CN110468611A - A kind of PRC-APMP pulping process of Eucalyptus urophylla - Google Patents
A kind of PRC-APMP pulping process of Eucalyptus urophylla Download PDFInfo
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- CN110468611A CN110468611A CN201910750012.9A CN201910750012A CN110468611A CN 110468611 A CN110468611 A CN 110468611A CN 201910750012 A CN201910750012 A CN 201910750012A CN 110468611 A CN110468611 A CN 110468611A
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
- D21B1/00—Fibrous raw materials or their mechanical treatment
- D21B1/02—Pretreatment of the raw materials by chemical or physical means
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
- D21B1/00—Fibrous raw materials or their mechanical treatment
- D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
- D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21D—TREATMENT OF THE MATERIALS BEFORE PASSING TO THE PAPER-MAKING MACHINE
- D21D1/00—Methods of beating or refining; Beaters of the Hollander type
- D21D1/20—Methods of refining
- D21D1/30—Disc mills
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Abstract
The invention discloses a kind of PRC-APMP pulping process of Eucalyptus urophylla, it includes following preparation step: the peeling of Eucalyptus urophylla timber, it chips, laggard pan feeding storage is screened to deposit, 1 section of wood chip steams in advance, enter wood chip mixing channel after chip washing, through wood chip pumping single-screw water extractor dehydration, 2 sections of wood chips steam in advance, 1 section of wood chip squeezes, 1 section of chip impregnation, 2 sections of wood chips squeeze, 2 sections of wood chip pre-soakings, 1 section of disc mill defibrination, cyclonic separation, cooling spiral is cooling, high density bleaching operation, acroll press washer dehydration concentration, 2 sections of disc mill defibrinations, cyclonic separation, eliminating potential pool placement disappears latent, double plate grinds defibrination, intermediate pool is placed, pressurized screen screening, buffer pool, the concentration of polydisc thickener, enter storage slurry tower after adding sulphur acid for adjusting pH value.The present invention, as raw material is prepared, formulates process flow and technological parameter according to Eucalyptus urophylla material feature using Eucalyptus urophylla, and slurrying is at low cost, and stock quality is good, meets the requirement of high-grade culture paper production, and the Paper bulk of production is higher.
Description
Technical field
The present invention relates to Manufacturing Pulps with E. urophylla technical field, the PRC-APMP pulping process of specially a kind of Eucalyptus urophylla.
Background technique
Eucalyptus is that China is only second to the maximum tree species of poplar cultivated area, and current Fibre Wood class product import volume is most
Big material kind.Eucalyptus is other than being largely used to production bleaching broad-leaved wood sulphate pulp, also by domestic reducing rules enterprise for producing
Chemi-mechanical pulp class product.Eucalyptus is many kinds of, diverse eucalyptus, and growth performance is different, fibr tissue form and chemistry
Composition difference is larger, and Paper Pulp difference is also larger.Eucalyptus urophylla originates in Indonesia, belongs to Perenniporia martius fast-growing
High megaphanerophyte, early growth is rapidly and energy is drought-resistant and barren, in China Guangdong, Guangxi and Hainan one with significant growth
Adaptability, be at present large area plantation the short-term or ultrashort period of felling in turn artificial forest tree species, wooden color is deeper, density compared with
Greatly.
The raw material of APMP slurrying at present are mainly American-European black poplar, and the material kind used is more single, on the one hand, poplar is good
Processing performance becomes China's board industry and consumes most log materials, and the buying of aspen fibers by using silicon raw material is in industry and to go
Comprehensive competition between industry；On the other hand, American-European black poplar large-scale plantation accelerates the droughtization of wetland, changes wetland soil knot
Structure also destroys the bio-diversity of wetland, and migratory bird is landed by barrier obstruction, and oviposition, the migration of fish are also destroyed.With
Yangtze River Zone turn national strategy into, Dongting Lake protection zone poplar of gradually clearing up and discharging restores ecology, and poplar is former at present
Material cannot difficulty meet supply requirement；Furthermore Gao Songdu paper product is increasingly favored by market, poplar PRC-APMP bulky
It spends relatively low, is not able to satisfy requirement of the paper product to slurry bulk.
Therefore, this department using Eucalyptus urophylla as slurrying raw material, a kind of independent research PRC-APMP slurrying of Eucalyptus urophylla
Method.
Summary of the invention
The purpose of the present invention is in view of the above problems, providing a kind of PRC-APMP pulping process of Eucalyptus urophylla, it uses tail
Ye An, which is used as, prepares raw material, and formulates process flow and technological parameter according to the material feature of Eucalyptus urophylla, and slurrying cost is lower, slurry
Expect better quality, fully meet the requirement of high-grade culture paper production, the Paper bulk of production is higher.
In order to achieve the above object, the technical solution adopted by the present invention is that: a kind of PRC-APMP pulping process of Eucalyptus urophylla, it
Including following preparation step:
Step A, Eucalyptus urophylla timber is taken, removed the peel, chipped, screening operation, after screening, the control of Eucalyptus urophylla strand length is
10-50mm；Dried thickness control is 2-6mm；By mass percentage, the qualification rate control of wood chip is 70-100%, percent of bark 0-
2%, Eucalyptus urophylla wood chip moisture 30-70%；
Step B, the made Eucalyptus urophylla wood chip of step A is sent into pre- storehouse of steaming to carry out steaming operation in advance, is then washed wood chip, wood chip
After single-screw water extractor is filtered dry moisture, it is sent into second of pre- steam of pre- steaming storehouse progress and operates, taking-up wood chip obtains standby material；
Step C, the made standby material of step B is sent into 1 section of MSD wood chip extruder, and added before 1 section of MSD wood chip extruder white
Water after completing wood chip extrusion operation, is sent into addition soak in 1 section of Presoaker and is impregnated, after the completion of immersion, be sent into 2 sections of MSD
Wood chip extruder is squeezed again, and adds plain boiled water before 2 sections of MSD wood chip extruders, after the completion of extruding, is sent into 2 sections of preimpregnation
Soak is added in device to be impregnated, is filtered dry soak after the completion of impregnating, obtains standby material；
Step D, the made standby material of step C is sent into 1 section of high concentration plate mill, partial bleaching medical fluid is added and carries out defibrination operation,
Pass through cyclone separator, cooling spiral conveyer after the completion of defibrination and send high density hypo tower to be separated, cooled down and highly concentrated in slurry
Standby material is made in whitening procedure；
Step E, the made standby material of step D is sent into dewatering spiral concentration, after completing dehydration concentration operation, is sent into 2 sections of mills
Machine is sent into eliminating potential pool after completing defibrination operation, slurry disappear it is latent after, be sent into double disc refiner and carry out low dense defibrination operation, defibrination is complete
At rear feeding intermediate pool, then after being selected good pulp screen by pressurized screen, it is sent into good stock tank, obtains standby material；
Step F, standby material made in step E is sent into polydisc thickener and carries out concentration operation, addition sulphur acid for adjusting pH value is 7-
7.8, then pass through in it is dense be pumped into storage slurry tower storage, finished product slurry.
Further, in step B, it is 40-90% that first time wood chip steams storehouse Level control in advance, and the temperature control of steam drain is
60-95℃；The control of chip washing coolant-temperature gage is 60-100 DEG C.
Further, in step B, it is 60-85% that second of wood chip steams storehouse Level control in advance, and the temperature control of steam drain is
70-90℃。
Further, in step C, the control of first time plain boiled water additive amount is 5-30m3/ h, the speed of 1 section of MSD wood chip extruder
Degree control is 10-70rpm, moment of torsion control 40-90kN.m, power control 200-1000kw, and 1 section of Presoaker Liquid level is
10-40%, NaOH are 0.3-2.8% to the control of over dry material dosage.
Further, in step C, second of plain boiled water additive amount control is 5-35m3/ h, the speed of 2 sections of MSD wood chip extruders
Degree control is 10-80rpm, moment of torsion control 45-95kN.m, power control 200-1000kw, and 2 sections of Presoaker Liquid levels are
10-40%, NaOH are 0.5-3.5%, H to the control of over dry material dosage2O2It is 1.0-4.0%, Na to the control of over dry material dosage2SiO3
It is 0.1-2.5% to the control of over dry material dosage.
Further, in step C and step D, soak and bleaching medical fluid are added to be modified amide base class compound
Based on composition bleach boosters, molecular formula main body is as follows:
。
Further, in step D, in 1 section of disc mill defibrination operation, medical fluid is bleached in high consistency refining entrance and blow-off pipe two
Point is added, high consistency refining entrance: NaOH is 0.1-1.8%, H to the control of over dry material dosage2O2To over dry material dosage 0.1-2.0%,
Bleach boosters 0.1-0.3%；On blow-off pipe: NaOH is 0.1-2.8%, H to the control of over dry material dosage2O2To over dry material dosage
0.1-2.5%, bleach boosters 0.1-0.3%, Mg (OH)2It is 0.1-2.0%, Na to the control of oven dry stock dosage2SiO3To oven dry stock
Dosage control is 1.0-4.0%；Highly concentrated drift tower: bleaching levels control is 10-40%, and bleaching temperature control is 70-100 DEG C, drift
White time control is 50-100min.
Further, in step E, in double plate defibrination operating process, refining concentration control is 4.5-7.5%, defibrination power control
It is made as 300-1600kw, the inlet pressure control of specific energy consumption 20-140kw/admt, double disc refiner are 0.5-2.8 bar, out
The pressure control of mouth is 2.3-5.6 bar, and double disc refiner exports the front and back pressure difference 0.1-0.7bar of pressure regulator valve.
Further, in step E, in the screening operation of pressurized screen, the screen slot control of pressurized screen is 0.1-0.3mm, into slurry
Concentration control be 1.0-3%, into slurry pressure control be 1.0-5.0 bar, inlet and outlet pressure difference control be 0-60kPa, slurry with it is good
The flow-ratio control of slurry is 10-40%；Operating load control is 30-90%.
Beneficial effects of the present invention: the present invention provides a kind of PRC-APMP pulping process of Eucalyptus urophylla, it uses caudal lobe
Eucalyptus, which is used as, prepares raw material, and formulates process flow and technological parameter according to the material feature of Eucalyptus urophylla, and slurrying cost is lower, slurry
Better quality, fully meets the requirement of high-grade culture paper production, and the Paper bulk of production is higher.
1, the present invention uses leaf tail eucalyptus for raw pulp, and Eucalyptus urophylla has wooden color deep, and density is big, at washing and preimpregnation
The saturate feature of waste liquid during reason is bleaching the waste water of color depth to reinforce the water suction swollen of chip washing process
Before can be discharged, chip washing coolant-temperature gage is greatly improved in the present invention, improves the moisture content of wood chip, improves washing for wood chip
It washs and squeezing effect.Before 1 section of MSD wood chip extruder and 1 section of MSD wood chip extruder, it is added to plain boiled water, may advantageously facilitate color
The discharge of the deep organic precipitate of element, mitigates the burden of bleaching, and improve the operational effect of wood chip extruder.
2, chip washing and steam temperature, wood chip greatly improved in order to effectively remove the eucalyptus oil in Eucalyptus piece in the present invention
In hot water extract be discharged effect it is preferable, avoid eucalyptus oil and pulping equipment, pulping process and wastewater treatment had an impact.
3, the present invention returns color to reduce the alkali of Eucalyptus piece, during wood chip preimpregnation, takes based on hydrogen peroxide, alkali
Supplemented by mode, improve H2O2Dosage, reduce the dosage of NaOH, effectively enhance Na2SiO3The collaboration of dosage is made
With keeping the consumption of hydrogen peroxide lower, the bulk of product slurry is more preferable.
4, the present invention improves preimpregnation Liquid level and reaction temperature, significantly improves the preimpregnation effect of wood chip.
5, the present invention be added in soak and bleaching medical fluid it is a kind of be modified based on amide base class compound at
The efficient bleach boosters of part, can more efficiently promote hydrogen peroxide to generate the stronger mistake of more oxidisability in bleaching process
Oxygen acid group compound eliminates the chromophoric group in lignin, achievees the purpose that bleached pulp together with HOO- ion；Improve dioxygen
The transformation efficiency of water, effectively improves the efficiency of hydrogen peroxide, so that the dosage of hydrogen peroxide be greatly lowered, improves the economic effect of bleaching
Benefit.
6, the present invention is deep according to Eucalyptus color, the feature more than extract, has carried out washing and 2 times are steamed operation in advance, be sent into wood
It is added to plain boiled water when piece extruder, allows the timely discharge system of alkali extractive, reduces the alkali extraction liquid of black liquor to later process
The effective consumption of hydrogen peroxide reduces the consumption of hydrogen peroxide in pulping process, has saved production cost, improves economic effect
Benefit.
7, the present invention is added to hydrogen peroxide, greatly improves entire pulping process in 1 section of disc mill defibrination operation
Bleaching effect.
8, it the characteristics of the present invention, fiber finer short according to Eucalyptus Fibers, is adjusted to beating degree control is slurried, with detection
Slurry tensile index is standard guidance control, reduces refining energy consumption, the better adaptability of manufacturing paper with pulp of slurry.
Specific embodiment
In order to make those skilled in the art more fully understand technical solution of the present invention, below with reference to embodiment to the present invention
Be described in detail, the description of this part be only it is exemplary and explanatory, should not have any limit to protection scope of the present invention
Production is used.
Embodiment 1:
The PRC-APMP pulping process of Eucalyptus urophylla includes following preparation step:
Step A, Eucalyptus urophylla timber is taken, removed the peel, chipped, screening operation, after screening, the control of Eucalyptus urophylla strand length is
19-25mm；Dried thickness control is 3-5mm；By mass percentage, the qualification rate control of wood chip is 70%, percent of bark 1.0%, tail
Leaf Eucalyptus piece moisture 30%；
Step B, the made Eucalyptus urophylla wood chip of step A is sent into pre- storehouse of steaming to carry out steaming operation in advance, wood chip steams storehouse Level control in advance and is
75%, the temperature control of steam drain is 85 DEG C, then washs wood chip, and the control of chip washing coolant-temperature gage is 75 DEG C, wood chip warp
After single-screw water extractor is filtered dry moisture, it to be sent into second of pre- steam of pre- steaming storehouse progress and operates, it is 75% that wood chip steams storehouse Level control in advance,
The temperature control of steam drain is 86 DEG C, takes out and is sufficiently filtered dry, obtains standby material；
Step C, the made standby material of step B is sent into 1 section of MSD wood chip extruder, and adds plain boiled water before MSD, plain boiled water additive amount
Control is 10m3/ h, the speed control of 1 section of MSD wood chip extruder are 45rpm, moment of torsion control 50kN.m, and power control is
500kw after completing wood chip extrusion operation, is sent into addition soak in 1 section of Presoaker and is impregnated, 1 section of Presoaker Liquid level
It is 0.5%, after the completion of immersion to the control of oven dry stock dosage for 25%, NaOH, is sent into 2 sections of MSD wood chip extruders and is squeezed again
Pressure, adds plain boiled water before MSD, and the control of plain boiled water additive amount is 12m3/ h, the speed control of 2 sections of MSD wood chip extruders are 55rpm,
Moment of torsion control is 50kN.m, power control 500kw, after the completion of extruding, is sent into addition soak in 2 sections of Presoakers and is soaked
Bubble, 2 sections of Presoaker Liquid levels are that 25%, NaOH is 3.95%, H to the control of oven dry stock dosage2O2It is to the control of oven dry stock dosage
3.0%, Na2SiO3It is 1.0% to the control of oven dry stock dosage, is filtered dry soak after the completion of impregnating, obtains standby material；
Step D, the made standby material of step C is sent into 1 section of disc mill, carries out defibrination and whitening procedure, adds in the highly concentrated mouth that is grinding into
Enter and bleach medical fluid, NaOH is 0.3%, H to the control of oven dry stock dosage2O2To oven dry stock dosage 1.0%, bleach boosters 0.1%；In
Bleaching medical fluid is added on blow-off pipe, NaOH is 1.0%, H to the control of oven dry stock dosage2O2To oven dry stock dosage 2.0%, bleaching promotes
Agent 0.1%, Mg (OH)2It is 0.5%, Na to the control of oven dry stock dosage2SiO3It is 1.5% to the control of oven dry stock dosage, bleaching levels
Control is 25%, and bleaching temperature control is 90 DEG C, and bleaching time control is 70min.Cyclonic separation is sequentially sent to after the completion of defibrination
Device, water-cooled screw conveyor and high density hypo tower, separated, cool down and high density bleaching operation, be made standby material；
Step E, the made standby material of step D spiral dewaterer is sent into slurry is concentrated, after completing dehydration concentration operation,
Be sent into 2 sections of disc mills, complete to be sent into eliminating potential pool after defibrination operation, slurry disappear it is latent after, be sent into double disc refiner and carry out low dense defibrination
Operation, it is 5.5% that double plate, which grinds refining concentration control, and defibrination power control is 700kw, specific energy consumption 25kw/admt, double plate defibrination
The inlet pressure control of machine is 1.2bar, and the pressure control of outlet is 2.9bar, and double disc refiner exports the front and back pressure of pressure regulator valve
Poor 0.2bar is sent into intermediate pool after completing defibrination operation, then after being selected good pulp screen by pressurized screen, is sent into good stock tank, obtains standby
Materials.The screen slot control of pressurized screen is 0.15mm, is 1.3% into slurry concentration control, is 2.6bar, inlet and outlet into slurry pressure control
Pressure difference control be 30kPa, the flow-ratio control of slurry and good slurry is 30%；Operating load control is 50%；
Step F, standby material made in step E is sent into polydisc mill and carries out defibrination operation, be then fed into dense storage slurry tower, addition sulphur
Acid for adjusting pH value, pH value control are 7.0, finished product slurry.
The made finished pulp quality index of embodiment 1: pulp brightness 77%ISO, freedom 220ml, tensile index 30Nm/
G, bulk 2.8,45 m of light scattering coefficient2/ kg, absorption coefficient of light 0.73m2/ kg, dirt count 100mm2/ kg, fibre bundle content
0.2%。
Embodiment 2:
The PRC-APMP pulping process of Eucalyptus urophylla includes following preparation step:
Step A, Eucalyptus urophylla timber is taken, removed the peel, chipped, screening operation, after screening, the control of Eucalyptus urophylla strand length is
19-25mm；Dried thickness control is 3-5mm；By mass percentage, the qualification rate control of wood chip is 85%, percent of bark 0.5%, tail
Leaf Eucalyptus piece moisture 50%；
Step B, the made Eucalyptus urophylla wood chip of step A is sent into pre- storehouse of steaming to carry out steaming operation in advance, wood chip steams storehouse Level control in advance and is
65%, the temperature control of steam drain is 80 DEG C, then washs wood chip, and the control of chip washing coolant-temperature gage is 60 DEG C, wood chip warp
After single-screw water extractor is filtered dry moisture, it to be sent into second of pre- steam of pre- steaming storehouse progress and operates, it is 65% that wood chip steams storehouse Level control in advance,
The temperature control of steam drain is 80 DEG C, takes out and is sufficiently filtered dry, obtains standby material；
Step C, the made standby material of step B is sent into 1 section of MSD wood chip extruder, and adds plain boiled water before MSD, plain boiled water additive amount
Control is 12m3/ h, the speed control of 1 section of MSD wood chip extruder are 50rpm, moment of torsion control 70kN.m, and power control is
600kw after completing wood chip extrusion operation, is sent into addition soak in 1 section of Presoaker and is impregnated, 1 section of Presoaker Liquid level
It is 0.3%, after the completion of immersion to the control of oven dry stock dosage for 22%, NaOH, is sent into 2 sections of MSD wood chip extruders and is squeezed again
Pressure, adds plain boiled water before MSD, and the control of plain boiled water additive amount is 10m3/ h, the speed control of 2 sections of MSD wood chip extruders are 60rpm,
Moment of torsion control is 70kN.m, power control 450kw, after the completion of extruding, is sent into addition soak in 2 sections of Presoakers and is soaked
Bubble, 2 sections of Presoaker Liquid levels are that 22%, NaOH is 3.5%, H to the control of oven dry stock dosage2O2It is to the control of oven dry stock dosage
2.6%, Na2SiO3It is 1.0% to the control of oven dry stock dosage, is filtered dry soak after the completion of impregnating, obtains standby material；
Step D, the made standby material of step C is sent into 1 section of disc mill, carries out defibrination and whitening procedure, adds in the highly concentrated mouth that is grinding into
Enter and bleach medical fluid, NaOH is 0.2%, H to the control of oven dry stock dosage2O2To oven dry stock dosage 0.8%, bleach boosters 0.1%；In
Bleaching medical fluid is added on blow-off pipe, NaOH is 0.8%, H to the control of oven dry stock dosage2O2To oven dry stock dosage 1.8%, bleaching promotes
Agent 0.1%, Mg (OH)2It is 0.8%, Na to the control of oven dry stock dosage2SiO3It is 1.5% to the control of oven dry stock dosage, bleaching levels
Control is 25%, and bleaching temperature control is 90 DEG C, and bleaching time control is 70min.Cyclonic separation is sequentially sent to after the completion of defibrination
Device, water-cooled screw conveyor and high density hypo tower, separated, cool down and high density bleaching operation, be made standby material；
Step E, the made standby material of step D spiral dewaterer is sent into slurry is concentrated, after completing dehydration concentration operation,
Be sent into 2 sections of disc mills, complete to be sent into eliminating potential pool after defibrination operation, slurry disappear it is latent after, be sent into double disc refiner and carry out low dense defibrination
Operation, it is 5.5% that double plate, which grinds refining concentration control, and defibrination power control is 700kw, specific energy consumption 25kw/admt, double plate defibrination
The inlet pressure control of machine is 1.2bar, and the pressure control of outlet is 2.9bar, and double disc refiner exports the front and back pressure of pressure regulator valve
Poor 0.2bar is sent into intermediate pool after completing defibrination operation, then after being selected good pulp screen by pressurized screen, is sent into good stock tank, obtains standby
Materials.The screen slot control of pressurized screen is 0.15mm, is 1.3% into slurry concentration control, is 2.6bar, inlet and outlet into slurry pressure control
Pressure difference control be 30kPa, the flow-ratio control of slurry and good slurry is 30%；Operating load control is 50%；
Step F, standby material made in step E is sent into polydisc mill and carries out defibrination operation, be then fed into dense storage slurry tower, addition sulphur
Acid for adjusting pH value, pH value control are 7.0, finished product slurry.
The made finished pulp quality index of embodiment 1: pulp brightness 80%ISO, freedom 220ml, tensile index 35Nm/
G, bulk 3.2,48 m of light scattering coefficient2/ kg, absorption coefficient of light 0.79m2/ kg, dirt count 40mm2/ kg, fibre bundle content
0.1%。
Compared with existing: the present invention is according to the wood characteristic of Eucalyptus urophylla, on the basis of existing poplar PRC-APMP slurrying,
Chip washing temperature improves 20%, and wood chip steam temperature improves 5-10%, wood chip steaming time 5-10min, wood chip be sent into
Before MSD wood chip extruder carries out extrusion operation, the washing and waste water displacement of wood chip are increased, one section of preimpregnation alkali charge increases 5-10
Kg/t slurry, two sections of leaching alkali charges reduce 3-8 kg/t slurry, and hydrogen peroxide reduces 2-6 kg/t slurry, and sodium metasilicate reduces 3-5 kg/t slurry,
Bleach paragraph alkali charge reduce 0-2 kg/t slurry, hydrogen peroxide increase 0-4 kg/t slurry, sodium metasilicate increase 2-5 kg/t slurry, preimpregnation and
Increase plus bleach boosters in bleaching medical fluid, MSD wood chip extruder, fiberizer technological parameter also carried out appropriate optimization, have
Effect has widened the raw material resources of reducing rules, improves stock quality, and pulping raw material cost is lower, slurrying power consumption is lower, slurry can
Drift performance is more preferable, and power consumption and chemicals cost are lower, can produce the reducing rules of higher whiteness and bulk, for the high loose paper of production
Product provides condition, has and saves timber resources benefit and environmental benefit.
It should be noted that, in this document, the terms "include", "comprise" or its any other variant are intended to non-row
His property includes, so that the process, method, article or equipment for including a series of elements not only includes those elements, and
And further include other elements that are not explicitly listed, or further include for this process, method, article or equipment institute it is intrinsic
Element.
Used herein a specific example illustrates the principle and implementation of the invention, the explanation of above example
It is merely used to help understand method and its core concept of the invention.The above is only a preferred embodiment of the present invention, it answers
When pointing out due to the finiteness of literal expression, and objectively there is unlimited specific structure, for the common skill of the art
For art personnel, without departing from the principle of the present invention, several improvement, retouching or variation can also be made, can also incited somebody to action
Above-mentioned technical characteristic is combined in the right way；These improve retouching, variation or combination, or the not improved structure by invention
Think and technical solution directly applies to other occasions, is regarded as protection scope of the present invention.
Claims (9)
1. a kind of PRC-APMP pulping process of Eucalyptus urophylla, which is characterized in that it includes following preparation step:
Step A, Eucalyptus urophylla timber is taken, removed the peel, chipped, screening operation, after screening, the control of Eucalyptus urophylla strand length is
10-50mm；Dried thickness control is 2-6mm；By mass percentage, the qualification rate control of wood chip is 70-100%, percent of bark 0-
2%, Eucalyptus urophylla wood chip moisture 30-70%；
Step B, the made Eucalyptus urophylla wood chip of step A is sent into pre- storehouse of steaming to carry out steaming operation in advance, is then washed wood chip, wood chip
After single-screw water extractor is filtered dry moisture, it is sent into second of pre- steam of pre- steaming storehouse progress and operates, taking-up wood chip obtains standby material；
Step C, the made standby material of step B is sent into 1 section of MSD wood chip extruder, and added before 1 section of MSD wood chip extruder white
Water after completing wood chip extrusion operation, is sent into addition soak in 1 section of Presoaker and is impregnated, after the completion of immersion, be sent into 2 sections of MSD
Wood chip extruder is squeezed again, and adds plain boiled water before 2 sections of MSD wood chip extruders, after the completion of extruding, is sent into 2 sections of preimpregnation
Soak is added in device to be impregnated, is filtered dry soak after the completion of impregnating, obtains standby material；
Step D, the made standby material of step C is sent into 1 section of high concentration plate mill, partial bleaching medical fluid is added and carries out defibrination operation,
Pass through cyclone separator, cooling spiral conveyer after the completion of defibrination and send high density hypo tower to be separated, cooled down and highly concentrated in slurry
Standby material is made in whitening procedure；
Step E, the made standby material of step D is sent into dewatering spiral concentration, after completing dehydration concentration operation, is sent into 2 sections of mills
Machine is sent into eliminating potential pool after completing defibrination operation, slurry disappear it is latent after, be sent into double disc refiner and carry out low dense defibrination operation, defibrination is complete
At rear feeding intermediate pool, then after being selected good pulp screen by pressurized screen, it is sent into good stock tank, obtains standby material；
Step F, standby material made in step E is sent into polydisc thickener and carries out concentration operation, addition sulphur acid for adjusting pH value is 7-
7.8, then pass through in it is dense be pumped into storage slurry tower storage, finished product slurry.
2. a kind of PRC-APMP pulping process of Eucalyptus urophylla according to claim 1, which is characterized in that in the step B,
It is 40-90% that first time wood chip steams storehouse Level control in advance, and the temperature control of steam drain is 60-95 DEG C；The control of chip washing coolant-temperature gage
It is 60-100 DEG C.
3. a kind of PRC-APMP pulping process of Eucalyptus urophylla according to claim 1, which is characterized in that in the step B,
It is 60-85% that second of wood chip steams storehouse Level control in advance, and the temperature control of steam drain is 70-90 DEG C.
4. a kind of PRC-APMP pulping process of Eucalyptus urophylla according to claim 1, which is characterized in that in the step C,
The control of first time plain boiled water additive amount is 5-30m3/ h, the speed control of 1 section of MSD wood chip extruder are 10-70rpm, moment of torsion control
For 40-90kN.m, power control 200-1000kw, 1 section of Presoaker Liquid level is 10-40%, and NaOH is to over dry material dosage control
It is made as 0.3-2.8%.
5. a kind of PRC-APMP pulping process of Eucalyptus urophylla according to claim 1, which is characterized in that in the step C,
Second of plain boiled water additive amount control is 5-35m3/ h, the speed control of 2 sections of MSD wood chip extruders are 10-80rpm, moment of torsion control
For 45-95kN.m, power control 200-1000kw, 2 sections of Presoaker Liquid levels are 10-40%, and NaOH is to over dry material dosage control
It is made as 0.5-3.5%, H2O2It is 1.0-4.0%, Na to the control of over dry material dosage2SiO3It is 0.1- to the control of over dry material dosage
2.5%.
6. a kind of PRC-APMP pulping process of Eucalyptus urophylla according to claim 1, which is characterized in that the step C and
In step D, soak and bleaching medical fluid are added to be modified the bleach boosters of composition based on amide base class compound,
Molecular formula main body is as follows:
。
7. a kind of PRC-APMP pulping process of Eucalyptus urophylla according to claim 1, which is characterized in that in the step D,
In 1 section of disc mill defibrination operation, bleaching medical fluid is added in high consistency refining entrance and blow-off pipe two o'clock；High consistency refining entrance: NaOH
It is 0.1-1.8%, H to the control of over dry material dosage2O2To over dry material dosage 0.1-2.0%, bleach boosters 0.1-0.3%；Blow-off pipe
Upper: NaOH is 0.1-2.8%, H to the control of over dry material dosage2O2To over dry material dosage 0.1-2.5%, bleach boosters 0.1-
0.3%, Mg (OH)2It is 0.1-2.0%, Na to the control of oven dry stock dosage2SiO3It is 1.0-4.0% to the control of oven dry stock dosage；It is high
Dense drift tower: bleaching levels control is 10-40%, and bleaching temperature control is 70-100 DEG C, and bleaching time control is 50-100min.
8. a kind of PRC-APMP pulping process of Eucalyptus urophylla according to claim 1, which is characterized in that in the step E,
In double plate defibrination operating process, refining concentration control is 4.5-7.5%, and defibrination power control is 300-1600kw, specific energy consumption
20-140kw/admt, the inlet pressure control of double disc refiner are 0.5-2.8 bar, and the pressure control of outlet is 2.3-5.6
Bar, double disc refiner export the front and back pressure difference 0.1-0.7bar of pressure regulator valve.
9. a kind of PRC-APMP pulping process of Eucalyptus urophylla according to claim 1, which is characterized in that in the step E,
In the screening operation of pressurized screen, the screen slot control of pressurized screen is 0.1-0.3mm, is 1.0-3% into slurry concentration control, into slurry pressure
Control is 1.0-5.0 bar, and the pressure difference control of inlet and outlet is 0-60kPa, and the flow-ratio control of slurry and good slurry is 10-40%；Fortune
Row load control system is 30-90%.
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Application publication date: 20191119 |