CN105568726A - Wet-strength wastepaper recycling double-pH-value chemical and mechanical pulping method - Google Patents

Wet-strength wastepaper recycling double-pH-value chemical and mechanical pulping method Download PDF

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Publication number
CN105568726A
CN105568726A CN201610070560.3A CN201610070560A CN105568726A CN 105568726 A CN105568726 A CN 105568726A CN 201610070560 A CN201610070560 A CN 201610070560A CN 105568726 A CN105568726 A CN 105568726A
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chemical
wet
chemical mechanical
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CN105568726B (en
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曹堪洲
范刚华
徐涛
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JIANGSU JINWO MACHINERY CO Ltd
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JIANGSU JINWO MACHINERY CO Ltd
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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
    • D21B1/30—Defibrating by other means
    • D21B1/32—Defibrating by other means of waste paper
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
    • D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
    • D21B1/30—Defibrating by other means
    • D21B1/34—Kneading or mixing; Pulpers
    • D21B1/345—Pulpers
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C1/00—Pretreatment of the finely-divided materials before digesting
    • D21C1/02—Pretreatment of the finely-divided materials before digesting with water or steam
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C1/00—Pretreatment of the finely-divided materials before digesting
    • D21C1/06—Pretreatment of the finely-divided materials before digesting with alkaline reacting compounds
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C5/00—Other processes for obtaining cellulose, e.g. cooking cotton linters ; Processes characterised by the choice of cellulose-containing starting materials
    • D21C5/02—Working-up waste paper
    • D21C5/022—Chemicals therefor
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/64—Paper recycling

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  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Mechanical Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Toxicology (AREA)
  • Paper (AREA)

Abstract

The invention discloses a wet-strength wastepaper recycling double-pH-value chemical and mechanical pulping method. The method includes a material preparation section, a steaming section, a first extrusion and impregnation chemical and mechanical treatment section, a second extrusion and impregnation chemical and mechanical treatment section, a latency and re-defibering section and a purification, screening and concentration section. Wet-strength wastepaper fiber dissociation re-pulping is achieved while original pulp strength is not reduced through the mechanical strong force effect and the chemical treatment effect. Furthermore, on the two extrusion and impregnation chemical and mechanical treatment sections connected in series, a wet strength agent in wastepaper is oxidized under the acid condition firstly, hydrolysis is further promoted under the alkaline condition, chemical bonding between molecules of the wet strength agent and between the wet strength agent and pulp fibers is more effectively damaged, and the fiber dissociation rate and the re-pulping yield are effectively increased. The problems that the wet-strength wastepaper recycling pulping dissociation rate is low and strength is greatly decreased are solved, and continuous, large-scale, low-water-consumption and low-energy-consumption pollution-free and environment-friendly pulping can be achieved.

Description

The two pH value chemical mechanical pulp-making method of a kind of wet strong waste paper recycling
Technical field
The present invention relates to a kind of pulping system and pulping process, be specifically related to a kind of waste paper recycling chemical-mechanical pulping system and pulping process.
Background technology
Waste paper is important raw material of papermaking fiber, and each state all takes much count of the recycling of waste paper resources, and world's waste paper yield brings up to 2.234 hundred million tons in 2010 by 1.826 hundred million tons in 2005; The rate of recovery brings up to 56.6% by 49.8%, and developed country is generally more than 60%, and Korea S, Germany are more than 80%.China's waste paper pulp-making increases to 5,305 ten thousand tons in 2010 by 2,810 ten thousand tons in 2005, accounts for and is always promoted to 62.7% with slurry amount proportion by 54.0%, and wherein the proportion of domestic waste paper slurry is promoted to 38.0% by 27.8%.To " 12 " period, secondary stock increment is about 1,400 ten thousand tons.The domestic waste paper rate of recovery will be increased to 46.7%, meanwhile, still will make full use of waste paper resources overseas, make China's paper industry waste paper utilization rate be increased to 72.1%.
At present, by the impact of the factors such as the lower and waste paper rate of recovery of domestic waste paper quality is on the low side, waste paper resources supply external dependence degree is higher, give up in U.S. useless, Europe and day is useless substantially all can enter China by Export resource, and quality is declining year by year, price is but improving year by year, and imbalance between supply and demand increasingly sharpens.
The regeneration of waste paper can save a large amount of protofibre resources, economize energy consumption, alleviate the pollution of environment, and compared to market pulp, the slurrying again of waste paper has obvious cost advantage.Along with the raising of people's living standard, also more and more higher to the requirement of paper and paperboard, a lot of paper kind particularly packaging group cardboard in order to can moist or have water to deposit in case still to there is certain intensity, often using wet strength agent when producing.These quantity with the waste paper of wet strength are in increasing trend year by year.Not containing the common paper of wet strength agent, fiber connects the Van der Waals force relying on hydrogen bond to be formed, and water can be broken hydrogen bond and connect, and makes paper size degradation.Wet strength agent resin can form the network structure of crosslinked, insoluble in water and covalent bond with cellulose, hemicellulose.Under normal circumstances, the paper through wet strengthening resin process will maintain more than 30% of former dry strength after by water complete wetting, can keep paper integrity degree, and only can maintain the former dry strength of 2 ~ 7% without the common paper of wet strength agent process.
Therefore, the waste paper that wet strength is high is recycled very difficult, there is the technical problems such as high screening reject content, low yield and high power consumption and be difficult to solve during pulping, and this is mainly because discongest equipment and process with conventional slurrying it fully can not be dispersed into paper pulp.Often be mingled with the wet strong waste paper that some are difficult to discongest in the waste paper of import, the solidity forever particularly employing high-load wet strength agent wets strong waste paper, discongests very difficulty, even if extend beating time or increase the effect that refining strength is also difficult to obtain.The waste paper that a lot of wet strength is higher is landfilled as solid waste, or as waste incineration, this had both caused the pollution of environment, wasted the waste paper resources that can be used for papermaking.
Many wet-strength papers contain high-quality bleached chemical fiber or high-quality long stuff, have very high value, and the shortage of current raw material of papermaking fiber impels the regeneration of paper industry to wet strong waste paper to carry out large technological improvement.
Wet strong waste paper process of repulping and technology are mainly divided into two classes at present: Mechanical Method and chemical method, and are all in conceptual phase advanced development.
[1] Mechanical Method wets strong waste paper process of repulping.(the Du Yong such as Du Yong, Wang Zhongyuan. the process [J] of useless wet-strength paper. Chinese papermaking, 2009,28 (7): 68 ~ 69) utilize Mechanical Method process to wet strong waste paper, do not need steam in processing procedure, only need that Purely mechanical is pulled an oar, defibrination discongests waste paper into qualified fibre stuff.First waste paper pass through high-concentration pulper size degradation, pulping concentration 12 ~ 15%, pulping time 25 ~ 30min, service intermittent, and after every pot of blowing, the larger scraps of paper of accumulation, because passing through pulper extraction plate sieve aperture, by retention pot, give over to making beating next time; High-concentration pulper has often broken one pot of slurry, is just transported to intermediate buffering by conveying worm and starches tank, slurry concentration dilution to 8 ~ 10% in tank; In buffering slurry tank, slurry utilizes high potential difference, certainly flow to Double screw pulp extruder and is concentrated into slurry dense 25 ~ 30%; Concentrated disposed slurry is through the paramount dense mill paste mill grinding of inclined screw conveyer conveying, and high dense mill refining concentration 20 ~ 30%, defibrination process adopts two series systems, and defibrination disposed slurry beating degree can reach beating degree during former pulping.The weak point of this technology is that (1) high dense pulping is produced discontinuous, and the time is longer; (2) power consumption is higher; (3) wet strength agent is without chemical treatment, can cause in postorder pulping and papermaking processes and flocculate, affect paper making; (4) result of use of the chemicals such as other resident auxiliary agent when the existence of wet strength agent can affect paper making.
[2] alkaline process chemical steaming wets strong waste paper process of repulping.(king builds Wang Jian etc., Qi Liang, galvanized iron army, Hua Kaikai .PAE is humidified the pulping process again [J] of strong true qualities waste paper. paper and papermaking, 2008,27 (5): 47-49) with the method process true qualities waste paper of chemical steaming, waste paper is loaded rotary spherical digester, liquor ratio 1:6, adds the caustic soda of 1% and the AQ of 0.05% carries out boiling, again by hydrabrusher size degradation after boiling.Maximum temperature of cooking 160 DEG C, under the condition of insulation 30min, unscreened yield can reach 82.7%, then slurrying loss late 17.3%.(the Cao Qingfu such as Cao Qingfu, Zhang Yuanbin, Zhang Guilan. wet strong waste paper optimization process method choice [J]. Chinese paper industry, 1998 (4): 45) with the spool cover paper of self-control digester treated containing wet strength agent, the aluminum sulfate boiling 2h of 7.5% is added in the boiling vessel loading waste paper, then through hydrabrusher size degradation, waste paper per ton utilized the Mechanical Method of hydrabrusher and beater device processes more originally, ton slurry power consumption is down to 146kw.h by original 1232kw.h, reduction expense 1148 yuan, achieves good effect.Alkaline process chemical steaming can decompose wet strength agent or destroy the chemical bond of wet strength agent and paper pulp fiber, and dissociate wet-strength paper.Existing problems: (1) secondary stock yield is lower, enter into pulp-making waste-water after a large amount of fibrous raw material degradeds, add difficulty and the cost of wastewater treatment; (2) if not to the secondary stock bleaching of dissociating, pulp brightness is very low, and can only be used for some in the less demanding cardboard of whiteness, paper pulp purposes is restricted; (3) chemical steaming method is to the chemical action of secondary stock than stronger, causes cellulosic degree of polymerization to decline, and causes the physical strength of pulping to decline.
[3] oxidizer treatment wets strong waste paper process of repulping.Polyamide-Polyamsne-Epichlorohydrin (PAE) resin accounts for leading wet strength agent in current paper industry, and thus, the research much about wet strong waste paper regenerated utilization all to be wet strong waste paper for PAE class.Oxidant can destroy network structure that PAE produces in page or directly destroy the chemical bond of it and paper pulp fiber, and dissociate wet-strength paper.Mainly contain:
(1) hypochlorite facture.Be in the wet-strength paper slurry of about 5% in concentration, slowly add NaOH solution and adjust pH value to 11, then add NaCIO bleaching liquor, process certain hour at the reaction temperatures.Question response terminates, and is transferred in high speed dispersor by paper stock mixed liquor and shears a few minutes, and slurry carries out copy paper again through washing.
Research shows: NaCIO consumption has the greatest impact to discongesting of wet-strength paper, when consumption reaches 0.5 ~ 0.8g/L, discongests and is easier to, discongest rate higher; PH value is comparatively special on the impact of NaCIO method, PAE resin is in wider pH value (4 ~ 10) scope, there is good stability, when particularly pH value is between 6.5 ~ 8.0, its character is the most stable, and the least destructible of the cross-bond between amide epoxy compound, discongests the most difficult, so the stability range of resin should be avoided, select to discongest under the condition of PH < 6.5 or highly basic (PH > 11); Temperature is also the key factor affecting slurrying again, and during with clorox or calcium hypochlorite process PAE wet-strength paper, higher treatment temperature is unfavorable for slurrying again; Mechanical shearing process is similar with the principle of refining to making beating to the effect of slurrying again, can increase fiber profit, thus is conducive to the intensity improving page.
Existing problems: hypochlorite facture effectively can process the PAE wet-strength paper of bleaching, and cost is lower, but it can not by the slurrying completely again of non-bleached wet-strength paper, and, can increase the load of the Adsorbable organic halogens such as chloroform, tetrachloroethanes (AOX) in sewage effluent, this is also the unfavorable factor that restriction hypochlorite uses.
(2) peroxidisulfates process is wet strong waste paper.(the Wang Lijuan such as Wang Lijuan, Yang Runan, Zhang Haitao, Deng. wet-strength paper again slurrying research [J]. Chinese papermaking, 2004,23 (4): 63-64) adopt potassium peroxydisulfate process to give up RMB paper, comparatively suitable treatment conditions are potassium peroxydisulfate consumption 6%, acid treatment pH value 3, time 30min, slurrying concentration 13%.Pulping rate can be controlled in more than 94%.Stephen.AFicher etc. (Ficher, S.A..Repulpingwet-strengthpaper[J] .TappiJ1997,80 (11): 141-147) contain the true qualities craft paper of PAE wet strength agent with sodium peroxydisulfate process.When the consumption of sodium peroxydisulfate is 1%, preliminary treatment pH value 11, under discongesting the condition of time 70min, the pulping yield again of true qualities craft paper (PAE consumption 0.6%) reaches 66%.When increasing further the consumption of sodium peroxydisulfate to 10%, preliminary treatment pH value and the time constant when, process another kind of true qualities craft paper (PAE consumption 0.4%), then pulping yield can reach 74%.Result shows, persulfate is poor to the treatment effect of the wet strong waste paper containing PAE in the basic conditions.
The model compound reaction mechanism of peroxidisulfates: the secondary amide key between the tertiary amine of oxidant easy attack PAE resin polymer or acid amides-epoxide, makes PAE resin generation decomposition reaction, thus cause wet-strength paper to lose wetly strengthening function.
Peroxidisulfates process wet strong waste paper again slurrying to be subject to processing the impact of the factors such as temperature, reaction time, oxidant consumption, pH value and mechanical shearing larger.Temperature raises and is conducive to slurrying again, and under neutral and alkali condition, the pulp strength after process a little more than NaCIO method, but needs slightly high temperature, and reaction speed is slightly slow, then slurrying whiteness is lower slightly; Peroxidisulfates again in pulping waste liquor the content of adsorbable organic halogen extremely low; Slurrying adds the wet strength agent of equivalent again without washing again, and the wet strength of residual peroxidisulfates on the paper of copy paper again affects the impact produced far below residual NaCIO, can save a large amount of washings.
Existing problems: in neutral or alkalescence again pulping process, because peroxidisulfates decomposes the free radical that the free radical hydrogen that can extract on lignin produced forms reactionless activity, and make most of wet strengthening resin not oxidized, so, peroxidisulfates is not too effective to unbleached kraft pulp, CTMP and OCC wet-strength paper, is difficult to slurrying again.Though excessive peroxidisulfates can overcome this side reaction, but expensive, and efficiency is not high, and has infringement to fiber.
Summary of the invention
Goal of the invention: in order to overcome the deficiencies in the prior art, the invention provides a kind of wet strong waste paper recycling chemical-mechanical pulping system, and then provides a kind of wet strong waste paper recycling chemical mechanical pulp-making method.
Technical scheme: for solving the problems of the technologies described above, wet strong waste paper recycling chemical-mechanical pulping system provided by the invention, by material operation traffic direction, this system comprises the first conveying equipment, Material disintegrator, the second conveying equipment, tumbler-type washing machine, inclined helix dehydrator, decatize storehouse, the 3rd conveying worm, the first double-screw impregnator, the first reaction warehouse, the 4th conveying worm, the second double-screw impregnator, the second reaction warehouse, the 5th conveying worm, latency chest, stock pump, defibrator, purification screening enrichment facility, storage sizing device;
The discharging opening of described first conveying equipment is just to the charging aperture of Material disintegrator, the discharging opening of described Material disintegrator is just to the charging aperture of the second conveying equipment, the discharging opening of described second conveying equipment is just to the charging aperture of tumbler-type washing machine, the discharging opening of described tumbler-type washing machine is communicated with the charging aperture of inclined helix dehydrator, the discharging opening of described inclined helix dehydrator is communicated with the charging aperture in decatize storehouse, the discharging opening in described decatize storehouse is communicated with the 3rd helical feed machine inlet capable, the discharging opening of described 3rd conveying worm is communicated with the charging aperture of the first double-screw impregnator, the discharging opening of described first double-screw impregnator is communicated with the charging aperture of the first reaction warehouse, the discharging opening of described first reaction warehouse is communicated with the charging aperture of the 4th conveying worm, the discharging opening of described 4th conveying worm is communicated with the charging aperture of the second double-screw impregnator, the discharging opening of described second double-screw impregnator is communicated with the charging aperture of the second reaction warehouse, the discharging opening of described second reaction warehouse is communicated with the charging aperture of the 5th conveying worm, the discharging opening of described 5th conveying worm is communicated to latency chest, described stock pump is located between latency chest and defibrator, the input of stock pump is communicated with the cavity volume of latency chest, slurry delivery side of pump is communicated with the charging aperture of defibrator, the charging aperture that enrichment facility is screened in discharging opening and the purification of described defibrator is communicated with, the discharging opening of described purification screening enrichment facility is connected with storage sizing device.
Preferably, native system also comprises tablet pump, the mode of communicating of the discharging opening of described tumbler-type washing machine and the charging aperture of inclined helix dehydrator is: below the discharging opening of tumbler-type washing machine, be provided with container, described tablet pump is located between this container and inclined helix dehydrator, the input of tablet pump is arranged in the cavity volume of this container, and tablet delivery side of pump is communicated with the charging aperture of inclined helix dehydrator.
Preferably, described Material disintegrator is shredder or hydrabrusher; Described first conveying equipment and the second conveying equipment are chain scraper conveyor or belt conveyor; Described purification screening enrichment facility comprises the pressurized screen, scummer and the concentrator that are linked in sequence, the discharging opening of described defibrator is communicated with the charging aperture of pressurized screen, the discharging opening of described pressurized screen is communicated with the charging aperture of scummer, the discharging opening of described scummer is communicated with the charging aperture of concentrator, and the discharging opening of described concentrator is connected with storage sizing device.
Preferably, described tumbler-type washing machine comprises body, rotary drum, rotary drum driving device; Described body one upper lateral part is provided with charging aperture, and its opposite side is provided with discharging opening, is provided with washing cavities in body, and described rotary drum is located in washing cavities also to drive by rotary drum driving device and is rotated; Organism bottom shape below described rotary drum position is inversed taper platform shape; One end of the contiguous charging aperture of described body is provided with water inlet, and the below of the lower frustum mouth of the inversed taper platform shape of described organism bottom is provided with the body be communicated with lower frustum mouth, and tube wall is provided with lower water inlet; The below of described body is provided with sediment pipe, and the upper end of described sediment pipe is provided with blow valve, and lower end is provided with lower blow valve.The tumbler-type washing machine of this structure is adopted to form up current by lower water inlet water inlet, the material effectively reducing proportion lighter precipitates downwards by the thrust of up current, the heavier heavy seeds of proportion such as metal object, stone etc. is only made to sink to sediment pipe, effectively can remove the heavy seeds in material, and greatly reduce material loss of easily causing in the process of washing removing impurities.
Preferably, described inclined helix dehydrator comprises spiral case, be provided with in spiral case and drive by driving device for slow-run the spiral rotated, the spiral of described spiral case and inside thereof is obliquely installed from low to high along mass transport direction, lower one end of described spiral case is the oblique lower end of shell, higher one end is the oblique upper end of shell, the top that described shell is positioned at the oblique lower end of shell is provided with charging aperture, the bottom being positioned at the oblique lower end of shell is provided with water discharge outlet, the bottom being positioned at the oblique upper end of shell is provided with discharging opening, the lower parallel being positioned at spiral in described spiral case is provided with sieve plate.
Decatize storehouse in native system can select conventional decatize storehouse, this area as oscillatory type discharging decatize storehouse.As a further improvement on the present invention, the decatize storehouse in native system preferably rotates material toggling formula decatize storehouse, described rotation material toggling formula decatize storehouse, and comprise warehouse, rotate poking device, discharge device, be provided with in warehouse and steam chamber, warehouse top is provided with charging aperture; Described rotation poking device comprises the material toggling dish be located at bottom warehouse, the material toggling sheet that described material toggling dish comprises chassis and can rotate on chassis; Described discharge device comprises housing and discharge motor, load displacing screw is provided with in housing, described load displacing screw comprises helical axis and is arranged on the helical blade on helical axis, and this helical axis is connected with the discharge motor-driven being located at housing side, and housing opposite side bottom is provided with discharging opening; Discharge device is positioned at below material toggling dish, and the position that the chassis of material toggling dish is docked with the housing of discharge device is provided with blanking opening.As a further improvement on the present invention, in this rotation material toggling formula decatize storehouse, rotate poking device and also comprise material toggling motor and central shaft, described center chassis is provided with through hole, described central shaft is fixedly connected with material toggling sheet through this through hole one end, and the other end is connected with material toggling motor-driven by shaft coupling; Described chassis is circular base plate, and described blanking opening is positioned on the eccentric position on chassis, and is positioned at the region, chassis of material toggling sheet revolving coverage method, for forming the blanking opening of four edges by with two sections of circular arcs of circular base plate concentric and two strings; Described steaming cavity wall is positioned at the uniform tread plate of top circumference of material toggling dish; Described warehouse is cylindrical or truncated cone-shaped; Be provided with steam inlet tube bottom described warehouse, described warehouse top is provided with opposing steam flow mouth and steam outlet; On the housing of described discharge device, the position of contiguous discharging opening is provided with steam outlet; Also comprise muffler, one end mouth of pipe of described muffler docks with the steam outlet of described discharge device, and the other end docks with the opposing steam flow mouth on described warehouse top; Described discharge motor is adjustable speed toothed gearing electric motor, and the helical axis of described load displacing screw is supported by bearing and bearing block, and two ends are provided with sealing and contain, and described helical blade is the variable-pitch auger blade changed from small to big gradually along helical axis throughput direction pitch.After material in warehouse reaches certain material level and meets sufficient stop steaming time, this rotation material toggling formula decatize storehouse is by rotating poking device, continuously pulping raw material layering is dialled in discharge device by first in first out by blanking opening, then measured by discharge device and send.Can eliminate on the one hand because of material be heated, compacting and volumetric expansion cause the arch formation that occurs in storehouse, improve capacity utilization rate; Another aspect material obtains sufficient decatize and softens, effectively can promote the removal efficiency of extruding chemical stain effect and water-soluble coloring matter and the resinous substances in advance in post-order process, reduce chemical cost, thus improve whiteness and the physical property of bleached chemi-mechanical pulp slurry; When material short interruption, can also, as a buffer container, guarantee to provide even, controlled material to system.While ensureing material decatizing effect, well maintain normal quantity-produced stability.Further, above-mentioned steam-return line design, can make full use of steam efficiency, while improving material decatize bating effect further, and energy-conserving and environment-protective.Further, material is in plug vertical drop in warehouse, and this rotation material toggling formula decatize storehouse effectively prevent the problem of material with poking device skidding rotation by tread plate.Further, helical blade on load displacing screw helical axis adopts varying pitch design, ensure that in the helical axis screw channel below blanking opening, material is full state on the one hand, material is made to be transitioned into loose condition (of surface) along helical axis throughput direction gradually by full state in course of conveying on the other hand, raise the efficiency, reduce spiral operating load and wearing and tearing, while realizing continuous metering discharging, improve the stability of system.
The first reaction warehouse wherein and the second reaction warehouse can select popular response storehouse, this area, as a further improvement on the present invention, and preferably even blanking type reaction warehouse.Described even blanking type reaction warehouse, comprise warehouse and even doffer, warehouse top is provided with charging aperture, is provided with blanking port bottom warehouse; Described even doffer, comprises housing, is provided with load displacing screw in housing, and housing one side lower part is provided with the discharging opening of reaction warehouse, and the charging aperture of this even doffer is the blanking port bottom reaction warehouse warehouse; Described load displacing screw comprises helical axis and is arranged on the helical blade on helical axis, and the described helical axis position be positioned at above discharging opening is fixed with even blanking ring, and described even blanking ring is consistent with the central axis of described helical axis; Described even blanking ring comprises body and multi start thread blade, described multi start thread blade is fixedly connected on the outer wall of body, described body retainer ring is around being socketed on helical axis, and the rotation direction of described multi start thread blade is consistent with the helical blade rotation direction on described load displacing screw.As a further improvement on the present invention, the warehouse of this even blanking type reaction warehouse is trapezoidal side storehouse; Described even doffer comprises the load displacing screw of more than two, and every root load displacing screw includes helical axis and helical blade, and described helical blade is the variable-pitch auger blade changed from small to big gradually along throughput direction pitch; The helical axis position be positioned at above discharging opening of every root load displacing screw is all fixed with even blanking ring, each even blanking ring is consistent with its corresponding helical axis central axis, and the multi start thread blade on each even blanking ring is consistent with the helical blade rotation direction on its corresponding load displacing screw; The load displacing screw of described more than two independently drives, and the helical axis of adjacent load displacing screw reversely rotates.This even blanking type reaction warehouse can realize even blanking by even blanking ring, be conducive to downstream pulping equipment steady production, fluctuation of load amplitude is reduced within 10 ~ 15% by more than original one times, reduces equipment failure rate, improve equipment dependability, stabilize stock quality.On this basis, reversely rotate by the load displacing screw of more than two further, make in two reverse rotations especially instead of material on contiguous load displacing screw under the common promotion of the helical blade rotated, more balanced passing forward, then the stirring through even blanking ring is broken up, and continuous uniform must fall to upstream device from discharging opening.On load displacing screw, the varying pitch design of helical blade can make material be transitioned into loose condition (of surface) along helical axis throughput direction gradually by full state in course of conveying, raises the efficiency, reduces spiral operating load and wearing and tearing.
Preferably, first, second double-screw impregnator in native system, described in the Chinese patent application of the application number as submitted on September 11st, 2012 is 201210332112.8, publication number is CN102864669A " a kind of double-screw impregnator " by name, its full content is incorporated herein by reference.Described in the Chinese patent application of " a kind of double-screw impregnator " by name that the grant number also can submitted to as on September 11st, 2012 is ZL201220458032.2, its full content is incorporated herein by reference.Above-mentioned double-screw impregnator comprises frame and is arranged on motor, speed-changing gear box, movable crown gear coupling, machine barrel and two screw rods in frame, described motor is connected with two screw drive by speed-changing gear box and movable crown gear coupling, described two screw rods are parallel to each other and be arranged in described machine barrel rotationally, described machine barrel one end is provided with charging aperture, and the other end is provided with discharging opening; Described screw rod is arranged with the first conveyor screw cover, the first extrusion spiral cover, the second conveyor screw cover, the second extrusion spiral cover, the 3rd conveyor screw cover and the 3rd extrusion spiral cover successively along throughput direction, the hand of spiral of described first, second, third conveyor screw cover is contrary with the hand of spiral that described first, second, third extrusion spiral overlaps, and the pitch of described first conveyor screw cover reduces gradually along throughput direction; Described machine barrel top is provided with to be overlapped corresponding liquid with the 3rd conveyor screw and adds hand-hole, and described machine barrel bottom is provided with waste liquid hole; The spiral shell rib of described first, second, third extrusion spiral cover has slot; Described machine barrel is upper and lower dissection type machine barrel, comprise symmetrical connect be fixedly installed on first machine barrel in frame and able to turn on or off second machine barrel be connected in frame.
The first reaction warehouse wherein and the second reaction warehouse also can form identical with above-mentioned decatize chamber structure, because through the material of double-screw impregnator extruding and kneading, its frictional heat temperature has met needed for reaction warehouse reaction, so when reaction warehouse uses the structure the same with decatize storehouse, Steam Heating can not be injected by steam pipe, certainly in case of need, also steam-heated mode can be selected.
For solving the problems of the technologies described above, one provided by the invention strong waste paper recycling chemical mechanical pulp-making method, it uses above-mentioned wet strong waste paper recycling chemical-mechanical pulping system, in the method, the percentage amounts of each dosage component is the percentage amounts accounting for over dry raw material weight, and this wet strong waste paper recycling chemical mechanical pulp-making method comprises:
1. material papering section:
After feedstock transportation to Material disintegrator is cracked into tablet, be delivered to tumbler-type washing machine add water adjustment concentration be 3 ~ 5% carry out washing, sediment removes the impurity be mingled in material, the material after washing and water are pumped to inclined helix dehydrator by tablet pump and remove residual impurity further and complete dehydration; Residual impurity and water are discharged by the screen cloth mesh of inclined helix dehydrator;
2. decatize workshop section:
Mass transport after the dehydration export material papering section is to decatize storehouse, and within the scope of the steam pressure of 0.3 ~ 0.6MPa, decatize makes material decatize soften for 15 ~ 30 minutes;
3. the first extrusion impregnating chemical mechanical processing section:
After the steaming export decatize workshop section, material is delivered in this section of double-screw impregnator to be extruded by conveying worm and rubs as silk bulk and be concentrated into 35 ~ 45% concentration, thereafter mix with the first chemical impregnation medicament height be metered into is dense in this section of double-screw impregnator, and the adjustment slurry that adds water is dense to 25 ~ 35%, realization homogenizes after chemical impregnation process and is expelled to reaction warehouse, in the temperature range of 80 ~ 95 DEG C, stop and react for 35 ~ 60 minutes;
4. the second extrusion impregnating chemical mechanical processing section:
By the slurry that the first extrusion impregnating chemical mechanical processing section reaction warehouse exports, to be delivered in this section of double-screw impregnator by further extruding and kneading by conveying worm and to be fibre bundle and single fiber mixture shape and to be concentrated into 35 ~ 45% concentration, thereafter mix with the second chemical impregnation medicament height be metered into is dense in this section of double-screw impregnator, and the adjustment slurry that adds water is dense to 25 ~ 35%, realization homogenizes after chemical impregnation process and is expelled to reaction warehouse, in the temperature range of 80 ~ 95 DEG C, stop and react for 35 ~ 60 minutes;
5. disappear and dive and the section of discongesting again:
By the slurry that the second extrusion impregnating chemical mechanical processing section reaction warehouse exports, being delivered in latency chest by conveying worm makes pelletizing shape fiber dispersion stretch elimination internal stress, the adjustment slurry that adds water is dense to 3 ~ 5%, adjustment slurry temperature range is 60 ~ 70 DEG C, thereafter be pumped to defibrator by stock pump to discongest again, isolate light, heavy seeds and thick waste material and wet-strength paper fiber;
6. purify, screen and enriching section:
To dive disappearing and the section of discongesting is separated the wet-strength paper fiber obtained again, being stored in after scummer purification, pressurized screen screening, concentrator are concentrated and storing in sizing device for copying.
Preferably, the sediment impurity obtained after tumbler-type washing machine washing in described 1. material papering section enters fixed-end forces system, the residual impurity of being discharged by the sieve plate mesh of inclined helix dehydrator and water enter water treatment system, are back to washing process through precipitation purification Posterior circle.
Preferably, according to the percentage by weight accounting for over dry raw material, in described 2. decatize workshop section, mass transport after dehydration is to the humectant again adding 0.1% ~ 0.15% during the decatize of decatize storehouse, described humectant again comprises the alcohol of linear or direct-connected ethoxylate or propoxylate, and defoamer is as siloxy group latex; In described 3. the first extrusion impregnating chemical mechanical processing section, the first chemical impregnation medicament is NaOH or Na of 1 ~ 2% 2cO 3, control in 11.5 ~ 12.5 scopes by the slurry pH value of alkali treatment; The second chemical impregnation medicament in described 4. the second extrusion impregnating chemical mechanical processing section is oxidant, controls in 11.5 ~ 12.5 scopes by the slurry pH value of oxidizer treatment; Described oxidant package is containing the NaOH of 1 ~ 3%, the H of 2 ~ 6% 2o 2, 1 ~ 2% Na 2siO 3with 0.2 ~ 0.5% chelating agent; Described chelating agent is any one of DTPA or EDTA.As further preferred, in described 2. decatize workshop section, the mass transport after dehydration is to the humectant again adding 0.1% during the decatize of decatize storehouse; In described 3. the first extrusion impregnating chemical mechanical processing section, the first chemical impregnation medicament is the NaOH of 1%; The second chemical impregnation pharmacy kit in described 4. the second extrusion impregnating chemical mechanical processing section is containing the NaOH of 1%, the H of 2% 2o 2, 1% Na 2siO 3with 0.2% DTPA.
As another kind of preferred version, according to the percentage by weight accounting for over dry raw material, in described 2. decatize workshop section, the mass transport after dehydration is to the humectant again adding 0.1% ~ 0.15% during the decatize of decatize storehouse; The first chemical impregnation medicament in described 3. the first extrusion impregnating chemical mechanical processing section is the H of 1 ~ 1.5% 2sO 4or the alum of 3 ~ 6%, control in 4.5 ~ 6 scopes by acid-treated slurry pH value; The second chemical impregnation medicament in described 4. the second extrusion impregnating chemical mechanical processing section is oxidant, controls in 11.5 ~ 12.5 scopes by the slurry pH value of oxidizer treatment; Described oxidant package is containing the NaOH of 1 ~ 3%, the H of 2 ~ 6% 2o 2, 1 ~ 2% Na 2siO 3with 0.2 ~ 0.5% chelating agent; Described chelating agent is any one of DTPA or EDTA.Further preferred as another kind of preferred version, in described 2. decatize workshop section, the mass transport after dehydration is to the humectant again adding 0.12% during the decatize of decatize storehouse; The first chemical impregnation medicament in described 3. the first extrusion impregnating chemical mechanical processing section is the H of 1.2% 2sO 4; The second chemical impregnation pharmacy kit in described 4. the second extrusion impregnating chemical mechanical processing section is containing the NaOH of 2%, the H of 4% 2o 2, 1.5% Na 2siO 3with 0.35% DTPA.Another kind as another kind of preferred version is further preferred, and in described 2. decatize workshop section, the mass transport after dehydration is to the humectant again adding 0.15% during the decatize of decatize storehouse; The first chemical impregnation medicament in described 3. the first extrusion impregnating chemical mechanical processing section is the H of 1.5% 2sO 4; The second chemical impregnation pharmacy kit in described 4. the second extrusion impregnating chemical mechanical processing section is containing the NaOH of 3%, the H of 6% 2o 2, 2% Na 2siO 3with 0.5% EDTA.
Beneficial effect: in chemical-mechanical pulping system provided by the invention and pulping process, adopt Material disintegrator, by mechanical shear, waste paper is cut into the scraps of paper, then double-screw impregnator is utilized to dissociate and Chemical Pretreatment equipment as fibre machinery, by the mechanical kneading action of double-screw impregnator screw rod, progressively to diminish and substep dissociates while fiber gradually in wet strong waste paper sheet appearance and size, carry out chemical treatment, realize chemical assistant and the height of slurry dense mix and homogenize flood, improve chemical reaction efficiency, reduce chemical cost 20 ~ 30%.
Further, chemical-mechanical pulping system provided by the invention, tumbler-type washing machine can be adopted to pass through the water inlet of lower water inlet and to form up current, the material that effective minimizing proportion is lighter precipitates downwards, the heavier heavy seeds of proportion such as metal object, stone etc. is only made to sink to sediment pipe, effectively can remove the heavy seeds in material, and greatly reduce material loss of easily causing in the process of washing removing impurities.
Further, chemical-mechanical pulping system provided by the invention, even blanking type reaction warehouse can be adopted to realize even blanking by even blanking ring, be conducive to downstream pulping equipment steady production, fluctuation of load amplitude is reduced within 10 ~ 15% by more than original one times, reduce equipment failure rate, improve equipment dependability, stabilize stock quality;
Further, chemical-mechanical pulping system provided by the invention, can adopt and rotate material toggling formula decatize storehouse material continuous stratification is dialled in discharge device by rotating poking device, prevent from material from skidding by tread plate to rotate, eliminate because material is heated the arch formation that volumetric expansion causes, improve capacity utilization rate, material obtains sufficient decatize and softens, effectively improve the removal efficiency of postorder chemistry extrusion impregnating effect and water-soluble coloured and resinous substances, reduce chemical cost.
Further, in chemical mechanical pulp-making method provided by the invention, can in the extrusion impregnating chemical mechanical processing section of two sections of series connection, first controlling pH value scope to wet strong waste paper through peracid treatment is 4.5 ~ 6, controlling pH value scope to wet strong waste paper through oxidizer treatment is again 11.5 ~ 12.5, avoid the pH value scope that in wet strong waste paper, wet strength agent character is the most stable, and pass through the method for two pH value process, first the wet strength agent in waste paper is oxidized in acid condition, then further facilitation of hydrolysis in the basic conditions, intermolecular and the chemical bond between wet strength agent and paper pulp fiber of more effective destruction wet strength agent, obtain wet-strength paper the fiber 96% even high dissociation yield of more than 98% or dissociate completely, effectively improve fiber dissociation yield and pulping yield again.
Generally speaking, under chemical-mechanical pulping system provided by the invention and pulping process rely on mechanical forceful action and chemical treatment to act on low (electricity) energy consumption, do not reduce while former pulp strength even increases, realize wet strong waste paper fibre and to dissociate slurrying again; Adopt environment-friendly type oxidant in slurry concentration 25 ~ 35% times slurrying again, reduce ton pulp-water consumption, using water wisely, realizes pollution-free environment-friendly pulping; And can for different wet strong waste paper characteristics, adopt different oxidants, different process conditions, intermolecular and the chemical bond between wet strength agent and paper pulp fiber of more effective destruction wet strength agent, the slurrying again realized containing all kinds of wet-strength papers of bleach chemical pulp, chemi-mechanical pulp or brown stock is recycled.Entirety solves wet strong waste paper and reclaims the problem that the pulping fibre rate of dissociation is low, pulp strength declines to a great extent, and can realize continuously, scale, low water consumption, low energy consumption pollution-free environment-friendly pulping.
Accompanying drawing explanation
Fig. 1 is the overall structure schematic diagram of wet strong waste paper recycling chemical-mechanical pulping system;
Fig. 2 is the structural representation of tumbler-type washing machine;
Fig. 3 is the left view of Fig. 2;
Fig. 4 is the structural representation of inclined helix dehydrator;
Fig. 5 is the structural representation rotating material toggling formula decatize storehouse;
Fig. 6 is the top view of Fig. 5;
Fig. 7 is the left view of Fig. 5;
Fig. 8 is the structural representation of even blanking type reaction warehouse;
Fig. 9 is the structural representation of even blanking ring in even blanking type reaction warehouse;
Figure 10 is the structural representation that even doffer in even blanking type reaction warehouse configures two load displacing screws.
Detailed description of the invention
Below in conjunction with the embodiment of accompanying drawing, system and the embodiment of method, the present invention is further described.
As shown in Figure 1, this wet strong waste paper recycling chemical-mechanical pulping system, by material operation traffic direction, comprise the first conveying equipment 1, Material disintegrator 2, second conveying equipment 3, tumbler-type washing machine 4, tablet pump 5, inclined helix dehydrator 6, decatize storehouse 7, the 3rd conveying worm 8, first double-screw impregnator 9, first reaction warehouse 10, the 4th conveying worm 11, second double-screw impregnator 12, second reaction warehouse 13, the 5th conveying worm 14, latency chest 15, stock pump 16, defibrator 17, purification screening enrichment facility 18, storage sizing device 19;
The discharging opening of described first conveying equipment 1 is just to the charging aperture of Material disintegrator 2, the discharging opening of described Material disintegrator 2 is just to the charging aperture of the second conveying equipment 3, the discharging opening of described second conveying equipment 3 is just to the charging aperture of tumbler-type washing machine 4, container (not shown) is provided with below the discharging opening of described tumbler-type washing machine 4, described tablet pump 5 is located between this container and inclined helix dehydrator 6, the input of tablet pump 5 is arranged in the cavity volume of this container, the output of tablet pump 5 is communicated with the charging aperture of inclined helix dehydrator 6, the discharging opening of described inclined helix dehydrator 6 is communicated with the charging aperture in decatize storehouse 7, the discharging opening in described decatize storehouse 7 is communicated with the 3rd conveying worm 8 charging aperture, the discharging opening of described 3rd conveying worm 8 is communicated with the charging aperture of the first double-screw impregnator 9, the discharging opening of described first double-screw impregnator 9 is communicated with the charging aperture of the first reaction warehouse 10, the discharging opening of described first reaction warehouse 10 is communicated with the charging aperture of the 4th conveying worm 11, the discharging opening of described 4th conveying worm 11 is communicated with the charging aperture of the second double-screw impregnator 12, the discharging opening of described second double-screw impregnator 12 is communicated with the charging aperture of the second reaction warehouse 13, the discharging opening of described second reaction warehouse 13 is communicated with the charging aperture of the 5th conveying worm 14, the discharging opening of described 5th conveying worm 14 is communicated to latency chest 15, described stock pump 16 is located between latency chest 15 and defibrator 17, the input of stock pump 16 is communicated with the cavity volume of latency chest 15, the output of stock pump 16 is communicated with the charging aperture of defibrator 17, the charging aperture that enrichment facility 18 is screened in discharging opening and the purification of described defibrator 17 is communicated with, the discharging opening of described purification screening enrichment facility 18 is connected with storage sizing device 19.In described storage sizing device 19, storage slurry is standby copies.Concrete, described purification screening enrichment facility 18 can comprise the pressurized screen 20, scummer 21 and the concentrator 22 that are linked in sequence, the discharging opening of described defibrator 17 is communicated with the charging aperture of pressurized screen 20, the discharging opening of described pressurized screen 20 is communicated with the charging aperture of scummer 21, the discharging opening of described scummer 21 is communicated with the charging aperture of concentrator 22, and the discharging opening of described concentrator 22 is connected with storage sizing device 19.
Material disintegrator 2 is wherein shredder or hydrabrusher, and the first conveying equipment 1 and the second conveying equipment 3 are chain scraper conveyor or belt conveyor.The crushing mechanism structure of described shredder is made up of the rotor of the stationary knife be fixed on casing counter-rotating relative to two, after material enters shredder, the shearing pair relying on the some cutterheads between two rotors and form between cutterhead and stationary knife, material cutting is broken into the tablet of certain size, rotor is that the axle of spline or hexagon section and the cutterhead on axle in tandem are formed by centre, can by adjustment cutterhead thickness adjust shear after the size of material; Shredder can configure hilted broadsword roll structure as required, also can adopt double knife roller or multitool roll structure.
Tumbler-type washing machine 4 wherein can select this area conventional rotary drum formula rinsing maching, provides a kind of specific implementation form herein, and as shown in Figures 2 and 3, this tumbler-type washing machine comprises body, rotary drum 402, rotary drum driving device 404; Described body one upper lateral part is provided with charging aperture 401, and its opposite side is provided with discharging opening 403, is provided with washing cavities in body, and described rotary drum 402 is located in washing cavities also to drive by rotary drum driving device 404 and is rotated; Organism bottom shape below described rotary drum 402 position is inversed taper platform shape; One end of the contiguous charging aperture 401 of described body is provided with water inlet 406, and the below of the lower frustum mouth of the inversed taper platform shape of described organism bottom is provided with the body be communicated with lower frustum mouth, and tube wall is provided with lower water inlet 407; The below of described body is provided with sediment pipe 405, and the upper end of described sediment pipe 405 is provided with blow valve 408, and lower end is provided with lower blow valve 409.During work, the material cracking into tablet through Material disintegrator enters the charging aperture 401 of tumbler-type washing machine, washings are added by upper water inlet 406 and lower water inlet 407, rotary drum 402 is driven by rotary drum driving device 404 and continuous slow circumvolve, after tablet enters scrubbing section, to wash rear tablet continuously by the rotation of rotary drum 402 to be transferred to by discharging opening 403, heavy seeds such as metal object, stone etc. sink to sediment pipe 405; During normal work, upper blow valve 408 is opened, lower blow valve 409 cuts out, be beneficial to slag charge and be precipitated into sediment pipe 405, when needs deslagging, upper blow valve 408 cuts out, lower blow valve 409 is opened, discharge sediment, then go up blow valve 408 and again open, lower blow valve 409 cuts out again, upper and lower blow valve alternately cuts out and opens and realizes sediment, and sediment enters fixed-end forces system after discharging.In the structure shown here, because the water inlet of lower water inlet 407 can form up current, the material that the thrust of up current can effectively reduce proportion lighter precipitates downwards, but heavier heavy seeds such as metal object, the stone etc. of proportion still can sink to sediment pipe, effectively can remove the heavy seeds in material, and greatly reduce material loss of easily causing in the process of washing removing impurities.
Inclined helix dehydrator 6 wherein can select the conventional inclined helix dehydrator in this area, provide a kind of specific implementation form herein, as shown in Figure 4, this inclined helix dehydrator comprises spiral case 602, be provided with in spiral case 602 and drive by driving device for slow-run 604 spiral 603 rotated, the spiral 603 of described spiral case 602 and inside thereof is obliquely installed from low to high along mass transport direction, the two ends of described spiral case 602 are respectively the oblique lower end of shell and the oblique upper end of shell, the top that described shell is positioned at the oblique lower end of shell is provided with charging aperture 601, the bottom being positioned at the oblique lower end of shell is provided with water discharge outlet 607, the bottom being positioned at the oblique upper end of shell is provided with discharging opening 605, the lower parallel being positioned at spiral 603 in described spiral case 602 is provided with sieve plate 606.During work, the material after tumbler-type washing machine washing and water are pumped to the charging aperture 601 of inclined helix dehydrator by tablet pump, and spiral 603 drives rotation by drive unit 604, and material is delivered to discharging opening 605 by spiral 603 lifting and discharges.Washings and residual impurity are discharged by the mesh of sieve plate 606 and are entered water treatment system through water discharge outlet 607, are back to washing process through precipitation purification Posterior circle.
Decatize storehouse 7 wherein can select conventional decatize storehouse, this area as oscillatory type discharging decatize storehouse, preferably rotates material toggling formula decatize storehouse.As shown in Fig. 5, Fig. 6, Fig. 7, described rotation material toggling formula decatize storehouse comprises warehouse 702, rotates poking device, discharge device, and be provided with in warehouse 702 and steam chamber, warehouse 702 top is provided with charging aperture 701; The material toggling dish that this rotation poking device comprises material toggling motor 712, central shaft 713 and is located at bottom warehouse, the material toggling sheet 715 that described material toggling dish comprises chassis 714 and can rotate on chassis; Center, chassis 714 is provided with through hole; Central shaft 713 is fixedly connected with material toggling sheet 715 through this through hole one end, and the other end is in transmission connection by shaft coupling and material toggling motor 712; This discharge device comprises housing 703 and discharge motor 704, and this discharge motor 704 is adjustable speed toothed gearing electric motor, is provided with load displacing screw in housing 703, the helical blade 706 that load displacing screw comprises helical axis 705 and is arranged on helical axis; The helical axis 705 of described load displacing screw is by the clutch shaft bearing seat 707 and the second bearing block 708 and the bearings that are located at both sides, two ends are respectively equipped with the first sealing culvert 709 and the second sealing culvert 710, this helical axis 705 is in transmission connection with the discharge motor 704 being located at housing side, housing 703 opposite side bottom is provided with discharging opening 711, and the helical blade 706 that described helical axis is provided with is the variable-pitch auger blade changed from small to big gradually along throughput direction pitch; This discharge device is positioned at below material toggling dish, the position that the chassis 714 of material toggling dish is docked with the housing 703 of discharge device is provided with blanking opening 716, this blanking opening 716 is positioned on the eccentric position on chassis 714, and is positioned at the region on the chassis 714 of material toggling sheet 715 revolving coverage method; The chassis 714 of above-mentioned material toggling dish is circular base plate, the housing 703 of discharge device is cylindrical shape, the limit of this blanking opening 716 is the butted line of circular base plate and discharge device housing, namely for forming the blanking opening of four edges by with two sections of circular arcs of circular base plate concentric and two strings; Described steaming cavity wall is positioned at the uniform some vertical bar shape tread plates 726 of top circumference of material toggling dish; Warehouse 702 is truncated cone-shaped, can certainly be cylindrical; Observation panel 718 is provided with in the middle part of warehouse; Bottom warehouse 702, uniform 4 steam inlet tubes of circumference, are respectively the first steam inlet tube 719, second steam inlet tube 720, the 3rd steam inlet tube 721, the 4th steam inlet tube 722; Described warehouse 702 top is provided with opposing steam flow mouth and steam outlet 723; On described discharge device housing 703, the position of contiguous discharging opening 711 is provided with steam outlet 724; This decatize storehouse also comprises muffler 725, and one end mouth of pipe of described muffler 725 docks with the steam outlet 724 of described discharge device, and the other end docks with the opposing steam flow mouth on described warehouse 702 top.During work, the material after inclined helix dehydrator dehydration is fallen into warehouse 702 from charging aperture 701 and steams in chamber.Steam enters steam inlet tube respectively by external steam pipeline, and then enters bottom steaming chamber, and a part is upwards evaporated decatize and softened material, and excess steam exports from steam outlet 723; Another part enters discharge device through blanking opening 716 downwards, then export from the steam outlet 724 of discharge device, being back to warehouse by the opposing steam flow mouth of muffler 725 through described warehouse top steams in chamber, affect by material nature angle of rest (repose), warehouse steams top, chamber in nothing material state, steam can be made to be back to decatize in steaming chamber smoothly and soften material, excess steam is recycled through steam outlet 723 or is discharged; After material in decatize storehouse warehouse 702 reaches certain material level and meets sufficient stop steaming time, start and rotate the material toggling motor 712 of poking device and the discharge motor 704 of discharge device, material toggling motor 712 drives material toggling sheet 715 to rotate by central shaft 713, and discharge motor 704 drives helical axis 705 to rotate; Because load displacing screw adopts adjustable speed toothed gearing electric motor to drive, reach metering conveying object by pre-setting load displacing screw rotating speed herein; In material toggling sheet 715 rotary course, continuously material layering is dialled in discharge device by first in first out by blanking opening 716, material is in plug vertical drop in the steaming chamber of warehouse 702, and tread plate 726 effectively prevents from material from skidding with poking device rotating; The screw channel material being now positioned at the helical axis 705 below blanking opening 716 is full state, in course of conveying, material is transitioned into loose condition (of surface) along helical axis throughput direction gradually by full state, and finally sent by the load displacing screw metering of discharge device, enter upstream device.
Double-screw impregnator wherein, described in the Chinese patent application of the application number as submitted on September 11st, 2012 is 201210332112.8, publication number is CN102864669A " a kind of double-screw impregnator " by name, it is incorporated herein by reference that its full content comprises accompanying drawing.Described in the Chinese patent application of " a kind of double-screw impregnator " by name that the grant number also can submitted to as on September 11st, 2012 is ZL201220458032.2, it is incorporated herein by reference that its full content comprises accompanying drawing.This double-screw impregnator comprises frame and is arranged on motor, speed-changing gear box, movable crown gear coupling, machine barrel and two screw rods in frame, described motor is connected with two screw drive by speed-changing gear box and movable crown gear coupling, described two screw rods are parallel to each other and be arranged in described machine barrel rotationally, described machine barrel one end is provided with charging aperture, and the other end is provided with discharging opening; Described screw rod is arranged with the first conveyor screw cover, the first extrusion spiral cover, the second conveyor screw cover, the second extrusion spiral cover, the 3rd conveyor screw cover and the 3rd extrusion spiral cover successively along throughput direction, the hand of spiral of described first, second, third conveyor screw cover is contrary with the hand of spiral that described first, second, third extrusion spiral overlaps, and the pitch of described first conveyor screw cover reduces gradually along throughput direction; Homogenizing ring is provided with between each conveyor screw cover and extrusion spiral overlap; Described machine barrel top is provided with to be overlapped corresponding liquid with the 3rd conveyor screw and adds hand-hole, and described machine barrel bottom is provided with waste liquid hole corresponding to the output that overlaps with first, second conveyor screw, and waste liquid hole place is provided with filtration castor, i.e. draining filter screen; The spiral shell rib of described first, second, third extrusion spiral cover has slot; Described machine barrel is upper and lower dissection type machine barrel, comprise symmetrical connect be fixedly installed on first machine barrel in frame and able to turn on or off second machine barrel be connected in frame.During work, material is advanced to discharging opening direction by two screw rods, and because the pitch of the first conveyor screw cover reduces gradually in course of conveying, material is gradually compressed and is full of screw channel; Be the first homogenizing ring place before entering reverse crush zone extrusion spiral cover, extruding force reaches maximum, and material is by strong compression; Under the effect of forward extrusion power, material is forced through the slot on the first extrusion spiral cover spiral shell rib, the material physical dimension of be squeezed, crumpling diminishes and by conquassation, equally after the second conveyor screw cover and the second extrusion spiral cover extrude homogenizing again, material have passed two sections of extruding and kneading sections successively and is rubbed and is dissociated into a bulk, bundle fiber shape and single fiber shape; Meanwhile, material contained humidity and the hydrotrope are extruded and are discharged by machine barrel filter castor and filtrate drain drilling and collected and enter water treatment system; Before the forward discharging end materials of the second extrusion spiral cover enters mixing section, hand-hole is added and medicine feeding hole is metered into chemical impregnation medicament and dilution water by metering chemical feeding device by machine barrel liquid, realize medicament to mix with the height of fiber is dense, adjustment slurry is dense to 25 ~ 35%, then discharges after the high dense mixing of the 3rd extrusion spiral cover.
The first reaction warehouse 10 wherein and the second reaction warehouse 13 can select popular response storehouse, this area, preferably even blanking type reaction warehouse.As shown in Figure 8, described even blanking type reaction warehouse comprises warehouse 1010 and even doffer, and warehouse 1010 is trapezoidal side storehouse, and warehouse top is provided with the charging aperture 1020 of reaction warehouse, is provided with blanking port bottom warehouse 1010; This even doffer comprises housing, is provided with load displacing screw in housing, the helical blade 1050 that described load displacing screw comprises helical axis 1040 and is arranged on helical axis; The helical axis 1040 of this load displacing screw is connected with the motor-driven being located at housing side, and housing opposite side bottom is provided with the discharging opening 1030 of reaction warehouse, this blanking port evenly bottom the charging aperture of doffer and warehouse 1010; Described helical axis 1040 position be positioned at above discharging opening 1030 is fixed with even blanking ring 1060; The structural representation of even blanking ring 1060 as shown in Figure 9, comprises body 1061, and the outer wall of body 1061 is fixedly connected with multi start thread blade 1062; The body 1061 of described even blanking ring is connected on described helical axis 1040 by welding or bolted, and even blanking ring 1060 is consistent with the central axis of helical axis 1040; The rotation direction of described multi start thread blade 1062 is consistent with helical blade 1050 rotation direction on described load displacing screw.Also the load displacing screw of two such drive can be comprised in the even doffer of certain this reaction warehouse, as shown in Figure 10, every root load displacing screw includes helical axis and helical blade, and described helical blade is the variable-pitch auger blade changed from small to big gradually along throughput direction pitch; The helical axis position be positioned at above discharging opening of every root load displacing screw is all fixed with even blanking ring, each even blanking ring is consistent with its corresponding helical axis central axis, and the multi start thread blade on each even blanking ring is consistent with the helical blade rotation direction on its corresponding load displacing screw; The helical axis of these two load displacing screws reversely rotates.In this configuration, to under the common promotion of the helical blade rotated in two reverse rotations of material on contiguous load displacing screw are especially anti-, more balanced passing forward, the stirring then through even blanking ring is broken up, and continuous uniform must fall to upstream device from discharging opening; On load displacing screw, the varying pitch design of helical blade can make material be transitioned into loose condition (of surface) along helical axis throughput direction gradually by full state in course of conveying, raises the efficiency, reduces spiral operating load and wearing and tearing.During work, slurry is sent in reaction warehouse warehouse 1010 continuously by the reaction warehouse feeding mouth 1020 at top, conveying equipment autoreaction storehouse, upstream, after meeting the requirement of the technological design time of staying, in warehouse, material fullness rate is 70 ~ 80%, now load displacing screw fill material is in being full of compaction state, in being full of block bulk in the helicla flute of slurry between load displacing screw helical blade 1050; When being positioned at the load displacing screw bottom reaction warehouse and starting and rotate, in helicla flute, transferred to load displacing screw one end close to discharging opening 1030 continuously in the material being full of block bulk; Slurry first passes through even blanking ring 1060 close to load displacing screw tail end before whereabouts, and after the multi start thread blade 1062 on even blanking ring 1060 stirs and breaks up, continuous uniform falls to upstream device.
The first reaction warehouse 10 wherein and the second reaction warehouse 13 also can form identical with above-mentioned decatize storehouse 7 structure, because through the material of double-screw impregnator extruding and kneading, its frictional heat temperature has met needed for reaction warehouse reaction, so when reaction warehouse uses the structure the same with decatize storehouse, Steam Heating can not be injected by steam pipe, certainly in case of need, also steam-heated mode can be selected.
Use the wet strong waste paper recycling chemical mechanical pulp-making method of above-mentioned wet strong waste paper recycling chemical-mechanical pulping system, in the method, the percentage amounts of each dosage component is the percentage amounts accounting for over dry raw material weight, and its detailed description of the invention is:
Embodiment 1: bleaching containing the paper machine of wet strength agent manufacture paper with pulp broken and leftover pieces again slurrying reclaim
Broken and leftover pieces are delivered to after hydrabrusher size degradation becomes the scraps of paper by chain and pan conveyor, be delivered to tumbler-type washing machine 4 add water adjustment concentration be 3% carry out washing remove the gred after, being pumped to inclined helix dehydrator 6 by tablet pump 5 dewaters concentrated, then decatize storehouse 7 decatize 15 minutes are delivered to, steam pressure 0.3MPa, according to the percentage by weight accounting for over dry raw material, when entering decatize storehouse charging aperture with vaporific spray into 0.1% humectant again, after steaming, tablet is sent into the first double-screw impregnator 9 by the 3rd conveying worm 8 and is extruded and crumple into a bulk and about being concentrated into 35% concentration, thereafter according to the percentage by weight accounting for over dry raw material, liquid NaOH and the proper amount of clear water of 1% is added by measuring pump, material and chemical impregnation medicament are in the first double-screw impregnator 9 machine after high dense mixing, adjustment slurry dense to about 25%, pH value controls to send into the first reaction warehouse 10 about 11.5, reaction temperature controls at about 80 DEG C, 35 minutes time of staying, deliver to the second double-screw impregnator 12 by the 4th conveying worm 11 after reaction terminates to extrude rubbing and be dissociated into bundle fiber and single fiber mixture shape and about being concentrated into 35% concentration, thereafter according to the percentage by weight accounting for over dry raw material, the NaOH of 1% is added by measuring pump, the H2O2 of 2%, the Na2SiO3 of 1%, the chelating agent DTPA of 0.2% and proper amount of clear water, material and chemical impregnation medicament are in the second double-screw impregnator 12 machine after high dense mixing, adjustment slurry is dense to about 25%, pH value controls to send into the second high dense reaction warehouse 13 about 11.5, reaction temperature controls at about 80 DEG C, 35 minutes time of staying, latency chest 15 is delivered to by the 5th conveying worm 14 after reaction terminates.Slurry is in latency chest 15, thin up slurry is dense to 3%, temperature 60 C, eliminates the internal stress that fiber produces in extruding and kneading process, makes pelletizing shape fiber dispersion and fully trails, then, being pumped to defibrator 17 by stock pump 16 to discongest again, and being separated and removing light, heavy seeds and thick waste material and wet-strength paper fiber, screening being separated the wet-strength paper fiber obtained through pressurized screen 20, scummer 21 purifies, and is stored in standby in storage sizing device 19 copying after concentrator 22 is concentrated.
In said process, the sediment obtained after tumbler-type washing machine washing enters fixed-end forces system, and the residual impurity of being discharged by the sieve plate mesh of inclined helix dehydrator and water enter water treatment system, is back to washing process through precipitation purification Posterior circle.In the present embodiment, according to the cleanliness factor of broken and leftover pieces, also washing step can be omitted.
Embodiment 2: the paper machine do not bleached containing wet strength agent manufacture paper with pulp broken and leftover pieces again slurrying reclaim
Broken is delivered to hydrabrusher size degradation with leftover pieces by chain and pan conveyor and becomes the scraps of paper, be delivered to tumbler-type washing machine 4 add water adjustment concentration be 4% carry out washing remove the gred after, being pumped to inclined helix dehydrator 6 by tablet pump 5 dewaters concentrated, then decatize storehouse 7 decatize 25 minutes are delivered to, steam pressure 0.45MPa, according to the percentage by weight accounting for over dry raw material, when being delivered to decatize storehouse charging aperture with vaporific spray into 0.12% humectant again; After steaming, tablet is sent into the first double-screw impregnator 9 by the 3rd conveying worm 8 and is extruded and crumple into a bulk and about being concentrated into 40% concentration, thereafter according to the percentage by weight accounting for over dry raw material, added the H of 1.2% by measuring pump 2sO 4and proper amount of clear water, material and chemical impregnation medicament in the first double-screw impregnator 9 machine after high dense mixing, adjustment slurry dense to about 30%, pH value controls to send into the first reaction warehouse 10 about 6, reaction temperature controls at about 90 DEG C, 45 minutes time of staying; Deliver to the second double-screw impregnator 12 by the 4th conveying worm 11 after reaction terminates to extrude rubbing and be dissociated into bundle fiber and single fiber mixture shape and about being concentrated into 40% concentration, thereafter according to the percentage by weight accounting for over dry raw material, the NaOH of 2%, the H of 4% is added by measuring pump 2o 2, 1.5% Na 2siO 3with 0.35% DTPA and proper amount of clear water, material and chemical impregnation medicament are in the second double-screw impregnator 12 machine after high dense mixing, adjustment slurry dense to about 30%, pH value controls to send into the second high dense reaction warehouses 13 about 12, reaction temperature controls at about 90 DEG C, 45 minutes time of staying; Latency chest 15 is delivered to by the 5th conveying worm 14 after reaction terminates.Slurry is in latency chest 15, thin up slurry is dense to 4%, temperature 65 DEG C, eliminates the internal stress that fiber produces in extruding and kneading process, makes pelletizing shape fiber dispersion and fully trails, then, being pumped to defibrator 17 by stock pump 16 to discongest again, and being separated and removing light, heavy seeds and thick waste material and wet-strength paper fiber, screening being separated the wet-strength paper fiber obtained through pressurized screen 20, scummer 21 purifies, and is stored in standby in storage sizing device 19 copying after concentrator 22 is concentrated.
In said process, the sediment obtained after tumbler-type washing machine washing enters fixed-end forces system, and the residual impurity of being discharged by the sieve plate mesh of inclined helix dehydrator and water enter water treatment system, is back to washing process through precipitation purification Posterior circle.In the present embodiment, according to the cleanliness factor of broken and leftover pieces, also washing step can be omitted.
Embodiment 3: do not bleach the waste paper containing wet strength agent and the slurrying recovery again of waste paper boxboard
Waste paper is delivered to shredder size degradation with waste paper boxboard by chain and pan conveyor and becomes the scraps of paper, be delivered to tumbler-type washing machine 4 add water adjustment concentration be 5% carry out washing remove the gred after, being pumped to inclined helix dehydrator 6 by tablet pump 5 dewaters concentrated, then decatize storehouse 7 decatize 30 minutes are delivered to, steam pressure 0.6MPa, according to the percentage by weight accounting for over dry raw material, when being delivered to decatize storehouse charging aperture with vaporific spray into 0.15% humectant again; After steaming, tablet is sent into the first double-screw impregnator 9 by the 3rd conveying worm 8 and is extruded and crumple into a bulk and about being concentrated into 45% concentration, thereafter according to the percentage by weight accounting for over dry raw material, added the H of 1.5% by measuring pump 2sO 4and proper amount of clear water, material and chemical impregnation medicament in the first double-screw impregnator 9 machine after high dense mixing, adjustment slurry dense to about 35%, pH value controls to send into the first reaction warehouse 10 about 4.5, reaction temperature controls at about 95 DEG C, 60 minutes time of staying; Deliver to the second double-screw impregnator 12 by the 4th conveying worm 11 after reaction terminates to extrude rubbing and be dissociated into bundle fiber and single fiber mixture shape and about being concentrated into 45% concentration, thereafter according to the percentage by weight accounting for over dry raw material, the NaOH of 3%, the H of 6% is added by measuring pump 2o 2, 2% Na 2siO 3with 0.5% EDTA and proper amount of clear water, material and chemical impregnation medicament are in the second double-screw impregnator 12 machine after high dense mixing, adjustment slurry dense to about 35%, pH value controls to send into the second high dense reaction warehouses 13 about 12.5, reaction temperature controls at about 95 DEG C, 60 minutes time of staying; Latency chest 15 is delivered to by the 5th conveying worm 14 after reaction terminates.Slurry is in latency chest 15, thin up slurry is dense to 5%, temperature 70 C, eliminates the internal stress that fiber produces in extruding and kneading process, makes pelletizing shape fiber dispersion and fully trails, then, being pumped to defibrator 17 by stock pump 16 to discongest again, and being separated and removing light, heavy seeds and thick waste material and wet-strength paper fiber, screening being separated the wet-strength paper fiber obtained through pressurized screen 20, scummer 21 purifies, and is stored in standby in storage sizing device 19 copying after concentrator 22 is concentrated.
In said process, the sediment obtained after tumbler-type washing machine washing enters fixed-end forces system, and the residual impurity of being discharged by the sieve plate mesh of inclined helix dehydrator and water enter water treatment system, is back to washing process through precipitation purification Posterior circle.
Embodiment 3 is preferred embodiment, the raw material of equal PAE accounting 1.0% is carried out respectively to the experiment under above-described embodiment process conditions and step, result shows, and is not reducing while former pulp strength even increases, and all achieves wet strong waste paper fibre and to dissociate slurrying again; Wherein embodiment 1 reduces chemical cost 20%, and fluctuation of load amplitude is reduced within 15%, and the fiber dissociation yield of acquisition is up to 85%.Embodiment 2 reduces chemical cost 25%, and fluctuation of load amplitude is reduced within 12%, and the fiber dissociation yield of acquisition is up to 96%.Embodiment 3 reduces chemical cost 30%, and fluctuation of load amplitude is reduced within 12%, and the fiber dissociation yield of acquisition is up to 98%.
Above embodiment does not form restriction to the present invention, and relevant staff is in the scope not departing from the technology of the present invention thought, and the various change carried out and amendment, all drop in protection scope of the present invention.

Claims (8)

1. the two pH value chemical mechanical pulp-making method of wet strong waste paper recycling, is characterized in that the method comprises:
1. material papering section: after feedstock transportation to Material disintegrator is cracked into tablet, be delivered to tumbler-type washing machine add water adjustment concentration be 3 ~ 5% carry out washing, sediment, decontamination, the material after washing and water are delivered to inclined helix dehydrator and dewater;
2. decatize workshop section: the mass transport after the dehydration export material papering section is to decatize storehouse, and decatize makes material decatize soften for 15 ~ 30 minutes within the scope of the steam pressure of 0.3 ~ 0.6MPa;
3. the first extrusion impregnating chemical mechanical processing section: after the steaming export decatize workshop section, material is delivered in this section of double-screw impregnator to be extruded by conveying worm and rubs as silk bulk and be concentrated into 35 ~ 45% concentration, thereafter mix with the first chemical impregnation medicament height be metered into is dense in this section of double-screw impregnator, and the adjustment slurry that adds water is dense to 25 ~ 35%, slurry pH value controls in acid range, realization homogenizes after chemical impregnation process and is expelled to reaction warehouse, in the temperature range of 80 ~ 95 DEG C, stop and react for 35 ~ 60 minutes;
4. the second extrusion impregnating chemical mechanical processing section: the slurry that the first extrusion impregnating chemical mechanical processing section reaction warehouse is exported, to be delivered in this section of double-screw impregnator by further extruding and kneading by conveying worm and to be fibre bundle and single fiber mixture shape and to be concentrated into 35 ~ 45% concentration, thereafter mix with the second chemical impregnation medicament height be metered into is dense in this section of double-screw impregnator, and the adjustment slurry that adds water is dense to 25 ~ 35%, slurry pH value controls in alkaline range, realization homogenizes after chemical impregnation process and is expelled to reaction warehouse, in the temperature range of 80 ~ 95 DEG C, stop and react for 35 ~ 60 minutes,
5. disappear and dive and the section of discongesting again: the slurry that the second extrusion impregnating chemical mechanical processing section reaction warehouse is exported, being delivered in latency chest by conveying worm makes pelletizing shape fiber dispersion stretch elimination internal stress, the adjustment slurry that adds water is dense to 3 ~ 5%, adjustment slurry temperature range is 60 ~ 70 DEG C, thereafter be pumped to defibrator by stock pump to discongest again, isolate light, heavy seeds and thick waste material and wet-strength paper fiber;
6. purifying, screen and enriching section: to dive disappearing and the section of discongesting is separated the wet-strength paper fiber obtained again, be stored in after scummer purification, pressurized screen screening, concentrator are concentrated and store in sizing device for copying.
2. the two pH value chemical mechanical pulp-making method of wet strong waste paper recycling according to claim 1, it is characterized in that: the sediment impurity obtained after tumbler-type washing machine washing in described 1. material papering section enters fixed-end forces system, the residual impurity of being discharged by the sieve plate mesh of inclined helix dehydrator and water enter water treatment system, are back to washing process through precipitation purification Posterior circle.
3. the two pH value chemical mechanical pulp-making method of wet strong waste paper recycling according to claim 1, it is characterized in that: the percentage by weight according to accounting for over dry raw material: in described 2. decatize workshop section, the mass transport after dehydration is to the humectant again adding 0.1% ~ 0.15% during the decatize of decatize storehouse.
4. the two pH value chemical mechanical pulp-making method of wet strong waste paper recycling according to claim 1, is characterized in that:
Slurry pH value in described 3. the first extrusion impregnating chemical mechanical processing section controls: slurry pH value controls in 4.5 ~ 6 scopes;
Slurry pH value in described 4. the second extrusion impregnating chemical mechanical processing section controls: slurry pH value controls in 11.5 ~ 12.5 scopes; Described second chemical impregnation medicament is oxidant.
5. the two pH value chemical mechanical pulp-making method of wet strong waste paper recycling according to claim 1, is characterized in that: the percentage by weight according to accounting for over dry raw material:
The first chemical impregnation medicament in described 3. the first extrusion impregnating chemical mechanical processing section is the H of 1 ~ 1.5% 2sO 4or the alum of 3 ~ 6%, control in 4.5 ~ 6 scopes by acid-treated slurry pH value;
The second chemical impregnation medicament in described 4. the second extrusion impregnating chemical mechanical processing section is oxidant, controls in 11.5 ~ 12.5 scopes by the slurry pH value of oxidizer treatment; Described oxidant package is containing the NaOH of 1 ~ 3%, the H of 2 ~ 6% 2o 2, 1 ~ 2% Na 2siO 3with 0.2 ~ 0.5% chelating agent.
6. the two pH value chemical mechanical pulp-making method of wet strong waste paper recycling according to claim 5, is characterized in that: described chelating agent is any one of DTPA or EDTA.
7. the two pH value chemical mechanical pulp-making method of wet strong waste paper recycling according to claim 1, is characterized in that: the percentage by weight according to accounting for over dry raw material:
In described 2. decatize workshop section, the mass transport after dehydration is to the humectant again adding 0.12% during the decatize of decatize storehouse;
The first chemical impregnation medicament in described 3. the first extrusion impregnating chemical mechanical processing section is the H of 1.2% 2sO 4;
The second chemical impregnation pharmacy kit in described 4. the second extrusion impregnating chemical mechanical processing section is containing the NaOH of 2%, the H of 4% 2o 2, 1.5% Na 2siO 3with 0.35% DTPA.
8. the two pH value chemical mechanical pulp-making method of wet strong waste paper recycling according to claim 1, is characterized in that: the percentage by weight according to accounting for over dry raw material:
In described 2. decatize workshop section, the mass transport after dehydration is to the humectant again adding 0.15% during the decatize of decatize storehouse;
The first chemical impregnation medicament in described 3. the first extrusion impregnating chemical mechanical processing section is the H of 1.5% 2sO 4;
The second chemical impregnation pharmacy kit in described 4. the second extrusion impregnating chemical mechanical processing section is containing the NaOH of 3%, the H of 6% 2o 2, 2% Na 2siO 3with 0.5% EDTA.
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CN104099795A (en) 2014-10-15

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