WO2002099187A1

WO2002099187A1 - Reduction of organically bound chlorine formed in chlorine dioxide bleaching

Info

Publication number: WO2002099187A1
Application number: PCT/SE2001/001287
Authority: WO
Inventors: Martin Ragnar; Ulla EKSTRÖM
Original assignee: Kvaerner Pulping Ab
Priority date: 2001-06-06
Filing date: 2001-06-06
Publication date: 2002-12-12

Abstract

The invention relates to an improvement in bleaching of kraft pulp. In ECF bleaching chlorine dioxide is most often a prefered bleaching chemical in certain process positions. The disadvantage is that residual amounts of organically bound chlorine in form of AOX, i.e. organically bond chlorine in effluents, and/or OCl, i.e. chlorine organically bound in the produced pulp, is obtained. A normal approach has been to reduce charges of chlorine dioxide in the D-stage. According to the invention could substantial reduction in OCl levels be obtaiend if a substantial charge of sulphamic acid is added to the D-stage, preferably the last stage if several D-stages is used in sequence. A higher charge of chlorine dioxide could thus be used without increasing the residual content of OCl in pulp produced, which result in a mroe efficient D-stage as well as potential savings related to costs for bleaching chemicals in additional bleaching stages. A major reduction of OC1 up to 50 % could be obtained with the invention. The sulphamic acid added captures in situ formed elemental chlorine in the chlorine dioxide stage, which elemental chlorine would otherwise stick to the pulp.

Description

Reduction of Organically Bound Chlorine Formed in Chlorine Dioxide Bleaching

BACKGROUND OF THE INVENTION

The present invention is related to the formation of chlorinated organic matter in chlorine dioxide bleaching of kraft pulp, and how to reduce the amount of organically bound chlorine in pulp (OCl) and/or reduce the amount of organically bound chlorine compounds (measured as e.g. AOX or TOC1) in the waste water.

The most efficient and inexpensive bleaching chemical so far known is elemental chlorine, the use of it has in most parts of the world come to an end during the last decade. The driving forces in this development has been environmental, expressed either as market demands or as environmental standards set by governments or a combination of the two. The negative environmental impact connected to the use of elemental chlorine is primarily the formation of chlorinated organic structures.

Following a massive introduction of oxygen delignification systems, the work needed in the subsequent bleaching could be significantly reduced and the ECF concept (Elemental Chlorine Free), i.e. bleaching without the use of any elemental chlorine or hypochlorite, was introduced. The chemical normally replacing the elemental chlorine is chlorine dioxide, which had been used for final brightening of pulp and for obtaining a good cleanliness, e.g. due to its excellent capability of removal of extractives.

The chlorinated structures, e.g. formed in chlorine bleaching, are denoted AOX (adsorbable organic halogene compounds) when found in the bleach effluents and OCl (organically bound chlorine) when stuck in the pulp. The amount of both AOX and OCl were largely reduced upon conversion to ECF bleaching, but a zero level was not reached and in fact a significant amount of OCl is still found in ECF bleached pulps and AOX in the effluents from chlorine dioxide stages. The levels are also significantly higher than those arising from TCF (Totally Chlorine Free) bleaching operations. This is due to the fact that when chlorine dioxide reacts with the lignin in pulp, hypochlorous acid in equilibrium with chlorine is formed, both of which are able to act as chlorinating agents. Also during manufacturing of chlorine dioxide at the mill site some elemental chlorine is produced, typically in the order of 1-4%, most often below 5% elemental chlorine, all dependent on the type of chlorine dioxide forming process used. Considering AOX in effluents it is urgent to keep in mind that although the discharges per ton of pulp produced have decreased significantly when switching to ECF -bleaching, the mills have simultaneuosly grown too, meaning that the total AOX load to the specific recipient need not have changed very much and thus still constituting a potential problem. In figure 1 is shown how the total amount of AOX in effluents may be constant even tough the AOX level per BDt pulp have decreased over time, due to that production volumes have increased.

A pulp having been bleached using chlorine dioxide in an ECF sequence is still easily identified due to its content of OCl, which hinders it from being used in certain paper products or at certain markets. For several mills producing market pulp this is a crucial fact, since it means certain customers will not be interested in a high OCl pulp.

For various reasons, a massive conversion to TCF bleaching has so far not occured, leaving the field open for innovative ways to approach the OCl and AOX problems in ECF- bleaching.

The obvious way, to reduce the overall charge of chlorine dioxide, has in several cases been entered upon in, what is often called "ECF-light" concepts, using a rather small charge of chlorine dioxide in the D-stage, often a charge factor of active chlorine as chlorine dioxide of below 1.

At the Tappi Pulping Conference Oct.22-25, 1989, two papers where presented where solutions to the AOX problem was presented. Lowering of the delignification in the D-stage (or C- or C/D-stage), by using a lower charge factor of active chlorine as chlorine dioxide (i.e. kappa factor) was identified as methods for decreasing AOX, and where compensation for the lower delignification effect in D-stages is made by higher charges in other stages. One paper was presented by J.Basta, L.Holtinger, J.Hook and P.Lundgren with the titel "LOW AOX, POSSIBIILITES AND CONSEQUNCES"(pp. 427-436), and the second paper was presented by H.Suss, W.Eul, N.Nimmerfroh and J.Meier, all from Degussa AG/Corp, with the titel "ENVIRONMENTAL ASPECTS OF SHORT-SEQUENCE BLEACHING" (pp. 527-537). The main approach in these papers, when AOX-reduction is the objective in ECF -bleaching, is to decrease the use of chlorine dioxide at the expense of higher charges of hydrogen peroxide. This approach is shown in EP,B,500813, where a charge factor of active chlorine as chlorine dioxide below 2.0 is used in the Do stage(i.e. the first D-stage in a multiple sequence D-E- D... etc.) , and where following P-stage (P=peroxide) use at least 3.0 kg of hydrogen peroxide per ton dry pulp, and having chlorine dioxide charges in following D-stages less or equal than the charge used in DO, i.e. from 20-100% of the DO charge.

In addition to this approach it has been proposed the first chlorine dioxide stage be pH profiled by means of a short-term reaction at low pH followed by an increase to alkaline conditions (Ljunggren, S., Bergnor, E. and Kolar, J. (1994): Modified Modern C102-Bleaching, International Pulp Bleaching Conference (IPBC), Vancouver, Canada, Vol. 1: 169-176. and Ljunggren, S., Bergnor-Gidnert, E. and Kolar, J. (1996): Chlorine Dioxide Bleaching with a Two-step Low-to-HighpH Profile, Tappi J. 79: 12, pp.152-160.).

This approach has many similarities with the Ultim-O process (no washing between DO and E). Although this approach indeed enabled significant reductions in the AOX discharges, the OCl content was less affected and most important, the need for alkali increased largely, making it less attractive.

Lately, a reductive alkaline post-treatment has been proposed as a way of significantly reducing the OCl content of a pulp,(see Ljunggren, S., Johansson, E. and Pettersson, B. (1998): Dechlorination of ODEDD Bleached Kraft Pulps, 5th European Workshop on Lignocellulosics and Pulp (EWLP), Aveiro, Portugal, pp. 437-440), which is a somewhat refined way of utilising the well-known fact that an alkali extraction undoubtedly is a very efficient way for the removal of OCl.

Although efficient, such a post-treatment of the pulp requires both additional washing equipment and additional bleaching towers, making also this approach less attractive for mill implementation.

Improvments in Chlorine Dioxide stages have been made for several purposes. In a paper presented by Lachenal, D. and Chirat, C (1998): High Temperature Chlorine Dioxide Delignification: A Breakthrough in ECF Bleaching of Hardwood Kraft Pulps, Pulping Conference, Atlanta, U.S.A., Vol. 2.pp. 601-604.), a modification of the conventional D-stage is suggested. With the objective to make the D-stage more efficient, and reduce charges of chlorine dioxide, it is proposed to modify the conventional 45°C D-stage to a high temperature (90- 100°C) D-stage having long retention time (1.5-4 hrs). An alternative modification achieving the same improvement was proposed where instead this high temperature is implemented after, "at the exit of, the D-stage when the chlorine dioxide have been consumed, during which process position the high temperature could not affect the break-down process of chlorine dioxide in the D-stage. This paper also indicates that the change from chlorine to chlorine dioxide bleaching will solve the AOX-problem.

SUMMARY OF THE INVENTION

The main objectives with the present invention is to reduce the total amount of chlorinated organic matter leaving the chlorine dioxide stage, and especially the total amount of AOX and OCl, where at least a substantial reduction in OCl levels is obtained. Using an additional charge of sulphamic acid in a chlorine dioxide stage is shown to be an efficient means of reducing the overall content of OCl in the pulp by about 50 percent, since sulphamic acid captures in situ formed elemental chlorine.

Yet another object is that this addition of sulphamic acid is made essentially only to the final D-stage, keeping down cost for chemicals as well as obtaining best bleaching effect in preceeding D-stages, in a bleaching sequence having several D-stages in sequence, i.e. like a DEDED sequence. In this implementation the most cost effective effect of the sulphamic acid is obtained.

DETAILED DESCRIPTION OF THE INVENTION

The invention is based upon the origin of OCl and ways to decrease it, without necessarily reducing the use of chlorine dioxide and still reaching the same final brightness. The distribution of OCl in ECF -bleached pulp is playing an important role.

It is important to understand the correspondence between AOX and OCl. In Fig. 2, the three major possible faiths of a chlorinated substance in the pulp are summarised. Following a chlorination there are thus three alternatives, either that the chlorinated structure sticks to the final pulp becoming OCl, or that it is liberated during subsequent bleaching stages becoming AOX, or that the structure is substituted/degraded so that the chlorine atoms form harmless chloride ions. Important to keep in mind is hence that there is no direct correspondence between AOX and OCl telling e.g. that a high AOX discharge means a low OCl content in the pulp at a certain chlorine dioxide charge.

5-stage sequence trials

In a series of trials the standard ECF bleaching sequence of DEDED, using an overall chlorine dioxide charge of 29.6 kg a Cl/BDt, was used to bleach the oxygen delignified HW kraft pulp from the second series of trials (kappa 9.8) to full brightness (above 89 % ISO). 19.6 kg a Cl/BDt was used in DO, and 5 kg a Cl/BDt in each of Dl and D2. The charge factor of active chlorine as chlorine dioxide in DO equaling (19.6/9.8=) 2.0 . This standard sequence was compared with three modified sequences, D*EDED, DEDE(SD) and D*EDE(SD). D* denotes a D-stage run at high temperature (90 °C) and long time (120 min). "S" denotes the presence of sulphamic acid. E stages were performed according to above. Dl and D2 stages were performed at 75 °C and 120 min.

General methods Kappa number, viscosity and ISO brightness were analysed using the respective SCAN standards. In addition, SCAN standard CM 52:94 "Pulps, papers and boards - organic chlorine" was used to determine the content of OCl in the pulp after different stages. All bleaching experiments were performed at 10 percent pulp consistency in plastic bags, which after intense kneeding were placed in heated water baths. The charge of sulphamic acid should be somewhat higher, i.e. on a molar basis, than the charge of active chlorine, in this investigation meaning 1.0 mmol sulphamic acid/BDt.

In those stages to which sulphamic acid addition was made, the charge of active chlorine was increased in order to compensate for the decreased oxidising capacity of the stage when the reduction of chlorine dioxide to chloride ion is broken at the level of elemental chlorine. The oxidising capacity of chlorine dioxide is decreased by 20 percent in the presence of sulphamic acid, which captures intermediately formed elemental chlorine, and following reaction pattern is developed with and without sulphamic acid.

+ IV sulphamic

C IO acid V C \

+ IV -I

C IO H - C l

In practise this means that 4 out of 5 electrons are used when chlorine dioxide bleaching in the presence of sulphamic acid is used and thus the charge of active chlorine to such stages were increased by 25 percent. This way, all the pulps were subjected to identical charges of "active" active chlorine. Ways to obtain a low OCl pulp and to reduce AOX discharges

Results from the 5-stage bleaching study on HW mill oxygen delignified kraft pulp are given in following table 1.

Table 1

Trial DEDED D*EDED DEDE(SD) D*EDE(SD) final kappa 2.1 0.6 2.5 1.2 final viscosity [ml/g] 975 937 939 911

ISO brightness [%] 89.4 89.9 89.4 89.5 total a Cl charge [kg/ADt] 27 27 27 27 total OCl [mg/kg] 152 158 88 116 total AOX [kg/ADt] 0.41 0.23 0.39 0.21

From the results it is clear that the AOX discharge could be reduced with about 50 percent using D* instead of D as the first bleaching stage. It should be noted that this result is obtained when comparing sequences with identical overall charge of chlorine dioxide. In addition to this reduction of AOX, the value can be even further reduced when the chlorine dioxide saving effect of the D*, (as e.g. noted by Lachenal, D. and Chirat, C (1998): High Temperature Chlorine Dioxide Delignification: A Breakthrough in ECF Bleaching of Hardwood Kraft Pulps, Pulping Conference, Atlanta, U.S.A., Vol. 2: 601-604.) is taken into account, here instead recorded as a higher final brightness.

This finding was very unexpected. One would else have anticipated that if the AOX levels experienced a decrease, then the OCl would increase by a similar order. However, the findings showed that the AOX-levels was decreased without a similar order of increase in OCl. The interpretation of the result should not be that less chlorination takes place or that less AOX is formed in a D*-stage than in a conventional D-stage. On the contrary it seems appropriate to suppose that under the tough conditions of the D* stage, a substantial part of the AOX formed in the stage is further degraded to e.g. harmless chloride ions. With this knowledge in mind it is interesting to compare D* with (AD), i.e. where A is performed as a hot acid treatment for long duration at e.g. 90-100 °C and 120 min according to concepts like GB 1.062.734. In GB 1.062.734 this acid treatment at pH 2.25, temperature 100°C and during 120 minutes was implemented in order to reduce brightness reversion. The extreme A-stage was followed by a conventional DO-stage at some 60°C without intermediate washing. In conformity with D*, an (AD) approach gives a potential to reduce the overall need for chlorine dioxide in the bleaching of especially HW kraft pulp, although D* has been shown to have a greater potential in this respect. However, in contradiction to D*, an (AD) approach will not enable any reduction of the AOX according to the mechanisms presented. Theoretically, D* can of course be utilised in any position in the bleaching sequence irrespective of the number of D-stages in the bleaching line. Although in general it is likely that the benefits of the stage primarily motivates its utilisation in the DO position, i.e. the first stage using chlorine dioxide.

From the results in Tabel. 1 it is also clear that the presence of sulphamic acid in the final D- stage is an efficient means of reducing the OCl content of the pulp. Having the OCl pattern shown in Fig. 3 in mind, it is easily concluded that the largest effect to the lowest charge of sulphamic acid is obtained when sulphamic acid addition is made to the last D-stage, although a larger effect of course can be obtained using it in all D-stages. Although sulphamic acid already today is commonly used in pulp mills, e.g. for the removal of scales in machinery upon shut-downs, its use in continous bleaching processes for obtaining low OCl pulp is new. The addition of sulphamic acid should be added in a continous manner during the bleaching process in the chlorine dioxide stage, i.e. so that sulphamic acid is present during the consumption of chlorine dioxide in the chlorine dioxode stage. The sulphamic acid could be added to the pulp before, after or during addition of the chlorine dioxode in a chlorine dioxide mixer. It should be added that the chlorine dioxide charge in a (SD) stage has to be increased by some 15-30%>, typically 25 percent, in order to compensate for the reduced oxidising power lost due to the capture of elemental chlorine by sulphamic acid. However, when utilised in D2-position, or in the final D-stage, this means a very moderate additional need for chlorine dioxide in this last stage. The two concepts D* and (SD) could also be utilised in the same sequence, thus enabling the manufacture of a pulp with low OCl content at the same time as the AOX discharges are kept low, as shown in Tab. 1.

It can be concluded that a 50 percent reduction of the overall AOX discharge of a DEDED sequence can be obtained by using a D*-stage instead of a conventional D-stage in DO position. The OCl content can also be fighted and decreased by about 50 percent even in an existing bleaching line by changing the last D-stage to operation with sulphamic acid addition in a (SD)-stage.

Claims

PATENT CLAIMS

1. A process for reducing the amount of organically bound chlorine formed in chlorine dioxide bleaching of kraft pulp, wherein the first chlorine dioxide bleaching stage used during the bleaching sequence is having a charge factor above 0.5 characterised in that sulphamic acid is added to at least one chlorine dioxide bleaching stage in the bleaching sequence.

2. A process according to claim 1, characterised in that sulphamic acid is added to at least one chlorine dioxide bleaching stage in the bleaching sequence in an amount exceeding that of the charge of active chlorine based upon a mol relation.

3. A process according to claim 2, characterised in that sulphamic acid is added to at least one chlorine dioxide bleaching stage in the bleaching sequence in an amount exceeding 0.5 mmol sulphamic acid/BDt of pulp, and preferably exceeding l.Ommol sulphamic acid/BDt of pulp.

4. A process according to any of preceeding claims, characterised in that the major part, i.e. more than 80% of total charge and preferably 100%, of the total charge of of sulphamic acid added to the bleaching sequence is added to the last chlorine dioxide bleaching stage in the bleaching sequence.

5. A process according to claim 4, characterised in that that the last chlorine dioxide bleaching stage is at least a D2 stage, i.e. a chlorine dioxide stage preceeded by at least a DO stage, the first chlorine dioxide stage, and a Dl stage, having extraction stages between chlorine dioxide stages, i.e. according to a D0-E-D1-E-D2 bleaching sequence.

6. A process according to any of preceeding claims, characterised in that the charge of chlorine dioxide used in the stage where sulphamic acid is added is increased by at least 10%, preferably increased 20%, as compared to a charge of chlorine dioxide used in this stage without addition of sulphamic acid and resulting in a final pulp brigfhness in the same order of ISO brightness, i.e. the same order of ISO brightness corresponing to +1% in final ISO brightness.

7. A process according to claim 5, characterised in that the very first chlorine dioxide stage DO is operated at a temparature above is operated at a temperature above 91°C , preferably above 95°C and at a retention time more than 90 minutes, preferably about 120 minutes an not more than 300 minutes.