WO2017179107A1 - 排ガスの処理システム - Google Patents

排ガスの処理システム Download PDF

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Publication number
WO2017179107A1
WO2017179107A1 PCT/JP2016/061736 JP2016061736W WO2017179107A1 WO 2017179107 A1 WO2017179107 A1 WO 2017179107A1 JP 2016061736 W JP2016061736 W JP 2016061736W WO 2017179107 A1 WO2017179107 A1 WO 2017179107A1
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WIPO (PCT)
Prior art keywords
exhaust gas
desulfurization
duct
moving bed
denitration
Prior art date
Application number
PCT/JP2016/061736
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English (en)
French (fr)
Japanese (ja)
Inventor
猪俣　誠
瀬戸　弘
晃理 中村
足立　健太郎
Original Assignee
日揮株式会社
株式会社セテック
日揮触媒化成株式会社
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Publication date
Application filed by 日揮株式会社, 株式会社セテック, 日揮触媒化成株式会社 filed Critical 日揮株式会社
Priority to PCT/JP2016/061736 priority Critical patent/WO2017179107A1/ja
Priority to CN201680067990.8A priority patent/CN108430604A/zh
Priority to JP2018511563A priority patent/JPWO2017179107A1/ja
Publication of WO2017179107A1 publication Critical patent/WO2017179107A1/ja

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    • 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
    • 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
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen oxides
    • 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
    • B01D53/81—Solid phase processes
    • B01D53/83—Solid phase processes with moving reactants
    • 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
    • B01D53/86—Catalytic processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/04—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of alkali metals, alkaline earth metals or magnesium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
    • B01J20/12—Naturally occurring clays or bleaching earth
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow

Definitions

  • the present invention relates to a technical field for removing air pollutants such as sulfur compounds, nitrogen compounds and soot contained in exhaust gas.
  • Sulfur oxides (SOx) and nitrogen oxides (NOx) are contained in exhaust gas discharged from thermal power plants, industrial boilers, cement kilns, and coke ovens using coal and heavy oil containing sulfur compounds and nitrogen compounds as fuel. It contains a lot of air pollutants such as firewood and is a source of environmental pollution such as acid rain, photochemical smog, and PM2.5.
  • an exhaust gas treatment system for removing air pollutants in the exhaust gas the exhaust gas is passed through a desulfurization device to remove SOx, and then the NOx removal device is passed through a NOx removal device.
  • Systems are known in which SOx is removed and then passed through a desulfurizer to remove SOx. The soot is removed by an electric dust collector installed in front of the desulfurization apparatus or denitration apparatus.
  • the temperature of the exhaust gas from a coke oven or the like is, for example, 250 ° C.
  • the temperature of the exhaust gas needs to be lowered to 100 ° C. or lower and then raised to a temperature suitable for the denitration reaction. For this reason, a plurality of heat exchangers are required, and a heat source is required for raising the temperature, so both the equipment cost and the operating cost are increased.
  • a material having high corrosion resistance must be used in order to prevent sulfuric acid corrosion from occurring in the heat exchanger, which also increases the cost.
  • semi-dry desulfurization requires the temperature of exhaust gas to be lower than 160 ° C.
  • Patent Document 1 describes a method for removing SOx from exhaust gas by allowing the exhaust gas to pass orthogonally to a moving bed composed of particles of a desulfurization agent that moves from top to bottom without using a bag filter. However, it does not describe the technique of the present invention.
  • the present invention has been made under such circumstances, and it is an object of the present invention to provide a technique capable of reducing facility costs and operation costs when removing sulfur oxides, nitrogen oxides, and soot in exhaust gas. .
  • the exhaust gas treatment system of the present invention is a system that performs desulfurization and dedusting on exhaust gas containing sulfur oxides, nitrogen oxides, and soot and having a temperature of 160 ° C. to 400 ° C., and then denitration, A dry desulfurization device for desulfurizing and dedusting the exhaust gas; A denitration device for performing denitration on the exhaust gas desulfurized by the desulfurization device,
  • the desulfurization apparatus includes a desulfurization tower and a supply unit for supplying a desulfurizing agent and particles constituting the moving bed into the desulfurization tower to form a downward flow of the desulfurization tower.
  • the gas velocity of the exhaust gas in the desulfurization tower is set to 0.2 to 1.2 m / s (seconds), and the space velocity is set to 300 to 1200 hr ⁇ 1 ((hour) ⁇ 1 ).
  • a temperature raising device is not provided in the exhaust gas flow path from the outlet of the desulfurization device to the inlet of the denitration device.
  • the desulfurizing agent for example, forms a moving layer as particles or exists as a powder in the particle gap forming the moving layer.
  • the present invention relates to a downflow of a desulfurizing agent and particles constituting a moving layer in a vertical duct in a dry desulfurization apparatus (the desulfurizing agent forms a moving layer as a particle or a moving layer).
  • the desulfurizing agent forms a moving layer as a particle or a moving layer.
  • Exhaust gas is brought into contact with the downflow in a crossflow manner.
  • the moving bed which consists of particle groups has a dust collection function between moving bed particles by optimizing a gas velocity, it can collect dust. Therefore, the moving bed can also serve as a dust removing device such as an electric dust collector required in the exhaust gas treatment device, and an electric dust collector and a bag filter are not necessary.
  • the desulfurization device in front of the denitration device, it is possible to remove dust from the exhaust gas. Therefore, it is possible to reduce clogging and wear due to soot in the honeycomb catalyst filled in the downstream denitration reactor. Further, since the diameter of the holes constituting the honeycomb catalyst can be reduced (the honeycomb holes are called cells and the number of cells is increased), it is possible to contribute to the reduction in the amount of catalyst filling and the extension of the life. .
  • FIG. 1 is a schematic diagram illustrating an overall configuration of an exhaust gas treatment system according to an embodiment of the present invention. It is explanatory drawing which shows the outline
  • Reference numeral 1 denotes a dry desulfurization apparatus.
  • Exhaust gas containing sulfur oxide (SOx), nitrogen oxide (NOx), and soot is supplied to the desulfurization apparatus 1, where SOx and soot are removed from the exhaust gas.
  • the exhaust gas include exhaust gas discharged from a thermal power plant, an industrial boiler, and a coke oven.
  • the speed of the gas passing through the moving bed of the desulfurization tower is 0.2 to 1.2 m / s (gas throughput (m 3 / s) / moving bed gas passage cross-sectional area ( m 2 )), more preferably 0.4 to 1.0 m / s, and the space velocity (SV) is 300 to 1,200 hr ⁇ 1 (gas throughput (m 3 / hr) / moving bed desulfurization tower). Volume (m 3 )).
  • the gas velocity can be set by dividing the gas flow rate by the size of the moving bed cross-sectional area through which the exhaust gas passes in a cross flow.
  • the space velocity can be set by changing the gas flow rate to the moving bed cross-sectional area x This can be done by dividing by the volume required by the depth.
  • a denitration device 2 is provided downstream of the desulfurization device 1.
  • the denitration device 2 includes a catalyst layer, and when ammonia gas and NOx in the exhaust gas pass through the catalyst layer, nitrogen and hydrogen are generated by a selective reduction reaction of NOx with NH 3 to remove NOx.
  • the exhaust gas flow path 11 located between the outlet of the desulfurization apparatus 1 and the inlet of the denitration apparatus 2 is not provided with a temperature increasing device such as a heat exchanger for increasing the temperature of the exhaust gas. Since the temperature of the exhaust gas supplied to the desulfurization apparatus 1 is normally 160 ° C. to 400 ° C., the exhaust gas leaves the desulfurization apparatus 1 while being maintained at this temperature and is supplied to the denitration apparatus 2.
  • the temperature of the exhaust gas supplied to the desulfurization apparatus 1 is more preferably 200 ° C. to 380 ° C.
  • a suitable temperature in the denitration apparatus 2 is 160 ° C. or higher, preferably 200 ° C. or higher. If the temperature is lower than this temperature, it becomes difficult to obtain high reaction efficiency, and the remaining S0x and NH 3 react to react with ammonium sulfate. Since it precipitates on the catalyst, the amount of the catalyst must be increased, which increases the catalyst cost.
  • the temperature of the exhaust gas is lowered at the front stage of the bag filter, and the exhaust gas emitted from the bag filter is further suitable for the denitration apparatus. The temperature must be raised to meet the temperature.
  • the desulfurization apparatus 1 since the desulfurization apparatus 1 has a dust collecting function as will be described later, it is not necessary to use a bag filter, the temperature of the exhaust gas is not lowered, the temperature is not raised, and the gas pressure loss is lost. Therefore, the exhaust gas from the exhaust gas source can be desulfurized and denitrated at the same temperature.
  • a heat exchanger 21 is provided at the subsequent stage of the denitration device 2, and the exhaust gas desulfurized and denitrated is cooled to, for example, 150 ° C. or less by the heat exchanger 21, and the chimney 23 is passed through the induction fan 22. To be discharged.
  • the desulfurization apparatus 1 includes a desulfurization tower for causing gas-solid reaction between the exhaust gas and the desulfurization agent particles.
  • the desulfurization tower has a lower side as shown in FIG.
  • the first chamber 3 corresponding to this area and the second chamber 4 corresponding to the upper area are provided.
  • the first chamber 3 is formed by the first duct 31, and the second chamber 4 is formed by the second duct 41.
  • the upper end portion of the first duct 31 and the lower end portion of the second duct 41 are connected by the connecting portion 5.
  • the first duct 31 and the second duct 41 correspond to the upper part and the lower part of the desulfurization tower, respectively.
  • the upper end portion of the first duct 31 and the lower end portion of the second duct 41 are connected by the connecting portion 5.
  • the granular material 100 When the granular material 100 is continuously supplied from the upper end of the second duct 41, a downward flow of the granular material 100 is formed from the second duct 41 to the first duct 31 due to the natural falling of the granular material 100.
  • the This downward flow can be called a moving bed because the group of the granular material 100 moves downward.
  • reference numeral 101 is assigned to the moving bed.
  • the granular material also serves as a desulfurizing agent (the desulfurizing agent forms a moving layer as particles), the granular material is inactive and the desulfurizing agent is supplied in powder form (the desulfurizing agent forms the moving layer)
  • the desulfurizing agent forms the moving layer
  • SOx in the exhaust gas reacts with calcium hydroxide in the desulfurizing agent and is fixed as calcium sulfate.
  • the exhaust gas rises and flows into the second duct 41 from the other side surface of the second duct 41, crosses the moving layer 101, and flows out from the one side surface. That is, if the exhaust gas flows in the second duct 41 so as to be orthogonal to the moving bed 101, a cross flow is formed.
  • the flue gas flowing out from the first duct 31 may be accompanied by a part of the powder as the desulfurization agent.
  • the powder is captured by the moving bed 101 and removed. Even when a part of the dust in the flue gas flows out without being captured by the moving layer 101 in the first duct 31, the dust is captured in the second duct 41. Therefore, the first duct 31 and the second duct 41 have a dust collecting function.
  • Each of the first duct 31 and the second duct 41 is configured as a structure in which flat rectangular tubes are arranged vertically as shown in FIG.
  • the heights H ⁇ b> 1 and H ⁇ b> 2 of the first duct 31 and the second duct 41 are set to the same dimension, for example, and the same is true for the widths W of the first duct 31 and the second duct 41.
  • the heights H1 and H2 and the widths W are not limited to being set to the same size, and may be set to different sizes.
  • the relationship between the thickness D1 of the first duct 31 and the thickness D2 of the second duct 41 is not particularly limited, but D2 is preferably the same as D1 or larger than D1.
  • connection part 5 is formed in a horizontally long inverted truncated pyramid shape.
  • the side surface group having the larger area is referred to as one side surface and the other side surface, as shown in FIG.
  • a plurality of inclined plates 61 constituting a louver are arranged in the vertical direction so as to extend across the entire width, that is, from end to end. Each of these inclined plates 61 is installed upward, and an exhaust gas passage is provided between the inclined plates 61 adjacent to each other vertically.
  • the other side surface (the side surface on the right side in FIG. 5) that is the outflow surface of the exhaust gas in the first duct 31 and the one side surface (the side surface on the left side in FIG. 5) that is the outflow surface of the exhaust gas in the second duct 41 are
  • a net 62 is provided along the outside of the inclined plate 61.
  • the net 62 is for preventing the moving layer 101 from flowing out of the ducts 31 and 41 on the flow of the exhaust gas
  • the void portion of the net 62 is a granular material constituting the moving layer 101 (hereinafter referred to as “moving for convenience”). It is set to be smaller than 100).
  • a grid screen may be used instead of the net.
  • the structure of the side surfaces of the first duct 31 and the second duct 41 is not limited to the structure in which the passage opening on the horizontally long slit is formed as shown in FIG.
  • the structure may be formed in a dispersed manner.
  • the hole formed in the side surface without using the net 62 may be set to a size that prevents the moving bed particles 100 from flowing out.
  • the exhaust gas flows from one side surface of the first duct 31 and flows out from the other side surface, then rises and flows in from the other side surface of the second duct 41 and flows out from the one side surface.
  • a flow path member 300 that forms a through flow path is provided around the first duct 31 and the second duct 41.
  • Reference numeral 301 denotes an exhaust gas inflow port, which is connected to an exhaust gas flow path from an exhaust gas source such as a thermal power plant.
  • An outflow port 302 corresponds to an outlet of the desulfurization apparatus 1 and is connected to a flow path for sending exhaust gas to the denitration apparatus 2.
  • 71 is a hopper that forms part of a desulfurizing agent supply unit for supplying a powdered desulfurizing agent into the connecting part 5
  • 71a is a valve for supplying and stopping the desulfurizing agent
  • 71b is a desulfurizing agent.
  • It is a supply pipe for the agent.
  • Reference numeral 72 denotes a hopper that forms part of a desulfurizing agent supply unit for supplying a powdery desulfurizing agent to the upper portion of the second duct 41
  • 72a denotes a valve for supplying and stopping the desulfurizing agent
  • 72b This is a desulfurization agent supply pipe.
  • a supply port 401 for supplying the moving bed particles 100 is provided at the upper end portion of the second duct 41, and a valve 402 for supplying and stopping the moving bed particles 100 is provided in the supply port.
  • a discharge port 403 that discharges the moving bed particles 100 is provided at the lower end of the first duct 31, and a valve 404 that opens and closes the discharge port 403 is provided at the discharge port 403.
  • the discharge port 403 and the valve 404 extend in the width direction of the first duct 31. Thereby, the uniformity of the density
  • a seal valve 405 having a sealing function is provided below the valve 404 in order to ensure the gas sealing performance inside the desulfurization apparatus 1.
  • the moving bed particle 100 As a form which supplies a desulfurization agent to the desulfurization tower 1, there exist both the case where a desulfurization agent serves as the moving bed particle 100, and the case where a desulfurization agent is supplied separately from the moving bed particle 100.
  • the moving bed particle 100 granular body
  • a mixture of calcium hydroxide, quick lime, coal ash, gypsum, or a used desulfurizing agent (calcium sulfate) is used.
  • a used desulfurizing agent calcium sulfate
  • coal ash clay minerals such as zeolite containing silica and alumina may be used.
  • the particle size of the moving bed particle 100 is set to, for example, the size of the particle size on the order of “mm”.
  • the shape of the moving bed particle 100 is not limited to a spherical shape, and may be a columnar shape.
  • exhaust gas from a thermal power plant or the like flows into the first duct 31 from the gap between the inflow port 301 and the inclined plate 61 on one side surface of the first duct 31.
  • the exhaust gas crosses the moving bed 101 of the powdered desulfurizing agent in the first duct 31, flows out from the gap between the inclined plates 61 on the other side, and rises along the flow path constituted by the flow path member 300. Then, it flows into the second duct 41 from the gap between the inclined plates 61 on the other side surface of the second duct 41.
  • the exhaust gas flowing into the second duct 41 crosses the moving bed 101 and flows out through the gap between the inclined plate 61 on one side and the outflow port 302. Is done.
  • the speed of the exhaust gas passing through the first duct 31 and the second duct 41 is set to, for example, 0.2 m / s to 1.2 m / s, and in this example, 1 m / s.
  • the SOx in the exhaust gas is absorbed by the calcium hydroxide desulfurization powder in the first duct 31 to become a calcium sulfate salt.
  • the operation of the desulfurization apparatus has been described for the case where the desulfurizing agent also serves as the moving bed particles 100.
  • the second duct 41 is provided in accordance with the particle size of the desulfurizing agent.
  • a method of selectively using the upper hopper 72 and the lower hopper 71 can be given.
  • the desulfurizing agent When the desulfurizing agent is separate from the moving bed particles 100, for example, calcium hydroxide powder having a particle size of 1 to 40 ⁇ m is used, but the particle size may be out of this range. The smaller the particle size of the desulfurizing agent, the shorter the reaction time can be. However, when the flue gas crosses the desulfurization tower 1, the desulfurizing agent may flow out to the outside through the net 62 along with the flue gas. There is. In this case, it is preferable to supply the desulfurizing agent from the lower hopper 71.
  • the reason for this is that even if the desulfurization agent flows out from the lower first duct 31 (first chamber 3), when the flue gas flows into the upper second duct 41, the desulfurization agent This is because it is captured by the moving layer 101. Therefore, it can be said that the first duct 31 (first chamber 3) functions as a reaction chamber, and the second duct 41 (second chamber 4) functions as a dust collection chamber. Whether or not it is preferable to supply the desulfurizing agent from the lower hopper 71 is determined by the balance between the particle size of the desulfurizing agent and the size of the hole of the net 62.
  • the particle size of the desulfurizing agent is For example, in the case of 40 ⁇ m or less, a mode in which the lower hopper 71 is used can be cited. Moreover, when the particle size of a desulfurization agent exceeds 40 micrometers, the aspect by which a powdery desulfurization agent is supplied to the upper end part of the 2nd duct 41 from the upper hopper 72 can be mentioned, for example.
  • the desulfurizing agent and the moving bed particle 100 are separate, a part of the powdery desulfurizing agent is interposed between the moving bed particles 101, but the powdery desulfurizing agent that is not interposed in the moving bed 101 is also used. Exists.
  • this desulfurizing agent is captured by the moving bed particles 101 when the exhaust gas moves sideways by the crossing flow, the powdery desulfurizing agent does not flow out of the second duct 41 at all or the outflow is suppressed as much as possible. It is done.
  • the direction of the exhaust gas flow across the first duct 31 and the direction of the exhaust gas flow across the second duct 41 are opposite, but they are configured to be in the same direction. Also good.
  • a desulfurizing agent is conveyed to the upper part of the other duct on the rear stage side, and It is necessary to convey the desulfurizing agent discharged from the lower side of the other duct to the upper part of one duct on the front stage side by, for example, a belt conveyor.
  • the exhaust gas is allowed to pass through the first duct 31 that is the lower side of the desulfurization tower, and then the second duct 41 that is the upper side of the desulfurization tower.
  • the degree of reduction in the desulfurization performance of the desulfurizing agent is smaller as it is closer to the outflow port 302.
  • the desulfurization performance is higher than a method in which the two ducts 31 and 41 are arranged side by side and the exhaust gas is crossed in the order of the one duct 31 and the other duct 41.
  • the denitration apparatus 2 will be described.
  • the denitration device 2 is configured such that exhaust gas flows in from, for example, an upper part of a vertical duct (tower) and flows out from the lower part, and a plurality of catalyst layers are provided at intervals in the middle of the duct.
  • a catalyst used for the catalyst layer for example, at least one component of oxides of V (vanadium), Si (silicon), Mn (manganese), W (tungsten), and Mo (molybdenum) and Ti (titanium) are used.
  • a composite oxide formed into a honeycomb shape, a plate shape, or a particle shape can be used.
  • a denitration catalyst it is not restricted to the catalyst described here, You may use another catalyst.
  • the amount of catalyst is suppressed. More specifically, it is preferable that the hole diameter is 3.2 mm or less, so that the amount of catalyst can be reduced and the life can be extended.
  • Ammonia necessary for NOx removal is supplied to the exhaust gas flow path upstream of the inflow port 301 shown in FIG. 5 in order to make the mixing of the exhaust gas and ammonia uniform. Alternatively, it may be supplied to the flow path 11 (see FIG. 1) between the desulfurization apparatus 1 and the denitration apparatus 2.
  • ammonia may be supplied from both the exhaust gas flow path and the flow path 11 in the preceding stage of the desulfurization apparatus 1.
  • the supply amount of ammonia is preferably set so that the molar ratio of ammonia to nitrogen oxide (ammonia / nitrogen oxide) in the exhaust gas at the inlet of the denitration apparatus 2 is 0.7 to 1.2. More preferably, it is set to be 9 to 1.0.
  • an ammonia supply unit for supplying ammonia is not shown, a flow rate adjusting unit is provided in an ammonia supply pipe having one end connected to an ammonia supply source, and the other end of the ammonia supply pipe is connected to, for example, the flow path 11. it can.
  • the exhaust gas flowing out from the desulfurization apparatus 1 is sent to the denitration apparatus 2 as it is, the exhaust gas flowing into the denitration apparatus 2 is maintained at a temperature of, for example, 160 to 400 ° C. Therefore, when passing through the catalyst layer, NOx in the exhaust gas Is converted to N 2 (nitrogen) and H 2 O (water) by selective catalytic reduction with NH 3 .
  • ammonia is supplied at the front stage of the desulfurization apparatus 1, the following advantages are obtained. That is, since the opportunity for ammonia to be dispersed in the piping and the packed bed in the desulfurization apparatus 1 before reaching the denitration apparatus increases, the dispersion of ammonia in the gas is larger than when ammonia is supplied before the denitration apparatus. Increases nature. For this reason, the shape of the piping and the structure of the ammonia disperser before being introduced into the denitration apparatus are simplified, and the distance from the disperser to the catalyst layer can be shortened.
  • the desulfurization apparatus is installed in the front stage, the denitration apparatus is installed in the rear stage, and the desulfurization apparatus 1 is provided with a dust collecting function. Therefore, it is not necessary to use a bag filter before the denitration apparatus, and the exhaust gas
  • the exhaust gas from the exhaust gas source such as a thermal power plant can be desulfurized and denitrated at the same temperature without performing the temperature lowering and temperature raising operations. Therefore, the equipment cost and operation cost can be kept low.
  • the denitration catalyst can reduce the hole diameter of the honeycomb, for example, to 3.2 mm or less, the apparatus becomes compact, and the equipment cost and operation cost can be suppressed.
  • the shape of the first duct 31 and the second duct 41 is not limited to a rectangular tube shape, and may be a cylindrical shape.
  • the powdery desulfurizing agent may be supplied from the upper part of the second duct 41 with the moving bed particles 100 interposed in advance.
  • the desulfurization tower constituting the desulfurization apparatus is not limited to the two-stage configuration with the first duct 31 and the second duct 41 as described above.
  • the desulfurization tower is configured by a single-stage duct.
  • the moving bed particles 100 preliminarily containing the agent or the moving bed particles 100 (moving bed particles also serving as the desulfurizing agent) composed of the desulfurizing agent may be supplied to form a downward flow.
  • the exhaust gas may be passed from one side surface of the duct to the other side surface, and the passed exhaust gas may be sent to the denitration device 2.
  • a bag filter is not necessary, and the same effect as the above-described embodiment is obtained.
  • two ducts (desulfurization towers) are arranged side by side, and in each duct, a powdery desulfurizing agent is previously interposed in the moving bed particles, and these are supplied from the top, or a moving bed that also serves as a desulfurizing agent.
  • a powdery desulfurizing agent is previously interposed in the moving bed particles, and these are supplied from the top, or a moving bed that also serves as a desulfurizing agent.
  • the moving bed particles 100 also used as the desulfurizing agent, a mixture of slaked lime or quick lime, coal ash, and a used desulfurizing agent, for example, these are kneaded with water, molded, cured, and dried. Can be used. Or what mixed slaked lime, coal ash, and clay minerals, such as a zeolite, can be used. In this case, the moving bed particles 100 may be columnar or spherical.
  • the desulfurizing agent can be a fine particle of the above desulfurizing agent or a fine particle of slaked lime having a size of several ⁇ m to several hundred ⁇ m.
  • Example 1 As the desulfurization apparatus, a structure was used in which moving bed particles also serving as a desulfurization agent were supplied from the upper part of a single-stage duct (desulfurization tower) to form a downward flow.
  • a columnar (6 mm ⁇ ⁇ 10 mm) extruded molded product having a composition of 40% by weight of slaked lime, 30% by weight of coal ash, and 30% by weight of a used desulfurizing agent (CaSO 4 ) was used.
  • the SOx in the exhaust gas at the outlet of the desulfurization tower is 42 ppm and the dust is 4 mg / Nm 3.
  • a honeycomb structure (45 cells ⁇ 45 cells, hole diameter: 2.78 mm) formed by composite oxide of V 2 O 5 and TiO 2 is arranged in the denitration tower to form a catalyst layer, and SV is 8300 hr ⁇
  • Two catalyst layers are provided on the upper and lower sides so as to be 1 (amount of catalyst: 13.25 m 3 ).
  • the NOx concentration in the exhaust gas at the exit of the denitration tower was 82 ppm.
  • the inlet gas temperature to the desulfurization tower is 220 ° C.
  • SOx in the exhaust gas at the outlet of the desulfurization tower is 15 ppm, NOx is 560 ppm, and dust is 2 mg / Nm3.
  • This exhaust gas is introduced into the denitration tower at 220 ° C.
  • a honeycomb structure (45 cells ⁇ 45 cells, hole diameter: 2.78 mm) is arranged in the denitration tower to form a catalyst layer, and the catalyst layer is set so that SV becomes 4970 hr ⁇ 1 (catalyst amount: 11.07 m 3 ). Are provided in two layers.
  • the NOx concentration in the exhaust gas at the exit of the denitration tower was 35 ppm.
  • Example 3 An annular portion of a double cylindrical container having an inner cylinder of 11 cm, an outer cylinder of 23.5 cm, and a height of 20 cm is filled with a desulfurization agent having a particle diameter of 2 mm, and dust having a particle diameter of 5 ⁇ m is contained from the inside of the double cylinder (concentration of 0.1 ⁇ m). 4 to 1.2 g / Nm 3 ) was allowed to flow and the dust collection efficiency was measured.
  • the gas velocity (the gas velocity at the inner cylinder inlet / the gas velocity at the outer cylinder outlet) was set in the following seven ways.
  • the unit of gas velocity is m / s.
  • Test Example 1 0.2 / 0.094 Test Example 2: 0.4 / 0.19 Test Example 3: 0.6 / 0.28 Test Example 4: 0.8 / 0.37 Test Example 5: 1.0 / 0.52 Test Example 6: 1.2 / 0.56 Test Example 7: 1.6 / 0.74
  • Test Example 1 Test 2 Test 3 Test 4 Test 5 Test 6 Test 7 Dust collection efficiency (%) 97.5 96.6 94.3 91.5 90.3 87.5 81.0 When the gas velocity increases, re-scattering due to the fluid drag force of the gas is likely to occur, and the dust collection efficiency is less than 90% from around 1.2 m / s.
  • the gas velocity is set to 0.2 to 1.2 m / s, and more preferably 0.4 to 1.0 m / s.
PCT/JP2016/061736 2016-04-11 2016-04-11 排ガスの処理システム WO2017179107A1 (ja)

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CN111871202A (zh) * 2020-07-14 2020-11-03 倪文利 一种船舶柴油机废气处理装置
CN113058427A (zh) * 2021-03-01 2021-07-02 安徽紫朔环境工程技术有限公司 一种电厂脱硫脱硝一体化设备
WO2022247372A1 (zh) * 2021-05-27 2022-12-01 江苏峰业科技环保集团股份有限公司 一种高效sds干法脱硫装置

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