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
  • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
  • D21C9/10—Bleaching ; Apparatus therefor
  • D21C9/16—Bleaching ; Apparatus therefor with per compounds
  • D21C9/166—Bleaching ; Apparatus therefor with per compounds with peracids
• • 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
  • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
  • D21C9/10—Bleaching ; Apparatus therefor
  • D21C9/147—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications
  • D21C9/153—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications with ozone

Definitions

• the present invention relates to a method for the production of bleached pulp with good strength characteristics according to the preamble of claim 1.
• the pulp is treated in at least one bleaching stage in which it comes into contact with ozone.
• the invention also relates to the bleaching sequences according to the preamble of claim 28 as well as to the pulp according to the preamble of claim 32.
• ozone-bleached softwood sulphate pulp is known to have a lower viscosity and about 10 % inferior tear strength. Viscosity has been found to correlate closely with tear strength for a given pulp. If the pulp viscosity could be improved, this would be reflected as an improvement in pulp strength.
• Treatment with borohydride is based on that the alkali-labile carbonyl groups formed in the pulp during ozonation are reduced by borohydride to alkali-stable alcohol groups (4).
• the alcohol groups formed in the reduction reaction are not stable, however, and are gradually oxidized back to carbonyl groups, for example on exposure to air.
• Other drawbacks include the high cost of borohydride and possible problems in treating the effluents.
• bleaching chemicals there are very few bleaching chemicals that can be employed together in the same bleaching stage.
• One of the chemicals will normally be more reactive than the other, and its bleaching reactions will therefore dominate.
• hydrogen peroxide and chlorine dioxide will react with each other, which means they are less effective together than separately.
• Ozone and peracetic acid (Paa) have been used as consecutive stages in an OZPaa sequence and the results compared with those from OZEZ and OZP sequences (10).
• the pulps used included pine pulp with a kappa number of 20 after the oxygen stage. The highest brightness achieved was 78 - 81 %, even though the ozone charge was around 20 kg/ADt and the peracetic acid charge 20 kg/ADt.
• prior to ozonation the sulphate pulps were steeped in acetic acid to which dimethylsulphoxide had been added. The problems associated with these solvents relate to fire hazards and the difficulty of their recovery from the bleaching filtrates.
• peracetic acid, ozone and oxygen have been employed under acidic conditions in a single stage (FI Patent Application No. 940412, reference 11).
• the pulp is first treated with peracetic acid, which reacts with lignin and opens up the pulp' s fibre structure.
• Peracetic acid treatment allows the use of a smaller ozone charge, which in turn reduces fibre damage. It is believed that treating the pulp with only small amounts of ozone will produce a stronger pulp than that obtained with the three-stage treatment O-Z-Paa.
• ozonation is followed by an alkaline extraction stage using either chlorine dioxide or peroxide.
• WO Published Application No. 92/21814 describes a bleaching sequence in which an ozone stage and a washing stage are followed by a Paa stage employing 2 % peracetic acid and 3 % NaOH. The slurry is then maintained at a temperature of 70 ° C for 240 min.
• a solvent such as an alcohol, aldehyde or carboxylic acid
• the main purpose of the solvent is to capture the harmful radicals formed during ozonation.
• Other proposed solvents include urea-methanol, methanol, DMF and DMSO.
• these are expensive and also present problems in relation to effluent treatment and cycle closure.
• the purpose of the present invention is to overcome the drawbacks of the prior art and to provide an entirely novel type of a process for the ozone bleaching of pulp.
• the present invention is based on the surprising fact that the treatment of an ozonated pulp with an oxidizing agent under acidic conditions can reduce or completely eliminate pulp alkali lability.
• the acid stage can be carried out either after washing or without any prior washing stage.
• residual lignin is extracted from the pulp fibres under alkaline conditions without breaking the cellulose chains.
• the alkali extraction can be performed with or without prior washing using peroxide and/or peroxide reinforced with oxygen.
• fully bleached pulp (ISO brightness > 87.5 %) with a kappa number of less than 2, a viscosity greater than 600 ml/g, a tear index (T70) of more than 13 mN-m 2 /g, and a zero-span tensile index (T70) of over 100 N-m/g measured for a wet sheet can be produced by means of the treatment.
• the invention can be applied in practice using bleaching sequences containing Z, Paa and P and/or E stages in this order, one essential requirement being that the Z stage is not followed by an alkali treatment stage before the ozonated pulp has been treated with an oxidizing agent, in particular a peroxy alkanoic acid.
• an oxidizing agent in particular a peroxy alkanoic acid.
• the bleaching sequences according to the invention are characterized by what is stated in the characterizing part of claim 28; the pulp according to the invention is characterized by what is stated in the characterizing part of claim 32.
• the invention can be used to reduce the alkali lability of ozonated pulp by bringing the pulp into contact with an oxidizing bleaching agent under conditions that are acid (including neutral or at most slightly acid conditions).
• an oxidizing bleaching agent under conditions that are acid (including neutral or at most slightly acid conditions).
• the carbonyl group contents of pulps to be bleached in accordance with the invention are doubled during ozonation, whereafter these contents clearly fall by 10 - 15 % (in some cases 20 %) as a result of treatment with peracetic acid subsequent to ozonation.
• the carbonyl content can be further reduced (by just under 30 %).
• the method according to the invention treats Z pulp with peracetic acid under acidic conditions prior to the alkaline stage, thereby oxidizing some of the carbonyl groups to carboxyl groups.
• the pH at the start of this treatment is acid, neutral or slightly acid (e.g., approx. 4.5 - 8), while the final pH is acid (usually approx. 4.5 - 5).
• the method according to the invention reduces the amount of carbohydrates dissolving under alkaline conditions.
• Carbohydrate dissolution is at least 30 % lower than in cases where the pulp is treated under alkaline conditions after ozonation. Preventing the dissolution of carbohydrates helps to improve tear strength, the strengths of individual fibres (zero-span strength) and yield, and also to reduce the solute content of the filtrate.
• the method does not employ organic solvents or other compounds that would capture radicals because the carbonyl groups formed by unwanted reactions are removed by the after-treatment according to the invention.
• the method according to the invention produces high-brightness pulps by reducing the residual lignin content before ozone treatment and carrying out an alkali treatment at the end of the bleaching stage, yielding pulp with 85 - 92 % brightness (sequence OOZPaaO or OOZPaaE, for example).
• Performing the alkaline treatment immediately after the Paa treatment also allows unreacted peroxide to be utilized at the high pH, thus leading to higher brightness.
• the method disclosed in the present invention allows the use of higher ozone charges than in the process described in reference 11, provided that the pulp is subsequently subjected to oxidation, for example with peracetic acid, under acidic conditions. Since the use of ozone as a bleaching agent is fairly economical in the long term, the present invention also offers economic benefits.
• Figure 4 shows the tear indexes of the bleached pulps
• Figure 5 shows the zero-span indexes (wet) of the bleached pulps
• Figure 6 shows the carbohydrate contents of the bleaching filtrates separately
• Figure 7 shows the total carbohydrate contents of the bleaching filtrates per tonne of bleached pulp
• Figure 8 shows the tear indexes of Z/Paa/EP pulp for different ozone and Paa charges
• Figure 9 shows the zero-span tensile index (wet) of Z/Paa/EP pulp.
• the bleaching sequence for pulp includes the following stages: -Z/Paa/P, -Z -Paa/P, -Z Paa -P, -Z/Paa E, -Z/Paa -E,
• Z ozone stage
• Paa peroxy acid stage
• P peroxide stage
• E alkaline extraction stage
• R an alkaline stage involving borohydride
• O oxygen delignification stage
• hyphen (-) indicates a washing stage.
• the Z stage should preferably be preceded by a peroxide (P) or pressurized peroxide (PO) stage.
• the pulp pH is not allowed to rise to well on the alkaline side between ozonation and treatment with oxidizing bleaching agent in order to avoid the dissolution of carbohydrates that would result at alkaline pH from the formation of alkali- labile groups through the reactions of ozone.
• the pH should preferably be kept between 2 and 8, the preferred pH being around 4.5 - 8 at the start and about 2.5 - 6 at the end.
• Ozone treatment and treatment with an oxidizing bleaching agent are performed either in the same bleaching stage or in different stages.
• Ozone treatment and treatment with an oxidizing bleaching agent can be carried out more or less simultaneously, or else the pulp can first be treated with ozone and then with an oxidizing bleaching agent.
• the simultaneous use of ozone and peroxy acid has not been found to cause any problems.
• the total oxidation equivalent to be used in bleaching is divided more or less equally between ozonation and peroxy acid treatment. Accordingly, ozone normally accounts for 30 - 90 % (preferably about 40 - 70 %) of the oxidation equivalent used in bleaching, while the peroxy acid accounts for 70 - 10 % (preferably about 60 - 30 %) of the oxidation equivalent used in bleaching.
• the oxidizing bleaching agent used according to the present invention is a peroxy acid such as a lower peroxy alkanoic acid, more particularly performic acid, peracetic acid or perpropionic acid, or peroxomonosulphuric acid (Caro' s acid) or mixtures thereof.
• Peracetic acid which is a particularly suitable peroxy alkanoic acid, is prepared by reacting acetic acid with hydrogen peroxide in the molar ratio 1:1 - 1 :2 with a small amount of sulphuric acid as catalyst. Peracetic acid is used either as an equilibrium product or in distilled form. Typical conditions for a peracetic acid stage are: peracetic acid charge 2 - 40 kg/BDt, pH 3 - 8, temperature 50 - 90 °C and reaction time 30 min - 6 hours. If necessary, the peracetic acid stage can include additives, e.g. magnesium sulphate and/or a chelating agent such as EDTA or DTP A, at the rate of 0.5 - 3 kg/BDt. Particularly suitable conditions for a peracetic acid treatment are: pH 4.5 - 7, reaction time 30 - 180 min, and temperature 50 - 80 °C.
• ozone stage typical conditions include a pulp consistency of 1 - 40 % (i.e. low, medium or high consistency).
• the ozone gas used for bleaching is a mixture of ozone and oxygen, usually containing 5 - 15 % ozone.
• the optimum pH for ozonation is between 2 and 5, preferably about 3.
• the pH is usually adjusted with sulphuric acid, although organic acids can also be used.
• a higher pH (5 - 10) can be employed. However, in this case some of the ozone decomposes and the charge therefore has to be increased to make good the loss.
• the temperature in the ozone stage can be 0 - 80° C. In industry, ozonation is performed at a temperature of around 50 -
• a high temperature has the same kind of impact as high pH.
• the ozone charge is
• the pulp is washed with water between the ozone and peroxy acid stages until it appears neutral or only slightly acidic. This washing further reduces the content of dissolved carbohydrates, improves both tear index and brightness, and appears to lower the content of carbonyl groups. Washing can be carried out in the usual way in one or more stages, with the water displaced from the pulp between washing stages by filtration.
• the pulp going forward to the alkali stage has a carbonyl group content of at least 10 %, usually at least 15 %, less than the pulp coming to the ozone stage.
• the alkaline treatment stage following the peroxy acid stage comprises any known treatment stage in which the pH of the pulp is made alkaline, i.e. raised to a pH of at least 8, preferably of around 10 - 12.
• Suitable alkaline stages include alkaline extraction (usually abbreviated E), possibly incorporating treatment with another chemical such as borohydride (R) or peroxide (P); an oxygen stage (O), a hydrogen peroxide stage (P, PO), and combinations thereof.
• E alkaline extraction
• R borohydride
• P peroxide
• O oxygen stage
• P, PO hydrogen peroxide stage
• the conditions for the alkaline stage correspond to those in known bleaching sequences.
• the borohydride charge is usually about 0.1 - 10 kg/BDt.
• the amount of peroxide used is generally 5 - 60 kg/BDt (0.5 - 6 %), which may be divided between the peroxide stage preceding ozonation and the peroxide stage following peroxy acid treatment.
• one preferred embodiment of the invention would be as follows: ozone stage using approx. 1 - 8 kg ozone/BDt (0.1 - 0.8 %), peroxy acid stage using approx. 1 - 30 kg peroxy acid/BDt (0.1 - 3 %), peroxide stage preceding ozonation using approx. 5 - 30 kg hydrogen peroxide/BDt (0.5 - 3 %), and peroxide stage following peroxy acid treatment using approx. 1 - 20 kg hydrogen peroxide/BDt (0.1 - 2 %).
• the pulp to be subjected to ozone bleaching may be chemical, chemi-mechanical or mechanical pulp.
• One very common type of pulp in this context would be oxygen- delignified sulphate pulp, more particularly oxygen-delignified softwood pulp.
• the pulp may be subjected to other treatments with agents such as enzymes, complexing agents and peroxide, depending on the treatment stages following ozonation. Examples of bleaching stages that may be used prior to ozonation include the following sequences:
• the pulp entering the ozone stage generally has a kappa number of about 2 - 16, preferably about 2 - 10.
• the treatment specified in the present invention yields a pulp with good strength characteristics and, depending on the bleaching sequence used, an ISO brightness of at least 85 units, usually over 87 units.
• the pulp has a kappa number of less than 2, in some cases under 1.8, a viscosity greater than 620 ml/g (closer to 700 ml/g, depending on the temperature of the peroxy acid stage), a tear index (T70) of over 14 mN-m 2 /g and a zero- span tensile index (T70), measured from wet sheets, of over 105 N-m/g.
• the zero-span tensile index (wet sheet) can be raised to almost 115 N-m/g by washing the pulp between the peroxy acid stage and the alkali stage.
• the tear index is preferably over 14.5 mN-m 2 /g.
• the bleaching sequences specified in the invention can be made part of cycle closure. This especially applies to sequences that do not contain a separate complexing agent stage (Q).
• the filtrate from the alkaline extraction stage is recovered and returned, at least in part, to pulp cooking, oxygen delignification or bleaching.
• One preferred embodiment is an alternative in which the alkali stage is performed after peroxy acid treatment without intermediate washing, whereby the filtrate from the alkaline extraction stage contains at least some peroxy acids, which form hydrogen peroxide. This filtrate can be recycled direct to oxygen delignification and to suitable peroxide stages.
• a sequence according to the invention can be used, such as OOXPaa/Z/Paa/O, where X represents an enzyme treatment.
• the principal enzymes used are hemicellulase or ligninase types such as xylanases and/or mannanases and laccase.
• the PO pulp had a kappa number of about 6, a brightness of about 75 % and a viscosity of 760 - 790 ml g.
• the pulp was then bleached using sequences according to the invention and also with reference sequences, as follows: Z-P, Z/Paa-P, Z-Paa-P, Z/D-P, Z/R-P and
• D-EOP-D Calculated in terms of oxidation equivalents, the same amounts of chemicals were charged to the Z, Z/Paa, Z-Paa and Z/D stages, i.e. 625 kg OXE/BDt. Based on the total OXE charge, the amount of ozone used was 50:50 in relation to the peracetic acid or chlorine dioxide ratio. Based on optimization experiments, the borohydride charge to the Z/R stage was 10 kg/BDt and the ozone charge 5 kg/BDt.
• the bleaching conditions are shown in Table 1.
• the characteristics of the pulps are shown in Table 2. Table 2. Characteristics of the Z, Z/Paa, Z-Paa, Z/D, Z/R and D-EOP-D pulps.
• ozonation causes a doubling of the pulp' s carbonyl content.
• the carbonyl content falls from 15.8 to 12.0 mmol/kg during the Paa treatment subsequent to the Z stage. Washing the pulp between the ozone and Paa stages (Z-Paa) lowered the carbonyl content still further (14.3 to 10.9 mmol/kg) after the Paa treatment.
• the alkali lability of ozone-bleached pulp falls significantly during Paa treatment, which is also reflected in the fact that the difference between borohydride and standard viscosities is only 0 - 20 ml/g.
• Table 4 shows the bleaching results and papermaking characteristics of the pulps at a tensile index of 70 N-m/g (T70).
• Figure 3 presents hydrogen peroxide consumption in the final stage of the sequences Z-P, Z/x-P, ZxP, x/Z-P and Paa-P.
• the Table shows that the strength of the TCF Z pulp can be improved by 13 - 16 % by including in the ozone stage an oxidative treatment at acid conditions with peracetic acid (Paa) or chlorine dioxide (D), or reduction with borohydride (R) without intermediate washing.
• An even better kappa reduction, brightness and tear index than for the Z/Paa-P pulp were obtained with the sequence Z-Paa-P, i.e. with intermediate washing.
• Zero-span tensile indexes measured from wet sheets were 14 - 23 units (15 - 25 %) greater for the Z-Paa-P than the Z-P pulp.
• a mill pulp subjected to the treatment O-Q-O-Pl was bleached using the sequences P-Z-P, P-Paa/Z-P, P-Paa Z/Q-P, P-Z/Paa-P, P-Z/R-P and P-Paa-P.
• the high carbonyl content of the Z pulp is clearly reflected in the difference between borohydride and standard viscosities, which was 60 ml/g.
• the corresponding difference in the case of the Z/Paa and Z/R pulps was much smaller (0 - 20 ml/g).
• the tear index of Z/PaaP pulp bleached using the sequence according to this invention is 1.2 units higher than that of pulp bleached with the reference sequence ZP.
• the bleaching experiments according to the invention were performed on softwood sulphate pulp with a kappa number of 16 and a viscosity of 810 ml/g that had been oxygen-delignified (O) at the mill.
• the pulp was subjected to chelation with EDTA
• the hydrogen peroxide charge in the peroxide stage was 20 kg/BDt (consumption 13 kg/BDt), the alkali charge 20 kg/BDt, pH 10.5, temperature 80 °C, reaction time 180 min and pressure about 6 bar.
• the additives were DTPA (5.5 kg/BDt) and MgSO 4 (2.5 kg/BDt). The kappa number was reduced to 5.6 by this treatment.
• Ozone bleaching (Z) was performed at medium consistency with an ozone charge of 0.5 kg/BDt (consumption 3.6 - 4.0 kg/BDt) at 50°C and pH 3.
• the peracetic acid stage (Paa) was carried out, without washing, using a distilled peracetic acid product with charges of 5, 15 or 20 kg/BDt (consumption 5, 10 and 12 kg/BDt) at 70 °C and pH 5 using a reaction time of 180 min.
• the NaOH charge was 20 kg BDt, which raised the pH to 10.5.
• the reaction time was 60 min and the temperature 70 °C.
• the E stage was boosted with a small (3 kg/BDt) peroxide charge (Ep stage).
• borohydride 0.5 kg/BDt was used in the E stage.
• the E stage was replaced by a peroxide stage (P) without intermediate washing, the hydrogen peroxide charge being 10 kg/BDt (consumption 5 kg/BDt).
• Peroxide (P stage) was used for final bleaching.
• the pulp viscosities resulting from said reducing (R) and (Paa) stages according to the invention are shown in Table 9.
• the method according to the invention can be used in environment-friendly processes in order to assist water cycle closure in a bleaching plant without the need for chelation and/or treatment of the acid filtrates.
• the use of ozone and peracetic acid together in the same stage was tested using the sequences O-O-Paa/Z/Paa and O-O-Z/Paa/E.
• As neither bleaching sequence involves a peroxide stage (P or PO) there is no need for a separate chelation stage or the special treatments that such a stage necessitates.
• Another advantage of this type of sequence is that it does not increase the sulphur load to the recovery system because pH adjustment is performed with peracetic acid instead of sulphuric acid.
• the bleaching results obtained are presented in Table 10.
• Table 10 Results from environment-friendly bleaching sequences O-O- Paa/Z/Paa and O-O-Z/Paa/E.
• Starting pulp O-O pulp, kappa no. 8.2, brightness 51.7 % and viscosity 780 ml/g.
• FIG. 6 shows the carbohydrate contents of the bleaching filtrates individually and in total per tonne of bleached pulp.
• use of the sequences according to the invention roughly halves the amount of carbohydrates found in the filtrates. Replacing some of the ozone charge with peracetic acid reduces the amount of oxalic acid formed through ozone reactions, thus easing the problem of oxalate precipitation. No oxalate precipitation occurs in Paa bleaching.
• the present invention is thus particularly useful in helping to achieve water cycle closure at pulp mills.
• Table 11 presents the optimum pH range for a combined ozone and peracetic acid stage (Z/Paa), though without restricting the invention to this.
• Z/Paa peracetic acid stage
• Experiments were performed using a softwood sulphate pulp pre-bleached using the sequence O-O-Q-(PO) to kappa number 5.5 and 74 % brightness. Final bleaching was performed with the sequence Z/Paa/E.
• the ozone charge was 5 kg BDt and the temperature 50 °C.
• the Paa stage was carried out with a peracetic acid charge of 15 kg/BDt at 70 ° C for 180 min.
• Also shown in the Table is the effect on bleachability of a pressurized Paa stage. In this case the ozone charge was only 2.5 kg/BDt, the peracetic acid charge only 10 kg/BDt, the temperature 50 °C and the reaction time 60 min.
• the highest brightness is achieved by performing the Z stage at pH 3.
• the results also reveal that the economic benefit achieved using the invention can be improved not just by omitting washing stages but also by pressurizing the peracetic acid stage. This reduces the amounts of chemicals needed and/or the reaction temperature in the Paa stage and/or the reaction time.
• Oxygen-delignified (O/O) mill sulphate pulp was bleached using different ozone and peracetic acid charges in Q-(OP)-Z/Paa/E p sequences.
• the bleaching conditions are shown in Table 12.
• Figure 8 presents the tear index of Z/Paa/EP pulp at a tensile index of 70 Nm/g for the different ozone and peracetic acid charges. It can be seen that the sequence O/OQ(PO)Z/Paa EP led to tear index values about 2 units higher than with the O/OQ(PO)ZP sequence. The tear indexes compare with those of ECF pulps.
• Figure 9 shows the zero-span tensile indexes (wet sheet) of Z/Paa/E p pulp for different ozone and peracetic acid charges.
• the index reflects the strengths of individual fibres.
• the bleaching process according to the invention also improves the strengths of individual fibres.

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• 1996
  • 1996-11-26 FI FI964715A patent/FI964715A/fi not_active IP Right Cessation
• 1997
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  • 1997-11-26 WO PCT/FI1997/000730 patent/WO1998023811A1/en not_active Application Discontinuation
  • 1997-11-26 AU AU50561/98A patent/AU5056198A/en not_active Abandoned
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