METHOD FOR PURIFICATION OF WASTE GASES

Abstract: Method for purification of waste gases by adding reagent and/or absorbent, which reacts with the pollutants, to the gases and by introducing the gases into a wetting reactor (10) for activating the reagent or absorbent contained in the gases. The gases are conveyed to the lower section of the wetting reactor and further upwards to wetting zone (30). The reagent or absorbent which has reacted completely or partly is separated from the gas by a filter (22) disposed in the upper section of the reactor. Preferably a high density of particles is maintained in the wetting zone. So thick an ash layer is maintained below the gas inlet level in the lower section of the wetting reactor that the ash layer, formed of particles separated from the gas, is capable of homogenizing the wet particles and water drops falling downwards from the wetting zone.

Description: Method for purification of waste gases The present invention relates to a method of purification of waste gases which are produced in, for example, com- bustion, gasification, or some chemical or metallurgical processes. Sulfur dioxides, ammonia, chlorine and fluor¬ ine compounds and condensing hydrocarbon compounds are typical pollutants contained in these gases. The present invention especially relates to a method in which reagent and/or absorbent which reacts with pollutants contained in the gases is activated by leading the gases into a wetting reactor. The reagent and/or absorbent is added to the process itself or to the gases discharged from the process. The gases are introduced into the wetting reac- tor for wetting them with water or steam in order to activate the reagent contained in the gases. The gases are first fed to the lower section of the wetting reactor and then further upwards to the wetting zone of thereof, where a suspension formed of the gas and the reagent is wetted with water or steam. The reagent and/or absorbent particles which have reacted either completely or par¬ tially are separated from the gases by a filter in the upper part of the wetting reactor before the gases are discharged from the reactor. Carbonates, oxides or hydr- oxides of, e.g., either alkali metals or alkaline earth metals are used as reagents or absorbents. As known, combustion of fossile fuels produces flue gases which contain sulfur oxide and cause environmental acidi- fication. The sulfur content of the flue gases varies depending on the sulfur content of the fuel. Efforts are made to find means for employing fuels which contain more and more sulfur even though the restrictions on sulfur emissions become tighter and tighter. Waste incineration plants, the number of which is continuously increasing, also produce sulfur-containing flue gases which have to be purified so as to be within the set limits. The flue gases produced in waste incineration plants when, e.g., plastic compounds are burnt contain, besides S0 2 and S0 3 emissions, also hydrochloric and hydrofluoric acids and other harmful gaseous and solid compounds. Process gases produced in various gasification processes may also contain harmful amounts of sulfuric or other compounds which have to be separated from the gases prior to further treatment thereof. Several methods have been developed for cutting down sulfur emissions of combustion plants. The most common method used so far is wet scrubbing in which method the gases are scrubbed with a water suspension of a reagent, such as lime, reacting with, e.g., sulfur oxides. The water suspension is sprayed into a gas flow in a scrubber arranged after a combustor, whereby sulfur is absorbed into the water suspension and sulfur dioxide reacts with lime, forming calcium sulphate or calcium sulphite CaO + S0 2 + 1/2 0 2 --> CaS0 4 or CaO + S0 2 —> CaS0 3 . Water suspension is sprayed in such an amount that sulfur compounds thus formed have not enough time to dry, but they are discharged as a slurry from the lower section of the scrubber. The wet scrubbing process is complicated as it requires means for preparing water suspension and means for after-treatment thereof. Furthermore, the method usually requires additional energy for drying the produced slurry in a slurry after-treatment plant. There¬ fore, the water suspension is usually fed into the system as dry as possible in order to minimize the energy re¬ quirement. Due to the considerable amount of water sus- pension used, the gas may be cooled to a relatively low temperature in the scrubber and, consequently, the gas discharged from the scrubber may cause corrosion and clogging of filters. Further, energy is consumed for reheating the flue gases prior to leading them out of the system. In the wet scrubbing system, the separation degree of, for example, S0 2 , is about 95%. During the last few years, semi-dry scrubbing methods have been developed, in which a fine alkali suspension, e.g., calcium hydroxide suspension is sprayed through nozzles into a hot flue gas flow in a contact reactor where sulfur oxides dissolve in water and, when the sus¬ pension dries, are bound to the lime compound. Water is evaporated in the contact reactor so as to form a solid waste, whereby reaction products of, for example, sulfur and lime are readily separable from the gases by means of a filter. It is attempted to maintain the consistency of the calcium hydroxide suspension on such a level that the heat content of the flue gases is sufficient for evapor¬ ating the water therefrom. The thick lime suspension, however, easily deposits layers on the reactor walls and especially around the spray nozzles, and may finally clog the nozzles entirely. The reactors have to be dimensioned relatively large for minimizing the drawbacks caused by deposits. Furthermore, as separate equipment is required for the production of lime suspension, a considerable amount of equipment will be needed in the semi-dry scrub¬ bing method as well, and the gas purification will be fairly expensive. A further drawback is the wearing effect of the lime suspension on the nozzles. The semi-dry scrubbing method is advantageous for the process because the pollutants in the gases may be removed as dry waste. The process has drawbacks of being difficult to control and providing a sulfur absorption below 90%, which is less than in wet scrubbing. A still further drawback is that inexpensive limestone cannot be used in the semi-dry method because it is very slow to react with sulfur. Either calcium oxide or calcium hydr- oxide, which are much more expensive, have to be used instead. In big combustion plants, the cost of absorbent is remarkable. Addition of limestone already into the actual combustion or gasification stage has also been suggested. As a result of such addition, limestone is calcined into cal¬ cium oxide in accordance with the following reaction CaC0 3 —> CaO + C0 2 . Calcium oxide is then capable of reacting already in the combustor with the sulfur oxides formed therein. The reaction takes place as follows: CaO + S0 2 + 1/2 0 2 —> CaS0 4 . When the reactions proceed, calcium sulphate or calcium sulphite layers, however, cover the surface of the cal- cium oxide particles preventing sulfur from penerating the particles, thereby slowing down and finally prevent¬ ing the reactions between sulfur and lime. Thus, lime will not react completely and will not, therefore, be optimally utilized. Many other parameters, such as Ca/S mole ratio, temperature and residence time also affect sulfur absorption. The closer to the dew point the reactions take place, the higher the reactivity of alkali compounds becomes. Better reactivity is caused by the fact that, in a wetted par¬ ticle, reactions take place in a water phase as fast ionic reactions. Close to the dew point, the particles stay wetted and the reactivity also remains on a desired level for a longer time. The moistness of the particles is preferably maintained on such a high level that water surrounds the particles, also penetrating them. As the water penetrates the lime particles, the sulphate or sulphite layer deposited on them will be broken, thereby revealing new reactive lime area. Sulfur dioxide con¬ tained in the gases dissolves in the water surrounding the particles and reacts with calcium compounds in the liquid phase. Finnish patent specification 78401 discloses a method in which sulfur dioxide of flue gases is caused to react in a reaction zone and to be thereby transformed into solid sulphates and sulphites separable from the flue gases. The flue gases are conducted into the lower section of a vertical, lengthy contact reactor. Additionally, powdered lime and water are separately brought into the reactor from several points for the sulfur to be absorbed by lime. Flue gas suspensions are discharged from the upper section of the flow-through reactor and are further con¬ ducted to a dust separation stage. By feeding the pow¬ dered lime and water separately into the reactor, produc¬ tion, treatment, and spraying of a water suspension are avoided. According to the specification, this method, when used in sulfur absorption with calcium oxide, results in about 80% S0 2 reduction with a mole ratio of Ca/S = 1.56 and about 90% S0 2 reduction with a mole ratio of Ca/S = 2.22. The 98% S0 2 reduction is not achieved until the mole ratio is Ca/S = 4. In this method either, the temperature of the flue gas flow must not be allowed to drop optimally close to the dew point as the solids contained in the flue gas suspension then would deposit layers on the walls of the tubes and other equipment, thus causing troubles in dust separation. European patent specification 0 104 335 discloses another two-phase, semi-dry flue gas purification system. In this method, dry reagent is fed into the flue gases in a con- tact reactor in a first stage and water or an aqueous solution, to which dissolved reagent has been added, in a second stage. In the first stage, an inactive surface layer is formed on the reagent particles. The layer slows down or prevents reactions between the reagent and, e.g., sulfur oxide. By adding water in the second stage, the reagent is reactivated. In this manner, the reagent is utilized more completely. The gas temperature is allowed to decrease to a level on which it always stays above the dew point, for example, to 105°C. The gas temperature must not, in this method either, be allowed to decrease too close to the dew point because any wetted particles possibly formed would cause difficulties in the long run, even if the reactivity of the reagent at a lower tempera¬ ture would be much better. According to the method, the required amount of reagent may be reduced by recycling reagent-containing solid material which has been separ- ated from the gas at a later stage and. then regenerated by either grinding or some other way. A drawback of this method is, however, separate equipment needed for handl¬ ing and storing of the recycled solids. U.S. patent specification 4,509,049 suggests a dry gas purification system in which lime is added to flue gases in a boiler and the lime is then allowed to react with the flue gases in a reactor. The lime, which has partly reacted with the pollutants in the flue gases, is separ- ated from the gases in a filter in the upper section of the reactor. The dry lime thus separated from the gases is collected and ground and then treated with dry steam in order to increase the reactivity of the dry lime, ■ whereafter the lime is recycled into the gas flow at a location prior to the reactor. The dry steam treatment of lime takes 2 to 24 hours, which is a long time involving high consumption of energy. An object of the present invention is to provide an im- proved method of purification of waste gases containing, e.g., sulfur, chlorine and fluorine compounds or other condensable compounds. Another object of the invention is to provide a method by which, e.g., sulfur reduction can be considerably im¬ proved, preferably even so that the amount of the reagent need not be increased. A further object of the invention is to provide a method by which a gas to be purified may be wetted very close to the dew point, for example, 0 - 20°C therefrom, in a wetting reactor, the method still allowing the particles separated from the gases to be removed in a dry state in the wetting reactor. For achieving the objects described above, it is charac¬ teristic to the method according to the invention that - so thick an ash layer is maintained below the gas inlet level in the lower section of the wetting reactor that the ash layer, formed of particles separated from the gas, is capable of homogenizing the wet ash particles and water drops falling downwards from the upper section of the wetting reactor. In the ash layer is preferably disposed a mechanical mixer, e.g., a blade mixer for mixing and grinding poss¬ ible lumps of particles smaller so as to homogenize the temperature and moistness of the ash layer. The purpose is to maintain the ash layer preferably so dry that the ashes may be conveyed out of the wetting reactor pneu¬ matically. The volume of the ash layer is maintained in the lower section of the wetting reactor, e.g., by regu- lating the amount of ashes discharged. Preferably the amount of the ash layer is at least 50 kg per 1 m 3 /s of fed gas. In practice, with a wetting reactor having a relatively straight bottom, this would mean an ash layer of at least about 25 cm at the bottom of the reactor. If the reactor bottom is V-shaped, the ash layer has to be thicker. It has been found that prerequisite for an ef¬ fective function of a horizontal blade mixer is that the ash level is preferably higher than the shaft of the mixer. On the other hand, the ash layer should not gen¬ erally be thicker than what is required for an effective function of the mixer in the upper part of the ash layer and for its capability of throwing particles from the ash layer to the gas space thereabove. Neither should the ash level be higher than the actual inlet level of the gas. The hot gas introduced into the reactor may also serve as a drying gas, and it is brought into contact with and to dry wetted ash particles and lumps of particles flowing downwardly from the wetting zone. Ash particles from the lower section of the reactor are carried away by the upwardly flowing drying gas and conveyed back upwards into the wetting zone in order to activate the still unreacted reagent or absorbent contained in the ash. In the wetting reactor, the particles are separated from the gases by means of a filter and are then returned to the lower section of the reactor. In this way, an internal circulation of reagent or absorbent particles is brought about in the wetting reactor and a relatively high den¬ sity of particles is maintained therein. The particles are separated from the gas, e.g., in a fabric filter, electric filter or some other equivalent type of separator. Particles are detached from the filter either intermittently or continuously, e.g., by pulse flushing, backwash or shaking, whereby the particles drop either separately or in lumps downwards in the wet- ting reactor. At least a part of the particles stick to each other in the wetting zone or at the filter and form bigger agglom¬ erates and pass thereafter downwards through the wetting zone all the way to the lower section of the reactor, whereas single small particles are easily carried away by the upwardly flowing gas and are conveyed from the wet- ting zone into the upper section of the reactor. Bigger lumps of particles and wet, heavy particles are dried and ground into finer particulates by mixing when they reach the ash layer in the lower section of the reactor. Thorough mixing of the particles by mixing members in the lower section of the reactor gives a positive effect, equalizing heat and moistness in the ash layer, for homo¬ genizing the ash material. As the particles are ground smaller, their reactive area increases and at least part of them whirls upwards above the ash level, being conse¬ quently carried away with the drying gases upwards and back into the wetting zone. In the wetting zone, the particles are reactivated and will again be capable of absorbing sulfur in the reaction zone. Mixing, which has been brought about by a mechanical or equivalent strong mixer, has been found to be of essential importance to the runnability of the wetting reactor. The task of mixing is - to serve as transfer means for ashes, conveying them from various parts of the reactor bottom towards the outlet/outlets; - to homogenize the ashes by mixing them to a suitable form for preferably pneumatic transfer; - to crush moist or dried lumps of ash to a fine form. Dry ash, which falls down during filter cleaning or is otherwise separated from the flue gas when it enters the reactor, serves as an efficient drying agent for the moist ash and water drops falling down from the wetting zone. The mixer mixes moist and dry substances, whereby the earlier mentioned homogenization is effected. The mixer also whirls ashes above the ash layer or ash buffer, whereby the hot gas (flue gas) conducted to the lower level carries it away, thereby causing internal ash circulation in the reactor. This will further intensify the transmission of the drying energy relieved by the gas to moist ash particles. Mixing and recycling of the particles increases the resi- dence time, dust density, Ca/S mole ratio and total sur¬ face area of the lime particles in the reaction zone, thereby decreasing the need for new reagent. According to the invention, an average particle density is maintained by internal circulation in the wetting reactor, which density is clearly higher than the particle density in the gas introduced into the reactor. The internal circu¬ lation can be controlled by regulating the amount and velocity of the particle flow whirling upwards from the ash layer. The location of the feeding point of the inlet gas also has an effect on the recycling. The shorter the distance from which the gas spray is directed to the ash layer, the more particles are entrained with the gas spray and are carried upwards therewith. Part of the particles is preferably removed from the reactor through an outlet disposed in the lower section of the wetting reactor below the drying zone. Part of the discharged particles may be returned to the wetting reac¬ tor if desired. Thus, external circulation of particles may also be provided in connection with the wetting reac¬ tor. Particles may be treated outside the reactor, for example, to regenerate some reagent. The particle density may be controlled in the reactor by regulating the amount of particles removed from the lower section of the reactor, for example, by leading particles from the ash layer over an adjustable overflow level to an ash discharge opening and further to an ash discharge duct. The volume of the ash layer may also be adjusted by a level control means, which controls the flow through a discharge opening or discharge duct. External particle circulation in the wetting reactor may be provided by connecting a filter or an equivalent par¬ ticle separator, which is either totally or partly dis¬ posed outside the reactor, to the upper section of the wetting reactor. In such a filter or particle separator, reacted and still unreacted absorbent particles are sep¬ arated from the gases, at least part of which particles is directly returned to the lower section of the wetting reactor, preferably to the drying zone. Particles may be detached from the filter either continuously or-intermit¬ tently and be returned to the lower section of the wet¬ ting reactor. Part of the material separated by means of the particle separator may be totally removed from the system. By the method according to the invention, it is possible to decrease the average temperature of the gases in the wetting reactor to a level which is about 0 - 20°C, pre¬ ferably 0 - 10°C, from the dew point, and even to the actual dew point, and still to avoid the drawbacks caused by too wet particles in the upper or lower sections of the reactor. The particles wetted in the wetting zone and falling downwardly are dried by the hot gas flow in the drying zone, thereby not causing any trouble in the lower section of the reactor. Due to recycling, the differences in temperature and moistness are very small also above the wetting zone, at various cross-sectional points of the reactor. In this way, local troubles caused by wetted particles or water drops are avoided. In accordance with a preferred embodiment of the inven¬ tion, layers formed by wetted particles on the walls of the wetting reactor may be avoided in such a manner that at least a part of the gas fed into the wetting zone is conducted into the wetting reactor as jacket flow so that the gases, either indirectly or directly, heat the reac- tor walls. The gas is conducted into the reactor through ducts disposed, e.g., in the walls, whereby the hot gas flowing in the ducts prevents the walls from cooling and thereby solids from depositing layers on the walls. The gases may also be injected directly to the inside of the reactor and caused to flow downwardly along the walls, protecting the walls. Thereby, the wetted particles are either directed away from the wall or they dry when pas¬ sing through the jacket flow prior to touching the wall. The jacket flow is brought about by feeding gas, e.g., into a cylindrical reactor via an annular opening in its wall. Removing of deposits from the walls may also be inten- sified by shaking or by constructing the walls of flex¬ ible material, whereby pressure fluctuations normally occuring in the system will shake the walls, causing the deposits to fall down. Especially in big reactors, gas may also be introduced into the inner part of the wetting zone for providing a gas distribution as even as possible in the reactor. Gas may be fed, e.g., through a plurality of nozzles or slots disposed in the gas duct in the middle part of the reac- tor. Gas may also be fed into the wetting reactor from several different levels. The hot gas introduced into the lower section of the reactor is of great significance because its task is, e.g. - to relieve drying energy for drying moist ash or water drops; - to convey ashes whirled by the mixer back to the wet¬ ting zone, thereby providing an internal ash circulaton in the reactor; and - to maintain the reactor walls warm, which further re¬ duces the tendency to deposit layers on the walls. By sprays of water or steam, a wetting zone is provided in the upper or middle section of the wetting reactor. Water is preferably sprayed into the flue gases, mainly downwards from above the gas inlets. Sprays of water or steam are preferably so arranged that as much as possible of the gas flow is evenly covered. The wetting zone of the wetting reactor is preferably provided with downwardly directed water or water vapor nozzles, disposed, for example, in the support members running horizontally through the wetting reactor. The filter disposed in the upper section of the wetting reactor is preferably a fabric filter such as a hose or cassette filter, or possibly an electric or some other equivalent type of filter, wherefrom particles are re¬ turned to the lower section of the reactor by shaking or back-blowing the filter. The lower section of the reactor is preferably provided with a mechanical mixer, mixing solid material accumu¬ lated in the lower section of the reactor. Mixing of solid material intensifies the equalization of the oist- ness and heat of the particles, whereby the particles which are still wet will be dried when coming into con¬ tact with drier and hotter particles. At the same time, the mixer breaks the lumps of particles so as to facili¬ tate them to be conveyed upwards in the reactor by the gas flow. Thus, the mixer intensifies the effect of the drying gas for bringing about internal circulation of particles in the reactor. The speed of the mixer is ad¬ justable, and together with the gas flow entering the mixing area, a wide range of adjustment of particle cir¬ culation is thereby provided. The lower section of the wetting reactor is provided with means for discharging particles from the reactor. Par- tides are preferably discharged by the mixer described above. The blades of the mixer can be directed askew so that they gradually move particles to one end of the lower section of the reactor, wherefrom the particles can be removed dry through a suitable sealing means. They may also be removed by a separate discharge screw or a dis¬ charge conveyor. Particles are discharged from the wet¬ ting reactor preferably in such a dry state that they can be further conveyed, for example, pneumatically. The discharge opening has to be so disposed that an ash storage is formed in the mixer, the volume (height) of the ash storage depending on the mixer dimensions. For example, if a blade mixer is used where the shaft is horizontal, the ash level is preferably at least the same as the shaft level. However, the ash level should not exceed the point above which the mixer no longer has any mixing effect in the upper layer of ash. With blade mixers, the effective height is about 1 to 4 times the mixer diameter. The mixer diameter is about twice the blade length. Besides blade mixers with horizontal shafts, also other types of mixers may be used. Cylindrical reactors may employ, e.g., vertical mixers or jet-mill based local mixers or grinders where steam or air brings about the mixing effect. If necessary, the lower section of the wetting reactor may be provided with a separate feeding point for reagent or absorbent. Several different reagents may be intro¬ duced into the wetting reactor for removing harmful sub¬ stances from the gases in one stage. The arrangement according to the invention provides e.g. the following advantages over the earlier known arrange¬ ments: - Several functions, such as sulfur absorption, wetting of reagent, particle separation and drying, may be con¬ centrated in one apparatus. Wetting of gas may be arranged in the same space as the existing ash separ- ation, whereby neither extra devices nor separate reac¬ tors are needed for each partial process. - By the present invention, it is possible to operate very close to the dew point, even almost at the dew point, as the filter is directly arranged in the reactor, and no gas ducts are needed, whereby the problem of lay¬ ers depositing on the walls of such gas ducts is avoided in conveyance of gas which becomes wet when close to the dew point. The possiblity of operating close to the dew point results in a highly efficient elimination of S0 2 , S0 3 , HC1 and HF emissions. - Internal circulation of particles through the wetting zone cuts down the consumption of reagent or absorbent. By this method, the residence time of the absorbent in the reactor becomes essentially longer, preferably about 2 to 10 times longer in comparison with earlier known once-through reactors. - Fine ash is also separated from the gases in this ap¬ paratus. Ash and consumed absorbent may be recovered dry and in a common step. Only one ash removal system and ash treatment is needed. Dry ash and absorbent may be con¬ veyed pneumatically. - In the earlier known methods, only if the S0 2 content of the inlet gas has been < 40 ppm, almost complete sulfur absorption has been provided in the wetting stage with S0 2 containing gases. By the method of the invention, com¬ plete sulfur removal is possible even though the S0 2 content of the inlet gas is > 100 ppm. - The method is simple. In the arrangement according to the invention, three main factors having an positive effect on absorbing reactions may be used simultaneously and optimally: - cooling of gas to a temperature level which is close to the dew point in order to provide fast reactions; - high Ca/S mole ratio in the reaction zone; and - long residence time for optimal utilization of the absorbent. The invention is further described below, by way of ex¬ ample, with reference to the accompanying schematic draw¬ ings, in which Fig. 1 is a schematic illustration of a preferred ap¬ paratus for implementing the method of the in¬ vention. Figs. 2 and 3 are schematic illustrations of two other appar¬ atuses for implementing the method of the inven¬ tion, and Fig. 4 shows the ratio of S0 2 reduction to Ca/S mole ratio in an embodiment of the invention. Fig. 1 discloses a wetting reactor 10 provided with gas inlets 12 and 14, a gas outlet duct 16 and a discharge duct 18 for particles separated from the gas. The wetting reactor is also provided with nozzles 20 for spraying water or steam into the wetting reactor above the gas inlets. The upper section of the reactor is provided with a filter 22 for separating particles from the upwardly flowing gas. The wetting reactor according to the invention may be disposed in the flue gas duct after the combustion cham¬ ber of a grate furnace, pulverized fuel combustor or fluidized bed combustor, such as a circulating fluidized bed reactor, whereby the wetting reactor is preferably disposed after the heat recovery boiler. Prior to enter¬ ing the wetting reactor, the flue gases are cooled to < 300°C, preferably to < 150°C. For removing sulfur oxides from the flue gases, absorbent, such as limestone, has been fed into the combustion chamber or fluidized bed reactor or thereafter. The absorbent is at least partly calcined in hot flue gas to calcium oxide, which absorbs sulfur as calcium sulphate and calcium sulphite. The lime/sulfur ratio of 1.5 - 2.1 produces about 80 to 95 % sulfur reduction in a circulating fluidized bed reactor. The flue gases still contain sulfur as well as unreacted lime when entering the wetting reactor. An important object of the wetting reactor according to the invention is to activate lime or other absorbent in the flue gases so that the rest of the sulfur will also be removable from the flue gases. In the arrangement shown in Fig. 1, flue gases containing sulfur and lime are conveyed through pipe 24 into the wetting reactor. Prior to feeding the flue gases into the reactor, they are divided into two separate flue gas flows in ducts 26 and 28. The flue gas flow in duct 26 is conducted into the reactor, substantially to the same level as the water sprays 20. The flue gas flow in duct 28 is conducted to a substantially lower level. One flue gas flow is conducted into the wetting reactor substantially to the same level as the water sprays, either above or below or to exactly the same level as the water sprays. It is essential that the gas fed into the reactor is well mixed with the water spray. Both the gas and the water are preferably fed into the reactor as a downwardly flowing spray, which, at a small distance from the inlet, turns upwards. In this manner, vortices of gas and water spray are provided in the wetting zone and thereby also a good mixing effect. The water sprays constitute a wetting zone 30 in the wetting reactor. In this wetting zone, the flue gases are wetted and cooled as close to the dew point thereof as possible, preferably to about 0 - 3°C therefrom. In the wetting zone, the lime particles are wetted, whereby sulfur is absorbed by the particles and fast ionic reac¬ tions between sulfur and calcium can take place in the liquid phase. Water is preferably sprayed from nozzles, which produce small drops, preferably < 100 μm in size, and which are large-angled so that the reactor cross-section and the gas flow are well covered. Water is sprayed downwardly. The wetting zone covers the vertical zone of the reactor which preferably equals the hydraulic diameter of the reactor. In the embodiment shown in Fig. 1, flue gas is introduced into the reactor as jacket flow. From duct 26 the gas is first conveyed into a tubular duct 32 surrounding the reactor. From the tubular duct, the gases are further conveyed into one or more downwardly directed ducts 36 defined by the reactor wall 34. The reactor is double- walled so as to form an inlet duct 36 for flue gas between the walls 34 and 38. From ducts 36, the flue gases are conveyed through inlets 12 into the wetting zone 30 in the reactor. Correspondingly, gas is conducted from the lower gas duct 28 to a tubular duct 42 surrounding the reactor and therfrom further to a downwardly directed duct 46 defined - by the reactor walls 44. From that duct 46, the flue gases flow into the lower section i.e. the drying or mixing zone 40, of the reactor. Introduction of gas into the wetting reactor is control- lable, e.g., by means of dampers 27 and 29 in ducts 26 and 28. Introduction of gas is also controllable by means of an adjustable slot 48 in the duct 46. The gases flow from the drying zone upwards, thereby drying particles flowing downdardly from the filter and the wetting zone. The flow of drying gas is automatically adjustable by members 47 and 49, in accordance with the temperature of the gas in the lower section of the reac¬ tor or the temperature of the particles to be discharged. Further, the lower section of the reactor is equipped with mechanical mixers 50. The embodiment shown in Fig. 1 has two such mixers lying on the bottom of the reactor and being provided with blades 52. The mixers break the lumps of particles falling down to the lower section of the reactor. At the same time, they equalize the tempera¬ ture and moistness between the particles. The mixers operate preferably so that they "splash" a portion of the particles from the ash layer upwards to the gas space of the drying zone, wherefrom the upwardly flowing hot gas flow carries these particles through the wetting zone possibly as far as the upper section of the reactor. The mixer blades are preferably so disposed that they, when rotating, gradually move particles to one end of the lower section of the reactor, said end being provided with a discharge duct 18 for particles. The particles preferably flow over an over-flow plate, not disclosed, into the discharge duct. In this manner, a "buffer" of particles, which equalizes the temperature and moistness of the down-flowing particles, is always maintained in the reactor. Fig. 2 shows a wetting reactor 10 similar to that of Fig. 1, except that gas is introduced into the lower section of the reactor via a gas inlet duct 54 disposed inside the reactor. The gas inlet duct is provided with down¬ wardly directed nozzles 56, through which the gas first flows towards the particles accumulated in the lower section of the reactor and thereafter upwards. In this way, mixing is provided also by means of gas among the particles accumulated in the lower section of the reac¬ tor. In the reactor according to Fig. 2, the amount of water fed into the wetting zone is regulated by a member 21 according to the temperature of the gas in the upper section of the reactor. The wetting reactor may be pro¬ vided with water nozzles on several different levels if required for the gas to be evenly wetted. In Figs. 1 and 2, the reactors are made up of hose fil¬ ter chambers, each of which has a standard filter and, in the lower section of the chamber, a wetting zone and a drying zone. Fig. 3 illustrates a reactor in which a filter 60 is disposed immediately outside the reactor chamber. Thus, in addition to internal circulation, also external circu¬ lation of particles is effected in the reactor. Some of the particles wetted in the wetting zone 30 separate from the gases by themselves and flow, because of their weight, down to the drying section, where they become under the influence of the drying gas. After drying, the particles again flow upwards, entrained with the gases, thereby constituting internal circulation. Part of the wetted particles follow the gases to the upper section of the reactor and to the filter 60 and will be returned via duct 62 to the drying section 40. If necessary, particles may be removed from the circulation by outlet means 64, which may be closed by a valve 66. In Fig. 3, the flue gas inlet ducts 26 and 28 may be connected to different points of the combustion pro¬ cesses, for example so that, the gas brought into the reactor via duct 26 has been more cooled than the gas brought via duct 28, which duct may bring hotter gas for ensuring the drying process. Compared with the prior art, the invention provides much better sulfur absorption of flue gases with much lower lime consumption, as indicated by the accompanying results of tests made on certain coal and limestone grades. Example Means in accordance with Fig. 1 was used in the test run. The wetting reactor was supplied with flue gases of about 870°C from a circulating fluidized bed reactor, which had been supplied with limestone the mole ratio Ca/S being 1.41 - 2.33. The theoretic S0 2 content of the flue gases was 860 to 960 ppm. The sulfur contained in the flue gases reacted already in the circulating fluidized bed reactor prior to the wetting reactor in such a manner that the S0 2 content of the flue gases entering the wet¬ ting reactor was about 60 to 201 ppm. The gases were conducted into the wetting reactor at a temperature of about 139 to 160°C. The theoretic dew point of the gases in the wetting reactor was about 54°C. The test results are shown by the table below. Ca/S Temp. S0 2 S0 2 so 2 after before after abs reactor reactor reactor mol/mol °C ppm ppm 2.00 66 136 61 93 2.08 81 77 53 95 The test results clearly indicate that, by the method according to the invention, sulfur absorption is almost complete even with very low Ca/S mole ratios when the final reactions take place nearly at the dew point, i.e. 1-5°C from the dew point. Very good results are achieved even with the highest temperatures, i.e. 10-30°C from the dew point, and with much lower lime consumption than in earlier known methods. According to information in literature, the wetting reac- tors of prior art have given about 90% S0 2 reduction with a mole ratio of Ca/S = 2.22. About 98% S0 2 reduction has not been achieved until the mole ratio has been Ca/S = 4. Fig. 4 shows the ratio of S0 2 reduction to Ca/S mole ratio received in the above described series of test runs when applying the method according to the invention. As a comparison, the figure also shows the ratio of S0 2 reduc¬ tion to the Ca/S mole ratio when the test run is per- formed without the wetting reactor. As a conclusion, the present invention enables combining of various stages of several different processes into a ' whole: - A wetting reactor, made up of the space below the fil¬ ter cassettes or the like. A nozzle system disposed in this space sprays water for wetting the ash and absorbent particles and for dropping the flue gas temperature close to the dew point, i.e. 0-20°C therefrom. - A fabric filter or the like, which operates either on the ordinary counterflow cleaning principle, with pres¬ sure pulses, backwash or shaking. - Combined mixing and transfer means for ash and absorb¬ ent, disposed, for example, in the receiving hopper at the bottom of the reactor. The mixing means preferably rotates at such a high velocity that it breaks the de- posits which, when wet, fall down from the walls and filter, and which are dried by the hot gas flow. - Circulation of ash and absorbent, which is brought about by blowing part of the incoming flue gas into the reactor via the lower section thereof. Gas may also be blown into the reactor from below the mixers in such a manner that the gas fluidizes the particle mass accumu¬ lated in the lower section of the reactor. The gas intro¬ duced into the reactor from the lower section thereof together with the main gas flow coming from the side walls dries the wet lumps of particles .falling down from the upper section of the wetting reactor. The gases catch part of the particles back into the wetting zone, thereby resulting in an internal circulation of particles in the wetting reactor.

Claims: We claim: 1. A method of purification of gases produced e.g. in combustion, gasification or chemical processes, said gases containing pollutants such as sulfur oxides, chlor¬ ine or fluorine compounds - by adding to the gases, in or after the process, reagent and/or absorbent reacting with pollutants con¬ tained in the gases, - by introducing the gases into a wetting reactor for wetting the gases by water or steam in order to activate the reagent and/or absorbent contained the gases, com¬ prising introduction of the gases into the wetting reac¬ tor to the lower section thereof and further upwards into the wetting zone of the wetting reactor, where the sus¬ pension produced of gas and reagent and/or absorbent is wetted with water and/or steam, and - by separating the completely or partly reacted reagent and/or absorbent particles in a filter disposed in the upper section of the wetting reactor prior to discharging the gases from the wetting reactor, characterized in that - so thick an ash layer is maintained below the gas inlet level in the lower section of the wetting reactor that the ash layer, formed of particles separated from the gas, is capable of homogenizing the wet ash particles and water drops falling downwards from the upper section of the wetting reactor. 2. A method as claimed in claim 1, characterized in that solid particles are separated from the gases discharged from the wetting reactor in a filter disposed in the upper section of the wetting reactor, from which filter particles are detached intermittently and then allowed to drop to the wetting zone and/or to the lower section of the wetting reactor. 3. A method as claimed in claim 1, characterized in that the inlet gas is brought into contact with and to dry wet particles flowing downwardly from the wetting zone. 4. A method as claimed in claim 1, characterized in that the gas fed into the space below the wetting zone is caused to recycle part of the particles accumulated in the lower section of the wetting reactor into the upper section thereof. 5. A method as claimed in claim 1, characterized in that in the ash layer is disposed a mixer for mixing wet par¬ ticles and water drops with the ash layer. 6. A method as claimed in claim 5, characterized in that the mixer also serves as a grinder breaking big lumps of particles. 7. A method as claimed in claim 1, characterized in that the gas fed into the space below the wetting zone is fed as one or more sprays which are at least partly directed downwardly so that the gas spray breaks lumps of par¬ ticles accumulated in the lower section of the reactor and mixes particles. 8. A method as claimed in claim 1, characterized in that particles are discharged from the lower section of the wetting reactor. 9. A method as claimed in claim 8, characterized in that part of the particles discharged from the lower section of the wetting reactor are recycled into the wetting reactor. 10. A method as claimed in claim 9, characterized in that particles are wetted outside the wetting reactor prior to recycling them. 11. A method as claimed in claim 1, characterized in that the gases are cooled in the wetting reactor to a tempera¬ ture of about 0-20°C from the dew point. 12. A method as claimed in claim 11, characterized in that the gases are cooled to a temperature of 0-10°C from the dew point. 13. A method as claimed in claim 1, characterized in that the volume of the ash layer is at least 50 kg per m 3 /s of inlet gas. 14. A method as claimed in claim 1, characterized in that the thickness of the ash layer is at least 25 cm. 15. A method as claimed in claim 1, characterized in that the ash layer extends at least to the level of the mixer shaft. 16. A method as claimed in claim 1, characterized in that at least a part of the gas to be introduced into the wetting zone is fed into the wetting reactor as jacket flow so that the gas flows into the wetting zone through ducts disposed in the walls of the wetting reactor and/or along the walls of the wetting reactor as a downwardly flowing spray, whereby the jacket flow prevents the walls from cooling and layers of solids from depositing on the walls. 17. A method as claimed in claim 1, characterized in that at least a part of the gas to be introduced into the drying zone is conducted into the wetting reactor as jacket flow so that the gas flows into the drying zone via ducts disposed in the walls of the wetting reactor, whereby cooling of the walls is prevented. 18. A method as claimed in claim 1, characterized in that water or steam is fed as downwardly directed sprays into the wetting zone. 19. A method as claimed in claim 1, characterized in that water or steam is fed into a plurality of zones in the wetting reactor. 20. A method as claimed in claim 1, characterized in that recycling or internal particle circulation in the wetting reactor is controlled by adjusting the flow of ash to be discharged.

Inventors: KUIVALAINEN REIJO, KUIVALAINEN, REIJO
Applicants: AHLSTROEM OY, A. AHLSTROM CORPORATION
Application year: 1991
Main classification: B01D53
IPC codes: B01D53