CN109338774A - Cellulose mixture pulp and preparation method thereof - Google Patents

Cellulose mixture pulp and preparation method thereof Download PDF

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Publication number
CN109338774A
CN109338774A CN201811089029.6A CN201811089029A CN109338774A CN 109338774 A CN109338774 A CN 109338774A CN 201811089029 A CN201811089029 A CN 201811089029A CN 109338774 A CN109338774 A CN 109338774A
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China
Prior art keywords
pulp
temperature
cotton
slurry
boiling
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CN201811089029.6A
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Chinese (zh)
Inventor
郭新武
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Bazhou Taichang Pulp Co Ltd
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Bazhou Taichang Pulp Co Ltd
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Priority to CN201811089029.6A priority Critical patent/CN109338774A/en
Publication of CN109338774A publication Critical patent/CN109338774A/en
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    • DTEXTILES; PAPER
    • D21PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21BFIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00Fibrous raw materials or their mechanical treatment
    • D21B1/04Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
    • D21B1/06Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by dry methods
    • DTEXTILES; PAPER
    • D21PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21CPRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C1/00Pretreatment of the finely-divided materials before digesting
    • D21C1/06Pretreatment of the finely-divided materials before digesting with alkaline reacting compounds
    • DTEXTILES; PAPER
    • D21PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21CPRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00Regeneration of pulp liquors or effluent waste waters
    • D21C11/10Concentrating spent liquor by evaporation
    • DTEXTILES; PAPER
    • D21PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21CPRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C7/00Digesters
    • DTEXTILES; PAPER
    • D21PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21CPRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00After-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
    • D21C9/02Washing ; Displacing cooking or pulp-treating liquors contained in the pulp by fluids, e.g. wash water or other pulp-treating agents
    • DTEXTILES; PAPER
    • D21PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21CPRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00After-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
    • D21C9/10Bleaching ; Apparatus therefor
    • D21C9/12Bleaching ; Apparatus therefor with halogens or halogen-containing compounds
    • DTEXTILES; PAPER
    • D21PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21DTREATMENT OF THE MATERIALS BEFORE PASSING TO THE PAPER-MAKING MACHINE
    • D21D1/00Methods of beating or refining; Beaters of the Hollander type
    • D21D1/02Methods of beating; Beaters of the Hollander type

Abstract

It is a kind of cellulose mixture pulp and preparation method thereof the present invention relates to viscose rayon technical field;Cotton pulp is mixed with wood pulp after the drift obtained by raw material papermaking grade wood pulp plate after the drift that the cellulose mixture pulp is obtained by raw material cotton linter, and cellulose mixture pulp is made;The present invention can better meet the index request of viscous fine short fine slurry compared with prior art, can adapt to different types of pulp machine and manufacture paper with pulp;After drift in cooking liquor caused by the preparation process of cotton pulp, COD decline 20% to 25%;After drift in wood pulp preparation process, boiling does not generate black liquor, COD decline 50% to 55%;Thus greatly reduce environmental pollution and production cost;Cellulose mixture pulp of the present invention is for viscous de- staple fiber production simultaneously, the characteristics such as the hygroscopicity of cotton fiber, the stiffness of skin-friendly and wood-fibred, coloring are merged, to make that there are more difference functions using one of cellulose mixture pulp raw material of the present invention viscous de- staple fiber obtained.

Description

Cellulose mixture pulp and preparation method thereof
Technical field
It is a kind of cellulose mixture pulp and preparation method thereof the present invention relates to viscose rayon technical field.
Background technique
The viscose rayon of single raw material production, performance is dull, has their own characteristics each, as the skin-friendly of fiber, stiffness, pliability, Gas permeability, coloring, moisture absorption hydrofuge, antibacterial bacteriostatic function etc., it is blended to become spinning in order to improve the comprehensive performance of weaving goods The mainstream of fabric.With the raising of China's viscose rayon production technology, the demand for producing multi-functional differentiation fiber species is more next Bigger, partial function is gradually developed from field of textiles part is preposition to viscose rayon manufacturing field, therefore mixes the production of pulp Also become a developing direction of pulp manufacture.
Existing compound cellulose pulp is first to mix the raw materials such as two or more cotton linter, timber, fiber crops, bamboo wood Repulping afterwards, manufacturing step are: condiment, wash material, washing, mashing are discongested, are mixed, the washing that cleans, pre-sour, pre- chlorine, bleaching, at acid It manages, drops miscellaneous washing, manufactures paper with pulp.
Existing compound cellulose pulp technique exists: 1. by two or more cotton linter, timber, fiber crops, bamboo wood Raw material carries out repulping after any mixing, since these types of raw material wood cellulose content height is different, alpha cellulose and hemicellulose Plain (pentosan) content also differs widely, repulping complex process after any mixing, be not well positioned to meet existing equipment and Technique requirement;2. timber, fiber crops, bamboo wood content of lignin are high, COD content is high in pulping and digesting liquid, can generate black liquor and easily cause ring Border pollution and high production cost.
Summary of the invention
The present invention provides a kind of cellulose mixture pulps and preparation method thereof, overcome the defects of the prior art, It can effectively solve existing compound cellulose pulp complex process and the prior art is not well positioned to meet existing equipment It is required that, COD content is high in pulping and digesting liquid and can lead to the problem of black liquor and easily causes environmental pollution and high production cost.
Technical solution of the present invention first is that being realized by following measures: a kind of cellulose mixture pulp passes through original Cotton pulp is mixed with wood pulp after the drift obtained by raw material papermaking grade wood pulp plate after the drift that material cotton linter obtains, and cellulose mixture is made Pulp;The index of cellulose mixture pulp are as follows: viscosity 10.2mPa.s to 11.8mPa.s, alpha cellulose 90% to 92%, ash ≤ 0.25%, iron content≤35ppm, whiteness 85% to 90%, pentosan≤3%, suction base number 520% to 600%, additional amount are 7ml's CS2Reactivity worth 10 seconds to 250 seconds, cotton fiber and wood-fibred weight percent be 20% to 80%:20% to 80%.
Here is further optimization or/and improvement of one of the above technical solutions of the invention:
Above-mentioned cellulose mixture pulp obtains in the steps below: the first step, and material is washed in mixing, and cotton pulp after drift is mixed with wood pulp after drift After wash material, wash material to pH value be 6 to 7;Second step, selected removal of impurities wash after material and carry out desanding, control slurry concentration with conical refiner It is 0.8% to 1.5%, desanding pressure is 0.25MPa to 0.35MPa;Third step is manufactured paper with pulp, and is manufactured paper with pulp after desanding with Fourdrinier pulp machine whole Finished product pulp is managed into, cellulose mixture pulp is obtained.
Cotton pulp obtains as follows after above-mentioned drift: the first step, and stock weighs raw material cotton linter;Second step, opener, The cotton linter packet shredding of outer packing will be removed with high speed opener;Third step, dry method removal of impurities, with opening or cleaning machine to cotton linter after shredding In boll hull, cotton stalk, cotton boll and cottonseed be purged;Cotton linter after 4th step, alkali steeping, prepared lye and removal of impurities exists It gives in leaching device and being mixed with dipping;5th step, squeezing squeeze the cotton linter after alkali leaching with pressafiner, make lye and cotton Short flannel is sufficiently mixed uniformly;6th step, spiral shell are sent, and the cotton linter containing alkali after Dip-squeeze is conveyed into rotary spherical digester;7th step, boiling, Boiling is carried out to the cotton linter containing alkali after Dip-squeeze;8th step, shove carry out shove to the slurry after boiling;9th step, beats Slurry is discongested, and is beaten after shove with steep-taper jordan, carries out sub-wire and brooming to fiber, the control of slurry concentration 2.5% to 3.5%;Tenth step, pulp washing are machine-washed with pulp washing and are expected, wash material to residual alkali concentration≤0.05g/L;Material is washed in 11st step, selected removal of impurities Carry out desanding with conical refiner afterwards, control slurry concentration is 0.8% to 1.5%, desander into slurry pressure be 0.25MPa extremely 0.35MPa;12nd step, bleaching are added sodium hypochlorite and are bleached after desanding, bleaching temperature is 40 DEG C to 46 DEG C, when bleaching Between be 1.5h to 3h, after bleaching be added dodium thiosulfate dechlorination to contain chlorine≤0.05g/L, viscosity be 8.28mpa.s to 9.72mpa.s; 13rd step, acid processing, is added hydrochloric acid or calgon is added simultaneously and carries out acid processing 40min to 60min for sulfuric acid, after processing Cotton pulp after being floated.
In the first step that after above-mentioned drift prepared by cotton pulp, by every 40m3Rotary spherical digester in feed intake 6300kg to 6700kg weighing cotton it is short Suede;Or/and the 4th in step, prepared lye and the cotton linter after removal of impurities are mixed with dipping giving in leaching device, and bath raio 1:2.5 is extremely 3.5, alkali charge is the 12% to 18% of cotton linter quality;Or/and the 7th in step, is steamed using heating three times and deflating three times It boils, is followed successively by dry run 10min, primary heating 20min to temperature is 130 DEG C, primary deflation 15min to temperature is 110 DEG C, two Secondary heating 20min is to temperature is 160 DEG C, secondary deflation 15min to temperature is 130 DEG C, heating 20min to temperature is 172 three times DEG C, be 168 DEG C to 172 DEG C in temperature to react 120min to 210min, deflation 60min to temperature be 105 DEG C, viscosity after boiling For 10mpa.s to 13mpa.s;Or/and the 8th in step, carries out shove to the slurry after boiling and extracts concentrated black liquid in slurry, it is dense Extraction rate of black liquor >=70%;Or/and the 12nd in step, be added after sodium hypochlorite chlorinity in slurry be 0.3g/L to 0.5g/L, Alkali content is 60g/m3To 100g/m3;Or/and the 13rd in step, is added after hydrochloric acid or sulfuric acid that acid content is 0.9g/L in slurry To 1.2g/L, the additional amount of calgon is the 0.01% to 0.02% of stock quality.
Wood pulp obtains as follows after above-mentioned drift: the first step, and stock, papermaking grade wood pulp plate is weighed and stocked up in batches; Second step feeds intake, and the papermaking grade wood pulp plate got ready is put into rotary spherical digester;Third step, leaching are steamed, and prepared alkali is added in rotary spherical digester Liquid is uniformly mixed, and carries out boiling to papermaking grade wood pulp plate;4th step, shove carry out shove with press master;5th step, pulp washing squeeze It is carried out washing material with Horizontal belt pulp dresser after slurry, washes material to residual alkali content≤150g/L;6th step, selected removal of impurities, is removed with taper Sand device cleans, and control slurry concentration is 0.8% to 1.5%, and desanding pressure is 0.25Mpa to 0.35Mpa;7th step is bleached, and is used Sodium hypochlorite is bleached, and bleaching temperature is 40 DEG C to 52 DEG C, and bleaching time is 1.5h to 3h, and dodium thiosulfate dechlorination is added after bleaching It is 90% to 92% to chlorine≤0.5g/L, viscosity 10.5mpa.s to 12mpa.s, wet pulp whiteness 85% to 87%, alpha cellulose is contained; 8th step, acid processing, is added hydrochloric acid or sulfuric acid carries out acid processing 40min to 60min, wood pulp after being floated after processing.
In the second step that after above-mentioned drift prepared by wood pulp, the papermaking grade wood pulp plate got ready is transported to elevator, steaming is promoted to Around ball mouth, by being put into rotary spherical digester after manual demolition outer packing, by every 40m3Rotary spherical digester in feed intake 6000kg to 6300kg papermaking Grade wood-pulp board;Or/and in third step, bath raio 1:3.4 to 4,19% to 28% that alkali charge is papermaking grade wood pulp plate quality are used Heating and progress boiling of deflating three times three times are followed successively by dry run 180min, primary heating 30min to temperature is 125 DEG C, one Secondary deflation 15min to temperature be 110 DEG C, secondary temperature elevation 25min to temperature is 145 DEG C, secondary deflation 15min to temperature is 130 DEG C, three times heating 30min be 165 DEG C, be 160 DEG C to 170 DEG C in temperature to temperature at react 90min to 150min, deflate 60min is 105 DEG C to temperature, and viscosity is 12mpa.s to 16mpa.s after boiling;Or/and the 4th in step, is squeezed with press master Slurry, separates high alkaline boiling yellow liquor, and shove pressure is 0.15Mpa to 0.2Mpa;Or/and the 7th in step, starches after sodium hypochlorite is added In material chlorinity be 0.25g/L to 0.40g/L, alkali content 90g/m3To 150g/m3;Or/and the 8th in step, be added hydrochloric acid or Acid content is 1g/L to 1.2g/L in slurry after sulfuric acid.
Technical solution of the present invention second is that being realized by following measures: a kind of cellulose mixture pulp and its preparation Method carries out in the steps below: material is washed in the first step, mixing, washes material after cotton pulp after drift is mixed with wood pulp after drift, washes material to pH value It is 6 to 7;Second step, selected removal of impurities wash after material and carry out desanding with conical refiner, and control slurry concentration is 0.8% to 1.5%, desanding Pressure is 0.25MPa to 0.35MPa;Third step is manufactured paper with pulp, and is manufactured paper with pulp after desanding with Fourdrinier pulp machine and is organized into finished product pulp, obtained Cellulose mixture pulp.
Here is further optimization or/and improvement of the technical scheme ii of the invention:
Cotton pulp obtains as follows after above-mentioned drift: the first step, and stock weighs raw material cotton linter;Second step, opener, with height Fast opener will remove the cotton linter packet shredding of outer packing;Third step, dry method removal of impurities, with opening or cleaning machine in cotton linter after shredding Boll hull, cotton stalk, cotton boll and cottonseed are purged;Cotton linter after 4th step, alkali steeping, prepared lye and removal of impurities is giving leaching It is mixed with dipping in device;5th step, squeezing squeeze the cotton linter after alkali leaching with pressafiner, make lye and cotton linter It is sufficiently mixed uniformly;6th step, spiral shell are sent, and the cotton linter containing alkali after Dip-squeeze is conveyed into rotary spherical digester;7th step, boiling, to leaching Stain cotton linter containing alkali after extruding carries out boiling;8th step, shove carry out shove to the slurry after boiling;9th step, mashing are dredged It solves, is beaten after shove with steep-taper jordan, sub-wire and brooming are carried out to fiber, slurry concentration control is 2.5% to 3.5%; Tenth step, pulp washing are machine-washed with pulp washing and are expected, wash material to residual alkali concentration≤0.05g/L;11st step, selected removal of impurities use cone after washing material Shape desander carries out desanding, and control slurry concentration is 0.8% to 1.5%, and desander is 0.25MPa to 0.35MPa into pressure is starched;Tenth Two steps, bleaching are added sodium hypochlorite and are bleached after desanding, bleaching temperature is 40 DEG C to 46 DEG C, and bleaching time is 1.5h to 3h, After bleaching be added dodium thiosulfate dechlorination to contain chlorine≤0.05g/L, viscosity be 8.28mpa.s to 9.72mpa.s;13rd step, acid at Reason, is added hydrochloric acid or calgon is added simultaneously and carries out acid processing 40min to 60min, cotton pulp after being floated after processing for sulfuric acid.
In the first step that after above-mentioned drift prepared by cotton pulp, by every 40m3Rotary spherical digester in feed intake 6300kg to 6700kg weighing cotton it is short Suede;Or/and the 4th in step, prepared lye and the cotton linter after removal of impurities are mixed with dipping giving in leaching device, and bath raio 1:2.5 is extremely 3.5, alkali charge is the 12% to 18% of cotton linter quality;Or/and the 7th in step, is steamed using heating three times and deflating three times It boils, is followed successively by dry run 10min, primary heating 20min to temperature is 130 DEG C, primary deflation 15min to temperature is 110 DEG C, two Secondary heating 20min is to temperature is 160 DEG C, secondary deflation 15min to temperature is 130 DEG C, heating 20min to temperature is 172 three times DEG C, be 168 DEG C to 172 DEG C in temperature to react 120min to 210min, deflation 60min to temperature be 105 DEG C, viscosity after boiling For 10mpa.s to 13mpa.s;Or/and the 8th in step, carries out shove to the slurry after boiling and extracts concentrated black liquid in slurry, it is dense Extraction rate of black liquor >=70%;Or/and the 12nd in step, be added after sodium hypochlorite chlorinity in slurry be 0.3g/L to 0.5g/L, Alkali content is 60g/m3To 100g/m3;Or/and the 13rd in step, is added after hydrochloric acid or sulfuric acid that acid content is 0.9g/L in slurry To 1.2g/L, the additional amount of calgon is the 0.01% to 0.02% of stock quality.
Wood pulp obtains as follows after above-mentioned drift: the first step, and stock, papermaking grade wood pulp plate is weighed and stocked up in batches; Second step feeds intake, and the papermaking grade wood pulp plate got ready is put into rotary spherical digester;Third step, leaching are steamed, and prepared alkali is added in rotary spherical digester Liquid is uniformly mixed, and carries out boiling to papermaking grade wood pulp plate;4th step, shove carry out shove with press master;5th step, pulp washing squeeze It is carried out washing material with Horizontal belt pulp dresser after slurry, washes material to residual alkali content≤150g/L;6th step, selected removal of impurities, is removed with taper Sand device cleans, and control slurry concentration is 0.8% to 1.5%, and desanding pressure is 0.25Mpa to 0.35Mpa;7th step is bleached, and is used Sodium hypochlorite is bleached, and bleaching temperature is 40 DEG C to 52 DEG C, and bleaching time is 1.5h to 3h, and dodium thiosulfate dechlorination is added after bleaching It is 90% to 92% to chlorine≤0.5g/L, viscosity 10.5mpa.s to 12mpa.s, wet pulp whiteness 85% to 87%, alpha cellulose is contained; 8th step, acid processing, is added hydrochloric acid or sulfuric acid carries out acid processing 40min to 60min, wood pulp after being floated after processing.
In the second step that after above-mentioned drift prepared by wood pulp, the papermaking grade wood pulp plate got ready is transported to elevator, steaming is promoted to Around ball mouth, by being put into rotary spherical digester after manual demolition outer packing, by every 40m3Rotary spherical digester in feed intake 6000kg to 6300kg papermaking Grade wood-pulp board;Or/and in third step, bath raio 1:3.4 to 4,19% to 28% that alkali charge is papermaking grade wood pulp plate quality are used Heating and progress boiling of deflating three times three times are followed successively by dry run 180min, primary heating 30min to temperature is 125 DEG C, one Secondary deflation 15min to temperature be 110 DEG C, secondary temperature elevation 25min to temperature is 145 DEG C, secondary deflation 15min to temperature is 130 DEG C, three times heating 30min be 165 DEG C, be 160 DEG C to 170 DEG C in temperature to temperature at react 90min to 150min, deflate 60min is 105 DEG C to temperature, and viscosity is 12mpa.s to 16mpa.s after boiling;Or/and the 4th in step, is squeezed with press master Slurry, separates high alkaline boiling yellow liquor, and shove pressure is 0.15Mpa to 0.2Mpa;Or/and the 7th in step, starches after sodium hypochlorite is added In material chlorinity be 0.25g/L to 0.40g/L, alkali content 90g/m3To 150g/m3;Or/and the 8th in step, be added hydrochloric acid or Acid content is 1g/L to 1.2g/L in slurry after sulfuric acid.
The present invention can better meet the index request of viscous fine short fine slurry compared with prior art, can adapt to different type Pulp machine manufacture paper with pulp;After drift in cooking liquor caused by the preparation process of cotton pulp, COD decline 20% to 25%;It is wooden after drift It starches in preparation process, boiling does not generate black liquor, COD decline 50% to 55%;It thus greatly reduces environmental pollution and is produced into This;Cellulose mixture pulp of the present invention has merged the hygroscopicity, skin-friendly and wood of cotton fiber for viscous de- staple fiber production simultaneously The characteristics such as stiffness, the coloring of fiber, to make obtained viscous de- using one of cellulose mixture pulp raw material of the present invention Staple fiber has more difference functions.
Specific embodiment
The present invention is not limited by the following examples, can determine according to the technique and scheme of the present invention with actual conditions specific Embodiment.It is previously mentioned various chemical reagent and chemical article in the present invention unless otherwise specified, is public in the prior art Know common chemical reagent and chemical article;Percentage in the present invention does not have specified otherwise such as, is mass percent;This hair It is the aqueous solution that solvent is water, for example, hydrochloric acid solution is aqueous hydrochloric acid solution if the solution in bright is without specified otherwise.
Embodiment 1, the cellulose mixture pulp, after the drift obtained by raw material cotton linter cotton pulp with pass through raw material papermaking level Wood pulp mixes after the drift that wood-pulp board obtains, and cellulose mixture pulp is made;The index of cellulose mixture pulp are as follows: viscosity 10.2mPa.s to 11.8mPa.s, alpha cellulose 90% to 92%, ash≤0.25%, iron content≤35ppm, whiteness 85% to 90%, pentosan≤3%, suction base number 520% to 600%, the CS that additional amount is 7ml2Reactivity worth 10 seconds to 250 seconds, cotton fiber Weight percent with wood-fibred is 20% to 80%:20% to 80%.Ppm is mass ratio.
Embodiment 2, the cellulose mixture pulp, after the drift obtained by raw material cotton linter cotton pulp with pass through raw material papermaking level Wood pulp mixes after the drift that wood-pulp board obtains, and cellulose mixture pulp is made;The index of cellulose mixture pulp are as follows: viscosity 10.2mPa.s or 11.8mPa.s, alpha cellulose 90% or 92%, ash≤0.25%, iron content≤35ppm, whiteness 85% or 90%, pentosan≤3%, suction base number 520% or 600%, the CS that additional amount is 7ml2Reactivity worth 10 seconds or 250 seconds, cotton fiber Weight percent with wood-fibred is 20% or 80%:20% or 80%.
Embodiment 3, the cellulose mixture pulp are obtained by following preparation methods: the first step, and material is washed in mixing, by cotton pulp after drift Material is washed after mixing with wood pulp after drift, washing material to pH value is 6 to 7;Second step, selected removal of impurities are carried out after washing material with conical refiner Desanding, control slurry concentration is 0.8% to 1.5%, and desanding pressure is 0.25MPa to 0.35MPa;Third step is manufactured paper with pulp, with length after desanding Net pulp machine, which is manufactured paper with pulp, is organized into finished product pulp, obtains cellulose mixture pulp.
Embodiment 4, as the optimization of above-described embodiment, cotton pulp obtains as follows after drift: the first step, stock, will be former Expect cotton linter weighing;Second step, opener will remove the cotton linter packet shredding of outer packing with high speed opener;Third step, dry method are removed It is miscellaneous, boll hull, cotton stalk, cotton boll and the cottonseed in cotton linter after shredding are purged with opening or cleaning machine;4th step, alkali steeping are prepared Cotton linter after good lye and removal of impurities is mixed with dipping giving in leaching device;5th step, squeezing, after being soaked with pressafiner to alkali Cotton linter is squeezed, and is sufficiently mixed lye and cotton linter uniformly;6th step, spiral shell are sent, and the cotton containing alkali after Dip-squeeze is short Suede is conveyed into rotary spherical digester;7th step, boiling carry out boiling to the cotton linter containing alkali after Dip-squeeze;8th step, shove, to boiling Slurry afterwards carries out shove;9th step, mashing are discongested, and are beaten after shove with steep-taper jordan, carry out sub-wire to fiber And brooming, slurry concentration control is 2.5% to 3.5%;Tenth step, pulp washing are machine-washed with pulp washing and are expected, wash material to residual alkali concentration≤0.05g/ L;11st step, selected removal of impurities wash after material and carry out desanding with conical refiner, and control slurry concentration is 0.8% to 1.5%, desander It is 0.25MPa to 0.35MPa into slurry pressure;12nd step, bleaching are added sodium hypochlorite and are bleached after desanding, bleaching temperature Be 40 DEG C to 46 DEG C, bleaching time be 1.5h to 3h, after bleaching be added dodium thiosulfate dechlorination to contain chlorine≤0.05g/L, viscosity is 8.28mpa.s to 9.72mpa.s;13rd step, acid processing, is added hydrochloric acid or calgon is added simultaneously and carries out at acid for sulfuric acid Manage 40min to 60min, cotton pulp after being floated after processing.In 4th step alkali steeping, alkali can be caustic soda;Slurry concentration control can pass through Add water management;Tap water can be added also with the waste water generated in production process when pulp washing machine washing material.
Embodiment 5, as the optimization of above-described embodiment, in the first step that after drift prepared by cotton pulp, by every 40m3Rotary spherical digester in The 6300kg to 6700kg that feeds intake weighing cotton linter;Or/and the 4th in step, prepared lye is giving with the cotton linter after removal of impurities It soaks in device and is mixed with dipping, bath raio 1:2.5 to 3.5, alkali charge is the 12% to 18% of cotton linter quality;Or/and the 7th in step, adopts Boiling is carried out with heating three times and three times deflation, is followed successively by dry run 10min, primary heating 20min to temperature is 130 DEG C, one Secondary deflation 15min to temperature be 110 DEG C, secondary temperature elevation 20min to temperature is 160 DEG C, secondary deflation 15min to temperature is 130 DEG C, three times heating 20min be 172 DEG C, be 168 DEG C to 172 DEG C in temperature to temperature at react 120min to 210min, deflate 60min is 105 DEG C to temperature, and viscosity is 10mpa.s to 13mpa.s after boiling;Or/and the 8th in step, to the slurry after boiling Carry out the concentrated black liquid in shove extraction slurry, concentrated black liquid recovery rate >=70%;Or/and the 12nd in step, after sodium hypochlorite is added In slurry chlorinity be 0.3g/L to 0.5g/L, alkali content 60g/m3To 100g/m3;Or/and the 13rd in step, and hydrochloric acid is added Or acid content is 0.9g/L to 1.2g/L in slurry after sulfuric acid, the additional amount of calgon be stock quality 0.01% to 0.02%.In 7th step, it can be welded in rotary spherical digester inner wall and install agitating device additional, using the rotary spherical digester boiling for heating up and deflating three times three times Technique reaches purification cellulose, reduces the degree of polymerization, destroys fiber primary wall purpose.
Embodiment 6, as the optimization of above-described embodiment, wood pulp obtains as follows after drift: the first step, stock, papermaking Grade wood-pulp board is weighed stocks up in batches;Second step feeds intake, and the papermaking grade wood pulp plate got ready is put into rotary spherical digester;Third step, leaching It steams, prepared lye is added in rotary spherical digester and is uniformly mixed, boiling is carried out to papermaking grade wood pulp plate;4th step, shove use shove Machine carries out shove;5th step, pulp washing are carried out washing material with Horizontal belt pulp dresser after shove, wash material to residual alkali content≤150g/L; 6th step, selected removal of impurities, is cleaned with conical refiner, and control slurry concentration is 0.8% to 1.5%, and desanding pressure is 0.25Mpa To 0.35Mpa;7th step, bleaching, is bleached with sodium hypochlorite, and bleaching temperature is 40 DEG C to 52 DEG C, bleaching time 1.5h Be added to 3h, after bleaching dodium thiosulfate dechlorination to contain chlorine≤0.5g/L, viscosity 10.5mpa.s to 12mpa.s, wet pulp whiteness 85% to 87%, alpha cellulose is 90% to 92%;8th step, acid processing, is added hydrochloric acid or sulfuric acid carries out acid processing 40min to 60min, Wood pulp after being floated after processing.In step 8, can also calgon, the additional amount of calgon is stock quality 0.01% to 0.02%.
Embodiment 7, as the optimization of above-described embodiment, in the second step that after drift prepared by wood pulp, by the papermaking level got ready wood Pulpboard is transported to elevator, is promoted to around rotary spherical digester mouth, by putting into rotary spherical digester after manual demolition outer packing, by every 40m3Rotary spherical digester In feed intake 6000kg to 6300kg papermaking grade wood pulp plate;Or/and in third step, bath raio 1:3.4 to 4, alkali charge are papermaking level wood The 19% to 28% of pulpboard quality carries out boiling using heating three times and three times deflation, is followed successively by dry run 180min, once rises Warm 30min to temperature be 125 DEG C, primary deflation 15min to temperature is 110 DEG C, secondary temperature elevation 25min to temperature is 145 DEG C, two Secondary deflation 15min is anti-to at temperature is 130 DEG C, heating 30min is 165 DEG C, is 160 DEG C to 170 DEG C in temperature to temperature three times Answering 90min to 150min, deflation 60min to temperature is 105 DEG C, and viscosity is 12mpa.s to 16mpa.s after boiling;Or/and the In four steps, shove is carried out with press master, separates high alkaline boiling yellow liquor, shove pressure is 0.15Mpa to 0.2Mpa;Or/and the 7th In step, be added after sodium hypochlorite chlorinity in slurry be 0.25g/L to 0.40g/L, alkali content 90g/m3To 150g/m3;Or/ With in the 8th step, be added after hydrochloric acid or sulfuric acid that acid content is 1g/L to 1.2g/L in slurry.It, can be in rotary spherical digester inner wall in third step Agitating device is installed in welding additional, using the rotary spherical digester digesting technoloy for heating up and deflating three times three times, reaches purification cellulose, reduces polymerization Degree destroys fiber primary wall purpose.
Above-described embodiment 1 obtains following test data through detection: viscous to the obtained cellulose mixture pulp of embodiment 7 Spend 10.2mPa.s to 11.8mPa.s, alpha cellulose 90% to 92%, ash≤0.25%, iron content≤35ppm, whiteness 85% to 90%, pentosan≤3%, suction base number 520% to 600%, the CS that additional amount is 7ml2Reactivity worth 10 seconds to 250 seconds, cotton fiber Weight percent with wood-fibred is 20% to 80%:20% to 80%.
Embodiment 8, the cellulose mixture pulp are obtained by following preparation methods: the first step, and material is washed in mixing, by cotton pulp after drift Material is washed after mixing with wood pulp after drift, washing material to pH value is 6;Second step, selected removal of impurities are removed after washing material with conical refiner Sand, control slurry concentration is 0.8%, and desanding pressure is 0.25MPa;Third step is manufactured paper with pulp, and is manufactured paper with pulp arrangement after desanding with Fourdrinier pulp machine At finished product pulp, cellulose mixture pulp is obtained.
In embodiment 8, cotton pulp obtains as follows after drift: the first step, and stock weighs raw material cotton linter;Second step, Opener will remove the cotton linter packet shredding of outer packing with high speed opener;Third step, dry method removal of impurities, with opening or cleaning machine to shredding after Boll hull, cotton stalk, cotton boll and cottonseed in cotton linter are purged;Cotton after 4th step, alkali steeping, prepared lye and removal of impurities Short flannel give leaching device in be mixed with dipping;5th step, squeezing squeeze the cotton linter after alkali leaching with pressafiner, make alkali Liquid and cotton linter are sufficiently mixed uniformly;6th step, spiral shell are sent, and the cotton linter containing alkali after Dip-squeeze is conveyed into rotary spherical digester;7th step, Boiling carries out boiling to the cotton linter containing alkali after Dip-squeeze;8th step, shove carry out shove to the slurry after boiling;9th Step, mashing are discongested, are beaten after shove with steep-taper jordan, carry out sub-wire and brooming to fiber, slurry concentration control exists 2.5%;Tenth step, pulp washing are machine-washed with pulp washing and are expected, washing material to residual alkali concentration is 0.05g/L;Material is washed in 11st step, selected removal of impurities Desanding is carried out with conical refiner afterwards, control slurry concentration is 0.8%, and desander is 0.25MPa into pressure is starched;12nd step, drift It is white, sodium hypochlorite is added after desanding and is bleached, bleaching temperature is 40 DEG C, and dodium thiosulfate is added after bleaching in bleaching time 1.5h Dechlorination is to containing chlorine 0.05g/L, viscosity 8.28mpa.s;13rd step, acid processing are added hydrochloric acid or sulfuric acid and six are added simultaneously partially Sodium phosphate carries out acid processing 40min, cotton pulp after being floated after processing.
In embodiment 8, in the first step that after drift prepared by cotton pulp, by every 40m3Rotary spherical digester in feed intake 6700kg weighing cotton it is short Suede;In 4th step, prepared lye and the cotton linter after removal of impurities are mixed with dipping giving in leaching device, and bath raio 1:2.5, alkali charge is The 12% of cotton linter quality;In 7th step, boiling is carried out using heating three times and three times deflation, is followed successively by dry run 10min, one Secondary heating 20min to temperature be 130 DEG C, primary deflation 15min to temperature is 110 DEG C, secondary temperature elevation 20min to temperature is 160 DEG C, secondary deflation 15min to temperature be 130 DEG C, heating 20min to temperature is 172 DEG C, is 168 DEG C to 172 DEG C in temperature three times Lower reaction 120min, deflation 60min to temperature are 105 DEG C, and viscosity is 10mpa.s after boiling;In 8th step, to the slurry after boiling Material carries out the concentrated black liquid in shove extraction slurry, and concentrated black liquid recovery rate is 70%;Or/and the 12nd in step, and sodium hypochlorite is added Afterwards in slurry chlorinity be 0.3g/L, alkali content 60g/m3;In 13rd step, acid content in slurry after addition hydrochloric acid or sulfuric acid For 0.9g/L, the additional amount of calgon is the 0.01% of stock quality.
In embodiment 8, wood pulp obtains as follows after drift: the first step, and stock, papermaking grade wood pulp plate is weighed in batches Stock;Second step feeds intake, and the papermaking grade wood pulp plate got ready is put into rotary spherical digester;Third step, leaching are steamed, and are added and are prepared in rotary spherical digester Good lye is uniformly mixed, and carries out boiling to papermaking grade wood pulp plate;4th step, shove carry out shove with press master;5th step, Pulp washing is carried out washing material with Horizontal belt pulp dresser after shove, and washing material to residual alkali content is 150g/L;6th step, selected removal of impurities are used Conical refiner cleans, and control slurry concentration is 0.8%, and desanding pressure is 0.25Mpa;7th step, bleaching, uses sodium hypochlorite It is bleached, bleaching temperature is 40 DEG C, bleaching time 1.5h, and dodium thiosulfate dechlorination is added after bleaching to contain chlorine be 0.5g/L, viscous Spend 10.5mpa.s, wet pulp whiteness 85%, alpha cellulose 90%;8th step, acid processing, is added hydrochloric acid or sulfuric acid carries out at acid Manage 40min, wood pulp after being floated after processing.
In embodiment 8, in the second step that after drift prepared by wood pulp, the papermaking grade wood pulp plate got ready is transported to elevator, is mentioned It rises to around rotary spherical digester mouth, by being put into rotary spherical digester after manual demolition outer packing, by every 40m3Rotary spherical digester in feed intake 6000kg papermaking level Wood-pulp board;In third step, bath raio 1:3.4,19% that alkali charge is papermaking grade wood pulp plate quality are put using heating three times and three times Gas carries out boiling, is followed successively by dry run 180min, primary heating 30min to temperature is 125 DEG C, primary deflation 15min to temperature It is 145 DEG C for 110 DEG C, secondary temperature elevation 25min to temperature, secondary deflation 15min to temperature is 130 DEG C, heats up 30min three times extremely Temperature reacts 90min at being 165 DEG C, being 160 DEG C to 170 DEG C in temperature, deflation 60min to temperature is 105 DEG C, viscosity after boiling For 12mpa.s;In 4th step, shove is carried out with press master, separates high alkaline boiling yellow liquor, shove pressure is 0.15Mpa;7th step In, be added after sodium hypochlorite chlorinity in slurry be 0.25g/L, alkali content 90g/m3;In 8th step, hydrochloric acid or sulfuric acid is added Acid content is 1g/L in slurry afterwards.
The cellulose mixture pulp that embodiment 8 obtains obtains following test data: viscosity 10.2mPa.s, first kind through detection Cellulose 90%, iron content 35ppm, whiteness 86%, pentosan 3%, inhales base number 520%, the CS that additional amount is 7ml at ash 0.23%2 Reactivity worth 250 seconds, cotton fiber and wood-fibred weight percent be 20%:80%.The present embodiment 8, can compared with prior art The index request of viscous fine short fine slurry is better met, and can adapt to different types of pulp machine and manufacture paper with pulp;The cotton after drift simultaneously The cooking liquor COD produced during the preparation process decline 22% of slurry, boiling does not generate black liquor in wood pulp preparation process after drift, under COD Drop 51%;Production cost reduces 30%.
Embodiment 9, the cellulose mixture pulp are obtained by following preparation methods: the first step, and material is washed in mixing, by cotton pulp after drift Material is washed after mixing with wood pulp after drift, washing material to pH value is 6;Second step, selected removal of impurities are removed after washing material with conical refiner Sand, control slurry concentration is 1.0%, and desanding pressure is 0.25MPa;Third step is manufactured paper with pulp, and is manufactured paper with pulp arrangement after desanding with Fourdrinier pulp machine At finished product pulp, cellulose mixture pulp is obtained.
In embodiment 9, cotton pulp obtains as follows after drift: the first step, and stock weighs raw material cotton linter;Second step, Opener will remove the cotton linter packet shredding of outer packing with high speed opener;Third step, dry method removal of impurities, with opening or cleaning machine to shredding after Boll hull, cotton stalk, cotton boll and cottonseed in cotton linter are purged;Cotton after 4th step, alkali steeping, prepared lye and removal of impurities Short flannel give leaching device in be mixed with dipping;5th step, squeezing squeeze the cotton linter after alkali leaching with pressafiner, make alkali Liquid and cotton linter are sufficiently mixed uniformly;6th step, spiral shell are sent, and the cotton linter containing alkali after Dip-squeeze is conveyed into rotary spherical digester;7th step, Boiling carries out boiling to the cotton linter containing alkali after Dip-squeeze;8th step, shove carry out shove to the slurry after boiling;9th Step, mashing are discongested, are beaten after shove with steep-taper jordan, carry out sub-wire and brooming to fiber, slurry concentration control exists 3.0%;Tenth step, pulp washing are machine-washed with pulp washing and are expected, washing material to residual alkali concentration is 0.02g/L;Material is washed in 11st step, selected removal of impurities Desanding is carried out with conical refiner afterwards, control slurry concentration is 0.9%, and desander is 0.25MPa into pressure is starched;12nd step, drift It is white, sodium hypochlorite is added after desanding and is bleached, bleaching temperature is 40 DEG C, and dodium thiosulfate is added after bleaching in bleaching time 1.8h Dechlorination is to containing chlorine 0.03g/L, viscosity 8.75mpa.s;13rd step, acid processing are added hydrochloric acid or sulfuric acid and six are added simultaneously partially Sodium phosphate carries out acid processing 50min, cotton pulp after being floated after processing.
In embodiment 9, in the first step that after drift prepared by cotton pulp, by every 40m3Rotary spherical digester in feed intake 6500kg weighing cotton it is short Suede;In 4th step, prepared lye with removal of impurities after cotton linter give leaching device in be mixed with dipping, bath raio 1:2.5 to 3.5, use Alkali number is the 15% of cotton linter quality;In 7th step, boiling is carried out using heating three times and three times deflation, is followed successively by dry run 10min, primary heating 20min to temperature are 130 DEG C, primary deflation 15min to temperature is 110 DEG C, secondary temperature elevation 20min to temperature Degree is 160 DEG C, secondary deflation 15min to temperature is 130 DEG C, heating 20min to temperature is 172 DEG C, is 168 DEG C in temperature three times It is 105 DEG C that 180min, deflation 60min to temperature are reacted to 172 DEG C, and viscosity is 11mpa.s after boiling;In 8th step, to steaming Slurry after boiling carries out the concentrated black liquid in shove extraction slurry, concentrated black liquid recovery rate 75%;In 12nd step, sodium hypochlorite is added Afterwards in slurry chlorinity be 0.4g/L, alkali content 70g/m3;In 13rd step, acid content in slurry after addition hydrochloric acid or sulfuric acid For 1.0g/L, the additional amount of calgon is the 0.01% of stock quality.
In embodiment 9, wood pulp obtains as follows after drift: the first step, and stock, papermaking grade wood pulp plate is weighed in batches Stock;Second step feeds intake, and the papermaking grade wood pulp plate got ready is put into rotary spherical digester;Third step, leaching are steamed, and are added and are prepared in rotary spherical digester Good lye is uniformly mixed, and carries out boiling to papermaking grade wood pulp plate;4th step, shove carry out shove with press master;5th step, Pulp washing is carried out washing material with Horizontal belt pulp dresser after shove, washes material to residual alkali content 100g/L;6th step, selected removal of impurities, with cone Shape desander cleans, and control slurry concentration is 0.9%, and desanding pressure is 0.25Mpa;7th step, bleaching, with sodium hypochlorite into Row bleaching, bleaching temperature are 40 DEG C, bleaching time 1.5h, and dodium thiosulfate dechlorination is added after bleaching to containing chlorine 0.3g/L, viscosity 11mpa.s, wet pulp whiteness 85%, alpha cellulose 90%;8th step, acid processing, is added hydrochloric acid or sulfuric acid carries out sour processing 50min, wood pulp after being floated after processing.
In embodiment 9, in the second step that after drift prepared by wood pulp, the papermaking grade wood pulp plate got ready is transported to elevator, is mentioned It rises to around rotary spherical digester mouth, by being put into rotary spherical digester after manual demolition outer packing, by every 40m3Rotary spherical digester in feed intake 6000kg papermaking level Wood-pulp board;In third step, bath raio 1:3.4,13% that alkali charge is papermaking grade wood pulp plate quality are put using heating three times and three times Gas carries out boiling, is followed successively by dry run 180min, primary heating 30min to temperature is 125 DEG C, primary deflation 15min to temperature It is 145 DEG C for 110 DEG C, secondary temperature elevation 25min to temperature, secondary deflation 15min to temperature is 130 DEG C, heats up 30min three times extremely Temperature reacts 120min at being 165 DEG C, being 160 DEG C to 170 DEG C in temperature, deflation 60min to temperature is 105 DEG C, glues after boiling Degree is 15mpa.s;In 4th step, shove is carried out with press master, separates high alkaline boiling yellow liquor, shove pressure is 0.15Mpa;7th In step, be added after sodium hypochlorite chlorinity in slurry be 0.25g/L, alkali content 90g/m3;In 8th step, hydrochloric acid or sulphur is added Acid content is 1g/L in slurry after acid.
The cellulose mixture pulp that embodiment 9 obtains obtains following test data: viscosity 10.8mPa.s, first kind through detection Cellulose 90%, iron content 30ppm, whiteness 85%, pentosan 2%, inhales base number 520%, the CS that additional amount is 7ml at ash 0.18%2 Reactivity worth 150 seconds, cotton fiber and wood-fibred weight percent be 60%:40%.The present embodiment 9, can compared with prior art The index request of viscous fine short fine slurry is better met, and can adapt to different types of pulp machine and manufacture paper with pulp;The cotton after drift simultaneously The cooking liquor COD produced during the preparation process decline 23% of slurry, boiling does not generate black liquor in wood pulp preparation process after drift, under COD Drop 50%;Production cost reduces 28%.
Embodiment 10, the cellulose mixture pulp are obtained by following preparation methods: the first step, and material is washed in mixing, by cotton after drift Slurry washes material after mixing with wood pulp after drift, and washing material to pH value is 7;Second step, selected removal of impurities are removed after washing material with conical refiner Sand, control slurry concentration is 1.5%, and desanding pressure is 0.35MPa;Third step is manufactured paper with pulp, and is manufactured paper with pulp arrangement after desanding with Fourdrinier pulp machine At finished product pulp, cellulose mixture pulp is obtained.
In embodiment 10, cotton pulp obtains as follows after drift: the first step, and stock weighs raw material cotton linter;Second Step, opener will remove the cotton linter packet shredding of outer packing with high speed opener;Third step, dry method removal of impurities, with opening or cleaning machine to shredding The boll hull in cotton linter, cotton stalk, cotton boll and cottonseed are purged afterwards;After 4th step, alkali steeping, prepared lye and removal of impurities Cotton linter give leaching device in be mixed with dipping;5th step, squeezing squeeze the cotton linter after alkali leaching with pressafiner, make Lye and cotton linter are sufficiently mixed uniformly;6th step, spiral shell are sent, and the cotton linter containing alkali after Dip-squeeze is conveyed into rotary spherical digester;7th Step, boiling carry out boiling to the cotton linter containing alkali after Dip-squeeze;8th step, shove carry out shove to the slurry after boiling; 9th step, mashing are discongested, and are beaten after shove with steep-taper jordan, carry out sub-wire and brooming, slurry concentration control to fiber 3.5%;Tenth step, pulp washing are machine-washed with pulp washing and are expected, wash material to residual alkali concentration 0.01g/L;Material is washed in 11st step, selected removal of impurities Desanding is carried out with conical refiner afterwards, control slurry concentration is 1.3%, and desander is 0.35MPa into pressure is starched;12nd step, drift It is white, sodium hypochlorite is added after desanding and is bleached, bleaching temperature is 46 DEG C, bleaching time 3h, and it is de- that dodium thiosulfate is added after bleaching Chlorine is to containing chlorine 0.02g/L, viscosity 8.4mpa.s;13rd step, acid processing, is added hydrochloric acid or hexa metaphosphoric acid is added in sulfuric acid simultaneously Sodium carries out acid processing 60min, cotton pulp after being floated after processing.
In embodiment 10, in the first step that after drift prepared by cotton pulp, by every 40m3Rotary spherical digester in feed intake 6700kg weighing cotton it is short Suede;In 4th step, prepared lye and the cotton linter after removal of impurities are mixed with dipping giving in leaching device, and bath raio 1:3.5, alkali charge is The 18% of cotton linter quality;Or/and the 7th in step, deflates using heating three times and three times and carries out boiling, is followed successively by dry run 10min, primary heating 20min to temperature are 130 DEG C, primary deflation 15min to temperature is 110 DEG C, secondary temperature elevation 20min to temperature Degree is 160 DEG C, secondary deflation 15min to temperature is 130 DEG C, heating 20min to temperature is 172 DEG C, is 168 DEG C in temperature three times It is 105 DEG C that 210min, deflation 60min to temperature are reacted to 172 DEG C, and viscosity is 12mpa.s after boiling;In 8th step, to steaming Slurry after boiling carries out the concentrated black liquid in shove extraction slurry, concentrated black liquid recovery rate 88%;In 12nd step, sodium hypochlorite is added Afterwards in slurry chlorinity be 0.3g/L, alkali content 60g/m3;In 13rd step, acid content in slurry after addition hydrochloric acid or sulfuric acid For 1.0g/L, the additional amount of calgon is the 0.02% of stock quality.
In embodiment 10, wood pulp obtains as follows after drift: the first step, and stock, papermaking grade wood pulp plate carries out weighing point Criticize stock;Second step feeds intake, and the papermaking grade wood pulp plate got ready is put into rotary spherical digester;Third step, leaching steam, are added and match in rotary spherical digester The lye made is uniformly mixed, and carries out boiling to papermaking grade wood pulp plate;4th step, shove carry out shove with press master;5th It walks, pulp washing, is carried out washing material with Horizontal belt pulp dresser after shove, wash material to residual alkali content 90g/L;6th step, selected removal of impurities are used Conical refiner cleans, and control slurry concentration is 1.5%, and desanding pressure is 0.35Mpa;7th step, bleaching, uses sodium hypochlorite It is bleached, bleaching temperature is 52 DEG C, bleaching time 3h, and dodium thiosulfate dechlorination is added after bleaching to containing chlorine 0.1g/L, viscosity extremely 12mpa.s, wet pulp whiteness 87%, alpha cellulose 92%;8th step, acid processing, is added hydrochloric acid or sulfuric acid carries out sour processing 60min, wood pulp after being floated after processing.
In embodiment 10, in the second step that after drift prepared by wood pulp, the papermaking grade wood pulp plate got ready is transported to elevator, is mentioned It rises to around rotary spherical digester mouth, by being put into rotary spherical digester after manual demolition outer packing, by every 40m3Rotary spherical digester in feed intake 6300kg papermaking level Wood-pulp board;In third step, bath raio 1:4,28% that alkali charge is papermaking grade wood pulp plate quality deflate using heating three times and three times Boiling is carried out, is followed successively by dry run 180min, primary heating 30min to temperature is 125 DEG C, primary deflation 15min to temperature is 110 DEG C, secondary temperature elevation 25min to temperature be 145 DEG C, secondary deflation 15min to temperature is 130 DEG C, heating 30min to temperature three times Degree reacts 150min at being 165 DEG C, being 160 DEG C to 170 DEG C in temperature, deflation 60min to temperature is 105 DEG C, viscosity after boiling For 16mpa.s;In 4th step, shove is carried out with press master, separates high alkaline boiling yellow liquor, shove pressure is 0.2Mpa;7th step In, be added after sodium hypochlorite chlorinity in slurry be 0.25g/L, alkali content 90g/m3;In 8th step, hydrochloric acid or sulfuric acid is added Acid content is 1.2g/L in slurry afterwards.
The cellulose mixture pulp that embodiment 10 obtains obtains following test data: viscosity 11.8mPa.s, first through detection Kind cellulose 92%, iron content 20ppm, whiteness 88%, pentosan 1%, inhales base number 600%, additional amount for 7ml's at ash 0.15% CS2Reactivity worth 230 seconds, cotton fiber and wood-fibred weight percent be 80%:20%;The present embodiment 10 compared with prior art, The index request of viscous fine short fine slurry can be better met, and can adapt to different types of pulp machine and manufacture paper with pulp;It is floating simultaneously The cooking liquor COD produced during the preparation process decline 22% of cotton pulp afterwards, boiling does not generate black liquor in wood pulp preparation process after drift, COD decline 53%;Production cost reduces 20%.
The advantages of present invention is compared with prior art:
1. the present invention matches corresponding slurrying work by its different characteristic using cotton linter and the difference slurrying of papermaking grade wood pulp plate Skill, after the index request for meeting viscous fine short fine slurry is made, the process or process progress mixing match is produced before manufacturing paper with pulp after drift Cellulose mixture pulp can adapt to different types of pulp machine and manufacture paper with pulp, and there are two types of fibers for the cellulose mixture pulp tool produced Common advantage, the pulp compared with prior art production can be good at meeting short rayon fiber Wesy slurry standard;
2. pulp-making of cotton linter of the present invention is using the dry method impurity removal process of optimization, the cooking liquor COD decline 20% to 25% of generation, at water Manage cost decline 30% to 40%;
3. papermaking grade wood pulp plate slurrying of the present invention is not done big using the technique that leaching is steamed using existing cotton pulp apparatus for production line Equipment is changed and increased, but is additionally arranged agitating device in rotary spherical digester, using dry run in 180 minutes, is completed to pulp The dipping split with lye is spread, alkali density effectively has been carried out to fiber, keeps part non-cellulosic impurity and half fiber molten before boiling In lye, the alpha cellulose of product is purer after boiling, and pentosan declines more, and reactivity worth is more optimized, can be fine Meet short rayon fiber Wesy slurry standard, while select papermaking grade wood pulp plate compared with wood raw material slurrying, equipment does not have to Big change is done, boiling does not generate black liquor, and COD decline 50% to 55%, production process pollutant is greatly reduced, and product is for viscous de- Staple fiber production, has merged the characteristics such as the hygroscopicity of cotton fiber, the stiffness of skin-friendly and wood-fibred, coloring, imparts viscous de- The more difference functions of staple fiber, belong to environment-friendly type pulping technique;
4. the present invention reduces 20% to 30% compared with prior art production cost.
In conclusion the present invention can better meet the index request of viscous fine short fine slurry, Neng Goushi compared with prior art Different types of pulp machine is answered to manufacture paper with pulp, the cooking liquor COD produced during the preparation process decline 20% to 25% of cotton pulp, is floating after drift Boiling does not generate black liquor in wood pulp preparation process afterwards, and COD decline 50% to 55% greatly reduces environmental pollution and production cost; For cellulose mixture pulp of the present invention for viscous de- staple fiber production, the hygroscopicity, skin-friendly and wood for having merged cotton fiber are fine simultaneously The characteristics such as stiffness, the coloring of dimension impart the viscous de- more difference functions of staple fiber, have a good application prospect.
The above technical features constitute embodiments of the present invention, can basis with stronger adaptability and implementation result Actual needs increases and decreases non-essential technical characteristic, to meet the needs of different situations.

Claims (11)

1. a kind of cellulose mixture pulp, it is characterised in that after the drift obtained by raw material cotton linter cotton pulp with pass through raw material papermaking Wood pulp mixes after the drift that grade wood-pulp board obtains, and cellulose mixture pulp is made;The index of cellulose mixture pulp are as follows: viscosity 10.2mPa.s to 11.8mPa.s, alpha cellulose 90% to 92%, ash≤0.25%, iron content≤35ppm, whiteness 85% to 90%, pentosan≤3%, suction base number 520% to 600%, the CS that additional amount is 7ml2Reactivity worth 10 seconds to 250 seconds, cotton fiber Weight percent with wood-fibred is 20% to 80%:20% to 80%.
2. cellulose mixture pulp according to claim 1, it is characterised in that obtain in the steps below: the first step, mixing Material is washed, washes material after cotton pulp after drift is mixed with wood pulp after drift, washing material to pH value is 6 to 7;Second step, selected removal of impurities are used after washing material Conical refiner carries out desanding, and control slurry concentration is 0.8% to 1.5%, and desanding pressure is 0.25MPa to 0.35MPa;Third step, It manufactures paper with pulp, is manufactured paper with pulp after desanding with Fourdrinier pulp machine and be organized into finished product pulp, obtain cellulose mixture pulp.
3. cellulose mixture pulp according to claim 2, it is characterised in that cotton pulp obtains as follows after drift: first Step, stock, raw material cotton linter is weighed;Second step, opener will remove the cotton linter packet shredding of outer packing with high speed opener; Third step, dry method removal of impurities, is purged boll hull, cotton stalk, cotton boll and the cottonseed in cotton linter after shredding with opening or cleaning machine;4th Step, alkali steeping, prepared lye and removal of impurities after cotton linter give soak device in be mixed with dipping;5th step, squeezing, with spiral pressure Cotton linter after crusher soaks alkali squeezes, and is sufficiently mixed lye and cotton linter uniformly;6th step, spiral shell are sent, and dipping is squeezed Cotton linter containing alkali after pressure is conveyed into rotary spherical digester;7th step, boiling carry out boiling to the cotton linter containing alkali after Dip-squeeze;8th Step, shove carry out shove to the slurry after boiling;9th step, mashing are discongested, and are beaten after shove with steep-taper jordan, Sub-wire and brooming are carried out to fiber, slurry concentration control is 2.5% to 3.5%;Tenth step, pulp washing are machine-washed with pulp washing and are expected, wash and expect to residual Alkali concentration≤0.05g/L;11st step, selected removal of impurities wash after material and carry out desanding with conical refiner, and control slurry concentration is 0.8% To 1.5%, desander is 0.25MPa to 0.35MPa into pressure is starched;12nd step, bleaching are added sodium hypochlorite and carry out after desanding Bleaching, bleaching temperature be 40 DEG C to 46 DEG C, bleaching time be 1.5h to 3h, after bleaching be added dodium thiosulfate dechlorination to contain chlorine≤ 0.05g/L, viscosity are 8.28mpa.s to 9.72mpa.s;13rd step, acid processing are added hydrochloric acid or sulfuric acid and six are added simultaneously partially Sodium phosphate carries out acid processing 40min to 60min, cotton pulp after being floated after processing.
4. cellulose mixture pulp according to claim 3, it is characterised in that in the first step that after drift prepared by cotton pulp, by every 40m3Rotary spherical digester in feed intake 6300kg to 6700kg weighing cotton linter;Or/and the 4th in step, after prepared lye and removal of impurities Cotton linter give leaching device in be mixed with dipping, bath raio 1:2.5 to 3.5, alkali charge be cotton linter quality 12% to 18%;Or/and In 7th step, boiling is carried out using heating three times and three times deflation, is followed successively by dry run 10min, primary heating 20min to temperature For 130 DEG C, primary deflation 15min to temperature be 110 DEG C, secondary temperature elevation 20min to temperature is 160 DEG C, secondary deflation 15min extremely Temperature is 130 DEG C, heating 20min reacts 120min extremely at being 172 DEG C, be 168 DEG C to 172 DEG C in temperature to temperature three times 210min, deflation 60min to temperature are 105 DEG C, and viscosity is 10mpa.s to 13mpa.s after boiling;Or/and the 8th in step, it is right Slurry after boiling carries out the concentrated black liquid in shove extraction slurry, concentrated black liquid recovery rate >=70%;Or/and the 12nd in step, adds Enter after sodium hypochlorite chlorinity in slurry be 0.3g/L to 0.5g/L, alkali content 60g/m3To 100g/m3;Or/and the 13rd In step, acid content is 0.9g/L to 1.2g/L in slurry after addition hydrochloric acid or sulfuric acid, and the additional amount of calgon is slurry matter The 0.01% to 0.02% of amount.
5. according to cellulose mixture pulp described in Claims 2 or 3 or 4, it is characterised in that wood pulp obtains as follows after drift Arrive: the first step, stock, papermaking grade wood pulp plate are weighed and are stocked up in batches;Second step feeds intake, the papermaking grade wood pulp plate that will be got ready It puts into rotary spherical digester;Third step, leaching are steamed, and prepared lye is added in rotary spherical digester and is uniformly mixed, steams to papermaking grade wood pulp plate It boils;4th step, shove carry out shove with press master;5th step, pulp washing are carried out washing material after shove with Horizontal belt pulp dresser, be washed Expect to residual alkali content≤150g/L;6th step, selected removal of impurities, is cleaned with conical refiner, control slurry concentration be 0.8% to 1.5%, desanding pressure is 0.25Mpa to 0.35Mpa;7th step, bleaching, is bleached with sodium hypochlorite, and bleaching temperature is 40 DEG C To 52 DEG C, bleaching time is 1.5h to 3h, and dodium thiosulfate dechlorination is added after bleaching to containing chlorine≤0.5g/L, viscosity 10.5mpa.s extremely 12mpa.s, wet pulp whiteness 85% to 87%, alpha cellulose are 90% to 92%;8th step, acid processing, be added hydrochloric acid or sulfuric acid into Row acid processing 40min to 60min, wood pulp after being floated after processing.
6. cellulose mixture pulp according to claim 5, it is characterised in that, will be standby in the second step that after drift prepared by wood pulp Good papermaking grade wood pulp plate is transported to elevator, is promoted to around rotary spherical digester mouth, by putting into rotary spherical digester after manual demolition outer packing, is pressed Every 40m3Rotary spherical digester in feed intake 6000kg to 6300kg papermaking grade wood pulp plate;Or/and in third step, bath raio 1:3.4 to 4, alkali is used Amount is the 19% to 28% of papermaking grade wood pulp plate quality, carries out boiling using heating three times and three times deflation, is followed successively by dry run 180min, primary heating 30min to temperature is 125 DEG C, primary deflation 15min to temperature is 110 DEG C, secondary temperature elevation 25min extremely Temperature is 145 DEG C, secondary deflation 15min to temperature is 130 DEG C, heating 30min to temperature is 165 DEG C, is 160 in temperature three times DEG C be 105 DEG C to 90min to 150min, deflation 60min to temperature is reacted at 170 DEG C, after boiling viscosity be 12mpa.s extremely 16mpa.s;Or/and the 4th in step, carries out shove with press master, separates high alkaline boiling yellow liquor, shove pressure be 0.15Mpa extremely 0.2Mpa;Or/and the 7th in step, is added after sodium hypochlorite that chlorinity is 0.25g/L to 0.40g/L in slurry, alkali content is 90g/m3To 150g/m3;Or/and the 8th in step, is added after hydrochloric acid or sulfuric acid that acid content is 1g/L to 1.2g/L in slurry.
7. a kind of preparation method of cellulose mixture pulp according to claim 1, it is characterised in that in the steps below into Row: material is washed in the first step, mixing, washes material after cotton pulp after drift is mixed with wood pulp after drift, and washing material to pH value is 6 to 7;Second step, essence Blanking is miscellaneous, washes after material and carries out desanding with conical refiner, and control slurry concentration is 0.8% to 1.5%, desanding pressure for 0.25MPa extremely 0.35MPa;Third step is manufactured paper with pulp, and is manufactured paper with pulp after desanding with Fourdrinier pulp machine and is organized into finished product pulp, and cellulose mixture pulp is obtained.
8. the preparation method of cellulose mixture pulp according to claim 7, it is characterised in that cotton pulp presses following sides after drift Method obtains: the first step, and stock weighs raw material cotton linter;Second step, opener will remove the cotton of outer packing with high speed opener Short flannel packet shredding;Third step, dry method removal of impurities, carries out boll hull, cotton stalk, cotton boll and the cottonseed in cotton linter after shredding with opening or cleaning machine It removes;4th step, alkali steeping, prepared lye with removal of impurities after cotton linter give leaching device in be mixed with dipping;5th step, pressure It squeezes, the cotton linter after alkali leaching is squeezed with pressafiner, is sufficiently mixed lye and cotton linter uniformly;6th step, spiral shell It send, the cotton linter containing alkali after Dip-squeeze is conveyed into rotary spherical digester;7th step, boiling, to the cotton linter containing alkali after Dip-squeeze into Row boiling;8th step, shove carry out shove to the slurry after boiling;9th step, mashing are discongested, and steep-taper refining is used after shove Machine is beaten, and carries out sub-wire and brooming to fiber, slurry concentration control is 2.5% to 3.5%;Tenth step, pulp washing are machine-washed with pulp washing Material washes material to residual alkali concentration≤0.05g/L;11st step, selected removal of impurities wash after material and carry out desanding with conical refiner, control Starching concentration is 0.8% to 1.5%, and desander is 0.25MPa to 0.35MPa into pressure is starched;12nd step, bleaching, is added after desanding Sodium hypochlorite is bleached, and bleaching temperature is 40 DEG C to 46 DEG C, and bleaching time is 1.5h to 3h, and dodium thiosulfate dechlorination is added after bleaching It is extremely 8.28mpa.s to 9.72mpa.s containing chlorine≤0.05g/L, viscosity;13rd step, acid processing, is added hydrochloric acid or sulfuric acid simultaneously Calgon is added and carries out acid processing 40min to 60min, cotton pulp after being floated after processing.
9. the preparation method of cellulose mixture pulp according to claim 8, it is characterised in that that after drift prepared by cotton pulp In one step, by every 40m3Rotary spherical digester in feed intake 6300kg to 6700kg weighing cotton linter;Or/and the 4th in step, prepared alkali Liquid with removal of impurities after cotton linter give leaching device in be mixed with dipping, bath raio 1:2.5 to 3.5, alkali charge be cotton linter quality 12% to 18%;Or/and the 7th in step, deflates using heating three times and three times and carries out boiling, is followed successively by dry run 10min, primary heating 20min to temperature be 130 DEG C, primary deflation 15min to temperature is 110 DEG C, secondary temperature elevation 20min to temperature is 160 DEG C, secondary Deflation 15min is reacted at temperature is 130 DEG C, heating 20min is 172 DEG C, is 168 DEG C to 172 DEG C in temperature to temperature three times 120min to 210min, deflation 60min to temperature are 105 DEG C, and viscosity is 10mpa.s to 13mpa.s after boiling;Or/and the In eight steps, the concentrated black liquid in shove extraction slurry, concentrated black liquid recovery rate >=70% are carried out to the slurry after boiling;Or/and the tenth In two steps, be added after sodium hypochlorite chlorinity in slurry be 0.3g/L to 0.5g/L, alkali content 60g/m3To 100g/m3;Or/ With in the 13rd step, be added after hydrochloric acid or sulfuric acid that acid content is 0.9g/L to 1.2g/L, the additional amount of calgon in slurry It is the 0.01% to 0.02% of stock quality.
10. according to the preparation method of cellulose mixture pulp described in claim 7 or 8 or 9, it is characterised in that wood pulp is pressed after drift Following methods obtain: the first step, and stock, papermaking grade wood pulp plate is weighed and stocked up in batches;Second step feeds intake, and makes what is got ready Paper grade wood-pulp board is put into rotary spherical digester;Third step, leaching are steamed, and prepared lye is added in rotary spherical digester and is uniformly mixed, to papermaking level wood Pulpboard carries out boiling;4th step, shove carry out shove with press master;5th step, pulp washing use Horizontal belt pulp dresser after shove It carries out washing material, washes material to residual alkali content≤150g/L;6th step, selected removal of impurities, is cleaned with conical refiner, and control slurry is dense Degree is 0.8% to 1.5%, and desanding pressure is 0.25Mpa to 0.35Mpa;7th step, bleaching, is bleached with sodium hypochlorite, is bleached Temperature is 40 DEG C to 52 DEG C, and bleaching time is 1.5h to 3h, and dodium thiosulfate dechlorination is added after bleaching to containing chlorine≤0.5g/L, viscosity 10.5mpa.s to 12mpa.s, wet pulp whiteness 85% to 87%, alpha cellulose are 90% to 92%;8th step, acid processing, is added salt Acid or sulfuric acid carry out acid processing 40min to 60min, wood pulp after being floated after processing.
11. the preparation method of cellulose mixture pulp according to claim 10, it is characterised in that after drift prepared by wood pulp In second step, the papermaking grade wood pulp plate got ready is transported to elevator, is promoted to around rotary spherical digester mouth, after manual demolition outer packing It puts into rotary spherical digester, by every 40m3Rotary spherical digester in feed intake 6000kg to 6300kg papermaking grade wood pulp plate;Or/and in third step, bath raio 1:3.4 to 4,19% to 28% that alkali charge is papermaking grade wood pulp plate quality carry out boiling using heating three times and three times deflation, according to Secondary is dry run 180min, primary heating 30min to temperature is 125 DEG C, primary deflation 15min to temperature is 110 DEG C, secondary Heating 25min to temperature is 145 DEG C, secondary deflation 15min to temperature is 130 DEG C, three times heating 30min to temperature be 165 DEG C, Reaction 90min to 150min, deflation 60min to temperature are 105 DEG C at being 160 DEG C to 170 DEG C in temperature, and viscosity is after boiling 12mpa.s to 16mpa.s;Or/and the 4th in step, carries out shove with press master, separates high alkaline boiling yellow liquor, shove pressure is 0.15Mpa to 0.2Mpa;Or/and the 7th in step, be added after sodium hypochlorite chlorinity in slurry be 0.25g/L to 0.40g/L, Alkali content is 90g/m3To 150g/m3;Or/and the 8th in step, be added after hydrochloric acid or sulfuric acid acid content in slurry be 1g/L extremely 1.2g/L。
CN201811089029.6A 2018-09-18 2018-09-18 Cellulose mixture pulp and preparation method thereof Pending CN109338774A (en)

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