Process for preparing a paper web

Abstract: The present invention concerns a process for preparing a paper web. According to the process a pulp is formed from a fibrous raw material, a web is formed from the pulp and it is dried on a paper machine. According to the invention the pulp is formed from a mechanical pulp produced from a peroxide bleached mechanical wood raw material of the genus Populus, the pH of stock of the mechanical pulp being set at 6.8 to 7.2 and the machine pH at 7.1 to 7.5 and the conductivity of the stock being set at 1000 to 1500 µS/cm. By using a relatively low pH value and a narrow pH range it is possible to reduce the sensitivity to disturbances of the paper making process. According to the present invention a mechanical aspen pulp can be combined with chemical pulp for preparing base paper of fine paper, whereby the mechanical pulp gives a high conductivity on the machine which improves the stability of the wet end and enhances water removal.

Description: The present invention concerns a process according to the preamble of claim 1 for producing a paper web. According to a process of this kind a fibrous raw material is slushed and the stock obtained is formed into a web which is dried. In paper making, mechanical pulps are used for, e.g., newsprint and SC and LWC papers. Compared to chemical pulp the particular advantage of mechanical pulps are their lower production costs and greater yields. Entirely new fields of applications are also being found for mechanical pulps, in particular hardwood pulps. In connection with the present invention it has been found that by using mechanical pulps made from aspen it is possible to manufacture qualities of fine papers that are essentially better than the present ones. At the same time, this leads to conditions of web formation that are, however, distinctly more difficult than for conventional fine papers and for newsprint prepared from spruce. The present invention relates to the control of these web forming conditions. In comparison to chemical pulps there are some considerable problems relating to mechanical pulps, such as high concentrations of LC substances (liquid and colloidal substances), amounting to 2000 to 8000 mg/l (when purely chemical pulps are used the corresponding amounts are 500 to 1000 mg/l). The high concentrations of disturbing substances increase the risk of disturbances to runability. The concentrations of lipophilic extractives which are particularly troublesome as regards runability are four times, or even up to seven times larger in bleached mechanical pulps than in chemical pulps. The lipophilic extractives are the main cause for most of the precipitates, stains and hole on a paper machine. The brightness of a paper containing mechanical pulps is lower and the brightness stability poorer than for a traditional fine paper containing solely chemical pulps. The large concentration of fines in the mechanical pulps is both an advantage and a disadvantage. It renders the paper a good bulk, because it has a large scattering capacity, and it gives the paper high opacity, but for the runability of the paper machine a high fines concentration is a disadvantage. The fines have a large specific surface which consumes a lot of the various paper chemicals, both process chemicals and functional chemicals. It is also necessary to use large amounts of chemicals in webs containing abundant amounts of fines in order to control dewatering. The fines have a large specific surface and they impair dewatering of the web during paper manufacture. The risk of pitch trouble increases in particular in the presence of bivalent or multivalent metal ions. These are capable of precipitating pitch already at small concentrations. In particular calcium gives rise to problems in processes wherein calcium carbonate has been used as a filler or a coating pigment and when mechanical pulp is employed. Mechanical pulps are produced from softwood, primarily spruce, and to a lesser extent from hardwood, such as aspen (lat. Populus tremula ). The pulps produced from different wood species contain varying amounts of lipophilic extractives. The extractives concentration of bleached spruce groundwood (PGW) is about 0.30 to 0.35 % and of bleached aspen pressure groundwood 0.60 to 0.70 %. Also the composition of the extractives is different for hardwood and softwood. Thus, spruce groundwood contains large amounts of free resinous acids, free fatty acids, fatty acid esters and free and esterified esters. The composition of the lipophilic extractives of aspen groundwood differs from that of spruce. In the extractives fraction of aspen groundwood the fatty acid esters dominate, there are only small amounts of free fatty acids and no resin acid can be found in the extractives of hardwood. Because of the high concentration of extractives in mechanical aspen pulp, mechanical pulps produced from aspen have been considered to involve great runability risks. There are also other problems associated with the use of aspen in paper making. The stone cells of the inner layer of the bark, i.e. the sclerides, have made it difficult to use aspen in chemical pulps and problems have also been cause by bark trash of aspen pressure groundwood. Furthermore, some 24 to 26 % of the aspen cells are vasculum cells, which increase the risk of runability problems when using aspen pulp. The small vasculum cells of aspen have been found to cause spot and stain formation on the web. In comparison to spruce, hardwood have a higher water retention (WRW) and the smaller fibres give a denser web. Both these factor reduce the dewatering of the web. The benefit of aspen compared to spruce is its lower lignin concentration which gives a higher brightness and improved brightness stability. Aspen would therefore be an interesting wood raw material in pulp making but for the above reasons and because of the smaller strength of aspen in comparison to spruce, the use of aspen has not increased in mechanical pulps. The relative of aspen, the poplar (lat. Populus balsamea ), is to some extent employed for production of groundwood pulps in Northern America, but the same kind of runability problems also appear in connection therewith. It is an object of the present invention to eliminate the problems related to the prior art and to provide an entirely novel solution for utilizing mechanical pulp produced from aspen in paper making, in particular for production of a base paper for a new generation of fine papers. In particular, the present invention concerns a solution for controlling the clearly more difficult web forming conditions of aspen. Higher brightness and brightness stability are required of fine papers. On a higher brightness level it is more critical to control e.g. the formation of stains and spot caused by pitch. The invention is based on the following surprising findings, which have made it possible substantially to improve the runability of aspen mechanical pulp on a paper machine. The amounts of organic matter dissolving from groundwood and other mechanical pulp and the variations of these amounts can be restricted by maintaining the pH of the paper machine relatively low and within a relatively narrow range. In addition to the low pH it is further possible to limit the amount of soluble total organic matter (COD) and the amount of organic anionic impurities by maintaining a relatively high conductivity. The relatively low pH and the relatively high conductivity are particularly advantageous as regards the pitch substance which disperses into water from aspen groundwood. According to Sundberg et al. (K. Sundberg, J. Thornton, R. Ekman, B. Holmbom, Nord. Pulp Pap.Res.J. 9 (1994) 2, 125 - 128) dispersion of pitch from pulp to water is promoted by the fact that the carbohydrates dissolving in water from pulp (spruce groundwood - TMP) sterically stabilize the pitch dispersion. When operating a process according to our invention the high conductivity restricts the solubility of the organic substance and when the concentration in water of the substance which stabilizes the pitch dispersion drops, it reduces the amount of pitch dispersing into water. We have also found that, depending on the specific application, the peroxide dosage needed for bleaching aspen groundwood is substantially smaller than the peroxide dosage for spruce groundwood, which also by itself reduces the amount of water-soluble substance. Surprisingly the concentration of extractives on the surface of the bleached aspen groundwood (coverage of extractives) is not higher than for spruce groundwood, even if the total concentration of extractives in aspen groundwood is about twice that of spruce groundwood. Concerning runability it is also essential to control dewatering. The use of aspen groundwood involves a significant risk in this respect because its fiber size is small and generally the water retention of hardwood pulps is greater for them because of their characteristic carbohydrate composition than for softwood pulps. By means of the present invention it has become possible to avoid both of these factors which cause risks to runability. First, when aspen groundwood was prepared as described in Example 1, it was surprisingly found that the Freeness of aspen groundwood could be left on a higher level than is required from a spruce groundwood produced for the corresponding purpose. This is because the aspen groundwood contains only small amounts of shives and coarse fibers which would have required processing into a low Freeness. Secondly, dewatering of a paper web containing aspen groundwood is significantly promoted when the wet end is operated in complience with the present invention. When chemical aspen pulp is used for manufacturing traditional fine papers, the vasculum cells of aspen give rise to spots and stains on the paper machine. The defoaming agents used for controlling the process appear to cause flocculation of small vasculum cells. These flocs bind loosely to the surface of the paper web and then attach to the roll surfaces of the press section or to the cylinder surfaces of the drying section generating light spots on the surface of the paper. When these spots are examined under a microscope, flocs of vasculum cells can be found. Surprisingly, when mechanical aspen pulp is used no flocculation of vasculum cells has been noticed. This is probably because the physical (stiffness) and chemical (more hydrophobic surface) properties of mechanical fibers are different from those of the fibers in chemical pulps. More specifically, the process according to the invention is mainly characterized by what is is stated in the characterizing part of claim 1. The present invention provides considerable advantages. Thus, by using a relatively low pH and a narrow pH range, the sensitivity to disturbances of the papermaking process can be reduced, because the amount of dissolved disturbing substances drops and the variation of the amount grows smaller. Paper is produced in a system which is in a constant state of interaction and change, whereby the present method, i.e. the operation of the machine, which includes the above-mentioned characteristics creates a stable and readily controllable situation. In comparison to the manufacture of traditional fine paper, the conductivity of the stock is kept on a high level of 1000 to 1500 µS/cm. Salts, in particular monovalent alkali metal ions, such as sodium and its salt derived from bleaching of the aspen pulp are responsible for the increase of the conductivity. The conductivity correlates with the sodium concentration of the process water. At high electrolyst concentration and high conductivity levels, variations in the electrolyst concentration (and conductivity) does not cause variations in the chemical phase equilibriums of the wet end nor is their influence on the dewatering on the paper machine as large as when operating at low conductivities (300 to 600 µS/cm of traditional fine papers). It is particularly advantageous to operate at high relative conductivity in connection with a mechanical aspen pulp having a high concentration of extractives. The high conductivity reduces the amount of carbohydrates dissolving from the pulp into water and, this way, also the amount of dispersing lipophilic extractives. For bleaching of aspen groundwood, the required peroxide dosage is much smaller than for spruce groundwood, which reduces the amount of water solubles. The amount of extractives on the surface of the bleached aspen groundwood (the coverage of extractives determined by ESCA) is not higher than for spruce groundwood. The combination of high conductivity, narrow pH range and the small amounts of bivalent ions create stable conditions at the wet end of the paper machine. Since the pH is over 7, calcium carbonate and similar calcium salts can be added as fillers and on the paper web without a substantial increase of the calcium concentration in the wire water. The present invention utilizes softwood fibers having a small fiber size for paper making. The dewatering of the prepared paper web is, however, by no means poor. On the contrary, a web containing aspen pulp is more readily dewatered than a web containing spruce groundwood. Surprisingly, it has been found that aspen can be ground to a higher Freeness level because smaller amounts of shives and coarse fibers are formed therefrom during grinding. Furthermore, in comparison to the manufacture of traditional fine papers, the relatively high conductivity promotes and stabilized water removal. According to a preferred embodiment of the invention, a mechanical pulp of aspen is combined with a chemical softwood pulp for preparing base paper for fine papers. Traditionally fine papers have been made entirely from chemical pulp. In comparison with this kind of fine paper making, the bleaching of the mechanical aspen pulp will give the machine a high conductivity level, which improves the stability of the wet end. It promotes water removal and increases stability of water removal. When a stock is produced containing about 30 to 60 wt-% aspen pulp having a brightness of 81 to 85 %, the conductivity is about 1100 to 1600 µS/cm, which is clearly higher than for a conventional fine paper process (300 to 600 µS/cm). The fact that the aspen pulp is readily dewatered makes it possible to achieve a surprisingly high, up to 48 %, dry substance content after the press section. This improves runability of the drying section, which minimizes the tacking risks and steam requirements and increases the capacity of the paper machine. With the aid of the invention it is possible to control the pitching problem much better with aspen than with spruce ground wood. In summary, it should be pointed out that by the present invention relating to controlling of the chemistry of the wet end of the mechanical aspen pulp is is possible much better to control the runability of the paper machine, in particular when preparing a base paper for fine papers having high brightness and high opacity. Retention and the anionic character can be controlled by substances known per se. By means of the invention the aqueous amounts of LC substances and in particular lipophilic extractives which are detrimental to the runability of the machine can be restricted and the properties of the aspen pulp can be optimized by controlling the grinding and refining so that excellent dewatering can be reached. A more stable and more easily steered process is obtained. The invention also comprises the improvement of the dewatering of hardwood pulps by control of the electrolyst concentrations of process water. According to recent studies the electrolyst concentration/conductivity has a greater influence on the behavior of hardwood pulp, on the water retention of the pulp, than softwood pulp. Further it has been found possible to remove the sclerides which are known to be problematic and surprisingly the vasculum cells of mechanical aspen pulps do not cause any runability problems under these conditions. The invention significantly improves the possibilities of using mechanical aspen pulp for producing fine papers having high brightness and opacity. The invention will be examined more closely with the aid of a detailed description and with reference to a number of working examples. Figure 1 depicts the COD of aspen ground wood vs. pH and conductivity, Figure 2 shows the LC turbidity of aspen ground wood vs. pH and conductivity, Figure 3 shows the anionic character of aspen ground wood vs. pH and conductivity, Figure 4 shows the dewatering time of mixtures of mechanical spruce and aspen pulps, respectively with chemical pine pulp vs. grammage of paper sheet measured with a DDA, and Figure 5 depicts the dry matter contents of mixtures of mechanical spruce and aspen pulps, respectively with chemical pine pulp vs. grammage of paper sheet measured with a DDA. According to the invention, the pulp is produced from P . tremula , P. tremuloides, P balsamea , P . balsamifera , P . trichocarpa or P . heterophylla ., in particular aspen (trembling aspen, P. tremula ; Canadian aspen, P. tremuloides ), or aspen varieties known as hybride aspens produced from different base aspens by hybridizing as well as other species produced by recombinant technology, or poplar. The raw material is used for producing groundwood (GW) or pressure groundwood (PGW) or it is disintegrated to form chips and the chips are used for producing thermomechanical pulp (TMP) of chemithermomechanical pulp (CTMP) by methods known per se. Preferably the mechanical aspen pulp contains about 10 to 20 % of +20... +48 mesh fibers, which confer mechanical strength to the pulp. In order to maximize light scattering, the portion of +100, +200 and -200 fractions should be as large as possible. Preferably they stand for distinctly more than 50 % of the whole pulp. In particular their proportion of the whole pulp is over 70 %, preferably over 80 %. On the other hand, the amount of the smallest fraction, i.e. the -200 mesh, should not be too large, because then dewatering on the paper machine would become more difficult. Preferably the proportion of this fraction is smaller than 50 %, in particular 45 % or less. The mechanical pulp is bleached after grinding or refining, respectively. Preferably the pulp is peroxide bleached at alkaline conditions. According to a preferred embodiment the pulp is bleached with a one, two or multistage bleaching sequence, the pulp being acidified between the bleaching stages and the peroxide residue being reduced. Generally the peroxide dosage is about 2 to 3.5 weight-% of the dry matter of the pulp, for aspen pulp 0.5 to 1.5 %, in particular 0.7 to 1.2 %. A dithionite bleaching step comprising the treatment of the pulp with Na 2 S 2 O 4 can be incorporated into the peroxide bleaching sequence. The mechanical pulp is washed before bleaching and after the bleaching with a mixture of water from the pulping section and clarified water from the paper machine in a washing press (filter press) by using typically about 0.1 to 10 m 3 water per ton of pulp. Water is removed from the pulp with the washing press, in order to increase the dry matter content of pulp from about 4 to 5 % to about 20 to 30 %. The effluent of the water removal are recycled to the mechanical pulp production. By means of the washing press impurities can be prevented from being transferred to the paper machine. We have found that there is a linear correlation between the conductivity of the pulp and the Na concentration. The dosages of bleaching chemicals and the displacement ratio during washing regulate the conductivity level on the paper machine. The sodium ions are accompanied by silicates which also have an influence on the conductivity. The bleached pulp is then refined to the desired degree of beating, which is, e.g. 30 to 100 CSF, preferably about 40 to 80 CSF. A stock is formed from the mechanical pulp together with a chemical pulp. The stock can contain other fiber materials and additives, such as fillers. Calcium carbonate, talcum and kaolin are examples of fillers. The dry matter content of the stock is about 0.1 to 5 %. Clarified filtrate of a circulating water of the paper machine is used as the aqueous phase of the stock. A fully bleached chemical softwood pulp is preferably added to the stock, whereby a paper web suitable as a base paper of fine papers is obtained. Said web has high bulk, high brightness and high opacity and good formation. The amount of the mechanical pulp is then for example 20 to 70 weight-%, preferably 30 to 60 weight-%, and the amount of the bleached softwood pulp is for example 80 to 30 weight-%, preferably 70 to 40 weight-% of the dry matter of the stock. The pH of the proportioning stock (i.e. the pH of the stock pumped to the paper machine) is set at 6.8 to 7.2, preferably the pH of the stock is 7.0 to 7.2, and the pH of the machine pulp at 7.1 to 7.5, preferably at about 7.1 to 7.3. If necessary a suitable base or acid is used for setting the pH of the stock and for adjusting the pH during paper making. The bases used comprise in particular alkali metal bicarbonates or carbonates and alkali metal hydroxides. The acids used include mineral acids and acid salts. The preferred acids are sulphuric acid and its acid salts such as alum, and the preferred base is sodium bicarbonate. A paper web is produced from the fibrous stock on a paper machine in a manner known per se. A preferred embodiment comprises in particular producing a base paper of fine papers having the following composition: 30 to 50 weight-% of its fibrous subtance comprises mechanical pulp produced from aspen and 70 to 50 weight-% comprises chemical softwood pulp. The solution according to the invention is particularly well suited to coating wherein calcium carbonate is used as a pigment of the coating colours. In particular, the calcium carbonate has a steep particle size distribution The following non-limiting examples illustrate the invention: Example 1 Manufacture of aspen groundwood on a pilot apparatus Pressure groundwood was prepared with a pressurized PGW70 process. The pulps were ground with a grinding stone having an average grain size of 73 mesh. The grindings were carried out with a one oven pilot grinder. The grinder was operated using the following settings: Inner pressure of grinder: 250 kPa, Flow of water jet: about 3.5 l/s (aimed consistency about 1.5 %) Temperateur of water jet: 70 °C The ground pulp was processed to a finished, bleached and postrefined pulp. The processing was performed sequentially as follows: Mainline screening; High-consistency refining of reject in two stages; Screening of refined reject; Combination of mainline and reject line accepts; Two-stage bleaching with peroxide + dithionite; Postrefinings The screening of the pulp was made using fractionating slit screening technique. The refining of the reject was carried out at high consistency in two stages. In both refining stage the reject was precipitated before grinding with a twin fabric press and diluted after the grinding with the effluent of the press. The reject refiner was provided with knives for high-consistency refining of pulp. Samples were taken after both refining steps. After the first step the sample was subjected to disintegration on a sample web and after the second step the disintegration was made in a container. The paper technical properties were only determined from the sample taken after the second refining step. The screening of the refined reject was made in a manner known per se. The pulps were bleached with a two-stage peroxide and hydrosulphide bleaching in two batches. First the pulp which were to be bleached were precipitated on a belt filter, and then they were fed to a high-consistency refiner operated with a rather large knife slit which was used as a chemical mixer. The peroxide solution which contained all bleaching chemicals was fed as screw water of the feed screw of the refiner. From the refiner the pulp was filled into large sacs in which the pulp was kept for about two hours. The aimed bleaching chemical dosage (90 % of production) was: H 2 O 2 1.5 %, usually 0.8 - 1 % NaOH 1.0 % Na 2 SiO 3 3.5 % DTPA 0.5 % DTPA was dosed mixed with the bleaching liquid. The acidification of the pulp was carried out with a 93 % sulphuric acid which was diluted with water at the ratio 1:10. The diluted acid was dosed to the bleaching pulp 8 1 per sac. From the slushed and acidified pulp, CSF, shives, BmcN-fractions and brightness were determined. During double-bleaching the peroxide residue was reduced after acidification by adding to the pulp in a pulper 1.33 kg sodium sulphite per sac. Then the pH was set at 6.5 by adding 50 % sodium hydroxide. In the previous test runs the aimed pH was 6.0. After this, a 10 % Na 2 S 2 O 4 solution was added for performing the dithionite bleaching. The dosing was 0.6 %. From the second bleaching batch pulp and paper technical properties were determined after double bleaching. The postrefining was carried out at low consistency with a Tampella T224 disc refiner. The pulp was refined at about 70 kWh/t specific energy consumption. The drainage of the finished pulp was 50 ml CSF. The fiber size distribution of the pulp was the following: Fiber fraction Percentage +14 0 % +28 1.6 % +48 16.0 % +200 43.0 % -200 39.4 % Example 2 Runability of aspen groundwood The amount of COD dissolving from the pulp prepared in Example 1 as a function of pH and conductivity was examined in this example. The results are given in Figures 1 to 3. Figure 1 depicts in the form of a bar chart the amount of soluble COD's at pH 7.2, 7.6 and 8.1 for two different conductivity levels, viz. 520 and 1600 µS/cm. A corresponding presentation of the influence of pH and conductivity on LC turbidity is shown in Figure 2 and on the anionic character in Figure 3. As Figure 1 shows, as pH rises the amount of dissolved COD grows and at low conductivity more impurities are dissolved than at higher conductivity. Similarly an increase of pH leads to a corresponding increase of the amount of anionic substance dissolved from aspen groundwood (cf. Figure 3). At low conductivities the amount of dissolved anionic substance is greater than at higher conductivity. Low pH, narrow pH range and high conductivity decrease the sensitivity of the process to disturbances beacuse the amounts of liquid and colloidal disturbing substances are smaller. Figure 2 shows the dependency of LC turbidity on pH and conductivity. There is a linear correlation between LC turbidity measured from the centrifugated filtrate with the concentration of pitch present in the solution in the form of a stable dispersion. It is apparent from the figure that there are less pitch substances dispersed in water at higher conductivities than at lower conductivities. Example 3 Dewatering of mixed pulp Dewatering of mixed pulps containing spruce and aspen groundwood, respectively, were compared using the Dynamic Drainage Analyzer technique (DDA) as follows: The chemical pulp was a bleached pine kraft which had been refined in two different ways: as such (not fractionated) and fractionated with separate refining of the accept and reject fractions. The drainage resistance of the pulp comprising mixtures of separately refined accepts and rejects was the same as for the refined non-fractionated pulp, i.e. 340 ml (CSF). The drainability of the spruce groundwood was <20 ml CSF and that of aspen groundwood 33 ml CSF. Pulp mixtures containing 60 % chemical pulp, 40 % groundwood and about 10 % carbonate filler (Filler L) and 0.8 % pulp starch. The pH of the pulps was in the range of 7 to 7.5 and the conductivity 400 to 500 µS/cm, which value was adjusted, if necessary, by adding NaCl. The dewatering times and the dry matter concentration of the sheet was determined by the DDA technique. The Dynamic Drainage Analyzer apparatus is used for simulating dewater on the wire section (to the water level) of the paper machine. The results are shown in Figures 4 and 5. As will appear from the figures, spruce groundwood gives essentially longer dewatering times than aspen groundwood. The dry matter content of a paper sheet made from aspen groundwood is clearly higher than for spruce groundwood. The results indicate that the dewatering properties of a paper web comprising mechanical aspen pulp, and thus the runability properties, are better than for a traditional spruce groundwood based paper. Example 4 Production of a base paper for fine papers A base paper was produced from a mechanical aspen pulp (GW) and chemical pine pulp, which were mixed at a weight ratio of 40 to 60. Ground calcium carbonate was added as a filler to the stock in an amount of about 10 % of the fibrous material. The base paper was produced on a gap former. The properties of the base paper were the following: grammage 53.3 g/m 2 bulk 1.45 cm 3 /g opacity 88 % brightness 82.5 % coarseness 240 ml/min porosity 170 ml/min filler content 12 % No problems with the runability of the base paper were encountered.

Claims: Process for preparing a paper web, according to which process a stock is formed from a fibrous raw material, a web is formed from the stock, and the web is dried, characterized in that the stock is formed from bleached mechanical pulp prepared from wood raw material of the Populus family, the pH of the stock being adjusted to 6.8 to 7.2 and the pH of the machine pulp being adjusted to 7.1 to 7.5 and the conductivity of the stock being adjusted 1000 to 1500 µS/cm. The process according to claim 1, wherein the pH of the stock is set at 7.0 - 7.2. The process according to claim 1 or claim 2, wherein the mechanical pulp is groundwood (GW), pressure groundwood (PGW), thermomechanical pulp (TMP) or chemimechanical pulp (CTMP). The process according to claim 3, wherein the mechanical pulp is peroxide bleached. The process according to any of the preceding claims, wherein a suspension is formed from the mechanical pulp, containing talcum, kaolin or calcium carbonate as a filler and having a dry matter content of about 0.1 to 5 %. The process according to any of the preceding claims, wherein the suspension is formed from mechanical pulp and bleached chemical softwood pulp. The process according to claim 6, wherein the amount of the mechanical pulp is 20 to 70 wt-%, preferably 30 to 60 wt- %, and the amount of chemical softwood pulp is 80 to 30 wt-%, preferably 70 to 40 wt-%, of the dry matter of the stock. The process according to any of the preceding claims, wherein the mechanical pulp is washed before and/or after bleaching, whereby the consistency of the pulp is raised from 4 to 5 % to a level of 20 to 30 %. The process according to claim 8, wherein the mechanical pulp is washed and dewatered on a fabric press. The process according to claim 8 or claim 9, wherein the water from the dewatering are recycled back to the preparation of the mechanical pulp. The process according to any of the preceding claims, wherein alkali metal hydroxide, alkali metal bicarbonate or mineral acid or an acid salt are used, if necessary, for adjusting the pH of the suspension. The process according to any of the preceding claims, wherein the mechanical pulp is manufactured from P. tremula , P . tremuloides , P balsamea , P . balsamifera , P . trichocarpa or P. heterophylla . The process according to any of the preceding claims, wherein the paper web is coated with a coating colour containing calcium carbonate. The process according to claim 13, wherein the paper web is coated with a coating colour containing a pigment having a steep particle size distribution.

Inventors: AENAES EEVA, LESKELAE MARKKU, NYGARD STINA, PITKAENEN MAIJA, AENAES, EEVA, LESKELAE, MARKKU, NYGARD, STINA, PITKAENEN, MAIJA, Änäs, Eeva, Leskelä, Markku, Pitkänen, Maija
Applicants: M REAL OYJ, M-REAL OYJ
Application year: 1998
Main classification: D21C9
IPC codes: D21H19, D21H21, D21C9, D21H23, D21B1, D21F11, D21H11