CN101054777A - Hardwood alkaline pulping processes and systems - Google Patents
Hardwood alkaline pulping processes and systems Download PDFInfo
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- CN101054777A CN101054777A CNA2007100981106A CN200710098110A CN101054777A CN 101054777 A CN101054777 A CN 101054777A CN A2007100981106 A CNA2007100981106 A CN A2007100981106A CN 200710098110 A CN200710098110 A CN 200710098110A CN 101054777 A CN101054777 A CN 101054777A
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- 238000000034 method Methods 0.000 title claims abstract description 37
- 230000008569 process Effects 0.000 title description 17
- 238000004537 pulping Methods 0.000 title description 4
- 239000011121 hardwood Substances 0.000 title description 2
- 239000002023 wood Substances 0.000 claims abstract description 76
- 229920005610 lignin Polymers 0.000 claims abstract description 64
- 239000000463 material Substances 0.000 claims abstract description 38
- 238000010411 cooking Methods 0.000 claims abstract description 32
- 239000002002 slurry Substances 0.000 claims abstract description 29
- 239000000126 substance Substances 0.000 claims abstract description 10
- 239000000835 fiber Substances 0.000 claims abstract description 4
- 238000009835 boiling Methods 0.000 claims description 99
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 36
- 239000003513 alkali Substances 0.000 claims description 26
- PYKYMHQGRFAEBM-UHFFFAOYSA-N anthraquinone Natural products CCC(=O)c1c(O)c2C(=O)C3C(C=CC=C3O)C(=O)c2cc1CC(=O)OC PYKYMHQGRFAEBM-UHFFFAOYSA-N 0.000 claims description 7
- 150000004056 anthraquinones Chemical class 0.000 claims description 7
- 239000005077 polysulfide Substances 0.000 claims description 6
- 229920001021 polysulfide Polymers 0.000 claims description 6
- 150000008117 polysulfides Polymers 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 5
- 238000010298 pulverizing process Methods 0.000 claims description 2
- 229920001131 Pulp (paper) Polymers 0.000 abstract description 17
- 239000002699 waste material Substances 0.000 abstract description 5
- 239000007787 solid Substances 0.000 abstract description 3
- 239000007788 liquid Substances 0.000 description 10
- 238000002791 soaking Methods 0.000 description 10
- 238000005406 washing Methods 0.000 description 7
- 239000002893 slag Substances 0.000 description 6
- 241001343274 Dichrostachys spicata Species 0.000 description 4
- 102100030386 Granzyme A Human genes 0.000 description 4
- 101001009599 Homo sapiens Granzyme A Proteins 0.000 description 4
- 230000029087 digestion Effects 0.000 description 4
- 239000002657 fibrous material Substances 0.000 description 4
- 239000000654 additive Substances 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 2
- 238000004061 bleaching Methods 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- 238000007781 pre-processing Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229940089401 xylon Drugs 0.000 description 2
- XOJVVFBFDXDTEG-UHFFFAOYSA-N Norphytane Natural products CC(C)CCCC(C)CCCC(C)CCCC(C)C XOJVVFBFDXDTEG-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 229920002522 Wood fibre Polymers 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000007844 bleaching agent Substances 0.000 description 1
- 206010061592 cardiac fibrillation Diseases 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000002600 fibrillogenic effect Effects 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 239000002025 wood fiber Substances 0.000 description 1
Images
Classifications
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C3/00—Pulping cellulose-containing materials
- D21C3/02—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate processes
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C3/00—Pulping cellulose-containing materials
- D21C3/02—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate processes
- D21C3/022—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate processes in presence of S-containing compounds
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C3/00—Pulping cellulose-containing materials
- D21C3/22—Other features of pulping processes
- D21C3/24—Continuous processes
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C3/00—Pulping cellulose-containing materials
- D21C3/22—Other features of pulping processes
- D21C3/26—Multistage processes
- D21C3/266—Multistage processes the same pulping agent being used in all stages
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C1/00—Pretreatment of the finely-divided materials before digesting
- D21C1/06—Pretreatment of the finely-divided materials before digesting with alkaline reacting compounds
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C3/00—Pulping cellulose-containing materials
- D21C3/22—Other features of pulping processes
- D21C3/222—Use of compounds accelerating the pulping processes
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C3/00—Pulping cellulose-containing materials
- D21C3/22—Other features of pulping processes
- D21C3/26—Multistage processes
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- Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Paper (AREA)
Abstract
On the condition of given Kappa value, waste solid in broad-leaf wood pulp can be reduced on specific cooking condition at the end of the cooking. S-lignin is found reacting faster than g-lignin and the ratio between the g-lignin and the s-lignin at the end of cooking of the broad-leaf wood is higher than that at the beginning. Therefore, when cooking broad-leaf wood, relatively demanding cooking condition is found being capable of reducing g-lignin content at the end of cooking, and in turn reducing the pulp waste solid percentage under the given Kappa value. While the preferred enforcement mode is chosen, a method and a system applied to producing chemical fiber pulp continuously from the crushed slurry of the broad-leaf wood material are provided, a first cooking towards the crushed slurry of the broad-leaf wood is carried out and the cooking condition is sufficient to reduce the content of s-lignin relatively to that of the g-lignin in the broad-leaf wood material; a second cooking towards the crushed slurry of the broad-leaf wood is carried out and the cooking condition is sufficient to reduce the g-lignin content remained in the broad-leaf wood material after the first cooking.
Description
CROSS-REFERENCE TO RELATED PATENT
The application is 60/791,431 U.S. Provisional Patent Application based on the application number of submitting on April 13rd, 2006 and requires the national priority of this provisional application according to 35 USC § 119 (e) that the full content of this provisional application is hereby incorporated by.
Technical field
The field that present invention relates in general to is the chemical treatment of pulverized fiber material.In a preferred embodiment, the present invention relates to pulverize subtraction pulping process and the system of leaf wood.
Background technology
Compare with the resulting paper pulp of needlebush chemical steaming, the characteristics of leaf wood chemical steaming are to access the thick slag of bigger paper pulp.The applicant finds, with respect to guaiacyl lignin (g-lignin), has a considerable amount of syringyl lignins (s-lignin) in the leaf wood cell intercellular layer.Specifically, the s-content of lignin in the leaf wood cell intercellular layer generally be the g-content of lignin 2-4 doubly.And in needlebush cell intercellular layer, be essentially the g-lignin.
Because the s-lignin accounts for main content and be easy to dissolving in digestion process in leaf wood, with respect to the conditions of cooking that obtains needlebush paper pulp, do not have so harsh so obtain the conditions of cooking of leaf wood paper pulp.Therefore, can expect, but conventionally this way is impossible leaf wood boiling to a higher Kappa value because the increase of useless slurry amount will make this way commercial be unfavorable.By comparing, needlebush can boiling to Kappa value (for example be about 30 under relative exacting terms, because in the intercellular layer all be the g-lignin basically), with the acquisition acceptable, approximately less than 0.5% thick slag content, and leaf wood by boiling to Kappa most 30 o'clock, will cause thick slag content be about 30% or more than.Therefore, for leaf wood paper pulp, conventional conditions of cooking is lower than 18 to obtain the thick slag of the low amount of acceptable for reaching 20Kappa value or lower, being typically.
Summary of the invention
Have been found that at present by can reduce the thick slag of paper pulp under the given Kappa value at the specific conditions of cooking of leaf wood boiling use in latter stage.Therefore, the invention provides the subtraction boiling method and the equipment that are used in particular for leaf wood, purpose is that the Kappa value after the boiling is increased to more than the normal level, and thick slag content is significantly less than normal level.The present invention can in conjunction with an effective xylon process make the Kappa value reduce to normal below because there is low amount hexenuronic acid (HexA) in the paper pulp.The present invention is of value to overall paper output and discharging of waste liquid.
Have been found that the s-lignin is faster than g-lignin reaction, and the g-lignin is at the content ratio in leaf wood boiling latter stage height during than early stage of cooking.Therefore, when the boiling leaf wood, adopt harsh relatively conditions of cooking (as higher boiling temperature) can reduce paper pulp waste residue percentage under the given Kappa value in boiling latter stage.Some aspect of the present invention provides the method and system that generates chemical cellulose from the slurry of broken leaf wood, slurry to broken leaf wood carries out the boiling first time, conditions of cooking is enough to reduce in the leaf wood material s-lignin with respect to the content of g-lignin, slurry to broken leaf wood carries out the boiling second time then, and conditions of cooking is enough to reduce after the boiling for the first time remaining g-content of lignin in the leaf wood material.
In some embodiments, the slurry of leaf wood is treated and make the leaf wood material bear 130 ℃-170 ℃ temperature, and the alkali consumption is timber effective alkali (EA) NaOH of 2-10%; And/or make the Kappa value of the leaf wood material of first boiling stage institute's boiling be 30-100.
According to other preferred embodiment, the first boiling stage carried out being lower than under 20% the low state of cure condition.The acquisition of this low state of cure condition is most preferably by adding the anthraquinone and/or the polysulfide of capacity.
According to certain embodiments of the present invention, the second boiling stage be in order to make the leaf wood slurry in the temperature of bearing 100 ℃-180 ℃, the alkali consumption is timber effective alkali (EA) NaOH of 2-10%; And/or make the Kappa value of the leaf wood material of second boiling stage institute's boiling be 15-30.
In some embodiments of the present invention, the second boiling stage preferably carried out being higher than under 20% the high curing degree condition.
The preprocessing process of the leaf wood material of pulverizing is optional.If the employing preliminary treatment was then carried out before the first boiling stage, the alkali consumption is timber effective alkali (EA) NaOH of 40-60%, and temperature is 80-120 ℃.
Behind the embodiment that below contemplating, describes in detail, with clearer understanding above-mentioned and other aspects and advantage of the present invention.
Description of drawings
Fig. 1 is the schematic diagram that is used to implement the demonstration apparatus of the inventive method, has comprised according to demonstration system of the present invention;
Fig. 2 is the lignin percentage composition curve map that leaves in the plain intercellular layer of the fibrillation of each sample point in the leaf wood digester cycle;
Fig. 3 is that representative is at the ratio of the s-in each stage of leaf wood digester cycle lignin to the g-lignin.
The specific embodiment
Accompanying drawing 1 has been described a preferred embodiment of the present invention.Wherein, accompanying drawing 1 has been described the treatment system 10 of a comminuted fibres material, and this system comprises a continuous steamer 11 that has a feeding system 12.Feeding system 12 can be LO-LEVEL feeding system or the TURBOFEED system that Andritz company sells, but also can use anyly be used to introduce, boiling chopped fibrous material and make the conventional feeding system of slurry; And/or use the soaking container of one or more separation; And/or unconventional system, as those have equipment and/or the chip bin of taking out pump (pumping into boiling vessel) in the forest farm.Can also use a plurality of soaking containers in some cases, finish (perhaps finishing), fill the slurry that pumps into from special container in the container, wherein contain or do not containing cooking additive in the process of pumping in case inject.
For example, the comminuted fibres material is introduced into feeding system 12 with the form of broad-leaved wood chip 13, this system such as United States Patent (USP) 5,763,075; 6,106,668; 6,325,890; 6,551,462; 6,336,993; System described in 6,841,042 (full content of each patent is incorporated this paper into way of reference integral body) is sold by Andritz company, and trade mark is TURBOFEED ; Perhaps as United States Patent (USP) 5,476,572; 5,700,355; System described in 5,968,314 (full content of each patent is incorporated this paper into way of reference integral body) is sold by Andritz company, and trade mark is LO-LEVEL .This system comprises wood chip sent into and carries out steam treatment in the container 14 that container 14 is preferably United States Patent (USP) 5,500,083; 5,617,975; 5,628,873; 4,958,741; Container described in 5,700,355 (full content of each patent is incorporated this paper into way of reference integral body) is produced by Andritz company, and trade mark is DIAMONDBACK , but also can use the boiling container of other types.From the wood chip of container 14 through a similar meter with the pipeline connection device, be preferably the Chip Tube that Andritz company provides.The slurry that will contain wood chip and liquid by the pressure means feeds soaking container (if use) or boiling vessel 11.
Slurry generally is pressurized to 5-15bar, by pipeline 21 slurry is pushed into the top of continuous steamer then.In boiling vessel 11 porch, use separator 22 to remove excess liquid in the slurry, feeding system 12 is discharged and be recovered into to the general top separator (Top Separator) that uses routine by pipeline 23 with excess liquid.In the processing procedure in container 14, the preliminary treatment under the following conditions of the slurry of leaf wood material: the alkali consumption is timber effective alkali (EA) NaOH of 40-60%, and temperature is 80-120 ℃, is preferably 100-110 ℃.
Want high when the boiling for the first time of the ratio of g-lignin and s-lignin begins in the leaf wood material after the boiling for the first time.High concentration s-lignin in the leaf wood material surface liquid can hinder the stripping of g-lignin in the leaf wood material.For reducing this obstruction, be necessary after the boiling first time, the leaf wood material to be washed.Therefore, the leaf wood material can be selected to be changed over to washing container 32 through pipeline 30, uses the cleaning solution of introducing through pipeline 34 to wash.Scrub raffinate is discharged from washing container 32 through pipeline 36.Washing step in the washing container 32 has reduced the s-lignin in the surface liquid, so the cooking additive of Shi Yonging will can not be subjected to the unfavorable loss of s-lignin afterwards.
Slurry through washing is discharged from optional washing container 32 through pipeline 38, directly enters boiling vessel 40, carries out the boiling second time there and further decomposes and reduce g-content of lignin in the leaf wood material.The decomposition of g-lignin can be finished by using high curing degree cooking liquor (that is, be higher than 20% sulphidity, be preferably the sulphidity of 25-40%), use AQ and/or polysulfide (referring to United States Patent (USP) 6,576,084, its full content is incorporated this paper into way of reference).Other cooking chemicals that good action is arranged under conditions of cooking as sulfide, also can be used in combination separately or with above-mentioned AQ and/or polysulfide.
The implementation condition in the second boiling stage is as follows in the boiling vessel 40: temperature is 100-180 ℃, is preferably 130-180 ℃, and the alkali consumption is the timber EA of 2-10%, and the Kappa value when boiling for the second time begins is preferably 40-60 for 30-100.In this stage, the temperature that temperature was brought down below the first boiling stage is favourable, but always unessential.
If do not provide enough alkali at first, be necessary in boiling vessel 40, to add white liquid in the second boiling stage.If added white liquid, the leaf wood material preferably will continue boiling under at least 130 ℃ temperature.The broad-leaved wood fiber material is preferably 15-30 through the Kappa value of pipeline 42 when boiling vessel 40 is discharged, more preferably 20-30.
Emphasis of the present invention is that the leaf wood material is divided into two different boiling stages.The H factor that obtains in second stage latter stage accounts at least 50% of total H factor of obtaining in the whole digestion process.In other words, the H factor of phase I acquisition accounts for below 50% of the H factor that whole digestion process (promptly when the second boiling stage finished) is obtained.
All boiling stages and washing stage (if use) also may all carry out in a boiling container.If use a container, will use and above-mentioned same operating parameter each in stage, and each latter stage in stage the material that do not need a person with the qualifications of a general be transferred to a plurality of containers.
First and second boilings of carrying out respectively in boiling vessel 11 and 40 or carrying out in a container are preferably with reference to one or more methods of more complete description in the following patent: United States Patent (USP) 5,489,363; 5,536,366; 5,547,012; 5,575,890; 5,620,562; 5,662,775 (full content of each patent is incorporated this paper into way of reference).Disclosed method and apparatus are to be produced by Andritz company (Glens Falls, New York) in these patents, and trade mark is LO-SOLIDS Pulping.
Method and apparatus of the present invention has generated the paper pulp of low HexA content under high relatively temperature, produced the new processing and/or the boiling of low alkali condition in the second boiling stage.The paper pulp of this low HexA content helps xylon to turn usefulness into, and the paper pulp of low Kappa value is provided for the following bleaching process conversely.About this respect, with reference to United States Patent (USP) 6,776,876 and 6,475,338, the full content of each patent is incorporated this paper into way of reference.Therefore, can use small amount of chemical substances to bleach this low Kappa value paper pulp, thereby form lower waste water load.In other words, because the HexA compounds content of paper pulp is low, the Kappa value that digestion process produces can be higher, pass through bleaching subsequently to lower Kappa value, and total chemical substance consumption is less.
Following non-limiting example has further described the present invention.
Embodiment
The leaf wood digester cycle used total EA of 17.5% (effective alkali NaOH) consumption, EA is soaking, is introducing in first (or upstream) boiling and second (or downstream) cooking process process.In each cooking process, used following condition:
Soak:
50% total EA or 8.75% EA load
Soaking temperature is 110 ℃
The time that reaches soaking temperature is 15 minutes
The time of keeping soaking temperature is 30 minutes
First (upstream) boiling:
Total EA of interpolation 30% or 5.25% EA load when boiling begins
Boiling temperature is 155 ℃
The time that reaches boiling temperature is 15 minutes
The time of keeping boiling temperature is 60 minutes
Second (downstream) boiling:
Total EA of interpolation 20% or 3.5% EA load when boiling begins
Boiling temperature is 156 ℃
The time of keeping boiling temperature is 120 minutes
Finish the sampling of immersion back at fibrous material (wood chip), use the described methods of people (" Methods in Lignin Chemistry " such as Lin, Springer-Verlag, Berlin (1992), its full content is incorporated this paper into way of reference) detection s-lignin and g-lignin in the laboratory.In addition, the sample point of fibrous material (wood chip) boiling mid-term (as, soaked the beginning back about 90 minutes) and latter stage of (upstream) boiling for the first time (as, soaked after the beginning about 120 minutes).Every kind of sample is all analyzed s-lignin and g-content of lignin with identical method.At last, mid-term of (downstream) boiling for the second time (as, soaked the beginning back about 180 minutes) also take a sample.Because the content of lignin in the final paper pulp that generates is very low usually, so that be difficult to accurately check s-lignin and g-lignin, so do not analyze s-lignin and g-content of lignin in the final paper pulp.
Accompanying drawing 2 is the lignin percentage composition curve maps that leave in the pristine fibre intercellular layer when each sample point.When soaking beginning, content of lignin is expressed as 100%, and in second (downstream) boiling latter stage, content of lignin only remaining about 3%.As general rule, wood chip contained 24% lignin before handling, according to the data of Fig. 2, this means that wood chip remaining content of lignin after handling only has an appointment 0.72%, will be inaccurate so at this moment s-lignin and g-lignin are detected.
The data of Fig. 3 have shown the rate of change of s-lignin and g-lignin in above-mentioned boiling process.First ratio 2.74 is the initial ratios before adding any liquid or any processing.Second ratio 2/87 is the ratio when soaking.Third and fourth ratio 2.64 and 2.54 is respectively the ratio in first mid-term in boiling stage and first latter stage in boiling stage.Five, be that final ratio 2.47 is the ratios in mid-term in the boiling stage second time.
Therefore, the data of Fig. 3 show that the decomposition of s-lignin or rate of dissolution want fast than the g-lignin.The result still is on the cellular level content of g-lignin, needs different conditions to make its decomposition and destruction or dissolving.Therefore, in order to destroy the g-lignin, must change operating condition in the boiling vessel at final stage of cooking.According to the present invention, boiling need guarantee the destruction of g-lignin and yield of raising paper pulp (thereby reducing waste residue) and physical property than higher temperature in early stage latter stage especially.
Although the present invention thinks the most practical and preferred embodiment is described with current, it must be understood that the present invention is not limited to the disclosed specific embodiment.On the contrary, this invention is intended to contain various modifications and of equal value change that is included in the appended claims scope.
Claims (18)
1. method of from the slurry of the leaf wood material pulverized, producing chemical fibre pulp continuously, comprising: (a) slurry to broken leaf wood carries out the boiling first time, and conditions of cooking is enough to reduce in the leaf wood material s-lignin with respect to the content of g-lignin; (b) slurry to broken leaf wood carries out the boiling second time, and conditions of cooking is enough to reduce after the boiling for the first time remaining g-content of lignin in the leaf wood material.
2. the described method of claim 1, wherein said step (a) comprise accepts the slurry of leaf wood material 130 ℃-170 ℃ temperature, and the alkali consumption is timber effective alkali (EA) NaOH of 2-10%.
3. it is 30-100 that the described method of claim 2, wherein said step (a) proceed to the Kappa value through the leaf wood material of boiling of discharging from the first boiling stage.
4. the described method of claim 1, wherein said step (a) are carried out being lower than under the low state of cure condition of 20% sulphidity.
5. the described method of claim 4, the low state of cure condition in the wherein said first boiling stage reaches by adding capacity anthraquinone and/or polysulfide.
6. each described method among the claim 1-5, wherein said step (b) comprises makes the leaf wood slurry bear 100 ℃-180 ℃ temperature, and the alkali consumption is timber effective alkali (EA) NaOH of 2-10%.
7. it is 15-30 that the described method of claim 6, wherein said step (b) proceed to the Kappa value through the leaf wood material of boiling of discharging from the second boiling stage.
8. the described method of claim 1, wherein said step (b) are carried out being higher than under the high curing degree condition of 20% sulphidity.
9. the described method of claim 1 also is included in the step of the broken broad-leaved wood slurry body of step (a) preliminary treatment before, and treatment conditions are that the alkali consumption is timber effective alkali (EA) NaOH of 40-60%, and temperature is 80-120 ℃.
10. be used for from the continuous system that produces chemical fibre pulp of slurry of the leaf wood material of pulverizing, comprise: first boiling vessel, be used for the slurry of broken leaf wood is carried out the boiling first time, conditions of cooking is enough to reduce in the leaf wood material s-lignin with respect to the content of g-lignin; Second boiling vessel is used for the slurry of broken leaf wood is carried out the boiling second time, and conditions of cooking is enough to reduce after the boiling for the first time remaining g-content of lignin in the leaf wood material.
11. the described system of claim 10, wherein said first boiling vessel makes broken broad-leaved wood slurry body bear 130 ℃-170 ℃ temperature, and the alkali consumption is timber effective alkali (EA) NaOH of 2-10%.
12. the described system of claim 11, wherein the Kappa value through the leaf wood material of boiling of discharging from the first boiling stage is 30-100.
13. the described system of claim 10, wherein said first boiling vessel moves being lower than under the low state of cure condition of 20% sulphidity.
14. the described system of claim 13, the low state of cure condition in the wherein said first boiling stage reaches by adding capacity anthraquinone and/or polysulfide.
15. each described system among the claim 10-14, wherein said second boiling vessel makes the leaf wood slurry bear 100 ℃-180 ℃ temperature, and the alkali consumption is timber effective alkali (EA) NaOH of 2-10%.
16. the described system of claim 15, wherein the Kappa value through the leaf wood material of boiling of discharging from the second boiling stage is 15-30.
17. the described system of claim 10, wherein said second boiling vessel moves being higher than under the high curing degree condition of 20% sulphidity.
18. the described system of claim 10 also comprised the pretreating containers that is used for the broken broad-leaved wood slurry body of preliminary treatment before first boiling vessel, described pretreated condition is that the alkali consumption is timber effective alkali (EA) NaOH of 40-60%, and temperature is 80-120 ℃.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US79143106P | 2006-04-13 | 2006-04-13 | |
| US60/791,431 | 2006-04-13 | ||
| US11/709,278 | 2007-02-22 | ||
| US11/709,278 US20070240837A1 (en) | 2006-04-13 | 2007-02-22 | Hardwood alkaline pulping processes and systems |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101054777A true CN101054777A (en) | 2007-10-17 |
| CN101054777B CN101054777B (en) | 2011-05-18 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007100981106A Expired - Fee Related CN101054777B (en) | 2006-04-13 | 2007-04-13 | Hardwood alkaline pulping processes and systems |
Country Status (14)
| Country | Link |
|---|---|
| US (2) | US20070240837A1 (en) |
| JP (1) | JP5101917B2 (en) |
| CN (1) | CN101054777B (en) |
| AU (1) | AU2007200969B2 (en) |
| BR (1) | BRPI0701613A (en) |
| CA (1) | CA2581993A1 (en) |
| CL (1) | CL2007001000A1 (en) |
| ES (1) | ES2319035B1 (en) |
| FI (1) | FI20070280A (en) |
| PT (1) | PT103701B (en) |
| RU (1) | RU2414555C2 (en) |
| SE (1) | SE531540C2 (en) |
| UY (1) | UY30266A1 (en) |
| ZA (1) | ZA200701944B (en) |
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| CN102016165A (en) * | 2008-03-20 | 2011-04-13 | 美卓制浆卡尔斯塔德公司 | Feeding system comprising parallel pumps for a continuous digester |
| CN102203342A (en) * | 2008-08-27 | 2011-09-28 | 美卓造纸机械(瑞典)公司 | A single vertical atmospheric vessel for steaming, slurrying, impregnating and digesting fibrous material |
| CN105568739A (en) * | 2014-10-15 | 2016-05-11 | 亚太森博（山东）浆纸有限公司 | Unbleached sulfate broadleaf wood pulp board and preparation method thereof |
| CN105568740A (en) * | 2014-10-15 | 2016-05-11 | 亚太森博（山东）浆纸有限公司 | High-strength low-whiteness sulfate broad-leaved wood pulp board and preparation method thereof |
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| US5885414A (en) * | 1997-08-18 | 1999-03-23 | Kvaerner Pulping Ab | Method of producing pulp with high alkali cooking in the last cooking stage |
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| JP4298059B2 (en) * | 1999-05-28 | 2009-07-15 | 日本製紙株式会社 | Cooking method of lignocellulosic material |
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| US6576084B1 (en) * | 1999-09-13 | 2003-06-10 | Andritz Inc. | Method of pretreating pulp with yield or strength-enhancing additive |
| IL154759A0 (en) * | 2000-09-05 | 2003-10-31 | Univ Michigan Tech | Genetic engineering of syringyl-enriched lignin in plants |
| JP4454822B2 (en) * | 2000-10-11 | 2010-04-21 | 日本製紙株式会社 | Pulp manufacturing method |
| CN1542217A (en) * | 2003-11-04 | 2004-11-03 | 季 中 | Method for preparing paper pulp by pharmaceutically catalyzing plant fiber at normal temperature and pressure |
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2007
- 2007-02-22 US US11/709,278 patent/US20070240837A1/en not_active Abandoned
- 2007-03-06 ZA ZA200701944A patent/ZA200701944B/en unknown
- 2007-03-06 AU AU2007200969A patent/AU2007200969B2/en not_active Ceased
- 2007-03-08 CA CA002581993A patent/CA2581993A1/en not_active Abandoned
- 2007-03-26 PT PT103701A patent/PT103701B/en not_active IP Right Cessation
- 2007-03-28 ES ES200700816A patent/ES2319035B1/en not_active Expired - Fee Related
- 2007-04-02 JP JP2007096441A patent/JP5101917B2/en not_active Expired - Fee Related
- 2007-04-10 UY UY30266A patent/UY30266A1/en not_active Application Discontinuation
- 2007-04-10 CL CL200701000A patent/CL2007001000A1/en unknown
- 2007-04-12 SE SE0700888A patent/SE531540C2/en not_active IP Right Cessation
- 2007-04-12 FI FI20070280A patent/FI20070280A/en not_active Application Discontinuation
- 2007-04-12 RU RU2007113735/12A patent/RU2414555C2/en not_active IP Right Cessation
- 2007-04-12 BR BRPI0701613-1A patent/BRPI0701613A/en not_active IP Right Cessation
- 2007-04-13 CN CN2007100981106A patent/CN101054777B/en not_active Expired - Fee Related
-
2012
- 2012-08-10 US US13/572,403 patent/US20120305209A1/en not_active Abandoned
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102016165A (en) * | 2008-03-20 | 2011-04-13 | 美卓制浆卡尔斯塔德公司 | Feeding system comprising parallel pumps for a continuous digester |
| CN102203342A (en) * | 2008-08-27 | 2011-09-28 | 美卓造纸机械(瑞典)公司 | A single vertical atmospheric vessel for steaming, slurrying, impregnating and digesting fibrous material |
| CN105568739A (en) * | 2014-10-15 | 2016-05-11 | 亚太森博（山东）浆纸有限公司 | Unbleached sulfate broadleaf wood pulp board and preparation method thereof |
| CN105568740A (en) * | 2014-10-15 | 2016-05-11 | 亚太森博（山东）浆纸有限公司 | High-strength low-whiteness sulfate broad-leaved wood pulp board and preparation method thereof |
| CN105568740B (en) * | 2014-10-15 | 2017-12-12 | 亚太森博（山东）浆纸有限公司 | Low whiteness sulfate leaf wood pulpboard of a kind of high intensity and preparation method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| PT103701A (en) | 2007-10-15 |
| FI20070280A (en) | 2007-10-14 |
| CA2581993A1 (en) | 2007-10-13 |
| CN101054777B (en) | 2011-05-18 |
| SE0700888L (en) | 2007-10-14 |
| SE531540C2 (en) | 2009-05-12 |
| JP2007284860A (en) | 2007-11-01 |
| ES2319035A1 (en) | 2009-05-01 |
| RU2414555C2 (en) | 2011-03-20 |
| US20120305209A1 (en) | 2012-12-06 |
| RU2007113735A (en) | 2008-10-20 |
| ES2319035B1 (en) | 2010-02-10 |
| AU2007200969A1 (en) | 2007-11-01 |
| BRPI0701613A (en) | 2008-03-11 |
| AU2007200969B2 (en) | 2011-11-03 |
| FI20070280A0 (en) | 2007-04-12 |
| US20070240837A1 (en) | 2007-10-18 |
| CL2007001000A1 (en) | 2008-05-30 |
| ZA200701944B (en) | 2008-08-27 |
| UY30266A1 (en) | 2007-11-30 |
| JP5101917B2 (en) | 2012-12-19 |
| PT103701B (en) | 2008-01-28 |
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