CA2071185C - Process for delignifying lignocellulosic pulp by means of oxygen - Google Patents

Abstract

IMPROVEMENT 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 ligin 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

2~7~8~

IMPROVEMENT IN A PROCESS FO~R DELIGNIFYING
LIGNp~ELkULOSIC PULP ~Y MEANS OF OXY~

Technical Field The present invention refers to an improvement in a process for delignifying lignocellulosic pulp hy means of o~ygen, 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 corrosi~e, 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 e~hibiting such properties is o~ygPn and, in recent years, its use has substantially increased. Thr~ugh an initial delignifying stage with o~ygen 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 ~7~1~5 stage, which does not contain chlorides, is entirely recoverable. Reduction o 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 ~unction of the low selectivity of o~ygen as a delignifying agent~ which is caused by the presence of free radicals derived from o~ygen during reaction, thus reducing the cellulose chain lengths.
Such a reduction is usually characteri~ed by increased reduction of the pulp viscosity after o~ygen del;gnification. Formation of these free radicals is increased by the presence of certain transition metals ound in the pulp, wherein their removal or inactivation nhances the process efficiency.

It is verified from the state of the art that magnesium salts have a veIy positive eff~ct on preventing cellulose chain degradation during treatment with o~ygen 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, ~or 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 o~ygen renders good results, but it requires additional installations for _ 2 ~

the bleaching process. The use of other additives, such as tin and manganese salts have relatively succeeded.
A typical bleaching se~uence for removing lignim from lignocellulosic material, for e~ample, 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 e~traction stage, D
is a chlorine dio~ide stage and E is a single alkaline e~traction stage. In this sequence, the main o~idizing components are chlorocompounds which produce dangerous organochloro-compounds in the effluent from the bleaching process, which are measured by calculating ~OCl (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 ma~imum 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.~. 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 aiminy at obtaining a more significant reduction of the Kappa Number. Thus, when, during the o~ygen delignifying process, the reaction temperature is increased from the usual 95-105C 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 protectiYe additives are not used. Some additives which are commonly employed ~or maintaining the viscosity during oxygen delignify:ing processes, for example, magnesium salts, have been verified to be inefficient when the process is carried out at temperatl~res higher than 100C. On the other hand, some other additives are not compatible with recovery of the effluent frorn the o~ygen delignifying process, which is one of the great advantageæ of the process.
Therefore, it is an object of the present invention to provide an improvement in o~ygen 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 o~ygen delignifying processes.

2071~

It is another object of the present invention to provide an improvement in an o~ygen delignifying process so that pulp viscosity is maintained even when the o~ygen deliynifying process is performed at elevated temperatures.

Summary Of The Inven~iQn These and other objects are achieved by the present invention through the use of an additive, which under certain process conditions, during o~ygen delignification of the lignocellulosic material, o~ygen is made to act more efficiently, as can be inferred rom 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 s~aller amount of chloro compound to attain the desired whiteness and, as a function of that, a smaller clischarge of TOCl or AOX in the effluent from the bleaching plant and will e~hibit 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 or reuse, which makes the process more economical. --2~71~

Detailed Description According to the present invention, the additive used is ethanol and its dosage may vary from 1 to 130 weight percent, preferably from 10 to 20%, wherein pre~erably 20 weight percent is added to the pulp, whose consistency may vary in a range of from 5-30%, preferably in a range of from 8-15%, the characteristic range of a pulp of middle consistency prior to the first bleaching stage, possihly immediately after the brown pulp storage tank, preferably together with alkali~ which can be sodium hydro~ide, o~idized white liquor and/or non-oxidi~ed 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 2-6 kgf/cm2, preferably at a pressure of 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 80-140C, preferably from 100-120C, wherein the high temperature range of 120C is preferable, for a period of time that can vary from 10 to 120 minutes, preferably 6D minutes.
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 e~periment results will be shown hereinbelow, whi~h are intended to illustrate the application of the invention and not to limit same.

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 tTAPPI)" and delignifying efficiency values and selectivity coefficient were determined in accordance with equations 1 and 2, respectively:

. EOUATION 1 Delignifying ~Initial Kappa Number -Efficiency (~) ~appa Number after treatment) X 100 Initial Kappa Number Delignifying Efficiency (%) Selectivity (Inltial VlSCoslty -Coefficient Viscosity after treatment3 X 100 ,.= . _ Initial viscosity 2 ~

Example 1 Th;s e~ample illustrates the temperature effect on the efficiency of an industrial process for delignifying, with o~ygen, a kraft pulp wherein the experiments were carried out without the use of an additive, with the use of ethanol as an additive 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 02~ton of kraft pulp, partial pressure of oxygen equal to 4 kgf~cm2, 20 weight percent of ethanol and 0.5 we.ight percent of MgSO4.7H20. Experimental results are shown in Table 1 as follows:

P ~ ~ ~ ~ ~ I~ O V~ _ ~ ~ ~ r~
q~
~ O
U~ ~

~ U

0 ~1 a ~3 ~o V~ r~O O ~1 It) ~D ~1 ~ 3 ~ O 0\ 3 ~ O ~i ~ U'l :~
O ~ ~ l O CO ~ I~ ~ i O\ ~ r I CO O CO

~O 0 C~ ~ O ~ ~ X U') ~ ~ ~ ~ O QO 00 U~ ~ ~ cr~ ~
--I O o o~ i o o o~ ~ o~ oo a~ 1:0 ~ ~\ 00 00 ~ æ ~ ~
.J ~ O ~ Tl m C7~ 0 Cl~ ~ 0 0 C~ O ~ `~ ~;
O _I ~ O O ~ ~ ~ O _ C~ ~ O O O~ S~ O _ ~ ~OU~U~OU~UlO~n~oU'~u,ou~U~ou~ouo 2 `--g C~ O O O ~ o o g 3 .

0 ~ ~ ~
v~ ~ a a a a GO a ~ a a a .,, ~ r ~ ~ r a a V .u ~ V V Ll V V V V V ~ ~ ~ ~
V ~ ~ W
Q~

18~

Example 2 This e~ample illustrates the ethanol feedstock effect on the efficiency of industrial o~ygen 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 33.8Iso was used. The reaction time was 60 minutes, using 15 kg 02/ton of pulp, 02 partial pressure of 4 kgf~cm2 at a temperature of 120~C. E~perimental results are shown in Table 2 as follows:

v ~
~ ~ ~ O Ul ~ I~ O ~ ~ O 1~ ~ 00 ~ ~ _ c a O~
C o ^ c~ ~o ul l~ u~ o . ~ ~o o ~ o r~
r ~ o ~ ~ a~ ~r ~ oo E~ ~

o ~ ~r ,~ r o oo ~o ~ ~ u~ ~ oo . r o~ u~

3 ~t u~ 00 r~ o~ o o~ ;r cr~ r o oo ~ Ul ~ ~ ~ ~ C~ r ~D eo 3: o~ o o o o o ~ o o o O ~ O o o o o o o U~ o U~ Ul o U~ U~ o U~ U~ o U~ Ul o U~ U~ o Ul Z--o o 9 0 0 0 0 0 9 0 o o o o O O O O O
~s~
V

~ ~ r u~ o ~ c~l ~ ~ u~

- 12 - 2~711~5 Example 3 This example illustrates the o~ygen partial pressure effect on the industrial o~ygen 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 33.8Iso was used. The reaction time was 60 minutes, using 15 kg 02/ton of pulp, 2 weight percent of sodium hydro~ide, 20 weight percent of MgSO4.7H20 at a temperature of 120Co E~periment results are shown in Table 3 as follows:

~ V
V

a~

O C~
al . . . .
t: rl U~ 3 ~O `D
3 ~ ;~

4,, ~O
O _I cl~ .J ~ r~

O L~ , . , . ~D
~ ~' 00 ~ ~ ~ O
.~ ~ ~ ~ ~ C
p ~3 .
~1 ~ ~ C`~ o cr y ~
a~ o o~ _~
l 0 3 ~ O O O O O

o ~ C~ O O O O O
h ,Y
~ .
.r~ O O O U~

5 J .~::
J- V ~J
W ~ ~ ~:

O
3 3 ':t ~7~18~

Egample 9 This e~ample 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 tr~atment does not involve the use of magnesium as additive. A
sample of conventional eucalyptus kraft pulp having a consistency of 12% which prior to treatment e~hibited a Kappa Number of 16.7, a viscosity of 30.8 cP and a whiteness of 33.8Iso was used. The reaction time was 60 minutes, using 15 kg 02Jton of pulp, an 02 partial pressure of 4 kgf/cm2, 20 weight percent of ethanol and 0.5 weight percent of MgSo4.7H20 at a temperature of 120C. ~periment results are shown in Table 4 as follows:

v c:
`O ~ ~ O .J ~ r~
~1 ~ O~ ~ ~ ~ ~ O
~1 a~ ~
Ql ~ u ) . ~ . . . . ~ .
F-rl ~ ~ u~3 ~D 00 3 3 3 ~ 3 ~ 3 ~ ;i' r.o U~
C O c~
~ U~

:~

U ~ O X ~ ~ ~ ~ 0 5~ ~D

~ ~ ~ O _ ~J O 0~

~ 00 0 ~ _ O O
t~ ~ 3 C~ O
CJ~ O O ~ O O O C: _~

~: n o U~ U~ o n c:, m o æ ~ê

O O O ~q u~ oq .C ~ .C ~

V

n ~ r~ oo ~ o ~
~ J J m n u~ m - 16 - 2~7~8~

As can be seen from the e~perimental results of E~ample 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 80-140C 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 100C in the absence of additives did not reach 38%, in the presence of ethanol at 120C this eficiency e~ceeded 46~, wherein the process selectivity coefficients, at lOO~C and at 120C, were similar. Thus, it is demonstrated that the use of ethanol in the lignocellulosic pulp o~ygen delignifying process, in accordance with the present invention, allows the ogygen delignifying process to be performed at higher temperatures resulting in a highex reduction of the Kappa Number without, however, prejudicing the pulp quality. It ~hould be pointed out the low values of selectivity obtained when o~ygen delignifying takes place at 120C in the absence of additives. In the e~periments without additives, an increase in the temperature confers an increase on the delignifying efficiency for the same amount of alkali but on the - 17 - 2~7~8~

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 lOO~C for foliage pulp has been verified to be impracticable due to the low selectivities. Therefore, delignifying efficiency is always limited ts a ma~imum of 40% with said pulps.
Th~ 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 refexring to e3periments of E~ampl~ 2 (Table 2), that a variation of the ethanol amount of from 10-130 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 o~ygen partial pressure effect on the delignifying and process selectivity, it can be verified, from the results of e~periments of E~ample 3 (Table 3), that in the pressure range of 2-4 kgf/cm2 good selectivity values are obtained, wherein the best value is achieved at 4 kgf/cm2. A
comparison between the selectivity values obtained from the use of the process in accordance with the present invention at 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.

- 18 - 2~7~8~

As can be seen from the results of e~periments 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 technique.s, i.e., o~ygen delignification in the absence of additives or in the presence of magnesium. The process of the present invention rendered delignifying efficiencies abo~e 47%, with selectivity values higher than those obtained with conventional processes. Choice of the most favorable alkali dosage for the o~ygen 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 (16)

1. Improvement in a process for delignifying with oxygen lignocellulosic pulp wherein a pulp from a baking step is treated with alkali and in the presence of oxygen is subjected to a delignifying process to reduce its lignin content, followed by a bleaching stage, the process being characterized in that ethanol is added to the lignocellulosic pulp prior to the bleaching stage, the lignocellulosic delignification being performed at elevated temperatures.

2. Improvement, in accordance with Claim 1, characterized in that the dosage of ethanol is, within the range of from 1 to 130 weight percent.

3. Improvement, in accordance with Claim 3, characterized in that the dosage of ethanol is about 20%.

4. Improvement, in accordance with Claim 1, characterized in that the pulp delignifying process temperature is within the range of from 80-140°C.

5. Improvement, in accordance with Claim 4, characterized in that the pulp delignifying temperature is, preferably, within the range of from about 100 to 120°C.

6. Improvement, in accordance with Claim 5, characterized in that the pulp delignifying temperature is about 120°C.

7. Improvement, in accordance with Claim 1, characterized in that the lignocellulosic pulp is a kraft pulp.

8. Improvement, in accordance with Claim 7, characterized in that the kraft pulp has an average consistency within the range of from 8-15%.

9. Improvement, 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.

10. Improvement, in accordance with Claim 9, characterized in that the alkali is sodium hydroxide.

11. Improvement, in accordance with Claim 10, characterized in that the amount of alkali is within the range of from 1.5 to 2.5 weight percent of sodium hydroxide.

12. Improvement, in accordance with Claim 11, characterized in that the amount of alkali is about 2.0 weight percent of sodium hydroxide.

13. Improvement, in accordance with Claim 1, characterized in that the oxygen pressure is within the range of from 2-6 kgf/cm2.

14. Improvement, in accordance with Claim 13, characterized in that the oxygen pressure is about 4 kgf/cm2.

15. Improvement, in accordance with Claim 1, characterized in that the pulp delignifying reaction time is within the range of from 10-120 minutes.

16. Improvement, in accordance with Claim 15, characterized in that the pulp delignifying reaction time is about 60 minutes.