CN101326326A - New catalystic reactor method for producing commercial grade pulp, native lignin and single cell protein - Google Patents
New catalystic reactor method for producing commercial grade pulp, native lignin and single cell protein Download PDFInfo
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- CN101326326A CN101326326A CNA2005800522284A CN200580052228A CN101326326A CN 101326326 A CN101326326 A CN 101326326A CN A2005800522284 A CNA2005800522284 A CN A2005800522284A CN 200580052228 A CN200580052228 A CN 200580052228A CN 101326326 A CN101326326 A CN 101326326A
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- lignin
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- lignocellulosic material
- dipping
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C1/00—Pretreatment of the finely-divided materials before digesting
- D21C1/04—Pretreatment of the finely-divided materials before digesting with acid reacting compounds
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C11/00—Regeneration of pulp liquors or effluent waste waters
- D21C11/0007—Recovery of by-products, i.e. compounds other than those necessary for pulping, for multiple uses or not otherwise provided for
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C3/00—Pulping cellulose-containing materials
- D21C3/02—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate processes
Abstract
A continuous and batch system to produce cellulose, native lignin and unicellular protein from any form of vegetation in a closed process. The biomass is mixed in the impregnate solution of nitric acid and/or ammonium hydroxide and water. After a period of time at room temperature and atmospheric pressure the chemical solution is recycled. The biomass is moved to the reactor and heated. Evaporated impregnate is recovered via absorption tower and recycled back to chemical solution. The biomass is moved to an alkaline solution, then cooled to separate pulp from black liquor. The black liquor is pumped to a separation tank and is treated to precipitate lignin. The solution is filtered to separate sweet liquor and lignin. The lignin is dried and the sweet liquor is fermented to produce unicellular protein.
Description
Technical field
The present invention relates to a kind of processing method of lignocellulosic material, particularly relate to the acid-catalyzed hydrolysis that makes the dipping wood chip reach the depolymerization of lignin matrix part, and distillation, the concentrated and recovery of acid catalyst subsequently.
Background technology
The processing method of lignocellulosic material often needs high temperature and high pressure to guarantee the chemical reaction course of enough speed in the prior art.Therefore, high-pressure bottle that must be specific and special equipment stand described exacting terms.This makes the assembling of treatment facility and maintenance very expensive, and operation is also very expensive, in addition the energy requirement height.
In addition, need strong chemicals usually so that produce the oxidation or the reduction reaction of wishing.Chemicals corrodes equipment and lignocellulosic material, will increase the maintenance cost of equipment conversely again.In case use, chemicals must be removed, this will produce potential environmental hazard and pollution.Even the water that uses in processing procedure also can be contaminated, thus need prudent disposal, with anti-pollution and environmental nuisance.Then, must buy fresh chemicals again to replenish that part of chemicals that loses in the processing procedure.
Mounted most of treatment facility is even expensive sophisticated equipment also only can be used for handling the vegetable material of limited kinds.Different vegetable materials needs different treatment conditions and chemicals, and sometimes also needs different processing methods, this means if not exclusively change production line, then can not handle other vegetable material.If can handle the various plants material, and need not to change or change equipment, that is ideal.
Therefore, an object of the present invention is to provide a kind of processing method of lignocellulosic material, described method has not only overcome above-mentioned restriction but also other desirable feature is provided.
This purpose of the present invention and other purposes by the reference summary of the invention and subsequently DETAILED DESCRIPTION OF THE PREFERRED will be understood.
Summary of the invention
The present invention relates to a kind of by any type of plant in an airtight process production of cellulose, native lignin and SCP continuously and batch system.
Hydrolysis catalysis reaction device method (Catalytic Reactor Process, but CRP) manufacturer's grade paper pulp, and can from the lignin of native form, isolate sweet liquid (carbohydrate and hemicellulose)---under high temperature or the unfavorable process conditions not by the native lignin of sex change.Convert sweet liquid to SCP again, the latter is convertible into many different products.The water of described method and catalytic chemistry product are recovered utilization.
The key of CRP method is the acid-catalyzed hydrolysis of dipping wood chip.Acid catalyst makes the lignin matrix part depolymerization in the chemical reactor, follows by the distillation of acid catalyst, concentrated and recovery, and the recovery of native form lignin.A large amount of art methods is all used oxidation/reduction chemical reaction mechanism in this area.This fundamental difference of reaction mechanism makes the CRP method have significant advantage.
For example, in the aqueous solution of nitric acid and/or ammonium hydroxide, plant is flooded.Make chemical solution recirculation after a period of time at normal temperature and pressure.Then living beings are moved in the catalytic reactor and heating.The maceration extract that evaporates reclaims by adsorption tower, and is back in the chemical solution again.Before cooling, living beings are moved in the alkaline solution so as from black liquor separating pulp.Paper pulp can be handled as required, so that produce vendible product.Black liquor is pumped to knockout drum handles, so that the lignin precipitation.Described solution is filtered to isolate sweet liquid and lignin.Dry lignin, and make sweet liquid fermentation with the manufacture order cell protein.
This method can be used the plant of any kind of, comprises leaf wood, needlebush, shrub, cereal, careless class or the like.This method can be used (pointing out that in the patent of having examined so far some raw material can not industrialization or can not specifically be implemented) as unique raw material with sawdust.
The quality and quantity of the lignin that produces has determined the reaction condition of whole process.A tangible advantage is to have eliminated " drying " raw material.In fact, can use green material, and for the acid-catalyzed hydrolysis of the native lignin polymer that depends on required paper pulp, lignin and sweet liquid quality or even preferably.
The CRP pulping process had not both required the impressed pressure in what stage in office, did not require the temperature range that approaches traditional sulfate pulp-making method yet.Basically all be lower than 90 ℃ and reaction system is not applied external pressure in the temperature in described each stage of method.
The CRP pulping process is an enclosed system, and in fact all chemicals that use in this individual system all are recovered reuse.Used water reclaims, filters reuse with the form that can sell byproduct or discharges as steam in this pulping process.The steam of discharging can be this pulping process provides energy, avoids thus even the loss of very a spot of loss of water and potential energy source.The recovery of catalytic chemistry product has solved the problem of high chemicals cost in the circulation of each pulping process.Before being introduced in the pulping process once more, only need a spot of chemicals to make concentration return to the concentration that each reclaims chemicals.The recovery of various chemicals does not need to consume external energy (this and sulfate pulp factory present recycle section different).
By using this novel method, obtain following benefit:
1. can use wet feed material---because moisture is necessary for hydrolysis, therefore need not wood chip is carried out drying.
2. use low temperature, low pressure and the input of energy seldom to be hydrolyzed.
3. use weak acid and weak base, farthest reduced cost of material and the degraded that has reduced end-product.
4. acid catalyst is distilled and recirculation, enables to carry out sealing and circulating.
5. the essentially no pollution of this chemical reactor pulping process.
6. this chemical reactor pulping process makes natural Klason lignin have high yield.
7. the paper pulp yield height of the chemical cellulose of chemical reactor.
8. the sweet liquid of post precipitation is suitable for the fermentation of SCP.
9. it is scalable that this chemical reactor method is utilized suitable mixer design, and when the operation cost with plan combines, in recoverable construction investment in two years.
10. this chemical reactor method efficient is very high, and its cost only is half of typical sulfur acid sulfite pulp factory.
This method can be used low especially bronsted lowry acids and bases bronsted lowry concentration at dipping and boiling stage, and low especially temperature.
Because the CRP pulping process is a chemicals or the moisture enclosed system to the discharging of environment near-zero, therefore, adopts the pulp mill of this method to satisfy easily and surmount present environment protectment protection.Free of contamination pulp mill also may obtain huge earning potential under EPA carbon dioxide pollution credit system.Production provides flexibility to paper pulp can to handle the ability of various plants under the situation of not changing machinery.At present, each pulp mill is designed to produce particular types paper pulp and adopts particular types timber as raw material.In addition, most pulp mills need satisfy the wood chip of the strict specification of quality.These restrictions have been avoided by the present invention.
Sell paper pulp separately, can realize the economic feasibility of CRP pulping process.Other benefit is potential EPA credit and produces native lignin product and the SCP of selling to other user.It is pointed out that the SCP from plant source does not contain any BSE pathogen, will be satisfying of feeding at present ox that the human consumption uses and the preferred feed of other domestic animals.
On the one hand, the present invention relates to a kind of method of producing paper pulp and lignin by lignocellulosic material, described paper pulp comprises cellulose, described method comprises: lignocellulosic material is contacted with acidic aqueous solution so that lignocellulosic material is flooded, and described acidic aqueous solution comprises the acid of about 1 0-40% weight; Divide two stage heating lignocellulosic materials, time of carrying out first heating period is enough to make the lignin depolymerization in the lignocellulosic material, but can not make cellulose or lignin degradation in the lignocellulosic material basically, second heating period carried out under the boiling point of described acid or higher temperature, so that distill out acid; Under the heating lignocellulosic material is contacted so that lignin is dissolved in this alkaline solution with alkaline aqueous solution, stayed black liquor; From black liquor, take out paper pulp; Enough acid is added in the black liquor so that the lignin precipitation; And from black liquor, take out lignin.
On the other hand, the present invention relates to a kind of processing method of lignocellulosic material, comprising: make lignocellulosic material be immersed in impregnation steps in the maceration extract; Make maceration extract dehydration, filtration, enrichment and be recycled to first recirculation step of impregnation steps; In catalytic reaction chamber, the lignocellulosic material that soaked is stirred and be heated to the above temperature of maceration extract evaporation point, produce the maceration extract vaporized and the catalytic reaction step of lignin thus; Make the maceration extract of having vaporized concentrate and be recycled to second recirculation step of described saturation process; In the presence of black iron (black iron) and alkaline solution, in boiling vessel, lignin is stirred to produce the boiling step of paper pulp and concentrated black liquid; Paper pulp is dewatered, washing and the dry treatment step of making dry pulp and rare black liquor thus; Make rare black liquor be recycled to the 3rd recirculation step of boiling step; Make concentrated black liquid cooling and in the presence of acid solution, stir, produce sweet liquid thus and be settled out the separating step of native form lignin; Sweet liquid is filtered so that take out the filtration step of native form lignin; Sweet liquid is added in the bacterium of fermentation tank, produces fermentation step thus as the SCP of tunning.Maceration extract can be salpeter solution or Ammonia.
On the other hand, the present invention relates to the treating apparatus of lignocellulosic material, described device comprises the dipping charging aperture that lignocellulosic material and maceration extract is conveyed into impregnating autoclave, and described impregnating autoclave comprises the dipping discharging opening; Catalytic reaction chamber is connected with impregnating autoclave by the dipping discharging opening, and described catalytic reaction chamber comprises first agitator and catalysis discharging opening; The boiling vessel unit is connected with catalytic reaction chamber by the catalysis discharging opening, and described boiling vessel unit comprises second rabbling mechanism and boiling vessel discharging opening; The lignin separator is connected with the boiling vessel unit by the boiling discharging opening, and described lignin separator comprises the 3rd rabbling mechanism and separator discharging opening; And fermentation tank is connected with the lignin separator by the separator discharging opening.
On the other hand, described impregnating autoclave can comprise the recirculation discharging opening that makes maceration extract recirculation and be back to impregnating autoclave.On the other hand, described boiling vessel unit can comprise the maceration extract upgrading unit that makes described maceration extract recirculation and be back to described impregnating autoclave.
On the other hand, the present invention relates to the SCP of utilizing said apparatus or said method to produce.On the other hand, the present invention relates to the native form lignin that utilizes said apparatus or said method to produce.Foregoing only is wide in range explanatory memorandum, and only relates to some aspect of the present invention.Described content does not also mean that limitation of the invention or regulation.Others of the present invention will be understood by reference DETAILED DESCRIPTION OF THE PREFERRED and claims.
Description of drawings
The preferred embodiments of the present invention will be described with reference to the accompanying drawings, wherein:
Fig. 1 is the schematic diagram according to the inventive method preferred embodiment used unit;
Fig. 2 is acid catalyzed hydrolysis mechanism;
Fig. 3 is the flow chart and the mass balance of paper pulp, lignin and protein in this catalytic reactor method (nitric acid);
Fig. 4 is the flow chart and the mass balance of paper pulp, lignin and protein in this catalytic reactor method (ammonium hydroxide);
Fig. 5 is the hot plate calibration curve that is used for the CRP test; With
Fig. 6 is by a series of pictures of different fibre sources by the fiber of CRP acquisition.
The specific embodiment
Fig. 1 shows the schematic diagram of the inventive method preferred embodiment.To place impregnation chamber 4 with maceration extract from the wood chip of charging aperture 2.After making the chip impregnation appropriate time, remove unnecessary maceration extract and clean, as being undertaken by filter mechanism 6; Be collected in then in the recycling can 10.Afterwards, for example carry out enrichment and be back in the impregnation chamber 4 by pump 12.Meanwhile, by suitable means, impregnated wood chip is delivered in the catalytic reactor 20 as spiral conveying mechanism 8.For 20 the conveying of control wood chip, can use various mechanisms from impregnation chamber 4 to catalytic reactor.In a preferred embodiment, storage tank 14 is preserved impregnated wood chip till they can be delivered in the measurement mechanism 18 by funnel 16.The charging rate that measurement mechanism 18 control wood chips enter catalytic reactor 20.
In catalytic reactor 20, by heater 22 wood chip is heated above the maceration extract evaporating temperature, but is enough to be low to moderate the temperature that the performance of formed lignifying compound is without prejudice.In addition, also wood chip is stirred, to guarantee the thorough heating of living beings.
From catalytic reactor 20, remove the maceration extract of devaporation by the mechanism as pump 24, and be collected in condensation chamber or the absorption tower 26.Dipping is condensed and is back in the recycling can 10 so that the utilization again in impregnation chamber 4.
Discharging opening 28 is conveyed into the living beings after the catalysis in the boiling vessel 30, mixes with alkaline solution in living beings described in the boiling vessel.In the presence of black iron (black iron) to this mixture heated and stirring, thereby produce black liquor and paper pulp.
From the paper pulp of boiling, remove unnecessary black liquor by the mechanism as squeezer 32.Be collected in the black liquor of removing in jars 34 and for example be back to boiling vessel 30 by pump 36.The paper pulp that squeezed is for example handled by wash engine 38 as required.
Black liquor is delivered in the lignin jar 40 by boiling vessel 30, is cooled, stirs also acidifying therein and form sweet liquid and lignin thus so that be settled out lignin.
Make sweet liquid and lignin by separator,, wherein, collect lignin and be used for further processing as filter 42.Sweet liquid enters fermentation tank 44 by filter 42.
In fermentation tank 44, bacterium is added in the sweet liquid to produce SCP, it can be handled again as required.
The method of the preferred embodiment of the present invention will be described below.Described method is schematically used the flowcharting of Fig. 3 and 4, and it uses nitric acid maceration extract and ammonium hydroxide maceration extract respectively.
1. the plant class is cut into the appropriate length of suitable with the current commercially available wood plate size that uses, leaf wood and needlebush, and makes raw material.Yet,, therefore, can use the littler wood chip of size because the fibre length of using in the CRP method that more weak chemicals and lower temperature produced is longer.
2. in the impregnation chamber 4 of raw material being packed into and carry out saturated with maceration extract.Maceration extract can be nitric acid, ammonium hydroxide and/or this two kinds of materials.For example, if raw material are leaf woods and use nitric acid that then wood chip can flood 18 hours in 15% nitric acid.If raw material are needlebush or other plant material, be immersed in 12% the nitric acid 16 hours.If maceration extract is an ammonium hydroxide, then wood chip is immersed in 10% the ammonium hydroxide, irrelevant with raw material.
3. unnecessary maceration extract is discharged, filter and make it to be returned to original concentration so that in recycling can 10, reuse.
With impregnated materials conveyance to the catalytic reactor 20 of pH2-5.In this stage, temperature maintenance is between 60 ℃ and 85 ℃, and the insulation maximum duration is 80 minutes.Catalytic reactor 20 being remained in this optimum temperature and the time range, to producing high yield and high-quality end-product, especially produce unmodified lignifying compound, is very important.If make the processing time of described material exceed Best Times, the oxidation of too much material will take place so, rather than the preferred catalyzing hydrolysis of lignin polymer, therefore, will produce inhibitory action to each stage subsequently.Impregnated material heating is exceeded optimum temperature yield will be descended, and the lignin state of hope is changed (causing inferior gel-like prod).The time that continues under optimum temperature is 10-80 minute, specifically depends on used raw material.The chemical reaction that takes place during the catalytic reaction step as shown in Figure 2.
In impregnated material heating process, maceration extract discharges with vapor form, reclaims and be delivered to condensation chamber or absorption tower 26, collects therein so that utilize again.After the enough time, lignin is by the molecular state of catalyzing hydrolysis for wishing, now, raw material prepare to be delivered to the alkaline bath stage.
In this catalytic stages, it is very important stirring in large-scale reactor, otherwise will not have time enough that impregnated whole material is thoroughly heated before the stage proceeding to alkaline boiling, will influence the yield and the quality of end-product thus.
5. caustic soda is added into, the material in boiling vessel 30 20 that pass through from catalytic reactor.Caustic soda concentration is as follows:
If raw material is a leaf wood, use 4L, 20% NaOH/200L water; If raw material is needlebush or other plant class, use 4L, 15% NaOH/200L water.
Alkaline bath is heated to 60-85 ℃ optimum temperature range, is incubated 60 minutes.In this alkali stage of pH9-12, in the presence of black iron plate, mixture is stirred, and from black liquor, isolate paper pulp.Make paper pulp by pulp screen and squeezer, so that squeeze out black liquor.Black liquor recirculation is got back in the alkaline boiling device.After all paper pulp take out from alkaline bath, paper pulp is washed and drying, and make residual black liquor be back to boiling vessel 30, be delivered to then in the lignin jar 40.
By method of the present invention, the picture that utilizes the fiber that various raw material obtain as shown in Figure 6.In this stage, the performance of CRP paper pulp is as shown in table 1.
Table 1:CRP paper pulp
*Analytical structure
Composition sample 1 sample 2
Chemical cellulose % 86.5 85.7
Beta cellulose % 1.3 4.1
Gamma-cellulose % 12.2 10.2
Kappa number 51.6 44.5
Lignin content % (calculated value) 7.74 6.68
Before test, make
*Sample carries out the chloric acid salinization, calculates the result according to the weight of chloric acid salinization sample.All results all calculate with respect to over dry base sample weight.α, β and gamma-cellulose: according to ESM 035B (benchmark: TAPPI n03).Kappa number: according to ESM 091B (benchmark: TAPPI T236).
6. black liquor is fed the temperature range (this is very important for the native state that keeps lignin) that also is cooled to 43-50 ℃ in the lignin jar 40 rapidly.To this, if maceration extract is a nitric acid, the sulfuric acid with 10% is added in the black liquor; If maceration extract is an ammonium hydroxide, add 12% hydrochloric acid.The ratio of sulfuric acid and black liquor be 2 liters of acid to 200 liters of black liquor, pH is 2-5.Start agitator, so that before mixture is cooled to below 43 ℃, from black liquor, be settled out lignin.Separating treatment needs about 1 hour.
7. from lignin jar 40, the lignin mixture of sweet liquid and precipitation is delivered in the fermentation tank.Sweet liquid is by filter 42, and the lignin powder is stayed above the filter.Native lignin is delivered to drier, carries out drying with 43-50 ℃ temperature range.The deviation of described temperature range will be destroyed the state of native lignin.The performance of native lignin is as shown in table 2.
The analysis result of table 2:CRP lignin
Composition sample 1 sample 2
Klason lignin % 83.0 76.7
8. a kind of bacterium (torula) is added in the sweet liquid in the fermentation tank 44, to activate sweat.Fermentation filters out SCP after finishing, dry and packing, and perhaps washing reduces the pH value and is used for other products.
9. recirculation after treatment is back in the technology of the present invention to the residual water in the sweat.
Agitator is used for catalytic reactor 20 and boiling vessel 30, and with regard to yield and quality that end-product is wished, using agitator is crucial for obtaining optimum.
In catalytic reactor 20, use agitator, so that reach and maintain the optimum temperature range of lignin generation depolymerization.Optimum temperature must reach as quickly as possible, with avoid we do not wish the lignin oxidation that occurs.Described oxidation will provide the chance that begins to form chemicals such as ketone, aldehyde to the lignifying compound, and described these chemical substances all are undesirable.In addition, the oxidation of lignin also will provide broken site, make between the lignin polymer to take place crosslinkedly, and this is another unwanted results.Oxidation also will cause the low yield of native lignin and sweet liquid, specifically decide according to the degree of oxidation reaction in the catalyst chamber.The design of agitator is according to adopting the batch process plant, still supplies with plant continuously and decides.Stirring not only is used for making the living beings of dipping to reach temperature rapidly, but also makes living beings itself begin to decompose.
When supplying with plant continuously, the agitator in the catalytic reactor 20 also will be delivered to the living beings of flooding in alkaline bath or the boiling vessel 30 continuously.
In boiling vessel 30, agitator is used for obtaining optimum yields.If reaction, living beings will fully enter in the alkaline solution and can sink, the surface of wood chip will begin to carry out boiling.This will take lignin out of and enter in the alkaline solution from wood chip.If the time that lignin stops in the presence of NaOH is oversize, it will begin oxidation, produce unwanted results.With violent especially stirring wood chip is torn into littler fragment, this makes and can promptly use NaOH before a large amount of lignins begins oxidation.The result is, being attached to sodium molecule on the lignin polymer unwinds site, that lignin is become is water-soluble.
Agitator also makes optimum temperature range distribution homogeneous.
The operating condition of the inventive method is as follows.
For handling 60 kilograms pine sheet, 31.5 liters wood chip is flooded with the propylhomoserin solution that contains that comprises 27.5 liters of nitric acid and 4 liters of ammonium hydroxide.
After flooding 12 hours, the taking-up acid solution is used for recirculation subsequently, and wood chip is placed reactor so that at 75 ℃, the highest 80 ℃, carries out catalytic hydrolysis reaction in 90 minutes time; This is to consider, when the temperature that reaches 75 ℃ in the reaction time, gas will reclaim NOx in water or in the acid solution of circulation.
When reaction finishes, wood chip is entered in the alkaline bath so that make the wood chip delignification, wherein in the mixture of 315 liters of 4%NaOH, it is carried out preheating in 75 ℃.Delignification reaction is at about 80 ℃ and be up to 90 ℃ and carried out 90 minutes.Make mixture by filter so that before from black liquor, isolating cellulose, stop the heating, make it to be cooled to 75 ℃.
Black liquor is delivered in the lignin jar, it is stirred and adds the concentrated sulfuric acid carefully, reduce to till 3.0 up to the pH value.It is left standstill, then by filter so that from sweet liquid, isolate lignin.
The sweet liquid that filters out is delivered to can be to the fermentation tank that wherein adds bacterium, thereby produces SCP.
When this method finishes, lignin and cellulose are washed so that respectively too much acid and caustic soda are regained.The water that is used for the inventive method is the running water or the circulating water of standard.
Be the details of utilizing the inventive method to test below.The pH value of used bronsted lowry acids and bases bronsted lowry is listed in the table 3, and the calibration curve of used hot plate is tabulated in the table 4 and shown in figure among Fig. 5.
Table 3: the pH value of bronsted lowry acids and bases bronsted lowry---May 17
Acid: temperature ℃ pH
12% nitric acid 18.2 1.86
10% sulfuric acid 18.3 1.85
12% hydrochloric acid 18.3 1.90
Alkali: temperature ℃ pH
10% ammonium hydroxide 18.2 12.42
15% NaOH 18.2 13.23
Table 4: hot plate calibration curve---May 17
Design temperature ℃
1.0 35
1.5 42
2.0 52
2.5 60
3.0 64
3.5 69
4.0 73
4.5 78
5.0 83
5.5 90
6.0 97
Nitric-acid test:
May 19
To 500 milliliters of northern kahikatea basic units (Sun Seed-Son thing Special)---weight is to add 500 ml waters in 64.49 grams and soaked 15 minutes.Water is discharged.Now weigh with beaker, weight in wet base is 503.75 grams (Buchner funnel vacuumized 15 minutes).Beaker weight 390.21 grams deduct absorption moisture weight: the 113.54-64.49=49.05 gram.
At 11:10 on 19 morning of May, be poured in 700 milliliters of nitric acid.The temperature of wood chip and acid is 60 °F.
Retain 440 ml waters (from soaking wood chip).％H
2O＝49.05/113.54＝43.2％
Hot plate is arranged on 83 ℃ (182) or 1.8-1.6 (closing switch).
In 9:05, the nitric acid maceration extract is added in the Buchner funnel.Gravity drainage 30 minutes and soak time 21 hours 55 minutes were up to May 20.
May 20
After the dipping, wood chip (wetting) is weighed as 215.96 grams
215.96-113.54=102.4/215.96 * 100%=47.42% nitric acid
102.42 gram nitric acid
102.42 the volume of gram nitric acid is about 800 milliliters.
The mornings 10, point began distillation (being set at 5), and the pH value that has 605 milliliters of nitric acid to be discharged from-to discharge acid is lower than zero.
After 10 minutes, turn down 1.6.Use pure nitric acid.90 ℃-nitric acid of vapor (steam) temperature splashes in the collection beaker that 100 ml waters are housed.
Minute temperature
10 94-95℃
20 91℃
25 74℃
In the time of 25 minutes, measure wood chip temperature=194 (88.9 ℃)
Sample #1-with the nitric acid of 50 milliliters of discharges flood-pH is less than zero.
We reclaim 110 milliliters of nitric acid/water distillation amount-10 milliliter pure HNO
310 * 100%=9.09%
Minute temperature
30 68 ℃ of 83 ℃ of wood chips
60 70℃
70 70 ℃ of 86 ℃ of wood chips
80 70℃ 92℃
The first recovery distillate of sample #2-in the time of 25 minutes-reclaim first in 110 milliliters, 100 milliliters is that water and 10 milliliters are nitric acid.
Pour 10 milliliter 15% NaOH in 1 premium on currency (alkaline bath mixture)
The morning, 11:40-75 ℃ alkaline boiling device added wood chip, and setting value is 10 to stir-add 2 black iron short column bodies.
Sample #3-carried out reclaiming the second time distillate-100 ml water and 1.5 milliliters of nitric acid in the time of 80 minutes.
Yield-101.5 for the second time
12 black iron short column bodies of 12: 10-interpolation.
12: 25-add 90 milliliter 15% NaOH, 87 ℃ of temperature-hot plate is set reduced to 4.
The temperature of 1: 15 timesharing in afternoon is 96 ℃ (too hot).
From black liquor, filter out paper pulp.The black liquor amount is 920 milliliters.Collection obtains 40 milliliters of samples (sample #4).
Making black liquor cooling-temperature in cold bath is 44 ℃.
In black liquor, add 10 milliliter 10% sulfuric acid, so that be settled out lignin and filter-time is 1: 45 afternoon.
0.86 gram filter paper
Add 10 milliliter 10% sulfuric acid and filtration in addition again.
The acid amount of Tian Jiaing is 80 milliliter 10% a sulfuric acid for the third time, and the time is 3: 15 afternoon-cover and shelve and spend the night.
Used pulp washing water-1600 milliliter
The black liquor that is produced-1000 milliliter
May 21
Dry pulp 22.08 gram-light browns, coarse staple fibre
Filter paper #1-1.22 gram-lignin weight-0.36 gram
(tare weight 0.86 gram) #2-0.99 gram-lignin weight-0.13 gram
Shelving the back (9: 20 morning) of spending the night, 1000 milliliters of sweet liquid/lignin mixtures are carried out vacuum filtration.
Sweet liquid measure is 910 milliliters
The weight of liquid and filter paper is 3.95 grams
Lignin weight=3.95-0.86=3.09 restrains (hard and black block)
Total lignin amount=3.09+0.36+0.13=3.58 gram
Black liquor proportion-0.999
Sweet liquor ratio is heavy by-1.003
Nitric acid-May 20
In 100.04 fresh wood chips, add nitric acid-consumption about 300 milliliters (too much) of 700 milliliter 12%
The pine sheet (Riverside pine chips) of point-begin in afternoons 4 to the river bank flood-and make dipping temperature reach 66 °F from the wood chip and the silver of conveyer belt bottom.
It is 15 minutes that 10: 15 morning-discharge nitric acid obtains the 660 milliliters-acid discharge time.
(sample #6)-short column body weight 183.79 grams
In 10: 40 morning, wood chip is put into distillation mechanism.The wood chip temperature is that 72-hot plate setting value manually is transferred to 1.0-1.6.
37 ℃ of 140-vapor (steam) temperatures of 55 minutes-wood chip temperature at 10 o'clock in the morning
70 ℃ of 184-vapor (steam) temperatures of 05 minute-wood chip temperature at 11 o'clock in the morning
In 11: 05 morning, begin 80 minutes countdown.
76 ℃ of 190-vapor (steam) temperatures of 10 minutes-wood chip temperature at 11 o'clock in the morning
64 ℃ of 184-vapor (steam) temperatures of 25 minutes-wood chip temperature at 11 o'clock in the morning
64 ℃ of 183-vapor (steam) temperatures of 45 minutes-wood chip temperature at 11 o'clock in the morning
64 ℃ of 12 noons-184-vapor (steam) temperature of wood chip temperature
At 12 o'clock in afternoon, 05 minute-hot plate was set in 2.0 to distill out nitric acid
75 ℃ of 196-vapor (steam) temperatures of 10 minutes-wood chip temperature at 12 o'clock in afternoon
85 ℃ of 198-vapor (steam) temperatures of 20 minutes-wood chip temperature at 12 o'clock in afternoon
At 12 o'clock in afternoon, 30 minutes-wood chip temperature-vapor (steam) temperature was 87 ℃
Nitric acid amount (distillation is collected and obtained) is 105.5 (sample #7), pH=.70,5.5 milliliters of HNO
3
Afternoon 1, point was added into the wood chip of dipping in 80 ℃ the alkaline bath.
1: 05, add other 10 milliliter 15% NaOH
1: 10, add other 10 milliliter 15% NaOH
1: 15, add other 10 milliliter 15% NaOH
In the time of 1, temperature is 80 ℃
1: 10,74 ℃
1: 20,76 ℃
1: 30,85 ℃-to set value be 4
1: 40,85 ℃
1: 50,86 ℃
2 points, 85 ℃
2: 10,85 ℃-close agitator/heating
Be recovered to 830 milliliters of black liquor, collect sample # 8
Add 30 milliliters of sulfuric acid.In 2: 30 timesharing temperature is 36 ℃.
Leach paper pulp (in the long fiber pulp adhesion-yellow-1200 of 100/0-15% milliliter)
Washing
May 22
The yellow 40 milliliters of sample #9N of sweet liquid-740 after the filtration milliliter-shallow straw
The paper pulp-42.67 that obtains 100 ℃ of dryings restrains
10: 30 morning, lignin filter cloth (dried overnight)-1.6 gram
The mornings 11 point, lignin filter paper #1 (air dried overnight) 2.89-0.86=2.83 gram
11: 15 morning, lignin filter paper #2 (air dried overnight) 2.82-0.86=1.96 gram
11: 30 morning, lignin filter paper #3 (air dried overnight) 1.51-0.86=0.65 gram
-light brown lignin-gross weight 7.04 grams
-Whatman filter paper #4-filter cloth nylon high-count fabric (deriving from pilot plant)
Black liquor proportion-0.985
Sweet liquor ratio is heavy by-0.989
During running water proportion-20 ℃ 0.982
Those of ordinary skills should be understood that, the various variations of described preferred embodiment in the present invention only otherwise depart from the scope of the present invention all and can implement, described scope is suitably limited by claim.
Claims (13)
1. method of producing paper pulp and lignin by lignocellulosic material, described paper pulp comprises cellulose, described method comprises:
Lignocellulosic material is contacted with acidic aqueous solution so that this lignocellulosic material is flooded, and described acidic aqueous solution comprises about 10% acid to about 40% weight;
Divide two stages that lignocellulosic material is heated, time of carrying out first heating period is as the criterion the lignin depolymerization in the lignocellulosic material with under the situation that does not make cellulose in this lignocellulosic material or lignin degradation basically; Second heating period carried out so that distill out acid on the boiling point of acid or boiling point;
Under the heating lignocellulosic material is contacted with alkaline aqueous solution,, stay black liquor so that lignin is dissolved in this alkaline aqueous solution;
From described black liquor, take out paper pulp;
The acid of q.s is added in this black liquor, so that make the lignin precipitation; With
From described black liquor, take out lignin.
2. the processing method of a lignocellulosic material comprises:
Impregnation steps wherein is immersed in lignocellulosic material in the dipping solution;
First recirculation step, wherein said dipping solution is discharged from, filtration, enrichment, and is recycled in the described impregnation steps;
Catalytic reaction step, the lignocellulosic material of wherein said immersion are stirred and are heated to the temperature more than the described dipping solution evaporation point in catalytic reaction chamber, produce the dipping solution and the lignin of vaporization thus;
Second recirculation step, the dipping solution of wherein said vaporization are concentrated and are recycled in the described saturation process;
Boiling step, wherein said lignin are stirred in boiling vessel to form paper pulp and concentrated black liquid in the presence of black iron and alkaline solution;
Treatment step wherein dewaters to described paper pulp, and washing is also dry, produces dry paper pulp and rare black liquor thus;
The 3rd recirculation step wherein is recycled to described rare black liquor in the described boiling step;
Separating step, wherein said concentrated black liquid is cooled in the presence of acid solution and stirs, and produces sweet liquid thus and is settled out the lignin of native form;
Filtration step wherein filters to remove the lignin of described native form described sweet liquid; With
Fermentation step wherein is added into described sweet liquid in the bacterium in the fermentation tank, produces the SCP as tunning thus.
3. method according to claim 2, wherein said dipping solution is a salpeter solution.
4. method according to claim 3, wherein said salpeter solution comprises the acid of 10-30% weight.
5. method according to claim 2, wherein said dipping solution are Ammonia.
6. method according to claim 5, wherein said Ammonia comprises the ammonium of 10-30% weight.
7. SCP of producing by the method for claim 2.
8. the lignin of a native form of producing by the method for claim 2.
9. the treating apparatus of a lignocellulosic material comprises:
Lignocellulosic material and dipping solution are supplied to dipping charging aperture in the impregnating autoclave, and described impregnating autoclave comprises the dipping discharging opening;
By described dipping discharging opening and the tank connected catalytic reaction chamber of described dipping, described catalytic reaction chamber comprises first agitator and catalysis discharging opening;
By the boiling vessel unit that described catalysis discharging opening is connected with described catalytic reaction chamber, described boiling vessel unit comprises second rabbling mechanism and boiling vessel discharging opening;
By the lignin separator that described boiling vessel discharging opening is connected with described boiling vessel unit, described lignin separator comprises the 3rd rabbling mechanism and separator discharging opening; With
The fermentation tank that is connected with described lignin separator by described separator discharging opening.
10. device according to claim 9, wherein said impregnating autoclave further comprises: be used for the described dipping solution of recirculation and make it to be back to the recirculation discharging opening of described impregnating autoclave.
11. according to claim 9 or 10 described devices, wherein said boiling vessel unit further comprises: the maceration extract upgrading unit that is used for making described dipping solution recirculation and makes it to be back to described impregnating autoclave.
12. the SCP of utilizing the device of claim 9 to produce.
13. utilize the lignin of the native form that the device of claim 9 produces.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/CA2005/001862 WO2007065241A1 (en) | 2005-12-07 | 2005-12-07 | A novel catalytic reactor process for the production of commercial grade pulp, native lignin and unicellular protein |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102553701A Division CN101962919B (en) | 2005-12-07 | 2005-12-07 | Novel catalytic reactor method for manufacturer-grade paper pulp, native lignin and single cell protein |
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| Publication Number | Publication Date |
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| CN101326326A true CN101326326A (en) | 2008-12-17 |
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| CNA2005800522284A Pending CN101326326A (en) | 2005-12-07 | 2005-12-07 | New catalystic reactor method for producing commercial grade pulp, native lignin and single cell protein |
Country Status (7)
| Country | Link |
|---|---|
| EP (1) | EP1969175B1 (en) |
| CN (1) | CN101326326A (en) |
| AT (1) | ATE553246T1 (en) |
| AU (1) | AU2005338842B2 (en) |
| BR (1) | BRPI0520735B1 (en) |
| RU (1) | RU2383675C1 (en) |
| WO (1) | WO2007065241A1 (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102449231A (en) * | 2009-05-26 | 2012-05-09 | 日本制纸株式会社 | Method for digesting lignocellulosic material |
| CN103380247A (en) * | 2011-02-22 | 2013-10-30 | 安德里兹有限公司 | Method and apparatus to produce pulp using pre- hydrolysis and kraft cooking |
| CN103429642A (en) * | 2011-03-09 | 2013-12-04 | 瑟里菲公司 | Separation of lignin from plant material |
| CN104499370A (en) * | 2014-11-25 | 2015-04-08 | 南通新世纪机电有限公司 | Adhesive film paper dipping drying method |
| CN105860091A (en) * | 2016-05-24 | 2016-08-17 | 安徽瑞丝环保能源有限公司 | Device for extracting lignin by water-assisted dissolution |
| CN109092212A (en) * | 2017-06-20 | 2018-12-28 | 北京化工大学 | Single two sections of continuous operation furfurals and paper pulp and lignin polygenerations systeme and method |
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| EP1740509A2 (en) * | 2004-04-02 | 2007-01-10 | Skill Associates, Inc. | Biomass converters and processes |
| CA2638159C (en) | 2008-07-24 | 2012-09-11 | Sunopta Bioprocess Inc. | Method and apparatus for treating a cellulosic feedstock |
| CA2638157C (en) | 2008-07-24 | 2013-05-28 | Sunopta Bioprocess Inc. | Method and apparatus for conveying a cellulosic feedstock |
| US9127325B2 (en) | 2008-07-24 | 2015-09-08 | Abengoa Bioenergy New Technologies, Llc. | Method and apparatus for treating a cellulosic feedstock |
| CA2638150C (en) | 2008-07-24 | 2012-03-27 | Sunopta Bioprocess Inc. | Method and apparatus for conveying a cellulosic feedstock |
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| JP2011001677A (en) * | 2010-01-08 | 2011-01-06 | Toa Kogyo:Kk | Apparatus and method for producing pulp, and high concentration pulper |
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| GB583074A (en) * | 1945-03-07 | 1946-12-06 | English Cellulose Derivatives | Improvements relating to processes for the production of cellulose pulp |
| DE2215739C2 (en) * | 1971-04-09 | 1985-05-15 | Kilborn Engineering Ltd., Toronto, Ontario | Process for pulping chopped wood |
| EP0012775B1 (en) * | 1978-12-20 | 1984-05-16 | Eric S. Prior | Process for pulping ligno-cellulosic material |
| SE434283B (en) * | 1982-12-01 | 1984-07-16 | Mo Och Domsjoe Ab | PROCEDURE FOR DELIGNIFICATION OF CELLULOSAMASSA WITH NITROGEN OXIDES AND Oxygen |
| EP0364632A1 (en) * | 1988-10-17 | 1990-04-25 | Zeneca Limited | Production of lignin |
| US5944953A (en) * | 1996-03-12 | 1999-08-31 | Le Centre Specialise En Pates Et Papiers (Cspp) Du College D'enseignement General Et Professionnel De Trois-Riveres | Process for simultaneous mechanical and chemical defibration of corn stalks and straw materials |
| FI122654B (en) * | 1997-12-08 | 2012-05-15 | Ovivo Luxembourg Sarl | Process for making paper cellulose pulp |
| US20030041982A1 (en) * | 2001-08-31 | 2003-03-06 | Prior Eric S. | Organic biomass fractionation process |
| AU2003291874A1 (en) * | 2003-06-03 | 2005-01-21 | David Tarasenko | Method for producing pulp and lignin |
-
2005
- 2005-12-07 AU AU2005338842A patent/AU2005338842B2/en not_active Ceased
- 2005-12-07 CN CNA2005800522284A patent/CN101326326A/en active Pending
- 2005-12-07 BR BRPI0520735A patent/BRPI0520735B1/en not_active IP Right Cessation
- 2005-12-07 WO PCT/CA2005/001862 patent/WO2007065241A1/en active Application Filing
- 2005-12-07 EP EP05816018A patent/EP1969175B1/en not_active Not-in-force
- 2005-12-07 RU RU2008126769/12A patent/RU2383675C1/en not_active IP Right Cessation
- 2005-12-07 AT AT05816018T patent/ATE553246T1/en active
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102449231A (en) * | 2009-05-26 | 2012-05-09 | 日本制纸株式会社 | Method for digesting lignocellulosic material |
| CN102449231B (en) * | 2009-05-26 | 2014-05-14 | 日本制纸株式会社 | Method for digesting lignocellulosic material |
| CN103380247A (en) * | 2011-02-22 | 2013-10-30 | 安德里兹有限公司 | Method and apparatus to produce pulp using pre- hydrolysis and kraft cooking |
| CN103380247B (en) * | 2011-02-22 | 2016-08-10 | 安德里兹有限公司 | Use the method and apparatus that prehydrolysis and kraft cooking produce paper pulp |
| CN103429642A (en) * | 2011-03-09 | 2013-12-04 | 瑟里菲公司 | Separation of lignin from plant material |
| CN104499370A (en) * | 2014-11-25 | 2015-04-08 | 南通新世纪机电有限公司 | Adhesive film paper dipping drying method |
| CN104499370B (en) * | 2014-11-25 | 2017-01-11 | 南通新世纪机电有限公司 | Adhesive film paper dipping drying method |
| CN105860091A (en) * | 2016-05-24 | 2016-08-17 | 安徽瑞丝环保能源有限公司 | Device for extracting lignin by water-assisted dissolution |
| CN109092212A (en) * | 2017-06-20 | 2018-12-28 | 北京化工大学 | Single two sections of continuous operation furfurals and paper pulp and lignin polygenerations systeme and method |
| CN109092212B (en) * | 2017-06-20 | 2024-03-22 | 北京化工大学 | Single-bed two-stage continuous operation furfural and paper pulp and lignin poly-generation system and method |
Also Published As
| Publication number | Publication date |
|---|---|
| AU2005338842B2 (en) | 2011-08-11 |
| RU2008126769A (en) | 2010-01-20 |
| BRPI0520735A2 (en) | 2009-05-26 |
| WO2007065241A1 (en) | 2007-06-14 |
| EP1969175A1 (en) | 2008-09-17 |
| AU2005338842A1 (en) | 2007-06-14 |
| RU2383675C1 (en) | 2010-03-10 |
| BRPI0520735B1 (en) | 2017-05-09 |
| EP1969175B1 (en) | 2012-04-11 |
| ATE553246T1 (en) | 2012-04-15 |
| EP1969175A4 (en) | 2011-03-16 |
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