WO2017022522A1 - Coal-fired power generation equipment - Google Patents

Coal-fired power generation equipment Download PDF

Info

Publication number
WO2017022522A1
WO2017022522A1 PCT/JP2016/071553 JP2016071553W WO2017022522A1 WO 2017022522 A1 WO2017022522 A1 WO 2017022522A1 JP 2016071553 W JP2016071553 W JP 2016071553W WO 2017022522 A1 WO2017022522 A1 WO 2017022522A1
Authority
WO
WIPO (PCT)
Prior art keywords
coal
denitration
exhaust gas
discharge
power generation
Prior art date
Application number
PCT/JP2016/071553
Other languages
French (fr)
Japanese (ja)
Inventor
敏和 吉河
健治 引野
啓一郎 盛田
Original Assignee
中国電力株式会社
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
Priority to JP2015-152882 priority Critical
Priority to JP2015152882 priority
Application filed by 中国電力株式会社 filed Critical 中国電力株式会社
Publication of WO2017022522A1 publication Critical patent/WO2017022522A1/en

Links

Images

Classifications

    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • B01D53/90Injecting reactants
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00Arrangements of devices for treating smoke or fumes
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02CCAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00Capture or disposal of greenhouse gases
    • Y02C20/10Capture or disposal of greenhouse gases of nitrous oxide (N2O)

Abstract

The present invention provides coal-fired power generation equipment that makes it possible to minimize the degradation of a denitration catalyst by preventing the surface of the denitration catalyst from becoming coated with sediment having an extremely small particle size. The coal-fired power generation equipment 1 is provided with: a coal pulverizer 30 that pulverizes coal in order to produce pulverized coal; a combustion boiler 40 that burns the pulverized coal produced in the coal pulverizer 30; a denitration device 60 that is arranged downstream from the combustion boiler 40 and that removes nitrogen oxides included in exhaust gas generated when the pulverized coal is burned in the combustion boiler 40; a discharge device 10 that is arranged upstream from the denitration device 60 and that negatively or positively charges coal ash included in the exhaust gas; and a charging device 15 that charges the denitration device 60 to the same polarity as the coal ash.

Description

Coal-fired power generation facility

The present invention relates to a coal-fired power generation facility. More specifically, the present invention relates to a coal-fired power generation facility that can suppress deterioration of a denitration catalyst that constitutes a denitration apparatus.

In coal-fired power plants, nitrogen oxides are generated as coal is burned, but it is necessary to keep nitrogen oxide emissions below a certain level by the Air Pollution Control Law and other standards. Therefore, denitration equipment is installed at power plants to reduce and decompose nitrogen oxides. In this denitration apparatus, a denitration catalyst containing an active component such as vanadium pentoxide is disposed, and denitration is realized by a reduction reaction at a high temperature by coexisting ammonia therein.

Since this denitration catalyst generally operates efficiently in a high temperature atmosphere of 300 ° C. to 400 ° C., it is necessary to denitrate exhaust gas containing a large amount of soot immediately after burning coal in a boiler. In order to maintain the performance of the denitration apparatus, it is necessary to replace or regenerate a catalyst whose activity has decreased with a new catalyst.

For example, the following Patent Document 1 discloses a method for replacing a denitration catalyst of a flue gas denitration apparatus filled with a plurality of stages of denitration catalysts, and a catalyst removal step of taking out a first-stage denitration catalyst located on the most upstream side. And a catalyst moving step for sequentially moving all the denitration catalysts in the second and subsequent stages to the upstream side of the first stage, and a catalyst for replenishing a new denitration catalyst in the most downstream stage that has been emptied through the catalyst moving process And a replenishment step. A method for replacing the denitration catalyst is disclosed.

JP 2013-052335 A

However, in the first place, there is no knowledge in the past regarding when to replace or regenerate the denitration catalyst. For this reason, the present situation is that the exhaust gas measurement at the site or the catalyst sample is actually collected and the catalyst performance test is carried out to measure the decrease in the denitration rate. Decreasing the function of denitration catalysts in the operation of coal-fired power plants gradually progresses over a long period of time, so it is extremely important to clarify this deterioration mechanism in order to predict deterioration and take measures to suppress deterioration. It is.

As a result of intensive investigations on the deterioration mechanism of the denitration catalyst, the present inventors have found that a deposit having a particle size far smaller than the conventional coal ash particle size range of several tens to hundreds of μm or less is a denitration catalyst. It was found that the surface of the catalyst was coated to form a coating layer, whereby contact between the denitration catalyst and the exhaust gas was hindered and the performance of the denitration catalyst was lowered.

Therefore, an object of the present invention is to provide a coal-fired power generation facility capable of suppressing deterioration of a denitration catalyst by preventing deposits having a small particle diameter from covering the surface of the denitration catalyst.

The present invention includes a pulverized coal machine that pulverizes coal to produce pulverized coal, a combustion boiler that burns the pulverized coal produced in the pulverized coal machine, and a pulverized powder disposed in a downstream side of the combustion boiler. A denitration device that removes nitrogen oxides contained in the exhaust gas generated by combustion of charcoal, a discharge device that is disposed upstream of the denitration device and charges coal ash contained in the exhaust gas to a positive electrode or a negative electrode, and the denitration device The present invention relates to a coal-fired power generation facility including a charging device that charges the device with the same polarity as coal ash.

The discharge device preferably includes a discharge electrode and a charging unit that applies a high voltage to the discharge electrode, and the corona discharge is generated from the discharge electrode to charge the coal ash to the positive electrode or the negative electrode. .

The coal-fired power generation facility further includes a rectifying plate that is arranged upstream of the denitration device and rectifies the exhaust gas introduced into the denitration device. It is preferable.

In addition, the denitration apparatus includes a cylindrical casing having conductivity, and a plurality of honeycomb catalysts accommodated in the casing, and a plurality of elongated plurality of exhaust gas circulation holes extending in a longitudinal direction. A honeycomb catalyst, and a sealing member disposed between the honeycomb catalysts disposed adjacent to each other in the lateral direction to prevent inflow of exhaust gas, wherein the plurality of honeycomb catalysts include a conductive carrier and the conductive carrier. It is preferable that the sealing member has conductivity.

According to the present invention, it is possible to provide a coal-fired power generation facility capable of suppressing deterioration of a denitration catalyst by preventing deposits having a small particle diameter from covering the surface of the denitration catalyst.

It is a figure which shows the structure of the coal thermal power generation equipment which concerns on one Embodiment of this invention. It is a figure which expands and shows the vicinity of the combustion boiler shown in FIG. It is a figure which expands and shows the vicinity of the denitration apparatus shown in FIG. It is a figure which shows typically the structure of the denitration catalyst layer which comprises a denitration apparatus.

Hereinafter, a preferred embodiment of a coal-fired power generation facility of the present invention will be described with reference to the drawings.
As shown in FIG. 1, the coal-fired power generation facility 1 of the present embodiment is provided on the downstream side of the coal bunker 20, the coal feeder 25, the pulverized coal machine 30, the combustion boiler 40, and the combustion boiler 40. Exhaust passage 50, denitration device 60, discharge device 10, charging device 15, air preheater 70, electrostatic precipitator 90, gas heater (for heat recovery) 80, induction fan 210, desulfurization provided in exhaust passage 50 The apparatus 220, the gas heater (for reheating) 230, the desulfurization ventilator 240, and the chimney 250 are provided.

The coal bunker 20 stores coal supplied from a coal silo (not shown) by a coal transportation facility. The coal feeder 25 supplies the coal supplied from the coal bunker 20 to the pulverized coal machine 30 at a predetermined supply speed.
The pulverized coal machine 30 pulverizes the coal supplied from the coal feeder 25 to produce pulverized coal. In the pulverized coal machine 30, the coal is pulverized to an average particle size of 60 μm to 80 μm. The particle size distribution of pulverized coal is about 10 to 15% at 150 μm or more, 30 to 40% at 75 to 150 μm, and 45 to 60% at less than 75 μm.
As the pulverized coal machine 30, a roller mill, a tube mill, a ball mill, a beater mill, an impeller mill, or the like is used.

The combustion boiler 40 burns the pulverized coal supplied from the pulverized coal machine 30 together with the forcibly supplied air. By burning pulverized coal, coal ash such as clinker ash and fly ash is generated and exhaust gas is generated.
In addition, clinker ash means the massive coal ash which fell to the bottom part of the combustion boiler 40 among the coal ash generate | occur | produced when pulverized coal is burned. Fly ash has a particle size (particle size of about 200 μm or less) of coal ash generated when pulverized coal is burned and blown up with combustion gas (exhaust gas) and circulated to the exhaust passage 50 side. Spherical coal ash.

The combustion boiler 40 will be described in detail with reference to FIG. 2. In FIG. 2, the combustion boiler 40 has a substantially inverted U shape as a whole, and the exhaust gas (combustion gas) is inverted U-shaped along the arrow in the figure. After passing through the secondary economizer 41e, it is again reversed into a U-shape.

Below the combustion boiler 40, a burner 41a for burning pulverized coal is disposed in the vicinity of the burner zone 41a 'inside the combustion boiler 40. Moreover, the 1st superheater 41b is arrange | positioned near the U-shaped top part inside the combustion boiler 40, and also the 2nd superheater 41c is arrange | positioned from there. Furthermore, from the vicinity of the terminal end of the second superheater 41c, a primary economizer 41d and a secondary economizer 41e are provided in two stages. Here, the economizer (also referred to as ECO) is a heat transfer surface group provided for preheating boiler feedwater using heat retained by exhaust gas.

According to the above combustion boiler 40, pulverized coal is burned in the burner zone 41a '. The combustion temperature of the pulverized coal ranges from 1300 ° C. to 1500 ° C., and the coal ash generated by the combustion rises along the direction of the arrow and together with the exhaust gas, the first superheater 41b, the second superheater 41c, The next economizer 41d and the secondary economizer 41e are sequentially passed. The combustion gas exchanges heat by passing through a heat transfer surface group provided for preheating boiler feed water, and the temperature is lowered to about 450 ° C. to 500 ° C. The time required for the exhaust gas to reach the economizer from the burner zone 41a 'is approximately 5 to 10 seconds.

The exhaust passage 50 is arranged on the downstream side of the combustion boiler 40 and distributes the exhaust gas generated in the combustion boiler 40 and the generated coal ash. In the exhaust passage 50, as described above, the denitration device 60, the discharge device 10, the charging device 15, the air preheater 70, the gas heater (for heat recovery) 80, the electric dust collector 90, the induction ventilator 210, the desulfurization device. 220, a gas heater (for reheating) 230, a desulfurization ventilator 240, and a chimney 250 are arranged.

The denitration device 60 removes nitrogen oxides in the exhaust gas. In the present embodiment, the denitration device 60 injects ammonia gas as a reducing agent into the exhaust gas at a relatively high temperature (300 ° C. to 400 ° C.), and the action of the denitration catalyst converts nitrogen oxides in the exhaust gas into harmless nitrogen. Nitrogen oxides in the exhaust gas are removed by a so-called dry ammonia catalytic reduction method that decomposes into water vapor.

As shown in FIG. 3, the denitration apparatus 60 includes a denitration reactor 61, a plurality of stages of denitration catalyst layers 62, 62, 62 disposed inside the denitration reactor 61, and upstream of the denitration catalyst layer 62. A rectifying layer 63 to be disposed, a rectifying plate 64 disposed in the vicinity of the inlet of the denitration reactor 61, and an ammonia injection portion 65 disposed on the upstream side of the denitration reactor 61 are provided.

The denitration reactor 61 is a place for denitration reaction in the denitration apparatus 60.
The denitration catalyst layer 62 is disposed in the denitration reactor 61 in a plurality of stages (three stages in this embodiment) at predetermined intervals along the exhaust gas flow path.

As shown in FIG. 4, the denitration catalyst layer 62 includes a plurality of honeycomb catalysts 622 as denitration catalysts. More specifically, the denitration catalyst layer 62 includes a plurality of casings 621, a plurality of honeycomb catalysts 622 accommodated in the plurality of casings 621, and a seal member 623.

The casing 621 is made of a rectangular tube-shaped metal member having one end and the other end opened. The casing 621 is arranged so that one end and the other end opened face the exhaust gas flow path in the denitration reactor 61, that is, the exhaust gas flows through the inside of the casing 621. The plurality of casings 621 are connected and arranged so as to be in contact with each other so as to block the exhaust gas flow path in the denitration reactor 61.

The honeycomb catalyst 622 is formed in a long shape (a rectangular parallelepiped shape) in which a plurality of exhaust gas circulation holes 624 extending in the longitudinal direction are formed. The plurality of honeycomb catalysts 622 are arranged so that the direction in which the exhaust gas circulation holes 624 extend is along the flow path of the exhaust gas. In the present embodiment, the plurality of honeycomb catalysts 622 are disposed inside the denitration reactor 61 while being accommodated in the casing 621.
In the present embodiment, the honeycomb catalyst 622 is formed by extruding after supporting a catalytic material such as vanadium or tungsten on a conductive carrier. The conductive carrier can be constituted by mixing a conductive material such as a metal fiber, carbon black, or a metal with a ceramic material such as titanium oxide or zirconium oxide.

The seal member 623 is arranged between the honeycomb catalysts 622 arranged adjacent to each other in the lateral direction, and prevents the exhaust gas from flowing into the gap between the honeycomb catalysts 622 arranged adjacent to each other. In the present embodiment, the sealing member 623 is configured by a sheet-like member having conductivity, and is formed in a portion of a predetermined length (for example, 150 mm from the end portion) on one end side and the other end side in the longitudinal direction of the honeycomb catalyst 622. It is wrapped around.

As the seal member 623, ceramic paper configured by mixing inorganic fibers mainly composed of alumina or silica and a binder having conductive fibers and conductive fillers can be used.

In the above-described denitration catalyst layer 62, as the honeycomb catalyst 622, for example, a catalyst having a rectangular parallelepiped shape of 150 mm × 150 mm × 860 mm and 400 exhaust gas circulation holes (20 × 20) having openings of 6 mm × 6 mm is used. Further, as the casing 621, a casing that can accommodate 72 honeycomb catalysts 622 (length 6 × width 12) is used. In addition, 120 to 150 casings 621 are used for one denitration catalyst layer 62. In other words, 9000 to 10,000 honeycomb catalysts 622 are installed in one denitration catalyst layer 62.

The rectifying layer 63 is disposed on the upstream side of the denitration catalyst layer 62. The rectifying layer 63 is composed of a metal member or the like having a plurality of openings formed in a lattice shape, and partitions the exhaust gas flow path in the denitration reactor 61. The rectifying layer 63 rectifies the exhaust gas introduced through the exhaust passage 50 and introduced into the denitration reactor 61, and uniformly guides it to the denitration catalyst layer 62.

The rectifying plate 64 is disposed on the upstream side of the rectifying layer 63 in the vicinity of the inlet of the denitration reactor 61. More specifically, the rectifying plate 64 is disposed at a bent portion of the inner wall of the denitration reactor 61 or the exhaust passage 50 and protrudes from the inner wall to the inner surface side. The rectifying plate 64 adjusts the flow of exhaust gas at the bent portion of the exhaust passage 50 or the denitration reactor 61.

The ammonia injection part 65 is arranged upstream of the denitration reactor 61 and injects ammonia into the exhaust passage 50.

The discharge device 10 is disposed on the upstream side of the denitration device 60, and charges the coal ash contained in the exhaust gas to the positive electrode or the negative electrode. Specifically, the discharge device 10 charges the coal ash contained in the exhaust gas to the same polarity as the denitration device 60 (honeycomb catalyst 622). The discharge device 10 includes a discharge electrode 12 and a charging unit 11. The discharge electrode 12 includes a positive electrode and a negative electrode, and is disposed on the inner surface of the exhaust passage 50 or the denitration reactor 61. In the present embodiment, the discharge electrode 12 is constituted by a rectifying plate 64.
The charging unit 11 applies a high voltage to the discharge electrode 12 (rectifying plate 64).

According to the above discharge device 10, corona discharge is generated from the positive electrode or the negative electrode of the discharge electrode 12 (rectifier plate 64) by applying a high voltage to the discharge electrode 12 (rectifier plate 64) by the charging unit 11. . When corona discharge is generated from the positive electrode of the discharge electrode 12, positive ions are generated. On the other hand, when corona discharge is generated from the negative electrode of the discharge electrode 12, negative ions are generated.
When corona discharge occurs from the positive electrode of the discharge electrode 12 (rectifying plate 64), the coal ash introduced into the denitration device 60 is charged to the positive electrode. On the other hand, when corona discharge is generated from the negative electrode of the discharge electrode 12 (rectifying plate 64), the coal ash introduced into the denitration device 60 is charged to the negative electrode. Thus, the coal ash passing through the discharge electrode 12 (rectifying plate 64) is charged to the positive electrode or the negative electrode and introduced into the denitration device 60 (denitration catalyst layer 62).

The charging device 15 is connected to the denitration device 60 and charges the denitration device 60 to the same polarity as the coal ash. In the present embodiment, the charging device 15 is connected to the denitration catalyst layers 62, 62, 62, respectively, and charges the denitration catalyst layer 62 to the same polarity (positive electrode or negative electrode) as the coal ash. Here, in the present embodiment, the casing 621, the honeycomb catalyst 622, and the seal member 623 constituting the denitration catalyst layer 62 are all configured to have conductivity. Thereby, the denitration catalyst layer 62 is charged to the same polarity (positive electrode or negative electrode) as the coal ash.

Coal ash contained in the exhaust gas is easily charged on the negative electrode (not easily charged on the positive electrode). From such a viewpoint, it is preferable that the discharge device 10 charges the coal ash, and the charging device 15 charges the denitration catalyst layer 62 to the negative electrode. Thereby, the denitration apparatus 60 (denitration catalyst layer 62) can be efficiently charged to the same polarity as coal ash.
On the other hand, the denitration catalyst layer 62 in the denitration apparatus 60 (denitration reactor 61) is easily charged to the positive electrode (not easily charged to the negative electrode). From such a viewpoint, it is preferable that the discharge device 10 charges the coal ash, and the charging device 15 charges the denitration catalyst layer 62 to the positive electrode. Thereby, the denitration apparatus 60 (denitration catalyst layer 62) can be efficiently charged to the same polarity as coal ash.

According to the denitration device 60, the discharge device 10, and the charging device 15 described above, first, ammonia is injected into the high-temperature exhaust gas (300 ° C. to 400 ° C.) flowing through the exhaust passage 50 in the ammonia injection section 65. The exhaust gas into which ammonia has been injected is rectified by the rectifying plate 64 and the rectifying layer 63.
Here, the coal ash passing through the rectifying plate 64 is charged to the positive electrode or the negative electrode by corona discharge generated from the rectifying plate 64. Then, the coal ash charged on the positive electrode or the negative electrode is introduced into the denitration device 60 (denitration catalyst layer 62).

In the denitration catalyst layer 62, when the exhaust gas containing ammonia passes through the exhaust gas circulation hole 624 of the honeycomb catalyst 622, nitrogen oxide and ammonia react according to the following chemical reaction formula, and decompose into harmless nitrogen and water vapor. Is done.
4NO + 4NH 3 + O 2 → 4N 2 + 6H 2 O
NO + NO 2 + 2NH 3 → 2N 2 + 3H 2 O

By the way, the denitration catalyst is deteriorated by use and the denitration rate is lowered. Causes of deterioration of the denitration catalyst include thermal deterioration such as sintering, chemical deterioration due to poisoning of catalyst components, and physical deterioration due to the coal ash covering the catalyst surface. The present inventors now have a much smaller particle size (1 μm or less, more specifically about several tens of nm) compared to the average particle size of coal ash, which is about several tens μm to one hundred μm. It has been found that deposits resulting from coal ash cover the surface of the denitration catalyst to form a coating layer, thereby inhibiting the contact between the denitration catalyst and the exhaust gas and reducing the performance of the denitration catalyst. Since the coal ash having such a small particle size has a small content, it has not been considered as a cause of deterioration of the denitration catalyst.

Here, in this embodiment, the denitration catalyst layer 62 is charged to the positive electrode or the negative electrode by the charging device 15. Thereby, since the coal ash charged to the positive electrode or the negative electrode and the honeycomb catalyst 622 are charged to the same polarity by the discharge device 10, when the exhaust gas containing coal ash passes through the exhaust gas circulation hole 624 of the honeycomb catalyst 622, It is possible to prevent ash (particularly, fine coal ash on which electric force easily acts) from being electrically attached to the surface of the honeycomb catalyst 622. Therefore, since it is possible to prevent the coating layer due to the fine coal ash from being formed on the surface of the honeycomb catalyst 622 (denitration catalyst), deterioration of the honeycomb catalyst can be suppressed.

The air preheater 70 is disposed downstream of the denitration device 60 in the exhaust passage 50. The air preheater 70 exchanges heat between the exhaust gas that has passed through the denitration device 60 and the combustion air sent from the push-in type ventilator 75 to cool the exhaust gas and heat the combustion air.

The gas heater 80 is disposed downstream of the air preheater 70 in the exhaust passage 50. The exhaust gas recovered by the air preheater 70 is supplied to the gas heater 80. The gas heater 80 further recovers heat from the exhaust gas.

The electrostatic precipitator 90 is disposed on the downstream side of the gas heater 80 in the exhaust passage 50. The exhaust gas recovered in the gas heater 80 is supplied to the electric dust collector 90. The electric dust collector 90 is a device that collects coal ash (fly ash) in exhaust gas by applying a voltage to electrodes. The fly ash collected by the electric dust collector 90 is collected by the fly ash collection device 120.

The induction ventilator 210 is disposed on the downstream side of the electric dust collector 90 in the exhaust passage 50. The induction ventilator 210 takes in the exhaust gas from which fly ash has been removed in the electrostatic precipitator 90 from the primary side and sends it to the secondary side.

The desulfurization device 220 is arranged on the downstream side of the induction fan 210 in the exhaust passage 50. The desulfurization apparatus 220 is supplied with exhaust gas sent from the induction fan 210. The desulfurization apparatus 220 sprays a mixed liquid of limestone and water on the exhaust gas, thereby absorbing the sulfur oxide contained in the exhaust gas into the mixed liquid to generate a desulfurized gypsum slurry, and dehydrating the desulfurized gypsum slurry. This produces desulfurized gypsum. The desulfurized gypsum generated in the desulfurization apparatus 220 is recovered by a desulfurization gypsum recovery apparatus 222 connected to this apparatus.

The gas heater 230 is disposed downstream of the desulfurization device 220 in the exhaust passage 50. The gas heater 230 is supplied with exhaust gas from which sulfur oxides have been removed in the desulfurization apparatus 220. The gas heater 230 heats the exhaust gas. The gas heater 80 and the gas heater 230 are disposed between the exhaust gas flowing between the air preheater 70 and the electric dust collector 90 and the exhaust gas flowing between the desulfurization device 220 and the desulfurization ventilator 240 in the exhaust passage 50. It may be configured as a gas heater that performs heat exchange.

The desulfurization ventilator 240 is disposed downstream of the gas heater 230 in the exhaust passage 50. The desulfurization ventilator 240 takes in the exhaust gas heated in the gas heater 230 from the primary side and sends it to the secondary side.
The chimney 250 is arranged on the downstream side of the desulfurization ventilator 240 in the exhaust passage 50. Exhaust gas heated by the gas heater 230 is introduced into the chimney 250. The chimney 250 discharges exhaust gas.

According to the coal-fired power generation facility 1 of the present embodiment described above, the following effects are obtained.

(1) Discharge device 10 for charging coal-fired power generation facility 1 upstream of denitration device 60 and charging coal ash contained in exhaust gas to the positive electrode or the negative electrode, and charging for charging denitration device 60 to the same polarity as coal ash And a device. Thereby, since the coal ash introduced into the denitration device 60 and the denitration device 60 (honeycomb catalyst 622) are charged with the same polarity, the exhaust gas containing coal ash passes through the exhaust gas circulation hole 624 of the honeycomb catalyst 622. Occasionally, coal ash (particularly, fine coal ash on which electric force is easily applied) can be prevented from being electrically attached to the surface of the honeycomb catalyst 622. Therefore, it is possible to prevent the coating layer due to the fine coal ash from being formed on the surface of the honeycomb catalyst 622, so that deterioration of the honeycomb catalyst 622 can be suppressed.

(2) The discharge device 10 includes the discharge electrode 12 and the charging unit 11 that applies a high voltage to the discharge electrode 12, and generates corona discharge from the discharge electrode 12 to generate coal ash as a positive electrode or The negative electrode was charged. Thereby, coal ash can be easily charged using the technique used in the electrostatic precipitator 90.

(3) The discharge electrode 12 of the discharge device 10 is constituted by a rectifying plate 64. As a result, the coal ash contained in the exhaust gas can be charged using the member that adjusts the flow of the exhaust gas introduced into the denitration catalyst layer 62, so that the coal ash contained in the exhaust gas can be effectively charged.

(4) The denitration device 60 includes a casing 621, a honeycomb catalyst 622, and a seal member 623, and the casing 621, the honeycomb catalyst 622, and the seal member 623 are all configured to have conductivity. did. Thereby, the honeycomb catalyst 622 can be charged appropriately. Therefore, since it can prevent more effectively that the coating layer resulting from a fine coal ash is formed in the surface of the honeycomb catalyst 622, deterioration of the honeycomb catalyst 622 can be suppressed more.

The preferred embodiment of the coal-fired power generation facility 1 of the present invention has been described above. However, the present invention is not limited to the above-described embodiment, and can be appropriately changed.
For example, in this embodiment, a honeycomb catalyst is used as the denitration catalyst, but the present invention is not limited to this. That is, as the denitration catalyst, a plate catalyst configured by applying a catalyst substance on the surface of a net-like substrate may be used.

Further, in this embodiment, the discharge electrode 12 of the discharge device 10 is configured by the rectifying plate 64, but is not limited thereto. That is, the discharge electrode may be constituted by a rectifying layer. Moreover, you may arrange | position a discharge electrode separately from a baffle plate.

DESCRIPTION OF SYMBOLS 1 Coal thermal power generation equipment 10 Discharge device 11 Charging part 12 Discharge electrode 15 Charging device 30 Pulverized coal machine 40 Combustion boiler 60 Denitration device 64 Rectification plate (discharge electrode)
621 Casing 622 Honeycomb catalyst 623 Seal member

Claims (4)

  1. A pulverized coal machine that pulverizes coal to produce pulverized coal;
    A combustion boiler for burning the pulverized coal produced in the pulverized coal machine;
    A denitration device that is disposed downstream of the combustion boiler and removes nitrogen oxides contained in exhaust gas generated by burning pulverized coal in the combustion boiler;
    A discharge device arranged on the upstream side of the denitration device and charging coal ash contained in the exhaust gas to the positive electrode or the negative electrode;
    A coal-fired power generation facility comprising: a charging device that charges the denitration device to the same polarity as coal ash.
  2. The said discharge apparatus is provided with the discharge electrode and the charge part which applies a high voltage to this discharge electrode, The coal ash is charged to a positive electrode or a negative electrode by generating a corona discharge from this discharge electrode. Coal-fired power plant.
  3. A rectifying plate arranged on the upstream side of the denitration device and rectifying the exhaust gas introduced into the denitration device;
    The coal discharge power generation facility according to claim 2, wherein the discharge device is configured such that the discharge electrode is constituted by the rectifying plate.
  4. The denitration apparatus is
    A cylindrical casing having conductivity;
    A plurality of honeycomb catalysts accommodated in the casing, a plurality of elongated honeycomb catalysts in which a plurality of exhaust gas circulation holes extending in the longitudinal direction are formed;
    A seal member disposed between the honeycomb catalysts disposed adjacent to each other in a short direction to prevent inflow of exhaust gas, and
    The plurality of honeycomb catalysts are configured to include a conductive carrier and a catalyst substance supported on the conductive carrier,
    The coal-fired power generation facility according to any one of claims 1 to 3, wherein the seal member has conductivity.
PCT/JP2016/071553 2015-07-31 2016-07-22 Coal-fired power generation equipment WO2017022522A1 (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP2015-152882 2015-07-31
JP2015152882 2015-07-31

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP2017505666A JP6233545B2 (en) 2015-07-31 2016-07-22 Coal-fired power generation facility

Publications (1)

Publication Number Publication Date
WO2017022522A1 true WO2017022522A1 (en) 2017-02-09

Family

ID=57942885

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2016/071553 WO2017022522A1 (en) 2015-07-31 2016-07-22 Coal-fired power generation equipment

Country Status (2)

Country Link
JP (1) JP6233545B2 (en)
WO (1) WO2017022522A1 (en)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0450121U (en) * 1990-08-27 1992-04-28
JP2001153309A (en) * 1999-11-26 2001-06-08 Babcock Hitachi Kk Pulverized coal boiler, its operating method, and method for remodeling pulverized coal boiler
JP2006257948A (en) * 2005-03-16 2006-09-28 Toyota Motor Corp Gas purifier
JP2006320818A (en) * 2005-05-18 2006-11-30 Toyota Motor Corp Pm purifying device and pm purifying method
JP2007107450A (en) * 2005-10-13 2007-04-26 Hino Motors Ltd Exhaust emission control device
JP2012067610A (en) * 2010-09-21 2012-04-05 Ngk Insulators Ltd Exhaust emission control device
JP2013504412A (en) * 2009-09-14 2013-02-07 エミテック ゲゼルシヤフト フユア エミツシオンス テクノロギー ミツト ベシユレンクテル ハフツング Exhaust gas treatment device having two honeycomb bodies for generating electric potential

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5248943B2 (en) * 1975-03-24 1977-12-13

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0450121U (en) * 1990-08-27 1992-04-28
JP2001153309A (en) * 1999-11-26 2001-06-08 Babcock Hitachi Kk Pulverized coal boiler, its operating method, and method for remodeling pulverized coal boiler
JP2006257948A (en) * 2005-03-16 2006-09-28 Toyota Motor Corp Gas purifier
JP2006320818A (en) * 2005-05-18 2006-11-30 Toyota Motor Corp Pm purifying device and pm purifying method
JP2007107450A (en) * 2005-10-13 2007-04-26 Hino Motors Ltd Exhaust emission control device
JP2013504412A (en) * 2009-09-14 2013-02-07 エミテック ゲゼルシヤフト フユア エミツシオンス テクノロギー ミツト ベシユレンクテル ハフツング Exhaust gas treatment device having two honeycomb bodies for generating electric potential
JP2012067610A (en) * 2010-09-21 2012-04-05 Ngk Insulators Ltd Exhaust emission control device

Also Published As

Publication number Publication date
JP6233545B2 (en) 2017-11-22
JPWO2017022522A1 (en) 2017-08-03

Similar Documents

Publication Publication Date Title
EP2959959B1 (en) Exhaust gas treatment system
Wang et al. Simultaneous removal of NOx, SO2 and Hg in nitrogen flow in a narrow reactor by ozone injection: Experimental results
CN100402130C (en) System and method for controlling nox emissions from boilers combusting carbonaceous fuels without using external reagent
CA2927302C (en) Dry sorbent injection during steady-state conditions in dry scrubber
JP3924150B2 (en) Gas combustion treatment method and apparatus
US7198769B2 (en) Multi-stage process for SCR of NOx
TW394816B (en) Method of reducing internal combustion engine emissions, and system for same
JP4388542B2 (en) Mercury removal method and mercury removal system
AU2008283781B2 (en) A low-temperature, moving bed catalytic reactor for control of NOx emissions from coal combustion
US20150030508A1 (en) Method and a device for removing nitrogen oxides and sulphur trioxide from a process gas
US7247285B2 (en) Reduction of sulfur, nitrogen oxides and volatile trace metals from combustion in furnaces and boilers
ES2500440T3 (en) Apparatus and method for treating discharge gas
JP5302597B2 (en) Exhaust gas treatment apparatus and exhaust gas treatment method
US7544339B2 (en) Method and apparatus for removing mercury from combustion exhaust gas
CN105716092B (en) A kind of system processing method of oil field ground sludge
CN105169942B (en) Flue gas of glass melting furnace dust-removal and desulfurizing denitration coprocessing system and processing method and application
US5165903A (en) Integrated process and apparatus for control of pollutants in coal-fired boilers
EP2463015B1 (en) Air pollution control device
US7776141B2 (en) Methods and apparatus for performing flue gas pollution control and/or energy recovery
JP2007530256A (en) Bromine addition to improve mercury removal from flue gas
JP2005516753A (en) A method for removing mercury from flue gases by oxidation.
US8808652B2 (en) Biomass boiler SCR NOx and CO reduction system
Van Caneghem et al. NOx reduction in waste incinerators by selective catalytic reduction (SCR) instead of selective non catalytic reduction (SNCR) compared from a life cycle perspective: a case study
ES2724702T3 (en) Exhaust gas treatment apparatus and method
CN102103047B (en) Method and device for detecting fume denitration catalyst activity

Legal Events

Date Code Title Description
ENP Entry into the national phase in:

Ref document number: 2017505666

Country of ref document: JP

Kind code of ref document: A

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 16832801

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase in:

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 16832801

Country of ref document: EP

Kind code of ref document: A1