CN102019135B - Flue gas-based combined desulfuration and denitration method and special device for method - Google Patents
Flue gas-based combined desulfuration and denitration method and special device for method Download PDFInfo
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- CN102019135B CN102019135B CN 201010546275 CN201010546275A CN102019135B CN 102019135 B CN102019135 B CN 102019135B CN 201010546275 CN201010546275 CN 201010546275 CN 201010546275 A CN201010546275 A CN 201010546275A CN 102019135 B CN102019135 B CN 102019135B
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Abstract
The invention discloses a flue gas-based desulduratoin and denitration method and a special device for the flue gas-based desulduratoin and denitration method. The special device comprises a denitration reactor body and a desulphurization reactor body, wherein the side wall of the desulphurization reactor body is provided with a flue inlet; the desulphurization reactor body and the denitration reactor body are communicated in parallel; the volume of the denitration reactor body is 1-2 times that of the desulphurization reactor body; the communicating position of the desulphurization reactor body and the denitration reactor body is provided with a device for spraying NH3; the top of the denitration reactor body is provided with a denitration reactor inlet for active coke; the bottom of the denitration reactor is provided with a denitration reactor outlet for the active coke; the top of the desulphurization reactor is provided with a desulphurization reactor inlet for the active coke; the bottom of the desulphurization reactor is provided with a desulphurization reactor outlet for the active coke; and the denitration reactor outlet for the active coke is communicated with a desulphurization reactor inlet for the active coke through a pipeline, and the desulphurization reactor outlet for the active coke is communicated with a regeneration reactor. The invention also provides a method for flue gas desulfurization and denitration by using the device.
Description
Technical field
The present invention relates to a kind of flue gas purifying method and device thereof, relate in particular to a kind of flue gas combined desulfurization and denitration method and isolated plant thereof.
Background technology
SO in the coal-fired flue-gas
2And NO
xThe environmental pollutions such as caused acid rain and photochemical fog have become the serious problems that affect environment for human survival, along with the raising of in recent years environmental requirement, control simultaneously SO
2And NO
xThe requirement of discharging is more urgent.With respect to the traditional desulphurization and denitration technology of independent application, the combined desulfurization and denitration technology has advantage aspect economy, the level of resources utilization, China's pollution that caused by coal burning is on the rise, greatly develop low expense, high efficiency pollution that caused by coal burning Prevention Technique is the task of top priority, the combined desulfurization and denitration technology that therefore has the advantages such as expense is low, compact conformation is subject to increasing attention.
Activated coke flue gas combined desulfurization and denitration technology is a kind of advanced person's dry method flue gas combined desulfurization and denitration technology, and this technology denitrification efficiency is high, and subtractive process does not consume water substantially, is adapted at China water-deficient area and applies; Remove the product resourcebility, can alleviate to a certain extent the present situation of present China sulphur shortage of resources; The coal-based adsorbent that adopts is take the relatively abundant coal of China's reserves as primary raw material, and raw material supply has sufficient the assurance.Therefore, this technology is that a kind of suitable China's national situation, efficient and economic coal-fired flue-gas pollute and jointly control technology.
The active coke desulphurizing technological principle is based on SO
2In activated coke surface sorption and catalytic action, the SO in the flue gas
2Under 110 ℃～180 ℃ temperature, generate sulfuric acid and be adsorbed in the activated coke hole with the chemical reaction that reacts of oxygen, water vapour in the flue gas, reaction equation is as follows:
2SO
2+O
2+2H
2O→2H
2SO
4
Activated coke denitrating technique principle is to utilize the catalysis characteristics of activated coke, adopts selective catalytic reduction reaction (SCR) method, allocates a small amount of NH in flue gas into
3, impel NO that selective catalytic reduction reaction occurs and generate harmless N
2Directly discharging, reaction equation is as follows:
4NO+4NH
3+O
2→4N
2+6H
2O
The disclosed a kind of flue gas desulfurization and denitration technique shortcoming of CN 1712108A is strictly to be divided into two sections, and middle junction is narrower, and wayward activated coke moves down speed, CO content is few in the regeneration gas, be difficult to separate, and between 120 ℃-180 ℃ of flue-gas temperatures, adopt CO as reducing agent NO
xRemoval efficiency is lower, and denitration effect is not as all adopting NH
3Removal efficiency during as reducing agent.Under the equal conditions, adopt CO to compare NH as reducing agent
3The time denitration efficiency low 10%-30%.
CN 1911491A discloses desulfurization denitration method, and the method is carried out in a reactor, top denitration, bottom desulfurization.The shortcoming of this invention is that flue gas flow direction is not easy control in the reactor, and the partial fume after the desulfurization is pasting easily reactor wall and directly entering the chimney discharge from the denitration outlet, and this part flue gas is not owing to have and NH
3Mix, cause denitration efficiency low; Spray NH
3Mouth is divided into two up and down, under the smoke evacuation effect, and NH
3Can not be evenly distributed on top denitrification activated coke bed, cause in the flue gas NO removal efficiency low.
Summary of the invention
An object of the present invention is to provide a kind of flue gas combined desulfurization and denitration device.
Another object of the present invention provides a kind of method of utilizing said apparatus to carry out flue gas combined desulfurization and denitration.
Flue gas combined desulfurization and denitration device provided by the present invention comprises that Benitration reactor body and sidewall are provided with the desulfurization reactor body of smoke inlet, the series connection of described desulfurization reactor body and described Benitration reactor body is communicated with, and the volume of described Benitration reactor is 1 times-2 times of volume of described desulfurization reactor; The connectivity part of described desulfurization reactor and described Benitration reactor is provided with spray NH
3Device; Be provided with spray NH in the described Benitration reactor
3Device; The sidewall of described Benitration reactor is provided with exhanst gas outlet; The top of described Benitration reactor is provided with the activated coke denitration reactor inlet, and described Benitration reactor bottom is provided with the outlet of activated coke Benitration reactor; The top of described desulfurization reactor is provided with the active coke desulphurizing reactor inlet, and the bottom of described desulfurization reactor is provided with the active coke desulphurizing reactor outlet; Described activated coke Benitration reactor outlet is connected by conveyance conduit with described active coke desulphurizing reactor inlet, and described active coke desulphurizing reactor outlet is connected with regeneration reactor.
In the said apparatus, the entrance of described regeneration reactor is located at its top, and its bottom is located in outlet, by the NO desorption district, NO enrichment region, the SO that are communicated with successively up and down
2Desorption district, SO
2Enrichment region and activated coke cooling zone form; The outlet of described regeneration reactor is connected with screening plant, and the outlet of the qualified particle diameter of described screening plant is connected with described activated coke denitration reactor inlet.
In the said apparatus, be provided with spray NH between described screening plant and the described activated coke denitration reactor inlet
3With N
2Or NH
3Device with the mist of air.
In the said apparatus, be provided with two parallel sieve plates in the described desulfurization reactor; Described sieve plate is divided into Three regions with described desulfurization reactor; Be provided with two parallel sieve plates in the described Benitration reactor; Described sieve plate is divided into Three regions with described Benitration reactor.
The method of flue gas desulfurization and denitrification provided by the invention comprises the steps: it is to utilize above-mentioned flue gas desulfurization and denitrification device that flue gas to be clean is carried out desulphurization denitration, obtains meeting the flue gas of discharge standard; When described flue gas to be clean entered described flue gas desulfurization and denitrification device and purifies, circulation added activated coke in described flue gas desulfurization and denitrification device.
In the said method, the purification route of described flue gas is: flue gas to be clean enters in the described desulfurization reactor from described smoke inlet, contacts with activated coke in the described desulfurization reactor; Then the spray NH of described flue gas by arranging between described desulfurization reactor and the Benitration reactor
3Device is with described spray NH
3The NH of device ejection
3Enter after the premixed in the described Benitration reactor; Activated coke in described flue gas and the described Benitration reactor contact, then meets the flue gas of discharge standard from described exhanst gas outlet discharge; The circulation route of described activated coke is: activated coke and the fresh activated coke of part enter in the described Benitration reactor from described activated coke denitration reactor inlet after the regeneration, and described activated coke relies on gravity to move in described Benitration reactor from top to bottom and adsorbs the spray NH that arranges in the described Benitration reactor
3The NH of device ejection
3, remove NO and SO in the flue gas
2Then export out by described active coke desulphurizing reactor inlet from described activated coke Benitration reactor and enter in the described desulfurization reactor; Described activated coke relies on gravity mobile in described desulfurization reactor from top to bottom, NO and SO in the absorption flue gas
2Then out enter in the described regeneration reactor by the entrance of described regeneration reactor from described active coke desulphurizing reactor outlet; Described activated coke is passed through described NO desorption district, NO enrichment region, SO successively
2Desorption district, SO
2Behind enrichment region and the activated coke cooling zone by described screening plant from the outlet of the qualified particle diameter of described screening plant out, then by described spray NH
3With N
2Or NH
3With the device of the mist of air, absorption NH
3With N
2Or NH
3Enter in the described Benitration reactor from described activated coke denitration reactor inlet with the mist of air and after replenishing fresh activated coke, begin new circulation.
In the said method, the temperature of described flue gas is 110 ℃-180 ℃, such as 110 ℃ or 180 ℃; Temperature in the described NO desorption district is 150 ℃-250 ℃, such as 150 ℃ or 250 ℃; Described SO
2Temperature in the desorption district is 350 ℃-450 ℃, such as 350 ℃ or 450 ℃; Temperature in the described activated coke cooling zone is 80 ℃-200 ℃, such as 80 ℃ or 200 ℃.
In the said method, NH described in the described mist
3Volume parts be 0.01%-1%, such as 0.01% or 1%.
In the said method, described activated coke can be one or more activated coke of producing as raw material take anthracite, bituminous coal or brown coal.
Flue gas desulfurization and denitrification device provided by the invention has following advantage:
(1) because the volume of Benitration reactor greater than the volume of desulfurization reactor, can make time that flue gas stops greater than its time that stops like this, thereby can improve the denitration efficiency of activated coke in desulfurization reactor in Benitration reactor; And flue gas some NO in desulfurization reactor is adsorbed by activated coke, again is removed and has improved denitration efficiency thereby then enter behind the Benitration reactor NO in the flue gas and activated coke generation chemical reaction; SO in the flue gas
2Be desulfurized successively the activated coke absorption in reactor and the Benitration reactor, thereby improved desulfuration efficiency by second adsorption.
(2) between desulfurization reactor and Benitration reactor, be provided with spray NH
3The device, thus make flue gas before entering Benitration reactor with NH
3Premixed is conducive to improve the denitration efficiency of activated coke; Further be provided with spray NH in the Benitration reactor
3Device can further promote NH
3Distribution in Benitration reactor makes activated coke fully absorb NH
3, further improve the denitration efficiency of activated coke; Screening plant outlet is provided with ammonia-gas spraying device with the activated coke denitration reactor inlet, can make the pre-absorbed portion NH of activated coke after the regeneration
3, be conducive to improve denitration efficiency.
(3) agent structure of desulfurization reactor and Benitration reactor is simple, easily processing, and air resistance is less, is conducive to the raising of denitrification efficiency; Desulfurization reactor and Benitration reactor internal structure are simple, can reduce the activated coke friction, reduce the crushing of activated coke, and flue gas is contacted fully with activated coke, are conducive to the raising of denitrification efficiency.
(4) different from existing desulfurization regeneration commercial plant, because existing desulfurization denitration method has increased denitrification apparatus, cause can adsorbing a certain amount of NO in the activated coke hole, characteristics according to desorption gas, the desorption reaction device is divided into two sections, top enrichment of N O, bottom enrichment SO
2, be conducive to gas purification and recycling.
The method of a kind of flue gas combined desulfurization and denitration provided by the invention because the method is utilized flue gas combined desulfurization and denitration device provided by the invention, has improved desulfurization and denitration efficiency simultaneously.
Description of drawings
Fig. 1 is the flue gas combined desulfurization and denitration apparatus structure schematic diagram of the embodiment of the invention 1.
Fig. 2 is the flue gas combined desulfurization and denitration apparatus structure schematic diagram of the embodiment of the invention 2.
Fig. 3 is desulfurization reactor and the internal structure schematic diagram of Benitration reactor and the flow direction schematic diagram of activated coke and flue gas thereof of the flue gas combined desulfurization and denitration device of the embodiment of the invention 1.
Fig. 4 is desulfurization reactor and the internal structure schematic diagram of Benitration reactor and the flow direction schematic diagram of activated coke and flue gas thereof of the flue gas combined desulfurization and denitration device of the embodiment of the invention 2.
The specific embodiment
Employed experimental technique is conventional method if no special instructions among the following embodiment.
Used material, reagent etc. if no special instructions, all can obtain from commercial channels among the following embodiment.
The following embodiment 3 of the present invention and 4 used activated coke are bought the emerging charcoal industry Co., Ltd in section.
SO in the flue gas among the following embodiment 3 of the present invention and 4
2SO with the production of NO employing Beijing BAIF-Maihak Analytical Instrument Co., Ltd.
2With the NO infrared analyzer, model is QGS-08B.Flue gas after the desulphurization denitration is introduced respectively analytical instrument, and analytical instrument is measured SO in the flue gas automatically
2With NO concentration, then signal is passed to computer data are preserved.Measure flue gas and enter concentration and the concentration behind the desulphurization denitration before the activated coke, can obtain removal efficiency by calculating.
Embodiment 1, flue gas combined desulfurization and denitration device
The structural representation of this device as shown in Figure 1, each mark is as follows among the figure: 1 desulfurization reactor, 2 Benitration reactors, 3 NO desorption districts, 4 NO enrichment regions, 5 SO
2Desorption district, 6 SO
2Enrichment region, 7 activated coke cooling zones, 8 screening plants, 9 exhanst gas outlets, 10 activated coke denitration reactor inlets, 11 smoke inlets, the outlet of 12 activated coke Benitration reactors, 13 active coke desulphurizing reactor inlets, 14 active coke desulphurizing reactor outlets.
Flue gas combined desulfurization and denitration device of the present invention comprises desulfurization reactor 1 and Benitration reactor 2, and 2 series connection of desulfurization reactor 1 and Benitration reactor are communicated with, and the volume of Benitration reactor 2 is 1.5 times of volume of desulfurization reactor 1; Desulfurization reactor 1 is positioned at the left side of Benitration reactor 2; The left side wall of desulfurization reactor 1 is provided with smoke inlet 11, and flue gas to be clean enters this device from this smoke inlet 11 and purifies; Connectivity part at desulfurization reactor 1 and Benitration reactor 2 is provided with spray NH
3Device; Make flue gas after the desulfurization before entering Benitration reactor 2 with NH
3Premixed; Left side in Benitration reactor 2 is provided with a spray NH
3Device further promotes NH
3Distribution in reactor makes activated coke fully adsorb NH
3The right side wall of Benitration reactor 2 is provided with exhanst gas outlet 9, and the flue gas after purifying meets discharge standard and directly discharges from this exhanst gas outlet 9.The top of Benitration reactor 2 is provided with activated coke denitration reactor inlet 10, and activated coke enters this device from this activated coke denitration reactor inlet 10; The bottom of Benitration reactor 2 is provided with activated coke Benitration reactor outlet 12, this activated coke Benitration reactor outlet 12 is connected with the active coke desulphurizing reactor inlet 13 that desulfurization reactor 1 top is provided with, and activated coke is entered in the desulfurization reactor 1 from Benitration reactor 2; Desulfurization reactor 1 bottom is provided with active coke desulphurizing reactor outlet 14, and this active coke desulphurizing reactor outlet 14 is communicated with the activated coke regeneration reactor, makes to enter in this regeneration reactor behind the activated coke purifying smoke to regenerate.This regeneration reactor is by the NO desorption district 3, NO enrichment region 4, the SO that are communicated with successively up and down
2Desorption district 5, SO
2Enrichment region 6 and activated coke cooling zone 7 form NO and SO that activated coke is adsorbed in purification process
2Carry out desorption and collection; This activated coke cooling zone 7 is connected with a screening plant 8, and the outlet of the qualified particle diameter of screening plant 8 is connected with activated coke denitration reactor inlet 10; Obtain the activated coke of release mesh through the outlet of the qualified particle diameter of screening plant 8 through the activated coke of regeneration; Be provided with a spray NH between screening plant 8 and the activated coke denitration reactor inlet 10
3With N
2Or NH
3With the device of the mist of air, activated coke is by this device absorption NH
3With N
2Or NH
3Behind the mist of air, enter into Benitration reactor 2 by activated coke denitration reactor inlet 10 after replenishing again the fresh activated coke of part, enter next circulation.
The flow direction schematic diagram of the desulfurization reactor 1 of this device and the internal structure schematic diagram of Benitration reactor 2 and activated coke and flue gas as shown in Figure 3.The inside of desulfurization reactor 1 and Benitration reactor 2 is equipped with two parallel sieve plates reactor is divided into Three regions: I district, II district and III district; Flue gas to be clean flows to the III district from the I district through the II district, discharges at last, and activated coke relies on gravity to move from top to bottom.I district and flue gas middle and high concentration SO
2Perhaps NO gas contact, activated coke is very fast in this zone decrease speed, SO in II, the III district flue gas
2Perhaps the NO gas concentration reduces gradually, and the activated coke decrease speed is slack-off, and III district activated coke decrease speed is the slowest.
Embodiment 2, flue gas combined desulfurization and denitration device
The structural representation of this device as shown in Figure 2, each mark is as follows among the figure: 1 desulfurization reactor, 2 Benitration reactors, 3 NO desorption districts, 4 NO enrichment regions, 5 SO
2Desorption district, 6 SO
2Enrichment region, 7 activated coke cooling zones, 8 screening plants, 9 exhanst gas outlets, 10 activated coke denitration reactor inlets, 11 smoke inlets, the outlet of 12 activated coke Benitration reactors, 13 active coke desulphurizing reactor inlets, 14 active coke desulphurizing reactor outlets.
Flue gas combined desulfurization and denitration device of the present invention comprises desulfurization reactor 1 and Benitration reactor 2, and 2 series connection of desulfurization reactor 1 and Benitration reactor are communicated with, and the volume of Benitration reactor 2 is 1.2 times of volume of desulfurization reactor 1; Desulfurization reactor 1 is positioned at the left side of Benitration reactor 2; The right side wall of desulfurization reactor 1 is provided with smoke inlet 11, and flue gas to be clean enters this device from this smoke inlet 11 and purifies; Connectivity part at desulfurization reactor 1 and Benitration reactor 2 is provided with spray NH
3Device; Make flue gas after the desulfurization before entering Benitration reactor 2 with NH
3Premixed; Right side in Benitration reactor 2 is provided with a spray NH
3Device further promotes NH
3Distribution in reactor makes activated coke fully adsorb NH
3The left side wall of Benitration reactor is provided with exhanst gas outlet 9, and the flue gas after purifying meets discharge standard and directly discharges from this exhanst gas outlet 9.The top of Benitration reactor 2 is provided with activated coke denitration reactor inlet 10, and activated coke enters this device from this activated coke denitration reactor inlet 10; The bottom of Benitration reactor 2 is provided with activated coke Benitration reactor outlet 12, and this activated coke Benitration reactor outlet 12 is connected with the active coke desulphurizing reactor inlet 13 that the desulfurization reactor top is provided with, and activated coke is entered in the desulfurization reactor 1 from Benitration reactor 2; Desulfurization reactor 1 bottom is provided with active coke desulphurizing reactor outlet 14, and this active coke desulphurizing reactor outlet 14 is communicated with the activated coke regeneration reactor, makes to enter in this regeneration reactor behind the activated coke purifying smoke to regenerate.This regeneration reactor is by the NO desorption district 3, NO enrichment region 4, the SO that are communicated with successively up and down
2Desorption district 5, SO
2Enrichment region 6 and activated coke cooling zone 7 form NO and SO that activated coke is adsorbed in purification process
2Carry out desorption and collection; This activated coke cooling zone 7 is connected with a screening plant 8, and the outlet of the qualified particle diameter of screening plant 8 is connected with activated coke denitration reactor inlet 10; The activated coke of the release mesh that the activated coke process screening plant 8 of process regeneration obtains; Be provided with a spray NH between screening plant 8 and the activated coke denitration reactor inlet 10
3With N
2Or NH
3With the device of the mist of air, activated coke is by this device absorption NH
3With N
2Or NH
3Behind the mist of air, enter into Benitration reactor 2 by activated coke denitration reactor inlet 10 after replenishing again the fresh activated coke of part, enter next circulation.
The internal structure schematic diagram of the desulfurization reactor of this device and Benitration reactor and the flow direction schematic diagram of activated coke and flue gas thereof are as shown in Figure 4.The inside of desulfurization reactor and Benitration reactor is equipped with two parallel sieve plates reactor is divided into Three regions: I district, II district and III district; Flue gas is mobile after the I district is by forward direction, then distinguishes stream to II district and III, and flue gas and I district Gas phase Smoke are to flowing in II district and the III district, and activated coke relies on gravity to move from top to bottom.I district and flue gas middle and high concentration SO
2Perhaps NO gas contact, activated coke is very fast in this zone decrease speed, SO in II, the III district flue gas
2Perhaps the NO gas concentration reduces gradually, and the activated coke decrease speed is slack-off.
500t is just filled in the Benitration reactor 2 in activated coke is added to embodiment 1 from denitration reactor inlet 10 the flue gas combined desulfurization and denitration device, and this activated coke relies on the spray NH of gravity mobile and absorption Benitration reactor 2 interior settings from top to bottom in Benitration reactor 2
3The NH of device ejection
3, remove NO and SO in the flue gas
2Then out enter in the desulfurization reactor 1 by active coke desulphurizing reactor inlet 13 from activated coke Benitration reactor outlet 12, this activated coke relies on gravity mobile in desulfurization reactor 1 from top to bottom, NO and SO in the absorption flue gas
2Then out enter in the regeneration reactor by the entrance of regeneration reactor from active coke desulphurizing reactor outlet 14; This activated coke is passed through NO desorption district 3, NO enrichment region 4, SO successively
2Desorption district 5, SO
2Enrichment region 6 and activated coke cooling zone 7, wherein, the temperature in the NO desorption district 3 is 150 ℃, then the higher concentration NO gas enrichment with desorption purifies recovery; SO
2Temperature in the desorption district 5 are 350 ℃, then with the high concentration SO of desorption
2The gas enrichment purifies reclaims; Temperature in the activated coke cooling zone 7 is 80 ℃; Enter screening plant 8 through cooled activated coke, from the outlet of the qualified particle diameter of the screening plant 8 spray NH through arranging between screening plant 8 and the activated coke denitration reactor inlet 10 out
3With N
2Or NH
3With the device absorption mist of the mist of air, wherein, NH in this mist
3Volumn concentration be 0.1%; In the activated coke of absorption mist, enter in the Benitration reactor 2 from activated coke denitration reactor inlet 10 with the additional fresh activated coke of the speed of 10kg/h, begin new circulation; With flue gas (SO to be clean
2Concentration is 5000mg/Nm
3, NO
xConcentration is 800mg/Nm
3, the temperature of flue gas is 110 ℃) and from being added to the desulfurization reactor 1 of this device, smoke inlet 11 contacts with activated coke, with NO and the SO in the absorption flue gas
2, the control flue gas flow rate is 50000Nm
3/ h; Flue gas from desulfurization reactor 1 out with the spray NH
3The NH of device ejection
3Enter after the premixed in the Benitration reactor 2 and contact with activated coke, to remove NO and the SO in the flue gas
2, then discharge the flue gas that meets discharge standard from exhanst gas outlet 9.Whole process SO
2Removal efficiency is 98%, NO
xRemoval efficiency is 80%.
Embodiment 4, carry out desulfurization and denitration with the flue gas combined desulfurization and denitration device of embodiment 2
500t is just filled in the Benitration reactor 2 in activated coke is added to embodiment 2 from activated coke denitration reactor inlet 10 the flue gas combined desulfurization and denitration device, and this activated coke relies on the spray NH of gravity mobile and absorption Benitration reactor 2 interior settings from top to bottom in Benitration reactor 2
3The NH of device ejection
3Then out enter in the desulfurization reactor 1 by active coke desulphurizing reactor inlet 13 from activated coke Benitration reactor outlet 12, this activated coke relies on gravity mobile in desulfurization reactor 1 from top to bottom, then out enters in the described regeneration reactor by the entrance of regeneration reactor from active coke desulphurizing reactor outlet 14; This activated coke is passed through NO desorption district 3, NO enrichment region 4, SO successively
2Desorption district 5, SO
2Enrichment region 6 and activated coke cooling zone 7, wherein, the temperature in the NO desorption district 3 is 250 ℃, then the higher concentration NO gas enrichment with desorption purifies recovery; SO
2Temperature in the desorption district 5 are 450 ℃, then with the high concentration SO of desorption
2The gas enrichment purifies reclaims; Temperature in the activated coke cooling zone is 200 ℃; Enter screening plant 8 through cooled activated coke, from the outlet of the qualified particle diameter of the screening plant 8 spray NH through arranging between screening plant 8 and the activated coke denitration reactor inlet 10 out
3With N
2Or NH
3With the device absorption mist of the mist of air, NH in this mist
3Volumn concentration be 1%, replenish fresh activated coke with the speed of 10kg/h in the activated coke of absorption mist to enter in the Benitration reactor 2 from activated coke denitration reactor inlet 10, begin new circulation; With flue gas (SO to be clean
2Concentration is 5000mg/Nm
3, NO
xConcentration is 800mg/Nm
3, the temperature of flue gas is 180 ℃) and from being added to the desulfurization reactor 1 of this device, smoke inlet 11 contacts with activated coke, with NO and the SO in the absorption flue gas
2, the control flue gas flow rate is 50000Nm
3/ h, flue gas from desulfurization reactor 1 out with the spray NH
3The NH of device ejection
3Enter after the premixed in the Benitration reactor 2 and contact with activated coke, to remove NO and the SO in the flue gas
2, then discharge the flue gas that obtains meeting discharge standard from exhanst gas outlet 9.Whole process SO
2Removal efficiency is 97%, NO
xRemoval efficiency is 76%.
Claims (5)
1. flue gas combined desulfurization and denitration device, it comprises that Benitration reactor body and sidewall are provided with the desulfurization reactor body of smoke inlet, it is characterized in that: described desulfurization reactor body and the series connection of described Benitration reactor body are communicated with, and the volume of described Benitration reactor is 1 times-2 times of described desulfurization reactor volume; The connectivity part of described desulfurization reactor and described Benitration reactor is provided with spray NH
3Device; Be provided with spray NH in the described Benitration reactor
3Device; The sidewall of described Benitration reactor is provided with exhanst gas outlet; The top of described Benitration reactor is provided with the activated coke denitration reactor inlet, and described Benitration reactor bottom is provided with the outlet of activated coke Benitration reactor; The top of described desulfurization reactor is provided with the active coke desulphurizing reactor inlet, and the bottom of described desulfurization reactor is provided with the active coke desulphurizing reactor outlet; Described activated coke Benitration reactor outlet is connected by conveyance conduit with described active coke desulphurizing reactor inlet, and described active coke desulphurizing reactor outlet is connected with the regeneration reactor entrance;
The entrance of described regeneration reactor is located at its top, and its bottom is located in outlet, by the NO desorption district, NO enrichment region, the SO that are communicated with successively up and down
2Desorption district, SO
2Enrichment region and activated coke cooling zone form; The outlet of described regeneration reactor is connected with screening plant, and the outlet of the qualified particle diameter of described screening plant is connected with described activated coke denitration reactor inlet;
Be provided with spray NH between described screening plant and the described activated coke denitration reactor inlet
3With N
2Or NH
3Device with the mist of air;
Be provided with two parallel sieve plates in the described desulfurization reactor; Described sieve plate is divided into Three regions with described desulfurization reactor; Be provided with two parallel sieve plates in the described Benitration reactor; Described sieve plate is divided into Three regions with described Benitration reactor.
2. the method for a flue gas desulfurization and denitrification is to utilize flue gas combined desulfurization and denitration device claimed in claim 1 that flue gas to be clean is carried out desulphurization denitration, obtains meeting the flue gas of discharge standard; When described flue gas to be clean entered described flue gas combined desulfurization and denitration device and purifies, circulation added activated coke in the described flue gas desulfurization and denitrification device.
3. method according to claim 2, it is characterized in that: flue gas to be clean enters in the described desulfurization reactor from described smoke inlet, contacts with activated coke in the described desulfurization reactor; Then the spray NH of described flue gas by arranging between described desulfurization reactor and the Benitration reactor
3Device is with described spray NH
3The NH of device ejection
3Enter after the premixed in the described Benitration reactor; Activated coke in described flue gas and the described Benitration reactor contact, then meets the flue gas of discharge standard from described exhanst gas outlet discharge; The circulation route of described activated coke is: activated coke and the fresh activated coke of part enter in the described Benitration reactor from described activated coke denitration reactor inlet after the regeneration, and described activated coke relies on gravity to move in described Benitration reactor from top to bottom and adsorbs the spray NH that arranges in the described Benitration reactor
3The NH of device ejection
3, remove NO and SO in the flue gas
2Then export out by described active coke desulphurizing reactor inlet from described activated coke Benitration reactor and enter in the described desulfurization reactor; Described activated coke relies on gravity mobile in described desulfurization reactor from top to bottom, NO and SO in the absorption flue gas
2Then out enter in the described regeneration reactor by the entrance of described regeneration reactor from described active coke desulphurizing reactor outlet; Described activated coke is passed through described NO desorption district, NO enrichment region, SO successively
2Desorption district, SO
2Behind enrichment region and the activated coke cooling zone by described screening plant from the outlet of the qualified particle diameter of described screening plant out, then by described spray NH
3With N
2Or NH
3With the device of the mist of air, absorption NH
3With N
2Or NH
3Enter in the described Benitration reactor from described activated coke denitration reactor inlet with the mist of air and after replenishing fresh activated coke, begin new circulation.
4. according to claim 2 or 3 described methods, it is characterized in that: the temperature of described flue gas is 110 ℃-180 ℃; Temperature in the described NO desorption district is 150 ℃-250 ℃; Described SO
2Temperature in the desorption district is 350 ℃-450 ℃; Temperature in the described activated coke cooling zone is 80 ℃-200 ℃.
5. method according to claim 4 is characterized in that: NH described in the described mist
3Volumn concentration be 0.01%-1%.
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| CN108744960B (en) * | 2018-06-14 | 2021-06-18 | 华北电力大学（保定） | Device and method for simultaneously desulfurizing, denitrifying, removing mercury and recycling flue gas |
| CN110261546A (en) * | 2019-06-28 | 2019-09-20 | 中冶南方都市环保工程技术股份有限公司 | The experimental rig and method of active coke desulphurizing and denitration performance can be tested simultaneously |
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