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
  • D21C11/00—Regeneration of pulp liquors or effluent waste waters
  • D21C11/0021—Introduction of various effluents, e.g. waste waters, into the pulping, recovery and regeneration cycle (closed-cycle)
• • 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
  • D21C3/00—Pulping cellulose-containing materials
  • D21C3/22—Other features of pulping processes

Definitions

• the present invention relates to a process for improving the final brightness of pulp. More particularly, the present invention relates to
• Rapid Displacement Heating is a low energy batch cooking process for producing kraft pulp. Combining the inherent advantages of batch cooking with the energy efficiencies of a continuous digester, RDH reuses the spent black liquors that are displaced from a cooked digester to pretreat the wood chips in a consequent cook. Thus, both the chemicals and the heat in these spent liquors are recycled to a consequent cook.
• the pretreatment of fresh wood chips in a consequent cook begins with lower temperature liquors (approximately 80 ⁇ 130°C), and is followed by high temperature liquors (approximately 130° to 165°C) which heat the digester to the highest possible temperature before raising the temperatures to the final cooking temperature ( 3 170°C) with steam.
• RDH and other alkaline cooking processes produce pulp that is relatively dark in color. Greater contrast is usually needed for the many uses of pulp and paper, so pulp is usually bleached to a high brightness in order to make white pulp for writing and printing papers and paperboard. Pulp color arises from changes in the lignin component of the raw material which occur in the pulping process.
• high cooking temperatures and low black liquor strength in the RDH process low bleachability problems have occurred following the use of conventional, ECF and TCF bleaching processes. High cooking temperatures and low black liquor strength seem to accelerate condensation reactions, resulting in the condensation of lignin with lignin and other wood extractives. As a result, the bleachability of pulp decreased.
• the present invention provides a method for improving pulp brightness. Based on modifications to a batch cooking process utilizing rapid displacement heating, the method of the present invention combines the steps of adding white liquor solution (% active alkalinity (AA) or effective alkalinity (EA)) or NaOH to both the warm fill and initial hot fill stages and cooking wood chips at lower temperatures than previously used in a batch type operation to produce pulp that has improved bleachability.
• white liquor solution % active alkalinity (AA) or effective alkalinity (EA)
• NaOH sodium nitrate
• AA active alkalinity
• EA effective alkalinity
• a total white liquor charge ranging from 15% AA ⁇ 35% AA is distributed over the warm, hot and cooking stages in a predetermined amount.
• cool white liquor is also added to the black liquor that is released from the cool liquor accumulator. Essentially, white liquor is added to every stage of the batch cooking process prior to the actual cook.
• FIG. 1 illustrates a schematic view of a digested and its associated equipment used in the current RDH cooking system.
• FIGS. 2A, 2B and 2C each illustrate white liquor profiling or the addition of white liquor at various stages of the RDH cooking process.
• plot A represents the addition of a small amount of white liquor at the beginning of the warm fill mode.
• Plot B represents the cooking stage and illustrates the presence of white liquor in the digester during the actual cooking of the chips.
• FIG. 2B illustrates the continuous addition of white liquor to the black liquor at each stage of the RDH cooking process, beginning with the warm fill and continuing through the end of the hot fill.
• White liquor as shown, is also present in the digester during the actual cook.
• FIG. 2C illustrates the continuous addition of white liquor at each RDH stage including the addition of white liquor to the washer filtrate from the displacement tank.
• FIG. 3 illustrates a Stage 3 RDH system without white liquor addition during the warm and hot fill modes.
• FIG. 4 illustrates a Stage 3 RDH system with the addition of white liquor during the warm and hot fill modes.
• FIG. 5 illustrates a plot of D1-brightness versus total (D100 + D1) available chlorine charge for the best case and baseline case RDH pulps.
• Plot A represents RDH pulp R3 (0.225 Kappa factor).
• Plot B represents RDH pulp R4 (0.27 Kappa factor).
• Plot C represents RDH pulp R7 (0.225 Kappa factor).
• Plot D represents RDH pulp R8 (0.27 Kappa factor).
• FIG. 5A illustrates a plot of D1-brightness versus D1-chlorine dioxide charge.
• Plot A represents RDH pulp R3 (0.225 Kappa factor).
• Plot B represents RDH pulp R4 (0.27 Kappa factor).
• Plot C represents RDH pulp R7 (0.225 Kappa factor).
• Plot D represents RDH pulp R8 (0.27 Kappa factor).
• FIG. 5A illustrates a plot of D1-brightness versus D1-chlorine dioxide charge.
• Plot A
• Plot C represents RDH pulp R7 (0.225 Kappa factor).
• Plot D represents RDH pulp R8 (0.27 Kappa factor).
• FIG. 6 illustrates the D1 -brightness versus the total available chlorine charge in the D100- and D1-stages for all 0.225 Kappa factor bleaches.
• Plot A represents RDH pulp R3.
• Plot B represents RDH pulp R12.
• Plot C represents RDH pulp R7.
• FIG. 6A illustrates the D1-brightness versus the D1-stage chlorine dioxide charges.
• Plot A represents RDH pulp R3 (0.225 Kappa factor).
• Plot B represents RDH pulp R12 (0.225 Kappa factor).
• Plot C represents RDH pulp R7 (0.225 Kappa factor).
• FIG. 7 illustrates the D1 -brightness versus the total available chlorine charge in the D100- and D1-stages for all 0.27 Kappa factor bleaches.
• Plot A represents RDH pulp R4.
• Plot B represents RDH pulp R12.
• Plot C represents RDH pulp R8.
• FIG. 7A illustrates the D1-brightness versus the D1 -stage chlorine dioxide charges.
• Plot A represents RDH pulp R4 (0.27 Kappa factor).
• Plot B represents RDH pulp R12 (0.27 Kappa factor).
• Plot C represents RDH pulp R8 (0.27 Kappa factor).
• the present invention provides a method for improving pulp bleachability, which is based on modifications to the existing RDH Cooking System for the digestion of wood chips. More specifically, the method involves the addition of a white liquor charge commencing at the start of the RDH cooking cycle and continuing until the time to temperature stage of the process, at which time the actual cook begins. The method of the present invention is also predicated on the use of somewhat lower cooking temperatures for the actual cook as compared to cooking temperatures commonly used in the RDH pulping process.
• a total white liquor charge ranging between approximately 15%AA ⁇ 35%AA is distributed over the warm black liquor, initial hot black liquor and cooking stages.
• the cool pad or cool liquor accumulator also receives a white liquor charge.
• the present invention utilizes lower cooking temperatures ranging between approximately 150°C ⁇ 167°C. As a result, pulp is produced which, upon bleaching with any combination of bleaching chemicals, is improved in final brightness.
• FIG. 1 schematically illustrates the type of apparatus for RDH that is used for the digestion of pulp. It should be understood that this figure illustrates very general features of the cooking apparatus, and modifications and variations in this system are indeed made as will be discussed in greater detail below. Many instrumentalities such as gauges, pressure vents, pumps and valves have been eliminated from the figures disclosed herein for reasons of simplicity.
• FIG. 1 is used to illustrate the existing RDH cooking process and to facilitate an understanding of the improvements to the process in accordance with the principles of the present invention.
• a digester is illustrated at 10 of the type generally used in the chemical digestion of wood chips.
• the digester 10 has a truncated bottom 12.
• An inlet valve 14 controls the entry of various reactive liquors into digester 10.
• the contents of digester 10 can be heated to a final cooking temperature by pumping cooking liquor through a heat exchanger or steam sparger which is connected to digester 10 by a
• Hot black liquor (temperature between 150°-168°C) is then pumped from the hot liquor accumulator (C tank) 28 by means of a pump 30 which is controlled by a valve 32 into the bottom of the digester 10 utilizing valve 14.
• black liquor is displaced from the digester 10 and returned to the warm liquor accumulator 24 and hot liquor accumulator 28 through lines 34 and 36, respectively.
• hot white liquor stored in the hot white liquor accumulator 38 is pumped out by means of a pump 30 where it combines with the hot black liquor leaving the hot liquor accumulator 28, the combined liquors then passing through a valve 32 and into the base of the digester 10.
• the inlet and outlet valves to the digester 10 are closed as the time to temperature stage commences. Steam is injected into the digester 10 and the temperature is increased to the cooking
• the temperature of the digester is maintained at about this temperature until the wood chips are digested, depending on white liquor charge and H-factor.
• washer filtrate (temperature approximately 70 ⁇ 85°C) stored in a displacement tank (D tank) 40 is pumped into the digester 10, utilizing pump 42 and valve 44. The contents are washed and the digester 10 is cooled. As the washer filtrate is added to the digester 10, the spent liquors are displaced and returned to the warm liquor accumulator 24 and the hot liquor accumulator 28 by lines 46 and 48, respectively. The displacement mode is concluded when all washer filtrate is used, which is based on the dilution factor of the washer. After displacement is completed, the digested pulp is then pumped out of the digester 10 to a discharge tank using pump 50.
• the present invention overcomes these problems and improves pulp bleachability by modifying the cooking process for wood chips.
• This improved RDH process utilizes a combination of higher alkalinity (or white liquor charge) and lower cooking temperatures. More specifically, white liquor is added during the warm and initial hot fill stages. This is in contrast to the existing RDH cooking process, wherein white liquor is added only during the middle of the hot fill mode. Further, when a cool pad is used in the present invention, white liquor is added to the cool black liquor leaving the cool liquor accumulator (or A tank).
• white liquor is added during each stage to the black liquor.
• white liquor profiling is illustrated in greater detail below in FIGS. 2A, 2B and 2C.
• plot A illustrates the addition of a small amount of white liquor at the beginning of the warm fill mode when warm black liquor leaves the B tank or warm liquor accumulator and flows to the digester.
• White liquor can also be added to the A tank or cool pad when used.
• Plot B represents the cooking stage and illustrates the presence of white liquor in the digester during the actual cooking of the chips. Black liquor is also present during the cook.
• FIG. 2B illustrates the continuous addition of white liquor to black liquor at each stage of the cooking process, beginning with the warm fill through the end of the hot fill mode.
• FIG. 2C illustrates the continuous addition of white liquor throughout the various stages, including the addition of white liquor to the washer filtrate from the displacement tank.
• FIG. 3 illustrates a Stage 3 RDH system where no white liquor is added during the warm and hot fill modes. Only warm black liquor is leaving the warm liquor accumulator (B tank) 24 to flow through line 56 during the warm fill mode and into line 20, which then empties into the digester 10. Although this RDH system contains two hot liquor accumulators 28 (C1 tank) and 58 (C2 tank),
• hot black liquor leaves the hot liquor accumulators 28 and 58 by lines 60 and 62, respectively, and flows to the digester 10 through lines 64 and 20.
• hot white liquor from the hot white liquor accumulator 38 mixes with the hot black liquor leaving hot liquor accumulator 58 by line 66. The mixture then flows through lines 64 and 20 and into the digester 10.
• FIG. 4 illustrates a Stage 3 RDH System with the addition of white liquor during the warm and hot fill modes.
• white liquor is added to the warm black liquor leaving the warm liquor accumulator 24 by line 70.
• the warm fill flows through lines 56 and 20 into the digester 10.
• Either cool or hot white liquor may be used during the warm fill mode.
• hot white liquor from the hot white liquor accumulator 38 is mixed with black liquor leaving hot liquor accumulator 28 by line 72, and is further mixed with the black liquor exiting the second hot liquor accumulator 58 by lines 62 and 66.
• the mixture of hot white and black liquors flows from the two hot liquor accumulators 28 and 58 through lines 64 and 20 into the digester 10.
• concentration of dissolved organic compounds at initial hot fill operation can be adjusted by adding white liquor to the hot fill line.
• concentration of dissolved organic compounds in the C1 black liquor and in the C2 black liquor decreases from 13.1% to 10.1% and 14.9% to 9.8%, respectively.
• warm black liquor temperatures between approximately 70° and 150°C and its strength between 3 and 20 g/l AA
• hot black liquor temperatures between approximately 100° and 168°C and its strength between 8 and 30 g/l AA
• warm and hot black liquor can be modified using white liquor profiling. These liquors can also be modified by sodium hydroxide (NaOH) profiling.
• NaOH sodium hydroxide
• the addition of white liquor or NaOH controls the total dissolved solids (TDS) concentration and black liquor strength using any combination of black liquor, white liquor ancS NaOH.
• the washer filtrate displacement stage in which the black liquor temperature is held between approximately 50° and 105°C and black liquor strength between 1 and 18 g/l AA, can be reinforced with any combination of white liquor or NaOH solution.
• Tables 1, 1A, 2, 2A, 3 and 3A provide the pulping results and conditions for a number of cooks used in preparing the RDH pulps for subsequent bleaching studies.
• a summary of the pulping results is provided in Table 3B.
• RDH pulps (R3, R4, R7, R8 and R12) were bleached using an (O)(D100)(EO)(D) sequence. However, each of the five RDH pulps were first oxygen delignified in stirred reactors using the conditions shown below in Table 4.
• FIGS. 7 and 7A show that the best do-able case RDH pulp (R12) gave intermediate brightness between the best case RDH pulp (R4) and the baseline case RDH pulp (R8).

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• Polysaccharides And Polysaccharide Derivatives (AREA)
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• Peptides Or Proteins (AREA)

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Cited By (5)

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Citations (3)

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• 1995
  • 1995-02-23 TW TW084101667A patent/TW270159B/zh active
  • 1995-03-02 AU AU19789/95A patent/AU684623B2/en not_active Ceased
  • 1995-03-02 CN CN95191955A patent/CN1143398A/zh active Pending
  • 1995-03-02 WO PCT/US1995/002719 patent/WO1995023891A1/en active IP Right Grant
  • 1995-03-02 JP JP7523062A patent/JP2876428B2/ja not_active Expired - Lifetime
  • 1995-03-02 AT AT95912729T patent/ATE172503T1/de active
  • 1995-03-02 MX MX9603876A patent/MX9603876A/es unknown
  • 1995-03-02 NZ NZ282616A patent/NZ282616A/en unknown
  • 1995-03-02 DE DE69505503T patent/DE69505503T2/de not_active Expired - Fee Related
  • 1995-03-02 RO RO96-01743A patent/RO117929B1/ro unknown
  • 1995-03-02 CA CA002184706A patent/CA2184706C/en not_active Expired - Fee Related
  • 1995-03-02 BR BR9506974A patent/BR9506974A/pt not_active IP Right Cessation
  • 1995-03-02 RU RU96121355A patent/RU2127342C1/ru active
  • 1995-03-02 ES ES95912729T patent/ES2126263T3/es not_active Expired - Lifetime
  • 1995-03-02 PL PL95316144A patent/PL316144A1/xx unknown
  • 1995-03-02 EP EP95912729A patent/EP0748412B1/de not_active Expired - Lifetime
  • 1995-03-03 ZA ZA951777A patent/ZA951777B/xx unknown
• 1996
  • 1996-08-23 NO NO963520A patent/NO963520L/no unknown
  • 1996-09-03 FI FI963448A patent/FI118348B/fi active IP Right Grant

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