrate components and lignin) by chemical Treatment, mechanical process process and cellulase treatment, corn cob residue is after cellulase treatment, the inversion rate of glucose of substrate can reach 97%, lignin yield after the final separation and purification of the method can up to 27%, to supply raw materials basis for follow-up processing and utilization or production have high value added product, the method cleans, and simple, convenient, cost is reasonable.
Accompanying drawing explanation
Fig. 1 is that the present invention realizes carbohydrate and lignin in corn cob residue and cleans the process flow sheet be effectively separated.
Embodiment
Below in conjunction with embodiment, the present invention is further described; Following embodiment is illustrative, is not determinate, can not limit protection scope of the present invention with following embodiment.
The raw material used in the present invention, if no special instructions, is conventional commercially available prod; The method used in the present invention, if no special instructions, is the ordinary method of this area.
The pH of the acetate-sodium acetate buffer used in the present invention is 4.5 – 5.0, and its compound method is: take sodium acetate (CH
3cOONa3H
2o), adding distil water dissolves, then adds glacial acetic acid, and it is 0.5mol/L that adding distil water is diluted to sodium acetate concentration, and the volumetric concentration of glacial acetic acid is 2.5%, and adjust ph to 4.5 – 5.0.
Embodiment 1
Realize a method for carbohydrate and lignin components clean separation in corn cob residue, step is as follows:
(1) first, corn cob residue after screening is added in the solution (NaOH solution) of 0.5% alkali dense (relative to over dry corn cob mass of residue), and at 80 DEG C, reaction 30min, and constantly stir in reaction process, fully react to make corn cob residuum feedstocks and liquid, after reaction terminates, solid-liquid is carried out suction filtration separation, collect black liquor, continue residue to be washed till neutrality after collecting black liquor, then put into room-dry and equilibrium water content, collect and for follow-up biological enzyme hydrolysis;
(2) enzymic hydrolysis is carried out to the corn cob solid residue after alkaline purification.Before carrying out enzymic hydrolysis, instrument is all through high-temperature sterilization process (121 DEG C, 60min);
(3) in enzymatic hydrolysis reaction device, pretreated corn cob solid residue is added, add acetic acid-sodium acetate (pH ≈ 4.8) damping fluid, the absolute dry mass (kg) of corn cob residue and the ratio of acetic acid-sodium acetate buffer volume (L) are 1:5, and constantly stirring makes corn cob residue disperse fully, add the cellulase of 44FPU/g substrate again, then adding distilled water makes the ultimate density of corn cob residue be 10%, sealing is placed in 50 DEG C of constant temperature culture oscillators reacts 76h, and rotating speed is 180rpm;
(4) carry out filtering separation to hydrolytic residue and hydrolyzed solution after enzymic hydrolysis, collect enzyme hydrolyzate, hydrolyzed solution is saccharified liquid, containing carbohydrates such as glucose, wood sugar and pectinoses, stores for future use;
Hydrolytic residue is exactly the thick lignin of enzymic hydrolysis, and thick for enzymic hydrolysis lignin is washed till neutrality, air-dry for subsequent use;
(5) the thick lignin of appropriate enzymolysis is got, make it be dissolved into comprising concentration is in the weakly acidic dioxane-water mixed liquid of 0.01mol/LHCl, the ratio of dioxane and water is 85:15, and the mass concentration of the thick lignin of enzymolysis is 5%, at 95 DEG C, carry out extracting, because dioxane boiling point is 86 DEG C, therefore, this reaction will reflux under the protection of nitrogen, timing from during first time backflow, extracting 2h, obtains mixture;
(6), after reaction terminates, filtered by mixed solution, the fresh dioxane-water mixed liquid (dioxane: the volume ratio of water is 85:15) of solid washs, and is washed till filtrate clarification.Filtrate is neutralized to neutrality with sodium bicarbonate, and at the temperature of 30 DEG C, carry out rotary evaporation with rotatory evaporator concentrate, concentration ratio is 1:20;
(7) after concentrated end, concentrated solution is added in a large amount of acid deionized waters (pH=2.0), and constantly stir, make lignin stripping, stripping, the lignin that is precipitated out are carried out filtration treatment with isolated lignin, the solid filtering gained fully washs through acid deionized water, after washing terminates, lignin is transferred to collection, lyophilize 28h in container, dried enzymolysis lignin n-hexane is to remove other impurity component, then continue to carry out vacuum-drying 6h under 30 DEG C of conditions, the lignin after final acquisition purifying.
Detected result:
Under above-mentioned processing condition: after hydrolysis 10h, in enzyme hydrolyzate, the concentration of glucose is 25500mg/L, and the inversion rate of glucose of substrate is 37%; After hydrolysis 76h, in hydrolyzed solution, the concentration of glucose is 45100mg/L, and the inversion rate of glucose of substrate is 66%, and the yield of final purifying lignin is 20%.
Embodiment 2
Realize a method for carbohydrate and lignin components clean separation in corn cob residue, step is as follows:
(1) first, take corn cob residuum feedstocks, put into shredder and the grinding that adds water, grinding concentration is 10%, and rotating speed is 1000rpm, and milling time is 30min; Corn cob residue after grinding through collecting, after equilibrium water content for follow-up cellulase treatment;
(2) enzymic hydrolysis is carried out to through grinding pretreated raw material.Before carrying out enzymic hydrolysis, instrument is all through high-temperature sterilization process (121 DEG C, 60min);
(3) the corn cob residue after adding grinding in enzymatic hydrolysis reaction device, add acetic acid-sodium acetate (pH ≈ 4.8) damping fluid, the absolute dry mass (kg) of corn cob residuum feedstocks and the ratio of acetic acid-sodium acetate buffer volume (L) are 1:5, add the cellulase of 10FPU/g substrate again, then adding distilled water makes the mass concentration of corn cob residue be 10%, after sealing, reactor is placed in constant temperature culture oscillator and reacts 76h, at 45 DEG C of temperature, react rotating speed is 140rpm;
(4) utilize strainer to realize carrying out filtering separation to hydrolytic residue and hydrolyzed solution after enzymic hydrolysis, collect enzyme hydrolyzate, hydrolyzed solution is saccharified liquid, containing carbohydrates such as glucose, wood sugar and pectinoses, stores for future use; Hydrolytic residue is exactly the thick lignin of enzymic hydrolysis, and thick lignin is washed till neutrality, air-dry for subsequent use;
(5) the thick lignin of appropriate over dry enzymolysis is got, its concentration being dissolved in HCl is made to be in the weakly acidic dioxane-water mixed liquid of 0.01mol/L, the ratio of dioxane and water is 85:15, and the concentration of the thick lignin of enzymolysis is 5%, and at 90 DEG C, carries out extracting with extractor, because dioxane boiling point is 86 DEG C, therefore, this reaction will reflux under the protection of nitrogen, timing from during first time backflow, extracting 3h, obtains mixture;
(6), after reaction terminates, filtered by mixed solution, the fresh dioxane-water mixed liquid (dioxane: the volume ratio of water is 85:15) of solid washs, and is washed till filtrate clarification.Filtrate is neutralized to neutrality with sodium bicarbonate, and at the temperature of 30 DEG C, carry out rotary evaporation with rotatory evaporator concentrate, concentration ratio is 1:40;
(7) after concentrated end, concentrated solution is added in a large amount of acid deionized waters (pH=2.0), and constantly stir, make lignin stripping, stripping, the lignin that is precipitated out are carried out filtration treatment with isolated lignin, the solid filtering gained fully washs through acid deionized water, after washing terminates, lignin is transferred to collection, lyophilize 24h in container, dried enzymolysis lignin n-hexane is to remove other impurity component, then through continuing to carry out vacuum-drying 10h under 30 DEG C of conditions, the lignin after final acquisition purifying.
Detected result:
Under above-mentioned processing condition: after hydrolysis 8h, in enzyme hydrolyzate, the concentration of glucose is 26250mg/L, and the inversion rate of glucose of substrate is 41%; After hydrolysis 76h, in hydrolyzed solution, the concentration of glucose is 61800mg/L, and the inversion rate of glucose of substrate is 97%, and purifying lignin yield is 27%.
Embodiment 3
Realize a method for carbohydrate and lignin components clean separation in corn cob residue, step is as follows:
(1) first, take appropriate corn cob residuum feedstocks, put into shredder and the grinding that adds water, grinding concentration is 30%, and rotating speed is 300rpm, and milling time is 10min.Then the corn cob residue after milled processed is collected, equilibrium water content is for follow-up cellulase treatment;
(2) enzymic hydrolysis is carried out to through grinding pretreated raw material.Before carrying out enzymic hydrolysis, instrument is all through high-temperature sterilization process (121 DEG C, 60min);
(3) the corn cob residue after adding grinding in enzymatic hydrolysis reaction device, add acetic acid-sodium acetate (pH ≈ 4.8) damping fluid, the absolute dry mass (kg) of corn cob residuum feedstocks and the ratio of acetic acid-sodium acetate buffer volume (L) are 1:5, add the cellulase of 44FPU/g substrate again, then distilled water is added, the mass concentration of corn cob residue is made to be 8%, after sealing, reactor is placed in constant temperature culture oscillator, at 60 DEG C, react 80h, rotating speed is 180rpm;
(4) carry out filtering separation to hydrolytic residue and hydrolyzed solution after enzymic hydrolysis, collect enzyme hydrolyzate, hydrolyzed solution is saccharified liquid, containing carbohydrates such as glucose, wood sugar and pectinoses, stores for future use;
Hydrolytic residue is exactly the thick lignin of enzymic hydrolysis, and thick lignin is washed till neutrality, air-dry for subsequent use;
(5) the thick lignin of a certain amount of over dry enzymolysis is got, its concentration being dissolved in HCl is made to be in the weakly acidic dioxane-water mixed liquid of 0.01mol/L, the ratio of dioxane and water is 85:15, and the concentration of the thick lignin of enzymolysis is 5%, at 100 DEG C, carry out extracting, because dioxane boiling point is 86 DEG C, therefore, this reaction will reflux under the protection of nitrogen, timing from during first time backflow, extracting 4h, obtains mixture;
(6), after reaction terminates, filtered by mixed solution, the fresh dioxane-water mixed liquid (dioxane: water=85:15) of solid washs, and is washed till filtrate clarification.Filtrate is neutralized to neutrality with sodium bicarbonate, and liquid carries out rotary evaporation with rotatory evaporator and concentrates at the temperature of 30 DEG C, and concentration ratio is 1:15;
(7) after concentrated end, concentrated solution is added in a large amount of acid deionized waters (pH=2.0), and constantly stir, make lignin stripping, stripping, the lignin that is precipitated out are carried out filtration treatment with isolated lignin, the solid filtering gained fully washs through acid deionized water, after washing terminates, lignin is transferred to collection, lyophilize 24h in container, dried enzymolysis lignin n-hexane is to remove other impurity component, then through continuing to carry out vacuum-drying 8h under 30 DEG C of conditions, the lignin after final acquisition purifying.
Detected result:
Under above-mentioned processing condition: after hydrolysis 10h, in enzyme hydrolyzate, the concentration of glucose is 31500mg/L, and the inversion rate of glucose of substrate is 50%; After hydrolysis 76h, in hydrolyzed solution, the concentration of glucose is 58100mg/L, and the inversion rate of glucose of substrate is 92%, and purifying lignin yield is 19%.
Claims (10)
1. realize a method for carbohydrate and lignin components clean separation in corn cob residue, it is characterized in that: step is as follows:
(1) first, the corn cob residue chosen is carried out electroplating effluent recycling and or mechanical preparation respectively:
1. electroplating effluent recycling and: corn cob residuum feedstocks is placed in reactor, add the NaOH of 0.1%-5.0% (relative to raw material absolute dry mass), reaction vessel is incubated 10-60min at the temperature of 60-90 DEG C, and constantly stir in reaction process, fully react to make corn cob residuum feedstocks and liquid, after reaction terminates, filter so that pretreatment fluid is separated with solid residue, reacted corn cob solid residue is washed to neutrality, and stores after air-dry equilibrium water content for follow-up cellulase treatment;
2. mechanical preparation: corn cob residue is put into shredder and added water and grinds, ensure that grinding concentration maintains in the scope of 1%-30%, rotating speed is 300-2000rpm, milling time is 10-60min, the corn cob solid residue after grinding through collecting, after equilibrium water content for follow-up cellulase treatment;
(2) cellulase treatment: carry out cellulase treatment to pretreated corn cob solid residue, before being processed, carries out high-temperature sterilization process to container used;
(3) aseptically, acetate-sodium acetate buffer is added in pretreated corn cob solid residue, the absolute dry mass of corn cob solid residue and acetate-sodium acetate buffer volume ratio are 1:5kg:L, biological enzyme mixed solution is added after abundant stirring, then adding distilled water makes the mass concentration of corn cob residue be 1% – 10%, carry out biological enzyme constant temperature culture enzymolysis processing under aseptic condition, namely obtain the residue after enzymic hydrolysis and biological enzyme hydrolysis liquid subsequently;
Wherein, the condition of described biological enzyme constant temperature culture enzymolysis processing is: temperature of reaction 40 – 55 DEG C, reaction times 10 – 80h, rotating speed 100 – 180rpm, and biological enzyme consumption used is 10 – 70FPU/g substrates;
(4) after cellulase treatment, separating bio enzyme hydrolyzate and residue, collection of biological enzyme hydrolyzate, must comprise the saccharified liquid of carbohydrate, store for future use;
Residue is the thick lignin of enzymolysis, and thick for enzymic hydrolysis lignin being washed till pH value is after 6 – 7, air-dry, store, for subsequent use after equilibrium water content;
(5) get the thick lignin of enzymolysis, make it be dissolved in comprising concentration is in the weakly acidic dioxane-water mixed liquid of 0.01mol/LHCl, wherein the volume ratio of dioxane and water is 85:15, the mass concentration of the thick lignin of enzymolysis is 5%, at 90-100 DEG C of temperature, extracting process is carried out to the thick lignin of enzymolysis, will ensure during extracting process to reflux under the protection of nitrogen, timing from during first time backflow, extracting 2-4h, obtains mixture;
(6) after extracting process terminates, filtered by mixture, the residue mixed solution that fresh dioxane and water form washs, and washing until filtrate clarification, is collected filtrate and is used for subsequent disposal for several times;
(7) sodium bicarbonate particle being added collected filtrate carrying out neutralizes until filtrate is in neutral, then rotary evaporation devices is utilized to carry out evaporation concentration process, temperature is 30 – 35 DEG C, concentration ratio is 1:15-40, the concentrated solution of gained is dropwise added in a large amount of acid deionized waters, in the process dropwise added, keeps uniform stirring to promote stripping, the precipitation of lignin;
(8) stripping, the lignin that is precipitated out are carried out filtration treatment with isolated lignin, the solid filtering gained fully washs through acid deionized water, after washing terminates, lignin is transferred to collection, lyophilize 20-28h in container, dried lignin n-hexane is to remove other impurity component, then through continuing to carry out vacuum-drying 6-10h under 30 DEG C of conditions, the lignin after final acquisition purifying.
2. the method realizing carbohydrate and lignin components clean separation in corn cob residue according to claim 1, is characterized in that: described step (1) middle corn cob residue is the residuum of corn cob raw material after acidic process extracts the wood sugar in corn cob.
3. the method realizing carbohydrate and lignin components clean separation in corn cob residue according to claim 2, it is characterized in that: main ingredient and the mass percent of described corn cob residue are as follows: dextran 63.68%, xylan 4.17%, Klason lignin 17.03%, ethanol extractum 10.64%, ash content 2.93%.
4. the method realizing carbohydrate and lignin components clean separation in corn cob residue according to claim 1, is characterized in that: described step (2) in the condition of high-temperature sterilization process be 121 DEG C of sterilizing 60min.
5. the method realizing carbohydrate and lignin components clean separation in corn cob residue according to claim 1, it is characterized in that: described step (3) in the pH of acetate-sodium acetate buffer be 4.5 – 5.0, its compound method is: take sodium acetate, adding distil water dissolves, add glacial acetic acid again, it is 0.5mol/L that adding distil water is diluted to sodium acetate concentration, and the volumetric concentration of glacial acetic acid is 2.5%, and adjust ph to 4.5 – 5.0.
6. the method realizing carbohydrate and lignin components clean separation in corn cob residue according to claim 1, is characterized in that: described step (3) middle biological enzyme is complex cellulase.
7. the method realizing carbohydrate and lignin components clean separation in corn cob residue according to claim 1, is characterized in that: described step (4) in utilize strainer to realize being separated of biological enzyme hydrolysis liquid and residue.
8. the method realizing carbohydrate and lignin components clean separation in corn cob residue according to claim 1, is characterized in that: described step (6) in the volume ratio of dioxane and water be 85:15.
9. the method realizing carbohydrate and lignin components clean separation in corn cob residue according to claim 1, is characterized in that: described step (7) middle stirring velocity is 50-200rpm; Or, described step (7) in the concentration ratio of evaporation concentration process be 1:20.
10. the method realizing carbohydrate and lignin components clean separation in corn cob residue according to claim 1, is characterized in that: described step (8) in the pH=2.0 of acid deionized water.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105695536A (en) * | 2016-04-07 | 2016-06-22 | 天津科技大学 | Pretreatment method of capable of implementing high-efficiency enzymolysis and saccharification on deciduous wood crotches |
| CN107523596A (en) * | 2017-09-11 | 2017-12-29 | 天津科技大学 | A kind of efficient enzyme hydrolysis of achievable biomass material and the method for preparing fermentable sugars |
| CN107893093A (en) * | 2017-12-12 | 2018-04-10 | 天津科技大学 | It is a kind of to strengthen corncob and the preprocess method of the efficient enzyme hydrolysis of corncob residue |
| CN108179644A (en) * | 2017-12-21 | 2018-06-19 | 中国科学院青岛生物能源与过程研究所 | A kind of method that lignin is extracted from biomass |
| CN108179159A (en) * | 2017-12-12 | 2018-06-19 | 天津科技大学 | A kind of method of the efficient enzyme hydrolysis production fermentable sugars of achievable corncob residue |
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| CN116083657A (en) * | 2022-12-05 | 2023-05-09 | 浙江华康药业股份有限公司 | System and method for co-producing high-grade xylose and high-end caramel pigment by utilizing corncob |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102153763A (en) * | 2010-09-27 | 2011-08-17 | 天津大学 | Lignocellulose acid/alkali coupling pretreatment method |
| CN102382310A (en) * | 2011-08-31 | 2012-03-21 | 广州优锐生物科技有限公司 | Lignin co-production method by comprehensively utilizing lignocellulose resources |
| CN102433358A (en) * | 2011-10-20 | 2012-05-02 | 清华大学 | Method for coproduction of xylose, lignin and ethanol from corncobs |
| CN103881115A (en) * | 2014-02-24 | 2014-06-25 | 广东中烟工业有限责任公司 | Method of extracting tobacco leaf lignin by enhanced enzymolysis process |
| CN104016948A (en) * | 2014-05-29 | 2014-09-03 | 陕西科技大学 | Method for preparing 2, 3-dihydro benzofuran by lignin low temperature pyrolysis |
-
2015
- 2015-07-28 CN CN201510451928.6A patent/CN105039458A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102153763A (en) * | 2010-09-27 | 2011-08-17 | 天津大学 | Lignocellulose acid/alkali coupling pretreatment method |
| CN102382310A (en) * | 2011-08-31 | 2012-03-21 | 广州优锐生物科技有限公司 | Lignin co-production method by comprehensively utilizing lignocellulose resources |
| CN102433358A (en) * | 2011-10-20 | 2012-05-02 | 清华大学 | Method for coproduction of xylose, lignin and ethanol from corncobs |
| CN103881115A (en) * | 2014-02-24 | 2014-06-25 | 广东中烟工业有限责任公司 | Method of extracting tobacco leaf lignin by enhanced enzymolysis process |
| CN104016948A (en) * | 2014-05-29 | 2014-09-03 | 陕西科技大学 | Method for preparing 2, 3-dihydro benzofuran by lignin low temperature pyrolysis |
Non-Patent Citations (3)
| Title |
|---|
| 刘江燕: "木质素及其模型物在不同热化学环境下的解构", 《中国博士学位论文全文数据库（电子期刊）工程科技I辑》 * |
| 崔艳: "玉米芯废渣中纤维糖及木质素的联产工艺研究", 《中国优秀硕士学位论文全文数据库（电子期刊）工程科技I辑》 * |
| 贾玲: "玉米芯木质纤维素组分分离研究", 《中国优秀硕士学位论文全文数据库（电子期刊）工程科技I辑》 * |
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|---|---|---|---|---|
| CN105695536A (en) * | 2016-04-07 | 2016-06-22 | 天津科技大学 | Pretreatment method of capable of implementing high-efficiency enzymolysis and saccharification on deciduous wood crotches |
| CN105695536B (en) * | 2016-04-07 | 2020-04-14 | 天津科技大学 | Pretreatment method capable of realizing efficient enzymatic saccharification of broadleaf wood brushwood |
| CN107523596A (en) * | 2017-09-11 | 2017-12-29 | 天津科技大学 | A kind of efficient enzyme hydrolysis of achievable biomass material and the method for preparing fermentable sugars |
| CN107893093A (en) * | 2017-12-12 | 2018-04-10 | 天津科技大学 | It is a kind of to strengthen corncob and the preprocess method of the efficient enzyme hydrolysis of corncob residue |
| CN108179159A (en) * | 2017-12-12 | 2018-06-19 | 天津科技大学 | A kind of method of the efficient enzyme hydrolysis production fermentable sugars of achievable corncob residue |
| CN108179644A (en) * | 2017-12-21 | 2018-06-19 | 中国科学院青岛生物能源与过程研究所 | A kind of method that lignin is extracted from biomass |
| CN108179644B (en) * | 2017-12-21 | 2019-11-12 | 中国科学院青岛生物能源与过程研究所 | A method of extracting lignin from biomass |
| CN111494434A (en) * | 2020-04-27 | 2020-08-07 | 南京素汇保健食品有限公司 | Application of nano-dispersion rapid fermentation method in plants |
| CN116083657A (en) * | 2022-12-05 | 2023-05-09 | 浙江华康药业股份有限公司 | System and method for co-producing high-grade xylose and high-end caramel pigment by utilizing corncob |
| WO2024119730A1 (en) * | 2022-12-05 | 2024-06-13 | 浙江华康药业股份有限公司 | System and method for co-production of premium-grade xylose and high-end caramel pigment using corncobs |
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