CN101148834B - Paper-making-stage broad-leaved wood pulp plate denaturalization producing technique - Google Patents

Paper-making-stage broad-leaved wood pulp plate denaturalization producing technique Download PDF

Info

Publication number
CN101148834B
CN101148834B CN2007100504677A CN200710050467A CN101148834B CN 101148834 B CN101148834 B CN 101148834B CN 2007100504677 A CN2007100504677 A CN 2007100504677A CN 200710050467 A CN200710050467 A CN 200710050467A CN 101148834 B CN101148834 B CN 101148834B
Authority
CN
China
Prior art keywords
slurry
pulp
wood
alkali
bleaching
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN2007100504677A
Other languages
Chinese (zh)
Other versions
CN101148834A (en
Inventor
冯涛
邓传东
孙毅
薛勤
徐发祥
饶芳秋
宋伟
柳永权
黄�俊
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Yibin Grace Group Co Ltd
Original Assignee
YIBIN CHANGYI POMACE CO Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by YIBIN CHANGYI POMACE CO Ltd filed Critical YIBIN CHANGYI POMACE CO Ltd
Priority to CN2007100504677A priority Critical patent/CN101148834B/en
Publication of CN101148834A publication Critical patent/CN101148834A/en
Application granted granted Critical
Publication of CN101148834B publication Critical patent/CN101148834B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Abstract

The present invention provides denaturating production process of paper-making hardwood pulp sheet pulp superior to available denaturated wood pulp sheet producing process. The denaturating production process includes the following steps: paging paper-making hardwood wood pulp sheet in a paging device, alkali dipping in 6-18 % concentration alkali solution in a dip vat to form 2.5-5.5 % concentration pulp, extruding in a extrude, debonding fiber, digesting, washing, depurating, bleaching, washing for the second time, and fishing pulp. The process can obtain high quality wood pulp of soluble viscose fiber stably and has wide material source.

Description

Paper-making-stage broad-leaved wood pulp plate denaturalization producing technique
Technical field
The present invention relates to paper-making-stage broad-leaved wood pulp plate denaturalization is the production method of dissolving grade cellulose viscose pulp.
Background technology
Development along with China's viscose industry, domestic enterprise is many with the raw materials for production of the cotton pulp dregs of rice as viscose, the resource of raw material cotton linter be subjected to cultivated area and growth cycle restriction and day by day the shortage, because grain and cotton is striven the outstanding of ground contradiction, the influence of the long period and the ecological balance has seriously restricted the development of China's viscose industry.Existing for this reason enterprise is used for viscose glue production with dissolving pulp, but the high fluctuation of the price of import dissolving pulp is big, has influenced the normal operation and the economic benefit of enterprise, seeks the substitute of dissolving pulp, is a vital task of enterprise.
China has produced voluntarily with import a large amount of papermaking level wood-pulp boards at present, but owing to has shortcomings such as viscosity height, reactivity worth difference and non-cellulosic impurity content height.Directly can't be used for the production of viscose with the wood pulp of papermaking level wood-pulp board production.Only a few enterprise attempts with the raw materials for production of bamboo pulp as viscose, and has obtained initial success, is CN02112175.3 as the patent No., and the patent of invention that name is called " bamboo pulp denatured productive technology " discloses a kind of production technology of bamboo pulp.But the bamboo fibre average length is lower than the papermaking xylon, production process is because of its ash, pentosan content height, and bamboo fibrid matter is hard, thick walled fiber is more, lumen is narrow, fibr tissue is fine and close, have air in the cell and cause shortcomings such as dissolving difficulty, chemical industry material consumption are big, cost height.
200610021387.4 patent application specification discloses a kind of Wood pomace modified producing technology, and the papermaking level wood-pulp board is produced the wood pulps that is used for viscose through sex change.Its processing step is: wood-pulp board paging, alkali steeping, discongest dispersion, boiling, washing, removal of impurities, bleaching, secondary washing, copy the dregs of rice.Wherein, wood-pulp board paging, alkali steeping, discongest disperse be with the papermaking level wood-pulp board through paging device one by one separately after, spray through alkali, carry the feeding cyclone separator by belt, discongest dispersion with agitator, send into pressafiner and push infiltration, technological parameter is: alkali charge is pressed wood-pulp board weight percent meter 6-17%, bath raio 1: 3-4.
The problem that above-mentioned Wood pomace modified producing technology exists is:
1, the spray mode is carried out alkali steeping: easily cause the wood-pulp board dipping inhomogeneous, especially the part that contacts with conveyer can not be flooded by alkali lye especially; Block pulpboard causes cyclone separator to stop up and discongests and disperse inequality.
2, dipping is 30g/l with the concentration of alkali, and concentration low reaction speed is slow, can not be with hemicellulose stripping in the wood-pulp board.
3, pressafiner extruding: the pitch of pressafiner equates, alkali lye further can not be pushed, infiltrates into fibrous inside, and degradation reaction is insufficient and fall poly-difficulty when causing boiling.
4, liquid initial temperature too high (〉=80 ℃) is boiled in boiling, and seepage velocity is fast, easy oxidative damage fiber and reduce the fine content of first before little steam bleeding; Do not add digestant before the boiling, easily cause half steaming even; Only be alkaline cooking, technology is single, and wood-pulp board is selected narrow range for use.
5, bleaching process is for transferring alkali-bleaching method, and technical process is simple, only is applicable to the needlebush pulpboard that lignin content is low relatively and is not suitable for the leaf wood pulpboard that lignin content is high relatively, fiber is short, and wood-pulp board is selected narrow range for use.
To sum up, above-mentioned existing sex change wood pulps production technology exists that wood-pulp board dipping is uneven, the hemicellulose stripping is slow, fall poly-difficulty, half steaming is even, boiling method is single, method for bleaching is single and condition is violent, wood-pulp board is selected deficiencies such as narrow range for use.
Yet the papermaking level wood-pulp board has dissimilar products according to different working conditions and technology, and wherein the leaf wood pulpboard is exactly that wherein a kind of, different sex change production process of papermaking level wood-pulp board has different production requirements.The leaf wood pulpboard has the individual character difference equally, is carrying out need providing denatured technology pointedly when sex change is produced.
Summary of the invention
Deficiencies such as the above-mentioned just existing sex change wood pulps production technology of technical problem to be solved by this invention exists that wood-pulp board dipping is uneven, the hemicellulose stripping is slow, falls poly-difficulty, half steaming is even, boiling method is single, method for bleaching is single and condition is violent.It is that the viscose of solubility is with the method for wood pulps, especially at the modified production process of papermaking level leaf wood pulpboard that the production of the insoluble papermaking level wood-pulp board of a kind of usefulness is provided.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows:
The modified production process of papermaking level leaf wood pulpboard is characterized in that may further comprise the steps: wood-pulp board paging, alkali steeping, squeeze, discongest dispersion, boiling, washing, removal of impurities, bleaching, secondary washing, copy the dregs of rice; Wherein, it is after papermaking level leaf wood pulpboard is separated one by one that described wood-pulp board paging, alkali steeping, squeezing are discongested, sending into concentration is in the alkali steeping bucket of 6%-18%, after flooding into concentration and being the slurry congee of 2.5%-5.5%, is pumped into the squeezer extruding and discongests loosen collagen fibre with slurry congee.
Beneficial effect of the present invention shows:
One, the present invention produces the viscose production wood pulps of solubility with insoluble paper-making-stage wood pulp plate denaturalization, and every index can match in excellence or beauty with cotton pulp dregs of rice index with similar viscose, and its quality index is:
Index Before the sex change After the sex change 200610021387.4 patent The cotton pulp dregs of rice
Viscosity (Mpa.s) 38.1 12.3 14.0 11.6
First fibre (%) ≤87.5 ≥91.8 ≤88.7 ≥96.0
Ash (%) ≤0.09 ≤0.09 ≤0.15 ≤0.06
Fe(ppm) ≤10.5 ≤9.0 ≤10.0 ≤10.0
Whiteness (%) ≥87 ≥88 ≥88 ≥82
Reactivity worth 7mlCS 2(S) Not enough 25ml ≤59 ≤100 ≤25
S10(%) 13.9 9.7 12.5 4.1
S18(%) 12.5 6.5 8.6 1.7
Two, the wood pulps quality index that adopts the present invention to produce has reached the requirement of dissolving grade wood pulp, can meet the production requirement of viscose fully, and the production cost reduction, is not subjected to the influence of foreign price fluctuation.With respect to cotton pulp production, bamboo pulp production, do not increase new environmental factor, waste water becomes yellow liquor by black liquor, and yellow liquor can be used further to boiling, has reduced the pollution of environment; The real realization protected environment, built a harmonious society.
Three, compare with 200610021387.4 patents, its advantage is:
1, impregnation method: in the impregnating equipment of belt stirrer, with concentration is the NaOH dipping pulping congee of 6%-18% (64g/l-235.5g/l), slurry congee concentration is 2.5%-5.5%, make the wood-pulp board dipping evenly, fully, and abundant stripping hemicellulose, the dipping back carries slurry congee conveniently not stop up conveying equipment with pump.
2, squeezing mode: adopt mandatory squeezing, alkali lye further can be pushed, infiltrates into fibrous inside, it is poly-easy and even to fall during boiling, simultaneously alkali lye unnecessary, that contain hemicellulose is extruded the fine content of the wood pulp first that helps purifying.
3, digesting technoloy: cooking liquor initial temperature low relatively (〉=40 ℃), slowly intensification is difficult for oxidized fibre and improves the fine content of first; Add digestant before the boiling, guarantee that boiling is even; Adopt the boiling method of caustic soda, sulfate, sulphite, the total alkali concn 60-120g/l of cooking liquor, total acid consumption 5-9%, holding temperature is controlled at 140-172 ℃ of scope, and the boiling mode is many, process combination is suitable for all papermaking level wood-pulp boards by force.
4, bleaching process: both can adopt the combined type tri-stage bleaching of " chlorination---alkali treatment---hypochlorite bleaching ", and can adopt " chlorination---alkali treatment---H again 2O 2Bleaching " the combined type tri-stage bleaching, under the mitigation condition, further remove delignification and purification first fibre, process combination is strong and be suitable for all papermaking level wood-pulp boards.
5, in a word, technology of the present invention can solve effectively that the wood-pulp board dipping that exists in the existing property wood pulps production process is uneven, the hemicellulose stripping is slow, fall poly-difficulty, half steaming is even, boiling method is single, method for bleaching is single and condition is violent, thereby make the quality of dissolving grade viscose wood pulps more excellent, more stable, be more suitable for the sex change production of papermaking level needlebush pulpboard.
The specific embodiment
Wood pomace modified producing technology step of the present invention is:
Pulpboard paging → alkali steeping → squeeze → discongest dispersion → boiling → washing → removal of impurities → bleaching → secondary washing → copy dregs of rice.
Wherein, described wood-pulp board paging, alkali steeping, squeezing discongest be with the papermaking level wood-pulp board through paging device one by one separately after, after the NaOH of 6%-18% floods into the slurry congee that concentration is 2.5%-5.5%, be pumped into squeezer with slurry congee and push and discongest loosen collagen fibre.
Described boiling is meant adopts soda processes (NaOH), sulfate process (NaOH+Na with the papermaking level wood-pulp board 2S), sulphite process (Na 2SO 3+ NaOH) carry out boiling, process conditions are: (1) soda processes, the total alkali concn 60-120g/l of kraft cooking liquid, liquor ratio 1: 2.5-4.0; Sulfite cooking liquid total acid consumption 5-9%, liquor ratio 1: 3.0-4.0; (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 3 times with interior little steam bleeding (the intensification number of times is decided on little steam bleeding number of times); (6) holding temperature 135-172 ℃, in the 2 hours total times of heating up.
Described washing is to wash material again to residual alkali≤100g/m3 after the wood pulp slurry after boiling is finished is delivered to extrusion equipment extraction yellow liquor from the batch turning pond.
Described removal of impurities is to utilize desander to carry out gravity desanding, centrifugal removal of impurities, starches the dense 0.4-1.0% of being controlled to be, desander advances to starch pressure 0.28-0.32Mpa.
Described blanching step comprises: chlorination, alkali treatment, hypochlorite bleaching, dechlorination and acid treatment, and not only can adopt tri-stage bleaching, but also can adopt single stage bleaching, technical parameter is: chlorination is led to chlorine dose 0.3-0.7%, is transferred alkali number 50-100g/m 3, bleaching temperature≤50 ℃, bleaching chlorine dosage by slurry volume than the hypochlorite/H that adds 0.3-0.8g/l 2O 2Bleaching agent is extraordinarily gone into the hypo dechlorination by 1.5~2.0 of residual chlorine dose in the slurry, is 1~2% to add hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
Described secondary washing is that the pH value of adjustment slurry is 6-9.
The described dregs of rice of copying are that the slurry of concentration≤1.5% is copied into dissolving pulp 600 * 800mm, that can store behind wet end, press section, drying section.
Below be that paper-making-stage wood pulp plate denaturalization is dissolving grade viscose fiber filament and short silk pulp quality standard:
Dissolving grade viscose fiber filament pulp quality standard
Index Unit Grade A Goods of inferior quality Third grade product
Viscosity Mpa.s 11.5-13.0 11.3-13.2 11.1-13.4
The first fibre ≥91.5 ≥91.0 ≥90.5
Ash ≤0.09 ≤0.10 ≤0.12
Fe ppm ≤10.0 ≤14.0 ≤18.0
Whiteness ≥82 ≥81 ≥81
Reactivity worth 7mlCS 2 S ≤250 Do not meet first-class
Big dust Individual/kg ≤0.8 ≤1.0 ≤1.2
Moisture 7.5-11.0 Be not more than 13.0 Be not more than 13.0
S10 ≤10.0 ≤10.5 ≤11.5
S18 ≤7.0 ≤7.5 ≤8.0
Dissolving grade viscose short fiber pulp quality standard
Index Unit Grade A Goods of inferior quality Third grade product
Viscosity Mpa.s 11.5-13.0 11.3-13.2 11.1-13.4
The first fibre ≥89.0 ≥88.5 ≥88.0
Ash ≤0.12 ≤0.14 ≤0.16
Fe ppm ≤18.0 ≤22.0 ≤26.0
Whiteness ≥80 ≥79 ≥78
Index Unit Grade A Goods of inferior quality Third grade product
Reactivity worth 7mlCS 2 S ≤250 Do not meet first-class
Big dust Individual/kg ≤1.3 ≤1.5 ≤1.7
Moisture 7.5-11.0 Be not more than 13.0 Be not more than 13.0
S10 ≤12.0 ≤12.5 ≤13.5
S18 ≤8.5 ≤9.0 ≤10.0
To help to understand the present invention by following embodiment:
Embodiment 1: sulfate process one
1, uses papermaking level leaf wood pulpboard 6000Kg, through the paging device paging.
2, the NaOH with 10% (8-14) floods into the slurry congee that concentration is 3.5% (2.5-5.5).
3, with slurry congee pump it is sent into the squeezer extruding and discongests loosen collagen fibre.
4, the wood pulp after will squeezing drops in the boiling vessel and carries out boiling, and process conditions are: (1) digestant: NaOH+Na 2S, the total alkali concn 80g/l of cooking liquor (60-100), liquor ratio 1: 3.5 (3.0-4.0); (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 3 heating curves of 2 little steam bleedings, heat up 2 hours total times; (6) holding temperature is 172 ± 2 ℃.(145-172)
5, the above-mentioned wood pulp slurry that obtains through boiling is delivered to extruding from the batch turning pond and washed material extraction yellow liquor, washing is to residual alkali≤100g/m3; Utilize desander to carry out centrifugal removal of impurities, starch the dense 0.6-0.9% of being controlled to be, advance to starch pressure 0.28-0.31Mpa.
6, adopt chlorination-alkali treatment-hypochlorite to bleach for three sections then, technical parameter is: chlorination is led to chlorine dose 0.6-0.7% (0.4-0.7), is transferred alkali number 80-100g/m 3, bleaching temperature≤50 ℃, bleaching chlorine dosage than the sodium hypochlorite bleaching agent that adds 0.3g/l (0.3-0.6), extraordinarily go into hypo dechlorination by 2.0 of residual chlorine dose in the slurry by slurry volume, are 1.5% to add hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
7, secondary washing is washed till slurry pH value 6-9
8, the wood pulp that obtains after the secondary washing is manufactured paper with pulp be the pulp of specification 600 * 800mm.
Embodiment 2: sulfate process two
1, uses papermaking level leaf wood pulpboard 6000Kg, through the paging device paging.
2, the NaOH with 8% (8-14) floods into the slurry congee that concentration is 4.5% (2.5-5.5).
3, with slurry congee pump it is sent into the squeezer extruding and discongests loosen collagen fibre.
4, the wood pulp after will squeezing drops in the boiling vessel and carries out boiling, and process conditions are: (1) digestant: NaOH+Na 2S, the total alkali concn 100g/l of cooking liquor (60-100), liquor ratio 1: 3.5 (3.0-4.0); (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 3 heating curves of 2 little steam bleedings, heat up 2 hours total times; (6) holding temperature is 155 ± 2 ℃.(145-172)
5, the above-mentioned wood pulp slurry that obtains through boiling is delivered to extruding from the batch turning pond and washed material extraction yellow liquor, washing is to residual alkali≤100g/m3; Utilize desander to carry out centrifugal removal of impurities, starch the dense 0.6-0.9% of being controlled to be, advance to starch pressure 0.28-0.31Mpa.
6, adopt chlorination-alkali treatment-hypochlorite to bleach for three sections then, technical parameter is: chlorination is led to chlorine dose 0.6-0.7% (0.4-0.7), is transferred alkali number 80-100g/m 3, bleaching temperature≤50 ℃, bleaching chlorine dosage than the sodium hypochlorite bleaching agent that adds 0.5g/l (0.4-0.6), extraordinarily go into hypo dechlorination by 2.0 of residual chlorine dose in the slurry by slurry volume, are 1.5% to add hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
7, secondary washing is washed till slurry pH value 6-9
8, the wood pulp that obtains after the secondary washing is manufactured paper with pulp be the pulp of specification 600 * 800mm.
Embodiment 3: sulfate process three
1, uses papermaking level leaf wood pulpboard 6000Kg, through the paging device paging.
2, flood into the slurry congee that concentration is 4.5% (2.5-5.5) with 6% NaOH.
3, with slurry congee pump it is sent into the squeezer extruding and discongests loosen collagen fibre.
4, the wood pulp after will squeezing drops in the boiling vessel and carries out boiling, and process conditions are: (1) digestant: NaOH+Na 2S, the total alkali concn 120g/l of cooking liquor (60-100), liquor ratio 1: 3.5 (3.0-4.0); (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 3 heating curves of 2 little steam bleedings, heat up 2 hours total times; (6) holding temperature is 135 ℃.
5, the above-mentioned wood pulp slurry that obtains through boiling is delivered to extruding from the batch turning pond and washed material extraction yellow liquor, washing is to residual alkali≤100g/m3; Utilize desander to carry out centrifugal removal of impurities, starch the dense 0.6-0.9% of being controlled to be, advance to starch pressure 0.28-0.31Mpa.
6, adopt chlorination-alkali treatment-hypochlorite to bleach for three sections then, technical parameter is: chlorination is led to chlorine dose 0.5% (0.4-0.7), is transferred alkali number 80-100g/m 3, bleaching temperature≤50 ℃, bleaching chlorine dosage than the sodium hypochlorite bleaching agent that adds 0.6g/l (0.4-0.6), extraordinarily go into hypo dechlorination by 2.0 of residual chlorine dose in the slurry by slurry volume, are 1.5% to add hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
7, secondary washing is washed till slurry pH value 6-9
8, the wood pulp that obtains after the secondary washing is manufactured paper with pulp be the pulp of specification 600 * 800mm.
Embodiment 4: soda processes one
1, uses papermaking level leaf wood pulpboard 6000Kg, through the paging device paging.
2, the NaOH with 12% (10-18) floods into the slurry congee that concentration is 2.5% (2.5-4.0).
3, with slurry congee pump it is sent into the squeezer extruding and discongests loosen collagen fibre.
4, the wood pulp after will squeezing drops in the boiling vessel and carries out boiling, and process conditions are: (1) digestant: NaOH, the total alkali concn 120g/l of cooking liquor, liquor ratio 1: 4.0 (3.0-4.0); (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 2 heating curves of 1 little steam bleeding, heat up 2 hours total times; (6) holding temperature is 135 ℃.
5, the above-mentioned wood pulp slurry that obtains through boiling is delivered to extruding from the batch turning pond and washed material extraction yellow liquor, washing is to residual alkali≤100g/m3; Utilize desander to carry out centrifugal removal of impurities, starch the dense 0.6-0.9% of being controlled to be, advance to starch pressure 0.28-0.31Mpa.
6, adopt chlorination-alkali treatment-H then 2O 2Bleach for three sections, technical parameter is: chlorination is led to chlorine dose 0.6% (0.4-0.7), is transferred alkali number 80-100g/m 3, bleaching temperature≤50 ℃, H 2O 2Consumption than the sodium hypochlorite bleaching agent that adds 0.7g/l (0.5-0.8), is extraordinarily gone into hypo dechlorination by 2.0 of residual chlorine dose in the slurry by slurry volume, is that 1.0% (1.0-2.0) adds hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
7, secondary washing is washed till slurry pH value 6-9
8, the wood pulp that obtains after the secondary washing is manufactured paper with pulp be the pulp of specification 600 * 800mm.
Embodiment 5: soda processes two
1, uses papermaking level leaf wood pulpboard 6000Kg, through the paging device paging.
2, flooding into concentration with the NaOH of 16% (10-18) is 5.5% slurry congee.
3, with slurry congee pump it is sent into the squeezer extruding and discongests loosen collagen fibre.
4, the wood pulp after will squeezing drops in the boiling vessel and carries out boiling, and process conditions are: (1) digestant: NaOH, the total alkali concn 60g/l of cooking liquor (40-87), liquor ratio 1: 4.0 (3.0-4.0); (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 2 heating curves of 1 little steam bleeding, heat up 2 hours total times; (6) 170 ± 2 ℃ of holding temperatures (150-172).
5, the above-mentioned wood pulp slurry that obtains through boiling is delivered to extruding from the batch turning pond and washed material extraction yellow liquor, washing is to residual alkali≤100g/m3; Utilize desander to carry out centrifugal removal of impurities, starch the dense 0.6-0.9% of being controlled to be, advance to starch pressure 0.28-0.31Mpa.
6, adopt chlorination-alkali treatment-H then 2O 2Bleach for three sections, technical parameter is: chlorination is led to chlorine dose 0.7% (0.4-0.7), is transferred alkali number 80-100g/m 3, bleaching temperature≤50 ℃, H 2O 2Consumption than the sodium hypochlorite bleaching agent that adds 0.6g/l (0.5-0.8), is extraordinarily gone into hypo dechlorination by 2.0 of residual chlorine dose in the slurry by slurry volume, is that 1.0% (1.0-2.0) adds hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
7, secondary washing is washed till slurry pH value 6-9
8, the wood pulp that obtains after the secondary washing is manufactured paper with pulp be the pulp of specification 600 * 800mm.
Embodiment 6: soda processes three
1, uses papermaking level leaf wood pulpboard 6000Kg, through the paging device paging.
2, flooding into concentration with 8% NaOH is 5.5% slurry congee.
3, with slurry congee pump it is sent into the squeezer extruding and discongests loosen collagen fibre.
4, the wood pulp after will squeezing drops in the boiling vessel and carries out boiling, and process conditions are: (1) digestant: NaOH, the total alkali concn 80g/l of cooking liquor (40-87), liquor ratio 1: 4.0 (3.0-4.0); (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 2 heating curves of 1 little steam bleeding, heat up 2 hours total times; (6) 160 ± 2 ℃ of holding temperatures (150-172).
5, the above-mentioned wood pulp slurry that obtains through boiling is delivered to extruding from the batch turning pond and washed material extraction yellow liquor, washing is to residual alkali≤100g/m3; Utilize desander to carry out centrifugal removal of impurities, starch the dense 0.6-0.9% of being controlled to be, advance to starch pressure 0.28-0.31Mpa.
6, adopt chlorination-alkali treatment-H then 2O 2Bleach for three sections, technical parameter is: chlorination is led to chlorine dose 0.6% (0.4-0.7), is transferred alkali number 80-100g/m 3, bleaching temperature≤50 ℃, H 2O 2Consumption than the sodium hypochlorite bleaching agent that adds 0.8g/l (0.5-0.8), is extraordinarily gone into hypo dechlorination by 2.0 of residual chlorine dose in the slurry by slurry volume, is that 1.0% (1.0-2.0) adds hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
7, secondary washing is washed till slurry pH value 6-9
8, the wood pulp that obtains after the secondary washing is manufactured paper with pulp be the pulp of specification 600 * 800mm.
Embodiment 7: sulphite process one
1, uses papermaking level leaf wood pulpboard 6000Kg, through the paging device paging.
2, the NaOH with 8% (10-18) floods into the slurry congee that concentration is 2.5% (2.5-4.0).
3, with slurry congee pump it is sent into the squeezer extruding and discongests loosen collagen fibre.
4, the wood pulp after will squeezing drops in the boiling vessel and carries out boiling, and process conditions are: (1) digestant: Na 2SO 3+ NaOH, cooking liquor total acid content 8%, liquor ratio 1: 4.0 (3.0-4.0); (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 2 heating curves of 1 little steam bleeding, heat up 2 hours total times; (6) 168 ± 2 ℃ of holding temperatures (150-172).
5, the above-mentioned wood pulp slurry that obtains through boiling is delivered to extruding from the batch turning pond and washed material extraction yellow liquor, washing is to residual alkali≤100g/m3; Utilize desander to carry out centrifugal removal of impurities, starch the dense 0.6-0.9% of being controlled to be, advance to starch pressure 0.28-0.31Mpa.
6, adopt chlorination-alkali treatment-H then 2O 2Bleach for three sections, technical parameter is: chlorination is led to chlorine dose 0.7% (0.4-0.7), is transferred alkali number 80-100g/m 3, bleaching temperature≤50 ℃, H 2O 2Consumption than the sodium hypochlorite bleaching agent that adds 0.7g/l (0.5-0.8), is extraordinarily gone into hypo dechlorination by 2.0 of residual chlorine dose in the slurry by slurry volume, is that 1.5% (1.0-2.0) adds hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
7, secondary washing is washed till slurry pH value 6-9
8, the wood pulp that obtains after the secondary washing is manufactured paper with pulp be the pulp of specification 600 * 800mm.
Embodiment 8: sulphite process two
1, uses papermaking level leaf wood pulpboard 6000Kg, through the paging device paging.
2, the NaOH with 14% (10-18) floods into the slurry congee that concentration is 3.5% (2.5-4.0).
3, with slurry congee pump it is sent into the squeezer extruding and discongests loosen collagen fibre.
4, the wood pulp after will squeezing drops in the boiling vessel and carries out boiling, and process conditions are: (1) digestant: Na 2SO 3+ NaOH, cooking liquor total acid content 6%, liquor ratio 1: 4.0 (3.0-4.0); (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 2 heating curves of 1 little steam bleeding, heat up 2 hours total times; (6) 170 ± 2 ℃ of holding temperatures (150-172).
5, the above-mentioned wood pulp slurry that obtains through boiling is delivered to extruding from the batch turning pond and washed material extraction yellow liquor, washing is to residual alkali≤100g/m3; Utilize desander to carry out centrifugal removal of impurities, starch the dense 0.6-0.9% of being controlled to be, advance to starch pressure 0.28-0.31Mpa.
6, adopt chlorination-alkali treatment-H then 2O 2Bleach for three sections, technical parameter is: chlorination is led to chlorine dose 0.5% (0.4-0.7), is transferred alkali number 80-100g/m 3, bleaching temperature≤50 ℃, H 2O 2Consumption than the sodium hypochlorite bleaching agent that adds 0.6g/l (0.5-0.8), is extraordinarily gone into hypo dechlorination by 2.0 of residual chlorine dose in the slurry by slurry volume, is that 1.5% (1.0-2.0) adds hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
7, secondary washing is washed till slurry pH value 6-9
8, the wood pulp that obtains after the secondary washing is manufactured paper with pulp be the pulp of specification 600 * 800mm.
Embodiment 9: sulphite process three
1, uses papermaking level leaf wood pulpboard 6000Kg, through the paging device paging.
2, the NaOH with 10% (10-18) floods into the slurry congee that concentration is 4.5% (2.5-4.0).
3, with slurry congee pump it is sent into the squeezer extruding and discongests loosen collagen fibre.
4, the wood pulp after will squeezing drops in the boiling vessel and carries out boiling, and process conditions are: (1) digestant: Na 2SO 3+ NaOH, cooking liquor total acid content 5%, liquor ratio 1: 4.0 (3.0-4.0); (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 2 heating curves of 1 little steam bleeding, heat up 2 hours total times; (6) 172 ℃ of holding temperatures (150-172).
5, the above-mentioned wood pulp slurry that obtains through boiling is delivered to extruding from the batch turning pond and washed material extraction yellow liquor, washing is to residual alkali≤100g/m3; Utilize desander to carry out centrifugal removal of impurities, starch the dense 0.6-0.9% of being controlled to be, advance to starch pressure 0.28-0.31Mpa.
6, adopt chlorination-alkali treatment-H then 2O 2Bleach for three sections, technical parameter is: chlorination is led to chlorine dose 0.5% (0.4-0.7), is transferred alkali number 80-100g/m 3, bleaching temperature≤50 ℃, H 2O 2Consumption than the sodium hypochlorite bleaching agent that adds 0.8g/l (0.5-0.8), is extraordinarily gone into hypo dechlorination by 2.0 of residual chlorine dose in the slurry by slurry volume, is that 1.5% (1.0-2.0) adds hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
7, secondary washing is washed till slurry pH value 6-9
8, the wood pulp that obtains after the secondary washing is manufactured paper with pulp be the pulp of specification 600 * 800mm.
Embodiment 10:
Can add the M-101 auxiliary agent in the foregoing description digestion process, addition is 0.15-0.25%.

Claims (5)

1. the modified production process of papermaking level leaf wood pulpboard is characterized in that may further comprise the steps: wood-pulp board paging, alkali steeping, squeeze, discongest dispersion, boiling, washing, removal of impurities, bleaching, secondary washing, copy the dregs of rice; Wherein, described wood-pulp board paging, alkali steeping, squeeze, discongest be with papermaking level leaf wood pulpboard one by one separately after, sending into concentration is in the alkali steeping bucket of 6%-18%, after flooding into concentration and being the slurry congee of 2.5%-5.5%, is pumped into the squeezer extruding and discongests loosen collagen fibre with slurry congee; Described boiling is meant adopts soda processes, sulfate process or sulphite process to carry out boiling papermaking level leaf wood pulpboard, and digestant is respectively NaOH, NaOH+Na 2S, Na 2SO 3+ NaOH, process conditions are: (1) soda processes, the total alkali concn 60-120g/l of kraft cooking liquid, liquor ratio 1: 2.5-4.0; Sulfite cooking liquid total acid consumption 5-9%, liquor ratio 1: 3.0-4.0; (2) cooking liquor initial temperature 〉=40 ℃; (3) heated up in advance 10-15 minute, to 105 ± 5 ℃; (4) stop behind the vapour dry run again 25~30 minutes; (5) adopt 3 times with interior little steam bleeding, the intensification number of times is decided on little steam bleeding number of times; (6) holding temperature 135-172 ℃, in the 2 hours total times of heating up; Described blanching step comprises: chlorination, alkali treatment, hypochlorite bleaching, dechlorination and acid treatment, adopt tri-stage bleaching, and technical parameter is: chlorination is led to chlorine dose 0.3-0.7%, is transferred alkali number 50-100g/m 3, bleaching temperature≤50 ℃, bleaching chlorine dosage than the hypochlorite bleaching that adds 0.3-0.8g/l, extraordinarily go into hypo dechlorination by 1.5~2.0 of residual chlorine dose in the slurry by slurry volume, are 1~2% to add hydrochloric acid and carry out acid treatment by the percentage by weight of slurry.
2. the modified production process of papermaking level leaf wood pulpboard according to claim 1 is characterized in that: described washing is to wash material again to residual alkali≤100g/m after the wood pulp slurry after boiling is finished is delivered to extrusion equipment extraction yellow liquor from the batch turning pond 3
3. the modified production process of papermaking level leaf wood pulpboard according to claim 1 is characterized in that: described removal of impurities is to utilize desander to carry out gravity desanding, centrifugal removal of impurities, starches the dense 0.4-1.0% of being controlled to be, desander advances to starch pressure 0.28-0.32MPa.
4. the modified production process of papermaking level leaf wood pulpboard according to claim 1 and 2 is characterized in that: described secondary washing is that the adjustment pH value of slurry is 6-9.
5. the modified production process of papermaking level leaf wood pulpboard according to claim 1 is characterized in that: the described dregs of rice of copying are dissolving pulps of storing of the slurry of concentration≤1.5% being copied into 600 * 800mm behind wet end, press section, drying section.
CN2007100504677A 2007-11-12 2007-11-12 Paper-making-stage broad-leaved wood pulp plate denaturalization producing technique Active CN101148834B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2007100504677A CN101148834B (en) 2007-11-12 2007-11-12 Paper-making-stage broad-leaved wood pulp plate denaturalization producing technique

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN2007100504677A CN101148834B (en) 2007-11-12 2007-11-12 Paper-making-stage broad-leaved wood pulp plate denaturalization producing technique

Publications (2)

Publication Number Publication Date
CN101148834A CN101148834A (en) 2008-03-26
CN101148834B true CN101148834B (en) 2010-06-23

Family

ID=39249525

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2007100504677A Active CN101148834B (en) 2007-11-12 2007-11-12 Paper-making-stage broad-leaved wood pulp plate denaturalization producing technique

Country Status (1)

Country Link
CN (1) CN101148834B (en)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101880981B (en) * 2010-07-09 2013-11-27 延边石岘白麓纸业股份有限公司 Method for making pulp
CN102407553A (en) * 2010-09-21 2012-04-11 大亚科技股份有限公司 Manufacturing method of high density fiberboard for whitened type E1 grade floor substrate
CN102677509B (en) * 2012-05-29 2014-06-18 宜宾丝丽雅集团有限公司 Material preparation process for preparing dissolving pulp by modifying bleached needle leave wood and broadleaf wood composite pulp
CN102691221B (en) * 2012-05-29 2014-06-18 宜宾丝丽雅集团有限公司 Material preparation technology applied in preparation of dissolving pulp by modifying bleached wood pulp
CN106702799B (en) * 2016-12-02 2018-04-10 山东银鹰股份有限公司 The method that papermaking grade wood pulp modification prepares viscose rayon dissolving pulp

Also Published As

Publication number Publication date
CN101148834A (en) 2008-03-26

Similar Documents

Publication Publication Date Title
CN101148836B (en) Paper-making-stage bamboo wood pulp plate denaturalization producing technique
CN102352572B (en) Preparation method for bamboo wood dissolving pulp
CN100572657C (en) Wood pomace modified producing technology
CN101148834B (en) Paper-making-stage broad-leaved wood pulp plate denaturalization producing technique
CN101158124A (en) Paper-making grade pulp bleaching plate modifying production technique
CN100402745C (en) Prepared bleach chemical pulp using grass kind plant as raw material and preparation method thereof
CN101435164B (en) Modified production process of paper making level sulphate wood pulp plate
CN102677505B (en) Steaming process for modifying bleaching bamboo paper pulp and bleaching wood paper pulp into dissolving pulp in compound way
CN101148835B (en) Paper-making-stage wood pulp plate denaturalization producing technique
CN103556249B (en) A kind of palm viscose and preparation method thereof
CN101158125B (en) Paper-making grade softwood pulp plate modifying production technique
CN101148832B (en) Paper-making-stage high viscosity wood pulp plate denaturalization producing technique
CN101148837B (en) Paper-making-stage primary color wood pulp plate denaturalization producing technique
CN106702799B (en) The method that papermaking grade wood pulp modification prepares viscose rayon dissolving pulp
CN101148833B (en) Paper-making-stage reclaiming wood pulp plate denaturalization producing technique
CN101735323A (en) Method for producing acetate fiber bamboo pulp
CN102677507A (en) Cooking process for carrying out composite modification on natural color bamboo paper pulp and cotton paper pulp to form dissolving pulp
CN102677500B (en) A kind of material preparation technology being applicable to pulp by modifying true color unbleached and preparing dissolving pulp
CN102337688B (en) Mixed pulp used for producing viscose fiber and its production process
CN101451312B (en) Method for preparing bleached chemical pulp by using grass type plants as raw materials
CN100406646C (en) Prepared high hardness pulp using grass kind plant as raw material and preparation method thereof
CN101353868B (en) Alkaline process cooking method for preparing high-hardness pulp from gramineae plants
CN102677506B (en) Cooking process for carrying out composite modification on bleached bamboo paper pulp and natural color wood pulp to form dissolving pulp
CN112853796A (en) Preparation method for modifying papermaking pulp into pulp special for lyocell fibers
CN102691222B (en) Cooking process for compound modification of bleached bamboo paper pulp and cotton paper pulp into dissolving pulp

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant
ASS Succession or assignment of patent right

Owner name: YIBIN GRACE GROUP COMPANY

Free format text: FORMER OWNER: YIBIN CHANGYI POMACE CO., LTD.

Effective date: 20130521

C41 Transfer of patent application or patent right or utility model
TR01 Transfer of patent right

Effective date of registration: 20130521

Address after: 644002 space Road, Nan'an economic and Technological Development Zone, Yibin, Sichuan

Patentee after: Yibin Grace Group Company

Address before: 644002 middle section of space Road, Nan'an economic and Technological Development Zone, Yibin, Sichuan

Patentee before: Yibin Changyi Pomace Co., Ltd.