FI59160C - FOERFARANDE FOER FOERAONGNING AV VAETSKA OCH ANORDNING FOER UTFOERANDE AV DETSAMMA - Google Patents

Description

ΠΕΞΕμΠ rm ^ ANNOUNCEMENT ΓΛ Λ cr \ LEAVE * W (11> UTtÄ06NIM «* SKRIFT 591 60 ^ ^ (SI) K» .IV? /Vita.3 F 22 B 1/26, B OI D 1/18 FINLAND —FINLAND (21) IWttlh * k.mui-P * t.nt »i» .elcn (nI 2 ^ 70/72 (22) Hukumlipllvl - AiMBlmlngrfag 08.09.72 (23) AlkupUvI · -GNtlghitadag 08.09-72 (41) Tullut | ulklMk (l —Mivlt offancllg 11.03.73

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Patent »Regulatory Regulation Amektm uchgd och utUkriftm puMicond 27 * 02.8l (32) (33) (31) otoolkou * —Bogird prior

Denmark-Danmark (DK) ^^ 6 ^ / 71 (71) Aktieselskabet Niro Atomizer, Gladsaxevej 305 »DK-2860 Sjfborg, Denmark-Danmark (DK) (72) Jörgen Damgaard-Iversen, Birkertfd, Klaus Erik Gude, Vedbaek,

Ovel Emil Hansen, Vaerl ^ se, Bj ^ rn Lund, Frederiksberg,

Mogens Petersen, Lyngby, Denmark-Danmark (DK) (7 * 0 Forssen & Salomaa Oy (5U) Liquid evaporation method and apparatus for carrying out the method -Förfarande för förängning av vätska och anordning för utforande av detsamma

The invention relates to a method for evaporating a liquid. In this context, both the case in which a liquid is evaporated from a solution or slurry which is still in liquid form after evaporation, the case in which the liquid or slurry is completely evaporated, and the case where it is desired to cool the warm gas by injecting water therein are considered. The invention thus comprises both the so-called spray drying and spray sealing as well as condensation, i.e. flue gas or flue gas cooling and / or humidification.

It is known to achieve such evaporation of a liquid from a slurry or solution by passing it into an evaporation chamber, to which a flow of warm drying gas is simultaneously introduced. The amount of steam that the drying gas can take with it as it passes through the evaporation chamber and is transported out of it is dependent on the gas inlet temperature, taking into account the moisture content of the given drying gas. In order to achieve a high evaporation capacity, it is therefore necessary to aim for a high temperature of the drying gas when it is introduced into the evaporation chamber. Therefore, in certain cases, flue gas from a bulb of 2,591,60, mainly an oil bulb, has been used as the drying gas, which is led directly to the evaporation chamber from the bulb. However, it has been found that the temperature of the drying gas can then become so high that special measures must be taken to protect the walls of the evaporation chamber. These walls can, for example, be lined with refractory stones or other refractory material, which, however, is a relatively expensive solution. In addition, e.g. in U.S. Patent No. 2,818,917, it has been proposed to calculate the temperature of the flue gas from the bulb by mixing this flue gas with cold air as the gas is introduced into the evaporation chamber. However, this latter solution does not achieve the desired high evaporation capacity.

In addition, when a high inlet gas inlet temperature is used, even if only spray agglomeration is performed, which means that the treated slurry or solution is still in liquid form after treatment, problems often arise as the evaporation process must be temporarily interrupted so that the chamber walls can be cleaned.

One solution is also disclosed in DE patent publication No. 576,448, which deals with a steam generator in which a 2: 1 mixture of water and oxygen is used as fuel, whereby the combustion gas becomes pure water vapor. The combustion gas stream is made to impinge on the corrugated plate d, which then heats up strongly, and water is sprayed on the other side of the plate from the spray nozzle c, whereby the water evaporates. If an attempt were made with this known structure to reduce by evaporating or evaporating to dryness an aqueous solution or other liquid containing a solid with the aid of normal flue gas from the burner, soot and other combustion products would deposit very quickly on one side of the plates. , which have been in a solution evaporated to dryness. As a result, the device should be stopped frequently to clean the discs d.

By the method according to the invention, the liquid is introduced mainly from above centrally into the evaporation chamber, into which warm flue gas or combustion gas is introduced, which from below is caused to flow mainly axially into the evaporation chamber and in the direction opposite the liquid inlet. The process according to the invention is characterized in that the liquid is introduced into the evaporation chamber in a dispersed form in a manner known per se and that a substantial part of the gas phase is discharged from the evaporation chamber at a level below the level of the liquid inlet.

From below and axially into the evaporation chamber, the warm flue gas or combustion gas first encounters the decomposed liquid from the inlet and since the gas phase is discharged from the evaporation chamber in a plane substantially , from which the gas phase is led out of the evaporation chamber. The gas stream directed axially upwards and towards the liquid inlet tends to spread the dispersed liquid so that the floating layer of liquid droplets is continuously like a protective umbrella above the jet-shaped flue gas stream. It can thus be achieved that some of the liquid droplets, when it comes to spray sealing, constantly meet the side wall of the evaporation chamber and keep this moist. Thus, the wall of the evaporation chamber is partly protected from warm flue gases and partly the solid constituents of the liquid - when this liquid is e.g. a solution or a slurry - which may be attached to the side wall of the evaporation chamber are released or dissolved by these liquid droplets. In the case of spray-drying a solution or slurry, a body below the ceiling surface of the evaporation chamber is preferably introduced into the liquid inlet so that the liquid particles, which are circulated in the direction towards the ceiling surface, have time to evaporate before encountering this.

It is known in connection with spray drying and spray compaction to introduce the flue gas from below into the evaporation chamber and to lead the gas phase out in a plane which is below the level of the liquid inlet. With this known method, it is cumbersome to achieve a dispersed inflow of drying gas into the evaporation chamber, i. that an attempt is made by means of special diffusing means to dissipate the drying gas stream so that it flows into the evaporation chamber in all directions. Similarly, a drying gas is used at a temperature so low that it does not damage the dispersing members or the wall of the evaporation chamber, although it encounters this until the liquid particles from the dispenser have substantially cooled it.

V.! 4,59160

The process according to the invention has also proved to be very suitable for the condensation of combustion gases, e.g. to give these gases a temperature and / or humidity such that they can be passed through and cleaned in conventional filter devices. The flue gases to be cleaned in the filter equipment must first have a temperature so low that the filter material is not damaged, and in the case of a filter device operating on an electrostatic principle, it is important for the proper operation of the filter device that there is a suitable amount of water vapor. It is known to cool and humidify the combustion gas or flue gas in a tower or pipe with a jet nozzle installation, and while the flue gas flows through such a condensing tower, water is injected into the gas stream by means of nozzles. However, the process according to the invention allows very efficient cooling and humidification using a simple diffuser, and it has been found that the special flow rates achieved by the process according to the invention do not cause problems in separating particles of ash, soot or other substances. must be refrigerated and / or humidified, may carry very large quantities.

According to the invention, flue gas with a temperature of more than 300 ° C, in particular more than 600 ° C, can be used. This high temperature also ensures the special flow pattern achieved by the method according to the invention so that the walls of the evaporation chamber are not damaged, and it has been shown that using the combustion or flue gas with said high temperature such as nitrophosphate fertilizer solution, which begins to decompose at 115-120 ° C.

The flue or flue gas used in the process according to the invention may, as previously mentioned, contain e.g. soot or ash particles from the combustion process by which the flue gas used is produced, but according to the invention sand or other particulate matter may be introduced into the flue gas stream before being introduced into the evaporation chamber. . This can be advantageous, for example, when the ore concentrate is treated in the evaporation chamber, which in further processing in the melting furnace requires a melting agent, e.g. sand, among them. This sand is usually present in the wet state, and it has been shown that using the process of the invention the sand can be fed directly to a growth gas stream, thus achieving partly drying of the sand and partly complete mixing of the sand and ore concentrate, which ore concentrate is treated in the evaporation chamber. According to the invention, the particulate matter is preferably introduced into the flue gas stream by a movement parallel to the flue gas stream.

According to the invention, the gas phase can be led out of the evaporation chamber in a plane which is close to or below the plane above which the flue gas is introduced into the evaporation chamber. Thus, the tendency is that the warm flue gas could otherwise, after flowing into the evaporation chamber, flow directly to the outlet point or points of the gas phase, and the residence time of the flue gas in the evaporation chamber is thus extended.

The previously mentioned, sometimes desirable wetting of the side wall of the evaporation chamber can be promoted so that the liquid, while being introduced into the evaporation chamber in a dispersed form, can be radially outwardly directed towards the side wall of the chamber according to the invention.

According to the invention, this can advantageously be achieved by introducing the liquid into the evaporation chamber by means of a centrifugal diffuser. Such a centrifugal diffuser has the advantage over a diffuser nozzle that the dissipation efficiency to a large extent somehow depends on the amount of liquid dissipated per unit time, which means that the amount of liquid dissipated by the centrifugal diffuser can be continuously adjusted depending on the weather speed. This is essential, for example, when the flue gas is led from a melting furnace which is fed in stages.

The invention further comprises an apparatus for carrying out the described method and is one having an evaporation chamber and a flue gas or flue gas weather pipe which is introduced from below and mainly centrally into the evaporation chamber and which descends into this chamber to produce a substantially axially directed flue gas flow. in addition one or more gas phase outlets lead to the evaporation chamber, and the device according to the invention is characterized in that the end leading to the evaporation chamber of the liquid inlet is provided in a known manner Such an apparatus absorbs a flow of 6,591,160 warm flue gas entering the evaporation chamber through the flue gas inlet pipe, as previously described, the jet well and the decomposed liquid from the liquid diffuser isolates it to some extent from the side wall of the evaporation chamber.

The invention will now be described in more detail with reference to the drawing, in which Figure 1 schematically shows a first embodiment of a spray sealing device according to the invention, Figures 2-4 show further embodiments for using an evaporation chamber the flue gas stream.

The evaporator shown in Fig. 1, which is a so-called spray sealing device, has an evaporation chamber made mainly of sheet metal, e.g. stainless steel, into which a central exhaust diffuser 11 is introduced centrally from above via a first to tank 14, which is for solution or slurry, which is evaporated. The centrifugal diffuser 11 is further connected to the cooling water line 15, by means of which the cooling water can be circulated through the diffuser. The evaporation chamber 10 has the shape of a double funnel at the bottom, and centrally into the evaporation chamber a flue gas line 16 is directed axially towards the centrifugal diffuser 11, which may be a refractory material coated with a stainless steel plate on the outside and which may be a flue gas burner 17. The device shown also has a pair of outlet pipes 18 through which the gas phase can be sucked out by means of the air pump shown.

The device shown in Figure 1 has not only a liquid tank 14 but also a liquid tank 19. The pump 20 can be used to pump sludge or solution through pipelines 21 to liquid dispersing members 22 in the discharge pipes 18, which suitably have the shape of a dispersing nozzle. Each of the outlet pipes 18 7 59160 descends into a cyclone 23 or other device capable of separating gases from the liquid phases, and these cyclones are connected to lines 24 for draining the gas phase and lines 25 serving to lead the separated liquid phase down to the liquid tank 14. , which are connected by means of lines 27 to a pump and a cooling water tank (not shown) so that the evaporation chamber can be injected internally with cooling water if the centrifugal diffuser 11 fails so that it does not lead the disintegrated solution or sludge into the evaporation chamber.

The flue gas pipe 16 is provided at its upper end with an outer collar 39, which forms an upwardly open trough or basin. The upper edge of the collar is provided with a number of spaced cuts, and the edge formed by the collar has an extension 40 into which the liquid inlet pipe 41 lowers, by means of which the trough or basin can be filled with liquid 42 from the tank 19 at an adjustable speed. The circumferential partition wall 43 in the evaporation chamber, together with the flue gas pipe 16 and the lower part of the wall of the evaporation chamber 10, delimits a pair of separated liquid collection troughs, 44 and 45, the former 47 connected to the liquid tank 14 for flow control, e.g., surface inspection mechanism.

The gutter or basin 39 may not have turbulence-inducing members, e.g., tubes with openings through which air is blown. These members serve to prevent clogging of the pool 39, which clogs result from the deposition of solid matter therein.

The apparatus shown in Figure 1 operates as follows: The slurry or solution to be evaporated is introduced into the tank 19, and the tank 14 contains a slurry or solution which, as will be seen below, has condensed upon evaporation of the liquid. The pump 13 pumps the condensed solution or slurry from the tank 14 to the centrifugal diffuser 11 through the pipeline 12, which, as shown in Figure 1, circulates the dispersed liquid with a substantial radial component so that a quantity of which is constantly changing. The burner 17 is in operation, and the formed warm flue gas flows directly into the chamber 10 through the flue gas pipe 16 in an axial and anti-diffuser 11 flow. At the same time, the gas phase is sucked out of the evaporation chamber 10 through the outlet pipe IS. and between the liquid particles without the flue gas coming into contact with the side wall of the evaporation chamber 10 until the gas has cooled sufficiently in the vaporization of the liquid particles.

From the liquid tank 19, the pump 20 is used to pump the non-condensed sludge or solution through the pipelines 21 to the nozzles 22 arranged in the discharge lines. The direct connection thus obtained between the vaporizable, non-condensed solution or in vapor form and becomes discharged together with the rest of the gas phase through lines 24. The refluxing and now more condensed part of the slurry or solution is separated by cyclones 23 and passed through lines 25 to a tank 14 from where it can be pumped to the centrifugal diffuser 11 as described above and introduced in disintegrated form to the evaporation chamber 10 where final compaction takes place.

In order to prevent layers of solids from the solution or slurry being treated from the evaporation chamber from adhering to the upper side of the flue gas line 16 and overheating the flue gas pipe 16, the pool 39 is filled with liquid from the tank 19 by means of pump 42 and pipe 41. The liquid is filled into the basin 39 at such a suitable rate that the liquid flows over the upper edge of the collar 39, through the cuts therein, and flows down the circumferential side of the tube 16 in a uniformly circulating and substantially continuous liquid film. The liquid can be passed at such a rate that there is a suitable amount of non-vaporized return liquid at the lower end of the tube 16, which is collected in a collecting trough 44 and passed through a drying line 46 to a checker 47. From here the liquid flows through a tube 48 to a tank 14. from the liquid flow and is therefore used as an indicator of whether the amount of liquid discharged from the pump 42 is suitable. This liquid surface can be felt, for example, by means of a float 49,

Is-.

5 59160 which can control an alarm device, which draws the operator's attention if the liquid level goes outside the predetermined limits. It will be appreciated that other forms of devices or mechanisms may be used to monitor or control the rate at which the pool 39 is filled with liquid through the tube A1.

Thus, according to the countercurrent principle, the device according to Figure 1 undergoes jet compaction or evaporation in two stages, of which the first vaporization stage takes place in the discharge line 18 and the second and final vaporization stage takes place in the evaporation chamber 10. The finished, concentrated liquid product via an outlet line 28 connected thereto. The centrifugal diffuser can be kept at a suitable temperature by means of a refrigerant circulating through the lines 15. It will be appreciated that, if desired, a certain amount of solution or slurry may be periodically or continuously passed directly from one liquid tank 14 and 19 to another so that, if necessary, recirculation can be performed with part of the solution or slurry in the device or withdrawn. first stage processing.

The embodiment of the evaporation chamber 10 shown in Figure 2 can be used in connection with a spray drying device and is then in fact a drying chamber, or for cooling flue gas, e.g. because the gas must pass through an electrostatic precipitator. The bottom of the drying chamber has the shape of a double funnel, and a conveyor screw 29 may be provided at the bottom of each funnel to transport the pre-dried powder out of the drying chamber 10. In the embodiment shown in Figure 2. as shown. At the bottom of each cyclone 23, a conveying device 30 can be detected for any separated powder.

In the embodiment of the evaporation chamber shown in Figure 3, which is made for use in a spray dryer, the chamber 10 has only a conical shape of a simple funnel at the bottom and has only one simple outlet line 18 well below the outlet of the flue gas pipe 16. The embodiment shown in Figure 4 is also intended for use in a spray dryer. The drying chamber, i.e. the evaporation chamber 10, here again has the shape of a double hopper and the two outlet lines 18 are introduced in and extend along the flue gas pipe 16 in the upward direction. However, the pipes 18 terminate the distance of the body below the outlet of the flue gas pipe 16.

The embodiment shown in Figure 5 is intended for use in a spray sealing device, and the lower part of the evaporation chamber 10 is shaped as a simple funnel. In addition, there is only one simple outlet line 18 for the gas phase, and this line is arranged in such a way that the use of a special cyclone is unnecessary.

The embodiments shown in Figures 2-5 may have a piping and tank system, as shown in Figure 1, but the evaporation chambers shown may, of course, also be used in conjunction with other forms of equipment, e.g., equipment where evaporation occurs in a single step, or - if working in two or more stages - where the evaporation takes place in two or more evaporation chambers, one or more of which may be shaped according to the principles of the invention.

Figure 6 shows an embodiment of a device according to the invention for spray drying an ore concentrate while adding a melting agent. In this device, flue gas is produced by a bulb 31, which may be, for example, a coal burner and where there is an ash outlet 32 at the bottom. The flue gas line of the bulb communicates with a flue gas pipe 16 descending to the evaporation chamber or drying chamber 10. a weighing belt 50 from which the substance falls down the second conveyor belt 51 and causes it to fall down into the shaft 52, which lowers into the housing of the injection motor 34, which is forced so that it can inject a stream of particulate material diagonally into the pipe 16 immediately above the venturi 35. This venturi site causes a similar decomposition of the particulate matter in the gas stream, which is introduced into the flue gas pipe 16 by means of an injector by a velocity component directed in the direction of flow of the flue gas. The entry of particulate matter into the introducer 34 and the position of the moving damper 55 placed in the shaft 52 can be controlled by sensors 53 and 54, of which sensor 54 is an acoustic sensor.

The drying chamber, i.e. the evaporation chamber 10, is provided with flue gas outlets, Π 59160 which are located below the obliquely directed guide plates 38 and communicate with the electrostatic precipitator 36 by means of the exhaust ducts 18. Flue gas released from the electrostatic precipitator 36 The dry powder can be removed in a known manner from the bottom of the evaporation chamber 10 and from the electrostatic precipitator 36.

When the ore concentrate is dried in the described apparatus, a melt, e.g. wet sand, can be introduced into the flue gas pipe 16 by means of the ejector 34. The wet sand is dried and passed to a gas stream and thus becomes well mixed with the ore product to be dried, which is taken out of the drying chamber 10 and then further processed in a melting furnace.

The invention will now be further illustrated by the following examples:

Example 1 In a waste incineration plant, waste was treated with varying calorific values. The spent incinerator was not equipped with a steam pan to use the flue gas heat. The temperature of the flue gas varied between 1050 ° C and 700 ° C depending on the calorific value of the raw material, and since it was desired to be cleaned of dust in an electrostatic precipitator, the gas had to be cooled to 300 ° C. This cooling was carried out in an apparatus with the evaporation chamber 10 shown in Figure 2, from which the flue gas was introduced into the pipe 16 and in the chamber 10 water was dispersed by means of a diffuser 11.

The evaporation chamber was 610 cm in diameter and the cylinder height was 495 cm. The flue gas pipe 16 was made with a rectangular cross-section of 1200 x 1200 cm for easy cleaning.

3

A flue gas volume of 44,000 m / h was introduced into the chamber 10, and a volume of water of 17,000 kg / h at 1050 ° C and 9,000 kg / h at 700 ° C was decomposed, while the volume of water was automatically adjusted so that the outlet gas temperature was kept substantially constant at 300 ° C. .

i2 5 91 60

Example 2.

A gas condensing apparatus with a structure similar to that shown in Fig. 2 without cyclones was used to condense part of the gas coming from the electric melting furnace before the gas was passed to an electrostatic precipitator.

The furnace was used to produce iron silicate and feed gas with a dust content of about 2 g / m 2 and a temperature between 160 ° C and 260 ° C.

The gas was led to a gas condenser with a vaporization chamber of 2.25 m in diameter and a cylindrical side wall of 1.0 m in height. The diameter of the gas inlet pipe was 0.40 m. rotated at 18,000 rpm.

The gas from the gas condenser was taken out through a pipe on the side of the conical bottom of the evaporation chamber and led to a conventional electrostatic precipitator and from there to the outside air.

The amount of water fed to the diffuser was controlled by a pneumatic control system depending on the temperature of the outlet gas coming from the gas condenser.

3

The amount of gas from the gas condenser was about 5000 m / h and despite strong fluctuations in the temperature of the gas from the melting furnace, it was possible to keep the temperature of the gas from the gas condenser constant at 62 ° C ± 1 ° C.

After condensing this gas, the dust separation in the electrostatic precipitator was so efficient that the dust content of the gas after it passed through the separator ...... 3 was only about 82 mg / m.

Example 3

In an apparatus such as that described in Example 1, gas cooling was combined with drying of rotted sewage sludge.

i3 5 91 60

The sewage sludge was concentrated in a condenser to a dry matter content of 7% and then passed to a diffuser 11. It was used as an initial temperature for drying gas, i.e. flue gas 130 ° C, to give a product with 10% water. The product can either be used as a soil improver or sent to an incinerator for incineration.

During periods when the amount of sewage sludge discharged was too small relative to the available flue gas from the incinerator, water was added to the sewage sludge to the extent sufficient to maintain the feed gas temperature at 130 ° C, which in this case was the optimum temperature for the electrostatic precipitator.

Example 4.

For drying in the treatment of sulphate copper concentrate for smelting, an apparatus equipped with an evaporation chamber, as shown in Fig. 3, was used.

The ore concentrate had a sludge shape with a dry matter content of 72%.

The drying chamber 10 was 13 m in diameter and had a cylinder height of 7.5 m. The distance from the mouth of the flue gas pipe 16 to the diffuser 11 was 4 m. The vertical distance from the diffuser to the chamber roof was 2.5 m, and the diffuser was equipped with 600 hp. motor.

The sludge was fed in an amount of 220 tons / hour. 200,000 kg of dusty flue gas, produced by burning pulverized coal and at a temperature of 1000 ° C, was passed through the flue gas pipe 16 per hour. The drying gas left the device at a temperature of 130 ° C.

A dried powder with 0.2% water was produced. The total amount produced, which was separated in the drying chamber, cyclones and electrostatic precipitators, was 3800 tons / day.

Example 5

The apparatus equipped with the evaporation chamber shown in Fig. 6 was used for spray drying while adding a melting agent in the treatment of a sulphate copper nickel concentrate.

The evaporation chamber 10 had a diameter of 10 m and a cylinder height of 6.45 m.

The diameter of the pipe 16 was 2 m. The vertical distance from the upper edge of the pipe 16 to the diffuser wheel 11 was 4 m.

49,000 kg / h of copper-nickel sludge with a dry matter content of 65% was introduced into the diffuser 11. The drying gas is produced in a bulb 31, to which 2600 kg / h of pulverized coal containing 20% ash are fed. About half of the ash is removed through the opening 32 in the bottom of the bulb. The amount of flue gas produced was 55,000 kg / h and its temperature was 1000 ° C as it left the bulb.

From the hopper 33, 8170 kg / h of sand containing 7% of the sand 16 is introduced by means of the injector 34.

The powder parts collected from the drying chamber and the electrostatic precipitator accounted for 70% and 30% of the total, respectively. The two parts were combined into one, making 39,500 kg / h. The product, which was free-flying, containing 99.9% dry matter, was well suited for pneumatic conveying and further processing in a melting furnace according to the Outokumpu method, as described in U.S. Patent No. 2,506,557.

Example 6.

In a spray sealing device of the type shown in Fig. 1, the cylindrical part of the evaporation chamber had a height of 275 cm and a diameter of 640 cm. The flue gas pipe 16 had a diameter of 150 cm, the outlet pipe 18 was introduced immediately below the cylindrical part of the evaporation chamber and the distance between the upper part of the inlet of this pipe and the diffuser wheel of the centrifugal diffuser 11 was 150 cm.

40,000 kg / h of nitrophosphate fertilizer solution was introduced into the device, and flue gas from the bulb was used as the dry mist gas, which consumed 1400 k / h of fuel oil; the flue gas temperature was 1600 ° C. The effluent with a moisture content of 65% and a temperature of 20 ° C was introduced into the tank 19. From here it was pumped to the nozzles 22 and sprayed into the outlet pipes 18, where the gas temperature

Claims (7)

For 15,591,60 nozzles was 130 ° C. The gas phase sucked out of lines 24 from cyclones 23 formed 68,000 m 2 / h and had a temperature of 85 ° C. 20,000 kg / h of concentrated water at a temperature of 85 ° C was taken through the outlet pipe 28. The evaporation chamber 10 was made of stainless steel and did not allow overloading resulting from the high drying gas temperature and there was no tendency to separate solids from the inner wall of the evaporation chamber. The product was not exposed to any significant thermal damage during the compaction process, as demonstrated by painting the nitrogen filter. It is clear that within the scope of the invention various changes can be made to the embodiments shown in the drawings, such as it is possible to combine the device details shown in Figures 1-6 in different ways. For example, the types of evaporation chambers shown in Figures 2-6 - when used in connection with spray drying - can be supplemented so that the outside of the tube 16 is protected by a liquid film. Pat ent t ivat iroukse t A method for evaporating a liquid, which liquid is introduced mainly centrally from above into the evaporation chamber (10), into which warm flue gas or fuel gas is introduced, which from below is introduced mainly axially into the evaporation chamber and in a direction opposite to the liquid inlet (11), in a known manner is discharged into the evaporation chamber (10) in a disintegrated form, and that a substantial part of the gas phase is discharged from the evaporation chamber in a plane substantially below the level of the liquid inlet point (11). Method according to Claim 1, characterized in that a flue gas with a temperature of more than 300 ° C, in particular more than 600 ° C, is used. 16,591 60 Method according to Claim 1 or 2, characterized in that the gas phase is discharged from the evaporation chamber in a plane which is close to or below the plane in which the flue gases are introduced into the evaporation chamber. Method according to one of Claims 1 to 3, characterized in that the liquid, while being introduced in a dispersed form into the vapor chamber, is moved radially outwards towards the side walls of the chamber, preferably by means of a centrifugal diffuser (11). Apparatus for carrying out the method according to any one of claims 1 to 3, wherein the apparatus comprises an evaporation chamber (10) and a flue gas or flue gas inlet pipe (16) introduced from below and substantially centrally into the evaporation chamber and into a substantially axially directed flue gas stream. from above a lower liquid supply pipe (12), in addition to which one or more gas phase discharge pipes (18) lower into the evaporation chamber, characterized in that the end of the liquid supply pipe descending into the evaporation chamber is provided in a manner (18) the top of the inlet is a substantial distance below the liquid diffuser (11). fc. Device according to Claim 5, characterized in that the liquid diffuser is a centrifugal diffuser (11). Device according to Claim 5 or 6, characterized in that the flue gas supply pipe (16) is connected to supply elements (33, 34) for particulate matter, predominantly adjacent to a venturi constriction (35) in the flue gas supply pipe. r. ·· i7 591 60