Process for bleaching mechanical wood pulp

Abstract: A paper pulp refining and bleaching process wherein the pulp is treated in a refiner (10,12) with a sodium hydrosulfite bleach liquor in the presence of a strong alkali such as NaOH, whereby bleaching takes place at alkaline pH, preferably 10 to 12. The process is preferably carried out by passing the pulp successively through a primary refiner (10) at elevated pressure, a secondary refiner (12) at atmospheric pressure and a bleaching tower (14), an alkaline hydrosulfite solution being fed to each.

Description: This invention relates to a process for bleaching mechanical wood pulp with sodium hydrosulfite as part of a refining process. In a typical conventional pulp refining process, wood chips or the like are subjected to two or more refining stages, in which they are ground mechanically by rotating grinding wheels or discs and then to a bleaching stage to remove chromophores and increase the brightness of the pulp. The first refining stage is generally carried out using steam at an elevated pressure, suitably 100-200 KPa. The subsequent refining stages can be carried out at atmospheric pressure. The resulting pulp is then subjected to post-bleaching in a tower or chest, at low to medium consistency. The most commonly used pulp bleaching agents are hydrogen peroxide, H 2 O 2 , and sodium hydrosulfite, Na 2 S 2 O 4 , also known as sodium dithionite. Whilst the peroxide generally provides greater brightness gains, it is relatively expensive and the hydrosulfite is therefore more commonly utilized. This compound cannot however be used at high concentration since its decomposition products tend to act as catalysts, promoting the decomposition of the hydrosulfite and inhibiting its bleaching activity. Barton and Treadway, in Pulp Paper 53, No.6. pp.180-181 propose feeding a part of the hydrosulfite to a refining stage before the pulp reaches the bleaching tower. The elevated temperature (typically 145°F, 62.5°C) and high pulp consistency were found to offer considerable advantages, as was the absence of air in a pressurised refiner. Rather than increase the total amount of hydrosulfite used, Barton and Treadway reduced the hydrosulfite concentration in the bleaching tower, splitting the total between the refiner and the tower. Melzer and Auhorn, in a paper given to the Wood Pulp Symposium in Munich in 1985, showed how the total hydrosulfite input could be reduced by feeding the greater part of the hydrosulfite used to the first stage of a two-stage refining process at pH 6, and adding the rest to the refined pulp before it entered a bleaching tower. This also gave a marked saving in energy consumption to produce the same mechanical pulp properties, or improved strength characteristics for the same energy input. No improvement in brightness was noted, however. FR-A-2,367,860 discloses a process for bleaching wood pulp in a refiner, preferably using chlorine dioxide or oxygenated water, with the latter the preferred pH range is 9 to 12. Sodium dithionite is mentioned as a possible alternative bleaching agent. The present invention consists in a process for simultaneously refining and bleaching wood pulp according to claim 1. This process can provide pulp of improved brightness without the need to increase significantly either the energy input or the overall amount of hydrosulfite used. The pH of the bleaching solution is preferably in the range from 10 to 12. Further bleaching may take place in a second. atmospheric refiner and/or in a bleaching tower. The total amount of hydrosulfite used in preferred processes in accordance with the invention need not exceed 1 wt.%. Adding the hydrosulfite to a primary pressurized refiner alone, an additon rate of 0.3 to 2% has been found to give a brightness gain of 10 points, while a similar gain can be obtained from a 1% overall addition split between the primary reactor and a secondary (atmospheric) reactor. For example, a 6 point brightness gain has been obtained with a hydrosulfite charge to the primary refiner of 0.25 to 0.50%, with a further 4 points gained by feeding the remaining 0.75 to 0.50% to the secondary refiner. The refining zone presents an efficient mass transfer system (i.e. vigorous mixing) as well as an air-free environment that contributes to an increased effectiveness of bleaching. The resulting higher temperature and higher consistencies presumably increase the bleaching reaction rate that reduces the lignin chromophores. The continual fracture of wood produces new surfaces and continually exposes the lignin chromophores to reduction. The strong alkali in the bleach liquor stabilizes the hydrosulfite and neutralizes the wood acids as they are released from the wood chips. Preferred processes in accordance with the invention as will be shown, have given brightness gains in the range 10 to 13 points. Typical tower bleaching of softwood TMP results in brightness gains of 6 to 8 points. A chelating agent may be added to the system before or during refining, such as ethylene diamine tetraacetic acid (EDTA) or Diethylene tetramine pentaacetic acid (DTPA). Preferred embodiments of the present invention will now be described with reference to the accompanying drawings wherein: Figure 1 shows schematically a process in accordance with a preferred embodiment of the invention; Figure 2 shows how the brightness gain obtained from the primary refiner varies with the pH of the bleach liquor; Figure 3 shows the effect of the NaOH concentration, based on the pulp, on the brightness gain in the primary refiner; Figure 4 shows how the brightness gain obtained from the primary refiner varies with the hydrosulfite concentration in the refiner; Figure 5 shows the relationship between the brightness gain in the primary refiner and the pH of the pulp leaving the refiner; Figure 6 illustrates the effect of post-bleaching on pulp leaving the primary refiner; Figure 7 shows brightness gains obtained by bleaching in the secondary refiner and by post bleaching and Figure 8 shows how the brightness gain varies with the distribution of hydrosulfite input between primary and secondary refiners, with and without post-bleaching. Referring first to Fig.1., pretreated wood chips are fed to a primary refiner 10 where they are milled at elevated pressure. The high-concentration thus produced is then fed to a secondary refiner 12 which is at atmospheric pressure. Finally the pulp is fed to a bleach tower 14 for post bleaching. At each of these three stages, an alkaline bleach liquor is added from a source 16. A series of trials was carried out to establish the optimum conditions for the process of the invention. The experimental details of these trials are as follows: MECHANICAL PULPING: Refining was done in a Sunds 20 inch (50.8cm) single rotating disk refiner, having a production rate of approximately 1Kg OD pulp/min. The primary refiner (OVP-20) was steam pressurized at 136 KPa (20 psi). Before refining, the wood chips (Swedish Spruce) were treated with 0.3% DTPA, steamed in a preheater (124°C) for 3 minutes and discharged into the refining zone. Dilution water was fed to the eye of the refiner by metering pumps. The resulting pulp had a freeness of approximately 350 ml CSF, and 18% consistency. For the bleaching runs, hydrosulfite solution was prepared at the required concentration and substituted for the dilution water. Secondary refining (ROP-20 Refiner) was carried out at atmospheric conditions. Coarse pulp from the primary refiner was fed to the secondary refiner via a calibrated conveyor. The CSF freeness and consistency after the secondary stage were 150 ml and 19% respectively. Bleaching in the secondary refiner was done in the same manner as in the primary stage. POST BLEACHING: Pulp for bleaching was collected from either refiner stage and stored in heavy gauge plastic bags. Brightness determination of the refined pulp was done immediately after refining. Post-refiner bleaching was performed using the equivalent of 7 g OD pulp in polyethylene bags. The pulp was diluted with hot (65 °C) deionized water to 3% consistency, sealed and mixed to disperse the fiber. The required amount of hydrosulfite was added under nitrogen purge, the bag was sealed, thoroughly mixed and placed in a constant temperature bath at 60°C for 60 min. At the end of the bleaching period, each bag was removed from the constant temperature bath, mixed, opened and the pH measured. The pulp was then diluted to 1% consistency with deionized water and the slurry adjusted to pH 4.5 prior to handsheet formation. Duplicate handsheets (3.5 g each) were made and air dried overnight at 50% relative humidity. Brightnesses were read on an Elrepho brightness meter and the ISO brightness reported as an average of five readings for each handsheet. BLEACH LIQUOR GENERATION: Sodium hydrosulfite was produced in a Ventron Borol® Bleach Generating Unit from Borol® Solution and a solution of sodium bisulfite fortified with SO 2 . The generated hydrosulfite concentration was 10%. Typically fifteen liters at the required hydrosulfite concentration was prepared from the generated hydrosulfite solution. The pH of the liquor was adjusted by adding NaOH to the required pH. The concentration of hydrosulfite was checked by iodometric titration. In a first series of trials, the effect of hydrosulfite bleach liquor pH was investigated. The results are illustrated in Fig.2. and the data summarized in table 1. To obtain maximum brightness in a pressurized refiner, alkali is provided to neutralize acidic components that are generated during refining from the extractives and resin present in softwoods. As shown in table 1 and Fig.2, the maximum brightness, a 10 point gain, was obtained with bleach liquor that has been adjusted to pH 10 to 12 with caustic soda. Table 1 also shows the concentration of caustic soda used in each case. The variation in brightness gain with NaOH concentration is illustrated in Fig.3. Table 1 and Fig. 3 suggest that under the conditions investigated no more than 1 wt.% NaOH should be used, the optimum occurring in the range of 0.8 to 1.0 wt.%. In a second series of trials, the amount of hydrosulfite added to the primary refiner charge was varied from 0.1 to 1.0 wt.% based on OD pulp. The results are shown in table 2, which also gives the constant reaction conditions, and in Fig. 4 of the drawings. As can be seen from Table 2 and Fig.4, a maximum gain of 10.3 brightness points above the unbleached brightness was obtained at a treat level of 0.3% hydrosulfite. Increasing hydrosulfite above this level resulted in decreased brightness presumably because of the high level of caustic soda present. This demonstrates that reductive bleaching carried out in the refining zone is more efficient than conventional low consistency bleaching, suggesting that continuous fracturing of wood exposes chromophores that are readily accessible to reduction by dithionite anion, probably via the sulfoxylate radical anion. These gas-solid reactions are exceedingly rapid and very efficient; hence achieving a large brightness gain for a small amount of hydrosulfite expended. While condensation reactions of lignin during refining can result in the further formation of chromophoric groups in the pulp, reduction of these chromophores may occur in situ because of the presence of dithionite thus minimizing their effect on brightness. In addition the refining zone is oxygen free and the decomposition of hydrosulfite by air oxidation is thereby minimized. Although not thoroughly investigated, there appears to be a pressure optimum. Increasing the pressure in the primary refiner to 204 KPa (30 psi) resulted in only a 5 point brightness gain compared to 10 point brightness gain at 136 KPa (20 psi). One can hypothesize that a threshold limit for hydrosulfite stability has been approached at this elevated pressure (temperature) and insufficient hydrosulfite is available for bleaching. Good bleaching practice also dictates that the post bleaching should be optimized. Fig.5 illustrates the effect of end bleached pH on brightness point gain. The uppermost curve represents primary refiner bleached pulp treated with 0.3% hydrosulfite and bleach liquor pH adjusted to 10 and 12 respectively. Here the maximum brightness gain, 13.5 points, was obtained at an end pH of 5.0, and a total hydrosulfite charge of 0.6%. Where the bleach liquor was adjusted to a pH 13.5, the optimum pH was found to be 5.8, and the overall brightness gain was only 11 points for the equivalent total hydrosulfite applied. These results are also set out in Table 3. In practical applications of refiner bleaching, pulp bleached in the refiner system must have the latency removed, be screened and cleaned before it is utilized in the paper making area. Some brightness reversion will occur on these processing operations. The effect of post bleaching on final pulp brightness is shown in Figs.6 and 7. Fig. 6 illustrates the bleach response at optimized conditions for both the primary refiner bleaching and post bleaching. Brightness gains in the range of 10 to 13.5 points can be obtained with the hydrosulfite level currently used in low consistency bleaching. An added benefit may be that under refiner bleaching conditions relatively lower levels of hydrosulfite are applied and thiosulfate formation should be minimized. However this still remains to be evaluated. As has been mentioned above, a chelating agent can also be used. High usage rates of organic chelant such as DTPA or EDTA should however be used with caution since they are alkaline solutions. Their contribution to the overall alkalinity should not exceed the alkalinity limit set by an optimized refiner bleaching system. SECONDARY REFINER (ATMOSPHERIC) BLEACHING. Hydrosulfite bleaching under atmospheric refining conditions was also investigated. Since the primary refiner and secondary refiner were not interconnected, pulp from the primary refiner was hand carried in plastic bags to the conveyor system feeding the secondary refiner. All bleaching done in the secondary refiner used hydrosulfite bleach liquor adjusted to pH 10. No pH optimization studies were carried out. The result (Fig.7, main curve, and table 4) shows modest brightness gains (2 to 4 points) from the secondary refiner. Post bleaching contributed an additional 6 brightness points when 1.0% hydrosulfite was used. Thus overall brightness gain of 8 to 10 points were achieved at applied hydrosulfite level (0.5% to 1.0%) typically used in conventional hydrosulfite bleach systems. The post bleaching results are shown in Table 5 and in three broken lines in Fig. 7. The reduced brightness gain during secondary refiner bleaching can be attributed to insufficient alkalinity. This is demonstrated (table 4) by the more acidic (pH 4.4) discharge pulp pHs. As shown in the primary refiner, caustic should preferably be added at a level such that the refiner discharge pulp pH is in the range of 5.0-5.5. It is assumed that more acidic conditions must have been present in the secondary refining system. At the high temperature in the refining zone significant quantities of hydrosulfite may have decomposed resulting in a minimum number of chromophores being reduced and hence lower brightness. In a final series of trials, a total hydrosulfite charge of 1% was split between the primary and secondary refiners in different ratios. Fig. 8 shows the results obtained without post bleaching and with post bleaching with additional hydrosulfite inputs of 0.5 and 0.75%. For comparison, the results obtained with primary refiner bleaching alone, at charges from 0.3 to 1.0%, are also shown. In appears from Fig.8 that the total hydrosulfite charge should preferably be split at a ratio between the primary and secondary refiners from 70:30 to 60:40. It is believed that by stabilizing the hydrosulfite against decomposition, the process of the invention also helps to reduce chemical attack on the apparatus and other problems caused by the decomposition products of sodium hydrosulfite.

Claims: A process for simultaneously refining and bleaching wood pulp in a refiner wherein wood chips or wood pulp and an aqueous alkaline bleaching solution are fed to the refiner, characterised in that at least one stage of said refining and bleaching process takes place in a primary pressurized refiner, in that said bleaching solution comprises a solution of sodium hydrosulfite and sodium hydroxide having a pH of 10 to 13.5 and is fed to the refiner to concentrations of not more than 2 wt.% of sodium hydrosulfite, based on oven-dried pulp, in that sodium hydroxide is added to a concentration, based on oven-dried pulp, of 0.8 to 1 wt.%, and in that the pulp is discharged from said primary refiner at a pH in the range 5-6. A process as claimed in claim 1 wherein the bleach liquor has a pH of 10 to 12. A process as claimed in claim 1 or claim 2 wherein after leaving the pressurized refiner the pulp is subjected to further bleaching in an atmospheric refiner and/or a bleaching tower. A process as claimed in any preceding claim wherein not more than 1.wt.% of sodium hydrosulfite is added, based on oven dried pulp. A process as claimed in any preceding claim wherein a chelating agent is added to the system before or during refining. A process as claimed in claim 5, wherein the chelating agent is ethylene diamine tetraacetic acid (EDTA) or diethylene tetramine pentaacetic acid (DTPA). A process as claimed in claim 1 which comprises the steps of: feeding wood chips to said pressurized refiner and milling said wood chips at elevated pressure to produce a pulp; feeding said bleaching solution to said pressurized refiner during said milling; discharging said pulp from the pressurized refiner at a pH from 5 to 6, passing said pulp to a secondary refiner and further refining said pulp in said secondary refiner at atmospheric pressure; adding further said bleaching solution to the pulp in said secondary refiner; passing the pulp from said secondary refiner to a bleaching tower; and bleaching said pulp in said bleaching tower with more of said bleaching solution.

Inventors: EDSTROM BERT ARNE, JOACHIMIDES THOMAS, LEVIS STEVEN H, MOLDENIUS HANS BERTIL STEVE, EDSTROM, BERT ARNE, JOACHIMIDES, THOMAS, LEVIS, STEVEN H., MOLDENIUS, HANS BERTIL STEVE
Applicants: MORTON INT INC, VALMET FIBERTECH AB, MORTON INTERNATIONAL, INC., VALMET FIBERTECH AKTIEBOLAG
Application year: 1989
Main classification: D21B1
IPC codes: D21B1, D21C9