The present invention relates to a process for the bleaching of chemical pulp, in which process the pulp is delignified with a peracid and additionally the pulp is chelated in order to bind heavy metals, such as Fe, Mn and/or Cu, into a chelate complex.

In the production of chemical pulp, a cellulose-containing material is cooked with suitable cooking chemicals, and the raw pulp thus obtained is delignified and bleached with oxidizing chemicals. The purpose of the conventional bleaching of chemical pulp is to complete the removal of lignin from the raw pulp obtained from the cook. Chlorine or chlorine dioxide has conventionally been used for bleaching, but recently a shift has increasingly been made to other, replacing bleaching chemicals. The bleaching takes place in a plurality of successive steps, for example so that the first step is an oxygen delignification, whereafter the delignification may be continued by using, for example, ozone, peracetic acid or hydrogen peroxide in acidic or alkaline conditions.

When oxygen-containing bleaching chemicals, such as oxygen, ozone, hydrogen peroxide and peracids, are used, problems are caused by heavy metals present in the pulp; these include in particular iron, manganese and copper, but also, for example, chromium and nickel. These heavy metals enter the raw pulp along with wood, process waters or cooking chemicals, and they catalyze the decomposition of the carbohydrates in the presence of oxygen chemicals, thereby increasing the consumption of the bleaching chemical and deteriorating the quality of the pulp. Furthermore, they cause after-darkening of the pulp. It is possible to remove the heavy metals, for example, by an acid wash preceding the bleaching step, but since the subsequent bleaching step in the bleaching sequence is usually alkaline, an acid wash performed at a low pH will increase the amount of alkali required for the adjustment of the pH. There is the further disadvantage that the acid wash may reduce the strength of the pulp and that earth-alkali metal ions which are regarded as advantageous for bleaching are removed in the wash. Earth-alkali metals, such as magnesium and calcium, stabilize peroxide in peroxide bleaching and protect the carbohydrates of the pulp from decomposition in the oxygen step; for this reason magnesium sulfate is often added to the bleaching steps.

An alternative method for mitigating the disadvantages due to heavy metals is chelating, wherein complexing agents are used as chelating agents. It is assumed that chelating has the advantage over acid wash that calcium and magnesium will better remain in the pulp. Known chelating agents which bind heavy metals include polycarboxylic acids, of which emylenediaminetetraacetic acid (EDTA) and diemylenerriaminepentaacetic acid (DTP A), and salts thereof, are the ones most commonly used.

The chelating of chemical pulp will in general not succeed satisfactorily in alkaline conditions, since iron forms very poorly soluble compounds by precipitating in the form of hydroxides, oxides and oxy hydroxides. When the pH rises above 7, manganese also begins to bind very strongly to the pulp. For this reason, chelating in bleaching has been carried out as a separate step in acidic conditions. Such a separate chelating step is very effective in binding heavy metals, but it neither bleaches the pulp nor deligmfies it; thus it serves only as a preliminary step for the subsequent oxygen chemical step. If the separate chelating step could be replaced by some sufficiently selective delignifying step, for example the kappa number in the cook could be raised owing to the improved delignification and the yield could be improved, or respectively, the delignification could be brought to a further point and higher degrees of brightness could be reached without a reduction of the strength of the pulp.

One delignification process which has been found to be highly selective is based on the use of peracids. In peracid delignification it is possible to use organic or inorganic peracids, of which peracetic acid and Caro's acid are the most commonly used. It has been observed that peracetic acid (PAA) is an especially selective delignification chemical by means of which the strength properties of the pulp can be maintained good. The PAA step is in fact itself not very sensitive to heavy metals, and even moderately high Fe or Mn concentrations do not affect the selectivity of PAA. In the PAA step the iron remains in the form of poorly soluble Fe(III), whereas a considerable amount of manganese dissolves. This released manganese will pass together with the pulp to the subsequent final bleaching with alkaline peroxide, in which manganese has a detrimental effect and before which the pulp must be chelated in order to avoid the said disadvantage. Furthermore, the PAA step removes from the pulp earth-alkali metals, mainly magnesium and calcium, which are useful in further bleaching.

In delignification with peracetic acid, the optimum pH is very close to that (4-6.5) used in the chelating step. However, chelating which binds heavy metals has not been successful in connection with a PAA step, since DTPA and EDTA, the most commonly used chelating agents, form with manganese a complex which decomposes peracetic acid very effectively. Furthermore, if DTPA decomposes in the reactions, large amounts of iron and manganese are left in the pulp; this is detrimental for the subsequent bleaching steps. In the PAA step the final pH is often rather low, approximately 4, in which case large amounts of Mg and Ca dissolve and, as a consequence, the Mg:Mn ratio in the pulp passing to the subsequent step is poor. The wrong metal profile is in general not seen in the pulp properties after the actual PAA steps; the viscosity is at a good level. However, in the subsequent alkaline peroxide step the wrong metal profile causes extra consumption of peroxide and a lowering of the viscosity of the pulp. Thus a separate chelating step between the PAA and peroxide steps has been required; such a step is futile in terms of delignification, but without it the strength of the pulp could be reduced and the con¬ sumption of peroxide could increase considerably in the peroxide step, which is the actual bleaching step.

The object of the present invention is to provide a process in which a chelating which binds heavy metals can be combined with peracid delignification, so that the process will be simpler than previously. The process is based on the use of new complexing agents, and it is characterized in that the chelating is carried out using a chemical selected from a group consisting of N-bis-((l,2-dicarboxy-ethoxy)-ethyl)- amine, N-bis-((l,2-dicarboxy-ethoxy)-ethyl)-aspartic acid and N-tris-((l,2- dicarboxy-ethoxy)-emyl)-amine and their alkali metal salts and earth-alkali metal salts, and that the peracid and chelating treatments aie performed simultaneously by combining the peracid and the said chelating chemical in the same solution phase.

The formulae of the four- and six-branch complexing agents (A, B, C) used as chelating agents in the process are:

A C

COOH

HOOC _x H

. — COOH i, COOH

~~- o- HOOC COOH Y 1 0

/

/

B HOOC, / — ^N

/ ' \

— o - _ / COOH HOOC — ^/ ^ COOH

N-bis-[(l,2-dicarboxy-emoxy)-emyl]-arnine (A) is hereinafter referred to by using the acronym BCEEA, N-bis-[l,2-dicarboxyethoxy)-ethyl]-aspartic acid (B) by using the acronym BCEEAA and N-tris-[(l,2-dicarboxy-ethoxy)-ethyl]-arnine (C) by using the acronym TCEEA.

The achievement of the invention is that peracid delignification, chelating and bleaching, which previously constituted three separate steps in the bleaching process, can be performed during two steps. As the separate chelating step is eliminated, the resources (e.g. a bleaching tower) required by it can be used, for example, for increasing the retention time in some other bleaching step.

The use of the new chelating agents has the additional advantage that, while they chelate iron and manganese sufficiently effectively, they hardly seem to chelate magnesium and calcium.

The peracid used as the delignification chemical may be peracetic acid, performic acid, perpropionic acid or a longer-chain percarboxylic acid. The peracid may also be monopersulfuric acid (Caro's acid) or a mixture of Caro's acid and a per¬ carboxylic acid, e.g. peracetic acid. Persulfates may also be used as a mixture with any of the above-mentioned peracids. It is also possible to use a combination of a peracid and chlorine dioxide, for example peracetic acid and chlorine dioxide simul¬ taneously. According to the invention, preferred peracids include peracetic acid, Caro's acid, or a mixture thereof. Especially preferably it is peracetic acid, the advantage of which over Caro's acid is that peracetic acid can be purified by dis¬ tillation and can be stored for relatively long periods, whereas Caro's acid must be used as an equilibrium solution which contains a large amount of unreacted acid. A large amount of unreacted acid complicates pH control.

The process according to the invention can be used advantageously in connection with ozone delignification in which part of the delignification is carried out with a peracid, such as peracetic acid. The process exploits the neutralization step following the ozone step, in which case the metal profile of the pulp can be adjusted so as to be suitable for further bleaching. At the same time part of the delignification work and the removal of the chromophores from the pulp can be left for the peracetic acid and/or chromophores may be removed from the pulp, whereby the further bleaching is facilitated. On the other hand, the strength of the pulp is also improved when part of the delignification is left for a peracid which is more selective than ozone.

In ozone delignification the pH is dropped to a very low level. Thereby the earth- alkali metals present in the pulp may be dissolved. Of the heavy metals, manganese is rather easily removed in an acid treatment, but iron is very poorly soluble. The ozonation is followed by a neutralization step. There is no wash between the steps, and thus the heavy metals may become rebound to the fiber. However, this problem can be avoided by using in this step complexing agents according to the invention, by means of which the heavy metals can be chelated into a soluble form.

It has further been observed that, if the pH of the neutralization step according to the invention, comprising a peracid delignification and chelation, is maintained within a suitable range and magnesium sulfate is added to the step, a suitable metal profile for the pulp is obtained before the subsequent alkaline peroxide step, in which case the viscosity of the pulp will remain considerably good in the further bleaching. The viscosities of pulps treated by a prior-known technique may be of the same order after the ozone and PAA steps, but owing to the wrong metal profile they will drop considerably during the subsequent alkaline peroxide step.

According to the invention, the pH of the peracid and chelating treatment step can be adjusted advantageously to a range of approximately 4-8. If the PAA delignification is carried out within a pH range of 4-5, PAA is relatively stable and its delignifying effect is at its best. Within a pH range of approximately 6-8, PAA is not equally stable, but respectively it serves, in addition to delignifying, also as a bleaching chemical. Since, owing to the relatively high price of PAA, it is most profitable to carry out the PAA delignification towards the end of the sequence, preferably immediately before the last alkaline peroxide, PAA can also be used as a bleaching chemical and the actual delignification can be left for the other delig-

nification chemicals, such as oxygen and ozone. A bleaching PAA step may be especially useful when the pulp is difficult to bleach.

There are no limitations on the use of the process in a multistep bleaching sequence; it can be used on a pulp coming directly from the cook, on an oxygen-delignified pulp, or on pulp after any step. The process is especially advantageous for use before alkaline peroxide bleaching.

The process is suitable for use on sulfate pulps and other chemical pulps made from softwood or hardwood or various grasses. The process can also be used for inhibiting after-darkening of bleached pulps.

The invention is illustrated in greater detail with the following examples. It should be pointed out that the mixture of chelating agents BCEEA + BCEEAA according to the invention, used in the examples, contained 18 % BCEEA and 34 % BCEEAA, the balance being mainly water. The doses (kilograms/metric ton of pulp) in the examples have been calculated for all chelating agents as 100 % sodium salts.

Preparation Example 1

A disodium maleate solution was prepared by dissolving 29.4 g (0.3 mol) of maleic anhydride in 50 ml of water and by adding to the reaction mixture 50 g of a 48 % caustic solution (0.6 mol NaOH). During the adding the temperature of the reaction mixture was maintained at 70-90 °C. 17 g (0.05 mol) of lanthanum(III) nitrate, La(NO3)3 ^x ° ^" ^O was added to the reaction mixture together with diethanolamine (10.5 g, 0.1 mol). The reaction mixture was stirred at 85 °C under a reflux condenser for 48 h. The reaction mixture was cooled and was rendered acidic (pH 1.8) by means of a concentrated sulfuric acid. Thereafter the reaction mixture was reheated to 60 °C, and 10 g of oxalic acid and 50 ml of water were added, the mixture was stirred at 60 °C for 20 minutes, and the La(III) oxalate precipitate formed was removed from the hot solution by filtration. The filtrate was cooled, and any precipitate subsequently formed was removed by filtration. The remaining solution (40 ml), which contained 54 % water, was analyzed for organic compounds by means of ^C NMR spectra and a mass spectrometer as silyl or methyl ester derivatives.

BCEEAA and BCEEA were identified from the 13 Q NMR spectrum. The unreacted starting substances were identified on the basis of reference spectra: diethanolamine

and maleic acid, as well as oxalic acid which was used for precipitating the catalyst. Malic acid and fumaric acid formed as byproducts of the reaction; these were also identified on the basis of reference spectra.

On the basis of a quantitative ^C NMR analysis, the composition of the obtained reaction mixture was as follows:

% by weight

BCEEAA 18.5

BCEEA 7.9 diethanolamine 1.2 maleic acid 2.2 malic acid 2.5 oxalic acid 0.3 fumaric acid 2.1 water 54.3

Na ₂ SO ₄ 11.0

The said analysis and the ascertaining of the moleculai- structures of the compounds BCEEA and BCEEAA by gas chromatography and mass spectrometry are described in the priority application FI-962261.

In order to isolate the compounds BCEEA and BCEEAA, a sample (13.25 g) of the reaction mixture obtained as described above was pretreated by adding to it 1.16 g of calcium carbonate. Thereupon the sulfate ions present in the sample precipitated as calcium sulfate.

The ion exchange resin used was a strong anion exchange resin (Bio-Rad AG 1 - X8, 200-400 mesh) in its formiate form. The sample was eluted through an ion exchange column with an eluent (1000 ml), the formic acid concentration of which was increased gradually so that the formic acid concentration of the eluent ranged from 0 to 2 mol/1. During the run, one hundred samples of 10-20 ml were collected and were analyzed by a liquid chromatograph. BCEEA and BCEEAA were isolated from the fractions. The ' C NMR spectra and GC-MS spectra of the reaction products were ascertained by comparing the spectrum data for the purified and isolated reaction products with the spectrum data for the reaction products identified from the reaction mixture. The spectrum data of the purified BCEEA and BCEEAA were found to be identical with those obtained from the reaction mixture.

Preparation Example 2

A magnesium maleate solution was prepared by dissolving 29.4 g (0.3 mol) of maleic anhydride in 50 ml of water and by adding to the reaction mixture 35.0 g of magnesium hydroxide (0.3 mol Mg(OH)2) slurried in 70 ml of water. During the adding the temperature of the reaction mixture was maintained at 70-90 °C. 17 g (0.05 mol) of lanthanum(III) nitrate, La(Nθ3)3 x 6 H2O was added to the reaction mixture together with diethanolamine (10.5 g, 0.1 mol). The pH of the reaction mixture was adjusted to a pH value of 1 1 by an addition of a 48 % sodium hydroxide solution. The reaction mixture was stirred at 85 °C under a reflux condenser for 10 hours. The reaction mixture was cooled and was rendered acidic (pH 1.8) by means of a concentrated sulfuric acid. Thereafter the reaction mixture was reheated to 60 °C, and 10 g of oxalic acid and 50 ml of water were added, the mixture was stirred at 60 °C for 20 minutes, and the formed precipitate was removed from the hot solution by filtration. The filtrate was cooled and any precipitate subsequently formed was removed by filtration. The remaining solution (42 ml), which contained 54 % water, was analyzed for organic compounds by means of 1-^C NMR spectra and mass spectrometer as silyl or methyl ester derivatives.

BCEEAA and BCEEA were identified from the ^C NMR spectra. The unreacted starting substances were identified on the basis of reference spectra: diethanolamine and maleic acid. Malic acid and fumaric acid formed as byproducts of the reaction; these were also identified on the basis of reference spectra.

The organic compound composition of the reaction product was as follows on the basis ofa quantitative ^C NMR analysis:

% by weight

BCEEAA 13.8

BCEEA 4.5 diethanolamine 7.5 maleic acid 2.3 malic acid 1.3 fumaric acid 0.3

Preparation Example 3

TCEEA was prepared by the method described in Example 1 by using triethanolamine (1.0 mol) and maleic anhydride (3.4 mol) as the starting substances.

TCEEA was identified from the ^C NMR spectrum. The unreacted starting substances were identified on the basis of reference spectra: triethanolamine and maleic acid, as well as oxalic acid used for precipitating the catalyst. Malic acid and fumaric acid formed as byproducts of the reaction; these were also identified on the basis of reference spectra.

On the basis of a quantitative ^C NMR analysis, the composition of the reaction product was as follows:

molar %

TCEEA 46.3 triethanolamine 18.5 maleic acid 11.5 fumaric acid 3.2 malic acid 13.5 oxalic acid 6.6

Example 1

The rate of decomposition of PAA in the presence of manganese was measured by using various chelating agents at a pH of approximately 4 and a temperature of 60 °C. Initially the PAA concentration was 2 g/l. The results are shown in Table 1.

Table 1

Chelating agent Chelating agent Residual PAA, % ppm Mn, ppm 5 min 15 min 30 min 60 min

No chelating agent 0.4 93.1 93.0 91.2 87.4

DTPA 140 0.4 13.5 5.5 0.0 0.0

EDTA 140 0.4 8.1 4.3 3.3 0.0

BCEEA + BCEEAA 140 0.4 99.9 97.8 98.1 95.8

The table shows that Mn alone does not decompose PAA very rapidly. DTPA and EDTA complexes decompose it very effectively. On the other hand, the results show the BCEEA + BCEEAA mixture according to the invention even improves the stability of PAA in the presence of manganese.

Example 2

The PAA step of the bleaching of a softwood sulfate pulp having a viscosity of 710 dm^/kg, a kappa number of 6.7 and a brightness of 79.7 % ISO was performed at two different pH values with and without magnesium sulfate by using various chelating agents. The pulp was first chelated as well as possible (chelating agent 2 kg/tp of DTPA, temperature 75 °C, time 60 min, pH 5.5), whereafter 4 ppm of Mn (=4 g of Mn/metric ton of dry pulp) was added to the PAA step. The addition was made in order that the effect of the chelating agents on the PAA conditions would show clearly. In practice pulps often contain more Mn, unless they are separately chelated before the PAA step. Furthermore, in the PAA step more heavy metals are released from the pulp and would require separate chelation. The PAA step was followed by an alkaline peroxide step.

From the results, which are shown in Table 2, it is observed that the elevated final pH (initial pH 7 and final pH approximately 5) yields a clearly better viscosity than does the lower pH (improvement of the order of approximately 100 dm /kg). At the higher pH, a viscosity approximately 40 dm^/kg higher is obtained by means of an addition of magnesium sulfate. The mixture of BCEEA and BCEEAA was the best of the chelating agents. At the lower pH the effect of magnesium sulfate was insig¬ nificant, and even with the use of chelating agents the improvement in the viscosity was only of the order of 30 dm^/kg. It is also to be noted that the viscosities after the PAA step were for all approximately of the same order (700-730 dm ³ /kg). How¬ ever, there are large differences (520-700 dm /kg) in the viscosities after the sub- sequent peroxide step; these are due to PAA steps performed in different ways.

Example 3

The tests measured the combined effect of magnesium sulfate and chelating agents when iron and manganese had been added to the PAA step. The results are shown in Table 3.

Tests 1 and 2 represent the worst and the best combinations when there was Fe 8 ppm and Mn 4 ppm (calculated per dry pulp) in the PAA step. The difference between the viscosities is approximately 250 dm^/kg and between the peroxide consumptions more than 16 kg/metric ton of pulp. In tests 3 and 4, a comparison was made between DTPA and the BCEEA and BCEEAA mixture when the final pH was approximately 4, in the presence of MgSO4 BCEEA + BCEEAA yields a viscosity improvement of an order of only approximately 30 dm^/kg and a peroxide consumption 4 kg/tp smaller. Tests 5-7 compared different chelating agents at an elevated pH when there was 8 ppm of iron in the PAA step. The use of chelating agents improves the viscosity by approximately 100-140 dm ³ /kg, while the consumption of peroxide is lowered by 4-8 kg/tp. This example, also, shows how the viscosities after the PAA step are substantially of the same order (except Test 1, in which it is clearly lower), but after the peroxide step the difference becomes considerably large.

Example 4

In the above examples, rather large PAA and peroxide doses were used, whereby an ISO brightness of 88 % was reached in almost all cases. In this example, a pulp having a viscosity of 710 dπ»3/kg, a kappa number of 6.7, and a brightness of 79.7 % ISO was chelated (2 kg/tp DTPA, temperature 75 °C, time 60 min, pH 5.5), and thereafter the pulp was delignified using a PAA dose of 12 kg and a peroxide dose of 10 kg. With a smaller PAA dose the initial pH may be approximately 6, in which case the final pH will be at a suitable level (final pH approximately 5). 8 ppm FE and 4 ppm Mn (calculated per dry pulp) were added to the PAA step. The results, which are presented in Table 4, show that MgSθ4 improves the viscosity by approximately 20 dm^/kg, while the consumption of peroxide is reduced by approximately the same amount. The BCEEA + BCEEAA mixture yields a viscosity approximately 30 chrP/kg higher than does DTPA. In neither case there is left a PAA residue, since the dose was so small that all of it was consumed. However, when DTPA was used, PAA had decomposed to such a degree that the kappa number remained higher. This is shown in the final brightness and the kappa number.

Example 5

An oxygen-delignified softwood sulfate pulp having after the oxygen step a kappa number of 7.9, a viscosity of 784 dm^/kg and a brightness of 45 % ISO was

bleached using a sequence of -Q-EOP-PAA-PO. In the PAA step, magnesium sulfate was used as a stabilizer with the mixture BCEEA + BCEEAA, with DTPA, and without a chelating agent. The results are shown in Table 5. The results show that BCEEA + BCEEAA together with magnesium sulfate yielded clearly the highest viscosity and the lowest peroxide consumption in the PO step. On the other hand, after the actual PAA step the viscosity differences were small (except for DTPA, with which it was clearly lowered).

Example 6

The raw material used in the example was a softwood sulfate pulp pretreated by chelation before the ozone(Z) step, in which case after chelation the amount of free heavy metal ions present in the pulp was insignificant. The initial kappa number of the ozone step was 6.7, the viscosity was 947 dm^/kg, and the brightness 51.7 % ISO. From the ozone step the pulp was transferred, without a wash, to the PAA step. During the Z and PAA delignification, however, detrimental heavy metal ions are released from the pulp, and in the subsequent alkaline peroxide step they have a disadvantageous effect on peroxide consumption and pulp quality.

As is evident from Table 6 showing the results, clear advantages are gained with the use of a mixture of BCEEA and BCEEAA in the PAA step in terms of both PAA delignification and the functioning of the subsequent alkaline peroxide step (cf. DTPA). An even clearer difference is observed when the results are compared with a Z/PAA-P sequence without a complexing agent.

The table shows that 8 g of Fe/metric ton of pulp and 4 g of Mn/metric ton of pulp were added to the Z step. The additions were made in order that the differences between the different treatment methods would show sufficiently clearly. In the presence of heavy metals, an addition of the BCEEA + BCEEAA mixture to the PAA step improves the result of the Z/PAA step considerably as compared with the reference in which no complexing agent is used. The said mixture also yields a clearly better result than does DTPA if the pulp quality and chemical consumption achieved with the sequence Z/PAA-P is compared in Z/PAA and P steps. In the final viscosities the difference between DTPA and the BCEEA + BCEEAA mixture was small, but with BCEEA + BCEEAA the brightness was higher and the consumption of peroxide was considerably small.

Example 7

A softwood sulfate pulp which had been oxygen delignified and had a kappa number of 9.7, a viscosity of 775 dm /kg and a brightness of 49.3 % ISO was bleached using the sequence PAA-P-PAA-P. The results are shown in Table 7. The results show that a PAA+Q treatment in which the initial pH is 5 yields a clearly lower viscosity than does a treatment in which the initial pH is 7. Regardless of the pH, DTPA yields lower viscosities (Tests 3 and 4) than does TCEEA and a mixture of BCEEA and BCEEAA, but nevertheless somewhat higher than without an addition of a chelating agent. As compared with a chelating agent-free PAA treat¬ ment, BCEEA + BCEEAA at its best yielded a viscosity value 200-280 dm ³ /kg higher, and compared with DTPA the difference was 200-50 dm ³ /kg.

Table 2

PAA

Test batch 1 2 3 4 5 6 7 8 9 10 114 12 13 14

Time, min 90 90 90 90 90 90 90 90 90 90 90 90 90 90

Temperature, °C 80 80 80 80 80 80 80 80 80 80 80 80 80 80

Consistency, % 12 12 12 12 12 12 12 12 12 12 12 12 12 12 pH, initial 7 7 7 7 7 7 7 5 5 5 5 5 5 5 pH, final 54 54 56 51 53 56 52 45 39 43 39 42 42 4

PAA, kg/tp 20 20 20 20 20 20 20 20 20 20 20 20 20 20

MgSO ₄ , kg/tp - 1 1 1 - - - - 1 1 1 - - -

Mn, ppm - 4 4 4 4 4 4 - 4 4 4 4 4 4

DTPA, kg/tp - - 2 - - 2 - - - 2 - - 2 -

BCEEA+ - - - 2 - - - - - - 2 - - 2

BCEEAA, kg/tp

Residual H2O2, kg/tp 14 02 06 08 03 08 09 08 05 07 1 03 08 11

Residual PAA, kg/tp 05 13 04 05 03 04 06 74 59 04 66 31 07 7

Kappa 28 22 35 26 32 34 27 22 21 32 22 21 27 22

Viscosity, dm ³ /kg 731 725 688 726 728 699 732 737 720 667 717 708 620 717

Brightness, % ISO 857 858 847 856 849 852 859 84 837 823 838 838 829 836

Peroxide I i i I 4 i i 1 I i 4 I I I

Time, min 90 90 90 90 90 90 90 90 90 90 90 90 90 90

Temperature, °C 90 90 90 90 90 90 90 90 90 90 90 90 90 90

Consistency, % 12 12 12 12 12 12 12 12 12 12 12 12 12 12 pH, initial 105 105 105 105 105 105 105 105 105 105 105 105 105 105 pH, final 105 107 104 103 105 104 104 104 104 104 105 105 104 105

H ₂ O ₂ , kg/tp 20 20 20 20 20 20 20 20 20 20 20 20 20 20

NaOH, kg/tp 12 12 12 12 12 12 12 12 12 12 12 12 12 12

Residual H2O2, kg/tp 121 32 131 169 102 95 162 101 46 89 71 45 11 10

Residual NaOH, kg/tp 77 73 77 84 8 77 82 63 6 54 6 53 62 72

Kappa 23 17 3 22 26 29 23 17 15 26 16 15 21 09

Viscosity, dm ³ /kg 593 638 624 698 656 585 662 573 540 523 545 540 571 576

Brightness, % ISO 882 891 884 8887 888 888 889 885 89 879 891 894 884 887

Table 3

PAA

Test 1 2 3 4 5 6 7

Time min. 90 90 90 90 90 90 90

Temperature °C 80 80 80 80 80 80 80

Consistency % 12 12 12 12 12 12 12 pH initial 5 7 5 5 7 7 7 pH final 4.2 5.3 4.3 4.3 5.4 5.5 5.6

PAA kg/tp 20 20 20 20 20 20 20

MgSO ₄ kg/tp - 1 1 1 - - -

Fe ppm 8 8 8 8 8 8 8

Mn ppm 4 4 - - - - -

DTPA kg/tp - - 2 - - 2 -

BCEEA + kg/tp - 2 - 2 - - 2

BCEEAA

Kappa 1.8 2.8 2.2 2.3 2.6 2.8 2.8

Viscosity dm /kg 647 707 719 725 707 718 715

Brightness % ISO 82.8 85.1 84.1 84.5 84.3 84.6 84.6

Peroxide I 4 i i I i I

Time min. 90 90 90 90 90 90 90

Temperature °C 90 90 90 90 90 90 90

Consistency % 12 12 12 12 12 12 12 pH initial 10.5 10.5 10.4 10.4 10.5 10.5 10.5 pH final 10.2 10.4 10.5 10.5 10.4 10.4 10.4

H ₂ 0 ₂ kg/tp 20 20 20 20 20 20 20

Residual kg/tp 0.1 16.3 0.9 4.1 4.5 8.4 1 1.6

H ₂ 0 ₂

Kappa 1.3 2.4 1.5 1.5 2.2 2.6 2.4

Viscosity dm ³ /kg 415 673 462 492 455 546 577

Brightness % ISO 89 88.9 88.8 88.8 88.8 88.7 88.7

Table 4

PAA

Test 1 2 3 4

Temperature °C 80 80 80 80

Consistency % 12 12 12 12 pH initial 6 6 62 62 pH final 5 5 52 52

PAA kg/tp 12 12 12 12

MgS0 ₄ kg/tp 1 - 1 -

Fe ppm 8 8 8 8

Mn ppm 4 4 4 4

Chelating agent BCEEA + BCEEAA BCEEA + BCEEAA DTPA DTPA kg/tp 2 2 2 2

Residual H2O2 kg/tp 04 06 07 06

Residual PAA kg/tp 04 05 05 04

Kappa 3 3 4 39

Viscosity dm^/kg 720 734 716 720

Brightness % ISO 846 846 846 846

Peroxide 4 4 4 4

Temperature °C 90 90 90 90

Consistency % 12 12 12 12 pH initial 104 104 104 104 pH final 101 103 102 103

H ₂ 0 ₂ kg/tp 10 10 10 10

NaOH kg/tp 7 7 7 7

Residual H ₂ 0 ₂ kg/tp 84 65 63 50

Residual NaOH kg/tp 39 36 36 39

Kappa 27 26 34 35

Viscosity dm ³ /kg 697 668 669 649

Brightness % ISO 880 880 876 877

Table 5

PO 4 4 4

Time nun 150 150 150

Temperature °C 97 97 97

Consistency % 15 15 15

PH 94 99 97

H ₂ 0 ₂ kg/tp 15 15 15

NaOH kg/tp 8 8 8

0 ₂ bar 6 6 6

MgS0 ₄ kg/tp 1 1 1

Residual H ₂ 0 ₂ kg/tp 13 45 26

Residual NaOH kg/tp 1 18 1

Kappa 16 15 16

Viscosity dm^/kg 561 643 574

Brightness % ISO 858 869 862

Table 6

Table 7

PAA

Test 1 3

Time nun 60 60 60 60 60 60 60 60

Temperature °C 80 80 80 80 80 80 80 80

Consistency % 12 12 12 12 12 12 12 12 pH initial 5 7-75 5 7-75 5 7-75 5 7-75 pH final 43 6 44 59 44 61 45 59

Chelating agent DTPA DTPA TCEEA TCEEA BCEEA + BCEEΛ+

BCEEAA BCEEAA

Dose kg/tp 2 2 2 2 2 2 PAA kg/tp 10 10 10 10 10 10 10 10

Residual H ₂ 0 ₂ kg/tp 04 05 03 07 04 05 04 06 Residual PAA kg/tp 19 07 17 05 2 05 12 07 Kappa 68 69 73 66 74 73 67 68

P 4 4 4 4 4 4 4 4

Time min 90 90 90 90 90 90 90 90

Temperature °C 90 90 90 90 90 90 90 90

Consistency % 12 12 12 12 12 12 12 12 pH initial 104 104 104 104 104 104 104 104

PH final 102 102 101 102 101 101 101 101

H ₂ 0 ₂ kg/tp 8 8 8 8 8 8 8 8

NaOH kg/tp 10 7 95 8 95 7 9 75

Residual H2O2 kg/tp 48 5 44 49 45 54 48 55

Residual NaOH kg/tp 31 32 26 28 27 31 29 33

Kappa 46 53 51 52 52 59 46 51

Viscosity dm ³ /kg 747 768 755 759 747 768 757 764

Brightness % ISO 747 764 738 76 736 754 755 765

PAA 4 4 4 Φ Φ Φ ψ 4

Time nun 60 60 60 60 60 60 60 60

Temperature °C 80 80 80 80 80 80 80 80

Consistency % 12 12 12 12 12 12 12 12 pH initial 5 7-75 5 7-75 5 7-75 5 7-75 pH final 45 6 47 62 47 61 49 62

ChelaUng agent DTPA DTPA TCEEA TCEEA BCEEA + BCEEA+

BCEEAA BCEEAA

Dose kg/tp 2 2 2 2 2 2 PAA kg/tp 10 10 10 10 10 10 10 10

Residual H2O2 kg/tp 06 06 05 22 05 07 08 11 Residual PAA kg/tp 44 08 62 05 42 05 34 11 Kappa 31 39 41 41 41 45 35 39

P 4 4 4 4 4 4 4 4

Time nun 180 180 180 180 180 180 180 180

Temperature °C 90 90 90 90 90 90 90 90

Consistency % 12 12 12 12 12 12 12 12

PH initial 104 104 104 104 104 104 104 104

PH final 99 101 10 101 102 102 101 101

H ₂ 0 ₂ kg/tp 20 20 20 20 20 20 20 20

NaOH kg/tp 13 11 13 12 13 11 13 11

Residual H ₂ 0 ₂ kg/tp 03 56 34 96 85 128 129 134

Residual NaOH kg/tp 2 35 34 61 41 56 57 56

Kappa 15 24 22 29 23 3 21 26

Viscosity dm-' /kg 426 515 503 648 585 675 656 708

Brightness % ISO 874 877 862 868 868 869 875 874