CN103459711A - Method and arrangement for treating filtrate after oxygen delignification of chemical pulp cooked to a high kappa number - Google Patents
Method and arrangement for treating filtrate after oxygen delignification of chemical pulp cooked to a high kappa number Download PDFInfo
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- CN103459711A CN103459711A CN2012800144257A CN201280014425A CN103459711A CN 103459711 A CN103459711 A CN 103459711A CN 2012800144257 A CN2012800144257 A CN 2012800144257A CN 201280014425 A CN201280014425 A CN 201280014425A CN 103459711 A CN103459711 A CN 103459711A
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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
- D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
- D21C9/02—Washing ; Displacing cooking or pulp-treating liquors contained in the pulp by fluids, e.g. wash water or other pulp-treating agents
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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
- D21C3/22—Other features of pulping processes
- D21C3/24—Continuous processes
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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
- D21C7/00—Digesters
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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
- D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
- D21C9/10—Bleaching ; Apparatus therefor
- D21C9/147—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications
Abstract
The present invention relates to a method and an arrangement for treating chemical pulp that has been cooked to a high kappa number. Pulp is produced by cooking in an alkaline cooking process to a kappa number of 50-120, preferably 60-100, the cooked pulp is washed, the washed pulp is led into an oxygen stage where the pulp is treated in the presence of oxygen and alkali for removing lignin, and the oxygen-treated pulp is washed, whereby lignin-containing washing filtrate is formed. In the oxygen stage the kappa number of the pulp decreases by at least 30 units. The filtrate downstream of the oxygen stage is treated for separating lignin, and the treated filtrate is led as washing liquid into the washing apparatus for the cooked pulp.
Description
Technical field
The present invention relates to the method and apparatus of by the paramount card uncle of pulp cooking the time, chemical pulp being processed.
Background technology
Kappa number is indicated remaining content of lignin, and in all factories all used as the desired value of boiling.The typical Kappa number for the treatment of bleached pulp is 14-20 for hardwood at present, and is 25-35 for cork.If not to association with pulp bleaching, the Kappa number after boiling is obviously higher, is generally 40-100.Usually treat bleached softwood paper pulp and processed that Kappa number is down to 10-20 in oxygen stage.
About the present invention, Gao Kabai paper pulp refers to the Kappa number that surpasses 50.Needing high strength properties and hardness but, in not needing the product of brightness or printing, usually using Gao Kabai paper pulp (high yield paper pulp).Based on this reason, cork is because its long fiber becomes the typical feedstock for high yield paper pulp.Cork has high lignin content, the chemical treatment that it need to be relatively long for this reason.The combination of intensity property and hardness is typical for softwood pulp.About high yield paper pulp, content of lignin is still high, to such an extent as to can not carry out defiber to paper pulp in the prior art under the condition of not carrying out mechanical treatment, but in this case, final products do not require printing or brightness.
Usually produce high yield paper pulp with sulfate process.The yield scope of high yield paper pulp is 50-70%.Known ground, used as having the filamental thread equipment that normal Kappa number designs and can not manufacture this paper pulp, and need other technology.Most important difference between filamental thread is, the Gao Kabai paper pulp after boiling is in following thick bits form, this slightly the bits form make its defiber need special defiber equipment, for example purge pipeline refiner (series connection refiner), or heat refining alternatively.Described device is similar type.In the defiber device of at first mentioning, the cooking of pulp in the bits form is drained into to the refiner of the purge pipeline that is arranged in the washing stage upstream from boiling vessel.The purpose of cooking of pulp defiber is that fiber is separated from each other, because after boiling, fiber is still in the bits matrix.This defiber makes the paper pulp of manufacture have Gao Kabai and has high yield value.Even paper pulp is carried out to the mechanical treatment of slight defiber, its effect is to have reduced the quality of paper pulp under alkali condition.
The Gao Kabai pulp manufacture is become to so-called thick slurry.Therefore, purpose is bleached this paper pulp.Production line for this paper pulp comprises pulp washing and screening.If the requirement of any special nature is set for pulp quality, described production line can comprise oxygen stage with the property adjustments by paper pulp to aspiration level.
During boiling, carbohydrate (cellulose and hemicellulose) is dissolved, cause cost of material obviously to improve, because the loss of carbohydrate is all large when boiling starts and finish.A kind of mode that reduces carbohydrate breakdown is to finish boiling under higher Kappa number.Usually, if finish boiling and utilize chlorine dioxide to be bleached paper pulp and do not need oxygen stage when high Kappa number, yield improves.In addition, the cost of bleaching and the discharge of raising effluent has surpassed the permission boundary.Can obtain technology in BAT(the best) keep the effluent discharge under factory's level, require to use oxygen stage, thereby the yield of carbohydrate is high as far as possible.The sharply development of oxygen delignification provides under a kind of condition substantially not losing yield the effective ways that reduce the card uncle who treats bleached pulp.Current trend has been to stop reaching obvious low-level boiling Kappa number.
Importantly selective in sulphate cook, that is, when dissolved lignin, a small amount of as far as possible carbohydrate (cellulose and hemicellulose) divides and dissolves.Because of chemical reaction, throw into question, it causes dissolving the obviously hemicellulose of amount in the ending phase of boiling.Therefore, also cause the decline of chemical pulp intensity in the terminal stage of dissolved carbon hydrate.In the situation of softwood pulp, the intensity of chemical pulp is one of the most basic index of quality.Except pulp properties, process recovery ratio is also important cost factor.Purpose in the past few years is to find such pulping process, by described pulping process, can realize yield high as far as possible from timber to paper pulp.It refers to, improves selectively or the only boiling of boiling to reach such Kappa number, thereby use, has more optionally the delignification method so that obvious yield benefit and Economic Importance thus to be provided.Difference in final card uncle scope between (being 25-40 for cork) sulphate cook method is enough little, makes with it and substantially can not get the difference aspect selective.In fact, the feasible method that improves yield is obviously under higher Kappa number level, to stop boiling, relatively higher than to association with pulp bleaching and in continuing to carry out with oxygen the boiling of delignification of carbohydrate yield wherein, with boiling, compare, known the method is to have more the mode of optionally paper pulp being carried out delignification.
Due to alkali condition, so oxygen delignification directly follows lignin closely during boiling, remove and occur.In industrial digestion process, not by the chemical pulp boiling to being starkly lower than Kappa number 25, because yield losses is remarkable.On the other hand, expectation is optimized to reach high as far as possible Kappa number to boiling, thereby maintenance Litter content is controlled and keep paper pulp to bleach.Between boiling and final bleaching, oxygen delignification is to have more optionally and the technique of milder.It decomposes lignin and is oxidized to alkaline bleach liquor soluble form, destroys the coloring compound existed in lignin and remove impurity (resin) from paper pulp.
About quality, in blowing pipe line fiber seperator, the paper pulp after the boiling vessel discharge being carried out to defiber is never so-called preferred plan, but under the condition of not using obvious mechanical load, paper pulp is carried out to chemical defiber to keep fibre property the best.
Nearest boiling research shows, boiling can be manufactured Gao Kabai paper pulp, its by defiber to following degree: even the paper pulp of this bits form still can carry out pumping and processing (Jiajun Wang under the 70-90 Kappa number in filamental thread, master's thesis, Aalto Yliopisto(A Ertuo institute), School of Science and Technology(science and technology university) 2010; WO patent application PCT/US10/57417).In addition, within this stage, the paper pulp of boiling contains the Litter of large component analysis, but the feature of Litter makes it can not limit, pulp pump is delivered to washing and operation stage subsequently.
FI patent application 20115277 provides a kind of method of pulp treatment, and described paper pulp is by the cork dust chemical steaming is manufactured to the Kappa number of 50-100, preferred 60-90, in described method,
Not in the situation that processed in the mechanical fiber seperator between boiling vessel and washing, the paper pulp of boiling is introduced to washing, this paper pulp is washed,
The paper pulp of washing is introduced to the first oxygen delignification in the stage, wherein under the existence of oxygen and alkali, described paper pulp is processed,
Paper pulp to oxygen delignification is washed, and in the stage subsequently, with the electrophilic chemicals, it is processed after washing, thereafter
With oxygen and alkali, described paper pulp is washed and processed in the stage at the second oxygen delignification, the paper pulp of processing is thus washed and introduces in bleaching process to carry out other processing.
Refer to following alkali stage according to the oxygen stage of present patent application, this alkali stage under the pH of 8.5-14 scope under mixing point at 1-20, preferably carry out in the mode of pressurizeing in the pressure limit of 8-12 bar (definitely), and wherein at least in the partial reaction time durations oxygen be present in fiber around.This oxygen stage can comprise one, two or even several step, and the reaction that each reactions steps comprises chemical mixing and reaction vessel or utilizes pipe to complete thus stops.In fact, treatment step herein refers to interpolation and the mixing of the chemicals used in this oxygen stage, and the stop in pipe or reactor part subsequently.According to practical method, reaction stop be 0.1 minute to being up to 120 minutes, thereby reaction stops the type of reactor that depends on expectation.About this point, oxygen stage also can be from knowing according to this both washing stage of oxygen stage upstream and downstream.
The most normally, by oxygen and alkali and prevent that some possible inhibitor that fiber is subject to damaged metal is metered in oxygen stage, or in addition the metal of carrying secretly in fiber is removed or processed so that its inactivation.Usually the amount with 1-60kg/admt is metered into alkali, and is metered into oxygen with the amount of 1-50kg/admt.When the dosage of the alkali dosage that is 0.8-1.4 * Ka Bai unit and oxygen is 0.7-1.3 * Ka Bai unit, can notice, when the uncle of the card in oxygen stage drops to 60 unit, the dosage that the dosage of oxygen stage alkali can be up to 90kg/adt and oxygen can be up to 70kg/adt.The alkali used is the most normally the white liquid of NaOH or oxidation, but all alkali compoundss that contain in principle the OH ion are all the alkali can be used under certain conditions in oxygen stage.Usually advantageously, be metered into the supplementary NaOH of chemical cycle in oxygen stage.Be metered into oxygen with gas form, wherein the content of oxygen is the most normally the 75-100% of proportion.The temperature of oxygen stage is 70-120 ℃ and is generally 80-105 ℃ most.Use has some suitable steam of 0.5-20 bar pressure and hot water by washing or the dilution described temperature that can raise.Steam can be directly used in heating, in paper pulp, mixes, or indirectly for heating.
In stage, especially, in the first processing, discharge a large amount of lignin (Kappa number reduces for example 30-70 unit) at the oxygen delignification of Gao Kabai paper pulp, this will consider in technique.When the amount of the lignin of removing, during for 40 Ka Bai unit for example, the quantitative change of the organic material discharged from paper pulp is high.In the situation that described card uncle descends, for example only the ratio of lignin is approximately 7% of paper pulp dry, and its carbohydrate loss in addition.The lignin of described amount promotes 60-120kg/adt by the COD of oxygen stage filtrate amount, and promotes the amount of dry with same ratio.Described oxygen stage is connected according to the countercurrent washing principle usually, so that the pulp washing function arranged between boiling and oxygen stage is replaced the liquid carried secretly in the paper pulp from washing, this filtrate that can be the cooking of pulp washing stage by this fluid separation applications, obtain filtrate from the washing of oxygen stage.Therefore, the COD of the wash liquid of the paper pulp of boiling will be 30-60g/l, and the COD of pulp suspension is 200-500kg/adt under 12% denseness.Usually, will be derived from the filtrate adverse current of pulp washing introduce in filamental thread, but to the filtrate processing of oxygen stage with high COD value, might not be favourable in this way.Industrial known COD level is starkly lower than the above-mentioned value in described research, when the filtrate adverse current that oxygen stage is produced is introduced same stage, in order to determine its characteristic, has carried out described research.The level above illustrated is enough high, thereby it hinders the operation of oxygen stage and causes chemicals and the consumption of circulation lignin.When summarizing the oxygen stage of Gao Kabai paper pulp, consider the amount of product.
Because described product is because the selectional feature of oxygen stage comprises lignin and a small amount of carbohydrate, so can say, in the wash filtrate of oxygen stage, the ratio of lignin and carbohydrate is higher than in black liquor.Thus, under the condition of oxygen stage technique not being disturbed, it is disadvantageous according to countercurrent action, using it in the washing of paper pulp of boiling.Therefore, clearly need will wash in new ways with oxygen stage and carry out on the whole in conjunction with the paper pulp with for the paramount card uncle of boiling, in many modes, this has more practicality.
Summary of the invention
The present invention relates to process the method for chemical pulp, in described method by by the wood chip chemical steaming to 50-120, preferably the Kappa number of 60-100 is manufactured paper pulp, paper pulp to boiling is washed, the paper pulp of washing is introduced in oxygen stage, wherein under oxygen and alkali existence, paper pulp is processed to remove delignification, and the paper pulp of oxygen treatments applied is washed, form thus the wash filtrate containing lignin.Described method characteristic is,
In described oxygen stage, at least 30 units of the Kappa number of described paper pulp decline, and
Filtrate to the washing in described oxygen stage downstream is processed with separating lignin, and the filtrate of processing is introduced in washing facility with the paper pulp for boiling as wash liquid.E for the washing facility of the paper pulp of boiling
10value is at least 8 usually, is at least preferably 10.
So-called E
10value defines detersive efficiency, thereby can dissimilar washer be compared mutually.E
10value is the numerical value for the combination definition of washer or several washers, and it has showed multiple desirable mixing of how to realize washer or washer combination.Desirable situation of mixing while being understood to again following: wash liquid is efficiently sneaked in the paper pulp of washing, make the liquid that remains in paper pulp equate with the concentration of liquid from its extraction.At E
10numerical value 10 in value refers to the denseness percentage of calculating, and now paper pulp is discharged washer.Dilution gfactor refers to the wash liquid that paper pulp per ton is used and discharge the difference between the liquid of washing facility together with paper pulp.
The invention still further relates to the device of being processed by the paper pulp of wood chip manufacture in digesting apparatus, wherein by the wood chip chemical steaming to 50-120, the preferred Kappa number of 60-100, described device at least comprises:
For the digesting apparatus of cellulose fibre material, for the washing facility of the paper pulp of boiling,
Equipment in the washing downstream of the paper pulp of boiling, its in oxygen stage to the delignified pulp lignin,
The equipment after oxygen stage, paper pulp washed, and
The wash filtrate adverse current is introduced in aforementioned washer to the filtrate line of usining as wash liquid.Be necessary that, the filtrate line in described oxygen stage downstream is provided with for the equipment from the filtrate separating lignin, and by this filtrate line be connected to for the washing facility of the paper pulp of boiling with by filtrate as the wash liquid after lignin separation.
E for the washing facility of the paper pulp of boiling
10value is at least preferably 8, is at least preferably 10.The washing facility that is used for the paper pulp of boiling generally includes the stage that surpasses one.The washing facility that is used for the paper pulp of boiling generally includes so-called boiling vessel washing and at least one washing facility between boiling vessel and oxygen treatments applied equipment.
The washing facility that is used for the paper pulp of boiling, as a stage, can be included in the boiling vessel washing of carrying out the boiling vessel bottom, the final displacement that for example high pattern of fever boiling vessel is replaced or occurred in batch cooking.The washing facility that is used for the paper pulp of boiling is included in one or more washers in its downstream, for example preferred single drum wash device, for example Drum Displacer
(DD) washer (Andritz Oy) or diffuser.If the paper pulp of boiling is containing the uncooked fraction of harmful amount knaur for example, at the E of total washing facility of the paper pulp for boiling
10under the prerequisite of exceedance of levels 8, can also the working pressure machine.The dilution gfactor of described washing facility will be 0-5, preferably 1-3.In order to ensure during boiling, discharging from the lignin of paper pulp and fully remove, enough detersive efficiencies are important.Remove in described washing and surpass 95%, preferably surpass 97% lignin.Simultaneously, also sulphur can be removed from paper pulp.
The present invention has filled up the performance of the bleached pulp of delignification under Gao Kabai, so that it is industrial feasible.In addition, its yield that makes pulp production is obviously more higher than the yield in the conventional fibre line.In addition, even manufacture paper pulp by the sulfate process of using conventional fibre line and recovery concept, still can from technique, reclaim poor sulphur lignin.From amount and the boiling/delignification performance of lignin, consider, the present invention more preferably is applied to cork, but it also can be applied to hardwood, especially has the hardwood species of high lignin content.
Shown in method, by alkaline cooking process for example sulphate cook, soda boiling or soda-anthraquinone boiling manufacture paper pulp.Described boiling method can also be the improvement of these methods.Preferred example is to have the sulphate cook that low state of cure is 5-25%.Sulphidity value lower than described value relates to soda boiling or its improvement.This boiling can be continuously cooking or batch cooking.
In described boiling, the Kappa number by pulp cooking to 50-120, preferred 60-100.This paper pulp has the lignin of about 7-14 % by weight, and this is significant amount substantially.If the card of the paper pulp of boiling uncle is 100-120, in described oxygen stage, this lignin is removed, make the Kappa number of this paper pulp be generally about 20-40 and approximately 50.Thus, from economy and technology two aspects, consider, the lignin of obviously measuring is transferred in the filtrate of oxygen stage.According to embodiment of the present invention, do not use the white liquid of oxidation, and preferably with NaOH, implement described oxygen stage, make thus lignin be released in solution, it is poor sulphur that this oxygen stage of implementing with the white liquid that uses oxidation is compared.The sulphur that is derived from the magnesium sulfate that is used as inhibitor enters described oxygen stage with the sulphur that is derived from the boiling chemicals.In this case, more advantageously, the washer of described oxygen stage upstream will be used for containing the liquid of the sulphur compound that produces autoxidizable white liquid.Sulphur is favourable lower than the lignin of normal value in many other application facet about lignin.The method according to this invention did not need or does not implement any independent chelation treatment before described oxygen stage.Can reduce thus the amount of effluent component and reduce process costs.
After described oxygen stage, described paper pulp is normally washed, thereby from liquid phase paper pulp reaction product isolated.Paper pulp per ton can be manufactured the lignin of 40-120kg, common 40-80kg amount.In the present invention, be preferably sulfur-bearing not or poor sulphur for the alkali of described oxygen stage, thus, when use substantially the liquid of sulfur-containing compound not when high-efficient washing is carried out to paper pulp in the downstream of oxygen stage and upstream, can obtain for paper pulp per ton poor sulphur lignin with 40-100kg amount containing lignin liquid.The monetary value of this lignin is so remarkable, makes it be worth reclaiming, and because of the washing of lignin compound being introduced to the oxygen stage upstream, is especially the main interference factors of described technique, makes this technique not have technology or economic base.The low-sulfur lignin refers to the lignin that in lignin, the sulfur content of dry is less than 1%.And the sulfur content of the lignin precipitated from the oxygen stage wash filtrate is dry approximately 0.66% according to research, the approximately 1.4%(sulphur that the sulfur content precipitated from black liquor is dry).
In the solution that presented herein, the filtrate of described oxygen stage is separated with described paper pulp and reclaim lignin from it, for example to be used as the raw material of chemical industry.Accordingly, the liquid that from it, has separated lignin can be used further to described oxygen stage, thereby is introduced into the washing of described oxygen stage upstream, and does not have the adverse effect to lignin.Thus, from any situation all the adverse current connected with the oxygen stage of Gao Kabai paper pulp be connected the oxygen reaction product of removing described oxygen stage in wash cycle and isolation technics, can be considered to have the investment of clear and definite economic aim, and be not only for guaranteeing the fringe cost of process function.
In order to optimize the sulfur content of lignin, the alkali of described oxygen stage is pure NaOH (NaOH) or can in oxygen stage, keeps enough some other hydroxide of high pH level.The pure described sodium hydroxide solution that refers to does not contain any sulphur herein, or contains very small amount of sulphur.Preferably, the chemicals of described oxygen stage is not the chemicals that contains sulphur compound.A kind of chemicals be generally used in described oxygen stage is the magnesium sulfate as inhibitor.Can require and be low to moderate according to sulfur content the requirement of which kind of degree according to pulp quality, its use is optimized.Although preferably do not use the white liquid of oxidation, but still can in conjunction with chemical regeneration, alkali be separated in chemical pulp factory, make a kind of fraction contain sulphur compound and another kind of fraction contains pure NaOH.In this case, surpass 40% mode with the sulphidity in boiling and form the chemicals ratio.When the paper pulp that uses the low-sulfur wash liquid be derived from lignin separation to boiling according to countercurrent action is washed, in the logistics of returning to the black liquor vaporizing workshop, sulphidity is back to " normally ".In another embodiment, the sulphidity of boiling is about 25-40%, but the sulphidity of the liquid in recovery is obviously lower, is for example 25-30%.
Prior art provides several technique that green liquor is classified into to NaOH and sulfur-bearing fraction in conjunction with chemical regeneration.For example, from FI 104334, FI 98226 and the known this technique of US 5607549.NaOH is used for to boiling for described oxygen stage and by the sulfur-bearing fraction.So, do not need to use the chemicals be purchased as the alkali in described oxygen stage, but can manufacture the chemicals needed in factory in conjunction with chemical cycle.
According to a kind of embodiment, the white liquid of oxidation also can be used in described oxygen stage.So, in the manufacture of white liquid, with oxygen, sulfide is carried out to oxidation, via thiosulfate to sulfate.If the sulfur content of expectation minimization lignin, this is not very favorable embodiment.
From the present invention, consider, not necessarily, but particularly based on the following fact: lignin separation becomes lucrative to described lignin separation method itself, and according to a kind of preferred embodiment, can be with low-sulfur form separating lignin in kraft process.So described technique comprises following character:
The brown paper boiling is to card uncle 50-120.
After boiling and described oxygen stage, it is the high-efficient washing of paper pulp.E for the washing facility of the paper pulp of boiling
10value is at least 8, preferably surpasses 10.The E of described oxygen stage
10value surpasses 4, preferably surpasses 7.The detersive efficiency required also depends on the levels of precision be in the suds the lignin separation of the lignin of boiling generation and oxygen stage.The washing of the paper pulp of boiling is more efficient, and the separation of the lignin that boiling produces is better, and the lignin that can produce with the low-sulfur form oxygen separation stage in the washing of described oxygen stage is more.
-the wash liquid of final stage of introducing the washing of described oxygen stage upstream is not containing the liquid of significant quantity sulphur.
-when expecting the lignin of unusual low-sulfur, the alkali during described oxygen stage is sulfur-bearing not preferably.
-in described oxygen stage, in order to be released in economically the obviously lignin of amount from paper pulp, the card uncle reduces at least 30 units, has preferably reduced and has surpassed 35 units.
In described oxygen stage, the lignin of the obvious part of paper pulp is dissolved in liquid mobile together with fiber, and it can separate with the filtrate of washer or forcing press thus.When lignin separates, can the washing for the paper pulp of boiling by the liquid of purifying thus.The paper pulp of washing itself is supplied to the production to cardboard, or can be bleached in addition the paper pulp of washing with the method provided equally in this patent application.
Because the modern chemistry pulp factories can almost completely be stopped sulphur, and in fact the sulphur loss can not occur in factory, so can clearly draw, the washing of the paper pulp of boiling can remove desulfuration efficiently, and be applicable to thus remove desulfuration from paper pulp, conventional washing technology has the E that surpasses 8
10value.
According to the present invention, be necessary that, can be processed with for paper pulp market boiling to the obvious paper pulp of high lignin content, described paper pulp can also wash to the cleanliness levels of expectation.This being to building bio-refineries and applying various processing methods and expanded brand-new possibility, consequently can be from fibre stuff separating lignin.Naturally, possible embodiment is restricted to complete affordable chemicals usually, because will make described technique lucrative, but still has several distinct methods that can be used in lignin separation.
The lignin separated can also be as the boiler of chemical pulp factory and the fuel in drying oven.
During recent years, the alternative materials of research for the manufacture of polymer and other carbon-based material recognized in wood processing industry and chemicals industry.At present, the most important raw material of polymer industry is crude oil, and its price and availability will make polymer have competitiveness with the wood type raw material in the long run.Thus, the lignin based on chemical pulping process also has market, and wherein it can replace the crude oil class product.Because most important chemical pulp manufacturing technique be take and used sulfenyl boiling chemicals as basis, so, if do not focus on removing sulphur from lignin, the availability of lignin chemical industry of separating from described sulfenyl boiling chemicals is low or be restricted.And if use the not chemicals of sulfur-bearing to complete described digesting technoloy, the quality of lignin improves, but the manufacture of paper pulp has many this features, and described technique does not have extensive competitiveness so far.Advantage of the present invention is, its manufacture is applicable to the further lignin of processing.
Oxygen stage is the simplest and the most known method to Gao Kabai delignified pulp lignin.Therefore, utilize following method to be processed paper pulp, wherein, fibre property is preferential, and the use target of fibrous raw material is known paper and fiber product.Also can use other lignin dissolution and separation method, replace oxygen stage, use it for Production Example as special lignin or for separating of for example hemicellulose.This method can comprise sour pulping process, the combination of the defiber that is applicable to straw pulp for example provided by Chempolis, the formic acid slurrying that is called CIMV technique or acid hydrolysis and oxygen stage.In this relation, there are several substitutes, because Gao Kabai paper pulp (the card uncle is for example 100) is the raw material for a large amount of different products, wherein by washing, from described Gao Kabai paper pulp, removed the boiling chemicals, be at first sulphur.Therefore, lignin is not only possibility product, but, except it, described product may also comprise for example hemicellulose.
The solution separated with paper pulp in oxygen stage can be processed with separating lignin in many ways.The most conventional Chemical Decomposition method is precipitation, wherein alkaline solution is neutralized or acidifying, thus alkali is precipitated from solution and its can be from liquid levigation.This needs a large amount of acid, and but then, it is for reclaiming the efficient and simple mode of lignin.At pH, be to precipitate approximately 15% lignin 10 times, and the lignin that is 8 times precipitations 50% at pH.The pH of oxygen stage is 10-13, is generally 10.5-12.In lignin separation, target needs not be fully separates.Even only separate approximately 50% lignin and then used as wash liquid from the wash filtrate of oxygen stage, in the washing of the paper pulp of boiling, still obtain satisfied result.On the other hand, lignin is circulated and understands deteriorated its quality by oxygen stage, thereby favourable purpose is higher separation degree.From further processing, consider, in the lignin reclaimed, more substantial intrinsic lignin is favourable.
Other lignin separation mode comprises multiple filter method, and its middle filtrator can be removed large chaining molecule, but makes ion and water pass.This method comprises multiple ultrafiltration or nanofiltration, diafiltration and reverse osmosis filter, dynamically cross flow one is filtered and other method that can molecule be separated from solution by it.When lignin being separated from solution, clean solution can be used for to the washing of the paper pulp of boiling, because organic carrier fluid is removed.
When being conceived to complex compound, wherein this solution is suitable, this advantage demonstration, and as independent step, it has obviously improved the economic potential of factory:
The pulp yield of filamental thread is obviously better.
Obtained a kind of solution, when Gao Kabai paper pulp is processed, utilized described solution, oxygen stage is brought into play function fully.
Formed a kind of wherein technique of separable low-sulfur lignin.
The whole chemical cycle of this technique is for example evaporated with recovery boiler and is remained unchanged, thereby whether the biorefining scheme that may need in order further to use lignin or not new technique department.
Larger output under the condition of chemical cycle still less.When from technique, reclaiming lignin, the amount of substance burnt in recovery boiler reduces, because the amount of the dry that paper pulp per ton produces descends, and chemical cycle still less.Therefore, need less boiler, or existing boiler can burn the more black liquor dry of a large amount for the paper pulp per ton of producing.
Because change is all influential to many unit, so will consider the item of following kind in development technology:
Total production capacity for steam of recovery boiler descends
Need the new separation department for lignin
The chemicals in described oxygen stage or other delignification stage may be than current use more expensive
The effluent output changes and is conventional in conjunction with not using like this
By the needs chemicals of sulfur-bearing or low-sulfur not, its price level is higher than the price level of sulfur-bearing chemicals.
The present invention is specially adapted to improve by sulfate process or its paper pulp of manufacturing.Can use the chemicals that for example improves yield, for example anthraquinone in conjunction with boiling.Mode with continuous or batch cooking is carried out boiling to paper pulp, thereby (Kappa number 50-120) stops delignification under the high lignin contents level, but makes the defiber point that reaches wood chip.For example in International Patent Application PCT/US10/57417, this method is described.As a kind of preferred embodiment, method of the present invention comprises a kind of following technique combination, and the mechanical defiber of wherein after boiling, complete paper pulp logistics being carried out can be omitted.Thus, or not for example not carrying out, under the condition of mechanical treatment, the paper pulp of boiling being drained into washing from boiling vessel in purge pipeline refiner mechanical defiber equipment, then drain in oxygen stage.In the mechanical fiber seperator, the application machine operation makes fiber discharge from the wood chip matrix, and this is unwanted in the method according to this embodiment.Described filamental thread naturally comprises pump, blender and shifts and chemicals and other material are sneaked into the relevant device of paper pulp for paper pulp.From energy economy, consider, it is favourable not using the mechanical fiber seperator, because the energy dissipation of washer, pump and blender between boiling vessel and the first oxygen stage is lower than 30kW/adt, and the energy consumption of defibrator is its twice.
More preferably after oxygen delignification, complete the screening of paper pulp.According to a kind of embodiment, when having several oxygen stage, sieve compartment is positioned at the downstream of the first oxygen stage.According to a kind of embodiment, this sieve compartment is between the first oxygen stage and washing subsequently.Alternatively, also can sieved paper pulp afterwards, but preferably before the washing after the second oxygen stage, paper pulp sieved.Described screening can also be divided into coarse fraction and dusting cover divides, and coarse fraction occurs in for example the first oxygen stage downstream thus, and dusting cover divides and occurs in the second oxygen stage downstream.Therefore, in order to manufacture paper pulp to be bleached, advantageously only before the first oxygen stage, after boiling, paper pulp is washed.Therefore, under the condition of not carrying out mechanical defiber and not sieved, by washing, will discharge from the paper pulp of boiling vessel and introduce the first oxygen stage.
Yet, can expect, before the first washing, after boiling vessel discharge paper pulp, implementing to remove knaur from paper pulp.Therefore, in the screening knaur, the Litter that will separate from main paper pulp logistics carries out gentle defiber.The Litter logistics of defiber can be back to the downstream in the same way that main paper pulp logistics separates to enter knaur separating feed or knaur.Be necessary that, described main paper pulp logistics do not carried out to mechanical defiber, and only the side logistics from its separation (for example preferably be less than 30%, most preferably be less than 20%) is carried out to defiber, thereby the knaur fraction is used for to washing and processing subsequently under appropraite condition.
Washing refers to one or more washing stages, and it occurs in one or more washing facilitys thus.
According to a kind of embodiment, before the first oxygen stage, preferably use single drum wash device, the pressure roller washer of for example being manufactured by Andritz is Drum Displacer
tM(DD)-washer, or vacuum drum washer or diffuser, the paper pulp to discharge from boiling vessel is washed.The washer of in the cylinder of wherein finding in for example washing forcing press and/or the roll gap between roller, paper pulp being suppressed, be not suitable for the pulp washing between boiling and the first oxygen stage.If realized the removal of knaur before the washing in boiling vessel downstream, also can the working pressure machine.In the time of before sieving the washing that has occurred in oxygen stage, can use following conventional washing technology and can also use thus washing forcing press or forcing press to complete the washing in the first oxygen stage downstream, this routine techniques can be used above-mentioned washing facility.
The first oxygen stage is obviously the continuation of boiling, its objective is the card uncle is reduced to a 30-70 Ka Bai unit.Simultaneously, the Litter content of paper pulp also declines to a great extent, and the amount of the Litter of removing in the screening of the paper pulp in some treatment step after the first oxygen stage thus is not obvious, because remove, will stop the yield benefit.In the second oxygen stage, the Kappa number of described paper pulp is down to the level of 10-20, preferably is down to 10-15 or lower value.
Research shows, in the first oxygen stage, the decline of the content of Litter even surpasses 95%, this means, thisly is combined in that to reduce Litter content aspect effective especially.
The known oxygen molecule can be only the phenolic lignin composition react with some.Under high alkalinity condition (pH > 10), Ionized lignin composition decomposes and because chain reaction reduces, and dissolves.Oxygen mainly reacts with the free phenol formula oh group of lignin formation carboxylic group, and it is water-soluble form by lignin conversion.Simultaneously, lignin generation depolymerization degrades.These reactions cause the phenolic hydroxyl group quantity of lignin to descend and the carboxylic group quantity of lignin improves.
According to oxygen delignification dynamics, in oxygen delignification, this phenolic lignin is removed, but oxygen delignification on the amount of non-phenolic lignin without any appreciable impact.About this chemistry, even the several series combination of the oxygen treatments applied under identical electrochemical conditions and treatment cycle are continued, still rest on the level place of 75-80% in the delignification level of oxygen stage.In addition, the condition of obviously observing becomes harsh, and particularly the decline of the quality of paper pulp and yield are low.Therefore, after oxygen stage, continuous delignification needs following chemicals, and it is also with other lignin composition react and/or produce new free phenol group.
In addition, for whether the processing of finding out paper pulp under acid condition can fully activate oxygen stage and test, but notice, do not help reducing card uncle nothing with the acid phase of lignin reaction itself.Acid phase has been strengthened the quality transmission, but does not change chemical composition.Find thus, after oxygen stage, paper pulp will experience the processing of using the bleaching chemical that reacts with non-phenolic lignin to carry out.What be applicable to this is so-called electrophilic bleaching chemical.These generally include peracid, the chlorine dioxide under acid condition, ozone or chlorine.Peracid for example comprises peracetic acid, Caron acid, persulfuric acid and peroxide molybdate.Can under own known and condition that provide, implement to utilize the pulp processing of these chemicals in the handbook of this area.Usually implement the processing of chlorine dioxide under following condition: the temperature of 40-90 ℃, the pH of 1.5-5.5, and the time period of 1-10 minute, but the longer time period be also feasible.In this processing, typical chlorine dioxide dosages is 2-20kg/adt.Representative condition about peracid treatment is: temperature is that 50-90 ℃ and time are 30-120 minute.The amount that is added into the chemicals in paper pulp depends on used peracid, but it typically is 2-20kg/adt.
Usually, under the pressure of 5-15 bar, preferably under the denseness of 5-35%, more preferably under the denseness of 7-18%, pressurization realizes utilizing the processing of ozone, thereby, at one or several some place, the gas ozoniferous that is preferably 8-18 % by weight, preferred 10-15% by one or more blenders by ozone content is introduced in paper pulp.Described gas is ozone and the mixture that serves as the oxygen of carrier gas.The amount that is metered into the ozone in paper pulp is 2-8kg/admt.PH, in acid range, is generally 1-5.Only, in allowing the long blender stopped or in the mode during paper pulp and the mixture of the ozone with carrier gas are introduced to reaction vessel, implement described ozone bleaching, the reaction that expectation is set in described reaction vessel stops.
After the electrophilic chemical treatments, utilize oxygen for the second time to the delignified pulp lignin, its objective is and Kappa number is down to 10-20 or in some cases even lower than 10 target Kappa number.Can in the bleaching process of fully not chloride (TCF) of routine or containing in the bleaching process of elemental chlorine (ECF) paper pulp do not bleached thereafter.
The accompanying drawing explanation
By according to embodiment of the present invention and with reference to appended schematic diagram, the present invention will be described in more detail, wherein:
Fig. 1 preferably carries out the schematic diagram of oxygen delignification under the condition of not carrying out lignin separation to Gao Kabai paper pulp; And
Fig. 2 is the schematic diagram of the preferred illustrative embodiment of the method according to this invention.
Specific embodiments
Described boiling vessel equipment comprises one or more pulp digesters.Boiling to the wood pulp of the Kappa number of 50-120, common 60-100 is transferred in purge tank 3 by purge pipeline 2 from the bottom of boiling vessel 1, paper pulp is sent into washer 5 by pipeline 4 from described purge tank 3 pumps.This washer is generally single drum wash device, and the pressure roller washer of for example being manufactured by Andritz is Drum Displacer
tM(DD)-washer, or diffuser or suction drum wash device.The paper pulp of washing is introduced in oxygen stage.Discharge is not carried out to mechanical defiber from the paper pulp of boiling vessel, and therefore described purge pipeline does not comprise the mechanical fiber seperator in the boiling vessel downstream.In addition, this is not sieved paper pulp before being in the first oxygen stage.Purge tank 3 is not indispensable, but depends on known washer own and the type of equipment combination, paper pulp directly can also be transferred in washer 5.
Black liquor is discharged by pipeline 33 from boiling vessel.
In this embodiment, the first oxygen stage comprises two reactors 7 and 8, that is, it is two step sections, but it can also be for a step or multistep stage, as above.In this oxygen stage, the Kappa number of paper pulp 30-70 the unit that usually descend.
Paper pulp is introduced to sieve compartment 10 from the first oxygen stage by pipeline 9.Paper pulp is further introduced to the washing 12 in oxygen stage downstream by pipeline 11, and wherein washer can also be for forcing press to replace single drum wash device or diffuser.
Then, in reaction vessel 14, with the electrophilic chemicals, paper pulp is processed, wherein the paper pulp of washing is discharged by pipeline 13 from washing facility 12.After the first oxygen stage, use the bleaching chemical reacted with non-phenolic lignin to be processed paper pulp.What be applicable to this is so-called electrophilic bleaching chemical.These generally include peracid, the chlorine dioxide under acid condition, ozone or chlorine.This processing is enough to promote the paramount card uncle's of boiling delignified pulp lignin with the bleaching process for actual.
After processing in reaction vessel 14, paper pulp is drained in washer 16 by pipeline 15, described washer 16 can be and the similar equipment of washer 12.Thereafter, the paper pulp of washing is transferred to the second oxygen stage by pipeline 17, described the second oxygen stage and the first oxygen stage are similar, comprise two steps 18 and 19.In this oxygen stage, the Kappa number of paper pulp is down to 10-20, preferred 10-15 or lower level.
Paper pulp is introduced to washer 21 from the second oxygen stage by pipeline 20, and described washer 21 can be single drum wash device or diffuser or is forcing press in addition.The paper pulp of washing is transferred to bleaching process by pipeline 27.After boiling, the paramount card uncle's of boiling paper pulp is processed, make its Kappa number be down to be conducive to the level of bleaching, but the quality of paper pulp remains on good level simultaneously, because do not need mechanical defiber.
Fig. 1 example the known washing that paper pulp is carried out according to countercurrent action itself.Thus, the filtrate that is derived from oxygen stage washing afterwards 21 is introduced in washer 16 as wash liquid by pipeline 22 adverse currents.Because implement to utilize the processing 14 of electrophilic chemicals under acid condition, so will be derived from the part of the filtrate of downstream washer, by pipeline 24, from this technique, discharge, but the washer 12 that a part is transferred to the first oxygen stage by pipeline 23 is usingd as wash liquid.Discharge is introduced to the washer 5 in boiling vessel downstream from the filtrate of washer 12 by pipeline 25, the filtrate that is derived from this washer is guided to the boiling vessel washing by pipeline 26 and enter in boiling vessel 1.In addition, water or other wash liquid are introduced in washer 21 and 12 by pipeline 32.
In conjunction with Fig. 2, in the situation that applicable, use and Reference numeral identical in Fig. 1.Wood pulp by boiling to the Kappa number of 50-120, common 60-100 is transferred to purge tank 3 by purge pipeline 2 from the bottom of boiling vessel 1, and paper pulp is pumped into one or several washer 5 by pipeline 4 from purge tank 3.Described washer is generally single drum wash device, and the pressure roller washer of for example being manufactured by Andritz is Drum Displacer
tM(DD)-washer, or diffuser or suction drum wash device.Before, by so-called boiling vessel washing, in digester bottom, the paper pulp to boiling is washed.The washing facility that is used for the paper pulp of boiling is the E of boiling vessel washing and washer 5
10value is at least 8, is at least preferably 10.
The paper pulp of washing is introduced in oxygen stage.In this embodiment, the first and second oxygen stage have respectively a reaction vessel 8 and 19, but can have more container, as shown in Figure 1.With the device of Fig. 1, compare, other difference is the processing of filtrate of the washer in oxygen stage downstream.In described oxygen stage, particularly, in the first processing, discharge a large amount of lignin.When the amount of the lignin of removing for example is 40 Ka Bai unit, the quantitative change of the organic material discharged from paper pulp is high.Along with described card uncle's decline, for example the ratio of lignin be only approximately 7% of paper pulp dry, and other carbohydrate loses.Given this, the solution C OD that characterizes organic substance in filtrate measures and can rise to 100-200kg/adt because of lignin.In Fig. 2,30-70 the unit if the Kappa number especially in reaction vessel 8 has descended, the filtrate of the washer 12 in the first oxygen stage 8 downstreams is contained a large amount of lignin.Therefore, by can known method itself, for example, by precipitation or filter filtrate 25 separating lignins of the washer 12 from the stage 29.Can apply multiple lignin separation method herein.Advantageously, the first oxygen treatments applied is used NaOH to replace the white liquid of oxidation to avoid sulphur compound as alkali.The lignin fraction reclaims with the low-sulfur form, thus advantageously used as the raw material of chemical industry.The result of lignin separation is, it is clean that filtrate liquid becomes, and in the boiling vessel downstream and washer 5 places of oxygen treatments applied upstream use filtrates, the filtrate that is derived from described washer is transferred to the boiling vessel washing by pipeline 32.To be used as the paper pulp wash liquid at washer 5 places under the condition of not separating lignin containing the filtrate 25 of lignin in Fig. 1.
Then, the form by the result of campaign with table shows, wherein in conjunction with oxygen stage, by multiple order, paper pulp is processed.To the Scandinavian(Scandinavia) softwood pulp (SW) tested.According to the data in table, notice, the delignified pulp lignin that will utilize acid peroxide (Caron acid) or chlorine dioxide treatment is to about 15 Kappa number level.And only or Kappa number at all untreated paper pulp acid-treated with hypochlorite in 20 level.Results verification the following fact: in oxygen stage, the card of Gao Kabai paper pulp uncle descends up to about 80%.Reactivation about oxygen stage with paper pulp, require to utilize electrophilic chemicals (Caron acid or chlorine dioxide) to be processed.Can be by this association with pulp bleaching to high brightness.
This method can provide a kind of efficient washing and delignification method, and described method is for from Gao Kabai pulp manufacture paper pulp, and the quality that makes paper pulp can be not deteriorated and yield is good.
Although above-mentioned explanation relates to embodiment of the present invention, described embodiment is considered to most preferred in view of existing knowledge, but be apparent that for those of ordinary skills, in the possible range the most widely limited separately by appended claims, can to the present invention, be improved with many different modes.
Claims (15)
1. a method of processing chemical pulp, in described method
By in alkaline digesting technoloy, the wood chip boiling being manufactured to paper pulp to the Kappa number of 50-120, preferred 60-100,
Paper pulp to described boiling is washed,
The paper pulp of described washing is introduced in oxygen stage, wherein under oxygen and alkali exist, described paper pulp is processed with except delignification, and the paper pulp of described oxygen treatments applied is washed, form thus the wash filtrate containing lignin, described method is characterised in that,
In described oxygen stage, at least 30 units of the Kappa number of described paper pulp decline, and
Filtrate to the washing in described oxygen stage downstream is processed with separating lignin, and using the filtrate of described processing as wash liquid, introduces in described washing facility with the paper pulp for described boiling.
2. method according to claim 1, is characterized in that, for the E of the described washing facility of the paper pulp of described boiling
10value is at least 8, is at least preferably 10.
3. method according to claim 1 and 2, is characterized in that, in described oxygen stage, and at least 35 Ka Bai units of the Kappa number of described paper pulp decline.
4. according to claim 1,2 or 3 described methods, it is characterized in that, during described oxygen stage, described alkali is NaOH.
5. according to the described method of any one in aforementioned claim, it is characterized in that, described paper pulp was not sieved before described oxygen stage, but sieved thereafter.
6. method according to claim 5, is characterized in that, described paper pulp is processed in two oxygen stage, and sieved between the washing in described the first oxygen stage and described the second oxygen stage downstream.
7. according to the described method of any one in aforementioned claim, it is characterized in that, described method is included in utilizes oxygen to process knaur separation before to described paper pulp.
8. according to the described method of any one in aforementioned claim, it is characterized in that, by the described lignin of precipitate and separate.
9. according to the described method of any one in aforementioned claim, it is characterized in that, described digesting technoloy is sulfate process.
10. according to the described method of any one in aforementioned claim 1-8, it is characterized in that, described digesting technoloy is soda process or its improvement.
11., according to the described method of any one in aforementioned claim, it is characterized in that, washing is discharged and caused to described paper pulp from described boiling vessel, wherein in the mechanical fiber seperator between described boiling vessel and described washing, do not processed.
12. according to the described method of any one in aforementioned claim, it is characterized in that, the lignin of described separation reclaimed and directly used or further processed.
13. the device to being processed by the paper pulp of wood chip manufacture in digesting apparatus, wherein by described wood chip chemical steaming to 50-120, the preferred Kappa number of 60-100, described device at least comprises:
For the digesting apparatus of cellulose fibre material, for the washing facility of the paper pulp of boiling,
Equipment in the washing downstream of the paper pulp of described boiling, it is in oxygen stage, described paper pulp being carried out to delignification,
The equipment after described oxygen stage, described paper pulp washed, and
The wash filtrate adverse current is caused to the filtrate line that aforementioned washer is usingd as wash liquid, it is characterized in that, described filtrate line in described oxygen stage downstream is provided with for the equipment from described filtrate separating lignin, and described filtrate line is connected to the washing facility for the paper pulp of boiling, described filtrate is used as to lignin separation wash liquid afterwards.
14. device according to claim 13, is characterized in that, described device comprises:
Washing facility, the paper pulp entry conductor of described washing facility is connected to the paper pulp delivery channel of described digesting apparatus, and described paper pulp delivery channel is connected to the paper pulp entry conductor of described oxygen treatments applied equipment, and
Washing facility after described oxygen treatments applied equipment, the paper pulp entry conductor of described washing facility is connected to the paper pulp delivery channel of described oxygen treatments applied equipment, so that described paper pulp is introduced in described washing facility, thus described lignin separation equipment is arranged in the filtrate line between described washing facility.
15. according to the described device of claim 13 or 14, it is characterized in that, for the E of the washing facility of the paper pulp of described boiling
10value is at least 8, is at least preferably 10.
Applications Claiming Priority (7)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI20115277A FI20115277A0 (en) | 2011-03-22 | 2011-03-22 | Method and arrangement for pulping |
| FI20115278A FI20115278A0 (en) | 2011-03-22 | 2011-03-22 | Method and apparatus for treating pulp |
| FI20115278 | 2011-03-22 | ||
| FI20115277 | 2011-03-22 | ||
| FI20115754A FI20115754A0 (en) | 2011-03-22 | 2011-07-15 | Process and arrangement for the treatment of chemical pulp |
| FI20115754 | 2011-07-15 | ||
| PCT/FI2012/050272 WO2012127111A1 (en) | 2011-03-22 | 2012-03-21 | Method and arrangement for treating filtrate after oxygen delignification of chemical pulp cooked to a high kappa number |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103459711A true CN103459711A (en) | 2013-12-18 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012800144257A Pending CN103459711A (en) | 2011-03-22 | 2012-03-21 | Method and arrangement for treating filtrate after oxygen delignification of chemical pulp cooked to a high kappa number |
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| Country | Link |
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| US (1) | US20140102648A1 (en) |
| EP (1) | EP2689063B1 (en) |
| JP (1) | JP2014508866A (en) |
| CN (1) | CN103459711A (en) |
| BR (1) | BR112013023777A2 (en) |
| CA (1) | CA2830312A1 (en) |
| CL (1) | CL2013002640A1 (en) |
| FI (1) | FI20115754A0 (en) |
| RU (1) | RU2013146897A (en) |
| WO (1) | WO2012127111A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104330525A (en) * | 2014-09-24 | 2015-02-04 | 朱琳 | Method for rapid evaluation of caustic soda- anthraquinone process pulping process of eucalyptus |
| CN104345126A (en) * | 2014-09-23 | 2015-02-11 | 朱琳 | Method for quickly evaluating unik sulfate pulping technology |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104345125B (en) * | 2014-09-23 | 2016-02-17 | 周栋 | A kind of method of Fast Evaluation willow sulfate pulping technique |
| CN104950857A (en) * | 2015-06-24 | 2015-09-30 | 黄红林 | Pulping cooking control method based on soft sensing |
| EP3464713B1 (en) * | 2016-05-27 | 2023-09-27 | Fibratech Pte. Ltd | A method and a system for production of high molecular weight lignin |
| FI129846B (en) * | 2019-02-01 | 2022-09-30 | Andritz Oy | Method for producing oxidized lignin in kraft pulp mill |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1070969A (en) * | 1991-08-14 | 1993-04-14 | 友联坎普专利控股有限公司 | The application of wash press in the pulp alkali addition process |
| WO2001059204A1 (en) * | 2000-02-14 | 2001-08-16 | Kiram Ab | Process for oxygen pulping of lignocellulosic material and recovery of pulping chemicals |
| WO2009104995A1 (en) * | 2008-02-21 | 2009-08-27 | Lignoboost Ab | A method for separating lignin from black liquor, a lignin product, and use of a lignin product for the production of fuels or materials |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA1070909A (en) * | 1976-05-04 | 1980-02-05 | Canadian Industries Limited | Nitrogen dioxide-oxygen delignification |
| SE465815B (en) * | 1985-04-04 | 1991-11-04 | Knut Lundquist | PROCEDURE FOR IMPROVING WOOD WITH ALKALILIGNIN |
| US5525195A (en) * | 1989-02-15 | 1996-06-11 | Union Camp Patent Holding, Inc. | Process for high consistency delignification using a low consistency alkali pretreatment |
| US5164044A (en) * | 1990-05-17 | 1992-11-17 | Union Camp Patent Holding, Inc. | Environmentally improved process for bleaching lignocellulosic materials with ozone |
| ZA92566B (en) * | 1991-02-01 | 1993-07-28 | Alcell Tech Inc | Pulping of lignocellulosic materials and recovery of resultant by-products. |
| US5489363A (en) * | 1993-05-04 | 1996-02-06 | Kamyr, Inc. | Pulping with low dissolved solids for improved pulp strength |
| WO2000047812A1 (en) * | 1999-02-15 | 2000-08-17 | Kiram Ab | Process for oxygen pulping of lignocellulosic material and recovery of pulping chemicals |
| US6942754B2 (en) * | 1999-03-23 | 2005-09-13 | Oji Paper Co., Ltd. | Process for producing xylooligosaccharide from lignocellulose pulp |
| US20020129911A1 (en) * | 2000-10-16 | 2002-09-19 | Marcoccia Bruno S. | Process and configuration for providing external upflow/internal downflow in a continuous digester |
| SE0202711D0 (en) * | 2002-09-12 | 2002-09-12 | Kiram Ab | Alkaline process for the manufacture of pulp using alkali metaborate as buffering alkali |
| JP4039250B2 (en) * | 2003-01-16 | 2008-01-30 | 王子製紙株式会社 | Method for producing bleached pulp |
| EP2061927A2 (en) * | 2006-05-19 | 2009-05-27 | The Research Foundation of the State University of New York | Methods for carbonate pretreatment and pulping of cellulosic material |
-
2011
- 2011-07-15 FI FI20115754A patent/FI20115754A0/en not_active Application Discontinuation
-
2012
- 2012-03-21 RU RU2013146897/12A patent/RU2013146897A/en not_active Application Discontinuation
- 2012-03-21 BR BR112013023777A patent/BR112013023777A2/en active Search and Examination
- 2012-03-21 EP EP12761412.1A patent/EP2689063B1/en active Active
- 2012-03-21 CA CA2830312A patent/CA2830312A1/en not_active Abandoned
- 2012-03-21 CN CN2012800144257A patent/CN103459711A/en active Pending
- 2012-03-21 US US13/261,740 patent/US20140102648A1/en not_active Abandoned
- 2012-03-21 JP JP2014500430A patent/JP2014508866A/en active Pending
- 2012-03-21 WO PCT/FI2012/050272 patent/WO2012127111A1/en active Application Filing
-
2013
- 2013-09-13 CL CL2013002640A patent/CL2013002640A1/en unknown
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1070969A (en) * | 1991-08-14 | 1993-04-14 | 友联坎普专利控股有限公司 | The application of wash press in the pulp alkali addition process |
| WO2001059204A1 (en) * | 2000-02-14 | 2001-08-16 | Kiram Ab | Process for oxygen pulping of lignocellulosic material and recovery of pulping chemicals |
| WO2009104995A1 (en) * | 2008-02-21 | 2009-08-27 | Lignoboost Ab | A method for separating lignin from black liquor, a lignin product, and use of a lignin product for the production of fuels or materials |
Non-Patent Citations (1)
| Title |
|---|
| DANIELEWICZ ETL: "oxygen delignification of high-kappa number pine kraft pulp", <<FIBERS & TEXTILES IN EASTERN EUROPE>> * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104345126A (en) * | 2014-09-23 | 2015-02-11 | 朱琳 | Method for quickly evaluating unik sulfate pulping technology |
| CN104330525A (en) * | 2014-09-24 | 2015-02-04 | 朱琳 | Method for rapid evaluation of caustic soda- anthraquinone process pulping process of eucalyptus |
| CN104330525B (en) * | 2014-09-24 | 2016-03-23 | 梁朔 | A kind of method of Fast Evaluation Eucalyptus soda anthraquinone process technique |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2830312A1 (en) | 2012-09-27 |
| FI20115754A0 (en) | 2011-07-15 |
| EP2689063A4 (en) | 2014-10-15 |
| RU2013146897A (en) | 2015-04-27 |
| JP2014508866A (en) | 2014-04-10 |
| BR112013023777A2 (en) | 2016-12-06 |
| US20140102648A1 (en) | 2014-04-17 |
| EP2689063B1 (en) | 2017-08-16 |
| CL2013002640A1 (en) | 2014-01-31 |
| WO2012127111A1 (en) | 2012-09-27 |
| EP2689063A1 (en) | 2014-01-29 |
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Application publication date: 20131218 |