Improvements in a process for delignifying lignocellulosic pulp by means of oxygen

Abstract: The present invention refers to an improvement for delignifying a lignocellulosic pulp by means of oxygen wherein ethanol is used as an additive and the process is carried out at high temperature thereby obtaining a higher reduction of lignin content of the lignocellulosic pulp, that is, a higher reduction of the Kappa Number in comparison with conventional processes without, however, prejudicing the pulp quality. The use of the present invention provides a pulp which, when subjected to subsequent bleaching sequences, will require a lower amount of chloro compounds in order to achieve the desired whiteness and will also exhibit a high viscosity thus rendering a product with good resistance properties.

Description: Technical Field The present invention refers to an improvement in a process for delignifying lignocellulosic pulp by means of oxygen, and more specifically, to an improvement in a process for delignifying lignocellulosic pulp by means of oxygen with the addition of ethanol. Background Art In conventional processes, bleaching of chemical pulps is carried out mainly by employing chlorine-containing compounds such as molecular chlorine, chlorine dioxide and hypochlorites, thus resulting in a corrosive, chlorine-enriched and hardly recoverable effluent, which has a high degree of environmental deterioration. In view of that and due to more rigorous environmental controls, there is nowadays a great interest in employing bleaching agents, which reduce the amount of chloro-compounds used in bleaching to the minimum so as to recover the major portion of the effluent. A bleaching agent exhibiting such properties is oxygen and, in recent years, its use has substantially increased. Through an initial delignifying stage with oxygen in an alkaline medium in a multistage bleaching sequence of, for example, a kraft pulp, the discharge of effluent from the bleaching plant can be reduced to half, due to the fact that effluent from the oxygen delignifying stage, which does not contain chlorides, is entirely recoverable. Reduction of effluent discharge during treatment with oxygen would be higher when the amount of lignin removed during oxygen delignification is higher than the usual 40-50%. This delignifying limit is a function of the low selectivity of oxygen as a delignifying agent, which is caused by the presence of free radicals derived from oxygen during reaction, thus reducing the cellulose chain lengths. Such a reduction is usually characterized by increased reduction of the pulp viscosity after oxygen delignification. Formation of these free radicals is increased by the presence of certain transition metals found in the pulp, wherein their removal or inactivation enhances the process efficiency. It is verified from the state of the art that magnesium salts have a very positive effect on preventing cellulose chain degradation during treatment with oxygen possibly due to inactivation of transition metals, as well as the combination of magnesium salts with chelating agents, e.g.triethanolamine plus magnesium, is also substantially effective in maintaining the pulp viscosity. Chelating agents, for example, DTPA, EDTA, HEDTA and NTA, in the absence of magnesium, have shown to be inefficient in maintaining pulp viscosity. Removal of transition metals by treating the pulp with acids or chelating agents prior to delignifying the pulp with oxygen renders good results, but it requires additional installations for the bleaching process. The use of other additives, such as tin and manganese salts have relatively succeeded. A typical bleaching sequence for removing lignim from lignocellulosic material, for example, kraft pulp of conifers or foliage, is (C+D) (E+O) DED, where (C+D) is a chlorine/dioxide stage, (E+O) is is oxygen-reinforced alkaline extraction stage, D is a chlorine dioxide stage and E is a single alkaline extraction stage. In this sequence, the main oxidizing components are chlorocompounds which produce dangerous organochloro-compounds in the effluent from the bleaching process, which are measured by calculating TOCl (total organic chlorine) or AOX (absorbable organic halogens). The need for chlorine-based compounds to bleach brown chemical pulps, for example, kraft, sulfide and organosolvent, and, consequently, the amount of TOCl and AOX discharged into the effluent from the bleaching is directly proportional to the lignin content of the pulp derived from the baking operation. Thus, the purpose of subjecting the brown pulp to various treatments prior to the bleaching operation is to reduce lignin content of the lignocellulosic material to the maximum so that, in the subsequent bleaching sequences, the smallest possible amount of chlorine-based compounds is consumed. A treatment which has been successfully used in the brown pulp is thus called oxygen delignification which due to the low oxygen selectivity, reduction of the Kappa Number of the pulp (indirect measurement of lignin content in the brown pulp) is generally limited to, e.g. in the case of kraft pulp of foliage, from 40-50% and of kraft pulp of conifers, from 45-50%. Increasing environmental pressure against the use of chlorine-based compounds has, however, led to several changes in the convention oxygen delignifying process aiming at obtaining a more significant reduction of the Kappa Number. Thus, when, during the oxygen delignifying process, the reaction temperature is increased from the usual 95-105°C to 120°C, reductions of the Kappa Number higher than 50% can be achieved for foliage and conifer kraft pulps. However, this gain in the delignifying rate of lignocellulosic material occurs in parallel with an accentuated reduction of the pulp viscosity, i.e., in a decrease of the process selectivity if carbohydrate protective additives are not used. Some additives which are commonly employed for maintaining the viscosity during oxygen delignifying processes, for example, magnesium salts, have been verified to be inefficient when the process is carried out at temperatures higher than 100°C. On the other hand, some other additives are not compatible with recovery of the effluent from the oxygen delignifying process, which is one of the great advantages of the process. From FR-A-2 189 572, a process for bleaching cellulosic pulp with oxygen and alkali is known, in which delignification of high consistency pulp is carried out using small amounts of additive, for instance ethanol, at a high pressure. However, the known process makes no provision for delignifying medium consistency pulp combining large additive amounts, very basic conditions, high temperatures and low pressures, without pulp degradation (reduced viscosity) caused by the low selectivity of oxygen as a delignifying agent. Therefore, it is an object of the present invention to provide an improvement in oxygen delignification which, without prejudice to the pulp amounts, leads to reductions of the lignin content in the lignocellulosic materials, which are higher than those attainable with conventional oxygen delignifying processes. It is another object of the present invention to provide an improvement in an oxygen delignifying process so that pulp viscosity is maintained even when the oxygen delignifying process is performed at elevated temperatures. Summary Of The Invention These and other objects are achieved by the present invention through the use of an additive, which under certain process conditions, during oxygen delignification of the lignocellulosic material, oxygen is made to act more efficiently, as can be inferred from a higher reduction of lignin content in the lignocellulosic material, i.e. a higher reduction of the Kappa Number, as compared with conventional techniques, without, however, prejudicing the quality of the pulp whose cellulosic chains are preserved from the action of free radicals derived from intermediates of the reaction of oxygen with the pulp and with transition metals. Consequently, the use of the invention renders a pulp which in the subsequent bleaching sequences will need a smaller amount of chloro compound to attain the desired whiteness and, as a function of that, a smaller discharge of TOCl or AOX in the effluent from the bleaching plant and will exhibit a high viscosity, since it will contain long chains of carbohydrates, thus resulting in a product having good resistance properties. Furthermore, as the employed additives are compatible from the recovery point of view, the use of the invention allows a more closed system in the bleaching plant and the additive can be partially recovered for reuse, which makes the process more economical. Detailed Description According to the present invention as defined in claim 1, the additive used is ethanol and its dosage may vary from 10 to 20% by weight, wherein preferably 20 weight percent is added to the pulp, whose consistency may vary in a range of from 8-15%, the characteristic range of a pulp of middle consistency prior to the first bleaching stage, possibly immediately after the brown pulp storage tank, together with alkali, which can be sodium hydroxide, oxidized white liquor and/or non-oxidized white liquor, wherein the pH is adjusted to a range between 7 and 13, more preferably to a range between 11 and 12, the additive-containing pulp being fed to a mixing apparatus to which oxygen is added at a pressure varying from 0.196-0.588 MPa (2-6 kgf/cm2), preferably at a pressure of 0.392 MPa (4 kgf/cm2), and then the pulp is passed to a pressure reactor where the delignification in the presence of oxygen takes place, at a temperature of from 100-120°C, wherein the high temperature range of 120°C is preferable, for a period of time that can vary from 10 to 120 minutes, preferably 60 minutes. The alkali used in the process of the invention is preferably sodium hydroxide as per claim 3 and is added in the amount stated in claims 4 and 5. To evaluate the effects of adding ethanol to the process for delignifying with oxygen a lignocellulosic material in comparison with the conventional processes, examples and respective tables with experiment results will be shown hereinbelow, which are intended to illustrate the application of the invention and not to limit same. Kappa Numbers, viscosity and whiteness of the pulp were calculated in accordance with the standard procedures of the "Technical Association of Pulp and Paper Industry (TAPPI)" and delignifying efficiency values and selectivity coefficient were determined in accordance with equations 1 and 2, respectively: EQUATION 1 Delignifying Efficiency (%)= (Initial Kappa Number - Kappa Number after treatment) X 100 Initial Kappa Number EQUATION 2 Selectivity Coefficient = Delignifying Efficiency % Initial viscosity - Viscosity after treatment X 100 Initial viscosity Example 1 This example illustrates the temperature effect on the efficiency of an industrial process for delignifying, with oxygen, a kraft pulp wherein the experiments were carried out without the use of an additive, with the use of ethanol as an additive in accordance with the invention,and with the use of magnesium as an additive. The sample consisted of a kraft pulp of conventional eucalyptus having a consistency of 12%, which, prior to treatment, had a Kappa Number of 16.7, viscosity of 30.8 cP and whiteness of 33.8°Iso. The reaction time was 60 minutes, using 15 kg O 2 /ton of kraft pulp, partial pressure of oxygen equal to 0.392 MPa (4 kgf/cm2), 20 weight percent of ethanol and 0.5 weight percent of MgSO4.7H20. Experimental results are shown in Table 1 as follows: Example 2 This example illustrates the ethanol feedstock effect on the efficiency of industrial oxygen delignification of a kraft pulp in accordance with the present invention. A sample of kraft pulp of conventional eucalyptus having a consistency of 12%, which prior to treatment had a Kappa Number of 16.7, a viscosity of 30.8 cP and a whiteness of 33.8°Iso was used. The reaction time was 60 minutes, using 15 kg O 2 /ton of pulp, O 2 partial pressure of 0.392 MPa (4 kgf/cm2) at a temperature of 120°C. Experimental results are shown in Table 2 as follows: Example 3 This example illustrates the oxygen partial pressure effect on the industrial oxygen delignification of a kraft pulp in accordance with the present invention. A sample of conventional eucalyptus kraft pulp having a consistency of 12%, which prior to treatment had a Kappa Number of 16.7, a viscosity of 30.8 cP and a whiteness of 33.8°Iso was used. The reaction time was 60 minutes, using 15 kg O 2 /ton of pulp, 2 weight percent of sodium hydroxide, 20 weight percent of MgSO4.7H20 at a temperature of 120°C. Experiment results are shown in Table 3 as follows: Example 4 This example illustrates the alkali feedstock effect on the efficiency of the oxygen delignification of an industrial kraft pulp in accordance with the present invention in comparison with conventional processes wherein treatment involves the use of magnesium as additive. A sample of conventional eucalyptus kraft pulp having a consistency of 12% which prior to treatment exhibited a Kappa Number of 16.7, a viscosity of 30.8 cP and a whiteness of 33.8°Iso was used. The reaction time was 60 minutes, using 15 kg O 2 /ton of pulp, an O 2 partial pressure of 0.392 MPa (4 kgf/cm2), 20 weight percent of ethanol and 0.5 weight percent of MgSo4.7H20 at a temperature of 120°C. Experiment results are shown in Table 4 as follows: As can be seen from the experimental results of Example 1 (Table 1), the use of ethanol as additive in the lignocellulosic pulp oxygen delignifying process of the present invention, provides an increase in the delignifying efficiency, by means of a higher reduction of the Kappa Number and an increase of the process selectivity allowing the process to be carried out at higher temperatures. In experiments in which ethanol was used as an additive, an increase in the process temperature of from 100-120 °C confers a significant increase on the delignifying efficiency to the same alkali feedstock, without, however, causing a significant decrease in the process selectivity. For an alkali dosage of 2% sodium hydroxide, while the delignifying efficiency at 100°C in the absence of additives did not reach 38%, in the presence of ethanol at 120°C this efficiency exceeded 46%, wherein the process selectivity coefficients, at 100°C and at 120°C, were similar. Thus, it is demonstrated that the use of ethanol in the lignocellulosic pulp oxygen delignifying process, in accordance with the present invention, allows the oxygen delignifying process to be performed at higher temperatures resulting in a higher reduction of the Kappa Number without, however, prejudicing the pulp quality. It should be pointed out the low values of selectivity obtained when oxygen delignifying takes place at 120°C in the absence of additives. In the experiments without additives, an increase in the temperature confers an increase on the delignifying efficiency for the same amount of alkali but on the other hand causes an accentuated decrease of the process selectivity, and these results are in conformity with the industrial results where the use of temperatures above 100°C for foliage pulp has been verified to be impracticable due to the low selectivities. Therefore, delignifying efficiency is always limited to a maximum of 40% with said pulps. The use of the present invention enables one to reach delignifying levels above 46%, with good selectivity and working at 120°C. Upon evaluating the ethanol dosage effect on the delignifying efficiency and on the selectivity, it can be inferred, from the results referring to experiments of Example 2 (Table 2), that a variation of the ethanol amount of from 10-20 weight percent causes small increases in the delignifying process efficiency and for a dosage of 20 weight percent the best selectivity coefficient for an alkali dosage of 2% sodium hydroxide was obtained. Evaluating the oxygen partial pressure effect on the delignifying and process selectivity, it can be verified, from the results of experiments of Example 3 (Table 3), that in the pressure range of 0.196-0.392 MPa (2-4 kgf/cm2) good selectivity values are obtained, wherein the best value is achieved at 0.392 MPa (4 kgf/cm2). A comparison between the selectivity values obtained from the use of the process in accordance with the present invention at 0.392 MPa (4 kgf/cm2) and processes in the absence of additives or only using magnesium as additive illustrates the great superiority of the process of the present invention. As can be seen from the results of experiments of Example 4 (Table 4), the use of ethanol as an additive in the ligocellulosic pulp oxygen delignifying process, in the present invention, gives better selectivity results when compared with conventional techniques, i.e., oxygen delignification in the absence of additives or in the presence of magnesium. The process of the present invention rendered delignifying efficiencies above 47%, with selectivity values higher than those obtained with conventional processes. Choice of the most favorable alkali dosage for the oxygen delignifying process of the present invention will depend on the minimal viscosity values which are acceptable by the pulp manufacturing industry. Results shown in Table 4 certainly point out that an increase in the alkali amount enhances the delignifying efficiency with concomitant decrease of the selectvity process, irrespective of the presence or absence of additives.

Claims: A process for delignifying lignocellulosic pulp comprising: (A) providing a pulp having a consistency within the range of from 8 to 15 percent; (B) adding ethanol to said pulp in an amount within the range of from 10 to 20 weight percent, and adding alkali to said pulp in an amount sufficient to produce an additive-containing pulp having a pH within the range of from 7 to 13; (C) thereafter adding oxygen, at a pressure within the range of from 0.196 to 0.588 MPa (2 to 6 kgf/cm 2 ) to the additive-containing pulp to produce oxygenated additive-containing pulp; (D) passing the oxygenated additive-containing pulp to a pressure reactor; and (E) delignifying said oxygenated additive-containing pulp at a temperature within the range of from 100 to 120 º C. Process in accordance with Claim 1, characterized in that the alkali is selected from the group consisting of sodium hydroxide, oxidized white liquor and/or non-oxidized white liquor. Process in accordance with Claim 2, characterized in that the alkali is sodium hydroxide. Process in accordance with Claim 3, characterized in that the amount of alkali is within the range of from 1.5 to 2.5 weight percent of sodium hydroxide. Process in accordance with Claim 4, characterized in that the amount of alkali is about 2.0 weight percent of sodium hydroxide.

Inventors: COLODETTE JORGE LUIZ, SANTOS DE CAMPOS ANA SABINA, COLODETTE, JORGE LUIZ, SANTOS DE CAMPOS, ANA SABINA
Applicants: WHITE MARTINS SA, S.A. WHITE MARTINS
Application year: 1992
Main classification: D21C9
IPC codes: D21C9