CN103045680B - Comprehensive utilization method of lignocellulose biomass - Google Patents
Comprehensive utilization method of lignocellulose biomass Download PDFInfo
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Abstract
A comprehensive utilization method of lignocellulose biomass comprises the following steps of: (a) alkaline hydrolysis processing: (i) processing the lignocellulose biomass by an alkaline solution to dissolve the lignin in the alkaline solution; (ii) then performing filtration and washing to obtain alkaline hydrolysis residues and liquid; (iii) separating the obtained liquid by a membrane device, and concentrating to obtain an alkaline lignin solution; (b) acid hydrolysis: performing acid hydrolysis of the alkaline hydrolysis residues, separating to obtain a pentose solution and acid hydrolysis residues; (c) cellulose enzymatic hydrolysis: performing enzymatic hydrolysis of the acid hydrolysis residues by using cellulase produced by a penicillium (Penicillium decumbens PD-G3-08), and then performing fermentation to produce ethanol. The method realizes the maximum resource utilization of lignocellulose biomass.
Description
Technical field
The present invention relates to a kind of method that fully utilizes lignocellulose biomass, specifically a kind of method that fully utilizes Mierocrystalline cellulose in lignocellulose biomass, hemicellulose and xylogen.
Background technology
Day by day serious along with the increasingly exhausted and environmental pollution of fossil fuel resource, utilizes the substitute that the renewable energy resources are petroleum chemicals to become further important.And alcohol fuel is the principal mode of the material of biomass liquid energy, it is also the most probable substitute of fossil oil.At present, world's alcohol production is mainly usingd starch based (corn, cassava etc.) and carbohydrate (sugarcane, the beet etc.) raw material as fermentation.Adopt microbial method method fermentative production of ethanol technology maturation, but high raw materials cost is restricted the industrial application of grain fermentative production of ethanol, exist simultaneously with people strive grain and grain strive etc. drawback, and cause provision price Continued, so it is imperative to find new raw material.Present scientist is more cheap sight trend of purchasing cost, the lignocellulose biomass widely of originating.
Lignocellulose biomass exists with the form of plant materials, main component is Mierocrystalline cellulose, hemicellulose and xylogen, wherein, Mierocrystalline cellulose accounts for 40% left and right, hemicellulose accounts for 25% left and right, xylogen accounts for 20% left and right, and the lignocellulose biomass total amount being generated by photosynthesis every year on the earth surpasses 2,000 hundred million tons, so Wooden Biomass is renewable resources abundant, the most cheap on the earth.
If can take lignocellulose biomass as raw material production ethanol, will greatly solve the mankind's energy problem, but still exist in this respect a lot of technical barriers not yet to solve.At present, take lignocellulose biomass in the process of raw material production ethanol, and the problem that runs into is that the extraction yield of cellulase hydrolysis is low, causes the high cost (accounting for the 40-50% of total cost of production) of enzymolysis, production cost is too high, cannot really realize industrialization.The low reason of extraction yield of cellulase hydrolysis is: hemicellulose is combined between Mierocrystalline cellulose and xylogen as molecule tamanori on the one hand, and the reticulated structure that xylogen has, as support frame, surround and add set Mierocrystalline cellulose and hemicellulose, xylogen and hemicellulose spatially can hinder contacting of cellulosic molecule and enzyme, enzyme accessibility is poor, has increased the difficulty of enzymolysis.Therefore be necessary lignocellulose biomass to carry out effective pre-treatment, destroy the spatial obstacle of xylogen and hemicellulose, also to avoid pre-treatment to produce simultaneously and be unfavorable for the enzyme inhibitor (as furfural, acetic acid etc.) of enzymolysis, thereby be conducive to cellulosic enzymolysis; On the other hand, in cellulosic molecule, with the intermolecular hydrogen bond that exists, aggregated structure complexity and degree of crystallinity are high, cellulase is low to crystalline cellulose enzymatic reaction vigour, therefore,, in order to improve the extraction yield of cellulase hydrolysis, need to adopt better pretreatment process or improve enzyme activity.
Take lignocellulose biomass in raw material production ethanol process, another problem running into is that hemicellulose, Mierocrystalline cellulose and xylogen are failed well to fully utilize, process in the prior art the technique of biomass, mainly with degraded carbohydrate, obtaining alcoholic product is greatly object, high purity and the high reactivity that can not take into account xylogen extract and later use, often, using xylogen as a removal object, cause the wasting of resources and environmental pollution, fail to reach resource maximum using.
In prior art, publication number is in the patent documentation of CN101696427A, to disclose a kind ofly with fibrous matter, to produce alcohol fuel and 2, the method of 3-butyleneglycol, by alkaline process pre-treatment, hemicellulose enzymolysis technique, more than 45% hemicellulose is changed into hypotoxic Xylose, obtained the Mierocrystalline cellulose residue of high cellulose content simultaneously.Hemicellulose hydrolysate wherein obtains 2 through fermentation, 3-butyleneglycol, Mierocrystalline cellulose residue obtains alcohol fuel through fermentation, Mierocrystalline cellulose and hemicellulose finally change into Industrial products utilized, but the object of this technique is Mierocrystalline cellulose wherein and hemicellulose to change into alcohol fuel and 2, 3-butyleneglycol, the pretreated object of alkaline process is to remove to greatest extent xylogen, using xylogen as removing thing, do not consider the quality problems such as purity of gained xylogen and the later use of xylogen, higher with alkali concn, to the activity of xylogen, destroy larger, so the separation of the method to three kinds of materials, the extraction effect of having ignored xylogen, only Mierocrystalline cellulose and hemicellulose have been carried out to effective industrial utilization, can not guarantee that xylogen can carry out effective industrial utilization.
Publication number be the Chinese patent literature of CN101725068A disclose a kind of for fractional separation the method and apparatus based on lignocellulose biomass, provide based on lignocellulose biomass, add can dissolved lignin the first solvent be that basic solvent is from described biomass extraction xylogen, adding second solvent that can dissolve hemicellulose is acid solvent extraction wood sugar again, and then extraction remains in the Mierocrystalline cellulose in biomass; Xylogen, Mierocrystalline cellulose, hemicellulose can both be separated, but while using dilute acid pretreatment in this technique, hemicellulose is not degraded to pentose, but exist with the form of oligopolymer; While using high concentrated acid, although the rate of recovery of pentose is high, the amount that generates furfural is relatively also high, and therefore, operating process is harsher to the requirement of potential of hydrogen.In the process of separating lignin, concentration of lye used is higher simultaneously, and larger to the activity destruction of xylogen, the xylogen of separating can only be used as the fuel of steam boiler or boiler of power plant, or is used as phenol chemical by degradation treatment, and value added is low.
Summary of the invention
For this reason, technical problem to be solved by this invention is to overcome Mierocrystalline cellulose in prior art, hemicellulose and xylogen to fail to be fully utilized, and the low problem of the extraction yield of cellulase hydrolysis, thereby a kind of method of comprehensive utilization of lignocellulose biomass has been proposed.
For achieving the above object, the invention provides a kind of method of comprehensive utilization of lignocellulose biomass, it is characterized in that comprising the following steps:
(a) alkaline hydrolysis is processed
(i) using alkaline solution to process described lignocellulose biomass makes lignin dissolution wherein in alkaline solution;
(ii) then filter, wash and obtain alkaline hydrolysis residue and liquid;
(iii) by separated, the concentrated alkali lignin solution that obtains of gained liquid process film device;
(b) acid hydrolysis
Described alkaline hydrolysis residue is carried out to acid hydrolysis, after separation, obtain pentose solution and acid hydrolysis residue;
(c) cellulase hydrolysis
Use cellulase to carry out enzymolysis to described acid hydrolysis residue, obtain the solution that main component is glucose.
There is no particular limitation for the kind of described acid solution, can be that lignocellulose biomass carries out the acid-hydrolyzed conventional acid of using, and for example acid can be one or more in sulfuric acid, hydrochloric acid, nitric acid and phosphoric acid.
Described acid-hydrolyzed temperature is 100-150 ℃, time is 0.5-3 hour, while carrying out described acid hydrolysis, the concentration of acid solution is that (as the acid of selecting is strong acid to 0.5-30 % by weight, the concentration of acid solution is lower, is about 0.5-5 % by weight, as the acid of selecting is weak acid, the concentration of acid solution is higher, is about 5-30 % by weight).
Described acid solution is phosphoric acid solution, and the concentration of phosphoric acid solution is 1-20 % by weight.
Described lignocellulose biomass can be one or more of maize straw, wheat straw, rice straw, bagasse, cotton bavin, cotton seed hull, corn cob, straw, kaoliang stalk, broad-leaved wood and wood chip.
According to raw material condition, carry out pre-treatment, lignocellulose biomass raw material is cut or pulverized, then this stalk section is carried out to scrubbing dust collection.
In described step (iii), also comprise the described concentrated alkali lignin solution obtaining dilute with water again, and then concentrated step.
In described step (iii), be also included in the concentrated step that obtains described alkali lignin solution afterwards or recycle alkaline solution wherein simultaneously.
Described step (iii) also comprises the alkali lignin solution process neutralization obtaining, filters and be dried, and obtains alkali lignin solid.
At alkaline hydrolysis described in institute's step (i), at 40-100 ℃, carry out.
In alkaline hydrolysis step described in institute's step (i), liquid-solid volume ratio is 5: 1-20: 1.
In alkaline hydrolysis step described in institute's step (i), the concentration of alkaline solution is 5-8 % by weight.
The time of processing at alkaline solution described in institute's step (i) is 1-6 hour.
Various alkali may be used to the present invention, includes but not limited to aqueous sodium hydroxide solution, potassium hydroxide aqueous solution, ammoniacal liquor etc.But, according to some preferred embodiment, the aqueous solution that alkaline solution is sodium hydroxide.
Described cellulase is for being cultivated the cellulase obtaining by a penicillium, this Penicillium notatum Classification And Nomenclature is PenicilliumdecumbensPD-G3-08, be preserved in Wuhan University's Chinese Typical Representative culture collection center, its deposit number is CCTCCM2011195, and preservation date is on June 13rd, 2011.
The condition of described cellulase hydrolysis is: substrate consumption is 80-150g/L, and the addition of cellulase is 10-15FPU/g Mierocrystalline cellulose, and temperature is that 45-55 ℃, pH are that 4-6, mixing speed are 50-200rpm, and enzymolysis transformation time is 2-7 days.
After cellulase hydrolysis saccharification, fermentation can adopt the method for well known to a person skilled in the art, fermentative production of ethanol.
Technique scheme of the present invention compared with prior art has the following advantages:
1, the present invention has adopted first alkaline hydrolysis, and the operational path of cellulase hydrolysis is finally carried out in acid hydrolysis, wherein, adopt alkaline hydrolysis treatment of lignocellulosic biomass, the liquid obtaining carries out membrane sepn, concentrated, improve the purity of alkali lignin, be conducive to use xylogen to produce high value-added product.
In the present invention, the cellulase that enzymolysis adopts Penicillium notatum (PenicilliumdecumbensPD-G3-08) to produce, this cellulase has higher vigor, has improved the extraction yield of cellulase hydrolysis.
As can be seen here, by aforesaid method of the present invention, improved on the one hand cellulosic extraction yield, on the other hand because the xylogen purity of extracting is higher, can be directly as producing other Industrial products as the raw material of resol.Therefore, the inventive method has solved the problem of complex utilization of lignocellulose biomass in prior art, makes the utilization of resources reach maximization.
2, the present invention adopts the dilution of alkali lignin solution with water, again concentrated, has further reduced the ash content in alkali lignin solution, and residual alkali content, has improved solid content, is more conducive to use it to produce high value-added product.
3, the present invention adopt concentrated obtain described alkali lignin solution after or recycling alkaline solution wherein simultaneously, spent caustic solution has obtained recycling, does not pollute the environment.
4, owing to adopting alkaline solution extraction to xylogen in the lower realization of lower temperature (40-100 ℃), reduced the destruction to xylogen.
5, the present invention adopts liquid-solid volume ratio in alkaline solution to be relatively applicable to extracting xylogen, avoided that liquid-solid ratio is too little is unfavorable for that liquid-solid mixing is also unfavorable for the alkaline hydrolysis of xylogen, it is large that the too large follow-up alkali of liquid-solid ratio reclaims load, and the wastewater flow rate of generation is also large, uneconomic problem.
6, the present invention adopts alkaline hydrolysis treatment of lignocellulosic biomass, the liquid-solid ratio, alkali consumption, the temperature and time that adopt due to the condition of alkaline hydrolysis, reduced the destruction of alkaline hydrolysis process to xylogen activity, applicant finds amazedly, and the xylogen finally obtaining is particularly suitable for producing modified phenolic resins.
7, in the present invention under the temperature of described acid hydrolytic reaction, time and concentration, can be by hydrolysis of hemicellulose more thorough, can stop again high temperature under acidic conditions, the reaction times is long and excessive concentration to cellulosic destruction.
8, acid hydrolysis of the present invention acid used is phosphoric acid solution, and the concentration of phosphoric acid solution is 1-20 % by weight, uses the above-mentioned acid solution can considerable damage Mierocrystalline cellulose, and due to phosphoric acid corrosion a little less than, therefore, maintenance of the equipment is simple, duration of service is long.
What 9, the present invention was used cultivates by Penicillium notatum the cellulase obtaining, at substrate consumption, be 80-150g/L, the addition of cellulase is 10-15FPU/g Mierocrystalline cellulose, temperature is that 45-55 ℃, pH are that 4-6, mixing speed are 50-200rpm, under the enzymolysis conversion condition of 2-7 days, enzymolysis transformation efficiency is the highest.
Accompanying drawing explanation
For content of the present invention is more likely to be clearly understood, below according to a particular embodiment of the invention and by reference to the accompanying drawings, the present invention is further detailed explanation, wherein
Fig. 1 is the schematic diagram of technical process of the present invention;
Fig. 2 is the schematic flow sheet that alkaline solution of the present invention extracts alkali lignin.
Embodiment
Below will by specific embodiment, the invention will be further described.
(1) the self-control cellulase that following examples are used is cultivated and is obtained by Penicillium notatum, and concrete cultural method is:
(A) bacterial classification multiplication culture
By naming number, being PenicilliumdecumbensPD-G3-08 Penicillium notatum seed liquor is linked in the fermentor tank that contains seed culture medium through 121 ℃ of sterilizing 30min and activates with the inoculum size of 5% (v/v), keep tank pressure 0.02-0.05MPa, air flow 0.5vvm, mixing speed 100-150rpm, 30 ℃ of cultivation 30-60 hour, the seed liquor after being activated.
Component in described seed culture medium and consumption are: get embodiment 1 acid hydrolysis residue 10-30g/L, wheat bran 20-50g/L, peptone 1-4g/L, ammonium sulfate 2-4g/L, all the other are water.
Component and consumption in described seed culture medium are preferably: acid hydrolysis residue 20g/L, wheat bran 40g/L, peptone 3g/L, ammonium sulfate 3g/L, all the other are water.
(B) prepare cellulase
Inoculum size by step (A) acquisition seed liquor with 10% (v/v) accesses in the 5L fermentor tank that 3L fermention medium is housed of sterilizing, in fermenting process, add defoamer and control foaming, keep tank pressure 0.02-0.05MPa, air flow 0.5-0.6vvm, mixing speed 100-150rpm, 30 ℃ of cultivation 80-136 hour, obtain fermented liquid.
In described fermention medium, each amounts of components is respectively: acid hydrolysis residue 30-50g/L, wheat bran 20-50g/L, Microcrystalline Cellulose or carboxymethyl cellulose 4-8g/L, ammonium sulfate 2-5g/L, potassium primary phosphate 2-4g/L, magnesium sulfate 0.4-0.6g/L, all the other are water, and the initial pH of substratum is 5.0-6.0.
In described fermention medium, each amounts of components is preferably: acid hydrolysis residue 45g/L, wheat bran 35g/L, Microcrystalline Cellulose 5g/L, ammonium sulfate 4g/L, potassium primary phosphate 3g/L, magnesium sulfate 0.6g/L, all the other are water, and the initial pH of substratum is 5.0-6.0.
The fermented liquid 8000rpm centrifuging and taking obtaining obtains supernatant liquor, must contain the crude enzyme liquid of cellulase, and this crude enzyme liquid can be directly used in cellulosic enzymolysis.
(2) test as follows the various performances of xylogen in following examples
The mensuration of content of lignin: comprise sour insoluble xylogen and sour solvable xylogen.Wherein the mensuration of sour insoluble xylogen adopts Klason method, according to GB GB/T2677.8-94, carries out; The solvable xylogen of acid carries out according to GB GB10337-89.
The mensuration of ash oontent: carry out according to GB/T2667.2-93.
The mensuration of moisture: carry out according to GB/T2667.3-93.
The mensuration of solid content in alkali lignin solution: get 100g solution to be measured, at 105 ℃, dry 24 hours, be cooled to room temperature, weigh the quality of remaining solid, this total mass number is the percentage ratio of the solid content of solution.
The mensuration of alkali content in alkali lignin solution and recovery alkali lye: get 0.5-1g testing liquid, make indicator with phenolphthalein, the hydrochloric acid soln of 0.2M/L is made titration reagent, is titrated to terminal, calculates the content of however, residual base in solution according to consumed hydrochloric acid volumeter.
Following examples can be referring to Fig. 1 and Fig. 2.
In following examples, pressure corresponding to acid hydrolysis temperature is the pressure of saturated vapor, therefore no longer for each embodiment provides pressure data.
In following examples, outside specified otherwise, percentage composition used all represents weight percentage, i.e. " % " expression " % by weight ".
Embodiment 1
(1) alkaline solution extracts alkali lignin
By the corn cob of 10.65kg (mass component forms: moisture 6.12%, Mierocrystalline cellulose 35.19%, hemicellulose 32.01%, xylogen 23.7%, other 2.95%, lower same) pulverize, then mix with alkaline solution, wherein liquid-solid volume ratio is 5: 1, the concentration of sodium hydroxide is 6%, then be warming up to 70 ℃, through the boiling alkaline hydrolysis of 1 hour, separation obtained alkaline hydrolysis residue and alkali lignin solution, with 10kg water, clean described alkaline hydrolysis residue, scavenging solution and described alkali lignin solution merge; Finally obtain 20.38kg alkaline hydrolysis residue (water ratio is 65% left and right) and 49.61kg alkali lignin solution; Alkali lignin solution with film device carry out separation concentrated after, add the dilution of 10kg water, reconcentration, finally obtains the alkali lignin concentrated solution of 6.29kg, and reclaims 53.32kg alkali lye.The solid content of this concentrated solution is 26.1% after measured, and alkali lignin content is 24.9%, and the content of however, residual base is 0.8%, and ash oontent is 1.2%, and in resulting alkali lye, the content of alkali is 4.39%, and the rate of recovery of alkali is 78%.The extraction yield of alkali lignin is 62%;
The calculation formula of alkali lignin extraction yield is as follows:
The extraction yield %=of alkali lignin (content of xylogen in quality * alkali lignin concentrated solution of alkali lignin concentrated solution)/(content of xylogen in corn cob quality * corn cob) * 100%.
(2) acid hydrolysis
Get alkaline solution in the present embodiment (1) and process the whole alkaline hydrolysis residues that obtain, then with phosphorus aqueous acid, be hydrolyzed, liquid-solid ratio is 10: 1 (mass ratio of new preparating acid solution and over dry alkaline hydrolysis residue), the mass concentration of phosphoric acid solution is 15%, acid-hydrolyzed temperature is 120 ℃, time is 0.5 hour, acid hydrolysis residue and pentose solution that rear separation obtains have been hydrolyzed, with 10kg water, clean described acid hydrolysis residue, scavenging solution and described pentose solution merge, finally obtain 12.91kg acid hydrolysis residue (water ratio is 65% left and right) and 75.55kg pentose solution, the concentration of pentose solution is 3.29%, the extraction yield of hemicellulose is 73%.
The calculation formula of hemicellulose extraction yield is as follows:
The extraction yield %=of hemicellulose (pentose solution quality * pentose solution concentration)/(content of hemicellulose in corn cob quality * corn cob) * 100%.
(3) cellulase hydrolysis
The condition of described enzymolysis is: cellulase is commercially available cellulase (jade of the He family Bioisystech Co., Ltd, 4w unit), get all acid hydrolytic residue that step (2) obtains as cellulosic substrate, according to the cellulosic addition of 15FPU/g, add cellulase, cellulosic substrate consumption is 125g/L, in temperature, be that 45 ℃, pH are 6, under the condition of mixing speed 200rpm, enzymolysis transforms 4 days, whole enzymolysis process is without pressurize, obtain the solution that main component is glucose, quality is 36.15kg, concentration is 5.6%, and cellulosic extraction yield is 54%.
The calculation formula of Mierocrystalline cellulose extraction yield is as follows:
Cellulosic extraction yield %=(concentration of the quality * glucose solution of glucose solution)/(cellulosic content in corn cob quality * corn cob) * 100%
The technique that glucose solution is produced ethanol is existing technique, does not repeat them here, and other embodiment is identical.
Embodiment 2
(1) alkaline solution extracts alkali lignin
Raw material and method are identical with embodiment 1 step (1), and difference is, liquid-solid volume ratio is 20: 1, and the concentration of sodium hydroxide is 5%, and the temperature that alkaline solution is processed is 100 ℃, and the time is 2 hours.Finally obtain 19.29kg alkaline hydrolysis residue (water ratio is 65% left and right) and 6.75kg alkali lignin concentrated solution, and reclaim 203.9kg alkali lye.The solid content of this concentrated solution is 25.2% after measured, and the alkali lignin content of concentrated solution is 23.6%, and the content of the however, residual base of concentrated solution is 0.7%, and the ash oontent of concentrated solution is 1.6%; And the content of alkali is 4.02% in the alkali lye reclaiming, the rate of recovery of alkali is 82%.The extraction yield of alkali lignin is 63%.
(2) acid hydrolysis
Get alkaline solution in the present embodiment (1) and process the whole alkaline hydrolysis residues that obtain, then with phosphorus aqueous acid, be hydrolyzed, liquid-solid ratio is 10: 1 (mass ratio of new preparating acid solution and over dry alkaline hydrolysis residue), the mass concentration of phosphoric acid solution is 20%, acid-hydrolyzed temperature is 100 ℃, time is 1 hour, acid hydrolysis residue and pentose solution that rear separation obtains have been hydrolyzed, with 10kg water, clean described acid hydrolysis residue, scavenging solution and described pentose solution merge, finally obtain 12.13kg acid hydrolysis residue (water ratio is 65% left and right) and 72.15kg pentose solution, the concentration of pentose solution is 3.21%, the extraction yield of hemicellulose is 68%.
(3) cellulase hydrolysis
The condition of described enzymolysis is: cellulase is above-mentioned penicillin (Penicillium decumbens PD-G3-08, be preserved in Wuhan University's Chinese Typical Representative culture collection center, its deposit number is CCTCC M 2011195) cultivate the cellulase obtain, get all acid hydrolytic residue that the present embodiment step (2) obtains as cellulosic substrate, according to the cellulosic addition of 15FPU/g, add cellulase, cellulosic substrate consumption is 150g/L, in temperature, it is 48 ℃, pH is 5.0, under the condition of mixing speed 50rpm, enzymolysis transforms 7 days, whole enzymolysis process is without pressurize, obtain the solution of glucose, quality is 32.56kg, concentration is 7.25%, cellulosic extraction yield is 63%.
Embodiment 3
(1) alkaline solution extracts alkali lignin
Raw material and method are identical with embodiment 1 step (1), and difference is, liquid-solid volume ratio is 10: 1, and the concentration of sodium hydroxide is 8%, and the temperature that alkaline solution is processed is 40 ℃, and the time is 6 hours.Finally obtain 21.47kg alkaline hydrolysis residue (water ratio is 65% left and right) and 5.98kg alkali lignin concentrated solution, and reclaim 97.87kg alkali lye.The solid content of this concentrated solution is 25.7% after measured, the alkali lignin content 24.1% of concentrated solution, and the content of the however, residual base of concentrated solution is 0.5%, the ash oontent of concentrated solution is 1.6%; And the content of alkali is 6.95% in the alkali lye reclaiming, the rate of recovery of alkali is 85%.The extraction yield of alkali lignin is 57%.
(2) acid hydrolysis
Get alkaline solution in the present embodiment (1) and process the whole alkaline hydrolysis residues that obtain, then with phosphorus aqueous acid, be hydrolyzed, liquid-solid ratio is 10: 1 (mass ratio of new preparating acid solution and over dry alkaline hydrolysis residue), the mass concentration of phosphoric acid solution is 5%, acid-hydrolyzed temperature is 150 ℃, time is 2 hours, acid hydrolysis residue and pentose solution that rear separation obtains have been hydrolyzed, with 10kg water, clean described acid hydrolysis residue, scavenging solution and described pentose solution merge, finally obtain 13.98kg acid hydrolysis residue (water ratio is 65% left and right) and 78.68kg pentose solution, the concentration of pentose solution is 3.29%, the extraction yield of hemicellulose is 76%.
(3) cellulase hydrolysis
The condition of described enzymolysis is: cellulase is above-mentioned Penicillium notatum (Penicillium decumbens PD-G3-08, be preserved in Wuhan University's Chinese Typical Representative culture collection center, its deposit number is CCTCC M 2011195) cultivate obtain cellulase, get all acid hydrolytic residue that the present embodiment step (2) obtains as cellulosic substrate, according to the cellulosic addition of 12FPU/g, add cellulase, cellulosic substrate consumption is 80g/L, in temperature, it is 45 ℃, pH is 6, under the condition of mixing speed 200rpm, enzymolysis transforms 2 days, whole enzymolysis process is without pressurize, obtain the solution of glucose, quality is 66.053kg, and concentration is 3.92%, cellulosic extraction rate reached 69%.
Embodiment 4
(1) alkaline solution extracts alkali lignin
Method is identical with embodiment 1 step (1), and difference is, raw material be 11.12kg Wheat Straw (mass component forms: moisture 10.1%, Mierocrystalline cellulose 44%, hemicellulose 22.2%, xylogen 17%, other 6.7%).Finally obtain 21.12kg alkaline hydrolysis residue (water ratio is 65% left and right) and 4.63kg alkali lignin concentrated solution, and reclaim 60.97kg alkali lye.The solid content of this concentrated solution is 25.9% after measured, and the alkali lignin content of concentrated solution is 24.5%, and the content of the however, residual base of concentrated solution is 0.7%, and the ash oontent of concentrated solution is 1.4%; And the content of alkali is 3.79% in the alkali lye reclaiming, the rate of recovery of alkali is 77%.The extraction yield of alkali lignin is 60%.
Alternatively, 10% sulphur acid for adjusting pH value to 3 for the alkali lignin solution obtaining can be filtered to washing, the dry alkali lignin solid that obtains.
(2) acid hydrolysis
Get alkaline solution in the present embodiment (1) and process the whole alkaline hydrolysis residues that obtain, then with sulphur aqueous acid, be hydrolyzed, liquid-solid ratio is 10: 1 (mass ratio of new preparating acid solution and over dry alkaline hydrolysis residue), the mass concentration of sulphuric acid soln is 0.5%, acid-hydrolyzed temperature is 120 ℃, time is 3 hours, acid hydrolysis residue and pentose solution that rear separation obtains have been hydrolyzed, with 10kg water, clean described acid hydrolysis residue, scavenging solution and described pentose solution merge, finally obtain 15.65kg acid hydrolysis residue (water ratio is 65% left and right) and 75.65kg pentose solution, the concentration of pentose solution is 2.35%, the extraction yield of hemicellulose is 72%.
(3) cellulase hydrolysis
The condition of described enzymolysis is: cellulase is commercially available cellulase (jade of the He family Bioisystech Co., Ltd, 4w unit), get all acid hydrolytic residue that step (2) obtains as cellulosic substrate, according to the cellulosic addition of 10FPU/g, add cellulase, cellulosic substrate consumption is 125g/L, in temperature, be that 55 ℃, pH are 4, under the condition of mixing speed 100rpm, enzymolysis transforms 5 days, whole enzymolysis process is without pressurize, obtain the solution of glucose, quality is 43.83kg, concentration is 6.25%, and cellulosic extraction yield is 56%.
Found through experiments, when acid solution adopts the weak acid that concentration expressed in percentage by weight is 30%, less to xylogen and cellulosic destruction, can realize object of the present invention.And the concentration of phosphoric acid solution is while being 1%, also can realize the present invention, just needed time of acid hydrolysis and temperature of reaction need corresponding increase.
Comparative example 1
Method is with embodiment 1 step (1), difference is: liquid with film device carry out there is no thin up after separated concentrated, concentrated step again, the rate of recovery of content, ash oontent and the alkali lye of the however, residual base of the extraction yield of alkali lignin, alkali lignin concentrated solution is in Table 1.
Comparative example 2
Method is with embodiment 1 step (1), and difference is: the temperature that alkaline solution is processed is 170 ℃, and the rate of recovery of content, ash oontent and the alkali lye of the however, residual base of alkali lignin extraction yield, alkali lignin concentrated solution is in Table 1.
Table 1
Comparative example 3
Get the acid hydrolysis residue obtaining in embodiment 2 steps (2), method according to embodiment 2 steps (3) is carried out cellulase hydrolysis, difference is, cellulase is commercially available cellulase (jade of the He family Bioisystech Co., Ltd, 4w unit), the quality of glucose solution is 32.5kg, concentration is 5.18%, and cellulosic extraction yield is 45%.
Comparative example 4
Get the acid hydrolysis residue obtaining in embodiment 3 steps (2), method according to embodiment 3 steps (3) is carried out cellulase hydrolysis, difference is, cellulase is commercially available cellulase (jade of the He family Bioisystech Co., Ltd, 4w unit), the quality of glucose solution is 66kg, concentration is 2.72%, and cellulosic extraction yield is 48%.
Test case 1
In the phenol of 10Kg, the alkali lignin concentrated solution that adds respectively 30Kg embodiment 1 and comparative example 1,2 to obtain, is warming up to 70 ℃, adds the sodium hydroxide solution (mass percent concentration is 50) of 1Kg, air distillation to 150 ℃, back flow reaction 90 minutes, is cooled to 70-80 ℃, adds 11Kg formaldehyde (mass percent concentration is 37%) reaction 90 minutes, be cooled to 50 ℃, regulate PH to 6.5-7, vacuum hydro-extraction is to viscosity 9000cp/25 ℃ left and right, discharging.The alkali lignin concentrated solution that finally can be obtained by embodiment 1 and comparative example 1,2 makes respectively lignin modification resol, and its performance index are tested by the following method, and property indices is listed in table 2.
The mensuration of resol solid content: carry out according to HG/T2711.
The mensuration of the viscosity of resol: carry out according to HG/T2712.
The mensuration of resol free phenol: carry out according to HG51342.
The mensuration of the free aldehyde of resol: carry out according to HG51343.
The mensuration of phenolic resin gel time: carry out according to HG51338.
The mensuration of water-content in resol: carry out according to HG51341.
The mensuration of resol pH value: carry out according to HG/T2501.
The performance index of the modified phenolic resins of table 2 Different Alkali lignin liquor
In the resol product that three kinds of Different Alkali lignin liquors obtain, the content of phenol and formaldehyde raises gradually, illustrate the alkali lignin solution that adds not only with formaldehyde between the activity of reacting die down gradually, but also affected reacting to each other of phenol and formaldehyde.The first alkali lignin solution is the alkali lignin solution that the present invention obtains, and the content of its however, residual base and ash oontent are all lower, does not substantially affect reacting between alkali lignin and phenol and formaldehyde; The second alkali lignin solution is the direct concentrated alkali lignin solution obtaining, and without water washing, the content of however, residual base and ash oontent are all higher, has affected reacting between alkali lignin and phenol and formaldehyde; And in the third alkali lignin solution, having passed through a high temperature steaming process, some active groups of xylogen are damaged under hot conditions, thereby the activity during with formaldehyde reaction weakens greatly.
The lignin liquor of 25% left and right that industrial soda xylogen (Gaotang, Shandong polynary xylogen company limited) is made into if directly use, synthesis technique and method are constant, method according to test case 1 is prepared modified phenolic resins, regulate after pH value, only at the bottom of bottle, there is a small amount of resin to produce, see that on the whole alkali lignin solution does not participate in reaction, after decompression dehydration, at the bottom of bottle, find that there is alkali lignin precipitation, cannot obtain alkali lignin modified novolac resin.
In sum, the alkali lignin solution that known the present invention obtains has higher activity, can be in order to prepare the products such as modified phenolic resins.
Obviously, above-described embodiment is only for example is clearly described, and the not restriction to embodiment.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here exhaustive without also giving all embodiments.And the apparent variation of being extended out thus or change are still among the protection domain in the invention.
Claims (10)
1. a method of comprehensive utilization for lignocellulose biomass, is characterized in that comprising the following steps:
(a) alkaline hydrolysis is processed
(I) used alkaline solution to process described lignocellulose biomass to make lignin dissolution wherein in alkaline solution, and described alkaline solution is sodium hydroxide, potassium hydroxide or ammoniacal liquor;
(II) then filter, wash and obtain alkaline hydrolysis residue and liquid;
(III) is by separated, the concentrated alkali lignin solution that obtains of gained liquid process film device;
(b) acid hydrolysis
Described alkaline hydrolysis residue is carried out to acid hydrolysis, obtain pentose solution and acid hydrolysis residue after separation, the acid adopting in described acid hydrolysis is one or more in sulfuric acid, hydrochloric acid, nitric acid or phosphoric acid;
(c) cellulase hydrolysis
Use cellulase to carry out enzymolysis to described acid hydrolysis residue, obtain the solution that main component is glucose, described cellulase is for being cultivated the cellulase obtaining by a penicillium, and this Penicillium notatum Classification And Nomenclature is
penicillium decumbenspD-G3-08, has been preserved in Wuhan University's Chinese Typical Representative culture collection center, and its deposit number is CCTCCM2011195,
Wherein, the preparation method of described cellulase is:
(1) bacterial classification multiplication culture
By naming number, be
penicillium decumbenspD-G3-08 Penicillium notatum seed liquor is linked in the fermentor tank that contains seed culture medium through 121 ℃ of sterilizing 30min and activates with the inoculum size of percent by volume 5%, keep tank pressure 0.02-0.05MPa, air flow 0.5vvm, mixing speed 100-150rpm, 30 ℃ of cultivation 30-60 hour, the seed liquor after being activated;
Component in described seed culture medium and consumption are: acid hydrolysis residue 10-30g/L, the wheat bran 20-50g/L in described step (b), peptone 1-4g/L, ammonium sulfate 2-4g/L, all the other are water;
(2) prepare cellulase
Inoculum size by step (1) acquisition seed liquor with percent by volume 10% accesses in the fermentor tank that 3L fermention medium is housed of sterilizing, in fermenting process, add defoamer and control foaming, keep tank pressure 0.02-0.05MPa, air flow 0.5-0.6vvm, mixing speed 100-150rpm, 30 ℃ of cultivation 80-136 hour, obtain fermented liquid;
In described fermention medium, each amounts of components is respectively: acid hydrolysis residue 30-50g/L, wheat bran 20-50g/L, Microcrystalline Cellulose or carboxymethyl cellulose 4-8g/L, ammonium sulfate 2-5g/L, potassium primary phosphate 2-4g/L, magnesium sulfate 0.4-0.6g/L, all the other are water, and the initial pH of substratum is 5.0-6.0;
The fermented liquid 8000rpm centrifuging and taking obtaining obtains supernatant liquor, must contain the crude enzyme liquid of described cellulase.
2. according to the method described in claim 1, it is characterized in that: in described step (III), also comprise the described concentrated alkali lignin solution obtaining dilute with water again, and then concentrated step.
3. according to the method described in claim 1 or 2, it is characterized in that: in described step (III), be also included in the concentrated step that obtains described alkali lignin solution afterwards or recycle alkaline solution wherein simultaneously.
4. method according to claim 3, is characterized in that: described step (III) also comprises the alkali lignin solution process neutralization obtaining, filters and be dried, and obtains alkali lignin solid.
5. method according to claim 4, is characterized in that: at alkaline hydrolysis described in described step (I), at 40-100 ℃, carry out.
6. method according to claim 5, is characterized in that: in described step (I), the concentration of alkaline solution is 5-8 %.
7. method according to claim 6, is characterized in that: the time of processing at alkaline solution described in described step (I) is 1-6 hour.
8. according to the method described in claim 6 or 7, it is characterized in that: described acid-hydrolyzed temperature is 100-150 ℃, the time is 0. 5-3 hour, and the concentration of acid solution is 0.5-20 %.
9. described method according to Claim 8, is characterized in that: described acid solution is phosphoric acid solution, and the concentration of phosphoric acid solution is 5-20 %.
10. according to the method described in claim 1,2,4,5,6,7 or 9, it is characterized in that: the condition of described cellulase hydrolysis is: substrate consumption is 80-150g/L, the addition of cellulase is 10-15FPU/g Mierocrystalline cellulose, temperature is that 45-55 ℃, pH are that 4-6, mixing speed are 50-200rpm, and enzymolysis transformation time is 2-7 days.
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| CN104387593A (en) * | 2014-09-28 | 2015-03-04 | 南开大学 | Method for separating lignin in garden garbage by utilizing high-temperature boiling |
| CN104911164A (en) * | 2015-05-11 | 2015-09-16 | 镇江博睿兴邦生物科技有限公司 | Method for improving cellulase use efficiency, and apparatus thereof |
| CN107245505B (en) * | 2017-07-20 | 2021-04-30 | 淮阴师范学院 | Multistage hydrolysis saccharification method for urban waste biomass resources |
| CN107502626A (en) * | 2017-08-23 | 2017-12-22 | 北京林业大学 | A kind of Application way of wood fibre residue |
| CN114763680B (en) * | 2021-01-15 | 2024-01-30 | 中国石油天然气股份有限公司 | Method for removing lignin from lignocellulose raw material |
| CN113443978B (en) * | 2021-06-24 | 2023-01-31 | 清华大学 | Method for alkali-heat total hydrolysis of lignocellulose and application thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1157853A (en) * | 1996-11-13 | 1997-08-27 | 山东大学 | Preparing method of high active cellulase |
| CN1339585A (en) * | 2000-08-21 | 2002-03-13 | 中国科学院化工冶金研究所 | Process for producing high activity cellulase by solid fermentation of steam puffed stalk |
| CN101619332A (en) * | 2009-08-13 | 2010-01-06 | 安徽丰原发酵技术工程研究有限公司 | Method for efficiently saccharifying bagasse |
| CN102061267A (en) * | 2010-11-26 | 2011-05-18 | 东北林业大学 | Engonus fungus with high enzyme activity and high capacity of efficiently degrading straw cellulose in northeast China region |
| CN102153763A (en) * | 2010-09-27 | 2011-08-17 | 天津大学 | Lignocellulose acid/alkali coupling pretreatment method |
-
2011
- 2011-10-11 CN CN201110306683.XA patent/CN103045680B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1157853A (en) * | 1996-11-13 | 1997-08-27 | 山东大学 | Preparing method of high active cellulase |
| CN1339585A (en) * | 2000-08-21 | 2002-03-13 | 中国科学院化工冶金研究所 | Process for producing high activity cellulase by solid fermentation of steam puffed stalk |
| CN101619332A (en) * | 2009-08-13 | 2010-01-06 | 安徽丰原发酵技术工程研究有限公司 | Method for efficiently saccharifying bagasse |
| CN102153763A (en) * | 2010-09-27 | 2011-08-17 | 天津大学 | Lignocellulose acid/alkali coupling pretreatment method |
| CN102061267A (en) * | 2010-11-26 | 2011-05-18 | 东北林业大学 | Engonus fungus with high enzyme activity and high capacity of efficiently degrading straw cellulose in northeast China region |
Non-Patent Citations (2)
| Title |
|---|
| Cao NJ等.Ethanol production from corn cob pretreated by the ammonia steeping process using genetically engineered yeast.《Biotechnology Letters》.1996,第18卷(第9期),参见第1013-1018页，特别是第1014-1015页的"材料与方法"部分以及第1017页的图1-4. * |
| Ethanol production from corn cob pretreated by the ammonia steeping process using genetically engineered yeast;Cao NJ等;《Biotechnology Letters》;19960930;第18卷(第9期);参见第1013-1018页，特别是第1014-1015页的"材料与方法"部分以及第1017页的图1-4 * |
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