CN101389808A - A method for manufacturing mechanical pulp - Google Patents
A method for manufacturing mechanical pulp Download PDFInfo
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- CN101389808A CN101389808A CNA2007800069607A CN200780006960A CN101389808A CN 101389808 A CN101389808 A CN 101389808A CN A2007800069607 A CNA2007800069607 A CN A2007800069607A CN 200780006960 A CN200780006960 A CN 200780006960A CN 101389808 A CN101389808 A CN 101389808A
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- ozonisation
- mechanical pulp
- refining
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- 238000000034 method Methods 0.000 title claims abstract description 115
- 229920001131 Pulp (paper) Polymers 0.000 title claims abstract description 71
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 7
- 238000006385 ozonation reaction Methods 0.000 claims abstract description 51
- 238000007670 refining Methods 0.000 claims abstract description 36
- 239000002994 raw material Substances 0.000 claims abstract description 28
- 239000002002 slurry Substances 0.000 claims description 153
- 239000003513 alkali Substances 0.000 claims description 47
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 29
- 238000004061 bleaching Methods 0.000 claims description 4
- 235000008331 Pinus X rigitaeda Nutrition 0.000 description 26
- 241000018646 Pinus brutia Species 0.000 description 26
- 235000011613 Pinus brutia Nutrition 0.000 description 26
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 24
- 150000007524 organic acids Chemical class 0.000 description 19
- 239000007788 liquid Substances 0.000 description 15
- 238000010009 beating Methods 0.000 description 9
- 230000002349 favourable effect Effects 0.000 description 7
- 239000000123 paper Substances 0.000 description 6
- 238000004134 energy conservation Methods 0.000 description 5
- 239000012634 fragment Substances 0.000 description 5
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 238000006386 neutralization reaction Methods 0.000 description 4
- 235000005985 organic acids Nutrition 0.000 description 4
- 206010033546 Pallor Diseases 0.000 description 3
- 239000000835 fiber Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 241000351396 Picea asperata Species 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000007799 cork Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 2
- 239000000347 magnesium hydroxide Substances 0.000 description 2
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241000218657 Picea Species 0.000 description 1
- 235000008124 Picea excelsa Nutrition 0.000 description 1
- 235000005205 Pinus Nutrition 0.000 description 1
- 241000218602 Pinus <genus> Species 0.000 description 1
- 235000008582 Pinus sylvestris Nutrition 0.000 description 1
- 241000218626 Pinus sylvestris Species 0.000 description 1
- 244000007853 Sarothamnus scoparius Species 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000011121 hardwood Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 239000001839 pinus sylvestris Substances 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Images
Classifications
-
- 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
-
- 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
- D21C9/153—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications with ozone
Landscapes
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Paper (AREA)
Abstract
The present invention relates to a method for manufacturing mechanical pulp, the method comprising: introducing raw material of the mechanical pulp, refining the raw material in a first refining stage in order to form the mechanical pulp, adjusting the pH of the mechanical pulp between 9 and 11 in aprocess step in which a first process delay is arranged, the first process delay being at least 0.5 hours, sorting the mechanical pulp into a first accepted stock (A1) and a first rejected stock (R1), ozonizing the first rejected stock (R1) whose pH at the start of the ozonation process is between 9 and 11, refining the ozonated first rejected stock (R1) in a second refining stage so that at least a part of it will belong to a second accepted stock, and -combining the accepted stocks. The present invention also relates to the use of the mechanical pulp.
Description
Technical field
The present invention relates to be used for the method for manufacturing machine paper pulp.
Background technology
Disclosed with the ozone treatment process of pulp at open FI 61926 and corresponding disclosing among the DE 2444475.Can after ozonisation, adjust the pH value of paper pulp.
Open FI 67412 and corresponding openly C A1083870 have disclosed wherein the process with the paper pulp fractionation, and a cut (may be thick cut) is with ozone treatment.During ozonisation, alkali is supplied in the process.
The problem relevant with the ozonisation process is that this process has produced strong organic acid.Organic acid has reduced the pH value of paper pulp, and this has caused the problem in the bleaching process, for example owing to handle the problem that the precipitated iron material in the water causes.Organic acid is also owing to causing corrosion to make treatment facility worsen.
Summary of the invention
Above-described shortcoming can overcome by method of the present invention, and method comprises the steps:
-raw material of mechanical pulp are introduced,
-at first refining stage with raw material refining forming mechanical pulp,
-arranged therein in the process steps of first process lag pH value of mechanical pulp adjusted between 9 to 11 that first process lag was at least 0.5 hour,
-mechanical pulp is categorized into first accept the slurry and the first refusal slurry,
-with ozone treatment first refusal slurry, its pH value when the ozonisation process begins between 9 to 11,
-at second refining stage that the first refusal slurry of ozone treatment is refining, make its to small part will belong to second accept slurry and
-will accept the slurry combination.
Mechanical pulp is handled in such a way, makes that the pH value at paper pulp after the ozonisation process is in constant level in whole paper pulp, therefore makes paper pulp be easier to bleaching.Compare with the mechanical pulp ozonisation process of prior art, novel method provides following advantage:
-reach target paper pulp beating degree energy consumption lower,
-better intensity characteristic,
-owing to the pH value be controlled to be higher than 4 pH value, so prevent to the corrosion of the process device that is positioned at ozonisation process rear and
The better final bleachability of-paper pulp.
In the method for the invention, the raw material of mechanical pulp are introduced in the process.Raw material can be the cork kinds, pine (Pinus sylvestris) for example, pine broom (genus Pinus, the kind that some are different), the mixture of dragon spruce (Picea abies) or pine and dragon spruce.The mixture of hardwood species and they and cork kind also can be used as raw material.Raw material can have the form of wooden fragment.The raw material of beginning also can be the logs that grinds in PGW (pressure ground material) process.
For example the raw material of wooden fragment are anhydrated with reach from 25% to 35% concentration of (typically 30%), and supply in the treater, and are in treater that it is refining in first refining stage.Treater can be dish type treater or the dish type treater that has tapered segment.Raw material are made with extra care in treater in the temperature that raises with under pressure, to form mechanical pulp.First refining stage also can be realized by beater grinder.
Preferred raw material are pines, because when raw material are pine, to compare method of the present invention the most favourable with other processes.Usually be known that the refining ability of pine.Yet by using ozone, this can be modified.Compare with paper pulp not, comprised chip and fragment still less with the paper pulp of ozone treatment with ozone treatment.Ozone treatment also has for the advantageous effects of removing resin, and this is important for the pine raw material.
Phase I is refining to be quite soft; Paper pulp is refined to the beating degree of 600 to 700ml CSF.The upper limit even can be higher than 700ml CSF.
Have two main selections after first refining stage: 1) all mechanical pulps can supply to the alkali treatment reactor, or 2) paper pulp can be categorized into first and accept the slurry and the first refusal slurry, and the refusal slurry supplies to the alkali treatment reactor.
Mainly select according to first, all mechanical pulp is fed into the alkali treatment reactor to realize the certain pH level.Mechanical pulp is with alkali treatment, NaOH (NaOH) for example, sodium carbonate (Na
2CO
3), magnesium hydroxide (Mg (OH)
2), or calcium hydroxide (Ca (OH)
2).Process in the alkali treatment reactor is arranged so that and has process lag that promptly paper pulp stopped 0.5 hour at least, typically from 1 hour to 2 hours in reactor.Processing delay is essential, because alkali should be penetrated into the interior section of fiber (or fibril aggregation thing, the fineness degree that depends on paper pulp are how) from the surface of paper pulp fiber, promptly the interior section of fiber and/or fibril aggregation thing should be processed to realize benefit of the present invention.Process lag also can be arranged as batch process as continuous process.
After paper pulp was processed in the alkali treatment reactor, it was sent to grader, for example sieve or rotary separator.Paper pulp is categorized as first accepts the slurry and the first refusal slurry.Classification step takes place with from 0.5% to 1.5% concentration, typically is approximately 1%, and first accept slurry keep this concentration after classification.Usually, the ratio of accepting slurry/refusal slurry can be roughly 20/80.Yet the ratio of accepting slurry/refusal slurry also can be 60/40 or 50/50.Therefore, accept slurry and can account for 20% to 60% of paper pulp total amount, or even account for 15% to 65% of paper pulp total amount.
The first refusal slurry is at first anhydrated, and makes the concentration of the refusal slurry of winning preferably be higher than 30%.More preferably, concentration is higher than 35%.Too much liquid circulation is got back in the process.The first refusal slurry is sent to ozone reactor with aforesaid concentration, therein with the loose and ozonisation of the first refusal slurry.Depend on amount that energy-conservation and requirement pulp quality, ozonisation process be arranged so that ozone paper pulp weight 0.5% to 10% between, and preferably paper pulp weight 1% to 4% between.Process temperature is between 20 ℃ and 90 ℃.Formed strong organic acid in the ozonisation process, but the first refusal slurry handles with alkali, this alkali is with the neutralization of these strong organic acids.Strong organic acid and alkali have formed cushioning liquid, though the ozonisation process has produced organic acid consistently, the pH value of cushioning liquid can remain certain level for a long time.When the ozonisation process finished, the refusal pH value of slurry was between 5 to 7, and this is favourable scope for process steps subsequently.
After ozonisation, the first refusal slurry is made with extra care in the main line that can comprise treater in succession is refining.The first refusal slurry can be categorized as second and accept the slurry and the second refusal slurry.The second refusal slurry can be transported for further making with extra care, and promptly is transported to the 3rd refining stage, but also can only it be removed from process.If there is the 3rd refining stage, then it is finished in the mode identical with aforementioned refining stage.
First receiving amount of accepting the slurry and the first refusal slurry makes up behind above-described process stage.The receiving amount of the first refusal slurry refer to paper pulp be categorized as first accept the slurry and the first refusal slurry after the slurry of acquired all acceptance.
Can accept slurry with ozone treatment and with the combination of the paper pulp of ozone treatment with first.Also can accept slurry first adds some alkali to first after with ozone treatment and accepts slurry.Alkali can be identical with the alkali that added before the ozonisation.In addition, can before as yet not by the receiving amount combination of accepting the slurry and the first refusal slurry of ozonisation, it be handled with alkali.
The beating degree of consequent slurry can be between 90 to 150ml CSF, and also can be lower limit 30 or 40ml CSF.Nature, above-described beating degree depends on the paper quality of hope.
Mainly select according to second, accept the slurry and the first refusal slurry behind first refining stage paper pulp being categorized as first in grader (for example sieve or rotary separator).Concentration in the grader is between 1% and 2%.Usually, the ratio of accepting slurry/refusal slurry can be roughly 20/80.Yet the ratio of accepting slurry/refusal slurry also can be 60/40 or 50/50.Therefore, accept slurry can the paper pulp total amount 20% to 60% between, or even the paper pulp total amount 15% to 65% between.
The first refusal slurry in the alkali treatment reactor with alkali treatment, NaOH (NaOH) for example, sodium carbonate (Na
2CO
3), magnesium hydroxide (Mg (OH)
2), or calcium hydroxide (Ca (OH)
2).The first refusal pH value of slurry depends on that the amount of ozone to be supplied with and pending raw material are enhanced the level between 9 to 11.After this liquid is removed from the first refusal slurry, made and realized preferably being higher than 30% concentration.Concentration more preferably is higher than 35%.Process is got back in too much liquid circulation.The first refusal slurry is sent to ozone reactor with aforesaid concentration, therein with the loose and ozonisation of the first refusal slurry.Depend on amount that energy-conservation and requirement pulp quality, ozonisation process be arranged so that ozone paper pulp weight 0.5% to 10% between, and preferably paper pulp weight 1% to 4% between.Process temperature is between 20 ℃ and 90 ℃.Formed strong organic acid in the ozonisation process, but the first refusal slurry handles with alkali, this alkali is with the neutralization of these strong organic acids.Strong organic acid and alkali have formed cushioning liquid, though the ozonisation process has produced organic acid consistently, the pH value of cushioning liquid can remain certain level for a long time.When the ozonisation process finished, the refusal pH value of slurry was between 5 to 7, and this is favourable scope for process steps subsequently.
After ozonisation, the first refusal slurry is sent to treater to realize second refining stage.Because the first refusal slurry is with ozone treatment,, makes and do not compare second refining stage and consumed energy still less with the slurry of ozone treatment so its characteristic changes.The first refusal slurry is transported to grader from treater, and this grader is categorized as second with the first refusal slurry and accepts the slurry and the second refusal slurry.The beating degree of accepting slurry (promptly comprise first accept the slurry that slurry and second is accepted slurry) can be between 90 to 150ml CSF, but also can be lower limit 30 or 40ml CSF.Nature, above-described beating degree depends on the paper quality of hope.
The second refusal slurry can be transported for further making with extra care, and promptly is transported to the 3rd refining stage, but also can only it be removed from process.If there is the 3rd refining stage, then it is finished in the mode identical with aforementioned refining stage.
First accepts slurry can remove and be used for other purposes from process, but also can accept slurry and second and accept the slurry combination first, make them can be used as a slurry and be sent to subsequently process steps, this process steps subsequently is blanching step normally.The pH value of slurry that obtains from second refining stage is between 5 to 7, and first accept slurry and have approximately identical pH value, so does not require that other step adjusts the pH value.
The level of before refining the pH value being adjusted between 9 to 11 has promoted bleaching stage, because the consumption of peroxide is minimized.Harmful wood extractive is soluble in the water that has added alkali.
The mechanical pulp that is obtained by this method (above-described first and second mainly select) is used for the sheet paper products manufacture process.Sheet paper products can be the paper that has comprised mechanical pulp, has for example comprised the printing paper of mechanical pulp, or it can be a cardboard.
Description of drawings
By example and explain the present invention with reference to the accompanying drawings, each figure is hereinafter:
Fig. 1 shows the explanatory view of first process;
Fig. 2 shows the explanatory view of second process;
Fig. 3 shows the explanatory view of third and fourth process;
Fig. 4 shows the anti-Zhang Zhibiao as the function of SEC (specific energy consumption); With
Fig. 5 shows the index of tearing as the function of intensity index.
The specific embodiment
Example 0
The method that does not comprise alkali treatment before ozonisation is used to handle the mechanical pulp of being made by pine.
As from Fig. 5 and Fig. 6 as seen, realized handling comparing by ozonisation pine refusal object+20% energy-conservation and better intensity characteristic with normal pine.
Example 1
Select by describe first process with reference to figure 1 hereinafter.
The raw material of mechanical pulp are at first anhydrated, for example in inspissator 1, anhydrate as fly press, and raw material are delivered in the treater 2 then, are made with extra care to form mechanical pulp in the temperature that raises with under pressure during wherein for example the raw material of pine fragment were made with extra care in the phase I.Concentration during subtractive process is approximately 30%.Preferred raw material are pines, because when raw material are pine, compare with other processes, and method of the present invention is the most favourable.Phase I is refining to be quite soft; Paper pulp is refined to the beating degree of 600 to 700ml CSF.Beating degree value even can be higher than 700ml CSF.Alkali with for example NaOH in alkali treatment reactor 3 comes pulp treatment.The first refusal pH value of slurry is elevated to the level between 9 to 11.In alkali treatment reactor 3, exist to postpone, make paper pulp remain in the alkali treatment reactor at least 0.5 hour, typically from 1 hour to 2 hours.Paper pulp is also diluted in the alkali treatment reactor, makes its concentration between 0.5% to 1.5%.
Paper pulp is classified as first and accepts the slurry A1 and the first refusal slurry R1 in the grader 4 of for example sieve.Usually, the ratio of accepting slurry/refusal slurry is roughly 20/80, but other ratios of describing in generality is described are suitable.
The first refusal slurry R1 delivers to for example inspissator 5 of fly press then, and it has removed liquid so that realized being higher than the mode of 35% concentration from slurry.Too much liquid 9 is circulated back to process.The first refusal slurry R1 is sent to ozone reactor 6 with aforesaid concentration, therein with the first refusal slurry ozonisation.Formed strong organic acid in the ozonisation process, but the first refusal slurry handles with alkali, this alkali is with the neutralization of these strong organic acids.Strong organic acid and alkali have formed cushioning liquid, though the ozonisation process has produced organic acid consistently, the pH value of cushioning liquid can remain certain level for a long time.When the ozonisation process finished, the refusal pH value of slurry was between 5 to 7, and this is favourable scope for process steps subsequently.
After ozonisation, the first refusal slurry R1 is sent to treater 7.After the first refusal slurry R1 was with ozone treatment, its characteristic changed, made and did not compare this refining stage with the slurry of ozone treatment and consumed energy still less.The first refusal slurry R1 can be transported to another treater 8 from treater 7.Also the first refusal slurry can be delivered to the grader (not shown), this grader is categorized as second with the first refusal slurry and accepts the slurry and the second refusal slurry.The second refusal slurry can be carried for further making with extra care, but also can only remove from process.
First receiving amount of accepting the slurry and the first refusal slurry can have been handled back combination in aforesaid mode at the first refusal slurry, makes them can be used as a slurry and delivers to subsequently process steps, and this process steps is blanching step normally.The pH value of slurry that is obtained is between 5 and 7.
Example 2
Hereinafter by describing second process with reference to figure 2.
The raw material of mechanical pulp are at first anhydrated, for example in inspissator 1, anhydrate as fly press, and raw material are delivered in the treater 2 then, are made with extra care to form mechanical pulp in the temperature that raises with under pressure during wherein for example the raw material of pine fragment were made with extra care in the phase I.The concentration of paper pulp is approximately 30%.Preferred raw material are pines, because when raw material are pine, compare with other processes, and method of the present invention is the most favourable.Phase I is refining to be quite soft; Paper pulp is refined to the beating degree of 600 to 700ml CSF.Alkali with for example NaOH in alkali treatment reactor 3 comes pulp treatment.The first refusal pH value of slurry is elevated to the level between 9 to 11.In alkali treatment reactor 3, exist to postpone, make paper pulp remain in the alkali treatment reactor at least 0.5 hour, typically from 1 hour to 2 hours.Paper pulp also is diluted to concentration between 0.5% to 1.5% simultaneously.
Paper pulp is classified as first and accepts the slurry A1 and the first refusal slurry R1 in the grader 4 of for example sieve.Usually, the ratio of accepting slurry/refusal slurry is roughly 20/80, but other ratios are suitable.
The first refusal slurry R1 delivers to for example inspissator 5 of fly press then, and it has removed liquid so that realized being higher than the mode of 35% concentration from slurry.Too much liquid 9 is circulated back to process.The first refusal slurry R1 is sent to ozone reactor 6 with aforesaid concentration, therein with the first refusal slurry R1 ozonisation.The amount of ozone slurry weight 0.5% and 10% between and preferably between 1% to 4%.In the temperature during the ozonisation between 20 ℃ to 90 ℃.
Formed strong organic acid in the ozonisation process, but the first refusal slurry handles with alkali, this alkali is with the neutralization of these strong organic acids.Strong organic acid and alkali have formed cushioning liquid, though the ozonisation process has produced organic acid consistently, the pH value of cushioning liquid can remain certain level for a long time.When the ozonisation process finished, the refusal pH value of slurry was between 5 to 7, and this is favourable scope for process steps subsequently.
After ozonisation, the first refusal slurry R1 is sent to treater 7.After the first refusal slurry R1 was with ozone treatment, its characteristic changed, made and did not compare second refining stage with the slurry of ozone treatment and consumed energy still less.The first refusal slurry R1 can be transported to another treater 8 from treater 7.Also the first refusal slurry can be delivered to the grader (not shown), this grader is categorized as second with the first refusal slurry and accepts the slurry and the second refusal slurry.The second refusal slurry can be carried for further making with extra care, but also can only remove from process.
First accepts slurry A1 delivers to ozone reactor 11 with the concentration between 0.5% to 1.5%.First accept slurry A1 in ozone reactor 11 by ozonisation.Ozone can be expelled to first and accept in the slurry A1.
First receiving amount of accepting the slurry A1 and the first refusal slurry R1 has been handled the back combination in aforesaid mode at the first refusal slurry, makes them can be used as a slurry and delivers to subsequently process steps, and this process steps is blanching step normally.The pH value of slurry that is obtained is between 5 and 7.
As seen from Figure 4 and Figure 5, compare by having realized with alkali treatment refusal object and ozonisation pine refusal object handling ± 30% energy-conservation and better intensity characteristic (point 4 and put 6) with normal pine.
Example 3
Hereinafter by describing the 3rd process with reference to figure 3.
The 3rd process is similar to the process in the example 2, and difference is that first accepts after the ozonisation of slurry in mixing reactor 13 with alkali treatment.First 0.5% percentage by weight (for example, 0.5% of 100% NaOH percentage by weight) of accepting slurry total amount of the amount of alkali for doing.Process lag is arranged into mixing reactor 13.Slurry stopped 0.5 hour in reactor 13 at least.
Example 4
Hereinafter by describing the 4th process with reference to figure 3.
The 4th process is similar to the process in the example 2, and difference is that first accepts after the ozonisation of slurry in mixing reactor 13 with alkali treatment.First 2% percentage by weight (for example, 2% of 100% NaOH percentage by weight) of accepting slurry total amount of the amount of alkali for doing.Process lag is arranged into mixing reactor 13.Slurry stopped 0.5 hour in reactor 13 at least.
As seen from Figure 4 and Figure 5, compare ± 30% energy-conservation and ± 30% better intensity characteristic (point 8 and point 9) by adding to accept to have realized in the slurry to handle with normal pine with alkali treatment pine refusal object, ozonisation pine refusal object and with alkali.
Persons skilled in the art understand that easily the process of describing can differently make up in above example.Persons skilled in the art also understand and require which kind of concentration to carry out each process steps.The mutual order of first process lag and classification step can reverse; In this case, if those skilled in the art recognize require the concentration adjustment and for two such processing of slurry requirement then first accept slurry and first the refusal slurry must handle dividually.
Claims (8)
1. method that is used for manufacturing machine paper pulp, method comprises:
-raw material of mechanical pulp are introduced,
-at first refining stage with raw material refining forming mechanical pulp,
-arranged therein in the process steps of first process lag pH value of mechanical pulp adjusted between 9 to 11 that this first process lag was at least 0.5 hour,
-mechanical pulp is categorized into first accept the slurry (A1) and the first refusal slurry (R1),
-with ozone treatment first refusal slurry (R1), its pH value when the ozonisation process begins between 9 to 11,
-at second refining stage that the first refusal slurry (R1) of ozonisation is refining, make its to small part will belong to second accept slurry and
-will accept the slurry combination.
2. method according to claim 1 is characterized in that, the first refusal slurry (R1) is being higher than ozonisation under 30% the concentration.
3. method according to claim 1 and 2 is characterized in that, the processing of the first refusal slurry (R1) comprises that first ozonisation and the refining refusal slurry (R1) is categorized as second accepts the slurry and the second refusal slurry.
4. according to the described method of any aforementioned claim, it is characterized in that first processing of accepting slurry (A1) comprises accepts slurry (A1) ozonisation with first.
5. method according to claim 4 is characterized in that, first accepts slurry (A1) ozonisation under 0.5% to 1.5% concentration.
6. according to the described method of any aforementioned claim, it is characterized in that, first processing of accepting slurry (A1) further is included in to be added alkali first of ozonisation in the process steps of wherein having arranged second process lag and accepts slurry (A1), and this second process lag was at least 0.5 hour.
7. according to the described method of any aforementioned claim, it is characterized in that, will accept slurry bleaching.
8. the use of mechanical pulp in the sheet paper products manufacture process of making according to any aforementioned claim.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI20065860A FI119062B (en) | 2006-12-28 | 2006-12-28 | Process for the manufacture of mechanical pulp |
| FI20065860 | 2006-12-28 | ||
| PCT/FI2007/050721 WO2008081078A1 (en) | 2006-12-28 | 2007-12-27 | A method for manufacturing mechanical pulp |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101389808A true CN101389808A (en) | 2009-03-18 |
| CN101389808B CN101389808B (en) | 2011-05-11 |
Family
ID=37623877
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007800069607A Expired - Fee Related CN101389808B (en) | 2006-12-28 | 2007-12-27 | A method for manufacturing mechanical pulp and paper products |
Country Status (9)
| Country | Link |
|---|---|
| US (1) | US20110036523A1 (en) |
| EP (1) | EP2097582A4 (en) |
| JP (1) | JP4882090B2 (en) |
| CN (1) | CN101389808B (en) |
| BR (1) | BRPI0707368A2 (en) |
| CA (1) | CA2633800C (en) |
| FI (1) | FI119062B (en) |
| RU (1) | RU2373313C1 (en) |
| WO (1) | WO2008081078A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111511988A (en) * | 2017-12-21 | 2020-08-07 | 比勒鲁迪克斯那斯公司 | Fractional extraction of fiber |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FI123113B (en) * | 2008-09-10 | 2012-11-15 | Upm Kymmene Corp | Procedure for the manufacture of mechanical pulp and the use of mechanical pulp |
| FR2937656B1 (en) * | 2008-10-24 | 2010-11-19 | Arkema France | PROCESS FOR PRODUCING PAPER PULP |
| JP5729095B2 (en) * | 2011-03-31 | 2015-06-03 | 日本製紙株式会社 | Method for producing hardwood mechanical pulp |
| FR2980805B1 (en) | 2011-09-30 | 2013-09-20 | Arkema France | ENZYMATIC PRETREATMENT OF WOOD IN A PROCESS FOR THE MANUFACTURE OF MECHANICAL PAPER PULP |
| WO2013176049A1 (en) * | 2012-05-21 | 2013-11-28 | 王子ホールディングス株式会社 | Method for producing fine fiber and fine-fiber-containing sheet |
| CA2824076A1 (en) | 2012-08-21 | 2014-02-21 | University Of New Brunswick | System and method for reclaiming rejects in sulfite pulping |
| SE538752C2 (en) * | 2014-11-21 | 2016-11-08 | Innventia Ab | Process for the production of a treated pulp, treated pulp, and textile fibres produced from the treated pulp |
Family Cites Families (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3013932A (en) * | 1958-01-14 | 1961-12-19 | Hawaiian Dev Company Ltd | Printing paper and process of making the same |
| NO131996C (en) | 1973-10-04 | 1975-09-03 | Papirind Forskningsinst | |
| FI67412C (en) | 1977-04-27 | 1985-03-11 | Myrens Verksted As | FOERFARANDE FOER BEHANDLING AV CELLULOSAHALTIG MASSA |
| NO142091C (en) * | 1977-10-17 | 1980-06-25 | Myrens Verksted As | PROCEDURE FOR OZONE TREATMENT OF REFINO MECHANICAL AND THERMOMECHANICAL MASS. |
| US4718980A (en) * | 1985-12-30 | 1988-01-12 | Weyerhaeuser Company | Interstage treatment of mechanical pulp |
| ES2073027T3 (en) * | 1990-05-17 | 1995-08-01 | Union Camp Patent Holding | ENVIRONMENTALLY IMPROVED PROCEDURE FOR WHITENING LIGNOCELLULOSIC MATERIALS. |
| US5503709A (en) * | 1994-07-27 | 1996-04-02 | Burton; Steven W. | Environmentally improved process for preparing recycled lignocellulosic materials for bleaching |
| SE520707C2 (en) * | 2001-12-05 | 2003-08-12 | Metso Paper Inc | Method and system for treating pulp in ozone bleaching |
| FI121792B (en) * | 2003-06-30 | 2011-04-15 | Andritz Oy | Method of treating pulp in connection with bleaching of chemical pulp |
| CN1263923C (en) * | 2004-09-15 | 2006-07-12 | 中国科学院广州化学研究所 | Supersonic chemical pretreating method for bagasse for wood-plastic composite material |
-
2006
- 2006-12-28 FI FI20065860A patent/FI119062B/en not_active IP Right Cessation
-
2007
- 2007-12-27 EP EP07858372.1A patent/EP2097582A4/en not_active Withdrawn
- 2007-12-27 RU RU2008126954/12A patent/RU2373313C1/en not_active IP Right Cessation
- 2007-12-27 CN CN2007800069607A patent/CN101389808B/en not_active Expired - Fee Related
- 2007-12-27 US US12/158,222 patent/US20110036523A1/en not_active Abandoned
- 2007-12-27 CA CA2633800A patent/CA2633800C/en not_active Expired - Fee Related
- 2007-12-27 WO PCT/FI2007/050721 patent/WO2008081078A1/en active Application Filing
- 2007-12-27 JP JP2009500882A patent/JP4882090B2/en not_active Expired - Fee Related
- 2007-12-27 BR BRPI0707368-2A patent/BRPI0707368A2/en not_active IP Right Cessation
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111511988A (en) * | 2017-12-21 | 2020-08-07 | 比勒鲁迪克斯那斯公司 | Fractional extraction of fiber |
| CN111511988B (en) * | 2017-12-21 | 2022-09-27 | 比勒鲁迪克斯那斯公司 | Fractional extraction of fiber |
Also Published As
| Publication number | Publication date |
|---|---|
| US20110036523A1 (en) | 2011-02-17 |
| EP2097582A1 (en) | 2009-09-09 |
| RU2373313C1 (en) | 2009-11-20 |
| JP4882090B2 (en) | 2012-02-22 |
| FI119062B (en) | 2008-07-15 |
| CA2633800A1 (en) | 2008-06-28 |
| WO2008081078A1 (en) | 2008-07-10 |
| FI20065860A0 (en) | 2006-12-28 |
| EP2097582A4 (en) | 2013-12-25 |
| CA2633800C (en) | 2011-08-02 |
| BRPI0707368A2 (en) | 2011-05-03 |
| CN101389808B (en) | 2011-05-11 |
| JP2009530508A (en) | 2009-08-27 |
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