WO2011055759A1 - Procédé et appareil pour le traitement de gaz d'échappement - Google Patents

Procédé et appareil pour le traitement de gaz d'échappement Download PDF

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Publication number
WO2011055759A1
WO2011055759A1 PCT/JP2010/069627 JP2010069627W WO2011055759A1 WO 2011055759 A1 WO2011055759 A1 WO 2011055759A1 JP 2010069627 W JP2010069627 W JP 2010069627W WO 2011055759 A1 WO2011055759 A1 WO 2011055759A1
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WIPO (PCT)
Prior art keywords
exhaust gas
combustion furnace
furnace
desulfurizing agent
combustion
Prior art date
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PCT/JP2010/069627
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English (en)
Japanese (ja)
Inventor
龍海 田野
幸弘 小山
敏明 中村
剛 村谷
一浩 ▲さい▼合
Original Assignee
宇部興産株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 宇部興産株式会社 filed Critical 宇部興産株式会社
Priority to JP2011539386A priority Critical patent/JP5969762B2/ja
Priority to CN201080050091.XA priority patent/CN102597626B/zh
Priority to IN3830DEN2012 priority patent/IN2012DN03830A/en
Priority to AU2010316285A priority patent/AU2010316285B2/en
Publication of WO2011055759A1 publication Critical patent/WO2011055759A1/fr

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • 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
    • B01D53/508—Sulfur oxides by treating the gases with solids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/003—Arrangements of devices for treating smoke or fumes for supplying chemicals to fumes, e.g. using injection devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J7/00—Arrangement of devices for supplying chemicals to fire
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/10—Intercepting solids by filters
    • F23J2217/102—Intercepting solids by filters electrostatic

Definitions

  • the present invention relates to a method and apparatus for treating exhaust gas in equipment equipped with a combustion furnace such as a boiler for burning a fuel containing a sulfur component.
  • the exhaust gas from the combustion furnace is usually processed by an exhaust gas treatment facility such as a denitration apparatus, a gas air heater, an electrostatic precipitator, and a desulfurization apparatus provided at the subsequent stage of the combustion furnace.
  • an exhaust gas treatment facility such as a denitration apparatus, a gas air heater, an electrostatic precipitator, and a desulfurization apparatus provided at the subsequent stage of the combustion furnace.
  • SO 3 in the exhaust gas is condensed as sulfuric acid (H 2 SO 4 ), which causes corrosion of the flue and various devices.
  • An object of the present invention is to provide an exhaust gas treatment method and apparatus that can efficiently and inexpensively and easily treat SO 3 in combustion gas in order to solve the above-described problems caused by the prior art.
  • an exhaust gas treatment method is a treatment of exhaust gas in which a fuel containing a sulfur component is combusted in a combustion furnace and combustion gas is discharged from the combustion furnace as exhaust gas.
  • the combustion furnace has an upper nose portion that narrows the space in the furnace above the furnace, and a desulfurizing agent is injected by a desulfurizing agent blowing means in the vicinity of the upper nose portion in the combustion furnace that discharges the exhaust gas. It is characterized by doing.
  • the exhaust gas discharged from the combustion furnace can be cooled to a temperature of 90 ° C. to 120 ° C. by the exhaust gas temperature reducing means and then supplied to the electric dust collector.
  • the desulfurizing agent is, for example, a calcium compound
  • the calcium compound preferably includes cement factory dust containing calcium carbonate (CaCO 3 ).
  • the exhaust gas temperature reduction means is a method in which the exhaust gas is indirectly cooled by a gas-water heat exchange means or a method in which water is sprayed into the exhaust gas and directly cooled. Can be configured.
  • the vicinity of the upper nose portion is, for example, a range in the height direction caused by the base of the triangle of the nose portion.
  • the desulfurizing agent blowing means has a pipe, and the pipe is a projecting pipe connected to the combustion furnace and projecting in the horizontal direction toward the inside of the combustion furnace.
  • the protrusion length of the protrusion pipe into the combustion furnace is preferably more than 0 and 600 mm or less.
  • An exhaust gas treatment apparatus includes a combustion furnace in which an upper nose portion is formed in the upper portion of the furnace that burns fuel and narrows the space in the furnace, and a desulfurizing agent is disposed in the vicinity of the upper nose portion in the combustion furnace. And a desulfurizing agent blowing means for injection.
  • the exhaust gas treatment apparatus further comprises exhaust gas temperature reducing means for reducing the temperature of the exhaust gas from the combustion furnace, and dust collection means for removing dust in the exhaust gas from the exhaust gas temperature reducing means,
  • the temperature reducing means can be configured to cool the exhaust gas discharged from the combustion furnace indirectly by the gas-water heat exchange means or directly by the water spray device.
  • SO 3 in combustion gas can be processed efficiently, cheaply and easily.
  • FIG. 1 is a schematic system diagram illustrating an example of an exhaust gas treatment facility that performs an exhaust gas treatment method according to an embodiment of the present invention. It is a horizontal sectional view of the blowing position of the desulfurization agent 0.8M above and 0.4L below in the combustion furnace of the Example of this invention. It is a simulation result regarding the supply position of the desulfurization agent in the processing method of the waste gas concerning one embodiment of the present invention. It is a simulation result regarding the intrusion piping in the processing method of the exhaust gas concerning one embodiment of the present invention.
  • FIG. 1 is a schematic system diagram showing an example of an exhaust gas treatment facility for implementing an exhaust gas treatment method according to an embodiment of the present invention.
  • an exhaust gas treatment facility 100 includes a desulfurization agent supply device 10 that stores a desulfurization agent conveyed by a truck 90 or the like and supplies it to a combustion furnace 20 such as a boiler, pulverized coal, heavy oil, and petroleum coke. And a combustion furnace 20 for burning fuel such as the above.
  • the type of the combustion furnace 20 is not particularly limited.
  • a boiler, particularly a pulverized coal fired boiler, is preferably used as the combustion furnace 20.
  • the exhaust gas treatment facility 100 includes an exhaust gas temperature reduction facility 30 that lowers the temperature of the exhaust gas discharged from the combustion furnace 20, and an electric dust collector 40 that captures dust in the exhaust gas discharged from the exhaust gas temperature reduction facility 30.
  • the exhaust gas discharged from the electrostatic precipitator 40 is conveyed by the blower 48 and discharged into the atmosphere through the chimney 49.
  • the desulfurization agent supply device 10 includes a storage tank 11 for storing the conveyed desulfurization agent, and a quantitative discharge mechanism 12 and a blower 13 for appropriately supplying the desulfurization agent stored in the storage tank 11 to the combustion furnace 20. It is configured.
  • the desulfurization agent conveyed from the storage tank 11 by the fixed discharge mechanism 12 and the blower 13 passes through, for example, a desulfurization agent supply pipe (pipe) (not shown) connected to the desulfurization agent inlet 14 provided in the wall 20a of the combustion furnace 20. And injected into the combustion furnace 20. It is preferable to install the desulfurizing agent blowing port 14 on the side wall of the combustion furnace 20.
  • the desulfurization agent inlet 14 of the desulfurization agent supply apparatus 10 can blow the desulfurization agent 15 into a position near a nose portion 21 (also referred to as an upper nose portion 21) formed above the combustion furnace 20. It is formed as follows.
  • the nose refers to a protrusion provided in the furnace, and prevents the combustion gas from flowing through the superheater by bypassing the combustion gas, thereby ensuring the residence time of the combustion gas. Have.
  • the vicinity position of the nose portion 21 is a portion indicated by H (L + M) in FIG. That is, the range of the height direction which the base of the triangle of the nose part 21 brings about, and the space of the combustion furnace which does not have the superheater 20b extended from the upper part of the nose part 21 to the space of the nose part 21 in the range of the height.
  • a desulfurizing agent is supplied to the space.
  • the number of desulfurization agent inlets 14 is 1 or 2 or more. Among these, considering that the desulfurizing agent is appropriately dispersed in the combustion furnace 20, 2 or more, particularly 4 to 6 is preferable. About the position of the desulfurization agent injection
  • a calcium compound is preferable, and calcium hydroxide, calcium oxide, and calcium carbonate are preferable. More preferably, cement factory dust whose main component is calcium carbonate can be used.
  • Cement factory dust is recovered from, for example, exhaust gas in the process of producing cement raw material, and is a dust having a particle size of about 2 microns, and can be obtained at a very low cost and in large quantities.
  • the injected desulfurizing agent 15 captures SO 3 generated by the combustion of fuel more suitably and efficiently.
  • the cement factory dust include dust recovered from a cement raw material pulverization step and dust recovered from cement firing exhaust gas.
  • CaCO 3 ⁇ CaO is obtained by the decarbonation reaction, and this CaO reacts with SO 2 by the desulfurization reaction to cause CaO + SO 2 + 0.5O 2 ⁇ CaSO 4. (Calcium sulfate). Moreover, CaO after the decarboxylation reaction captures SO 3 . It has been confirmed by the present inventor that such a desulfurization reaction is most activated by injecting the desulfurizing agent 15 into the vicinity of the upper nose portion 21 of the combustion furnace 20.
  • the desulfurization ability of the desulfurizing agent is larger as the specific surface area of the desulfurizing agent is larger.
  • cement factory dust used as the desulfurizing agent 15 will be described. Table 2 shows the physical properties when cement factory dust (calcium carbonate is 75 mass%, silica is 13 mass%, alumina is 7 mass%, iron oxide is 2 mass%, and other 3 mass%).
  • the decarboxylation reaction of the cement factory dust starts at around 700 ° C and shows the maximum peak at 741 ° C.
  • a structural change accompanied by heat generation is confirmed from around 1200 ° C.
  • the peak temperature of the change is 1288 ° C.
  • the temperature is preferably less than 1200 ° C.
  • the molar ratio (Ca / S) of calcium (Ca) of the desulfurizing agent to the sulfur content (S) in the fuel is preferably 0.5 to 3, and preferably 1 to 2.5. When the molar ratio is greater than 3, the amount of dust increases.
  • Air ratio 1.17 Coal total moisture [arrival base mass%]: 9 mass%
  • Coal industry analysis [mass-dry base mass%]: moisture 3 mass%, ash 13 mass%, volatile matter 34 mass%, fixed carbon 50 mass%, Elemental analysis of coal [anhydrous ashless base mass%]: carbon 83 mass%, hydrogen 5 mass%, oxygen 9 mass%, nitrogen 2 mass%, sulfur 1 mass%, (2) Calculation model The following calculation model was used for combustion, heat transfer, and fluid calculation.
  • Two-phase flow model Lagradian two-layer flow model
  • Turbulence model k- ⁇ model
  • Volatile release model Overall primary reaction model
  • Gas combustion model Eddy-breakup model
  • Char combustion model Shrinking core primary reaction model
  • Radiation heat transfer model Discrete transfer method (3) Boundary conditions The following conditions were set as boundary conditions.
  • Boiler outlet target oxygen concentration 3% by volume
  • Boiler outlet target temperature 370 ° C
  • the gas temperature is about 1800 ° C. in the vicinity of the burner, approximately 1200 ° C. at the nose inlet, 1000 ° C. at the nose outlet, and 700 ° C. at the superheater outlet. It is known that particles having a particle size of several tens of ⁇ m or less become equal to the gas temperature within 0.1 seconds. Therefore, the temperature of the particles blown into the furnace can be regarded as equivalent to the gas temperature.
  • FIG. 3 shows the simulation results of the particle dispersion state and particle temperature history when the desulfurization agent is blown into the upper side of the nose part, the nose part, and the lower side of the nose part.
  • FIG. 3A when blown into the upper part of the nose portion, the gas flow is less disturbed and the particles flow straight from the blow port in the gas flow direction. Therefore, the particle temperature does not vary and the dispersion state is not good.
  • FIG. 3B when the gas is blown into the nose portion, the gas flow in the nose portion is disturbed, so that the particles are also violently dispersed in the front, rear, left and right and dispersed throughout. Therefore, the particle temperature has a wide distribution at the nose exit. The residence time of the particles becomes longer due to the disturbance.
  • the particles when blown to the lower side of the nose portion, the particles are once heated to 1200 ° C. or higher and then enter the nose portion, where they are vigorously mixed and dispersed throughout. Yes.
  • the structure change of the particles occurs as described above, and the reaction activity of the desulfurizing agent decreases. From this result, it became clear that it was necessary to blow a desulfurizing agent into the nose part.
  • the piping as the desulfurizing agent blowing means is connected to the combustion furnace 20, and the desulfurizing agent is supplied into the combustion furnace.
  • the pipe may have a structure that does not protrude into the combustion furnace 20 (projection length is zero), but is preferably a protruding pipe that protrudes in the horizontal direction toward the inside of the combustion furnace. Thereby, dispersion
  • the projecting length of the projecting pipe into the combustion furnace is more than 0 and 600 mm or less, preferably 100 to 500 mm. If the penetration length is too long, it is not economical and the construction of the penetration piping becomes difficult.
  • the protrusion length refers to the distance from the inner wall of the combustion furnace 20 to the tip of the protrusion pipe.
  • FIG. 4 shows the locus of dust particles.
  • Fig.4 (a) in the case of a plunging pipe, it turns out that particle
  • the particles are close to the wall of the combustion furnace. From this result, it is shown that when there is a protruding pipe, the desulfurization agent is more dispersed and the residence time is long. Thereby, the improvement of a desulfurization rate can be aimed at.
  • the cause of the effect of the intrusion piping is not clear, but the swirl flow of the gas in the furnace is stronger than the center of the furnace wall, and this strong flow is necessary to disperse the dust particles widely. It is estimated that it is better to avoid.
  • the preferable furnace temperature when injecting the desulfurizing agent 15 into the vicinity of the upper nose portion 21 is in the range of 1050 ° C. to 1150 ° C.
  • the exhaust gas from which SO 2 and SO 3 have been removed in the combustion furnace 20 in this way is discharged from the combustion furnace 20 through the flue 22 and supplied to the exhaust gas temperature reduction equipment 30 at the subsequent stage.
  • the production reaction proceeds as the temperature increases.
  • the decomposition reaction is governed by an equilibrium reaction.
  • the decomposition reaction occurred at 1050 ° C. or higher, and almost the entire amount was decomposed at 1150 ° C. or higher. From the above results, it was evaluated that the temperature range of 1050 ° C. to 1150 ° C. was preferable for the desulfurization reaction from the generation reaction and the decomposition reaction.
  • the exhaust gas temperature reducing equipment 30 is composed of, for example, a gas air heater 31 and a gas-water heat exchanger 32 or a water spray device 33.
  • a method for lowering the temperature of the exhaust gas there are three possible methods: (1) increasing the capacity of the gas air heater, (2) indirect cooling, and (3) direct cooling.
  • direct cooling of (3) that is, cooling by spraying water on the exhaust gas, for example
  • the heat of the exhaust gas is exchanged with the circulating water of the gas-water heat exchanger 32 disposed on the downstream side of the gas air heater 31 to preheat the water supplied to the combustion furnace 20 and used.
  • SO 3 is contained about 1% of SO 2 and the acid dew point is about 120 ° C. to 130 ° C. Therefore, heat recovery from the exhaust gas has a temperature of the exhaust gas of 150 ° C. It was the limit until it reached about °C.
  • the exhaust gas treatment method according to the present embodiment SO 3 in the exhaust gas is removed in advance by the desulfurizing agent 15 injected into the vicinity of the upper nose portion 21 in the combustion furnace 20,
  • the acid dew point can be significantly lowered.
  • the temperature of the exhaust gas can be cooled to about 100 ° C., and as a result, the amount of heat recovery can be increased to significantly improve the energy efficiency.
  • each device provided in the exhaust gas temperature reduction facility 30 with an expensive corrosion-resistant material.
  • the material of the portion of the gas-water heat exchanger 32 that contacts the exhaust gas can be an inexpensive carbon steel (carbon steel) material. It has been found that lowering the temperature of the exhaust gas by using the exhaust gas temperature reducing equipment 30 greatly affects the maintenance and improvement of the dust collection performance of the electric dust collector 40 in the next stage.
  • the SO 3 in the exhaust gas is removed by the desulfurization agent 15 in the combustion furnace 20, but a certain solution is seen for problems such as corrosion. If SO 3 is removed from the dust collector, the dust collection performance of the electrostatic precipitator 40 will be significantly reduced.
  • the dust collecting performance of the electrostatic precipitator 40 (1) the temperature of the exhaust gas, (2) the speed of the exhaust gas (flow rate) determined by the elements of the concentration of (3) SO 3, SO 3 (3) It is said that the higher the concentration of, the better the dust collection performance.
  • SO 3 is removed by the desulfurization agent 15 injected in the vicinity of the upper nose portion 21 in the combustion furnace 20, so that the exhaust gas having a low SO 3 concentration is discharged.
  • the concentration of SO 3 in the exhaust gas becomes a level that does not affect the dust collection performance of the electric dust collector 40, and the dust collection performance can be maintained and improved.
  • the testing machine used in the examples is an 80t steam / h boiler with the power generation equipment shown in FIG. Pulverized coal and air were supplied to a pulverized coal fired boiler.
  • the desulfurizing agent used was cement factory dust recovered from the cyclone exhaust gas in the raw material grinding process of the cement factory described above.
  • the chemical composition of cement factory dust was measured by X-ray fluorescence analysis. As a result, CaO 60.6 wt%, SiO 2 is 20.8 wt%, Al 2 O 3 is 10.3 wt%.
  • the weight average particle diameter of the used cement factory dust was about 2 microns.
  • the blowing position in Examples 1 and 2 shown below is in the furnace ⁇ , and the blowing position in Example 3 is in the furnace ⁇ .
  • the blowing position of ⁇ in the furnace is 4 of A, B, C, D at a height of 0.8 M above the apex of the nose portion 21 shown in FIG. 2A (the apex of the triangle of the nose portion 21 in FIG. 1).
  • the blowing position of ⁇ in the furnace is E, F, and G at a height 0.4 L below the apex shown in FIG.
  • the desulfurizing agent is supplied so as to avoid the position where the superheater 20b exists.
  • B and C in FIG. 2A are located between the center point and the end point of the side surface.
  • E, F, and G in FIG. 2B are located at the center line portion of each side surface of the combustion furnace.
  • Table 1 shows the SO 3 measurement results obtained in the examples. Note that SO 3 was measured at the entrance of the electrostatic precipitator.
  • Example 1 SOx concentration of SO 2 + SO 3 in the furnace is that 200 ppm, was blown cement plant dust such that the molar ratio of Ca / S is 0.93 in the furnace. As a result, the SO 3 concentration was less than 0.05 ppm.
  • Example 2 In Example 2, when the SOx concentration in the furnace was 180 ppm and the Ca / S molar ratio of the cement factory dust blown into the furnace was 2.06, the SO 3 concentration was the same as in Example 1. It was less than 0.05 ppm.
  • Example 3 In Example 3, when the SOx concentration in the furnace was 150 ppm and the Ca / S molar ratio of the cement factory dust blown into the furnace was 2.92, the SO 3 concentration was in Examples 1 and 2. Similarly, it was less than 0.05 ppm. In Examples 1, 2, and 3, when cement factory dust was not blown, the SOx concentration in the furnace was the same as that before desulfurization.
  • the acid dew point of the exhaust gas can be reduced from 126 ° C to less than 88 ° C. .
  • heat equivalent to 50 ° C. is recovered from the exhaust gas that maintains a temperature of about 150 ° C. when passing through the gas air heater 31. Even if this heat is used as a preheating source of water supplied to the combustion furnace 20, corrosion due to condensation of SO 3 can be prevented.
  • the steam for heating the heating water in the combustion furnace can be reduced by 2.5 t / h, and the energy efficiency can be improved by about 3%.
  • SO 3 in exhaust gas can be efficiently and cheaply and easily treated, and thermal energy is efficiently prevented while preventing corrosion and the like of the facility. It can be used well.
  • Desulfurization agent supply apparatus 11 Reservoir tank 12 Fixed discharge mechanism 13 Blower 14 Desulfurization agent injection port 15 Desulfurization agent 20 Combustion furnace 20a Wall part 20b Superheater 21 Nose part 22 Flue 30 Exhaust gas temperature reduction equipment 31 Gas air heater 32 Gas-water heat Exchanger 33 Water spraying device 40 Electric dust collector 48 Blower 49 Chimney 100 Exhaust gas treatment equipment

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  • Chemical & Material Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • Health & Medical Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
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Abstract

L'invention porte sur un appareil pour le traitement de SO3 contenu dans un gaz de combustion plus rapidement et avec un rendement élevé et à moindre coût. L'invention porte de manière spécifique sur une installation de traitement de gaz d'échappement (100) qui comprend une unité d'alimentation en agent de désulfurisation (10), un four de combustion (20), une installation de diminution de température de gaz d'échappement (30), et un collecteur de poussière électrique (40). L'unité d'alimentation en agent de désulfurisation (10) permet l'introduction d'un agent de désulfurisation dans une position disposée adjacente à une section de nez supérieure (21) dans le four de combustion (20) à travers une entrée d'agent de désulfurisation (14). L'installation (100) peut être adaptée de telle sorte qu'un gaz d'échappement est délivré dans l'installation de diminution de température de gaz d'échappement (30) par l'intermédiaire d'un trajet de fumée (22), une poussière est retirée au moyen du collecteur de poussière électrique (40) tout en diminuant la température du gaz d'échappement, et la poussière est déchargée dans l'air à travers une cheminée (49).
PCT/JP2010/069627 2009-11-06 2010-11-04 Procédé et appareil pour le traitement de gaz d'échappement WO2011055759A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
JP2011539386A JP5969762B2 (ja) 2009-11-06 2010-11-04 排ガスの処理方法および装置
CN201080050091.XA CN102597626B (zh) 2009-11-06 2010-11-04 处理废气的方法和设备
IN3830DEN2012 IN2012DN03830A (fr) 2009-11-06 2010-11-04
AU2010316285A AU2010316285B2 (en) 2009-11-06 2010-11-04 Method and apparatus for treatment of exhaust gas

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Application Number Priority Date Filing Date Title
JP2009-254872 2009-11-06
JP2009254872 2009-11-06

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WO2011055759A1 true WO2011055759A1 (fr) 2011-05-12

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CN (1) CN102597626B (fr)
AU (1) AU2010316285B2 (fr)
IN (1) IN2012DN03830A (fr)
WO (1) WO2011055759A1 (fr)

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CN106287761A (zh) * 2016-08-30 2017-01-04 滁州朝昱农业科技有限公司 一种农作物秸秆高效焚烧系统
CN106287745A (zh) * 2016-08-30 2017-01-04 滁州朝昱农业科技有限公司 一种农作物秸秆焚烧供热系统
JP2019141795A (ja) * 2018-02-21 2019-08-29 太平洋セメント株式会社 脱硫剤及びセメントキルン抽気ガスの脱硫方法

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US9909508B2 (en) * 2014-06-26 2018-03-06 General Electric Company Automatic combustion system characterization
JP6678452B2 (ja) * 2015-12-28 2020-04-08 川崎重工業株式会社 ボイラ及び腐食抑制方法

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