Area of the invention.

The present invention relates to a process tor combusting black liquor m recovery boilers The invention also includes a recovery boiler for implementing the process according to the invention.

State of the art and problems:

Recovery boilers for combusting black liquor which is obtained during cellulose coo mg have been well known for many decades. Their task is, on the one hand, to generate energy by means of the combustion and, on the other hand, to recover chemicals which were used during the cellulose cooking and which are released m the smelt state during the combustion and tapped off from the bottom part of the recovery boiler. Recovery boilers are large installations and, apart from generating a large quantity of energy and recovered chemicals, also generate a large quantity of flue gases. These flue gases contain, inter alia, nitrogen oxides which have arisen during the combustion of the liquor.

During recent years, ever stricter requirements have been introduced with regard to the discharge of nitrogen oxides into the atmospnere . It is well known that these oxides contribute to acidification and other unfavourable effects on the natural environment. Nevertheless, the quantity of nitrogen oxides which is emitted from the recovery boilers of the wood- processing industry s low as compared with that originating from cars, etc. While the contents are normally within the range or 40 /0 mg of NOAMJ (calculated as the effective heat value _^ n a reducing medium) , even these low contents have to be decreased substantially m future The discharges have been shown

to depend principal! ^* , on the nitrogen content of the fuel, _^ . the black liquor, and this content will increase in the future as the chemical cycles are closed ever more stringently This will result m the nitrogen oxide emissions increasing A countcrmeasures are not taken

Factors whicn can effect the formation of nitrogen oxides are awe11 time, temperature and oxygen content . As a result of experience gained rrom conventional power boilers based on coal, oil and gas, it is known that substoichiometric conditions with regard to the oxygen supplied to the combustion zone, m combination with a final combustion, for the purpose of obtaining maximum energy evolution, m a so-called overfire air register which is placed directly above (or after) the combustion zone, result in a lower No, emission.

This technique has also, for a long time now, been used for other reasons m recovery boilers, where primary air and secondary air have been supplied below

(before) the black liquor, and tertiary air has been supplied immediately above (after) , in a similar manner to that m which overfire air has been used for power boilers. This is described in more αetail by Anderson &

Jackson in the TAPPI Journal for January 1991, pp. 115-

118.

SE 468 171 discloses a method for decreasing the content of mtiogen oxides in the flue gas, in which method a part of the combustion air is supplied, as a final portion, at a very high level so that a higher grade of reducing atmosphere _s maintained, without any extra addition or reducing substances, e er a distance of 10-20 metres or greater, from the reαron of the liquor lmection and up to tne ooint of the final addition of air, corresponding to a dwell time under normal Aadmg of 2.5 Z seconαs or more. This method presupposes ' hat tn^ recovery boiler rs

- -

relatively tall so that the reducing atmospheie can be maintained for a sufficiently long time

Another method has oeen proDOsed for reducing the N0_ in the recovery boiler, which method uses the technique, which has ioeen developed for power toilers, involving thermal or selective non-catalytIC reduction (SNCR) , by means of supplying a reducing substance, m the form of natural gas, ammonia or urea, relatively high up the recovery boiler for the purpose of reducing nitrogen oxides which have been formed. When natural gas is used, large quantities of uncombusted residual products are formed which have to be finally combusted by means of a further addition of air. When urea or ammonia is used, they are normally added, m the form of an aqueous solution, to the upper parts of the furnace space. A ma]or disadvantage of using this method in a recovery boiler is that an aqueous solution is being supplied, involving the risk of causing water/smelt explosions. This can occur, for example, in association with faulty handling and if corrosion damage arises which is caused by the urea solution.

An alternative to introducing an aqueous solution of ammonia can be to introduce it after volatilization using spray guns This procedure requires many spray guns and the handling of concentrated ammonia in the immediate vicinity of the Doiler. In addition, there is the risk of obtaining very high concentrations of ammonia locally in the furnace, and consequently non-optimal conditions for NO _y reduction.

SE 460 221 discloses a method of supplying ammonia gas to an MBC (Multiple Bed Combustion) boiler, in which method the ammonia gas is supplied t _^ secondary and/or tertiary air, which is mixed with flue Qas and supplied to one or more upper flurdized Peds for the purpose of fluidizmg these beds. While this technique can function well _n an MBC boiler, r ^r does not do so in a recovery dorler since the temperature distribution is much detter in an MBC boiler.

Solution and advantages:

However, the present invention has resulted _^ n a process for obtaining, in association w th the combustion of blac liquor m recovery boilers, liue gases having a low content of nitrogen oxides, m which process a part of the combustion air is supplied, as a final portion, at a high level so that a reducing atmosphere is maintained, from the region of the liquor injection and up to the final addition of air, over a distance of 10-20 metres or more, corresponding to a mean dwell time under normal loading of 2.5-5 seconds or more. The method is characterized in that ammonia is supplied to the said final portion of combustion air in a quantity corresponding to 100-400% of Ahe stoichiometπc requirement for complete reduction of nitrogen oxides present in the flue gas. If the boiler- is not equipped with a flue gas wash, the ammonia rs preferably supplied in a quantity corresponding to 100- 200%. If the boiler is equipped with a flue gas wasn, the ammonia is preferably supplied m a quantity corresponding to 100-300%.

The ammonia is added to the combustion air either in conjunction with the latter being introduced, or even more preferably before the latter is introduced, into the furnace space. The ammonia is preferably added m gasified form, with the gasification taking place either by means of volatilization of pure, liquid ammonia or by means of evaporating ammonia from its aqueous solution.

It is simplest to add the ammonia directly to the combustion air either immediately upstream or immediately downstream of the arr fan. Alternatively, ammonia gas can be supplied directly to the air ports (supply openings) by way of separate compressed air- driven feed lines.

The final portion or the comoustion air, which portion contains ammonia according to the invention, can be supplied in two stages at two high levels

The quantitv of ammonia-containmq combustion ii wnicn, accordmσ to the invention, is to be added at the nign level (B, constitutes approximately 2 5-50%, preferably 5-15%, of the total combustion air

The process according to the invention also includes the proportion of nitrogen oxides m the flue gases being monitored with the aid of a control system which automatically regulates the supply of air to the different levels and the supply of ammonia to the combustion air. The quantity of ammonia whicn is to be supplied, i.e 100-400% of the stoichiometπc requirement for complete reduction of nitrogen oxides present in the flue gas, preferably 100-200% for boilers without a flue gas wash and 100-300% for boilers with a flue gas wash, is determined by measuring the content of nitrogen oxide and ammonia in departing flue gases The stoichiometπc requirement which is meant in this patent application is set m the conventional manner at 1 mol of NH-, per mole of NC . The quantity of ammonia which is added then becomes 1-4 mol per mole of nitrogen oxide, preferably 1-2 mol per mole for boilers without a flue gas wash and 1 3 mol per mole for boilers with a flue gas wash.

The requisite quantity of ammonia can be obtained either by buying it or else generating t internally m the mill, for example dy stripping condensates.

When the nitrogen oxides are reduced, it is assumed that nitrogen and water are formed m accordance with the following overall reaction

NO + NH, + OH → N - 2 HA

The aim _-, that all the ammonia should be oxidized to mtroσen Any possible discnarge f ammonia in the flue gases is minimized by measuring and

adjusting the quantity added. In the case cf boilers wmch are equipped with a flue gas wash, a larger- quantity of ammonia can b_ added without there having to be any increase in the discharge of ammonia This is advantageous since a h gh level of ammonia addition results in a greater reduction ol the nitrogen oxides

The invention also includes a recovery boiler for combusting black liquor m accordance with the described method. The recovery boiler is characterized n that, rn addition to conventional devices for supplying primary air, secondary air and tertiary air, and devices for supplying high tertiary air or quaternary air at a substantially higher level, in accordance with SE 468 171, it also includes devices for supplying ammonia to the said high tertiary air or quaternary air. In this context, high tertiary air is understood to mean air which has been branched off from the normal tertiary air line, while quaternary air is understood to mean air which comes from a separate line.

In the recovery boiler according to the invention, the devices for supplying ammonia-containing high tertiary air or quaternary air can be situated at one or more levels around 10-20 metres above the revel at which the liquor is injected.

The recovery boiler according to the invention can be provided with two or more rows of supply openings, on either side of the furnace space, for supplying ammonia-containing high tertiary air or quaternary air, with it being possible tor one level to be at approxrmately 10 metres and the other at approximately A metres adove the level at which the liquor is injected.

According to the invention, it is expedient for the uppermost air supply openings, for the ammonia- containing air, to be located directly below, preferably 1-4 metres below, and even more preferably 2-3 metres below, the region where the oone is narrowest, i.e. where the rnternal "nose" rs arranged

rmally the recover' ooiler according to the invention is characterized in tnat rt rncludes a control system for automatreally controlling the different supply streams of --he combustion air and also a control system for the ammonia supply

Consequently, a major advantage of the invention is that, since the ammonia s supplied in gaseous form, Aere is no rrsk of water /smelt explosions . A further advantage is that the ammonia is introduced into the boiler where it does the most good, i.e. when almost all the combustion reactions hav° finished and the temperature has fallen tc approximately 950°C Yet another advantage is that only small quantities of concentrated ammonia have to be nandled m the immediate vicinity of the boiler since this ammonia is rapidly diluted in the high tertiary air or quaternary air. In addition, the turbulence which the ets of high tertiary air or quaternary air create m the boiler distribute the ammonia very efficiently m the boiler, with optimum concentration conditions bemα created for reducing nitrogen oxides

In that which follows, the invention will be described m more detail with reference to the attached drawing, which schematically shows a recovery boiler according to the invention m cross section, and a diagram which shows the effect which is achieved by the invention .

ϊπef description of the figures

Figure 1 shows α recovery boiler for maκιng use of the invention Figure 2 shows a comparative diagram of the nitrogen oxide content in the flue gases when supplymq air/ammonia

Figure 3 shows two alternative emPodiments for adding ammonia to the air

Detailed description or tne invention:

The recovery boiler as shown in Frg 1, wnion is of a conventional type for a steam production of approx 250 t/h, includes liquor sprayers 1 hicr. ire situated m the lower parr or the recovery boiler. Openings ^ for plowing in secondary air are located below these liquor sprayers 1. Start burners, which are fed with oil or gas, are also present at this level. Openings 3 for supplying primary air are present below the level for supplying the secondary air. Openings 4 for blowing in tertiary air are located above the liquor sprayers 1. Additional an supply openings 8 are present, on both sides or the furnace space, at a nigh level in the boiler directly below the region where a tapering of the boiler, the so-called "nose" 5, is located. Whrle there can be several of these open ngs, expediently eight on both sides, the actual number is not critical. In accordance with SE 468 171, a part of the tertiary air, which would normally be supplied lower down at position 4 m the boiler, is supplied through these air openings. The quantity which is normally introduced at position 4 is thus decreased, and this quantity is allowed to flow m at the most highly situated an supply devices 8. Expediently, the quantity of air which is supplied at this upper position amounts to a quantity corresponding to 5 15% of the total air intake. In accordance with the invention, ammonia gas is supplied to this quantity of air before the latter is introduced at position 8. This means that a gas atmosphere, which is entirely or partially reducing depending on the content of ammonia, carbon monoxide and smaller quantrtres of hydroαen and hydrogen sulphide, is present m the region from position 4 to position b otherwise, the boiler includes conventional devices, such as n heat exchanqer and, under the boiler, a collecting vessel , termed drssolver tank, for smelt, wnich consists A recovered chemicals in the ror of known sodium salts

At position b, and immediately thereafter, the reducing gases are combusted to nitrogen, carbon dioxide, water, etc and release the last quantity of energy which is possible This combustion takes place at a temperature of the order of 900 1100°C, A which temperature only very small quantities of nitrogen oxides are formed. These measures result in the quantity of nitrogen oxides being markedly decreased This is snown in the attached diagram (Figure 2 > . The diagram makes clear, on the one hand, the improved result whicn is achieved with the invention as compared with only adding quaternary air (i.e without ammonia in accordance with SE 468 171) and, on the other hand, that the effect achieved improves as the amount of ammonia added becomes more overstoichiometric As has previously been mentioned, any departing excess of ammonia can advantageously be washed away in a flue gas wash.

Figure 1 also shows a further row of air intakes for overfire air at position 9 While these air intakes can be dispensed with, they can also complement the air intakes at position 8. The number ot air intakes at position 9 can be the same as at position 8, expediently eight intakes on both sides of tne turnace Figure J shows two alternative methods of adding the ammonia to the air Part no 10 symbolizes the ammonia source Metering is effected using a device 11, after which the ammonia is volatilized, 12, and the flow is measured, 13 According to alternative 1, the ammonia is supplied to each air box 16 (foi tne supply openings 8, 9) tnrough separate compressed an -driven, 18, feed lines 14, 15 Each such feed line can be regulated separately. According to alternative 2, the ammonia is instead supplied to tne a r immediately downstream of the air fan 17, before the air lrne divides for supply to the different air boxes 16

As has Deen said above, the essential point with regard to the invention is that ammonia s added to tne las- part ol th ^Ω an which is supplied at a nigh

- L O - level in the recovery boiler . In addition, the quantity of air at lower levels is decreased to such a degree that an environment which is i educing, or almost reducing, is obtained for a very long time, approximately 2.5-5 seconds, in the normal recovery boiler. This time is to be compared with that mch _^ obtained, namely approximately 0.6 seconds, when the last part of tne air is added at the tertiary position

4, approximately 2 metres above the liquor sprayers. Besides resulting m a more reducing atmosphere below the level of the uppermost air addition, decreasing the addition of tertiary air at the same time as making an addition of quaternary air also results, as compared with conventional operating conditions, m a lower temperature below thrs level and a temperature above the level which is higher relatively. The distribution of air between the tertiary level and the quaternary level can thus be used as a method for guiding the temperature above the site of quaternary air addition to a level which is optimal for reducing nitrogen oxides. This temperature depends, to a high degree, on the content of reducing substances, such as hydrogen, in the flue gases. For example, Lyon '"Thermal DeNO. " ,

Env. Sci. Tech. Vol. 21, No. 3, 1987ι has demonstrated that the optimum temperature decreases from 950A to

700°C when the H./NH ratio increases from 0 to 1.3.

Consequently, by means of arranging the overfire air intake so high up the boiler and at that point admitting a part of the air which would otherwise have been admitted at the tertiary air rntake, and in this way obtaining a lower content A nitrogen oxides, the opportunity has been obtained to regulate the content of nitrogen oxides in the exhaust gases by means of adding ammonia to the overfire air and varying the air streams. According to the invention, this can be done automatically by measuring tne content of nitrogen oxide and ammonia in the flue gases ana allowing these measured values, for example via computer, to control both valves for blowing the

quantities of an mtc tne primary, secondary, tertiary and tiign tertiary or quaternary „ιr rntakes and also the quantity of ammonia gas which i added to the nigh tertiary or quaternary air intakes. In this way, it is possible to compensate for variations in the quality ot the fuel, etc. and consistently obtain a minimal quantity of nitrogen oxides in the flue gases without _j eopardizing other operational parameters or occasioning an unacceptably nigh content of ammonia in the flue gas.

The invention has been described m conjunction with a modern recovery boiler for a steam production of approximately 250 t/h and having a normal height of approximately 50 metres, with the uppermost air ιntaκe, for ammonia-containing air, expediently being placed at approximately 16 metres above the liquor sprayers. The same ratio between height and distance above the liquor sprayers can also be used m the case of larger boilers. However, in the case of shorter boilers, another ratio may be expedient since, n the case of such boilers, the dwell time may m any case be too short for satisfactory reduction of the nitrogen oxides .

The invention is not limited to the exemplary embodiment shown and can be varied in different ways within the scope of the patent claims. Other reducing agents, for example urea, can naturally be used in addition to, or instead of, ammonia.