CN103045685B - 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: (a) performing N-stage acid hydrolysis of lignocellulose biomass, wherein the temperature for the first stage acid hydrolysis is 100-150 DEG C, the temperatures of subsequent stages of acid hydrolysis decrease by 5-25 DEG C stage by stage, and N is an integer more than or equal to 2; (b) processing the acid hydrolysis residues by using an alkaline solution so as to extract alkaline lignin; (c) performing enzymatic hydrolysis of the alkaline hydrolysis residues obtained by alkaline solution processing in step (b) by using cellulase to obtain a glucose solution and enzymatic hydrolysis residues; (d) after step (c) is complete, returning the obtained enzymatic hydrolysis residues to step (b) for alkaline solution processing, or combining the enzymatic hydrolysis residues with new acid hydrolysis residues and performing alkaline solution processing in step (b), then orderly performing steps (c) and (d), cycling the steps so as to further extract lignin and to perform enzymatic hydrolysis of the celluose. 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 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 lignocellulose 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 raw material production ethanol process, the first problem running into is that hemicellulose, Mierocrystalline cellulose and xylogen are failed to fully utilize well, the Technology of existing processing biomass, mainly with degraded carbohydrate, obtaining ethanol is greatly object, can not extract simultaneously and obtain high purity, highly active xylogen, often xylogen is removed to object as one, simultaneously in double cellulosic utilization, also there is the shortcoming that generates a lot of cellulase inhibitors, finally also can affect the productive rate of ethanol.
As disclosed a kind of combined pretreatment method and system thereof of lignocellulose biomass in CN100564667C, after being pulverized, lignocellulose biomass packs in circulating reaction still, and inject diluted acid, opening recycle pump is to carry out circulating reaction at 50 ℃-200 ℃ in temperature, reaction finish after by the hydrolyzed solution obtaining; After remaining lignocellulose rinses in circulating reaction still, put into ball mill and add alkali lye and carry out ball milling, further except delignification, ball milling complete except after alkali for follow-up enzymolysis, obtain ethanol.This patent adopts an acidolysis to remove hemicellulose can cause two disadvantageous effects, on the one hand, if want as far as possible hemicelluloses of removing, need adopt higher temperature and/or long reaction times more, cause like this pentose of hydrolysis in early stage under comparatively high temps, easily to produce the cellulase inhibitors such as furfural and acetic acid, thereby reduce enzymolysis transformation efficiency; On the other hand, if do not adopt higher temperature and/or long reaction times, after acidolysis, in residue, contain more hemicellulose, be unfavorable for that alkaline solution extracts alkali lignin, if wanting dissolved lignin as much as possible just need to improve the temperature of alkali concn, alkaline purification and extend the time of alkaline purification, cause the active part of xylogen to be damaged, can not utilize its xylogen to remove to produce high value-added product, therefore, technique scheme can not be taken into account the comprehensive utilization of Mierocrystalline cellulose, hemicellulose and xylogen simultaneously.
In the process of raw material production ethanol, run into the low conversion rate that another problem is cellulase hydrolysis take lignocellulose biomass, cause 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 reason of the low conversion rate 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, and cellulase is low to crystalline cellulose enzymatic reaction vigour, therefore, in order to improve the transformation efficiency of cellulase hydrolysis, need to improve the vigor of enzyme.
The system and method that utilizes agriculture and forestry organic waste material to produce furfural is disclosed in CN101130530B, by two-step approach, produce furfural, comprise hydrolysis system and dehydration Distallation systm, wherein hydrolysis system comprises the N level acid hydrolytic reaction still that mutual head and the tail connect, and agriculture and forestry organic waste material continuous hydrolysis is generated to pentose solution.The shortcoming that above-mentioned N level acid hydrolysis system exists is, because hydrolysis temperature in hydrolytic reaction pots at different levels is identical, therefore large to xylogen and cellulosic destructive rate, and the enzyme inhibitors such as the furfural generating, acetic acid is more, is unfavorable for the comprehensive utilization of lignocellulose biomass.
Summary of the invention
For this reason, technical problem to be solved by this invention is while overcoming the comprehensive utilization Mierocrystalline cellulose that exists in prior art, hemicellulose and xylogen, can not obtain highly active xylogen, higher hemicellulose and the problem of Mierocrystalline cellulose extraction yield simultaneously, thereby propose a kind of method of lignocellulose biomass comprehensive utilization.
For achieving the above object, the invention provides a kind of method of comprehensive utilization of lignocellulose biomass, comprise the following steps:
(a), to lignocellulose biomass acid hydrolysis, after separation, obtain pentose solution and acid hydrolysis residue;
(b) with alkaline solution, process described acid hydrolysis residue, thereby extract alkali lignin;
(c) use cellulase to process to alkaline solution described in step (b) the alkaline hydrolysis residue obtaining and carry out enzymolysis, obtain glucose solution and enzymolysis residue;
(d) after step (c) completes, by the described enzymolysis residue obtaining return step (b) carry out alkaline solution processing or described enzymolysis residue and new acid hydrolysis residue are merged after carry out again step (b) alkaline solution process, then carry out successively step (c) and (d), so circulation, thus further extract xylogen and carry out cellulase hydrolysis.
In described step (a), to the acid hydrolysis of described lignocellulose, it is the acid hydrolysis of N level, the acid-hydrolyzed reactor of N level is end to end, one of them reactor is made as to the first step, last is made as N level, the acid solution of new preparation adds in first step acid hydrolytic reaction still, the acid solution that first step acid hydrolytic reaction still is discharged adds in the acid hydrolytic reaction still of the second stage, the acid solution of discharging in the acid hydrolytic reaction still of the second stage adds in third stage acid hydrolytic reaction still, successively sequentially, until the acid solution that N-1 level acid hydrolytic reaction still is discharged adds in N level acid hydrolytic reaction still, the acid solution that N level acid hydrolytic reaction still is discharged is final pentose solution, take out the acid hydrolysis residue in first step acid hydrolytic reaction still, then pack new lignocellulose biomass raw material into, then using first step acid hydrolytic reaction still as N level acid hydrolytic reaction still, using second stage acid hydrolytic reaction still as first step acid hydrolytic reaction still, third stage acid hydrolytic reaction still is as second stage acid hydrolytic reaction still, until N level acid hydrolytic reaction still is as N-1 level acid hydrolytic reaction still, reaction is again hydrolyzed, so hydrolysis moves in circles and can realize the continuous hydrolysis of lignocellulose biomass,
Wherein, the acid-hydrolyzed temperature of the first step is 100-150 ℃, and later every grade is reduced 5-25 ℃ step by step, and N is more than or equal to 2 integer.
Further, the acid-hydrolyzed temperature of the described first step is 120-140 ℃, and every grade is reduced 10-20 ℃ step by step subsequently.
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, for example one or more in sulfuric acid, hydrochloric acid, nitric acid and phosphoric acid.
Concentration and the time of the acid-hydrolyzed acid solution of described N level are not particularly limited, it can be concentration and the time that lignocellulose biomass carries out acid-hydrolyzed conventional acid solution, for example in the acid hydrolysis of described N level, the concentration of the acid solution of every grade of hydrolysis reaction is that (as the acid of selecting is strong acid to 0.5-30 % by weight, the concentration of acid solution is lower, be about 0.5-5 % by weight, as the acid of selecting is weak acid, the concentration of acid solution is higher, be about 5-30 % by weight), the time of every grade of hydrolysis reaction in the acid hydrolysis of described N level (being the residence time of acid solution in reactor) is 0.25-2 hour.The concentration of preferably phosphoric acid is 1-20 % by weight.
Described N is the integer of 3-5.
Described lignocellulose biomass can be one or more of maize 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.
The concrete steps of described step (b) are:
(i) with alkaline solution, processing described acid hydrolysis residue makes lignin dissolution wherein in alkaline solution;
(ii) then filter, wash and obtain solid and liquid;
(iii) by separated, the concentrated alkali lignin solution that obtains of gained liquid process film device.
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), also comprise the alkali lignin solution process neutralization obtaining, filter and be dried, obtain the step of alkali lignin solid.
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 alkaline solution is processed and is carried out at 40-100 ℃.
In described alkaline solution processing, liquid-solid volume ratio is 5: 1-20: 1.
The time that described alkaline solution is processed is 1-6 hour.
In described alkaline solution processing, the concentration of alkaline solution is 0.8-5 % by weight.
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 Penicillium decumbens PD-G3-08, be preserved in Wuhan University's Chinese Typical Representative culture collection center (being called for short CCTCC), depositary institution address: Wuhan University's preservation center.The numbering of registering on the books is CCTCC M 2011195, and preservation date is on June 13rd, 2011.Take this bacterial strain as the cellulosic bacterial strain of enzymolysis.
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, produces ethanol.
Technique scheme of the present invention compared with prior art has the following advantages:
1, the present invention adopts first acidolysis, alkaline hydrolysis again, the operational path of last enzymolysis extracts respectively hemicellulose, xylogen and Mierocrystalline cellulose, and after enzymolysis, adopt circulation technology respectively Mierocrystalline cellulose and xylogen to be replaced to extraction process, improved on the one hand the extraction yield of Mierocrystalline cellulose and xylogen, can weaken by this method on the other hand acidolysis, alkaline hydrolysis treatment condition, under the prerequisite of extraction yield that guarantees hemicellulose, further protection xylogen and Mierocrystalline cellulose are not destroyed, and can make xylogen and cellulosic utilization maximize; As can be seen here, aforesaid method of the present invention has solved the problem of complex utilization of the lignocellulose biomass of prior art, makes the utilization of resources reach maximization.
2. the present invention has adopted the mode of multistage acidolysis to the acidolysis of lignocellulose biomass, and (the acid-hydrolyzed temperature of the first step is 100-150 ℃ in acidolysis process, to have adopted the method reducing step by step to N order reaction still temperature from first step reactor, every grade is reduced 5-25 ℃ step by step subsequently), the method can adopt different acid hydrolysis temperature according to the complexity of hemicellulose acidolysis and pentose damaed cordition, that is to say that the material in N order reaction still is new material, hemicellulose is more easily removed, therefore acid-hydrolyzed temperature is lower, in addition, in N order reaction still, the concentration of pentose is the highest, adopt lower hydrolysis temperature, can prevent from generating furfural and acetic acid, thereby reduce furfural and the restraining effect of acetic acid to cellulase, and material in first step reactor is removed remaining hemicellulose more difficult, adopts higher acid-hydrolyzed temperature to be conducive to farthest extract hemicellulose, adopt technique scheme can farthest extract hemicellulose, destroy as little as possible xylogen and Mierocrystalline cellulose simultaneously, keep the activity of xylogen, also reduced in addition energy consumption.
Adopt aforesaid method to make the later half cellulosic extraction yield of acidolysis can reach 80 % by weight, cellulosic rate of loss is less than 9 % by weight, and the rate of loss of xylogen is less than 10 % by weight; In addition, because the structure of xylogen is not destroyed, so the activity of the xylogen extracting through alkaline solution is higher, can be directly as the raw material of producing other high value added product (as resol); By most hemicelluloses, be extracted simultaneously, after alkaline hydrolysis, most xylogen are extracted by alkaline solution, thereby eliminated cellulosic spatial obstacle, made cellulase more easily contact Mierocrystalline cellulose, improved cellulosic extraction yield, reduced the usage quantity of cellulase, shortened enzymolysis time, reduced production cost, on the other hand, because the enzyme inhibitor generating in acidolysis process is less, also improved cellulosic extraction yield; As can be seen here, by aforesaid method of the present invention, further solved the problem of complex utilization of the lignocellulose biomass of prior art, made the utilization of resources reach maximization.
3, the preferred 3-5 level of described N level, it is both economical within the scope of this that (equipment investment is few, easy and simple to handle) can obtain again high hemicellulose extraction yield, and to xylogen and cellulosic destructive rate minimum (the more multipair xylogen of progression and cellulosic destructive rate are larger).
4. the preferred 120-140 ℃ of the acid-hydrolyzed temperature of the first step in the present invention, every grade of preferred 10-20 ℃ of temperature reducing step by step subsequently, above-mentioned scope can guarantee under the higher prerequisite of hemicellulose extraction yield, lower to xylogen and cellulosic destructive rate, and the enzyme inhibitors such as the furfural generating and acetic acid is still less.
5, the present invention has adopted film device separation and concentrated step in alkaline hydrolysis process, has improved the purity of alkali lignin, is conducive to produce high value-added product.
6, the present invention is by the wooden solution with water dilution of alkali, again concentrated, has further reduced the ash oontent in alkali lignin solution, and remaining alkali content, has improved solid content, is conducive to use xylogen to produce high value-added product.
7, 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.
8, because the alkaline solution treatment temp (40-100 ℃) lower is lower, realize lignin extraction, further protect the activity of xylogen.
9, 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.
10, the condition that alkaline solution of the present invention is processed adopts liquid-solid ratio, alkali consumption, the temperature and time being more preferably, and the activity of the alkali lignin finally obtaining is very high, and the xylogen therefore finally obtaining is particularly suitable as the xylogen of modified phenolic resins.
11, cellulase of the present invention is for being cultivated the cellulase obtaining by a penicillium, this Penicillium notatum Classification And Nomenclature is Penicillium decumbens PD-G3-08, be preserved in Wuhan University's Chinese Typical Representative culture collection center, its deposit number is CCTCC M 2011195, the cellulase that adopts this Penicillium notatum to produce has higher vigor, has further improved the extraction yield of cellulase hydrolysis.
What 12. the present invention were 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;
Fig. 3 is N level acidolysis equipment schematic diagram used.
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 Penicillium decumbens PD-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 GB 10337-89.
The mensuration of ash oontent: carry out according to GB/T 2667.2-93.
The mensuration of moisture: carry out according to GB/T 2667.3-93.
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, Fig. 2 and Fig. 3.
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) N level acid hydrolysis
In the present embodiment: employing be three grades of acid hydrolysiss, first corn cob is smashed, wash dedusting with water.First reactor is made as to the first step, last is made as the third stage, the acid solution of newly preparation is added in first step hydrolytic reaction pot, the acid solution that first step acid hydrolytic reaction still is discharged adds in the acid hydrolytic reaction still of the second stage, the acid solution that second stage acid hydrolytic reaction still is discharged adds in third stage acid hydrolytic reaction still, the solution of discharging in third stage acid hydrolytic reaction still is final pentose solution, then the acid hydrolysis residue in first step acid hydrolytic reaction still is discharged, and pack new corn cob raw material into, using it as third stage acid hydrolytic reaction still, using former second stage acid hydrolytic reaction still as first step acid hydrolytic reaction still, using former third stage acid hydrolytic reaction still as second stage acid hydrolytic reaction still, carry out again acid hydrolytic reaction, so hydrolysis moves in circles and can realize the continuous hydrolysis of lignocellulose biomass,
Wherein, the acid-hydrolyzed temperature of the first step is 140 ℃, and the acid-hydrolyzed temperature in the second stage is 120 ℃, and the acid-hydrolyzed temperature of the third stage is 100 ℃; Every grade of acid-hydrolyzed time is 1 hour, and acid solution is phosphate aqueous solution, and the concentration of phosphoric acid solution is 5%, and liquid-solid ratio is 8: 1 (mass ratio of new preparating acid solution and over dry corn cob raw material, lower together), by aforesaid method to 1.06 * 10
3the corn cob raw material that kg is new carries out after continuous acid hydrolysis processing, uses 1 * 10
3the water of kg is washed described acid hydrolysis residue, and water lotion and acid hydrolysis solution merge, and finally obtaining pentose solution is 8.02 * 10
3kg, pentose concentration is 3.14%, the weight that obtains acid hydrolysis residue is 1.97 * 10
3kg (water ratio is 65% left and right, and the over dry content of hemicellulose is 12.83%, and cellulosic over dry content is 49.63%, and the over dry content of xylogen is 33%).The extraction yield of hemicellulose is 74%.
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%
(2) alkaline solution extracts alkali lignin
The all acid hydrolytic residue that the present embodiment step (1) is obtained and sodium hydroxide solution are mixed, are warming up to 70 ℃, through the boiling alkaline hydrolysis of 1 hour, wherein liquid-solid volume ratio is 5: 1, the concentration of sodium hydroxide is 3%, and separation obtains alkaline hydrolysis residue and alkali lignin solution, with 1 * 10
3kg water cleans described alkaline hydrolysis residue, and scavenging solution and described alkali lignin solution merge; Finally obtain 3.51 * 10
3kg alkali lignin solution and 1.64 * 10
3kg alkaline hydrolysis residue (water ratio is 65% left and right); Alkali lignin content in alkali lignin solution is 3.17%, and the extraction yield of alkali lignin is 44%.
The extraction yield formula of alkali lignin is as follows:
Alkali lignin extraction yield %=(content of lignin in quality * alkali lignin solution of alkali lignin solution)/(content of xylogen in corn cob quality * corn cob) * 100%
(3) cellulase hydrolysis alcohol prepared by fermenting
The condition of described enzymolysis is: cellulase is commercially available cellulase (jade of the He family Bioisystech Co., Ltd, 4w unit), get the described alkaline solution of step (2) and process whole alkaline hydrolysis residues of obtaining as cellulosic substrate, according to the cellulosic addition of 15FPU/g, add cellulase, cellulosic substrate consumption is 125g/L, in temperature, be that 48 ℃, pH are 5.0, under the condition of mixing speed 50rpm, enzymolysis transforms 2 days, and whole enzymolysis process, without pressurize, obtains 1.12 * 10
3kg enzymolysis residue (water ratio is 65% left and right), also obtains glucose solution, and quality is 4.58 * 10
3kg, concentration is 3.93%, cellulosic extraction yield is 48%.
The 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%
It is existing technique that glucose solution is produced ethanol, does not repeat them here, and following examples are same.
(4) circular treatment
Whole enzymolysis residues that step (3) is obtained return to step (2) and carry out alkaline solution processing for the second time, and alkaline solution processing is for the second time identical with the condition that alkaline solution step in the present embodiment (2) Suo Shu is processed; Obtain 0.85 * 10
3kg is alkaline hydrolysis residue (water ratio is 65% left and right) and 2.01 * 10 for the second time
3kg alkali lignin solution, in alkali lignin solution, the content of alkali lignin is 4.65%; The extraction yield of alkali lignin is 37% for the second time;
The described residue of alkaline hydrolysis is for the second time carried out to enzymolysis for the second time, and the condition of enzymolysis is identical with the condition of enzymolysis described in step in the present embodiment (3) for the second time; Obtaining quality is 2.37 * 10
3the glucose solution that kg, concentration are 5.54%, cellulosic extraction yield is 35% for the second time.
In sum, the extraction yield of the hemicellulose of corn cob is 74%, and cellulosic total extraction yield is 83%, and total extraction yield of xylogen is 81%.
Embodiment 2
(1) N level acid hydrolysis
Raw material and method be with embodiment 1 step (1), and difference is, the acid-hydrolyzed temperature of the first step is 135 ℃, and the acid-hydrolyzed temperature in the second stage is 120 ℃, and the acid-hydrolyzed temperature of the third stage is 105 ℃; The weight that finally obtains acid hydrolysis residue is 2.03 * 10
3kg (water-content 65% left and right, the over dry content of hemicellulose is 13.92%, cellulosic over dry content is 49.02%, the over dry content of xylogen is 32.64%), final pentose solution is 7.97 * 10
3kg, pentose concentration is 3.04%, the extraction yield of hemicellulose is 71%.
(2) alkaline solution extracts alkali lignin
The acid hydrolysis residue obtaining in the present embodiment step (1) is mixed with sodium hydroxide solution, and wherein liquid-solid volume ratio is 10: 1, and the concentration of sodium hydroxide is 3%, then be warming up to 70 ℃, through the boiling alkaline hydrolysis of 1 hour, separation obtained alkaline hydrolysis residue and alkali lignin solution, with 1 * 10
3kg water cleans described alkaline hydrolysis residue, and scavenging solution and described alkali lignin solution merge; Finally obtain 1.70 * 10
3kg alkaline hydrolysis residue (water ratio is about 65%) and 7.11 * 10
3kg alkali lignin solution; Alkali lignin solution with film device carry out separation concentrated after, add 1.0 * 10
3the dilution of kg water, reconcentration, finally obtains 0.46 * 10
3the alkali lignin concentrated solution of kg, and reclaim 7.65 * 10
3kg alkali lye.The solid content of this concentrated solution is 25.1% after measured, and alkali lignin content is 23.7%, and the content of however, residual base is 0.5%, and ash oontent is 1.4%, and in resulting alkali lye, the content of alkali is 2.23%, and the rate of recovery of alkali is 80%; The extraction yield of alkali lignin is 43%.
(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 the described alkaline solution of step (2) and process whole residues of obtaining as cellulosic substrate, according to the cellulosic addition of 10FPU/g, add cellulase, cellulosic substrate consumption is 150g/L, in temperature, be that 55 ℃, pH are 4, under the condition of mixing speed 200rpm, enzymolysis transforms 7 days, and whole enzymolysis process is without pressurize.Obtain 1.15 * 10
3kg enzymolysis residue (water ratio is 65% left and right), also obtains glucose solution, and quality is 4.56 * 10
3kg, concentration is 4.19%, cellulosic extraction rate reached 51%.
(4) circular treatment
Whole enzymolysis residues that step (3) is obtained return to step (2) and carry out alkaline solution processing for the second time, and alkaline solution processing is for the second time identical with the condition that alkaline solution step in the present embodiment (2) Suo Shu is processed; Obtain 0.85 * 10
3kg is alkaline hydrolysis residue (water ratio is 65% left and right) and 0.43 * 10 for the second time
3kg alkali lignin concentrated solution, in alkali lignin concentrated solution, the content of alkali lignin is 23.5%; The extraction yield of alkali lignin is 40% for the second time;
The described residue of alkaline hydrolysis is for the second time carried out to enzymolysis for the second time, and the condition of enzymolysis is identical with the condition of enzymolysis described in step in the present embodiment (3) for the second time; Obtaining quality is 2.29 * 10
3kg, the glucose solution that concentration is 5.56%, cellulosic extraction yield is 34% for the second time.
In sum, the extraction yield of hemicellulose is 71%, and cellulosic total extraction yield is 85%, and total extraction yield of xylogen is 83%.
Embodiment 3
(1) N level acid hydrolysis
Raw material and method be with embodiment 1 step (1), and difference is, in every order reaction still, the concentration of phosphoric acid solution is 10%, every grade of acid-hydrolyzed time is 2 hours, the acid-hydrolyzed temperature of the first step is 100 ℃, and the acid-hydrolyzed temperature in the second stage is 95 ℃, and the acid-hydrolyzed temperature of the third stage is 90 ℃; The weight that finally obtains acid hydrolysis residue is 2.1 * 10
3kg (water-content 65% left and right, the over dry content of hemicellulose is 13.94%, cellulosic over dry content is 48.74%, the over dry content of xylogen is 33.04%), final pentose solution is 7.9 * 10
3kg, pentose concentration is 3.02%, the extraction yield of hemicellulose is 70%.
(2) alkaline solution extracts alkali lignin
By all acid hydrolytic residue obtaining in the present embodiment step (1) according to embodiment 2 steps (2) processing method, difference is, liquid-solid volume ratio is 10: 1, and the concentration of sodium hydroxide is 5%, the temperature that alkaline solution is processed is 40 ℃, and the time is 6 hours.Finally obtain 1.79 * 10
3kg alkaline hydrolysis residue (water ratio is 65% left and right) and 0.43 * 10
3kg alkali lignin concentrated solution, and reclaim 7.86 * 10
3kg alkali lye.The solid content of this concentrated solution is 25.3% after measured, and the alkali lignin content of concentrated solution is 23.7%, 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 3.92% in the alkali lye reclaiming, the rate of recovery of alkali is 84%.The extraction yield of alkali lignin is 40%.
(3) cellulase hydrolysis
Get the present embodiment step (2) alkaline solution and process the whole alkaline hydrolysis residues that obtain, method according to embodiment 1 step (3) is carried out cellulase hydrolysis, difference is: cellulase is that cellulase is above-mentioned Penicillium notatum (Penicillium decumbens PD-G3-08, its deposit number is CCTCC M 2011195) cultivate the cellulase obtaining, obtain 1.1 * 10
3kg enzymolysis residue (water ratio is about 65%), also obtains glucose solution, and quality is 5 * 10
3kg, concentration is 4.79%, cellulosic extraction yield is 64%.
(4) circular treatment
Whole enzymolysis residues that step (3) is obtained return to step (2) and carry out alkaline solution processing for the second time, and alkaline solution processing is for the second time identical with the condition that alkaline solution step in the present embodiment (2) Suo Shu is processed; Obtain 0.75 * 10
3kg is alkaline hydrolysis residue (water ratio is 65% left and right) and 0.49 * 10 for the second time
3kg alkali lignin concentrated solution, in alkali lignin concentrated solution, the content of alkali lignin is 24.9%; The extraction yield of alkali lignin is 48% for the second time;
The described residue of alkaline hydrolysis is for the second time carried out to enzymolysis for the second time, and the condition of enzymolysis is identical with the condition of enzymolysis described in step in the present embodiment (3) for the second time; Obtaining quality is 2.08 * 10
3the glucose solution that kg, concentration are 4.49%, cellulosic extraction yield is 25% for the second time.
In sum, the extraction yield of hemicellulose is 70%, and cellulosic extraction yield is 89%, and total extraction yield of xylogen is 88%.
Embodiment 4
(1) N level acid hydrolysis
Raw material, technique and method are with embodiment 1 step (1), and difference is: acid solution is sulphuric acid soln, and concentration is 1%; Every grade of acid-hydrolyzed time is 0.5 hour; The acid-hydrolyzed temperature of the first step is 120 ℃, and the acid-hydrolyzed temperature in the second stage is 110 ℃, and the acid-hydrolyzed temperature of the third stage is 100 ℃, and the acid-hydrolyzed temperature of the fourth stage is 90 ℃, and the acid-hydrolyzed temperature of level V is 80 ℃.The weight that finally obtains acid hydrolysis residue is 2.0 * 10
3kg (water-content 65% left and right, the over dry content of hemicellulose is 10.74%, cellulosic over dry content is 50.93%, the over dry content of xylogen is 33.84%), final pentose solution is 8.0 * 10
3kg, pentose concentration is 3.32%, the extraction yield of hemicellulose is 78%.
(2) alkaline solution extracts alkali lignin
By the acid hydrolysis residue obtaining in the present embodiment step (1), according to the method for embodiment 2 steps (2), carry out alkaline solution processing, difference is, liquid-solid volume ratio is 20: 1, the concentration of sodium hydroxide is 0.8%, and the temperature that alkaline solution is processed is 100 ℃, and the time is 2 hours.Finally obtain 1.64 * 10
3kg alkaline hydrolysis residue (water ratio is 65% left and right) and 0.49 * 10
3kg alkali lignin concentrated solution, and reclaim 14.53 * 10
3kg alkali lye.The solid content of this concentrated solution is 25.2% after measured, and the alkali lignin content of concentrated solution is 23.8%, and the content of the however, residual base of concentrated solution is 0.8%, and the ash oontent of concentrated solution is 1.4%; And the rate of recovery of alkali is 70%, the extraction yield of alkali lignin is 46%.
(3) cellulase hydrolysis alcohol prepared by fermenting
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 the described alkaline solution of the present embodiment step (2) and process whole residues of obtaining 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 5 days, whole enzymolysis process is without pressurize.Obtain 1.09 * 10
3kg enzymolysis residue (water ratio is 65% left and right), also obtains the solution of glucose, and quality is 7.76 * 10
3kg, concentration is 2.51%, cellulosic extraction rate reached 52%.
(4) circular treatment
Whole enzymolysis residues in step (3) are returned in step (2), after merging with new acid hydrolysis residue (another batch of acid hydrolysis residue that corn cob obtains after step acid hydrolysis), carry out again alkaline solution processing, after alkaline solution is finished dealing with, carry out again the cellulase hydrolysis of step (3), and then enzymolysis residue is returned in step (2), again merge with new acid hydrolysis residue, so can form circular treatment.
Adopt aforesaid method to 10.06 * 10
3kg corn cob is processed, and the extraction yield that finally obtains the hemicellulose of corn cob is 78%, and cellulosic total extraction yield is 86%, and total extraction yield of xylogen is 86%.
Embodiment 5
(1) N level acid hydrolysis
Technique and method be with embodiment 1 step (1), and difference is, raw material is 1.11 * 10
3the Wheat Straw of kg (mass component forms: moisture 10.1%, Mierocrystalline cellulose 44%, hemicellulose 22.2%, xylogen 17%, other 6.7%), acid solution is the sulfuric acid of 0.6 % by weight, every grade of acid-hydrolyzed time is 1 hour, the acid-hydrolyzed temperature of the first step is 150 ℃, the acid-hydrolyzed temperature in the second stage is 125 ℃, and the acid-hydrolyzed temperature of the third stage is 100 ℃.The weight that finally obtains acid hydrolysis residue is 2.15 * 10
3kg (water-content 65% left and right, the over dry content of hemicellulose is 6.56%, cellulosic over dry content is 60.05%, the over dry content of xylogen is 23.48%), final pentose solution is 7.85 * 10
3kg, pentose concentration is 2.52%, hemicellulose extraction yield is 80%.
(2) alkaline solution extracts alkali lignin
The acid hydrolysis residue obtaining in the present embodiment step (1) is carried out to alkaline hydrolysis according to the processing method of embodiment 2 steps (2); Finally obtain 1.9 * 10
3kg alkaline hydrolysis residue (water ratio is 65% left and right) and 0.32 * 10
3the alkali lignin concentrated solution of kg, and reclaim 4.29 * 10
3kg alkali lye.The solid content of this alkali lignin concentrated solution is 26.1% after measured, and alkali lignin content is 24.5%, and the content of however, residual base is 0.5%, and ash oontent is 1.6%; And the content of alkali is 2.05% in the alkali lye reclaiming, and the rate of recovery of alkali is 78%, and the extraction yield of alkali lignin is 42%.
Alternatively, 10% sulphur acid for adjusting pH value to 3 for the alkali lignin concentrated solution obtaining can be filtered to washing and the dry alkali lignin solid that obtains.
(3) cellulase hydrolysis
Get the present embodiment step (2) alkaline solution and process the whole alkaline hydrolysis residues that obtain, according to the method for embodiment 1 step (3), carry out cellulase hydrolysis, obtain 1.24 * 10
3kg enzymolysis residue (water ratio is 65% left and right), also obtains glucose solution, and quality is 5.32 * 10
3kg, concentration is 4.32%, cellulosic extraction yield is 47%.
(4) circular treatment
Whole enzymolysis residues that step (3) is obtained return to step (2) and carry out alkaline solution processing for the second time, and alkaline solution processing is for the second time identical with the condition that alkaline solution step in the present embodiment (2) Suo Shu is processed; Obtain 1.0 * 10
3kg is alkaline hydrolysis residue (water ratio is 65% left and right) and 0.35 * 10 for the second time
3kg alkali lignin concentrated solution, in alkali lignin concentrated solution, the content of alkali lignin is 23.8%; The extraction yield of alkali lignin is 43% for the second time.
The described residue of alkaline hydrolysis is for the second time carried out to enzymolysis for the second time, and the condition of enzymolysis is identical with the condition of enzymolysis described in step in the present embodiment (3) for the second time; Obtaining quality is 2.81 * 10
3kg, the glucose solution that concentration is 6.6%, cellulosic extraction yield is 38% for the second time.
In sum, the extraction yield of hemicellulose is 80%, and cellulosic total extraction yield is 85%, and total extraction yield of xylogen is 85%.
Embodiment 6
(1) acid hydrolysis
By 10.6kg corn cob, (mass component forms: moisture 6.12%, Mierocrystalline cellulose 35.19%, hemicellulose 32.1%, xylogen 23.7%, other is 2.95% years old, lower same) smash, wash dedusting with water, then with 80kg sulphuric acid soln, be hydrolyzed, the mass concentration of sulphuric acid soln is 1%, acid-hydrolyzed temperature is 120 ℃, 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, (water content is 65% finally to obtain 19.61kg acid hydrolysis residue, the over dry content of hemicellulose is 15.89%, the over dry content of xylogen is 31.75%, cellulosic over dry content is 47.78%) and 80.37kg pentose solution, the concentration of pentose solution is 2.88%.The extraction yield of hemicellulose is 68%.
(2) alkaline solution extracts alkali lignin
By obtaining all acid hydrolytic residue in the present embodiment step (1), mix with sodium hydroxide solution, liquid-solid volume ratio is 5: 1, the concentration of sodium hydroxide is 3%, be warming up to 70 ℃, boiling alkaline hydrolysis through 1 hour, separation obtains alkaline hydrolysis residue and alkali lignin solution, with 10kg water, cleans described alkaline hydrolysis residue, and scavenging solution and described alkali lignin solution merge; Finally obtain 16.52kg alkaline hydrolysis residue (water content is 65% left and right) and 34.66kg alkali lignin solution, the content 2.92% of xylogen in alkali lignin solution, alkali lignin extraction yield is 40%.
(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 the described alkaline solution of step (2) and process whole residues of obtaining as cellulosic substrate, according to the cellulosic addition of 15FPU/g, add cellulase, cellulosic substrate consumption is 125g/L, in temperature, be that 48 ℃, pH are 5.0, under the condition of mixing speed 100rpm, enzymolysis transforms 3 days, and whole enzymolysis process is without pressurize.Finally obtaining enzymolysis residue is 12.13kg (water content is 65%), also obtains glucose solution, and its quality is 46.5kg, and concentration is 3.32%, cellulosic extraction rate reached 41%.
(4) circular treatment
Whole enzymolysis residues that step (3) is obtained return to step (2) and carry out alkaline solution processing for the second time, and alkaline solution processing is for the second time identical with the condition that alkaline solution step in the present embodiment (2) Suo Shu is processed; Obtain 9.65kg alkaline hydrolysis residue (water ratio is 65% left and right) and 20.82kg alkali lignin solution for the second time, in alkali lignin solution, the content of alkali lignin is 4.01%; The extraction yield of alkali lignin is 33% for the second time;
The described residue of alkaline hydrolysis is for the second time carried out to enzymolysis for the second time, and the condition of enzymolysis is identical with the condition of enzymolysis described in step in the present embodiment (3) for the second time; Obtaining quality is 27.01kg, the glucose solution that concentration is 4.16%, and cellulosic extraction yield is 30% for the second time.
In sum, the extraction yield of the hemicellulose of corn cob is 68%, and cellulosic total extraction yield is 71%, and total extraction yield of xylogen is 73%.
Comparative example 1
(1) N level acid hydrolysis
Method is with embodiment 1 step (1), and temperature when difference is the 1st, 2 and 3 grades of acid hydrolysiss is identical numerical value, and the numerical value of the rate of loss of the extraction yield of hemicellulose, cellulosic rate of loss and xylogen is in Table 1:
Table 1
Comparative example 2
Method is with embodiment 5 steps (1), and difference is that the 1st, 2 and 3 grades of acid-hydrolyzed temperature are identical numerical value, and the numerical value of the rate of loss of the extraction yield of hemicellulose, cellulosic rate of loss and xylogen is in Table 2.
Table 2
Comparative example 3
The acid hydrolysis residue of getting in embodiment 2 steps (1) carries out alkaline solution processing, method is with embodiment 2 steps (2), difference is: liquid with film device carry out there is no thin up after separated concentrated, concentrated step, the rate of recovery table 3 of content, ash oontent and the alkali lye of the however, residual base of the extraction yield of alkali lignin, alkali lignin concentrated solution again:
Comparative example 4
The acid hydrolysis residue of getting in embodiment 2 steps (1) carries out alkaline solution processing, method is with embodiment 2 steps (2), difference is: the temperature that alkaline solution is processed is 170 ℃, the rate of recovery table 3 of content, ash content and the alkali lye of the however, residual base of alkali lignin extraction yield, alkali lignin concentrated solution:
Table 3
Comparative example 5
Technique and method are with embodiment 3, difference is that step (3) cellulase hydrolysis cellulase used is commercially available cellulase (jade of the He family Bioisystech Co., Ltd, 4w unit), only carry out primary fiber element enzymolysis, do not carry out the circulation technology of step (4), obtaining quality is 5.0 * 10
3the glucose solution that kg, concentration are 3.0%.Cellulosic extraction yield is 40%.
Test case 1
In the phenol of 10Kg, the alkali lignin concentrated solution that adds respectively 30Kg embodiment 2 and comparative example 3,4 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 2 and comparative example 3,4 makes respectively lignin modification resol, and its performance index are tested by the following method, and property indices is listed in table 4:
The mensuration of resol solid content: carry out according to HG/T 2711.
The mensuration of the viscosity of resol: carry out according to HG/T 2712.
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/T 2501.
The performance index of the modified phenolic resins of table 4 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.
In each embodiment, only with amplitudes such as temperature, be reduced to example above, but according to principle of the present invention and experiment test, the amplitude such as non-reduces also can realize object of the present invention, does not repeat them here.
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 (13)
1. a method of comprehensive utilization for lignocellulose biomass, is characterized in that comprising the following steps:
(a) lignocellulose biomass is carried out to acid hydrolysis, after separation, obtain pentose solution and acid hydrolysis residue;
(b) with alkaline solution, process described acid hydrolysis residue, thereby extract alkali lignin;
(c) use cellulase to process to alkaline solution described in step (b) the alkaline hydrolysis residue obtaining and carry out enzymolysis, obtain glucose solution and enzymolysis residue;
(d) after step (c) completes, by the described enzymolysis residue obtaining return step (b) carry out alkaline solution processing or described enzymolysis residue and new acid hydrolysis residue are merged after carry out again step (b) alkaline solution process, then carry out successively step (c) and (d), so circulation, thereby further extract xylogen and carry out cellulase hydrolysis
Wherein, in described step (a), described acid hydrolysis is the acid hydrolysis of N level, the acid-hydrolyzed reactor of N level is end to end, one of them reactor is made as to the first step, last is made as N level, the acid solution of new preparation adds in first step acid hydrolytic reaction still, the acid solution that first step acid hydrolytic reaction still is discharged adds in the acid hydrolytic reaction still of the second stage, the acid solution of discharging in the acid hydrolytic reaction still of the second stage adds in third stage acid hydrolytic reaction still, successively sequentially, until the acid solution that N-1 level acid hydrolytic reaction still is discharged adds in N level acid hydrolytic reaction still, the acid solution that N level acid hydrolytic reaction still is discharged is final pentose solution, take out the acid hydrolysis residue in first step acid hydrolytic reaction still, then pack new lignocellulose biomass raw material into, then using first step acid hydrolytic reaction still as N level acid hydrolytic reaction still, using second stage acid hydrolytic reaction still as first step acid hydrolytic reaction still, third stage acid hydrolytic reaction still is as second stage acid hydrolytic reaction still, until N level acid hydrolytic reaction still is as N-1 level acid hydrolytic reaction still, reaction is again hydrolyzed, so hydrolysis moves in circles and can realize the continuous hydrolysis of lignocellulose biomass,
Wherein, the acid-hydrolyzed temperature of the described first step is 100-150 ℃, and every grade is reduced 5-25 ℃ step by step subsequently, and N is more than or equal to 2 integer.
2. method according to claim 1, is characterized in that: the acid-hydrolyzed temperature of the first step is 120-140 ℃, and every grade is reduced 10-20 ℃ step by step subsequently.
3. method according to claim 1 and 2, is characterized in that: the integer that described N is 3-5.
4. method according to claim 3, is characterized in that: the concrete steps of described step (b) are:
(I) processes described acid hydrolysis residue with alkaline solution makes lignin dissolution wherein in alkaline solution;
(II) then filter, wash and obtain solid and liquid;
(III) is by separated, the concentrated alkali lignin solution that obtains of gained liquid process film device.
5. method according to claim 4, is characterized in that: in described step (III), also comprises the described concentrated alkali lignin solution obtaining dilute with water again, and then concentrated step.
6. according to the method described in claim 4 or 5, it is characterized in that: in described step (III), also comprise the alkali lignin solution process neutralization obtaining, filter and be dried, obtain the step of alkali lignin solid.
7. method according to claim 6, 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.
8. method according to claim 7, is characterized in that: described alkaline solution is processed and carried out at 40-100 ℃.
9. method according to claim 8, is characterized in that: in described alkaline solution processing, liquid-solid volume ratio is 5:1-20:1.
10. according to the method described in any one in claim 7-9, it is characterized in that: in described alkaline solution processing, the concentration of alkaline solution is 0.8-5 % by weight.
11. methods according to claim 10, is characterized in that: the time that described alkaline solution is processed is 1-6 hour.
12. methods according to claim 11, is characterized in that: described cellulase is for being cultivated the cellulase obtaining by a penicillium, 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 CCTCC M 2011195.
13. methods according to claim 12, 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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| 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 |
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