CN212348227U - Flue gas desulfurization and denitrification activated carbon distribution system - Google Patents
Flue gas desulfurization and denitrification activated carbon distribution system Download PDFInfo
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- CN212348227U CN212348227U CN202020233408.4U CN202020233408U CN212348227U CN 212348227 U CN212348227 U CN 212348227U CN 202020233408 U CN202020233408 U CN 202020233408U CN 212348227 U CN212348227 U CN 212348227U
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Abstract
The utility model discloses a flue gas desulfurization denitration active carbon cloth system, this system include analytic tower, desulfurizing tower, denitration tower. The original flue gas sequentially passes through a desulfurization tower and a denitration tower to complete the desulfurization and denitration process; the discharge gate of desorption tower links to each other with the feed inlet of denitration tower through first active carbon conveyor. The discharge port of the desulfurizing tower is connected with the feed inlet of the desorption tower through a second activated carbon conveying device. The discharge port of the denitration tower is also connected with the feed inlet of the desorption tower through a second activated carbon conveying device. And the bypass active carbon conveying device is led out from the first active carbon conveying device and is connected with a feed inlet of the desulfurizing tower. According to the scheme, the active carbon circulation quantity of the desulfurization tower and the denitration tower is independently and accurately controlled, the abrasion loss of the active carbon is reduced, and the operation cost and the dust emission concentration are reduced.
Description
Technical Field
The utility model relates to a flue gas treatment facility technique, concretely relates to flue gas desulfurization denitration active carbon cloth system belongs to flue gas purification technical field.
Background
In steel plants, many flue gas purifications adopt two-stage activated carbon flue gas purification processes: the flue gas flow is that the flue gas is discharged from a chimney after passing through a primary adsorption tower (the main function is desulfurization) and a secondary adsorption tower (the main function is denitration); the flow of the active carbon is that the resolved active carbon is conveyed to a secondary adsorption tower by a secondary tower feeding conveyor, the conveyor is conveyed to the primary adsorption tower by the primary tower after the active carbon adsorbs part of pollutants, and the active carbon adsorbing the pollutants is conveyed to the resolution tower by the resolution tower feeding conveyor and is recycled.
In the prior art, activated carbon circulates in series among a secondary adsorption tower, a primary adsorption tower and an analytical tower, and the circulating amounts of the activated carbon in the primary adsorption tower and the secondary adsorption tower are required to be the same. For the characteristics of activated carbon and sintered pellet flue gas, in order to meet the requirement of desulfurization efficiency, the circulating amount of activated carbon of a primary adsorption tower is generally larger than that of activated carbon of a secondary adsorption tower. The activated carbon circulation of the system needs to be set at maximum demand. Namely, during actual operation, the circulation amount of the activated carbon of the first-stage adsorption tower and the circulation amount of the activated carbon of the second-stage adsorption tower are set according to the circulation amount value of the activated carbon of the first-stage adsorption tower. However, the raw flue gas volume and the pollutant concentration in the flue gas of each project are different, and the flue gas volume and the pollutant difficulty are also fluctuated frequently, so that the activated carbon circulation volume of the system needs to be set according to the maximum requirement and is unscientific, and great waste is caused.
Since each item (or a given item is in)At different times) of SO2The concentration ratio of the active carbon to the NOx is inconsistent, the principle of the active carbon for desulfurization and denitration is different, the removal effect is different, if the design needs to be refined, the circulation amount of the active carbon in the first-stage adsorption tower is required to be inconsistent with that of the active carbon in the second-stage adsorption tower, and the circulation amount of the active carbon is required to be adjusted at any time according to the smoke gas amount and the pollutant concentration.
The utility model discloses the people provides a new active carbon material stream process control method according to former gas capacity and pollutant concentration, can make the active carbon circulation volume of one-level adsorption tower adapt to desulfurization function in real time. The circulating quantity of the active carbon of the secondary adsorption tower is adapted to the dosage of NOx removed from the flue gas in real time. In the method, the circulation amount of the activated carbon of the first-stage adsorption tower and the second-stage adsorption tower is independently controlled, so that the loss of the activated carbon of the adsorbent is reduced, and the operating cost is reduced. Meanwhile, the circulation quantity of the activated carbon of the secondary adsorption tower is reduced, the moving speed of the activated carbon in the tower is reduced, the dust emission concentration can be reduced, and the environmental protection index is improved.
SUMMERY OF THE UTILITY MODEL
Not enough to prior art, the utility model provides a flue gas desulfurization denitration active carbon cloth system and cloth method, this scheme is to carrying out the SOx/NOx control in-process to the flue gas (for example sintering pelletizing flue gas), because the SO in the flue gas2The concentration ratio of the activated carbon is inconsistent with that of NOx, the principles of desulfurization and denitration by the activated carbon are different, and the removal effect is different, so that the optimal circulating amount of the required activated carbon is different. The flue gas desulfurization and denitration activated carbon distribution system and the distribution method can be finely designed, so that the activated carbon circulation volume of the desulfurization tower can adapt to the desulfurization function in real time, the activated carbon circulation volume of the denitration tower can adapt to the function of removing NOx from flue gas in real time, and the activated carbon circulation volume can be adjusted at any time according to the flue gas volume and the pollutant concentration; therefore, the active carbon circulation quantity of the desulfurization tower and the denitration tower is independently controlled, the loss of the adsorbent active carbon is reduced, and the operation cost is reduced. Meanwhile, the circulation quantity of the activated carbon in the denitration tower can be reduced, the moving speed of the activated carbon in the tower is reduced, the dust emission concentration can be reduced, and the environmental protection index can be improved.
In order to achieve the above object, the utility model discloses the technical scheme who adopts specifically as follows:
according to the utility model discloses a first embodiment provides a flue gas desulfurization denitration active carbon cloth system, and this system includes analytic tower, desulfurizing tower, denitration tower. According to the trend of the flue gas, the raw flue gas inlet pipe is connected with the air inlet of the desulfurizing tower. And the exhaust port of the desulfurization tower is connected with the air inlet of the denitration tower through a first pipeline. And the exhaust port of the denitration tower is connected with the purified flue gas exhaust pipe. The discharge port of the desorption tower is connected with the feed inlet of the denitration tower through a first activated carbon conveying device. And the discharge port of the desulfurizing tower is connected with the feed inlet of the desorption tower through a second activated carbon conveying device. And the discharge port of the denitration tower is directly connected with the feed inlet of the desorption tower through a second activated carbon conveying device. And the bypass active carbon conveying device is led out from the first active carbon conveying device and is connected with a feed inlet of the desulfurizing tower.
Preferably, m desulfurization units are arranged in the desulfurization tower. And n denitration units are arranged in the denitration tower. Wherein: m and n are each independently 1 to 8, preferably 2 to 5.
Preferably, the original flue gas inlet pipe is provided with a first concentration detection device, a second concentration detection device and a flow detection device. And a third concentration detection device is arranged on the first pipeline. And a fourth concentration detection device is arranged on the clean flue gas exhaust pipe.
Preferably, a first valve is arranged between the first activated carbon conveying device and the denitration tower or a first valve is arranged at a discharge outlet of the denitration tower.
Preferably, a first valve is arranged between the first activated carbon conveying device and any one of the denitration units, or a first valve is arranged at a discharge port of any one of the denitration units.
Preferably, a second valve is arranged between the bypass activated carbon conveying device and the desulfurizing tower or a second valve is arranged at a discharge port of the desulfurizing tower.
Preferably, a second valve is arranged between the bypass activated carbon conveying device and any one of the desulfurization units, or a second valve is arranged at the discharge port of any one of the desulfurization units.
According to the utility model discloses a second embodiment provides an adopt first embodiment flue gas desulfurization denitration active carbon cloth system carry out flue gas desulfurization denitration active carbon cloth's method, this method includes following step:
1) and conveying the raw flue gas to a desulfurizing tower through a raw flue gas inlet pipe for desulfurization treatment. And conveying the desulfurized flue gas subjected to desulfurization treatment to a denitration tower through a first pipeline for denitration treatment. And discharging the denitrated clean flue gas through a clean flue gas exhaust pipe.
2) The activated carbon after the thermal regeneration treatment of the desorption tower is conveyed to the denitration tower through the first activated carbon conveying device to carry out denitration treatment on the flue gas. And conveying the denitrated activated carbon to an analytical tower through a second activated carbon conveying device for thermal regeneration treatment. And meanwhile, a bypass active carbon conveying device is also led out of the first active carbon conveying device. And the bypass active carbon conveying device conveys active carbon to a desulfurizing tower to desulfurize the flue gas. And conveying the desulfurized activated carbon to an analytical tower through a second activated carbon conveying device for thermal regeneration treatment, and circulating the steps.
Preferably, the method further comprises: a first concentration detection device is arranged on the raw flue gas inlet pipe to detect SO in the raw flue gas in real time2Has a concentration of c1, mg/Nm3. A second concentration detection device is also arranged for detecting NO in the original smoke in real timeXHas a concentration of c2, mg/Nm3. The flow detection device is also arranged to detect the flow of the original flue gas in real time as q, Nm3/h。
Preferably, the first pipeline is provided with a third concentration detection device for detecting SO in the desulfurized flue gas in real time2Has a concentration of c3, mg/Nm3. The clean flue gas exhaust pipe is provided with a fourth concentration detection device for detecting NO in the clean flue gas in real timeXHas a concentration of c4, mg/Nm3。
Preferably, the method further comprises the step of arranging a first valve between the first activated carbon conveying device and any one of the denitration units, and adjusting the first valve according to working conditions to control the addition amount of the activated carbon in any one of the denitration units. Or the discharge gate department of any denitration unit all is equipped with first valve, adjusts the active carbon addition amount of first valve control any denitration unit according to the operating mode.
Preferably, a second valve is arranged between the bypass activated carbon conveying device and any one of the desulfurization units, and the second valve is used for controlling the activated carbon adding amount of any one of the desulfurization units according to working conditions. Or the discharge port of any one of the desulfurization units is provided with a second valve, and the addition amount of the activated carbon of any one of the desulfurization units is controlled by the second valve according to the working condition.
Preferably, SO is set2Concentration discharge standard of CS，mg/Nm3. Setting NOx concentration emission standard to CN，mg/Nm3. When C3 is not less than CSThe circulating amount of the activated carbon of the desulfurizing tower is Z1 t/h. When C4 is not less than CNThe circulation amount of the activated carbon in the denitration tower is Z2 t/h. Calculating the circulation amount of the activated carbon in the desulfurizing tower:
Z1＝a*q*(c1-Cs)*S1*10-9… formula I.
Where a is a first system constant. S1 is the desulfurization value of activated carbon, mg/gAC.
Calculating the activated carbon circulation amount of the denitration tower:
Z2＝b*q*(c2-CN)*S2*10-9… formula II.
Where b is a second system constant. S2 is the denitration value of activated carbon, mg/gAC.
And adjusting the second valve to control the circulating quantity of the activated carbon delivered to the desulfurizing tower to be the calculated value Z1 of the formula I, t/h. And adjusting the first valve to control the circulation amount of the activated carbon conveyed to the denitration tower to be the calculated value Z2, t/h of the formula II. The circulating amount of the activated carbon in the analytical column was (Z1+ Z2).
Preferably, the circulation amount of the activated carbon to be fed to the denitration tower is controlled by controlling the opening time of the first valve. The opening time of the second valve is controlled to control the circulation quantity of the activated carbon conveyed to the desulfurizing tower through the bypass activated carbon conveying device. Or the discharge time of the denitration tower is controlled to control the circulation amount of the activated carbon entering the denitration tower. The discharge time of the desulfurizing tower is controlled to control the circulation amount of the active carbon entering the desulfurizing tower. The activated carbon circulation amount in the desorption tower is controlled by controlling the activated carbon blanking time of the desorption tower.
And setting the blanking time of the activated carbon of the desorption tower as T, h. The blanking time (i.e. the opening time of any one of the second valves) of each desulfurization unit is t2, h. The blanking time (i.e. the opening time of any one of the first valves) per denitration unit is t1, h.
The method specifically comprises the following steps:
t1 ═ T × Z2/[ n ═ (Z1+ Z2) ] … formula III.
T2 ═ T × Z1/[ m ═ (Z1+ Z2) ] … formula IV.
The opening time of the first valve is controlled to be the calculated value t1, h of formula III. The opening time of the second valve is controlled to be the calculated value t2, h of formula IV.
Preferably, the first system constant a is in the range of 0.5 to 3, preferably 1 to 2. S1 is 10 to 30, preferably 15 to 25. The second system constant b is between 0.8 and 6, preferably between 1.5 and 4. S2 is 5 to 10, preferably 8 to 15.
Generally, pollutants (SO) are adsorbed in the flue gas desulfurization and denitrification process, particularly in the desulfurization and denitrification process of sintered pellet flue gas2And NOx) is recycled after thermal regeneration treatment by an desorption tower, and a desulfurization tower and an activated carbon denitration tower are generally used in series in the prior art, that is, activated carbon after thermal regeneration treatment by the activated carbon desorption tower is conveyed to the denitration tower for denitration, and then the denitrated activated carbon is conveyed to the desulfurization tower for desulfurization treatment, and then the desulfurized activated carbon is conveyed to the activated carbon desorption tower for thermal regeneration and is recycled in sequence. However, because the raw flue gas volume and the pollutant concentration in the flue gas are different, and the flue gas volume and the pollutant difficulty are often fluctuated, the circulating volume of the activated carbon of the system needs to be set according to the maximum requirement (if the activated carbon volume required by desulfurization is larger than the activated carbon volume required by denitration, the activated carbon volume conveyed by the desorption tower is fed according to the activated carbon volume required by desulfurization, and then the activated carbon volume is sequentially subjected to denitration and desulfurization treatment by the denitration tower and the desulfurization tower, and if the activated carbon volume required by desulfurization is smaller than the activated carbon volume required by denitration, the activated carbon volume conveyed by the desorption tower is fed according to the activated carbon volume required by denitrationThe material is sequentially subjected to denitration and desulfurization treatment through a denitration tower and a desulfurization tower). Therefore, in order to meet the emission standard of the flue gas, the circulating amount of the activated carbon of the flue gas treatment system needs to be distributed according to the maximum circulating amount. This undoubtedly increases the adsorbent active carbon loss (active carbon abrasion loss), increasing the operating cost. Meanwhile, the circulation amount of the activated carbon in the denitration tower is increased, the moving speed of the activated carbon in the tower is accelerated, the dust emission concentration is increased, and the environment is polluted.
The utility model discloses in, through increasing bypass active carbon conveyor (the discharge gate of intercommunication analytic tower and the feed inlet of desulfurizing tower), change active carbon desulfurizing tower and active carbon denitration tower into parallelly connected by establishing ties, under the prerequisite of guaranteeing that the required active carbon of denitration tower is the best circulation volume, then carry out the cloth through bypass active carbon conveyor to the active carbon in the desulfurizing tower, make the required active carbon of desulfurization also reach the best circulation volume, the activity of system has been improved, the rational distribution to the accurate reposition of redundant personnel of active carbon desulfurizing tower and active carbon denitration tower cloth has been realized. Therefore, the aim of independently and accurately controlling the circulation quantity of the activated carbon of the desulfurization tower and the denitration tower is fulfilled, the loss of the activated carbon of the adsorbent is reduced, and the operating cost is reduced. Meanwhile, the circulation quantity of the activated carbon in the denitration tower can be reduced, the moving speed of the activated carbon in the tower is reduced, the dust emission concentration can be reduced, and the environmental protection index can be improved.
The utility model discloses in, because the pollutant concentration and the flow of former flue gas are the dynamic variable that changes in the operating condition, carry out scientific cloth to active carbon desulfurizing tower and active carbon denitration tower for further realizing the accuracy, the utility model discloses be provided with first concentration detection device in the former flue gas intake pipe, SO detects in the former flue gas in real time2Has a concentration of c1, mg/Nm3. A second concentration detection device is also arranged for detecting NO in the original smoke in real timeXHas a concentration of c2, mg/Nm3. The flow detection device is also arranged to detect the flow of the original flue gas in real time as q, Nm3H is used as the reference value. The first pipeline is provided with a third concentration detection device for detecting SO in the desulfurized flue gas in real time2Has a concentration of c3, mg/Nm3. Be provided with fourth concentration detection device real-time detection on clean flue gas exhaust pipe and go out cleanNO in flue gasXHas a concentration of c4, mg/Nm3。
Further, a first valve is arranged between the first activated carbon conveying device and any denitration unit, and the activated carbon adding amount of any denitration unit is controlled. And a second valve is arranged on the bypass activated carbon conveying device to control the addition amount of the activated carbon conveyed to the desulfurizing tower (or any desulfurizing unit) by the bypass activated carbon conveying device.
Further, SO is set2Concentration discharge standard of CS，mg/Nm3. Setting NOx concentration emission standard to CN，mg/Nm3. When C3 is not less than CSThe circulating amount of the activated carbon of the desulfurizing tower is Z1 t/h (namely the circulating amount of the optimal activated carbon when the desulfurizing effect reaches the standard). When C4 is not less than CNThe circulating amount of the activated carbon in the denitration tower is Z2, t/h (namely the circulating amount of the optimal activated carbon when the denitration effect reaches the standard). Then:
Z1＝a*q*(c1-Cs)*S1*10-9… formula I.
Where a is a first system constant (which may be self-learning variable depending on the system), preferably a is 0.5-3, more preferably 1-2. S1 is the desulfurization value of activated carbon, mg/gAC.
Z2＝b*q*(c2-CN)*S2*10-9… formula II.
Where b is a second system constant (which may be self-learning variable depending on the system), preferably b is 0.8 to 6, more preferably 1.5 to 4. S2 is the denitration value of activated carbon, mg/gAC.
And adjusting the second valve to control the circulating quantity of the activated carbon delivered to the desulfurizing tower to be the calculated value Z1 of the formula I, t/h. And adjusting the first valve to control the circulation amount of the activated carbon conveyed to the denitration tower to be the calculated value Z2, t/h of the formula II. The circulating amount of the activated carbon in the analytical column was (Z1+ Z2).
The utility model discloses in, in any unloading cycle time T (h), the activated carbon circulation volume of carrying to the denitration tower is controlled through the opening time of controlling first valve. The opening time of the second valve is controlled to control the circulation quantity of the activated carbon conveyed to the desulfurizing tower through the bypass activated carbon conveying device. Or the discharge time of the denitration tower is controlled to control the circulation amount of the activated carbon entering the denitration tower. The discharge time of the desulfurizing tower is controlled to control the circulation amount of the active carbon entering the desulfurizing tower. The activated carbon circulation amount in the desorption tower is controlled by controlling the activated carbon blanking time of the desorption tower.
And setting the blanking time of the activated carbon of the desorption tower as T, h. The blanking time (i.e. the opening time of any one of the second valves) of each desulfurization unit is t2, h. The blanking time (i.e. the opening time of any one of the first valves) per denitration unit is t1, h.
The method specifically comprises the following steps:
t1 ═ T × Z2/[ n ═ (Z1+ Z2) ] … formula III.
T2 ═ T × Z1/[ m ═ (Z1+ Z2) ] … formula IV.
The opening time of the first valve is controlled to be the calculated value t1, h of formula III. The opening time of the second valve is controlled to be the calculated value t2, h of formula IV.
Preferably, the technical scheme of the utility model is particularly suitable for the condition that the circulation volume demand of the active carbon in the denitration tower is less than the circulation volume demand of the active carbon in the desulfurization tower; that is to say, to handling special flue gas, sulfur oxide concentration is high in the flue gas and nitrogen oxide content is lower, handles this flue gas, and is great to the quantity of the required active carbon of desulfurization, and is less to the quantity of the required active carbon of denitration, the technical scheme of the utility model is particularly suitable for. In the prior art, the activated carbon trends are all 'analytic tower → denitration tower → desulfurization tower', and when the amount of activated carbon required by the denitration tower is less than that required by the desulfurization tower, in order to ensure the desulfurization and denitration effects, the circulation amount of the activated carbon is usually calculated and determined according to the maximum amount of the activated carbon required by the desulfurization and denitration, which causes the excessive circulation of the activated carbon in a treatment system, causes the waste of resources, and also causes unnecessary abrasion and consumption of the activated carbon. That is, in the solution of the prior art, in any one of the desulfurization tower and the denitration tower, the activated carbon of one of the devices (the desulfurization tower or the denitration tower) is always excessive, which causes waste of resources.
The technical scheme of the utility model, can be according to the specific characteristics of flue gas, through calculating the accurate demand of active carbon in desulfurizing tower and the denitration tower, then adopt the utility model discloses a system, accurate supplies active carbon for desulfurizing tower and denitration tower. Namely, on the basis of ensuring the effect of treating flue gas (desulfurization and denitration), the circulation amount of the activated carbon in the desulfurization tower and the denitration tower is accurately controlled, so that resources are saved, and unnecessary abrasion and consumption of the activated carbon are avoided.
Furthermore, adopt the technical scheme of the utility model, relative prior art scheme, the technical scheme of the utility model save a conveyor. In the prior art, 3 activated carbon conveying devices are provided, which are respectively an analytic tower → a denitration tower, a denitration tower → a desulfurization tower, and a desulfurization tower → an analytic tower. The technical scheme of the utility model in, active carbon conveyor is 2, is analytic tower → denitration tower and denitration tower, denitration tower and denitration tower → analytic tower respectively. According to engineering practice experience, the manufacturing cost of the activated carbon conveying device is 300-. Adopt the technical scheme of the utility model, saved 1 active carbon conveyor, reduced investment in earlier stage and later stage operation, maintenance cost.
In the utility model, S1 is the desulfurization value of activated carbon, mg/gAC. I.e. the removal of sulphide per gram of activated carbon is S1 mg. S2 is the denitration value of activated carbon, mg/gAC. Namely, the removal of nitrogen oxides per gram of the activated carbon is S2 mg. And AC represents activated carbon.
In the present invention, the height of the desorption column is 20 to 100m, preferably 25 to 80m, more preferably 30 to 60m, and still more preferably 40 to 50 m. The height of the desulfurization tower is 20 to 100m, preferably 30 to 80m, and more preferably 40 to 60 m. The height of the denitration tower is 20-100m, preferably 30-80m, and more preferably 40-60 m.
Compared with the prior art, the beneficial effects of the utility model are as follows:
the flue gas desulfurization and denitration activated carbon distribution system and the distribution method can be finely designed, SO that the activated carbon circulation volume of the desulfurization tower is adaptive to desulfurization (SO) in real time2) Function, the active carbon circulation volume of the denitration tower adapts to the function of removing NOx from the flue gas in real time, andadjusting at any time according to the smoke amount and the pollutant concentration; therefore, the independent and accurate control of the circulation quantity of the activated carbon of the desulfurization tower and the denitration tower is realized, the loss of the activated carbon of the adsorbent (the abrasion loss of the activated carbon) is reduced, and the operating cost is reduced. Meanwhile, the circulation quantity of the activated carbon in the denitration tower can be reduced, the moving speed of the activated carbon in the tower is reduced, the dust emission concentration can be reduced, and the environmental protection index can be improved.
Drawings
FIG. 1 is the utility model discloses a flue gas desulfurization denitration active carbon cloth system structure picture.
FIG. 2 is the control schematic diagram of flue gas desulfurization and denitration active carbon distributing system.
FIG. 3 is a control flow chart of the flue gas desulfurization and denitrification activated carbon distribution system.
Reference numerals: 1: a resolution tower; 2: a desulfurizing tower; 201: a desulfurization unit; 3: a denitration tower; 301: a denitration unit; 4: a first activated carbon delivery device; 5: a second activated carbon delivery device; 6: a bypass activated carbon delivery device; 7: an original flue gas inlet pipeline; 8: a clean flue gas inlet duct; c1: a first concentration detection device; c2: a second concentration detection device; c3: a third concentration detection means; c4: a fourth concentration detection means; m1: a first valve; m2: a second valve; q: a flow rate detection device.
Detailed Description
The technical solution of the present invention is illustrated below, and the claimed invention includes but is not limited to the following embodiments.
The utility model provides a flue gas desulfurization denitration active carbon cloth system, this system includes analytic tower 1, desulfurizing tower 2, denitration tower 3. According to the trend of the flue gas, the raw flue gas inlet pipe 7 is connected with the air inlet of the desulfurizing tower 2. And the exhaust port of the desulfurization tower 2 is connected with the air inlet of the denitration tower 3 through a first pipeline L1. And the exhaust port of the denitration tower 3 is connected with the purified flue gas exhaust pipe 8. The discharge hole of the desorption tower 1 is connected with the feed inlet of the denitration tower 3 through a first activated carbon conveying device 4. And the discharge port of the desulfurizing tower 2 is connected with the feed inlet of the desorption tower 1 through a second activated carbon conveying device 5. And a discharge outlet of the denitration tower 3 is directly connected with a feed inlet of the desorption tower 1 through a second activated carbon conveying device 5. And a bypass active carbon conveying device 6 is led out from the first active carbon conveying device 4 and is connected with a feed inlet of the desulfurizing tower 2.
Preferably, m desulfurization units 201 are arranged in the desulfurization tower 2. And n denitration units 301 are arranged in the denitration tower 3. Wherein: m and n are each independently 1 to 8, preferably 2 to 5.
Preferably, the raw flue gas inlet pipe 7 is provided with a first concentration detection device C1, a second concentration detection device C2, and a flow rate detection device Q. The first pipeline L1 is provided with a third concentration detection device C3. And a fourth concentration detection device C4 is arranged on the clean flue gas exhaust pipe 8.
Preferably, a first valve M1 is provided between the first activated carbon conveying device 4 and the denitration tower 3, or a first valve M1 is provided at a discharge outlet of the denitration tower 3.
Preferably, a first valve M1 is provided between the first activated carbon conveying device 4 and any one of the denitration units 301, or a first valve M1 is provided at a discharge port of any one of the denitration units 301.
Preferably, a second valve M2 is provided between the bypass activated carbon delivery device 6 and the desulfurization tower 2, or a second valve M2 is provided at the discharge outlet of the desulfurization tower 2.
Preferably, a second valve M2 is provided between the bypass activated carbon delivery device 6 and any one of the desulfurization units 201, or a second valve M2 is provided at the discharge port of any one of the desulfurization units 201.
Example 1
As shown in fig. 1, a flue gas desulfurization and denitrification activated carbon distribution system comprises a desorption tower 1, a desulfurization tower 2 and a denitrification tower 3. According to the trend of the flue gas, the raw flue gas inlet pipe 7 is connected with the air inlet of the desulfurizing tower 2. And the exhaust port of the desulfurization tower 2 is connected with the air inlet of the denitration tower 3 through a first pipeline L1. And the exhaust port of the denitration tower 3 is connected with the purified flue gas exhaust pipe 8. The discharge hole of the desorption tower 1 is connected with the feed inlet of the denitration tower 3 through a first activated carbon conveying device 4. And the discharge port of the desulfurizing tower 2 is connected with the feed inlet of the desorption tower 1 through a second activated carbon conveying device 5. And a discharge outlet of the denitration tower 3 is directly connected with a feed inlet of the desorption tower 1 through a second activated carbon conveying device 5. And a bypass active carbon conveying device 6 is led out from the first active carbon conveying device 4 and is connected with a feed inlet of the desulfurizing tower 2. The height of the analytical column 1 was 45 m.
Example 2
Example 1 was repeated except that 3 desulfurization units 201 were provided in the desulfurization tower 2.
Example 3
Example 2 was repeated except that 3 denitration units 301 were provided in the denitration tower 3.
Example 4
In the embodiment 3, as shown in fig. 2, the raw flue gas inlet pipe 7 is provided with a first concentration detection device C1, a second concentration detection device C2 and a flow rate detection device Q. The first pipeline L1 is provided with a third concentration detection device C3. And a fourth concentration detection device C4 is arranged on the clean flue gas exhaust pipe 8.
Example 5
Example 4 was repeated except that a first valve M1 was provided between the first activated carbon transfer device 4 and the denitration tower 3.
Example 6
Example 5 was repeated except that a first valve M1 was provided between the first activated carbon transfer device 4 and any of the denitration units 301.
Example 7
Example 6 was repeated except that a second valve M2 was provided between the bypass activated carbon transfer means 6 and the desulfurization tower 2.
Example 8
Example 7 was repeated except that a second valve M2 was provided between the bypass activated carbon transfer device 6 and any of the desulfurization units 201.
Claims (21)
1. The utility model provides a flue gas desulfurization denitration active carbon cloth system which characterized in that: the system comprises a desorption tower (1), a desulfurization tower (2) and a denitration tower (3); according to the trend of the flue gas, a raw flue gas inlet pipe (7) is connected with an air inlet of the desulfurizing tower (2); an exhaust port of the desulfurization tower (2) is connected with an air inlet of the denitration tower (3) through a first pipeline (L1); an exhaust port of the denitration tower (3) is connected with a clean flue gas exhaust pipe (8); the discharge hole of the desorption tower (1) is connected with the feed hole of the denitration tower (3) through a first activated carbon conveying device (4); the discharge port of the desulfurizing tower (2) is connected with the feed port of the desorption tower (1) through a second activated carbon conveying device (5); the discharge outlet of the denitration tower (3) is directly connected with the feed inlet of the desorption tower (1) through a second activated carbon conveying device (5); a bypass active carbon conveying device (6) is led out from the first active carbon conveying device (4) and is connected with a feed inlet of the desulfurizing tower (2);
wherein: the height of the desorption tower (1) is 20-100 m.
2. The system of claim 1, wherein: m desulfurization units (201) are arranged in the desulfurization tower (2); and n denitration units (301) are arranged in the denitration tower (3).
3. The system of claim 2, wherein: m and n are each independently 1 to 8.
4. The system of claim 2, wherein: m and n are each independently 2 to 5.
5. The system according to any one of claims 1-4, wherein: and a first concentration detection device (C1), a second concentration detection device (C2) and a flow detection device (Q) are arranged on the original flue gas inlet pipe (7).
6. The system according to any one of claims 1-4, wherein: the first pipeline (L1) is provided with a third concentration detection device (C3).
7. The system of claim 5, wherein: the first pipeline (L1) is provided with a third concentration detection device (C3).
8. The system according to any one of claims 1-4, 7, wherein: and a fourth concentration detection device (C4) is arranged on the clean flue gas exhaust pipe (8).
9. The system of claim 5, wherein: and a fourth concentration detection device (C4) is arranged on the clean flue gas exhaust pipe (8).
10. The system of claim 6, wherein: and a fourth concentration detection device (C4) is arranged on the clean flue gas exhaust pipe (8).
11. The system of any one of claims 1-4, 7, 9-10, wherein: a first valve (M1) is arranged between the first activated carbon conveying device (4) and the denitration tower (3) or a first valve (M1) is arranged at the discharge outlet of the denitration tower (3).
12. The system of claim 5, wherein: a first valve (M1) is arranged between the first activated carbon conveying device (4) and the denitration tower (3) or a first valve (M1) is arranged at the discharge outlet of the denitration tower (3).
13. The system of claim 6, wherein: a first valve (M1) is arranged between the first activated carbon conveying device (4) and the denitration tower (3) or a first valve (M1) is arranged at the discharge outlet of the denitration tower (3).
14. The system of claim 8, wherein: a first valve (M1) is arranged between the first activated carbon conveying device (4) and the denitration tower (3) or a first valve (M1) is arranged at the discharge outlet of the denitration tower (3).
15. The system according to any one of claims 2-4, wherein: a first valve (M1) is arranged between the first activated carbon conveying device (4) and any denitration unit (301) or a first valve (M1) is arranged at the discharge outlet of any denitration unit (301).
16. The system of any one of claims 1-4, 7, 9-10, 12-14, wherein: and a second valve (M2) is arranged between the bypass activated carbon conveying device (6) and the desulfurizing tower (2) or a second valve (M2) is arranged at the discharge outlet of the desulfurizing tower (2).
17. The system of claim 5, wherein: and a second valve (M2) is arranged between the bypass activated carbon conveying device (6) and the desulfurizing tower (2) or a second valve (M2) is arranged at the discharge outlet of the desulfurizing tower (2).
18. The system of claim 6, wherein: and a second valve (M2) is arranged between the bypass activated carbon conveying device (6) and the desulfurizing tower (2) or a second valve (M2) is arranged at the discharge outlet of the desulfurizing tower (2).
19. The system of claim 8, wherein: and a second valve (M2) is arranged between the bypass activated carbon conveying device (6) and the desulfurizing tower (2) or a second valve (M2) is arranged at the discharge outlet of the desulfurizing tower (2).
20. The system according to any one of claims 2-4, wherein: and a second valve (M2) is arranged between the bypass activated carbon conveying device (6) and any one of the desulfurization units (201) or a second valve (M2) is arranged at the discharge outlet of any one of the desulfurization units (201).
21. The system of claim 15, wherein: and a second valve (M2) is arranged between the bypass activated carbon conveying device (6) and any one of the desulfurization units (201) or a second valve (M2) is arranged at the discharge outlet of any one of the desulfurization units (201).
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