WO2003000387A1 - So3 separating and removing equipment for flue gas - Google Patents
So3 separating and removing equipment for flue gas Download PDFInfo
- Publication number
- WO2003000387A1 WO2003000387A1 PCT/JP2002/006185 JP0206185W WO03000387A1 WO 2003000387 A1 WO2003000387 A1 WO 2003000387A1 JP 0206185 W JP0206185 W JP 0206185W WO 03000387 A1 WO03000387 A1 WO 03000387A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- flue gas
- water
- sodium carbonate
- wet desulfurization
- flue
- Prior art date
Links
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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
-
- 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
Definitions
- the present invention relates to S 0 3 minutes remover flue gas, in particular to so 3 minutes removing device for removing sulfur trioxide (SO 3) content in the flue gas from the furnace using a fuel containing sulfur.
- SO 2 in the flue gas is further oxidized and converted to sulfur trioxide (S ⁇ 3 ) in the boiler and denitration equipment.
- SO 3 passes through an air preheater, etc., and the flue gas temperature decreases.For example, when it falls below 300 ° C, it reacts with the moisture in the flue gas to form SO 3 + H 20 ⁇ H generating a 2 S 0 4 I Ri H 2 S_ ⁇ 4 gas into the reaction of.
- the H 2 S 0 4 gas of flue gas temperature to produce a fine sulfate mist becomes below the dew point of sulfuric acid.
- wet EP forms a water film on the electrode by spraying water or an alkaline solution onto the collecting electrode of the electrostatic precipitator, and cleans and removes the collected sulfuric acid mist from the electrode. It is like that.
- a device has been devised to prevent the generation of sulfuric acid mist by adding a neutralizing agent for SO 3 to flue gas without using wet EP.
- a neutralizing agent for SO 3 for SO 3 to flue gas without using wet EP.
- this type of apparatus for example, there is an apparatus described in JP-A-2000-317720.
- the apparatus of this publication Ri by the fact that the flue gas with relatively flue gas temperature is high the location of the desulfurization apparatus upstream in the S 0 3 neutralizer introducing alkaline powders, such as carbonate calcium ⁇ beam The SO 3 in the flue gas is removed.
- Purpose of the present invention has been made in view of the above problems, without causing an increase in plant construction co be sampled by the installation of wet EP, provides SO 3 minutes remover inhibitory available-flue gas to increase in plant operation costs And
- a flue gas passage which guides flue gas from a furnace for combusting a fuel containing sulfur to a chimney, and which is disposed on the flue gas passage.
- a sodium carbonate supply device for supplying 2 C 0 3 ), an upstream side of the wet desulfurization device, and a downstream side of a flue gas passage portion to which the sodium carbonate is supplied, for cooling the flue gas.
- 30 3 component in the flue gas is condensed in liquid form 1 ⁇ 2 30 4, and SO 3 separation device for separating and removing from the flue gas, the flue gas S 0 3 minutes removing device equipped with is provided Te.
- the supply amount of sodium carbonate is reduced to such an extent that only a part of SO 3 in the flue gas can be removed, instead of removing the entire amount of SO 3 in the flue gas.
- the remaining SO 3 that could not be removed by the supply of sodium carbonate is removed from the flue gas by installing a separate SO 3 separation device.
- SO 3 separation equipment of the present invention Ru der those separating and removing S_ ⁇ 3 component from the flue to cool the flue gas.
- the S 0 3 of I in sea urchin flue gas described above to generate the H 2 SO 4 reacts with moisture in the flue gas when the temperature drops below a certain degree (for example 3 0 0 ° about C).
- a certain degree for example 3 0 0 ° about C.
- SO 3 in the flue gas is condensed into liquid H 2 SO 4 and separated from the flue gas. This makes it possible to remove SO 3 in the flue gas in the form of H 2 SO 4 liquid in the SO 3 separation device, and the SO 3 minutes in the flue gas at the inlet of the wet desulfurization device will decrease. .
- the SO 3 separation device of the present invention removes SO 3 from flue gas by cooling flue gas, it also functions as a heat recovery device from flue gas. Therefore, the heat recovered by the SO 3 separation device is reused (for example, (For example, heating the boiler feed water) can further reduce the plant operating costs.
- the sodium carbonate supply device supplies sodium hydrogen carbonate (NaHCO 3 ) powder into the flue gas and forms sodium carbonate fine particles in the flue gas. You may do it. Bicarbonate isocyanatomethyl Li ⁇ beam powder supplied to the flue gas are shorted with a flue gas heat, 2 N a HCO 3 ⁇ N a 2 CO 3 + C 0 2 + H 2 0 results in decomposition of carbonate diisocyanato Lithium (Na 2 CO 3 ) is produced in the flue gas.
- the Na 2 CO 3 particles have a porous structure with a high porosity and a large specific surface area because the portion from which CO or H 2 O has been removed becomes voids. Therefore, the resulting N a 2 C 0 3 particles S 0 3 minutes is to be converted to N a 2 SO 4 and SO 3 minutes and efficiently react in the flue gas.
- a heat exchanger for lowering the flue gas temperature using cooling water may be used for the SO 3 separation device.
- Ri by the lowering the flue gas temperature using a heat exchanger, condensation of H 2 SO 4 takes place in the heat transfer surface in contact with the flue gas, liquid H 2 SO 4 The generated to adhere to the heat transfer surface become .
- Liquid H 2 SO 4 adhering to the heat transfer surface can be easily removed by cleaning the heat transfer surface during operation using cleaning water.
- Ni will this Yo, by lowering the flue gas temperature using a heat exchanger, it is possible that the S 0 3 minutes to remove in the form of aqueous H 2 SO 4 in the flue gas easily and inexpensively in the present invention Becomes
- the absorbent circulation system of the wet desulfurization system It is preferable to be supplied and used as makeup water.
- SO 2 in the flue gas is absorbed into the flue gas by atomizing the aqueous solution of the So 2 absorbent into the flue gas.In this process, the flue gas is saturated with water vapor. A considerable amount of water is absorbed together with the smoke
- the circulation system needs to be constantly replenished with water as it is removed from the tower.
- the heat exchanger used in the S 0 3 separating apparatus Le a simple structure. Ann De. Tube type heat exchanger and the child is preferred.
- the inner surface of the casing and the outer surface of the tube as a heat transfer surface which come into contact with the flue gas are made of, for example, a corrosion-resistant material having chemical resistance such as stainless steel, or for example, PTFE (polytetrafluoroethylene).
- a corrosion-resistant material having chemical resistance such as stainless steel, or for example, PTFE (polytetrafluoroethylene).
- PTFE polytetrafluoroethylene
- the wet desulfurization unit is provided with a cooling tower for spraying water into the flue gas to lower the temperature of the flue gas flowing into the absorption tower, and the So 3 separation device is disposed at the top of the cooling tower.
- the washing device supplies the wastewater after washing the heat transfer surface into the cooling tower and, together with the water sprayed into the cooling tower, turns it into makeup water for the absorbent circulator in the absorption tower. It is also possible to supply by supplying.
- the flue gas flows into the tower from the flue gas inlet at the top of the cooling tower, and the temperature decreases due to the evaporation of water sprayed into the flue gas while flowing downward in the tower.
- a considerable amount of the sprayed water evaporates and is removed from the cooling tower together with the flue gas, so it is necessary to replenish the cooling tower with water only for the amount of evaporation. Therefore, the flue gas inlet of the cooling tower upper Ri by the the provision of the S o 3 separation equipment, flue gas temperature flowing into the cooling tower is reduced, the cooling The amount of water evaporating in the tower is reduced.
- the so 3 separation device since the so 3 separation device is located above the cooling tower, the water after washing the heat transfer surface falls into the cooling tower due to gravity and absorbs the so 2 of the absorption tower from the bottom of the cooling tower together with the sprayed water. It is supplied to the agent circulation device. Therefore, there is no need to separately provide a transfer pump or the like for supplying the washing water to the absorbent circulation device.
- boiler feedwater as cooling water for the heat exchanger, and to recover the heat of flue gas into the boiler feedwater.
- a gas / gas heater for exchanging heat between the flue gas supplied to the chimney and the flue gas discharged from the furnace is arranged in the flue gas passage on the upstream side of the SO 3 separation device. It is possible to supply the Na 2 CO 3 to the flue gas passage downstream of the air preheater. By exchanging heat between the flue gas at the outlet of the wet desulfurization unit and the flue gas discharged from the furnace using a gas heater, the temperature of the flue gas discharged from the chimney is raised and the generation of white smoke is prevented. can do.
- N a HCO 3 powder discharge The supply of Na 2 CO 3 with a porous structure becomes better when supplied to a portion where the smoke temperature is higher. Further, N a 2 C 0 3 is to react with SO 3 and H 2 S 0 4 gaseous in the flue gas, N a 2 C 0 of the third supply as much as possible flue gas temperature is high mist form H 2 preferred for better to supply the part S 0 4 is small to remove the 3 minutes SO.
- the existing wet desulfurization device is used as described above. Ri due to be made of the S 0 3 minutes removal device, it is possible to produce a very low cost sO 3 minutes removal device.
- the devices arranged on the flue gas passage between the above-mentioned sodium carbonate supply device and the wet type desulfurization device should be constituted only by devices which do not have a movable member at the contact portion with the flue gas. Is preferred.
- N a HS 0 4 (acidic sulfate reacts with S 0 3 min in yet some N a HS 0 3 produced evacuated by reacting Generates sodium).
- the N a HSO 4 is extremely hygroscopic is high when there is a device having a variable dynamic member, such as a blower one or damper attached to the movable portion. In some cases arise problems such as sticking. For this reason, in the flue gas passage between the sodium carbonate supply device and the desulfurization device, devices such as blowers and dampers that have movable members in contact with the flue gas should not be placed and fixed. It is preferable to prevent such problems as occurring.
- sodium carbonate supply device between the sodium carbonate supply device and the wet desulfurization device, there is provided a sodium carbonate removal device for removing the SO 3 component in the flue gas and the sodium carbonate after the reaction.
- sodium carbonate supply device It is also possible to configure the device disposed on the smoke exhaust passage between the device and the sodium carbonate removing device only as an appliance having no movable member at the contact portion with the smoke exhaust.
- the smoke exhaust gas after passing through the removal device has a high hygroscopic N because a HS 0 4 has been removed, problems such as sticking of the movable member of the device on the flue gas passage is prevented.
- the smoke exhaust passage between the sodium carbonate supply device and the sodium carbonate removal device is provided with movable members such as a propeller damper to prevent problems such as sticking.
- FIG. 1 (A) is a diagram schematically showing the overall configuration of an embodiment of the SO 3 removal device of the present invention
- FIG. 1 (B) is a diagram showing the SO 3 concentration in the flue gas at each part in FIG. 1 (A).
- the ⁇ to bright figures, FIG, 3 to 2 FIG. 1 (a), illustrating the configuration of an embodiment of the SO 3 separation device used in the S 0 3 minutes dividing removed by device (B) is S 0 3 separate shows an arrangement of the apparatus
- FIG. 4 is an exemplary diagram
- Figure 5 carbon isocyanatomethyl Li um supply apparatus for use in S 0 3 minutes remover of Figure 1 showing another example of the placement of the S 0 3 separation device
- Fig. 6 (A) is a diagram illustrating the configuration of the configuration, Fig.
- FIG. 6 (A) is a diagram showing the device configuration when flue gas treatment is performed using only a wet desulfurization device
- Fig. 6 (B) is the flue gas in each part of Fig. 6 (A).
- diagram for explaining the SO 3 concentration in each part of FIG. 7 (a) shows the device configuration of the Hare rows flue gas treatment using only wet desulfurization apparatus
- FIG. 7 (B) FIG. 7 (a) it is a diagram illustrating the S 0 3 concentration in the flue gas that put on.
- FIG. 6 (A) is a diagram illustrating a schematic configuration of an apparatus in the case of performing flue gas treatment using only a wet desulfurization apparatus.
- 1 is the furnace such as a boiler, 3 flue through which combustion flue boiler 1, 7 is a desulfurization apparatus for removing S 0 2 in the flue gas.
- a desulfurization apparatus 7 general known type wet desulfurization apparatus (eg, calcium hydroxide, in aqueous solution and the form of C a SO 4 by contacting the flue gas of SO 2 absorbent such as calcium carbonate also the removal of S 0 2 present in the flue gas, or by using magnesium hydroxide and hydroxide isocyanatomethyl re um, which removes the SO 2 in the flue gas in the form of M g SO 4 or N a 2 SO 4 ) Is used.
- the flue gas from which SO 2 has been removed by the desulfurization unit 7 passes through the flue 9 on the downstream side, and is discharged to the atmosphere from the chimney 11.
- the combustion gas (smoke exhaust) generated by the combustion of heavy oil in the boiler 1 passes through an air preheater (air heater) 5 provided in the flue 3 and exchanges heat with the combustion air supplied to the boiler 1. Then, it is sucked by a desulfurization fan (not shown), flows through the flue 3, and is supplied to the desulfurization unit 7.
- the flue gas supplied to the wet desulfurization device 7 contains not only SO 2 but also sulfuric acid gas and mist. Since the flue gas temperature drops below the sulfuric acid dew point when passing through the wet desulfurization unit, all sulfuric acid gas in the flue gas is discharged. Sulfuric acid mist will result. Although S 0 2 In wet desulfurization apparatus 7 is removed with high efficiency, since the removal rate of sulfuric acid mists of wet desulfurization system is low, typically, sulfuric acid mist concentration in the flue gas in a wet desulfurization apparatus 7 outlet comparative It is a very high value.
- FIG. 6 (B) shows the S 0 2 concentration and SO 3 concentration in flue gas temperature and flue gas at the location indicated by III from I in FIG. 6 (A). Note that represents the total concentration of S_ ⁇ 3 gas and mist-like H 2 SO 4 in the flue gas in FIG. 6 (B) as the SO 3 concentration.
- a sodium carbonate supply device 20 a particle size of 20 microns When injecting sodium bicarbonate powder of less than
- Relatively low flue temperatures e.g. 6 0 ° or approximately C
- Ji raw gaseous C 0 2 and between H 2 O and is released carbonate isocyanatomethyl Li um (N a 2 co 3) is generated. Since the portion of the generated sodium carbonate from which the gas has been released remains as voids, the particle size hardly changes from that of the sodium hydrogencarbonate powder, but the porous particles have large porosity.
- N a 2 S 0 4 This is, N a 2 CO 3 and the particles, and therefore maintained substantially the same diameter, is readily collected by N a 2 C 0 3 particles as well as the desulfurization apparatus 7 unreacted It is. Further, since Na 2 C 0 3 and Na 2 SO 4 are both water-soluble, they can be easily discharged out of the system without generating scale in a desulfurization device. At the same time a small amount as a byproduct N a HSO 4 is also water soluble FIG. 7 (A) system in the case of adding the carbonate Na Application Benefits um supply apparatus shown by reference numeral 2 0 in the apparatus shown in FIG. 6 (A) configuration, FIG.
- FIG. 7 (B) the flue gas temperature at the location of the III from I in FIG. 7 (a), shows the S 0 2 concentration and SO 3 concentration.
- Fig. 7 (A) by supplying sodium bicarbonate powder from the sodium carbonate supply device 20 into the exhaust gas downstream of the air preheater 5, the porous Na and generation of 2 CO 3 particles, and the S 0 3-minute removal in the flue gas becomes favorable by N a 2 C 0 3.
- the configuration of the sodium carbonate supply device 20 will be described later.
- the removal efficiency of SO 3 in the wet desulfurization unit 7 is equivalent to that in Fig. 6, the SO 3 concentration (in this case, the sulfuric acid mist concentration) at the inlet of the wet desulfurization unit 7 (point II 'in Fig. 7) Need to be reduced to about 2.5 ppm.
- the amount of N a HC 0 3 to be supplied for this purpose generates a 1.5 from about 5 equivalents N a 2 CO 3 with respect to SO 3 content in the flue 3 You need as much as you need.
- the present invention avoids reducing the SO 3 concentration in the flue gas to the required concentration with only NaHCO 3 supplied from the sodium carbonate supply device 20 and uses the SO 3 separation device described below. by removing a substantial portion of the S 0 3 present in the flue gas upstream of the wet desulfurization apparatus 7, thereby reducing the bran preparative operation costs by reducing the consumption of N a HCO 3.
- FIG. 1 is a view similar to FIGS. 6 and 7 showing the configuration of an embodiment of the present invention, and the same reference numerals as those in FIGS. 6 and 7 indicate the same elements.
- SO 3 is added to the flue between the air preheater 5 and the wet desulfurization device 7.
- the point that the separating device 10 is provided is different from the case of FIG.
- the SO 3 separation device 10 should be cooled using a heat exchanger until the flue gas temperature becomes lower than the dew point temperature of the H 2 SO 4 gas. Ri by the one in which to condense S 0 3 present in the flue gas in the form of liquid like H 2 SO 4.
- Fig. 1 (B) shows the flue gas temperature, SO 2 concentration and SO 3 concentration at each location shown in Fig. 1 (A).
- the temperature of the flue gas and the SO 2 concentration at the inlet (point II,) of the SO 3 separation device 10 are the same as those in FIG. 6 and FIG. 0 3 concentration as about 4 ppm, and summer considerably lower compared with the case of FIG.
- the flue gas temperature dropped from 160 ° C to 100 ° C.
- the dew point of H 2 SO 4 gas is about 110 ° C, and almost all SO 3 in the flue gas condenses in the SO 3 separation device 10 in the form of liquid H 2 SO 4 . Since this condensation occurs on the heat transfer surface of the heat exchanger in the SO 3 separation device 10, most of the condensed H 2 SO 4 adheres to the heat transfer surface and is separated and removed from the flue gas. Become.
- S 0 3 concentration is reduced from 4 ppm inlet 2. 5 ppm.
- N a HC 0 3 after supplied from carbonic acid Na Application Benefits um supply equipment 2 0 (FIG. 1, II points) is 2 . Increased from 5 ppm to 4 ppm.
- Residual SO 3 concentration of becomes more N a HC 0 3 supply increased even more the amount of S 0 3 lower concentration decreased difficulty no longer must increase the SO 3 concentration in order to reduce LPPM N the amount of a HCO 3 residual S 0 3 concentration is increased as the lower. Therefore, when the permissible residual concentration of S 0 3 after N a HC 0 3 supply 2. increases from 5 ppm to 4 ppm, N a HCO 3 supply amount that is required is about 3 0% less.
- the provision of the so 3 separation device 10 significantly reduces the consumption of NaHCO 3 .
- FIG. 1 Although in the example of FIG. 1 is provided with air heater 5 to preheat the combustion air and flue gas boiler combustion air is heat exchanged with S 0 3 separation device upstream, wet EP 8 outlets in addition to the air heater 5 Heat exchange between the flue gas at the chimney (or the chimney 11 inlet) and the flue gas upstream of the SO 3 separation device to heat the flue gas discharged from the chimney produces white smoke due to water vapor at the chimney.
- a gas / gas heater may be provided to prevent this.
- the SO 3 separation device 10 of the present embodiment includes a casing 10 a through which flue gas passes from above and a lower portion, and a cooling water inside the casing 10 a, which is disposed at a right angle to the flow of the flue gas.
- a heat exchanger 100 of a shell 'and' tube type consisting of a tube 10b through which the water passes, and a washing device 101 arranged above the group of tubes 10b.
- the washing device 101 is arranged, for example, in parallel with the tube 10b, and has a header pipe 101a supplied with industrial water, and a plurality of branch pipes extending horizontally from the header to the top of the tube 10b group.
- 101b nozzles 101c that spray water from each branch pipe toward the tube 10b group
- header pipes 1 It has an on-off valve 1 Old which controls the supply of water from 01 a to each branch pipe.
- each branch pipe 101b is provided with two nozzles 101b in total, and a total of 10 nozzles 101c are provided, and each nozzle is shown by a circle centered on each nozzle in FIG. Spray the area with water.
- the mist circle from each nozzle is sufficiently overlapped with the adjacent spray circle, and is cleaned by the ten nozzles without leaving the outer circumference of all tubes of the heat exchanger. It is possible.
- the smoke discharged from the upper part of the casing 10a comes into contact with the tube 10b inside the casing 10a, and is discharged on the outer periphery of the low-temperature tube 10b.
- S 0 3 component condenses as H 2 SO 4 liquid, adhere to.
- the amount of H 2 SO 4 deposited on the outer circumference of the tube 10 b increases with time and forms scale with the dust in the flue gas.
- the outer circumference of the tube is periodically cleaned by the cleaning device 101. By washing water with water, it is possible to prevent a decrease in the heat exchange efficiency of the tube due to the accumulation of scale on the outer periphery of the tube 10b, and to reduce the condensed H
- the 2 S 0 4 are separated and removed from the flue gas.
- the surface of the tube 10b and the inner surface of the casing 10a are all PTFE (polytetrafluoroethylene) or PFA with high chemical resistance. (4F Tsui-Dani Ethylene Park Mouth Anolequinolenebininoleatenore Copolymer) is applied to prevent corrosion of tube and casing.
- the casing 10a and the tube 10b may be made of a corrosion-resistant material such as stainless steel having high chemical resistance.
- boiler feedwater is used as cooling water supplied to the tube 10b.
- this exhaust heat is supplied to the boiler feed water by the heat exchanger 100.
- the fuel consumption of the boiler can be significantly reduced.
- the supply amount of NaHCO 3 from the sodium carbonate supply device 20 is significantly reduced while exhausting smoke. Because it is possible to remove the S 0 3, but that have relatively high sulfur content (for example 2% or more) by using an inexpensive heavy oil it is possible to reduce the operating costs of the boiler , Furthermore, the on to use the heat exchanger 1 0 0 S 0 3 separator 1 0 as Ekonomaiza one for heating the boiler feed water, it is possible to significantly reduce fuel consumption in addition to the I have.
- the wastewater after the tube 10b surface cleaning contains sulfuric acid adhering to the tube. This Therefore, the wastewater after washing cannot be discharged as it is, and neutralization with sulfuric acid is required.
- the wastewater after washing the tube 10b is supplied to the absorption tower of the wet desulfurization unit 7 to neutralize the washing wastewater without separately providing a wastewater treatment facility, and to reduce the S o of the absorption tower.
- the water consumption of the wet desulfurization unit 7 can be reduced by using it as makeup water for the absorbent aqueous solution.
- FIG. 3 is a diagram schematically showing the arrangement of the SO 3 separation device when the washing wastewater of the SO 3 separation device 10 is used as makeup water for the absorption tower.
- cooling tower 7 3 reduce the flue gas temperature flowing into the absorption tower 7 3 is intended to improve the absorption efficiency of the S 0 2.
- cooling tower 7 3 Inside, the flue gas enters the cooling tower from the inlet provided at the top of the cooling tower, flows downward in the tower, and flows into the absorption tower 71 from the flue gas passage 77 provided at the bottom of the cooling tower ⁇ 3 I do.
- cooling tower 73 industrial water supplied from the outside is sprayed from the cooling nozzle 73a into the flue gas, and a part thereof evaporates to lower the flue gas temperature.
- the water sprayed from the cooling nozzles 73a is temporarily stored in the water tank 73b below the cooling tower 73, and overflows from the smoke exhaust passages 77 when the water level rises, causing the aqueous solution of the absorbent in the absorption tower to flow. It flows into the circulating water tank 7 1 b.
- the aqueous solution of the absorbent in the circulating water tank 71b is sprayed into the smoke exhaust from the nozzle 71a at the top of the absorption tower by the circulation pump 75, and the sprayed absorbent exhausts the smoke flowing upward in the absorption tower 71. contact, is recovered, for example, C a S in smoke in the form of SO 4 0 2 absorption to the circulation water tank 7 1 b and.
- the SO 3 separation device 10 is arranged at the smoke exhaust inlet above the cooling tower 73. Therefore, SO 3 separation device 1 effluent containing H 2 S 0 4 after cleaning the tubes of 0 is to lower the cooling tower 7 3 enters the bottom of the water tank 7 3 b, absorption and further overflows Feed into 7 lb of recirculating water in tower 71. As a result, H 2 SO 4 in the washing wastewater reacts with the SO 2 absorbent (eg, calcium hydroxide) to be neutralized, and the amount of makeup water to the circulating water tank 71 b is reduced. .
- SO 2 absorbent eg, calcium hydroxide
- the temperature of the flue gas flowing into the cooling tower 73 is considerably reduced due to passing through the SO 3 separation device 10 (see FIG. 1 (B)). For this reason, the amount of water that evaporates when cooling the exhaust gas in the cooling tower 71 is reduced, and the water consumption itself in the cooling tower is reduced. Therefore, in the present embodiment, the consumption of industrial water in the wet desulfurization apparatus 7 can be significantly reduced in addition to the above-described reduction of the makeup water.
- the absorption tower 71 has a smoke exhaust passage 77 at the inlet and a cooling nozzle 73a to spray water to discharge smoke. even in a configuration for cooling, it is possible to obtain a reduction effect of the flue gas passage 7 7 top of S 0 3 Ri by the placing the separator 1 0 3 equivalent industrial water.
- the silo 2 0 as N a HCO 3 powder supply from N a HC 0 3 powder fluidity by increasing large dispensing device in the silo becomes uniform, the flip Yu Daizu air Supplied. Fried soybean air is passed through a free soy blower 204 through an air pipe 205, and through a number of pores of a diffuser plate 203 provided on the bottom wall 201 of the sieve opening 201.Na HCO 3 powder 210 It is shot inside. As a result, the NaHCO 3 powder in the silo 201 flows smoothly without forming lumps and flows into the quantitative supply device 206.
- N a HC 0 3 supply amount of the powder to flue 3 (flow rate) can be adjusted Ri by the Rukoto changing the operating speed of the dispensing device 2 0 6.
- S 0 3 separator 1 0 of the present embodiment regardless of the type of wet desulfurization apparatus, FIG. 3, it can be installed on a wet desulfurization system, as shown in FIG. Further, the sodium carbonate supply device 20 of the present embodiment can be easily connected to the flue 3 via the nozzle 315 as shown in FIG. For this reason, for example, as shown in Fig. 6, even existing flue gas treatment equipment that uses only desulfurization equipment to perform flue gas treatment can be easily modified by using existing wet desulfurization equipment as it is. it is possible to perform additional installation of the S 0 3 separation equipment and carbonate isocyanatomethyl Li ⁇ beam feeder 2 0. Therefore, the renovation work using the existing wet desulfurization equipment According to the method of fabricating the SO 3 minutes remover, it is possible to configure a very low cost SO 3 minutes remover.
- wet EP is not installed at the outlet of the wet desulfurizer.
- the wet EP is installed at the outlet of the ⁇ desulfurizer 7 in the configuration of FIG. Needless to say, the consumption of ( 3 ) can be further reduced.
- particles such as sulfuric acid mist in the flue gas are charged, and a dielectric such as water is sprayed on the charged particles.
- an electrostatic precipitator of the type in which the dielectric is dielectrically polarized by applying a voltage, and fine particles such as sulfuric acid mist charged on the dielectric having a relatively large particle diameter are captured. .
- the trapping efficiency of submicron particles is achieved by trapping the mist of sulfuric acid particles from the submicron into relatively large dielectric particles and trapping them together with the dielectric particles. Therefore, it is possible to reduce the size of the apparatus while maintaining the same SO 3 removal efficiency as in wet EP.
- a part of Na HSO 3 generated by the reaction between sodium carbonate supplied in the flue gas and SO 3 further reacts with the SO 3 component in the flue gas to produce N N generating a a HS 0 4 (acidic sulfate isocyanatomethyl Li um), this N a HS_ ⁇ 4 is extremely hygroscopic high, attached to the movable portion when there is a device having a good sea urchin movable member such Purowa Ya damper, Problems such as sticking may occur. For this reason, equipment such as a propel damper that has movable members should not be placed in the flue gas passage between the sodium carbonate supply device and the wet desulfurization device to prevent problems such as adhesion. It is preferred to prevent this from occurring.
- the reaction product of a carbonate isocyanatomethyl Li um and so 3 If a removable sodium carbonate removal device is provided, no problem such as sticking will occur even if devices with movable members are placed in the smoke exhaust passage downstream of the sodium carbonate removal device. . However, also in this case, equipment having a movable member, such as a propeller damper, should not be placed in the smoke exhaust passage between the sodium carbonate supply device and the sodium carbonate removal device. It is preferable to prevent the occurrence of problems such as sticking. As described above, according to the present invention, it is possible to remove SO 3 from flue gas without increasing the plant operation cost. In addition, by modifying a flue gas treatment system that has an existing wet desulfurization system, it is possible to easily configure an SO 3 removal system, and the cost of the system can be further reduced. To play.
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/470,196 US20040047773A1 (en) | 2001-06-21 | 2002-06-20 | So3 separating and removing equipment for flue gas |
EP02743672A EP1402937A4 (en) | 2001-06-21 | 2002-06-20 | DEVICE FOR DISCONNECTING AND REMOVING SO3 FROM SMOKE GAS |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2001-188405 | 2001-06-21 | ||
JP2001188405A JP4841065B2 (ja) | 2001-06-21 | 2001-06-21 | 排煙のso3分除去装置 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2003000387A1 true WO2003000387A1 (en) | 2003-01-03 |
Family
ID=19027512
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2002/006185 WO2003000387A1 (en) | 2001-06-21 | 2002-06-20 | So3 separating and removing equipment for flue gas |
Country Status (4)
Country | Link |
---|---|
US (1) | US20040047773A1 (ja) |
EP (1) | EP1402937A4 (ja) |
JP (1) | JP4841065B2 (ja) |
WO (1) | WO2003000387A1 (ja) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN109876616A (zh) * | 2019-04-11 | 2019-06-14 | 东南大学 | 一种燃煤锅炉烟气三氧化硫脱除装置 |
US11260401B2 (en) * | 2018-10-01 | 2022-03-01 | DOOSAN Heavy Industries Construction Co., LTD | Dust collecting module, desulfurizing apparatus having same, and method of installing dust collecting module |
Families Citing this family (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7938885B2 (en) * | 2004-05-08 | 2011-05-10 | Qingbao Huang | Device for the removal of soot dust of fuel oil combustion |
WO2005115593A1 (es) * | 2004-05-25 | 2005-12-08 | Ferroatlantica, S.L. | Procedimiento para la obtención de manganeso electrolítico a partir de residuos de la fabricacíon de ferroaleaciones |
US7481987B2 (en) * | 2005-09-15 | 2009-01-27 | Solvay Chemicals | Method of removing sulfur trioxide from a flue gas stream |
JP5307974B2 (ja) * | 2006-03-17 | 2013-10-02 | 三菱重工業株式会社 | 排ガス処理装置 |
KR101326812B1 (ko) * | 2011-05-17 | 2013-11-07 | 현대자동차 주식회사 | 배기가스 후처리 방법 |
US20140072483A1 (en) | 2012-09-10 | 2014-03-13 | Mitsubishi Heavy Industries, Ltd. | Desulfurization device and particulate collection system |
US8877152B2 (en) | 2013-02-27 | 2014-11-04 | Alstom Technology Ltd | Oxidation system and method for cleaning waste combustion flue gas |
CN103697487B (zh) * | 2013-12-30 | 2016-05-11 | 上海克莱德贝尔格曼机械有限公司 | 一种烟气处理装置 |
JP6723793B2 (ja) * | 2016-03-31 | 2020-07-15 | 三菱日立パワーシステムズ株式会社 | 脱硫処理装置及び脱硫処理装置の運転方法 |
CN106914124A (zh) * | 2017-04-24 | 2017-07-04 | 中国计量大学 | 湿法脱硫塔内热管换热节水除雾防石膏雨装置 |
CN107648978B (zh) * | 2017-10-27 | 2024-03-22 | 中冶华天工程技术有限公司 | 湿法脱硫烟气消除烟羽系统及方法 |
CN108187463A (zh) * | 2018-02-24 | 2018-06-22 | 厦门锐传科技有限公司 | Fcc烟气的治理系统及其治理方法 |
KR102079796B1 (ko) * | 2018-10-04 | 2020-02-20 | 두산중공업 주식회사 | 집진 모듈 및 이를 포함하는 탈황 장치 |
CN109999603A (zh) * | 2019-04-11 | 2019-07-12 | 通用技术集团工程设计有限公司 | 一种降低湿法洗涤湿烟气温度和含水量的设备和方法 |
CN110028085A (zh) * | 2019-04-23 | 2019-07-19 | 鞍钢集团工程技术有限公司 | 一种利用脱硫灰制取元明粉的工艺及系统 |
CN111486464B (zh) * | 2020-03-25 | 2024-04-26 | 清华大学 | 基于余热法污染物资源化的无废垃圾电厂工艺方式与系统 |
CN112473348B (zh) * | 2020-11-06 | 2022-09-16 | 上海市政工程设计研究总院(集团)有限公司 | 一种烟气处理系统及烟气处理方法 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0727324A (ja) * | 1993-07-09 | 1995-01-27 | Babcock Hitachi Kk | 排ガスの熱回収装置 |
EP0937491A2 (en) * | 1998-02-23 | 1999-08-25 | Mitsubishi Heavy Industries, Ltd. | Flue gas treating process and apparatus |
US6180074B1 (en) * | 1995-10-31 | 2001-01-30 | Novacarb | Method for processing flue gases containing sulphur oxides |
Family Cites Families (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4189309A (en) * | 1978-03-14 | 1980-02-19 | Hoekstra Irenus A | Desulfurization of flue gas |
JPS61167431A (ja) * | 1985-01-21 | 1986-07-29 | Asahi Chem Ind Co Ltd | 脱硫方法 |
US5198201A (en) * | 1988-03-08 | 1993-03-30 | Johnson Arthur F | Removal of sulphur and nitrogen oxides from flue gases |
US5122352A (en) * | 1988-03-08 | 1992-06-16 | Johnson Arthur F | Heat exchanger and pollutant removal system |
US5230870A (en) * | 1992-05-26 | 1993-07-27 | Johnson Arthur F | Method for converting noxious pollutants from flue gas into merchantable by-products |
US6143263A (en) * | 1994-04-29 | 2000-11-07 | The Babcock & Wilcox Company | Method and system for SO2 and SO3 control by dry sorbent/reagent injection and wet scrubbing |
JPH11147018A (ja) * | 1997-11-17 | 1999-06-02 | Mitsubishi Heavy Ind Ltd | So3 ミストの捕集装置 |
JP3564296B2 (ja) * | 1998-05-18 | 2004-09-08 | 三菱重工業株式会社 | 排煙処理方法 |
JPH11319477A (ja) * | 1998-05-13 | 1999-11-24 | Takehiko Morimoto | 化石燃料の燃焼排ガスの処理方法 |
JP3840858B2 (ja) * | 1998-11-26 | 2006-11-01 | 旭硝子株式会社 | 酸性成分除去剤及び酸性成分除去方法 |
JP3872247B2 (ja) * | 1999-03-12 | 2007-01-24 | 有限会社矢上船舶機器サービス | 横置円筒回転式廃frpの熱分解方法 |
JP2001327830A (ja) * | 2000-05-22 | 2001-11-27 | Ishikawajima Harima Heavy Ind Co Ltd | 排煙処理装置 |
JP2002071120A (ja) * | 2000-08-30 | 2002-03-08 | Fuji Kikai Kk | 燃焼排ガス処理装置 |
JP2002263442A (ja) * | 2001-03-12 | 2002-09-17 | Mitsubishi Heavy Ind Ltd | 排煙のso3分除去装置 |
JP4606651B2 (ja) * | 2001-06-07 | 2011-01-05 | 三菱重工メカトロシステムズ株式会社 | 排煙のso3分除去装置 |
-
2001
- 2001-06-21 JP JP2001188405A patent/JP4841065B2/ja not_active Expired - Lifetime
-
2002
- 2002-06-20 US US10/470,196 patent/US20040047773A1/en not_active Abandoned
- 2002-06-20 EP EP02743672A patent/EP1402937A4/en active Pending
- 2002-06-20 WO PCT/JP2002/006185 patent/WO2003000387A1/ja not_active Application Discontinuation
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0727324A (ja) * | 1993-07-09 | 1995-01-27 | Babcock Hitachi Kk | 排ガスの熱回収装置 |
US6180074B1 (en) * | 1995-10-31 | 2001-01-30 | Novacarb | Method for processing flue gases containing sulphur oxides |
EP0937491A2 (en) * | 1998-02-23 | 1999-08-25 | Mitsubishi Heavy Industries, Ltd. | Flue gas treating process and apparatus |
Non-Patent Citations (1)
Title |
---|
See also references of EP1402937A4 * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US11260401B2 (en) * | 2018-10-01 | 2022-03-01 | DOOSAN Heavy Industries Construction Co., LTD | Dust collecting module, desulfurizing apparatus having same, and method of installing dust collecting module |
CN109876616A (zh) * | 2019-04-11 | 2019-06-14 | 东南大学 | 一种燃煤锅炉烟气三氧化硫脱除装置 |
Also Published As
Publication number | Publication date |
---|---|
US20040047773A1 (en) | 2004-03-11 |
JP2003001054A (ja) | 2003-01-07 |
EP1402937A4 (en) | 2007-08-08 |
JP4841065B2 (ja) | 2011-12-21 |
EP1402937A1 (en) | 2004-03-31 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2003000387A1 (en) | So3 separating and removing equipment for flue gas | |
CN104761010B (zh) | 用于使废水蒸发和减少酸性气体排放的设备和方法 | |
US5603909A (en) | Selective catalytic reduction reactor integrated with condensing heat exchanger for multiple pollutant capture/removal | |
KR102175549B1 (ko) | 텐터후단 배기가스 상의 악취와 백연의 저감 수단 및 고점성 오염물질의 회수 수단을 갖는 다단형 배기가스 처리 공정 시스템 | |
JP7005166B2 (ja) | 廃水を蒸発させて酸性ガス排出を減らすための装置及び方法 | |
WO2014129030A1 (ja) | 排ガス処理システム及び排ガス処理方法 | |
US6726748B2 (en) | Method of converting a downflow/upflow wet flue gas desulfurization (WFGD) system to an upflow single-loop WFGD system | |
US9650269B2 (en) | System and method for reducing gas emissions from wet flue gas desulfurization waste water | |
SI9520025A (en) | Flue gas scrubbing apparatus | |
JP4606651B2 (ja) | 排煙のso3分除去装置 | |
WO2004023040A1 (ja) | 排煙処理システム | |
CN103868087A (zh) | 一种协同增强pm2.5脱除和烟气余热深度利用的方法及装置 | |
CN101956991A (zh) | 一种湿法烟气净化尾气的除湿工艺及装置 | |
JP2013078742A (ja) | 排ガス処理装置と排ガス処理方法 | |
US9724638B2 (en) | Apparatus and method for evaporating waste water and reducing acid gas emissions | |
JP6740185B2 (ja) | 加圧流動炉システムにおける排ガス脱硫方法及び加圧流動炉システム | |
CN105396451B (zh) | 一种喷淋脱硫塔内碱液清洗高效脱除so3的工艺 | |
CN205235747U (zh) | 一种喷淋脱硫塔内碱液清洗高效脱除so3的工艺装置 | |
CN113101779A (zh) | 一种含硫、尘工业烟气净化系统及方法 | |
JP3856394B2 (ja) | タール含有排ガスの処理設備および排ガス処理におけるタール除去方法 | |
CN216703843U (zh) | 一种新型高效超净除尘与消白一体化装置 | |
CN208097647U (zh) | 烟气污染物处理系统及烟囱 | |
CN116808802A (zh) | 烧结烟气处理设备 | |
CN111320223A (zh) | 预防脱硫废水粘壁的干燥塔、方法及脱硫废水处理系统 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): US |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE TR |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
WWE | Wipo information: entry into national phase |
Ref document number: 2002743672 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 10470196 Country of ref document: US |
|
ENP | Entry into the national phase |
Ref document number: 2004102690 Country of ref document: RU Kind code of ref document: A |
|
WWP | Wipo information: published in national office |
Ref document number: 2002743672 Country of ref document: EP |
|
WWW | Wipo information: withdrawn in national office |
Ref document number: 2002743672 Country of ref document: EP |