Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/34—Chemical or biological purification of waste gases
  • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
  • B01D53/75—Multi-step processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2257/00—Components to be removed
  • B01D2257/20—Halogens or halogen compounds
  • B01D2257/204—Inorganic halogen compounds
  • B01D2257/2045—Hydrochloric acid
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2257/00—Components to be removed
  • B01D2257/20—Halogens or halogen compounds
  • B01D2257/204—Inorganic halogen compounds
  • B01D2257/2047—Hydrofluoric acid
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2257/00—Components to be removed
  • B01D2257/30—Sulfur compounds
  • B01D2257/302—Sulfur oxides
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2257/00—Components to be removed
  • B01D2257/40—Nitrogen compounds
  • B01D2257/404—Nitrogen oxides other than dinitrogen oxide

Definitions

• the invention relates to a device for removing gases such as S0 2 , N0 X HC 1 and / or HF from a raw gas or flue gas from an incinerator.
• a method for removing gases, such as from a raw gas, is already known from EP 0 294 658 A1.
• the method also has the following properties, particularly disadvantageous even in the extreme exhaust gas states mentioned.
• the flue gas with an evaporative cooler of e.g. B. cooled to 150 ° C to 70 ° C, a long residence time of the gas and thus a large cooling tower apparatus with a large space requirement, high weight and high costs is required to completely evaporate the injected water; at the outlet of the cooler, the non-evaporable flue gas constituents, in particular H 2 S0 4 droplets, which form from the S0 3 content of the flue gas, and the flying dust still remain despite the long dwell time.
• H 2 S0 4 droplets which form from the S0 3 content of the flue gas
• flying dust still remain despite the long dwell time.
• at lower temperatures in the cooler than 150 ° C there is also a constant formation of S0 3 -H 2 S0 4 droplets, especially on the dust particles still present
• ammonia NH 3 reactant is introduced into the connecting channel between the cooler and the reactor, the H 2 S0 4 droplets spontaneously form ammonium sulfate. If the temperature is between about 60 ° C and 80 ° C, ammonium sulfite is sometimes formed. Both compounds occur in solid as well as pasty and sticky form, which means that the channel clogs up in a short time and the exhaust gas cleaning process has to be interrupted to remove the deposits. In addition, the ammonium sulfite produced is thermally unstable and the cause of increased clean gas emissions if it is not oxidized to ammonium sulfate.
• the humidity of the flue gas entering the cooler is already high from the start (is the dew point temperature z. B. already 50 ° C)
• this is further increased by the evaporated cooling water in the cooler and by the evaporated water in the reactor, so that it is finally about 68 ° C in the filter downstream of the reactor.
• Such a high dew point temperature prevents the completely dry filter operation that is absolutely necessary to obtain a dry end product.
• the end product as it is removed from the dust collector, is not yet suitable for an intermediate silo storage, suitable for transport and for use as fertilizer.
• the product may also contain sulfitic as well as still moist and acidic components that can emit harmful vapors and that lead to caking of the product during storage and to corrosion on the inner walls of the bunker or silo. Sulphitic and acidic components are harmful to the plants.
• the object of the invention is to avoid the aforementioned disadvantages, which occur in particular in the purification of exhaust gases with a high moisture and SO 2 content, and to improve the overall efficiency of the device.
• the device has an evaporative cooler
• the evaporative cooler is operatively connected to at least one cooling device
• the outlet line for sump water is to the evaporation cooler and directly or via a flow divider above the sump water provided in the evaporation cooler 2.2. connected to a reaction chamber connected downstream in the flow direction of the raw gas,
• a further line for reaction gas is connected to the evaporation cooler in the evaporation cooler or sump water level, which connects the evaporation cooler directly or indirectly to the reaction chamber,
• the reaction chamber has at least one outlet line or outlet channel for a dust mixture.
• the combination of cooling air admixture to hot flue gas with a subsequent further cooling in an evaporative cooler has the following advantages for the aforementioned difficult flue gas conditions (high inlet moisture, high S0 2 content) and for an economically operable, dry cleaning process, which are shown using an example .
• the total volume flow of the reaction gas is not 1.3 times the amount of flue gas, but only 1.27 times.
• This Vorteyl comes into its own when the temperature of the fresh air before it is fed in is lower than 15 ° C in the colder season or when the fresh air is cooled below 15 ° C in the warmer season.
• the pre-absorbed, acidic gases and trapped droplets in the evaporation cooler than dilute acid can be neutralized together with the ammonia before being injected into the reaction chamber and no longer require radiation-chemical treatment. As a result, the energy consumption of the method can be reduced.
• the acidic cooling water flow for fine temperature regulation which is injected via the nozzle assembly in the middle part of the reaction chamber, can buffer residual ammonia portions which have not yet reacted in the middle and rear part of the reaction chamber.
• the water content of the solution injected via the nozzle assemblies also evaporates during the immediately starting exothermic reaction with the S0 of the reaction gas and thus serves as a coolant, and since the driving air at the nozzle outlet has a high relative speed between the reaction gas (slowly) and the ammonia water -Droplets (quickly) causes a high gas turbulence is advantageously generated for mixing in the direction of flow and transverse to the direction of flow.
• the compressed air portion of the two-component nozzles can be adjusted separately via the valve, a high penetration depth of the nozzle jet can be set in the longitudinal direction of the reaction chamber, so that the reaction zone is not only limited to the front, inlet-side part of the reaction chamber, but largely over the entire area Length of the reaction chamber can be spread. As a result, the ammonia is largely available for reaction in the entire reaction chamber volume. Since the sump cycle water in contact with the mixed gas assumes an equilibrium temperature between about 50 ° C and 60 ° C, it can be used directly as warm rinsing water to remove the reaction chamber deposits.
• the solubility of warm water is advantageously greater than that of cold water
• it is advantageous over the mechanically acting cleaning methods that uneven and angled, indented or bulged points of the reaction chamber can also be cleaned from the deposits with the nozzle sticks. Since the ammonia is only injected into the reaction chamber, there is also no need to clean the inlet channels for the reaction gas upstream and in the gas distributor.
• the collecting container for the interim collection of the washing solution has the advantage that not yet fully reacted, sulfite components, as are to be expected on the walls of the reaction chamber, are here oxidized with air and then injected back into the reaction chamber as a stable sulfate solution for drying can be. This sulfate portion no longer requires radiation and thus also reduces the energy consumption required for the process.
• the collecting container, together with the pH value measurement and control pHC advantageously brings about a process control, since the pH value of the wash solution emerging from the reaction chamber provides conclusions. over allowed whether the reaction proceeds with excess or deficit of ammonia.
• the dew point temperature at the outlet of the reaction chamber is around 60 ° C to 62 ° C and the electrostatic precipitator is operated at 85 ° C to 90 ° C, a dew point distance of 25 ° C can be ensured in the filter, which is necessary for dry operation is.
• the end product as it comes from the filter, is not yet suitable for direct storage, packaging, transport and use as a fertilizer. It may still be too damp for this and it may still contain too much acid. To this end, it is advantageous to convey the product into a heated mixer while it is still warm and, if necessary, to carry out drying and neutralization with heated, concentrated or gaseous ammonia diluted with air. Still acidic and sulfitic fractions in the end product, which are responsible for Plant are harmful, can be neutralized and z. T.
• the no longer oxidized sulfites are volatilized again at a temperature higher than about 60 ° C to 70 ° C and can be fed back as reaction precursors with the exhaust air stream to the reaction chamber become.
• Ammonium sulfate in its pure form reacts acidically with water and is therefore only suitable for soils with sufficient buffering action (calcareous or basic soils).
• the ash remaining in the coal combustion process in particular the ash, slag and fly ash which originates from lignite combustion, can be used to neutralize the ammonium sulfate by adding up to the product is mixed to the neutral pH value in the mixer or in the bunker.
• This mixing of the end product with the ash present on site has the additional advantage that the ash moisture residues, the z. T. still present, can take up (z. B.
• FIG. 1 shows a schematic illustration of a device for removing gases such as SC> 2, N0 ⁇ , HCl and / or HF from a raw gas or flue gas,
• Figure 2 shows a gas divider with numerous outlet channels for feeding a reaction chamber with a flue gas mixture and a nozzle assembly, parts of the invention, as shown in Fig. 1, have been omitted for better understanding.
• 1 denotes an input line for raw gas, which can consist essentially of CO2, S0 2 , N0 ⁇ , HCl, HF and air.
• the raw gas or flue gas 1 ' is passed via the line.
• the raw gas 1 ' passes from a boiler (not shown in the drawing) via the inlet line 1 and an adjustable flap 3 into an evaporator cooler 8.
• the raw gas 1' is mixed with fresh air 2 'in a proportion between 5 and 50 vol %, preferably between 20 and 40 vol% of the raw gas, based on the normal state, mixed.
• the fresh air 2 ' is fed into the line 1 via a fresh air line 2 and a throttle valve 3'. performed so that the mixture can then be introduced together into the interior of the evaporator cooler 8.
• the fresh air 2 ' which has a sufficiently low temperature in the winter and transition months, can advantageously also be cooled in the summer months when the outside temperature is approximately 15 ° C. by injecting cold water 4'.
• the air-flue gas mixture 1 ', 2' is then brought into contact with water and / or with an aqueous solution of the sump water 5 'in the evaporative cooler 8.
• the cooling water introduced via a line 4 is added to the evaporative cooler 8 in a somewhat larger amount, which is necessary in order to cool the air / flue gas mixture or the mixed gas 1 ', 2' by water evaporation so that the resulting reaction gas 10 'has the desired temperature between 50 ° C and 100 ° C or between 60 ° C and 90 ° C.
• the line 15 extends into the interior de ⁇ evaporator cooler 8 and has at the outlet end a nozzle 82 through which the sump water 5 'is again added to the reaction gas 10' or the gas mixture 1 ', 2', so that a further reaction of the sump water 5 'with the mixed gas 1', 2 'occurs.
• the valve 55 can be controlled via a temperature-dependent actuator TC1, so that more or less sump water 5 'is supplied to the evaporator cooler 8 as a function of the temperature.
• the evaporative cooler 8 can consist of a corrosion-resistant, glass-fiber reinforced plastic.
• the inner walls can also be continuously wetted with a base load liquid flow 141 without substantial temperature control and thus cooled.
• the base load liquid flow flows via a line 142, which is connected at one end to the line 5 for sump water and at the other end via a controllable valve 57 to the upper end of the evaporator cooler 8 or a nozzle assembly 58 having a plurality of nozzles.
• the liquid flow 141 can be directed to the side walls or inner walls of the evaporator cooler 8, and these can be cooled.
• the valve 57 cannot be regulated via a temperature element, although this is also possible. It is sufficient, however, if only the valve 55 and thus the inflow to the nozzle assembly 82 is controlled via the temperature element TCl, so that the medium passed through the valve 55 is injected in such a way that the desired target temperature is between 50.degree. C. and 100.degree the reaction gas 10 'sets.
• the system is designed as a DC system. However, it is also possible to operate the mass transfer by means of a counterflow system, so that the mixed gas 1 ', 2' flows in in the lower part and the cooled mixed gas can be removed in the upper part of the evaporator cooler 8.
• reaction gas 10 'and the entrained liquid droplets from the evaporator cooler 8 are fed to a gas distributor 11 consisting of a container, which for this purpose is connected via a further line 10 to the lower region of the evaporator cooler 8 above the sump water level.
• the gas distributor 11 is shown in perspective in FIG. 2, the individual outlines of the gas distributor 11 and an adjoining reaction chamber 13 being shown in solid lines, although, since they are invisible, they would have to be dashed in individual cases.
• the gas distributor 11 consists of an elongated container and has numerous outlet channels 12 arranged side by side, which can be opened or closed via valves or flaps.
• the gas distributor 11 is designed as a tubular housing to which the channels 12 connect and expand in a trapezoidal shape.
• the individual channels 12 consist of housing arrangements which are rectangular in cross section, the Inlet openings 43 of the channels 12 extend over the entire width of the reaction chamber 13.
• the inflow of the gas mixture via the channels 12 to the reaction chamber can also be controlled, wherein the inlet openings 43 can be connected to adjustable throttle valves.
• the gas distributor 11 has a sump line 7, so that part of the liquid droplets or water droplets entrained from the evaporator cooler 8 collects in the sump of the gas distributor and then via the circulation pump 9 provided in line 5 is returned to the bottom circuit, d. H. the sump water from the gas distributor 11 reaches line 5 via line 7 and is mixed there with the sump water 5 '. The sump water 5 ′ reaches the interior of the evaporator cooler 8 via the line 5, 15 either via the nozzle assembly 18 or the nozzle 82.
• the sump 6 of the evaporator cooler 8 is connected to the sump of the gas distributor 11, so that the sump 6 of the evaporator cooler 8 can have approximately the same fill level as the sump in the gas distributor 11.
• the sump fill level in the sump of the gas distributor 11 is over a liquid control element LC1 is measured and the cooling water flow 4 'is regulated via the valve 64 in the line 4 so that the fill levels can be kept the same or constant.
• acidic sump water From the outlet line 5 of the sump of the evaporator cooler 8, acidic sump water, to which acidic gases such as S0 3 , HCL and HF are admixed, passes via lines 15 and 151 for cooling in the reaction chamber.
• mer 13 via nozzle assemblies 18 and 19 which are arranged in the reaction chamber.
• the sump water is injected via the nozzle sticks 18 and 19 and the associated nozzles 50, which are arranged on the nozzle sticks.
• the individual nozzles can be designed as single-substance or also as multi-substance nozzles.
• a valve 56 is arranged in line 15, which regulates the cooling water flow as a function of a control element FC1 for cooling liquid and a further measuring point FI for ammonia.
• the control element FC1 is operatively connected via a measuring line or transmitter line 66 to a line 16 for the flow of NH 2 and H 2 O (ammonia spirit).
• the line 16 is connected to the reaction chamber and the nozzle assembly 18 via a valve 67.
• the flow in line 15 is set to approximately one third to two thirds of the cooling water requirement, while a valve 59 regulates the flow of cooling water in line 151 as a function of the desired filter temperature TC2.
• the gas distributor 11 connected to the evaporation cooler 8 via the line 10 is operatively connected to the reaction chamber 13 via numerous outlet channels 12.
• the individual outlet channels 12 can expand trapezoidally in the direction of the reaction chamber and correspond with their outlet end approximately to the total width of the reaction chamber 13.
• the inlet openings 43 of the outlet channels 12 can be completely or partially closed or opened via flap valves as required.
• the nozzle assembly 18 can be charged with ammonia NH - ⁇ - H- j O via the line 16 and the valve 67.
• the ammonia can be injected with the one- or two-substance nozzles 50 as an aqueous solution or in a liquid or gaseous state.
• the injection of commercially available 10 to 35% ammonia solution 16 '(NH 3 ⁇ H 2 0) is advantageous, so that this mixture reaches the interior of the reaction chamber 13 via the two-component nozzles 50 of the nozzle assembly 18.
• the jet width of the droplet-air jet from the two-substance nozzles 50 is approximately 0.3 to 1 times the length L of the reaction chamber when viewed in the direction of flow. It can advantageously be 0.5 to 0.8 times.
• the amount of compressed air 17 'required for this purpose, which reaches the reaction chamber via a line 17, is controlled via valves 68 and 69, which are operatively connected to the nozzle assembly 18 and the nozzle assembly 19 via the lines 17. Pure oxygen 0 2 or air enriched with oxygen can also be used as compressed air.
• the electron emitters or electron beam accelerators 20 are provided partly inside or outside of the reaction chamber 13.
• the supply line 17, which is divided into two line segments, is connected to the two nozzle blocks 18 and 19, the flow rate of this line being controlled by the valves 68 and 69.
• Compressed air, pure oxygen 0 2 or also mixtures thereof can be supplied via the lines 17 to the nozzle assemblies 18 and 19, as a result of which the oxidation within the reaction chamber 13 is improved.
• the electron guns 20 can be provided on the one hand inside or outside the reaction chamber 13.
• the electron emitters 20 arranged within the reaction chamber likewise extend over the entire width of the reaction chamber 13 or have approximately the same width as the nozzle assembly 18. It can For example, a plurality of electron emitters 20 can be evenly distributed over the entire reaction chamber at a parallel distance. It is also possible that the electron emitters 20, according to FIG.
• the electron emitters 20 shown in FIG. 2 can also be arranged on the outside of the sides 51 and 52 with a parallel spacing from one another and thus cover the entire surface of the side walls 51 and 52. It is also possible that one or more electron emitters 20 are provided on an upper side 70 of the reaction chamber 13.
• the flow rate in the line 16 can be controlled via the valve 67 and measured via the measuring point FI, which is operatively connected to the line 16 via the transmitter line 66.
• control circuit FC1 processes the setpoint specification via a computing algorithm such that a certain amount of sump water is supplied to the nozzle assembly 18 via lines 5 and 15 in proportion to the flow rate of the ammonia 16 'in an order of magnitude of 100% of the flow rate 16'. This gives a 50% diluted ammonia solution, so that there is now an inflow of 12.5% ammonia (NH to the nozzle assembly 18).
• the pre-absorbed, acidic flue gas components SO ⁇ and O ⁇ , hydrogen halide and dust, which form the total of the sump water 5 ', are taken up in the sump water 5' of the sump 6 and mixed with the ammonia solution 16 'from the line 16. If the sump water 5 ', as mentioned, is mixed with the ammonia solution 16', these absorbed flue gas components S0 3 and NO ⁇ are already neutralized in the liquid to the corresponding ammonia salts and also injected via the nozzle assembly 18, evaporated and dried in the gas stream within the reaction chamber 13 .
• a temperature deviation of approximately +/- 10 ° C. can occur between the inlet opening 43 and the outlet opening 62 if the sump water 5 'is injected via the line 16 and the nozzle assembly 18.
• the line 15 is, as already mentioned, connected to the line 16 via the valve 56, which can be controlled or regulated via the liquid control part FC1.
• the cooling water 4 ' can be fed to the evaporative cooler 8 via the cooling water line 4, so that part of the absorbed acid is absorbed from the flue gas via the cooling water. Then the cooling water is fed back into the sump water circuit and, as already mentioned, is fed via line 5 to the nozzle assembly 18 in the reaction chamber 13 to dilute the metered ammonia solution via line 15.
• the actuators TC1, TC2
• a fine temperature control by means of the control valves 55, 59 and thus the inflow to the reaction chamber 13 and / or to the evaporative cooler 8 can be regulated or controlled.
• the nozzle sticks 22 mainly extend on the underside and on the side walls 51, 53 and on the upper side 70 of the reaction chamber 13.
• a partial stream of the sump water 5 ′ flows via the line 5, the pump 9 and a line 24 to the nozzle sticks 22
• the relatively strongly concentrated washing solution 21 flows off from the inclined or perpendicular side walls 51 and 54 and passes via the inclined side wall 51 to a sump 47 provided in the reaction chamber 13 and via a line 21 to a collecting container 39 which holds the solution or absorbs the ammonia salt.
• the container 39 is connected to a control circuit LC2, which includes a level measurement, a feed pump 91 and the valve 66 that can be controlled via a control line 48.
• a control circuit LC2 which includes a level measurement, a feed pump 91 and the valve 66 that can be controlled via a control line 48.
• An approximately constant fill level can thus be maintained in the container 39. If there are still sulfitic salts in the washing solution 21 ', these are largely oxidized during the dwell time of the solution in the collecting container 39 by a fine-bubbled air injection via the line 17 and the control valve 67, so that (NH 4 ) 2 SO 4 can form.
• the exhaust air from the container 39 reaches the reaction chamber 13 via a vent line 38.
• Optimal oxidation can be achieved via the pH transmitter pHC, for which purpose the pH value is recorded and an acidic solution 5 'is metered into the container 39 via a control valve 65 and an ammoniacal solution 16' via line 16.
• the exact dosing takes place via valves 64 and 65 in lines 5, 16 and 61 in connection with a level control LC2. In this way it is ensured that additional cooling water 4 'is only added to the container 39 via the line 4 and the valve 66 and a line 75 if necessary.
• a further nozzle assembly 40 is provided behind the emitters 20 in the upper region of the reaction chamber 13 and is used for metering in liquid H 2 O 2 or gaseous O3 (ozone), which is supplied via line 31, a valve 71 and the nozzle assembly 40 reaches the reaction chamber 13.
• the input of the oxidizing agent takes place, as seen in the flow direction of the gas, approximately in the second half of the reaction chamber 13.
• the production filter 27 is indicated schematically in FIG. 1 and consists of a container 63 with the associated filter 27, which is connected to an outlet opening 62 of the reaction chamber 13 via a conveying device 26.
• the inner walls or at least some of the inner walls in the exit area of the reaction chamber 13 and the exit channel 62 are heated electrically or by means of hot water from the outside. Furthermore, heating or evaporation of residual water components in the gas and / or on the inner walls is also possible if, for this purpose, microwave generators are effectively connected to the reaction chamber 13 and / or the channel 62.
• the gas loaded with ammonium sulfate aerosols and with dust particles is fed via a conveyor device 26 having one or more screw conveyors 25, which is integrated in the outlet channel 62, to the product filter 27, which in the Container 63 is provided.
• hollow screws 25 which are circular in cross section and are arranged in the axial direction are located, the axes of which are operatively connected to a rotary drive or a motor 30 at the respective channel end connector.
• the direction of rotation is selected so that the screw runs in the direction of flow.
• the outer screw conveyor of the screw conveyor 25 is designed to be slightly resilient, but nevertheless so stable that the screw conveyor can be connected to the axis by means of spaced webs.
• the screw belt width is approximately 0.01 to 0.04 times, advantageously 0.02 to 0.2 times the channel diameter of the conveyor device 26.
• tooth elements or a tooth belt can be provided on the outer circumference of the screw belt e.g. B. consists of a harder material than the screw conveyor. Due to the high loading of the gas with foreign substances, deposits form particularly on the inside walls of the conveying device, particularly when there are not yet evaporated droplets in the gas.
• the latter sweeps along the inner wall of the screw channel and in the process continuously scrapes new deposits from the inner wall of the conveyor channel.
• the dust-like removals are carried by the flow of the gas in the direction of the production filter 27, with larger removed particles also being fed to the production filter 27 via the conveyor device 26, so that they can then be collected in a dust collection bunker 72. It is particularly advantageous if the sewer pipes 62 of the conveying device 26 extend somewhat inclined and have an angle between the vertical and the longitudinal axis of the screw of 20 °.
• the filter material received in the collecting bunker is fed via a line 37 and via a heatable mixer 32 to a pelletizing device 33. This will completely dry the filtered product. Any acid residues still present can be neutralized by entering ammonia 73 via a line 34. To fully absorb the moisture, the concentrated or diluted ammonia from line 34 should be approximately the temperature of the filtered product.
• the temperature of the filtered product 37 ' is in the mixer 32 between 40 ° C and 100 ° C, especially in a temperature range between 60 ° C and 90 ° C.
• the average residence time of the end product 37 'in the mixer 32 should be between 0.5 and 20 hours, in particular between one and eight hours.
• the exhaust air from the mixer is returned to the front part of the reaction chamber 13 via a line 41 or added to the reaction chamber 13 via the vent line 38. If ammonia is required (NH-g), this can be added to the heated air via line 34.
• the mixer 32 can also be provided on the lower part of the filter 27, which for this purpose tapers conically downwards and forms a collecting bunker 72.
• One or more of the converging inner walls of the bunker 72 can be acted upon by screw conveyors, so that the mix adhering to the inner walls is directed in the direction of a discharge trough 74.
• the product discharged via the filter 27 consists mainly of ammonium sulfate and can therefore be used as a fertilizer.
• Ammonium sulfate reacts very easily in water, especially in the acidic pH range, which is disadvantageous for soils. For this reason, it is advantageous to add fly ash to the filtered product 37 'via a line 35. Only as much fly ash 35 'can be added to the mixer 32 or the collecting bunker 72 until the aqueous slurry of the mixture is approximately in the neutral pH range.
• the fly ash contains valuable trace elements such as Ca, K, Mg, Fe, Mn, Cu, Zn, P and other substances that are important for plant growth, and the fly ash from lignite combustion has a very low proportion of harmful substances, such as Example Pb, As, Cd, Hg and other substances, brown coal fly ash and ground slag can be mixed with a weight fraction of 0.1% to 20%, in particular between 1% and 10%. As a result, the neutral pH range of the mixed product 72 'may not yet be fully reached. In any case, however, the acidic character of the fertilizer thus obtained is significantly reduced or completely eliminated.
• the material to be conveyed 37 'and the neutralized, mixed product 42' enriched with ash is fed to the pelletizing device 33, so that a product which can be stored or poured or scattered is obtained, with a grain size of between 1 mm and 6 mm or 2 mm and 4 mm.
• the granulation takes place in particular without further moistening in a granulation press with a downstream pellet cooler, which is however not shown in the drawing.
• the inner lining of the reaction chamber 13 is advantageously lined with radiation and corrosion-resistant, ceramic or basaltic tiles or molded parts.
• the pipes inside the reaction chamber 13 and the nozzle assemblies 18, 19, 22, 40 can preferably also consist of radiation and corrosion-resistant graphite, the nozzles themselves of radiation and corrosion-resistant ceramic.
• the inner walls of the collection bunker 72 also serve to mix the material, similarly to the mixer device 32.
• nozzle assembly for single-substance nozzles Outlet line of the container 39 'washing solution line screw conveyor conveyor device filter exhaust gas line for residual gases exhaust line' clean gas engine line mixer pelletizer line line 'fly ash line' product, end product ventilation line container for receiving ammonia salt nozzle line supply line line • product inlet opening nozzles for 18 sump flow divider flow divider outlet nozzle, multi-substance nozzle Side wall, inner wall, underside side wall, inner wall side wall, inner wall side wall, inner wall Control valve for sump water Control valve control valve nozzle block Control valve control valve for washing solution 23 * second inlet line outlet opening, outlet channel tank valve valve valve, sender line valve, control valve valve valve upper side valve Liquid flow supply line for cooling water from evaporative cooler

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• 1996
  • 1996-09-27 DE DE1996139808 patent/DE19639808C1/de not_active Expired - Fee Related
• 1997
  • 1997-09-19 AU AU47046/97A patent/AU4704697A/en not_active Abandoned
  • 1997-09-19 WO PCT/EP1997/005148 patent/WO1998013127A1/de active Application Filing
  • 1997-09-19 CN CN 97180099 patent/CN1238710A/zh active Pending
• 1999
  • 1999-03-26 BG BG103290A patent/BG103290A/xx unknown

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