CN1839227B - Multi-stage AP mechanical pulping process with refiner flow line treatment - Google Patents
Multi-stage AP mechanical pulping process with refiner flow line treatment Download PDFInfo
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- CN1839227B CN1839227B CN2003801104737A CN200380110473A CN1839227B CN 1839227 B CN1839227 B CN 1839227B CN 2003801104737 A CN2003801104737 A CN 2003801104737A CN 200380110473 A CN200380110473 A CN 200380110473A CN 1839227 B CN1839227 B CN 1839227B
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- intermediate line
- alkaline peroxide
- machinery pulping
- paper pulp
- fiberizer
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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
- D21C9/16—Bleaching ; Apparatus therefor with per compounds
- D21C9/163—Bleaching ; Apparatus therefor with per compounds with peroxides
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
- D21B1/00—Fibrous raw materials or their mechanical treatment
- D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
- D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
- D21B1/14—Disintegrating in mills
- D21B1/16—Disintegrating in mills in the presence of chemical agents
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Abstract
The invention combines the step of adding chemicals such as alkaline peroxid e to an intermediate line after refining, with the step of applying chemicals such as alkaline peroxide as a pre-treatment before primary refining and/or applying chemicals such as alkaline peroxide at the primary refiner. This is implemented tin the preferred embodiment, by material, refining the material into a pulp in a superatmospheric refiner, and adding chemicals in the post refining blowline.
Description
Technical field
The present invention relates to a kind of technology of from lignocellulosic substance such as wood chip or analog, producing paper pulp by the mode of chemical-mechanical slurrying.
Background technology
Using basic peroxide chemicals (APMP) can be traced back to 1962 in the machinery pulping system.Since then, with regard to have many different technological designs develop into before the early stage of paste mill grinding or between stage applied chemistry material.In recent years, different chemical in the machinery pulping of fiberizer is handled how to influence pulp property and technical process has been carried out extensively and systematic research.For hardwood, to compare with caustic soda with other conventional chemical substance preliminary treatment such as alkaline sulfite, the preliminary treatment of alkaline peroxide (AP) generally makes it have better optical property, better bleachability and the higher paper output under similar strength.Compare with hydrogen peroxide after bleaching technology, the using basic peroxide makes some hardwood species, such have higher specific volume (bulk) under given tensile strength before defibrination.
In a broad sense, in the pulping process of alkaline peroxide fiberizer machinery pulping, during fiberizer defiber and the fibrillation or before, hydrogen peroxide, dissimilar alkali and the different stabilizer of hydrogen peroxide of different amounts are applied to lignocellulosic substance together.The early stage of development of this pulping process, two kinds of methods have been used.Wherein a kind of is the technology of using basic peroxide on wood chip, and finishes before bleaching or near finishing bleaching action; A kind of method in addition is to use all alkaline peroxides in fiberizer, before the alkaline peroxide of fiberizer is used, or without preliminary treatment or and stabilizing agent or carry out preliminary treatment together with other alkalescence.
Usually, will cause on treatment facility, forming the situation of dirt at adding chemical substance such as silicate before the fiberizer.Because the formation of silicate precipitates, the fiberizer self zone also can form dirt, particularly can cause the card polishing of fiberizer when handling soft wood.
Certain location application chemical substance in the fiberizer downstream has also been proposed.But, these schemes do not get around the situation of using Chemical Pretreatment or wood chip.In addition, this chemical substance that adds in the downstream is also incompatible with the high pressure of defibrination.
Summary of the invention
With compare in the position of fiberizer or during its upstream position applied chemistry material, in order to obtain bleaching efficiency relatively preferably, the present invention is directly introducing chemical substance immediately in lignocellulosic substance behind the defibrination.
Use together with alkaline peroxide preliminary treatment lignocellulosic substance before the technology of the introducing of the chemical substance in fiberizer downstream and use chemical substance such as the defibrination, wherein fiberizer can be one-level, secondary and/or three grades of fiberizers.Preferably, in order to obtain the advantage of high pressure defibrination, fiberizer is provided with a high-pressure bottle.
According to the present invention, the introducing of fiberizer chemicals downstream can be optionally and be used for APMP, the technology of (pretreated mixer chemical treatment) is used together to be referred to as P-RC, this technology is in conjunction with two kinds of ideas, a kind of idea is to use chemical substance such as alkaline peroxide to carry out preliminary treatment to the wood fibre charging before first defibrination, and another kind of idea is applied chemistry material such as an alkaline peroxide in the one-level fiberizer.
The preferred embodiments of the present invention are included in or locate to use near the atmospheric valve (blow valve) of the intermediate line of rearmounted fiberizer and surpass whole alkaline peroxides of 1/3rd (and/or the chemical substance that is used to bleach known in this field or other lignocellulosic substance is processed into the chemical substance of paper pulp or paper pulp precursor), and in soaking into, the chemistry of the thin slice of fiberizer and fiberizer upstream adds chemical substance, thereby produce the technology of conserve energy more, and make chemical substance that a better bleaching efficiency be arranged before discharging from fiberizer.
Compare with routine techniques, main benefit of the present invention is that more chemical reaction is moved on to the downstream, thereby have good chemical efficiency, thus in rearmounted fiberizer blow line, carry out the phase counterweight or the interpolation of more chemical substance and/or the interpolation of chemical stabilizer.
Further benefit of the present invention be reduced during the elementary defibrination of high pressure or before high temperature and/or the harmful effect that produces of other condition, this harmful effect is known as brightness and the formation that influences paper pulp.
Owing in high-pressure system, carry out, to compare with the APMP system of the P-RC of other type, another benefit of the present invention is to obtain more high-quality steam and/or heat, wherein primary refiner is open to atmosphere fully or import is open to atmosphere.
Description of drawings
By following accompanying drawing the present invention is better explained and illustrates, wherein:
What Fig. 1 showed is the flow chart of the APMP technology of general P-RC.
Figure 1A shows is the flow chart that lignocellulosic substance is transported to the step of the fiberizer that is provided with container when the atmospheric pressure and discharges during at atmospheric pressure.
Figure 1B shows is the flow chart that lignocellulosic substance is transported to the step of the fiberizer that is provided with pressure vessel when the atmospheric pressure and discharges during at pressure.
Fig. 1 C shows is will be provided with the primary pulp that generates in the fiberizer of container to be transported to flow chart in the high dense tower by conveying equipment under normal pressure.
Fig. 1 D shows is directly will be provided with the primary pulp that generates in the fiberizer of container to be transported to flow chart in the high dense tower under normal pressure.
Fig. 1 E shows is will be provided with the primary pulp that generates in the fiberizer of pressure vessel to be transported to flow chart in the high dense tower by conveying equipment.
Fig. 1 F is the flow chart of related embodiment of the present invention, demonstration be will be provided with the primary pulp that generates in the fiberizer of pressure vessel to be transported to step in the high dense tower.
Fig. 2 is the two kinds of prior aries and the P-RC table of comparisons relatively.
Fig. 3 is the relation curve of energy consumption and beating degree (freeness) among two kinds of prior aries and the P-RC.
Fig. 4 is the relation curve of energy consumption and density among two kinds of prior aries and the P-RC.
Fig. 5 is the curve of tensile of tensile development among two kinds of prior aries and the P-RC.
Fig. 6 is the curve of burst development among two kinds of prior aries and the P-RC.
Fig. 7 is the curve of brightness development among two kinds of prior aries and the P-RC.
Fig. 8 is the curve of the light scattering coefficient of paper pulp among two kinds of prior aries and the P-RC as the function of beating degree.
Fig. 9 is according to P-RC, and normal pressure and pressure vessel are handled the table of comparisons of aspen wood chip.
Figure 10 is according to P-RC, and normal pressure and pressure vessel are handled the table of comparisons of birch wood chips.
Figure 11 is the flow chart of the embodiment of the invention, demonstration be that the primary pulp that will produce in the fiberizer pressure vessel is transported to the step in the retention tower, and in the intermediate line that has control valve thereafter, add chemical substance.
Figure 12 is the flow chart of the embodiment of the invention, demonstration be that the primary pulp that will produce in the fiberizer pressure vessel is transported to the step in the retention tower, and add the chemical substance of alkaline peroxide in the intermediate line before the separator import.
Figure 13 is the flow chart of the embodiment of the invention, demonstration be that the primary pulp that will produce in the fiberizer pressure vessel is transported to the step in the retention tower, and in the intermediate line of separator, add the chemical substance of alkaline peroxide.
Figure 14 is the flow chart of the embodiment of the invention, demonstration be that the primary pulp that will produce in the fiberizer pressure vessel is transported to the step in the retention tower, and in the intermediate line that separator is discharged, add the chemical substance of alkaline peroxide.
Figure 15 is according to the present invention, adds chemical substance processing white birch and the blow line of maple wood chips and the table of comparisons of refiner eye.
Figure 16 is according to the present invention, adds chemical substance processing dragon spruce and the blow line of red pine wood chips and the table of comparisons of refiner eye.
Figure 17 is according to the present invention, adds the blow line of chemical substance processing wood chip and the table of comparisons of refiner eye under elevated pressures.
Figure 18 is the flow chart of the embodiment of the invention, demonstration to be the primary pulp that will produce in the pressure vessel be transported to step in the tower by intermediate line.
The specific embodiment
Fig. 1 has introduced the simplified flow chart of P-RC alkaline peroxide machinery pulping (APMP) technology.P-RC technology is generally soaked in the step/ phase 1,2 in chip pretreatment/chip and is used alkaline peroxide, and mass transport is in primary refiner 3 simultaneously.
The pre-treatment step of finishing in stage 1 and 2 among Fig. 1 preferably includes one or both normal pressure compression devices, as pressafiner.Chip material is sent into by import, at least through a constricted zone and an extended region, discharges then.Chemism solution (pretreatment solution) joins in the material, normally or when discharging decompress(ion), be penetrated in the material thereby help solution.
The step of carrying out after the elementary defibrination can be carried out in the downstream of fiberizer by the chemical substance of varying level, perhaps carries out in the upstream of other technology.In one embodiment of the invention, Hou Zhi defibrination electrochemical conditions improves by intermediate line solutions additive or the additive that is added into the solution of intermediate line.Intermediate line is located between fiberizer and the retention tower.For example, as shown in figure 11, after discharge or the exposure, alkaline peroxide solution is used for the paper pulp of blow line 30 intermediate line from fiberizer.Chemical substance can be used near blow line 30 or along the point of blow line 30.
Injecting chemical substance in the position of intermediate line can inject by hole on the intermediate line or syringe such as the nozzle related with pipeline.Nozzle can be in a different manner along or near intermediate line, be provided with, be beneficial to control chemical additive.For example, the effect of additive in bleaching process and/or PROCESS FOR TREATMENT depended in control.Thereby the chemical substance in the paper pulp stream can be carried out modification by injection sequence, flow velocity, component and/or duration and kept.The other factors that the structure of the degree of depth that other variables such as syringe inject on stream, the angle of syringe, injector orifice and syringe are installed can improve to obtain ideal results.Can change the introducing of chemical substance by the introducing position of the pressure change chemical substance in defibrination, used.For example, alkaline peroxide can be behind atmospheric valve be introduced (less than several inches to several feet) immediately, special pressure less than the low pressure defibrination under the situation of 45psi in.Alkaline peroxide also can the cyclone separator after atmospheric valve before (less than several inches to several feet) introduce immediately, use at pressure especially greater than the high pressure defibrination under the situation of 45psi.In other cases, alkaline peroxide can be between cyclone separator and atmospheric valve, even introduces in cyclone separator.
Fiberizer can be elementary, secondary and/or three grades, and is provided with pressure vessel or discharges pressurization fully from being preheating to fiberizer.Pressure in the fiberizer helps when discharging paper pulp to be discharged from fiberizer.Discharge can be by changing as atmospheric valve or controlling.The pressure that helps paper pulp to be discharged to intermediate line can make the retention time of paper pulp in the part intermediate line be several seconds to a few minutes.Paper pulp has very high speed and violent disturbance when flowing through intermediate line.These situations have strengthened the mixing between chemical substance and the paper pulp.Paper pulp stream terminal strong disturbance and high thermograde also help chemical substance is transported in the independent paper pulp fiber and fibre wall in.
In example, paper pulp can be about 100 ℃ or higher, and chemical liquid can be about 40 ℃ or lower.Solution preferable range in the intermediate line is about 10 ℃-25 ℃, but can be as high as 80 ℃.It is when having improved temperature and/or pressure that the application of intermediate line alkaline peroxide can reduce alkaline peroxide open-assembly time in high temperature, particularly defibrination.This when being injected in rearmounted defibrination in paper pulp substance help and make things convenient for the stable of hydrogen peroxide and strengthen effect.In intermediate line of the present invention, use and be higher than atmospheric refiner system the steam/heat/liquid in the paper pulp can better be utilized again.This steam can shift by jet chimney 36.These characteristics also can make paper pulp that high beating degree is arranged, and contain the chips of low content, and well known in the art is that higher defibrination pressure can produce low content chips or clean paper pulp.In some instances, pressure can be included in the cyclone separator 32 or replace cyclone separator 32.Pressure helps to increase the utilization again of the steam/heat/liquid in the paper pulp.
In one embodiment of this invention, can realize influencing the optimum process of hydrogen peroxide effectiveness and brightness development when pressurizeing fully when elementary defibrination.Be referred to as P-RC APTMP in an ad hoc structure, this is entirely normal pressure or inlet pressure with container pressure in the primary refiner is that the P-RC APMP of normal pressure is different.
That Figure 1A represents to Fig. 1 F is the different embodiment of P-RC technology shown in Figure 1.For example, Figure 1A, 1B represent be at material in 1 and/or 2 after the preliminary treatment, in lignocellulosic substance, add solution can be more significantly near the downstream of cross conveyer 10, pressafiner and fiberizer 3 or generation in the fiberizer itself, the entry zone of advancing hole 14 and/or fiberizer plate 16 on the parts of fiberizer itself such as ribbon feeder 12, the fiberizer dish.Chemical additive used herein is " joining the material in the fiberizer ", near position 10,12,14 and 16.Fiberizer in the P-RC technology can be provided with non-pressure vessel 3A or pressurizing vessel 3B, but the import of fiberizer normal pressure normally.Can fall by gravity from the discharge of the pressurizing vessel 20a of preliminary defibrination.In any case, the discharge of fiberizer directly or indirectly is transported to (but being subjected to temperature controlled influence) in the high concentration bleaching tower 24 well known in the art.
In one embodiment of the invention, chemical reaction takes place in pretreatment solution, refiner solution (if there is) and intermediate line solutions in lignocellulosic substance.According to lignocellulosic substance and process equipment, in order to optimize technology, and/or eliminate or reduce undesirable chemical effect and destruction, revise the exposure of material in chemical reagent and be good.This chemical correction can add chemical additive and finish by order in the whole technology, and can be in conjunction with the condition of other variation such as temperature, concentration, pressure and the duration of further improving beneficial effect.
Lignocellulosic substance with the P-RC PROCESS FOR TREATMENT can discharge 4 as having the primary pulp that can survey beating degree, the paper pulp that is referred to as to form handmade paper that can be suitable from primary refiner container (20a is discharged in normal pressure discharge 20 or pressurization).Shown in Fig. 1 C and D, normal pressure in the fiberizer discharge can by transmission equipment 22 as the screw rod transmission device transmission in tower 24, or more directly transmit 28 by chute or similar devices.Shown in Fig. 1 E and F, in pressurizing vessel, concise paper pulp can be discharged by atmospheric valve usually, directly or indirectly is transported in the tower.Selectable, shown in Fig. 1 C and E, the paper pulp of bleaching in the tower can further further be handled in as the secondary grinding pulp grinder.The high concentration of retention tower 24 can allow the chemical bleaching reaction to continue to carry out from the upstream of tower always.
In one embodiment of the invention, as shown in figure 15, the effluent in the atmospheric valve can be by in the indirect feed track retention tower of separator and/or pressure.
A large amount of alkaline peroxides in the primary refiner (making a large amount of chemical reactions transfer to the chemical treatment stage of fiberizer) have improved efficient.This is because the variation of chip form and quality, except the natural character of wood chip and fiber different, is not impossible, often makes the preliminary treatment/impregnation stage of wood chip be difficult to obtain good chemical distribution.In these cases, the hybrid reaction in the primary refiner helps to improve chemical distribution, thereby has improved chemical efficiency.
According to one embodiment of the invention, in rearmounted defibrination intermediate line, add chemical substance and can use pressurized refiner and higher temperature defibrination.For example, in the intermediate line of blow line, add chemical substance and help to provide fast and distribution more direct chemical substance, cut the colour solid position with effective bleaching as hydrogen peroxide is distributed to.Because the target hydroperoxidation in useful reaction position very fast response, does not expand to more uniform position in the technology forward part, thereby can obtain this efficient.Usually, the inlet temperature between the fiberizer plate has been removed a section colour solid, and makes the hemicellulose alkali reaction carry out very soon, thus the too early reduction of pH.According to another embodiment of the present invention, carry out chemical mixing in the intermediate line of rearmounted defibrination and make the very fast distribution of chemical substance, thereby enough overcome the paper pulp temperature rise to a great extent.For example this temperature rise is about 80 ℃-155 ℃.
In one embodiment of this invention, paper pulp can remain in the interstage high consistency retention tower.The concentration of the paper pulp in the high consistency retention tower is about 20%-40%, preferably is about 30%.The temperature of the paper pulp in the high consistency retention tower is about 60 ℃-95 ℃.According to the needed chemical reaction of chemical treatment, paper pulp can keep in retention tower about 30 minutes to 2 hours.Conservation condition includes but not limited to temperature, pressure, pH, chemical concentrations, solid concentration and time, and these conditions can be controlled and/or bleached pulp, thereby continues to limit the decomposition of the bleaching agent that causes with the incoherent reaction of association with pulp bleaching.This incoherent reaction can be no production meaning, poor efficiency and/or harmful to association with pulp bleaching.For example, according to the situation and the type of the lignocellulosic substance that uses in the technology, and according to type, size and the operating condition of equipment self, may need, also may not need the control of some and/or used condition.For example, the condition of temperature can change by adding, gas-pressurized and other heating or the cooling means of chemical substance in the technical process.The change approach of temperature can use during the conveying of primary pulp equipment 22, utilizes mixing screw to add entry when paper pulp mixes and is transported to tower and realizes.If primary pulp directly is discharged in the tower 28, the temperature of primary pulp also can heat adjustment by mode well known in the art in tower.For example, paper pulp can carry out the adjustment of heat by adding liquid or gas, and/or uses heat exchanger such as tubular type, heat exchanger such as tower to adjust.
Term used herein " control " be construed as comprise initiatively with passive.Thereby control can be passed through the follow-on test of static hardware structure or one or more technological parameters, and controls one or more state-variables and realize.
Electrochemical conditions among the present invention in the creationary technology can stop incoherent reaction to be revised by additive.For example, this correction can be carried out in pre-treatment step 1 and/or 2, and at plate, atmospheric valve 20a, blow line 30, the separator 32 on hole, the fiberizer dish 16 of advancing of cross conveyer 10, ribbon feeder 12, fiberizer dish 14, and and/or separator after carry out.The example of stabilizing agent can be a complexing reagent.Complexing reagent refers to and can form the compound that is referred to as complex compound association with the metal that lignocellulosic substance closes in the elementary middle paper pulp.These metals comprise monovalent metal sodium and potassium, earth-alkali divalent metals calcium, magnesium and barium, and heavy metal such as iron, copper and manganese.The metal ion that is retained in the process in the material makes that oxidation bleaching (as hydrogen peroxide) effect is relatively poor, thereby causes the luxus consumption of chemical substance commonly known in the art.In order to reduce or to eliminate the influence of these metal ions in technology, can use complex compound such as diethylene triamine pentacetic acid (DTPA) (DTPA), edathamil (EDTA) and nitrilotriacetic acid (NTA).Other known complexing agent of this area can be used alone or in combination according to process conditions.In addition, silicate known in this field and sulfate can be used as stabilizing agent, have other function simultaneously.
Further embodiment of the present invention and scheme can describe by following example.
Embodiment
A organizes embodiment
Several different test technologies have been shown among the following embodiment.Unless stated otherwise, the material of following example and condition are as follows: timber; The mixing of 50% white poplar and 50% linden in this research.The white poplar center is rotten, thereby than the difficulty bleaching of expecting usually.Timber all from the Wisconsin of the U.S., is further being debarked earlier, is being chipped and primary election before the processing.
Chemical immersion: wood chip is used steam pre-treatment 10 minutes earlier, soaking money with the alkaline peroxide chemical liquid, suppresses at 4: 1 with compression ratio with the 560GS impressafiner of Andritz then.Chemical liquid is introduced when pressure discharges, and allows 30 minutes retention time before defibrination.
Defibrination: in all defibrination processes, use be that (36 ") model, 401 double disc atmospheric refiner, conventional rotating speed is 1200rpm to Andritz 92cm.Between elementary and secondary, there are 15 minutes or more retention time, do not have solution before the secondary afterwards elementary.Refining concentration is 20% at elementary and secondary.
The paper pulp test: except beating degree, what used paper pulp test was adopted is the standard of paper pulp papermaking and TIA (Tappi), and what beating degree was followed is the method for testing of canadian standard freeness (CSF).
Compare three kinds of technologies.In first technology, all alkaline matters (3.3% total alkalinity, (TA) and 2.4% H have been used in immersion (preliminary treatment) stage of wood chip
2O
2, and 0.2%DTPA, 0.07%MgSO
4And 3%Na
2SiO
3) (only using the chip impregnation in a stage), defibrination under normal pressure then.Therefore, this " technology " is referred to as " wood chip ".Second kind of technology has almost been used total peroxide chemicals of 2/3rds (or 2.4%TA, 1.6%H in the chip impregnation stage
2O
2, 0.08%DTPA, 0.04%MgSO
4And 2.4%Na
2SiO
3), and in the eyelet of primary refiner, used about 1/3rd chemical substance (1.0%TA, 1.0%H
2O
2, 0.19%DTPA, 0.05%MgSO
4And 0.9%Na
2SiO
3); This technology is referred to as " chip+refiner ", represents the present invention.In being called the third technology of " fiberizer ", wood chip is at first suppressed with the method in the aforementioned technology, all then alkaline peroxide chemical substance (4.2%TA, 3.3%H
2O
2, 0.36%DTPA, 0.11%MgSO
4And 4.3%Na
2SiO
3) in the eyelet of primary refiner, use.In all technology, before the defibrination of second stage, the paper pulp that elementary defibrination obtains keeps 15 minutes (temperature is about 80-90 ℃) in the drum lid.Do not clean in the middle of not having.
Fig. 2 has summed up some process conditions and the result of every kind of technology.Paper pulp is that the second stage defibrination obtains.At the hydrogen peroxide bleaching stage of machinery pulping, lower TA/H
2O
2Ratio at high temperature is preferably the possibility that prevents or reduce the reaction of alkalescence dead colorization usually.Owing to this reason, TA/H as shown in table 1, minimum
2O
2Ratio 1.27 is used for " fiberizer " technology, and next to the lowest 1.31 are used for " chip+refiner " technology, and the highest 1.37 are used for " wood chip " technology.In " fiberizer " technology, more TA (4.2%) be used to prevent pH since the heat that high temperature and defibrination produce during defibrination, descend too soon or too slow.Among Fig. 2, keep the hydrogen peroxide and the pH of reasonable amount in every kind of technology.
From the angle of chemistry, " wood chip " and " chip+refiner " between main difference be that the latter tends to more peroxide chemicals is transferred to the chemical treatment stage of fiberizer more.
The data of collecting behind the second defibrination in the different process of examination are presented in the curve of Fig. 3-8.Fig. 3 shows be the different chemical material to the influence of pulp beating degree and the relation of energy expenditure rate (SEC), energy expenditure rate is included in the energy of wood chip pretreatment stage consumption.The SEC of " wood chip+technology " is slightly less than " wood chip " technology, but the SEC of two kinds of technology mean consumptions is about 200kwh/odmt, less than the fiberizer bleaching process, although compare with aforesaid two kinds of technologies, latter's " fiberizer " has used more corrosive chemical, but " chip+refiner " technology has identical residue pH value, promptly 8.2.Therefore, in refiner eye, add alkaline chemical during high temperature and cause, perhaps produce the irrelevant side reaction of pulp property progress at the more alkali of nonproductive consumption.
Should be noted that in commodity production, the SEC of the chemical-mechanical pulping of hardwood is generally less than the result who obtains in the laboratory.Therefore, the SEC value among Fig. 3 is preferably used in contrast, rather than uses its absolute value.
Owing to the performance, particularly strength character of many paper pulp, depend on the density of handmade paper, this performance is also analyzed with SEC, and the result is as shown in Figure 4.In this case, for stronger refiner chemical treatment P-RC APMP technology, " chip+refiner " technology has best efficient for the improvement of handmade paper density, this in " wood chip " and " fiberizer " technology too.These results show that in chemical-mechanical pulping machining energy efficient not only depends on uses for how many chemical substances, also depends on how to use these chemical substances.
But, for the intrinsic property of paper pulp, some difference in these three kinds of technologies, as illustrated in Figures 5 and 6, this shows that as long as add chemical substance before defibrination the mechanism that influences the fibre strength performance remains equally.
For the optical property of paper pulp, in machinery pulping, the brightness of paper pulp is relevant with beating degree usually.Fig. 7 shows the brightness of different beating degrees in every kind of technology.What is interesting is that " chip+refiner " technology and " fiberizer " technology are similar to the influence of brightness, even aforementioned less albic material, the i.e. 2.6%H of having used
2O
2/ 3.4%TA contrasts 3.3%H
2O
2/ 4.2%TA.Add all chemical substances in impregnation stage, have the bleaching efficiency of 2 or more a plurality of points to be lower than " chip+refiner " technology in " wood chip " technology.This shows that how bleaching efficiency distributes for the chemical substance between chip impregnation and the defibrination in the P-RCAPMP process is responsive.The comparison that adds all chemical substances in this case in chip impregnation stage or the refiner eye is the most effective in bleaching and hydrogen peroxide consumption.
Fig. 8 is presented in the technology of all researchs, and light scattering property does not have difference, and this shows that the surface of paper pulp forms mechanism and still is consistent as long as add chemical substance before defibrination.
B organizes test
What following example showed is a kind of different defibrination structure, and wherein the pressure test of primary refiner import can be ignored, the pressure in the container (near 140KPa).The advantage of this structure is:
Better carry out the fiberizer (300t/d or higher) of steam treatment, particularly high power capacity when 1) fiberizer is discharged;
2) conveniently primary pulp is transported in middle high concentration (HC) tower from fiberizer;
3) can use some steam (by cyclone separator separate vapour and paper pulp fiber) that produce in the elementary defibrination;
4) be easy to the existing TMP conversion journey P-RC APMP of system technology.
These examples show: the bleaching efficiency that uses primary refiner and container to obtain during all as normal pressure with import under low pressure (140KPa) container and import are the situation of normal pressure is identical.Before paper pulp left container and fiberizer plate, the temperature between the temperature of import and primary refiner plate can be removed and be cut colour solid and make the hemicellulose basic hydrolysis enough fast, thereby pH is quite low.Paper pulp that discharge from primary refiner, the cyclone separator is tested in following example, and pH value scope is 9.3-9.7, even wherein hydrogen peroxide also is easy to stablize under observed high temperature (80-90 ℃).
The material and the condition of following test are as follows:
Timber: the timber of using in this research is white poplar and the birch wood chips from pulp mill's purchase of Canadian east.
Chip impregnation: adopt conventional test wood chip dipping systems in this research.In the P-RC of all researchs APMP, have only DTPA to use in the phase I of chip impregnation.Wood chip soaks with alkaline peroxide (AP) in second stage then.Before defibrination, the processing wood chip of AP keeps 30-45 minute (not having steam).
Atmospheric refiner system: in the P-RC APMP technology of examination, use Andritz36 " double plate 401 systems of diameter (92cm) usually.This system comprises twin-screw feeder, fiberizer and the open belt emission of opening measurement belt, inclination.This system is used for defibrination elementary and subsequently.When being used for elementary defibrination, the paper pulp of discharge is collected with drum, and with covering, at high temperature (is generally 80-90 ℃) and places a period of time.
" diameter (92cm) compression system repacks the structure of atmospheric inlet/pressurizing vessel into to pressurized refiner system: Andritz single-deck 36.Original refiner system has the standard feature of conventional TMP system.Import department is a normal pressure when making the operation of this system, is provided with a valve at the top of vertical steam pipe, and valve keeps open when defibrination.During test, plug screw feeder (PSF) running speed is 50rpm (rated speed of TMP is 10-20rpm), thereby the wood chip of guaranteeing chemical immersion is not compressed.The wood chip that AP soaks is placed in the chip bin, and chip bin is transported to wood chip in the air blast (blower).Wood chip is blown in the cyclone separator then, and is displaced in the conveyer of PSF charging.Wood chip falls into vertical steam pipe before entering fiberizer then.During defibrination, the Pressure control of primary refiner import is zero, and the pressure in the container is 140KPa.Primary pulp is blown in the cyclone separator, and discharges and to be collected in the drum, handles with the similar mode of normal pressure defibrination then.
The paper pulp test: luminance test adopts the TAPPI standard.The hydrogen peroxide residue is measured with the standard iodine titration.
To the white birch bought and white poplar wood chip in the primary refiner that is provided with pressurizing vessel and atmospheric inlet defibrination and the defibrination among the P-RC APMP compare.The result shows that the bleaching efficiency of these two kinds of defibrinations is close.For some equipment, can simplify the operation of technology, engineering and P-RC APMP technology greatly with pressurizing vessel.
What Fig. 9 represented is the electrochemical conditions that white poplar is used in P-RC APMP, and the brightness of pressurization and the acquisition of non-pressure vessel primary refiner.The AP chemical substance of applications similar in two kinds of containers, and total chemical depletion amount (H of the 5.2-5.4% of total alkali, TA, 3.7-3.9% of similar amount
2O
2), normal pressure obtains similar brightness with pressurizing vessel, obtains the ISO of 84.2%ISO and 84.7% respectively.
Residue pH (8.8-9.0) in two containers is higher than ideal value (near 7.0-8.5), H a little
2O
2Residue (1.5-2.0% on the o.d. paper pulp) also is higher than normal value (0.5-1.0%), and this shows that if chemical treatment is optimized then the pulp property in two containers can further improve.
It is pointed out that the bleaching efficiency (3.7-3.9%H shown in the table 1
2O
2, consume 4% TA, the ISO brightness that obtains is 84.2-84.7%) contrast or be better than TMP or CTMP paper pulp at H
2O
2In bleaching efficiency.
What Figure 10 represented is the result and the condition of the P-RC APMP defibrination of white birch.This special birch wood chips is a little than the difficult bleaching of white poplar.Use similar AP chemical method, normal pressure and pressure vessel once more, obtain close bleaching efficiency: 3.1-3.2%TA and 3.4-3.6%H
2O
2, the brightness of ISO reaches 82.4-82.6%.In this scheme, residual chemicals (0.1-0.2%TA, 0.5-0.6%H
2O
2With pH be 8) at desirable H
2O
2Conditions of bleaching in.
C organizes test
This group test shows, in other factors, when chemical formulation and distribution are optimized, can use in the intermediate line in pressurized refiner system in the alkaline peroxide chemical substance in refiner chemical treatment stage, thereby obtain and the close bleaching efficiency of P-RC APMP of import normal pressure.Because retention time in intermediate line is very short, identical technology also can be used for high pressure defibrination system, is beneficial in 4bar or the defibrination system that more moves under the high pressure.
Timber
Before further handling, all hardwood (white birch and maple) is processed into chip form, and mixes respectively.All corks (dragon spruce, pine and cork compound) were processed into round log and peeling and mixing before further handling.
Chip impregnation
Unless stated otherwise, wood chip is with soaking twice in AP chemical substance (comprising NaOH, hydrogen peroxide, DTPA, magnesium sulfate and sodium metasilicate) in the Andritz 560GS impressafiner system.In some cases, the RT-pressafiner uses (using 1.4bar steam treatment 20 seconds before compacting) in first impregnation stage.
Defibrination
Description of the process
P-RC (carry out preliminary treatment with refiner chemical treatment, wherein the AP chemical substance distributes between the stage in wood chip preliminary treatment and fiberizer) technology is used in all tests of carrying out.When filling in intermediate line for the AP chemical substance, according to the concrete defibrination energy that uses in the fiberizer, the electric charge of chemical substance and the performance of raw material, the paper pulp of discharging from blow line covers in the plastic bag of circular drum, and keeps 85-95 ℃.
The paper pulp test
All beating degree test canadian standard freeness (CSF), (brightness Tappi T218 OM-83, light scattering and absorption coefficient of light Tappi T425OM-86 (to handmade paper Tappi 205 OM-88) use the Tappi method to all optical performance tests.
Figure 15 shows uses the result that the AP chemical substance obtains in refiner eye or intermediate line be refiner chemical (RC) processing stage.White birch and maple have been used in this test.For every kind of timber variety, on its wood chip, carry out some Chemical Pretreatment (preliminary treatment).For birch wood chips, handle with 0.3%DTPA in first impregnation stage, then at the second impregnation stage 0.2%MgSO
4, 4.4% silicate, 2.8%TA and 2.8%H
2O
2Handle.For maple wood chips, handle with 0.5%DTPA in first impregnation stage, then at the second impregnation stage 0.1%MgSO
4, 2.0% silicate, 1.6%TA and 2.6%H
2O
2Handle.Pretreated wood chip is used the AP chemical substance treatment of analog quantity then refiner chemical (RC) processing stage, but in different sites: the refiner eye before defibrination, another follows the intermediate line behind the defibrination closely.
For white birch, the H of two kinds of technologies (A1 and A2) shared 5.2%
2O
2With 4.6% total alkalinity (TA), and the H with similar amount
2O
2Residue (1.0%-1.1%) and final pH (8.9-9.0).Final pH is high relatively, if use long retention time, then shows the acquisition higher brightness.With add AP chemical substance (A2) in intermediate line and compare, the sample brightness that adding AP additive obtains in refiner eye (A1) is close, as 84.8% couple of 84.2%ISO.Nuance in the brightness to small part may be the nuance of its beating degree, and the former container is 285ml, and the latter is 315ml.From the angle of chemistry, two kinds of technologies have the close absorption coefficient of light, and the former is 0.27m
2/ kg, the latter are 0.25m
2/ kg.
For maple, adding AP chemical substance (A4) in intermediate line in fact has higher brightness, and promptly 81.9%ISO is higher than the brightness of using the AP chemical substance in refiner eye (A3), i.e. 79.2%ISO.Difference in this case is that the former hangs down beating degree (295 couples of 320mL) and low absorption coefficient (0.32 couple of 0.5m
2/ kg) combination.
Cork, promptly dragon spruce and Korean pine also have been used for investigating the influence that different AP chemistry are used.Figure 16 has summed up these results, and is presented at refiner eye or intermediate line once more and uses the brightness that the AP chemical substance obtains being similar to.For dragon spruce, wood chip is at first used 0.3%DTPA, 0.05%MgSO
4, 0.7% silicate, 0.2%TA and 0.5%H
2O
2Soak, use 0.1%DTPA, 0.08%MgSO then
4, 1.8% silicate, 1.4%TA and 1.9%H
2O
2Carrying out the second time soaks.For Korean pine, wood chip is at first used 0.4%TA, 0.5%H
2O
2, 0.3%DTPA, 0.04%MgSO
4Soak with 0.5% silicate, use 0.4%TA, 0.6%H then
2O
2, 0.14%DTPA, 0.05%MgSO
4Carrying out the second time with 0.4% silicate soaks.For dragon spruce, for example as shown in figure 16, in blow line technology (A6), use and technology A5 similar amount AP chemical substance, obtain approximate or slightly high brightness, be 78.8%ISO to 78.2%ISO, wherein the AP chemical substance of the latter half is used for refiner eye among the A5.The nuance of this brightness may be their slightly beating degrees of difference once more, and promptly 47ml is to 49ml, and 0.56 couple of 0.60m of the absorption coefficient of nuance
2The combined influence of/kg.
For Korean pine, blow line technology, i.e. A8, A7 compares with refiner eye technology, has slightly high brightness, i.e. 71.8 couples of 71.2%ISO, the lower absorption coefficient of light, i.e. 0.84 couple of 1.01m
2/ kg, but higher beating degree is arranged, i.e. 99 couples of 82mL.For this situation, owing to the influence to brightness, the difference of the absorption coefficient of light may be that the difference of its beating degree causes.The chemically treated amount of AP is consistent in this two kinds of technologies.
As shown in figure 17, the cork of dragon spruce and pine tree is combined in the refiner chemical treatment stage and uses HIGH PRESSURE TREATMENT.In this case, the RT-pressafiner used in the phase I of soaking, and Andritz model 560GS impressafiner uses in second stage.For this chemical treatment, first impregnation stage 0.4%TA, 0.6%H
2O
2, 0.18%DTPA, 0.03%MgSO
4With 0.3% sodium metasilicate; Second impregnation stage 0.4%TA, 0.7%H
2O
2, 0.15%DTPA, 0.05%MgSO
4With 0.4% sodium metasilicate; Use 0.9%TA, 1.5%H in the refiner chemical treatment stage
2O
2, 0.18%DTPA, 0.09%MgSO
4With 1.8% sodium metasilicate, or in the refiner eye of A9, use, perhaps in the intermediate line of A10, use.For the technology A9 and the A10 that use, both have close chemical charge and prescription, but the pressure of A9 in primary refiner is 2.1bar, and the pressure in another A10 is 4.2bar.The result that Figure 17 represents shows bleaching efficiency and brightness (the usefulness 1.7%TA and the 2.8%H that can obtain to be similar in higher pressure process A10
2O
2, and reach 73.7-73.4%ISO).Sample has the close absorption coefficient of light (0.96-1.1m
2/ kg).These results show, after chemical method is optimized, and close bleaching efficiency and brightness (scope is at least 70-75%ISO) even can under very high pressure (4.2bar or 60psi), obtain.Compare with low pressure, the high pressure defibrination can utilize high-quality steam again with better efficient, simultaneously for hard beating pulp, has an opportunity to reduce fragment (fibre bundle).
Claims (33)
1. the method for an alkaline peroxide machinery pulping, wherein: lignocellulosic substance is preliminary treatment in a forcing press at least, when expanding, the lignocellulosic substance of discharging uses the alkaline peroxide solution soaking from forcing press, between two counterrotating dishes pretreated material is carried out defibrination in the fiberizer container, formation temperature is at least 80 ℃ primary pulp;
From pressure vessel be transported in intermediate line at least 80 ℃ the time primary pulp;
When the primary pulp temperature is at least 80 ℃, in the primary pulp of intermediate line, add the alkaline peroxide intermediate line solutions;
Mix intermediate line solutions and primary pulp, in intermediate line, form reactant mixture;
The reactant mixture that temperature is at least 80 ℃ is discharged in the preserving container;
In preserving container, keep reactant mixture, generate the material of bleaching.
2. the method for alkaline peroxide machinery pulping according to claim 1 is characterized in that fiberizer container wherein is in the high pressure.
3. the method for alkaline peroxide machinery pulping according to claim 1 is characterized in that fiberizer container wherein is a normal pressure.
4. the method for alkaline peroxide machinery pulping according to claim 1 is characterized in that fiberizer wherein is a primary refiner.
5. the method for alkaline peroxide machinery pulping according to claim 1 is characterized in that fiberizer wherein is the secondary grinding pulp grinder.
6. the method for alkaline peroxide machinery pulping according to claim 1 is characterized in that intermediate line wherein is provided with inlet part, and alkaline peroxide solution injects from described inlet part.
7. the method for alkaline peroxide machinery pulping according to claim 1 is characterized in that intermediate line wherein connects pressure vessel and paper pulp preserving container, and paper pulp remained in the preserving container before further handling.
8. the method for alkaline peroxide machinery pulping according to claim 1 is characterized in that paper pulp wherein kept a retention period in intermediate line before further handling.
9. the method for alkaline peroxide machinery pulping according to claim 1 is characterized in that the compacting back being suppressed once more with the material of alkaline peroxide solution soaking and expanding, and soaks once more with alkaline peroxide solution before the defibrination in described fiberizer.
10. according to the method for the described alkaline peroxide machinery pulping of arbitrary claim among the claim 1-9, it is characterized in that also injecting in the fiberizer alkaline peroxide solution.
11., it is characterized in that the alkaline peroxide of the adding of the paper pulp in intermediate line immediately solution after the atmospheric valve of intermediate line according to the method for the described alkaline peroxide machinery pulping of arbitrary claim among the claim 1-9.
12., it is characterized in that wherein said soaking solution contains alkali, peroxide and stabilizing agent according to the method for the described alkaline peroxide machinery pulping of arbitrary claim among the claim 1-9; Described intermediate line solutions contains alkali, peroxide and stabilizing agent; The temperature of described intermediate line solutions is less than 80 ℃.
13. the method for alkaline peroxide machinery pulping according to claim 1 is characterized in that:
When the paper pulp temperature is at least 80 ℃, paper pulp is transported to intermediate line from container;
Paper pulp when the paper pulp temperature is at least 80 ℃ in intermediate line adds alkaline peroxide; And
Mix intermediate line solutions and paper pulp, in intermediate line, form reactant mixture.
14. the method for alkaline peroxide machinery pulping according to claim 13 is characterized in that temperature is at least 80 ℃ reactant mixture to be discharged in the preserving container from middle pipeline.
15. the method for alkaline peroxide machinery pulping according to claim 14, it is characterized in that the mixing in the intermediate line after, and then mixture is transported in the paper pulp separator, then the paper pulp that separates is discharged in the described preserving container.
16. the method for alkaline peroxide machinery pulping according to claim 15, the step that it is characterized in that in paper pulp adding alkaline peroxide solution adds intermediate line solutions before being included in separator immediately.
17. according to the method for claim 1 or 14 described alkaline peroxide machinery pulpings, the temperature range that it is characterized in that being transported to from container the paper pulp of intermediate line is 80 ℃-155 ℃, concentration is 20-60%.
18. the method for alkaline peroxide machinery pulping according to claim 17, the temperature that it is characterized in that remaining on the mixture in the preserving container are 60 ℃-95 ℃, concentration is 20-40%.
19. the method for alkaline peroxide machinery pulping according to claim 18 is characterized in that it is that concentration is 30% in 85 ℃-95 ℃ the preserving container that wherein said reactant mixture remains on temperature.
20. the method for alkaline peroxide machinery pulping according to claim 7 is characterized in that:
Lignocellulosic substance is a wood chip;
Fiberizer is a primary refiner; And
Preserving container is a bleaching tower.
21. the method for alkaline peroxide machinery pulping according to claim 20, be provided with separator after it is characterized in that being provided with the intermediate line of atmospheric valve, the step that adds the alkaline peroxide intermediate line solutions in the primary pulp in intermediate line adds the alkaline peroxide intermediate line solutions before being included in separator immediately.
22. the method for alkaline peroxide machinery pulping according to claim 20, be provided with separator after it is characterized in that being provided with the intermediate line of atmospheric valve, the step that adds the alkaline peroxide intermediate line solutions in the primary pulp in intermediate line is included in the separator place and adds the alkaline peroxide intermediate line solutions.
23. the method for alkaline peroxide machinery pulping according to claim 20, be provided with separator after it is characterized in that being provided with the intermediate line of atmospheric valve, the step that adds the alkaline peroxide intermediate line solutions in the primary pulp in intermediate line adds the alkaline peroxide intermediate line solutions after being included in separator.
24. the method for alkaline peroxide machinery pulping according to claim 20 is characterized in that the primary pulp of bleaching in the bleaching tower wherein further is processed into the secondary paper pulp of bleaching.
25. the method for alkaline peroxide machinery pulping according to claim 24 is characterized in that the secondary paper pulp bleached is by following step production:
The elementary bleached pulp of defibrination once more;
Secondary paper pulp is discharged to from the secondary grinding pulp grinder in the intermediate line that is provided with at least one solution inlet port part;
Partly inject the alkaline peroxide intermediate line solutions by at least one solution inlet port;
Mix the secondary paper pulp in intermediate line solutions and the intermediate line;
From middle pipeline, discharge material; And
To keep based on the material of lignocellulose a stage of reaction.
26. the method for alkaline peroxide machinery pulping according to claim 9 is characterized in that the solution of wherein said immersion contains 0.3% DTPA; The described solution that soaks once more contains 0.2% MgSO
4, 4.4% silicate, 2.8% TA and 2.8% H
2O
2And described intermediate line solutions contains 0.16% DTPA, 0.16% MgSO
4, 2.3% silicate, contain 1.8% TA of 0.5% residue and contain 2.4% H of 1.1% residue
2O
2
27. the method for alkaline peroxide machinery pulping according to claim 9 is characterized in that the solution of wherein said immersion contains 0.5% DTPA; The described solution that soaks once more contains 0.2% DTPA, 0.1% MgSO
4, 2.0% silicate, 1.6% TA and 2.6% H
2O
2And described intermediate line solutions contains 0.13% DTPA, 0.13% MgSO
4, 2.5% silicate, contain 1.2% TA of 0.1% residue and contain 2.1% H of 2.1% residue
2O
2
28. the method for alkaline peroxide machinery pulping according to claim 9 is characterized in that the solution of wherein said immersion contains 0.3% DTPA, 0.05% MgSO
4, 0.7% silicate, 0.2% TA and 0.5% H
2O
2The described solution that soaks once more contains 0.1% DTPA, 0.08% MgSO
4, 1.8% silicate, 1.4% TA and 1.9% H
2O
2And described intermediate line solutions contains 0.22% DTPA, 0.11% MgSO
4, 1.1% silicate, contain 0.9% TA of 0.2% residue and contain 1.2% H of 1.7% residue
2O
2
29. the method for alkaline peroxide machinery pulping according to claim 9 is characterized in that the solution of wherein said immersion contains 0.4% TA, 0.5% H
2O
2, 0.2% DTPA, 0.04% MgSO
4With 0.5% silicate; The described solution that soaks once more contains 0.14% DTPA, 0.05% MgSO
4, 0.5% silicate, 0.4% TA and 0.6% H
2O
2And described intermediate line solutions contains 0.18% DTPA, 0.06% MgSO
4, 1.8% silicate, contain 1.2% TA of 0.1% residue and contain 1.8% H of 1.1% residue
2O
2
30. the method for alkaline peroxide machinery pulping according to claim 9 is characterized in that the solution of wherein said immersion contains 0.4% TA, 0.6% H
2O
2, 0.18% DTPA, 0.03% MgSO
4With 0.3% silicate; The described solution that soaks once more contains 0.15% DTPA, 0.05% MgSO
4, 0.4% silicate, 0.4% TA and 0.7% H
2O
2And described intermediate line solutions contains 1.7% TA and contains 2.8% H of 1.1% residue
2O
2
31. the method for alkaline peroxide machinery pulping according to claim 2 is characterized in that pressure in the fiberizer container wherein remains on to be at least 240KPa.
32. the method for alkaline peroxide machinery pulping according to claim 31, the temperature range that it is characterized in that being transported to from container the paper pulp of intermediate line is 80 ℃-155 ℃, and concentration is 20-60%.
33. the method for alkaline peroxide machinery pulping according to claim 32 is characterized in that wherein said soaking solution contains alkali, peroxide and stabilizing agent; Described intermediate line solutions contains alkali, peroxide and stabilizing agent; The temperature of described intermediate line solutions is less than 80 ℃.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/US2003/031341 WO2005042830A1 (en) | 2003-10-02 | 2003-10-02 | Multi-stage ap mechanical pulping with refiner flow line treatment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1839227A CN1839227A (en) | 2006-09-27 |
| CN1839227B true CN1839227B (en) | 2011-08-17 |
Family
ID=34548798
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2003801104737A Ceased CN1839227B (en) | 2003-10-02 | 2003-10-02 | Multi-stage AP mechanical pulping process with refiner flow line treatment |
Country Status (8)
| Country | Link |
|---|---|
| JP (1) | JP4580343B2 (en) |
| CN (1) | CN1839227B (en) |
| AU (1) | AU2003279120A1 (en) |
| BR (1) | BR0318520A (en) |
| CA (1) | CA2533535C (en) |
| FI (1) | FI20060305A (en) |
| SE (2) | SE0950616L (en) |
| WO (1) | WO2005042830A1 (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003008703A1 (en) | 2001-07-19 | 2003-01-30 | Andritz Inc. | Four stage alkaline peroxide mechanical pulping |
| US20040200586A1 (en) * | 2002-07-19 | 2004-10-14 | Martin Herkel | Four stage alkaline peroxide mechanical pulping |
| US8262851B2 (en) | 2006-08-10 | 2012-09-11 | Andritz Inc. | Processes and systems for the pulping of lignocellulosic materials |
| US8282773B2 (en) * | 2007-12-14 | 2012-10-09 | Andritz Inc. | Method and system to enhance fiber development by addition of treatment agent during mechanical pulping |
| US8734611B2 (en) * | 2008-03-12 | 2014-05-27 | Andritz Inc. | Medium consistency refining method of pulp and system |
| CN102011334B (en) * | 2010-11-11 | 2013-04-10 | 梁锋 | Method for pulping and making paper by using eucalyptus bark |
| EP4240900A1 (en) | 2020-11-06 | 2023-09-13 | Kimberly-Clark Worldwide, Inc. | High porosity non-wood pulp |
| US20240003087A1 (en) * | 2020-11-06 | 2024-01-04 | Kimberly-Clark Worldwide, Inc. | Dispersible non-wood pulp |
| WO2022098962A1 (en) * | 2020-11-06 | 2022-05-12 | Kimberly-Clark Worldwide, Inc. | High brightness non-wood pulp |
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|---|---|---|---|---|
| US4294653A (en) * | 1974-09-23 | 1981-10-13 | Mo Och Domsjo Aktiebolag | Process for manufacturing chemimechanical cellulose pulp in a high yield within the range from 65 to 95% |
| US4311553A (en) * | 1979-01-12 | 1982-01-19 | Sunds Defibrator Ab | Method for use in the defibration or refining of lignocellulose-containing fibrous materials |
| US4718980A (en) * | 1985-12-30 | 1988-01-12 | Weyerhaeuser Company | Interstage treatment of mechanical pulp |
| US4756799A (en) * | 1985-03-13 | 1988-07-12 | Eka Ab | Method of manufacturing bleached chemimechanical and semichemical fibre pulp by means of a one-stage impregnation process |
| WO1995034711A1 (en) * | 1994-06-15 | 1995-12-21 | SCA Mölnlycke AB | A light drainability, bulky chemimechanical pulp that has a low shive content and a low fine-material content |
| WO2003008703A1 (en) * | 2001-07-19 | 2003-01-30 | Andritz Inc. | Four stage alkaline peroxide mechanical pulping |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FI61215B (en) * | 1976-11-23 | 1982-02-26 | Defibrator Ab | SAFETY RANGE OF CONTAINER FRAMSTAELLA LIGNOCELLULOSAHALTIGA FIBERMATERIAL |
| CA1074606A (en) * | 1977-06-08 | 1980-04-01 | Llewellyn E. Clark | Method and apparatus for thermo-mechanical pulping |
| JPS5685488A (en) * | 1979-12-17 | 1981-07-11 | Mitsubishi Gas Chemical Co | Hydrogen peroxide refiner bleaching method of pulp |
| JPS5725492A (en) * | 1980-07-16 | 1982-02-10 | Mitsubishi Gas Chemical Co | Hydrogen peroxide refiner bleaching of high yield pulp |
| FR2613388B1 (en) * | 1987-04-02 | 1990-05-04 | Atochem | PROCESS FOR BLEACHING PASTA |
| FI113552B (en) * | 1999-12-09 | 2004-05-14 | Upm Kymmene Corp | Process for producing printing paper |
| JP2002294574A (en) * | 2001-03-30 | 2002-10-09 | Nippon Paper Industries Co Ltd | Method for bulky pulp production |
| US6743332B2 (en) * | 2001-05-16 | 2004-06-01 | Weyerhaeuser Company | High temperature peroxide bleaching of mechanical pulps |
| JP4814448B2 (en) * | 2001-08-06 | 2011-11-16 | 日本製紙株式会社 | Coated paper for printing |
-
2003
- 2003-10-02 BR BRPI0318520-6A patent/BR0318520A/en active Search and Examination
- 2003-10-02 AU AU2003279120A patent/AU2003279120A1/en not_active Abandoned
- 2003-10-02 CA CA2533535A patent/CA2533535C/en not_active Expired - Lifetime
- 2003-10-02 SE SE0950616A patent/SE0950616L/en not_active Application Discontinuation
- 2003-10-02 JP JP2005510190A patent/JP4580343B2/en not_active Expired - Fee Related
- 2003-10-02 WO PCT/US2003/031341 patent/WO2005042830A1/en active Application Filing
- 2003-10-02 CN CN2003801104737A patent/CN1839227B/en not_active Ceased
-
2006
- 2006-03-30 FI FI20060305A patent/FI20060305A/en not_active IP Right Cessation
- 2006-03-31 SE SE0600722A patent/SE532130C2/en not_active IP Right Cessation
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4294653A (en) * | 1974-09-23 | 1981-10-13 | Mo Och Domsjo Aktiebolag | Process for manufacturing chemimechanical cellulose pulp in a high yield within the range from 65 to 95% |
| US4311553A (en) * | 1979-01-12 | 1982-01-19 | Sunds Defibrator Ab | Method for use in the defibration or refining of lignocellulose-containing fibrous materials |
| US4756799A (en) * | 1985-03-13 | 1988-07-12 | Eka Ab | Method of manufacturing bleached chemimechanical and semichemical fibre pulp by means of a one-stage impregnation process |
| US4718980A (en) * | 1985-12-30 | 1988-01-12 | Weyerhaeuser Company | Interstage treatment of mechanical pulp |
| WO1995034711A1 (en) * | 1994-06-15 | 1995-12-21 | SCA Mölnlycke AB | A light drainability, bulky chemimechanical pulp that has a low shive content and a low fine-material content |
| WO2003008703A1 (en) * | 2001-07-19 | 2003-01-30 | Andritz Inc. | Four stage alkaline peroxide mechanical pulping |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2005042830A1 (en) | 2005-05-12 |
| CA2533535C (en) | 2012-01-03 |
| SE0600722L (en) | 2006-03-31 |
| BR0318520A (en) | 2006-09-12 |
| AU2003279120A1 (en) | 2005-05-19 |
| JP4580343B2 (en) | 2010-11-10 |
| SE0950616L (en) | 2009-08-27 |
| CN1839227A (en) | 2006-09-27 |
| JP2007521404A (en) | 2007-08-02 |
| FI20060305A (en) | 2006-03-30 |
| SE532130C2 (en) | 2009-10-27 |
| CA2533535A1 (en) | 2005-05-12 |
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