Classifications

• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
  • D21C3/00—Pulping cellulose-containing materials
  • D21C3/22—Other features of pulping processes
  • D21C3/26—Multistage processes
• • D—TEXTILES; PAPER
  • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
  • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
  • D21C3/00—Pulping cellulose-containing materials
  • D21C3/22—Other features of pulping processes
  • D21C3/26—Multistage processes
  • D21C3/266—Multistage processes the same pulping agent being used in all stages

Definitions

• This invention relates to a process for the manufacturing of cellulose mechanical pulps and pulps obtained thereby.
• Mechanical pulp plants typically have a lower specific capital cost to build and mechancial pulps typically have a high yield and can be cheaper to produce that chemical pulps.
• mechanicals pulps do not provide the pollution problems which are associated with chemical pulps.
• mechanical pulps have not been of the same high quality as chemical pulps and thus to achieve an end pulp which is of the required quality but at the same time economic to produce it is a well known technique to combine mechanical and chemical pulps.
• the aforementioned developments in mechanical pulp processes which stem from the basic RMP process have led to some mechanical pulps having the characteristics of a chemical pulp and they can thus be used as a replacement, in whole or in part, for chemical pulps in those applications where chemical pulps have traditionally been used.
• the present invention has its basis in the surprising discovery that the whole pulp can be subjected to a two stage digestion and refining process with the second addition of an aqueous sodium sulphite solution taking place prior to or with the cellulose material entering or after the first refining stage followed by digestion after the chemical addition.
• the process can be carried out with significant savings in energy requirements even though the whole pulp is processed in the two digestion and refining steps whilst increase in many of the desirable properties of the pulp for end use applications are obtained.
• the process has particular application either singly or in combination for pinus radiata corewood and/or pinus radiata slab wood, eucalypts and New Zealand hardwoods but it is believed that it has similar application to other wood types and species.
• the present invention requires a relatively high total charge of digestion chemicals the total charge is split into two separate charges of which the first charge is preferably lower but preferably in an impregnation process rather than a simple mixing stage.
• the resultant pulp is low in fines, has high strength characteristics and is produced with low energy requirements.
• the total chemical charge in the present invention is in the order of that required in a CMP process but does not require the high energy demands of a CMP process for some wood types, particularly pine species and hardwood/softwood blends.
• the object of the present invention is to provide a process for the manufacture of cellulose mechanical pulps which provides a high yield pulp of improved quality which can be used as a substitute for chemical pulps and is achieved without increases or at lesser increases in refining energy inputs.
• the invention can be said to consist of a process for the manufacturing of cellulose pulp using two or more chemical addition and digestion stages in conjunction with mechanical pulping techniques.
• mechanical pulping as used herein has its normal meaning in the art and refers to the process of disruption of a cellulose substance by mechanical action to yield a product consisting mainly of liberated and separated single cellulose fibres and their fragments and which is suitable for use in the manufacture of paper and other products.
• the invention consists of a process for the manufacturing of a cellulose pulp from material in particulate form comprising the steps of impregnating the material with digestion chemicals, digesting the impregnated material, adding further digesting chemicals and mechanically refining the resultant mixture to reduce the material to predominantly whole fibres, digesting the impregnated and refined mixture and then further refining the resulting pulp product, if required.
• wood chips are washed in washer 10 and conveyed to a surge/pre-steaming vessel 11.
• live steam is added to remove air and preheat the chips to a temperature in the range of 80-100°C.
• Discharge of chips from vessel 11 is maintained at a controlled rate to a compression screw feeder 12 wherein excess liquid is removed and the chips are dewatered to over 20% dryness.
• the chips are dewatered to over 40% dryness.
• the chips are then delivered to an impregnation device 13 (preferably an inclined screw conveyor).
• Digestion chemicals are delivered to or between the feeder device 12 and/or the impregnation device 13 with delivery being at a temperature below 100°C, preferably under 50°C.
• These delignifying chemicals in aqueous form are of known composition, primarily of the sodium sulphite family, and are added at a level of 0.5 to 5% active chemical on bone dried fibre. Condensation of steam within the chips causes the liquor to be absorbed into the chips. Retention time within the liquor zone of the impregnation device 13 is 5 to 20 minutes but preferably over 7 minutes.
• the chips On leaving the liquor zone of the impregnation device 13 the chips may be subjected to direct steam heating to raise the temperature of the chips to within the range of 80-100°C.
• the impregnated chips are then fed to a primary digester 14 by a pressure sealing device 13a such as a compression screw, rotary valve or similar.
• the residence time within the digester 14 is in the range of 3 to 20 minutes, but preferably 5 to 10 minutes, with heating by direct steam injection to give a vapour phase reaction.
• the pressure of the primary digester 14 is in the range of 0-800 kPa overpressure, but more preferably 200 to 400 kPa overpressure.
• Product from primary digester 14 is by controlled metering in accordance with known procedures and fed via feeder/pressure seal 15 to a primary refiner 16 (such as a disc refiner) operating at 0 to 600 kPa overpressure but more preferably 200 to 300 kPa overpressure. Further digestion or cooking chemicals of known composition are added to the product feed to the primary refiner 16 for subsequent reaction in the secondary digester 19. The cooking chemicals are mixed with the chip/pulp mixture present in the primary refiner 16 by the refiner action. Addition of the sulphite based cooking chemicals is in the range of 2 to 20% active chemical on bone dried fibre preferably 5% to 10.% on bone dried fibre.
• the pulp and steam generated in the primary refiner 16 are discharged through a common blowline to a cyclone 17 where water and/or spent process liquor is added for consistency control during the subsequent digestion phase.
• Pulp and liquor is discharged from cyclone 17 by a feeder/pressure seal device 18 (preferably a compression screw) and enters the secondary digester 19.
• the residence time within the secondary digester 19 is in the range of 20 to 120 minutes but more. preferably 30 to 60 minutes at an overpressure in the range of 100 to 800 kPa but more preferably 300 to 600 kPa overpressure.
• Discharge from the secondary digester 19 is achieved by injecting water/spent liquor through lines 20 and 21 into the base of the secondary digester 19 and mixing this with the pulp.
• the motive force for discharging the pulp is provided by the internal pressure in the digester.
• the digester may be discharged by screw conveyor or other methods.
• Discharged pulp is passed to a washer 22, preferably a press washing system, wherein it is washed and pressed and passed by a feeder/pressure seal 23 to a secondary refiner 24.
• the secondary refiner 24 may operate at a pressure in the range 0 to 600 kPa overpressure but preferably 200 to 300 kPa overpressure.
• Steam and pulp are discharged from secondary refiner 24 through a common blowline to a cyclone 25 where they are separated and discharged in substantially the same manner as that from the primary refiner 16.
• the resultant pulp may then be treated in accordance with accepted pulping practices, such as latency removal, screening, cleaning and bleaching.
• accepted pulping practices such as latency removal, screening, cleaning and bleaching.
• the resulting pulp product may be dried or used directly or indirectly for its intended end use.
• either or both the refining stages in refiners 16 and 24 may take place at atmospheric pressure with screws or other discharge and conveying devices; two or more stages of refining may be present prior to or after the secondary digester 19; pulp from the secondary digester 19 may be discharged directly from the pulping process outlined as being an inter- or post- refining stage; inter-stage washing and de-watering could be included between first stage digesting and first stage refining; a further stage or stages of chemical addition, refining, digesting with or without inter-stage washing and de-watering could be added.
• the affect of the inter-stage or post-digesting stage is to give a change in fibre properties, improving some, but of significance, is a major reduction in refining energy requirements to achieve the desired end use properties.
• the process according to the present invention results in a high-yield mechanical pulp of at least a similar but generally improved quality over pulps obtained with similar known process but without increases or at lesser increases in refining energy inputs.
• High levels of combined sulpher at the same freeness level can thus be achieved without'figher power usage as is normally the case with some chemi-mechanical (CMP) or chemi-thermomechanical (CTMP) processes.
• CMP chemi-mechanical
• CTMP chemi-thermomechanical
• SCTMP sulphonated chemi-thermomechanical pulp
• the digestion/refining process treatment allows high sulphonation to be achieved giving better brightness, absorbency, softness and fibre flexibility with a major reduction in refining energy requirements.
• the process results in clean fibre separation, improved fibre yield with reduced fines and improved bulk, tear index, tensile index, stretch, burst and other wet and dry web properties.
• Test runs of the process of the present invention have been carried out and the results of the properties of the process and RMP and CTMP pulp for unbleached screened and cleaned pulp (tested to SCAN standards using a 60 gsm handsheet) are set out below.
• the pulp product prior to bleaching stage(s) contains a low quantity of fibre bundles, that is less than substantially 10% and preferably substantially none.
• the process can be used for soft woods, blends of soft woods and blends of softwoods and hardwoods. For the last case superior quality is obtained than when using other high yield processes.
• CTMP chemi-thermomechanical pulp process
• RMP refiner mechanical pulp process
• Blends of chips of different wood species and single species were treated in a steaming vessel for 10 minutes at about 95 degrees centigrade (condensate was drained and the vessel charged with cold impregnation chemical, sodium sulphite, of sufficient concentration to give the desired final sulphur content.
• the impregnation liquor was heated by recirculation through an external heat exchanger to about 95 degrees centigrade and the liquor then drained.
• the impregnated chips were digested at about 130 degrees centigrade using direct steam injection for 5 minutes.
• the digested chips were discharged by screw conveyor and fed to a pressurized double disc refiner operating at about 2 bar overpressure.
• the resulting pulp was again refined by a second pass through the same refiner under the same pressure conditions.
• Blends of chips of different wood species and single species were treated in a steaming vessel for 10 minutes at about 95 degrees centigrade '(condensate was drained and the vessel charged with cold impregnation chemical, sodium sulphite, of sufficient concentration to give the desired final sulphur content.
• the impregnation liquor was heated by recirculation through an external heat exchanger to about 95 degrees centigrade and the liquor then drained.
• the impregnated chips were digested at about 130 degrees centigrade using direct steam injection for 5 minutes.
• the digested chips were discharged by screw conveyor and fed to a pressurized double disc refiner.
• the refiner secondary digestion chemical sodium sulphite liquor
• the pulp/liquor mixture was conveyed by refiner generated steam (blown) back to the primary cooking vessel and digested at 160 degrees centigrade for about 60 minutes.
• Digested pulp was discharged and refined for a second time. Both refining stages were pressurised at about 2 bar overpressure.
• Example 3 The process of Example 3 was carried out.
• the pulp had further digestion chemicals added at the entry to the second stage refiner and a third stage of digestion was carried out followed by a third stage of refining at atmospheric pressure.
• the results of this process are shown in the extreme right hand column marked ' SCTMP ' in the table which follows.
• the resultant pulp from the process according to the invention is unexpectedly suitable for further refining development to improve various properties, in particular tensile index, burst, air resistance, that will enhance its performance in its selected end use.

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• Paper (AREA)
• Polysaccharides And Polysaccharide Derivatives (AREA)
• Materials For Medical Uses (AREA)

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ID=19921155

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Cited By (5)

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Citations (3)

• 1985
  • 1985-04-04 NZ NZ211684A patent/NZ211684A/xx unknown
• 1986
  • 1986-04-03 CA CA000505773A patent/CA1273454A/en not_active Expired - Lifetime
  • 1986-04-03 NO NO861307A patent/NO167159C/no not_active IP Right Cessation
  • 1986-04-03 ZA ZA862454A patent/ZA862454B/xx unknown
  • 1986-04-04 DE DE8686302491T patent/DE3667515D1/de not_active Expired - Lifetime
  • 1986-04-04 KR KR1019860002568A patent/KR930003394B1/ko not_active IP Right Cessation
  • 1986-04-04 PT PT82341A patent/PT82341B/pt not_active IP Right Cessation
  • 1986-04-04 AR AR86303572A patent/AR243623A1/es active
  • 1986-04-04 FI FI861453A patent/FI83238C/fi not_active IP Right Cessation
  • 1986-04-04 AU AU55650/86A patent/AU585331B2/en not_active Ceased
  • 1986-04-04 ES ES554182A patent/ES8705940A1/es not_active Expired
  • 1986-04-04 BR BR8601558A patent/BR8601558A/pt not_active IP Right Cessation
  • 1986-04-04 JP JP61079058A patent/JPS61282491A/ja active Pending
  • 1986-04-04 EP EP86302491A patent/EP0199481B1/de not_active Expired
• 1987
  • 1987-10-10 MY MYPI87002889A patent/MY102502A/en unknown

Patent Citations (3)

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