CN112403189B - Flue gas desulfurization and denitrification activated carbon distribution system and distribution method - Google Patents
Flue gas desulfurization and denitrification activated carbon distribution system and distribution method Download PDFInfo
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- CN112403189B CN112403189B CN202010128153.XA CN202010128153A CN112403189B CN 112403189 B CN112403189 B CN 112403189B CN 202010128153 A CN202010128153 A CN 202010128153A CN 112403189 B CN112403189 B CN 112403189B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
Abstract
The invention discloses a flue gas desulfurization and denitrification active carbon distribution system which comprises an analytic tower, a desulfurization tower and a denitrification tower. The original flue gas is processed by desulfurization and denitrification through a desulfurization tower and a denitrification tower in sequence. 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 gate of denitration tower passes through the third active carbon conveyor and links to each other with the feed inlet of desulfurizing tower. The first bypass active carbon conveying device is led out from the first active carbon conveying device and communicated to the third active carbon conveying device or communicated to a feed inlet of the desulfurizing tower. The invention realizes the independent and accurate control of the circulation amount of the activated carbon of the desulfurization tower and the denitration tower, reduces the loss of the activated carbon, and reduces the operation cost and the dust emission concentration.
Description
Technical Field
The invention relates to a flue gas treatment device technology, in particular to a flue gas desulfurization and denitrification activated carbon distribution system and a distribution method, and belongs to the technical field of flue gas purification.
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 activated carbon is as follows: the desorbed active carbon is conveyed to the second-stage adsorption tower by the second-stage tower feeding conveyor, part of pollutants are adsorbed by the active carbon and then conveyed to the first-stage adsorption tower by the first-stage tower feeding conveyor, and the active carbon adsorbed with the pollutants is conveyed to the desorption tower by the desorption tower feeding conveyor for cyclic utilization.
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.
SO due to each item (or given item at different times)2The 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 inventor provides a novel active carbon material flow process control method according to the raw smoke volume and the pollutant concentration, and the active carbon circulation volume of a first-stage adsorption tower can be adapted to the 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.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a flue gas desulfurization and denitrification activated carbon distribution systemThe scheme aims at the SO in the flue gas (such as sintering pellet flue gas) in the process of desulfurization and denitrification2The 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 purpose, the technical scheme adopted by the invention is as follows:
according to a first embodiment of the invention, a flue gas desulfurization and denitrification activated carbon distribution system is provided, and the system comprises a desorption tower, a desulfurization tower and a denitrification 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 connected with the feed inlet of the desulfurization tower through a third activated carbon conveying device. And a first bypass active carbon conveying device is led out from the first active carbon conveying device and communicated to the third active carbon conveying device or communicated to a feed inlet of the desulfurizing tower.
Preferably, a second bypass activated carbon conveying device is arranged at the upstream of the third activated carbon conveying device, and the second bypass activated carbon conveying device is connected to the second activated carbon conveying device.
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 third activated carbon conveying device and the desulfurizing tower.
Preferably, a second valve is arranged between the third activated carbon conveying device and any one of the desulfurization units.
Preferably, a third valve is arranged between the first bypass activated carbon conveying device and the desulfurizing tower, and a fourth valve is arranged on the second bypass activated carbon conveying device.
According to a second embodiment of the present invention, there is provided a method for performing a flue gas desulfurization and denitrification activated carbon distribution process by using the flue gas desulfurization and denitrification activated carbon distribution system of the first embodiment, the method comprising the steps of:
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 a desulfurization tower through a third activated carbon conveying device to perform desulfurization treatment on 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.
Wherein: and a first bypass active carbon conveying device is led out from the first active carbon conveying device, and a second bypass active carbon conveying device is led out from the upstream of the third active carbon conveying device.
Optionally, the first bypass activated carbon delivery device delivers activated carbon to a desulfurization tower for desulfurization of flue gas. The second bypass active carbon conveying device conveys the active carbon to the desorption tower for thermal regeneration treatment.
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 timeXIn a concentration of 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 or arranging a first valve at a discharge port of 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.
Preferably, a second valve is arranged between the third 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.
Preferably, the first bypass activated carbon delivery device is provided with a third valve, and the third valve controls the addition amount of the activated carbon delivered to the desulfurizing tower by the first bypass activated carbon delivery device according to working conditions.
Preferably, the second bypass activated carbon conveying device is provided with a fourth valve, and the fourth valve is adjusted according to working conditions to control the conveying amount of the activated carbon conveyed to the desorption tower by the second bypass activated carbon conveying device.
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.
Preferably, the circulating amount of the activated carbon in the analytical column is set to Z3. And (4) judging:
when Z1 is larger than Z2, the circulating amount of activated carbon in the desorption column, Z3, is adjusted to Z1. And opening the first valve, the second valve and the third valve, and closing the fourth valve. The material flow condition of the activated carbon is adjusted so that the circulating amount of the activated carbon conveyed to the denitration tower by the first activated carbon conveying device is Z2. The circulating quantity of the activated carbon conveyed to the desulfurizing tower through the first bypass activated carbon conveying device is (Z1-Z2). The circulating amount of the activated carbon conveyed to the desulfurizing tower by the third activated carbon conveying device is Z2.
When Z1 is Z2, the circulating amount of activated carbon in the desorption column, Z3 is Z1. And opening the first valve and the second valve, and closing the third valve and the fourth valve. And adjusting the material flow condition of the activated carbon so that the activated carbon sequentially passes through the desorption tower → the denitration tower → the desulfurization tower.
When Z1 is less than Z2, the circulating amount of the activated carbon in the desorption column is adjusted to Z2 from Z3. And opening the first valve, the second valve and the fourth valve, and closing the third valve. The flow conditions of the activated carbon were adjusted so that the circulating amount of the activated carbon conveyed to the denitration tower by the first activated carbon conveying device was Z2, and the circulating amount of the activated carbon conveyed to the desorption tower by the second bypass activated carbon conveying device was (Z2-Z1). The circulating amount of the activated carbon conveyed to the desulfurizing tower by the third activated carbon conveying device is Z1.
Preferably, 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 desulfurization tower is controlled to control the circulation amount of the activated carbon entering the desorption tower, the opening time of the third valve is controlled to control the circulation amount of the activated carbon conveyed to the desulfurization tower through the first bypass activated carbon conveying device, and the opening time of the fourth valve is controlled to control the circulation amount of the activated carbon conveyed to the desorption tower through the second bypass activated carbon conveying device. 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 method specifically comprises the following steps:
when Z1 is more than Z2, the circulating amount of the activated carbon of the denitration tower is Z2, and the circulating amount of the activated carbon of the desulfurization tower is Z1. The fourth valve is closed. The discharging time t1 for controlling any one denitration unit of the first valve-regulated denitration tower is as follows: t1 ═ T × Z2/(n × Z1). The opening time t3 for controlling the third valve is as follows: t3 ═ T (Z1-Z2)/Z1. Controlling the second valve to adjust the discharge time t2 of any desulfurization unit of the desulfurization tower as follows: t2 ═ T/m.
When Z1 is equal to Z2, the third and fourth valves are closed. The discharging time t1 for controlling any one denitration unit of the first valve-regulated denitration tower is as follows: t1 ═ T/n. Controlling the second valve to adjust the discharge time t2 of any desulfurization unit of the desulfurization tower as follows: t2 ═ T/m.
When Z1 < Z2, the third valve is closed. The circulating amount of the activated carbon of the denitration tower is Z2, and the circulating amount of the activated carbon of the desulfurization tower is Z1. The discharging time t1 for controlling any one denitration unit of the first valve-regulated denitration tower is as follows: t1 ═ T/n. The opening time t4 for controlling the fourth valve is: t4 ═ T (Z2-Z1)/Z2. Controlling the second valve to adjust the discharge time t2 of any desulfurization unit of the desulfurization tower as follows: t2 ═ Z1/(Z2 ×).
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.
In the present invention, "optionally" means performing or not performing, selectively adjusting according to actual working condition production requirements.
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, the raw flue gas amount and the pollutant concentration in the flue gas are different, and the flue gas amount and the pollutant difficulty are also fluctuated frequently, so the activated carbon circulation amount of the system needs to be set according to the maximum requirement. Generally, when the optimal circulation amount of the activated carbon required for desulfurization is larger than that required for denitration or when the optimal circulation amount of the activated carbon required for desulfurization is smaller than that required for denitration, the circulation amount of the activated carbon of the flue gas treatment system is distributed according to the maximum circulation amount (i.e., the optimal circulation amount of the activated carbon required for desulfurization) in order to meet the emission standards of flue gas. Further increasing the loss of the adsorbent active carbon and improving 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.
In the invention, on the basis of the serial connection of the activated carbon desulfurization tower and the activated carbon denitration tower, by adding the bypass activated carbon conveying device (communicating the discharge hole of the desorption tower with the feed inlet of the desulfurization tower and communicating the discharge hole of the denitration tower with the feed inlet of the desorption tower), on the premise of ensuring the optimum circulation amount of the activated carbon required by the denitration tower, the activated carbon conveyed into the desulfurization tower by the bypass activated carbon conveying device is supplemented or reduced, so that the optimum circulation amount of the activated carbon required by desulfurization is also achieved, the activity of the system is improved, and the reasonable distribution of the material distribution of the activated carbon desulfurization tower and the activated carbon denitration tower is realized. 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 total circulation volume of the activated carbon of the system can be reduced, the moving speed of the activated carbon in the desulfurization or denitration tower is reduced, the dust emission concentration can be reduced, and the environmental protection index can be improved.
In the invention, because the pollutant concentration and flow of the original flue gas in the actual working condition are dynamic variables which change, in order to further realize accurate scientific material distribution on the activated carbon desulfurization tower and the activated carbon denitration tower, the original flue gas inlet pipe is provided with the first concentration detection device which detects SO in the original 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 timeXIn a concentration of 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. 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。
Further, in order to realize the accurate distribution of the activated carbon for desulfurization and denitrification, a first valve is arranged between the first activated carbon conveying device and any one of the denitrification units, and the addition amount of the activated carbon in any one of the denitrification units is controlled by adjusting the first valve according to working conditions. And a second valve is arranged between the third activated carbon conveying device and any one of the desulfurization units, and the second valve is used for controlling the addition amount of the activated carbon of any one of the denitration units according to the working condition. And the third valve is used for controlling the addition amount of the activated carbon conveyed to the desulfurizing tower by the first bypass activated carbon conveying device according to the working condition. And a fourth valve is arranged on the second bypass activated carbon conveying device, and the fourth valve is adjusted according to the working condition to control the conveying amount of the activated carbon conveyed to the desorption tower by the second 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. When C4 is not more 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.
Wherein a is a first system constant (a is 0.5-3, preferably 1-2). S1 is the desulfurization value of activated carbon, mg/gAC (S1 is 10-30, preferably 15-25).
Calculating the activated carbon circulation amount of the denitration tower:
Z2＝b*q*(c2-CN)*S2*10-9… formula II.
Wherein b is a second system constant (b is 0.8 to 6, preferably 1.5 to 4). S2 is the denitration value of activated carbon, mg/gAC (S2 is 5-10, preferably 8-15).
In the present invention, the circulating amount of activated carbon in the analytical column was set to Z3. Then, judging:
when Z1 is larger than Z2, the circulating amount of activated carbon in the desorption column, Z3, is adjusted to Z1. And opening the first valve, the second valve and the third valve, and closing the fourth valve. The material flow condition of the activated carbon is adjusted so that the circulating amount of the activated carbon conveyed to the denitration tower by the first activated carbon conveying device is Z2. The circulating quantity of the activated carbon conveyed to the desulfurizing tower through the first bypass activated carbon conveying device is (Z1-Z2). The circulating amount of the activated carbon conveyed to the desulfurizing tower by the third activated carbon conveying device is Z2.
When Z1 is Z2, the circulating amount of activated carbon in the desorption column, Z3 is Z1. And opening the first valve and the second valve, and closing the third valve and the fourth valve. And adjusting the material flow condition of the activated carbon so that the activated carbon sequentially passes through the desorption tower → the denitration tower → the desulfurization tower.
When Z1 is less than Z2, the circulating amount of the activated carbon in the desorption column is adjusted to Z2 from Z3. And opening the first valve, the second valve and the fourth valve, and closing the third valve. The flow conditions of the activated carbon were adjusted so that the circulating amount of the activated carbon conveyed to the denitration tower by the first activated carbon conveying device was Z2, and the circulating amount of the activated carbon conveyed to the desorption tower by the second bypass activated carbon conveying device was (Z2-Z1). The circulating amount of the activated carbon conveyed to the desulfurizing tower by the third activated carbon conveying device is Z1.
In the invention, the activated carbon conveying device is continuous and uniform conveying equipment, only one point is blanked at the same time (namely only one certain desulfurization unit and/or denitration unit is blanked at the same time period), and the blanking amount can be accurately controlled by controlling the blanking time of each point. Therefore, the circulation quantity of the activated carbon entering the denitration tower is controlled by controlling the unloading time of the denitration tower, the circulation quantity of the activated carbon entering the desorption tower is controlled by controlling the unloading time of the desulfurization tower, the circulation quantity of the activated carbon conveyed to the desulfurization tower through the first bypass activated carbon conveying device is controlled by controlling the opening time of the third valve, and the circulation quantity of the activated carbon conveyed to the desorption tower through the second bypass activated carbon conveying device is controlled by controlling the opening time of the fourth valve. The activated carbon circulation amount in the desorption tower is controlled by controlling the activated carbon blanking time of the desorption tower.
In the present invention, the activated carbon feeding time in the analytical column is set to T (e.g., 1 hour, 3 hours, 5 hours, 10 hours, 20 hours, etc.) h. The method specifically comprises the following steps:
when Z1 is more than Z2, the circulating amount of the activated carbon of the denitration tower is Z2, and the circulating amount of the activated carbon of the desulfurization tower is Z1. The discharging time t1 for controlling any one denitration unit of the first valve-regulated denitration tower is as follows: t1 ═ T × Z2/(n × Z1), the opening time T3 for controlling the third valve is: t3 ═ T (Z1-Z2)/Z1. Controlling the second valve to adjust the discharge time t2 of any desulfurization unit of the desulfurization tower as follows: t2 ═ T/m.
When Z1 is equal to Z2, the third and fourth valves are closed. The discharging time t1 for controlling any one denitration unit of the first valve-regulated denitration tower is as follows: t1 ═ T/n. Controlling the second valve to adjust the discharge time t2 of any desulfurization unit of the desulfurization tower as follows: t2 ═ T/m.
When Z1 is less than Z2, the circulating amount of the activated carbon in the denitration tower is Z2, and the circulating amount of the activated carbon in the desulfurization tower is Z1. The discharging time t1 for controlling any one denitration unit of the first valve-regulated denitration tower is as follows: t1 ═ T/n. The opening time t4 for controlling the fourth valve is: t4 ═ T (Z2-Z1)/Z2. Controlling the second valve to adjust the discharge time t2 of any desulfurization unit of the desulfurization tower as follows: t2 ═ T × Z1/(Z2 × m).
In the present invention, S1 is the desulfurization number 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 the activated carbon, mg/gAC. I.e., the removal of nitrogen oxides per gram of 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 invention has the following beneficial effects:
the flue gas desulfurization and denitrification activated carbon distribution system and the distribution method can be designed finely, SO that the activated carbon circulation volume of the desulfurization tower can adapt to desulfurization (SO) in real time2) The method has the functions that the circulation volume of the activated carbon of the denitration tower is adapted to the function of removing NOx from the flue gas in real time, and is adjusted at any time according to the flue gas volume and the pollutant concentration; therefore, the independent and accurate control of the circulating amount of the activated carbon of the desulfurization tower and the denitration tower for the original flue gas treatment with different pollutant content compositions is realized, the loss (abrasion) of the activated carbon of the adsorbent is reduced, and the operating cost is reduced. Meanwhile, the total circulation volume of the activated carbon can be reduced, the moving speed of the activated carbon in the desulfurization or denitration tower is reduced, the dust emission concentration can be reduced, and the environmental protection index can be improved.
Drawings
FIG. 1 is a structural diagram of a flue gas desulfurization and denitrification activated carbon distribution system.
FIG. 2 is a control schematic diagram of the flue gas desulfurization and denitrification activated carbon distribution system.
FIG. 3 is a control flow chart of the flue gas desulfurization and denitrification activated carbon distribution system of the present invention.
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 third active carbon total dispersing device; 7: a first bypass activated carbon delivery device; 8: an original flue gas inlet pipeline; 9: a clean flue gas inlet duct; 10: a second bypass activated carbon delivery device; 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; m3: a third valve; m4: a fourth valve; q: a flow rate detection device.
Detailed Description
The technical solution of the present invention is illustrated below, and the claimed scope of the present invention includes, but is not limited to, the following examples.
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 8 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 a clean flue gas exhaust pipe 9. 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 the discharge outlet of the denitration tower 3 is connected with the feed inlet of the desulfurization tower 2 through a third activated carbon conveying device 6. And a first bypass activated carbon conveying device 7 is led out from the first activated carbon conveying device 4, and the first bypass activated carbon conveying device 7 is communicated to a third activated carbon conveying device 6 or communicated to a feed inlet of the desulfurizing tower 2.
Preferably, a second bypass activated carbon delivery device 10 is arranged upstream of the third activated carbon delivery device 6, and the second bypass activated carbon delivery device 10 is connected to the second activated carbon delivery device 5.
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 intake pipe 8 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. The clean flue gas exhaust pipe 9 is provided with a fourth concentration detection device C4.
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 third activated carbon delivery device 6 and the desulfurization tower 2.
Preferably, a second valve M2 is provided between the third activated carbon delivery device 6 and any one of the desulfurization units 201.
Preferably, a third valve M3 is provided between the first bypass activated carbon transfer device 7 and the desulfurization tower 2. The second bypass activated carbon conveying device 10 is provided with a fourth valve M4.
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 8 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 a clean flue gas exhaust pipe 9. The discharge hole of the desorption tower 1 is connected with the feed inlet of the denitration tower 3 through a first active 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 the discharge outlet of the denitration tower 3 is connected with the feed inlet of the desulfurization tower 2 through a third activated carbon conveying device 6. And a first bypass activated carbon conveying device 7 is led out from the first activated carbon conveying device 4, and the first bypass activated carbon conveying device 7 is communicated to a third activated carbon conveying device 6 or communicated to a feed inlet of the desulfurizing tower 2.
Example 2
Example 1 was repeated except that a second bypass activated carbon delivery device 10 was provided upstream of the third activated carbon delivery device 6, the second bypass activated carbon delivery device 10 being connected to the second activated carbon delivery device 5.
Example 3
Example 2 was repeated except that 3 desulfurization units 201 were provided in the desulfurization tower 2.
Example 4
Example 3 was repeated except that 3 denitration units 301 were provided in the denitration tower 3.
Example 5
In the embodiment 4, as shown in fig. 2, the raw flue gas inlet pipe 8 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. The clean flue gas exhaust pipe 9 is provided with a fourth concentration detection device C4.
Example 6
Example 5 was repeated except that a first valve M1 was provided between the first activated carbon transfer device 4 and the denitration tower 3.
Example 7
Example 6 was repeated except that a first valve M1 was provided between the first activated carbon feeding device 4 and any of the denitration units 301.
Example 8
Example 7 was repeated except that a second valve M2 was provided between the third activated carbon delivery device 6 and the desulfurization tower 2.
Example 9
Example 8 was repeated except that a second valve M2 was provided between the third activated carbon delivery device 6 and any of the desulfurization units 201.
Example 10
Example 9 was repeated except that a third valve M3 was provided between the first bypass activated carbon delivery apparatus 7 and the desulfurization tower 2.
Example 11
Example 10 was repeated except that the second bypass activated carbon conveying apparatus 10 was provided with a fourth valve M4.
Claims (13)
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 (8) 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 (9); 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 connected with the feed inlet of the desulfurization tower (2) through a third activated carbon conveying device (6); a first bypass activated carbon conveying device (7) is led out of the first activated carbon conveying device (4), and the first bypass activated carbon conveying device (7) is communicated to a third activated carbon conveying device (6) or a feed inlet of the desulfurizing tower (2); the upstream of the third activated carbon conveying device (6) is provided with a second bypass activated carbon conveying device (10), and the second bypass activated carbon conveying device (10) is connected to the second activated carbon conveying device (5).
2. The system of claim 1, wherein: m desulfurization units (201) are arranged in the desulfurization tower (2); n denitration units (301) are arranged in the denitration tower (3); wherein: m and n are each independently 1 to 8.
3. The system of claim 2, wherein: m and n are each independently 2 to 5.
4. The system of claim 1, wherein: a first concentration detection device (C1), a second concentration detection device (C2) and a flow detection device (Q) are arranged on the raw flue gas inlet pipe (8); a third concentration detection device (C3) is arranged on the first pipeline (L1); and a fourth concentration detection device (C4) is arranged on the clean flue gas exhaust pipe (9).
5. The system according to any one of claims 1-4, 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); and/or
A second valve (M2) is arranged between the third activated carbon conveying device (6) and the desulfurizing tower (2); and/or
And a third valve (M3) is arranged between the first bypass activated carbon conveying device (7) and the desulfurizing tower (2), and a fourth valve (M4) is arranged on the second bypass activated carbon conveying device (10).
6. The system of claim 5, 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); and/or
And a second valve (M2) is arranged between the third activated carbon conveying device (6) and any one of the desulfurization units (201).
7. The method for distributing the activated carbon for flue gas desulfurization and denitrification by using the activated carbon distribution system for flue gas desulfurization and denitrification according to any one of claims 1 to 6, characterized by comprising the following steps: the method comprises the following steps:
1) the raw flue gas is conveyed into a desulfurizing tower (2) through a raw flue gas inlet pipe (8) for desulfurization treatment; conveying the desulfurized flue gas subjected to desulfurization treatment to a denitration tower (3) through a first pipeline (L1) for denitration treatment; the purified flue gas after the denitration treatment is discharged through a purified flue gas exhaust pipe (9);
2) the activated carbon subjected to the thermal regeneration treatment in the desorption tower (1) is conveyed to a denitration tower (3) through a first activated carbon conveying device (4) to perform denitration treatment on the flue gas; the activated carbon after denitration treatment is conveyed to a desulfurization tower (2) through a third activated carbon conveying device (6) to carry out desulfurization treatment on the flue gas; the activated carbon after the desulfurization treatment is conveyed to the desorption tower (1) through a second activated carbon conveying device (5) for thermal regeneration treatment, and the circulation is carried out;
wherein: a first bypass active carbon conveying device (7) is led out from the first active carbon conveying device (4), and a second bypass active carbon conveying device (10) is led out from the upstream of the third active carbon conveying device (6); optionally, the first bypass active carbon conveying device (7) conveys active carbon to the desulfurizing tower (2) to desulfurize the flue gas; the second bypass active carbon conveying device (10) conveys the active carbon to the desorption tower (1) for heat regeneration treatment.
8. The method of claim 7, wherein: the method further comprises the following steps: a first concentration detection device (C1) is arranged on the raw flue gas inlet pipe (8) to detect SO in the raw flue gas in real time2Has a concentration of c1, mg/Nm3(ii) a A second concentration detection device (C2) is also arranged to detect NO in the original smoke in real timeXHas a concentration of c2, mg/Nm3(ii) a A flow detection device (Q) is also arranged for detecting the flow of the original flue gas in real time as Q, Nm3H; and/or
A third concentration detection device (C3) is arranged on the first pipeline (L1) to detect SO in the desulfurized flue gas in real time2Has a concentration of c3, mg/Nm3(ii) a The clean flue gas exhaust pipe (9) is provided with a fourth concentration detection device (C4) for detecting NO in the clean flue gas in real timeXHas a concentration of c4, mg/Nm3。
9. The method of claim 8, wherein: the method further comprises the following steps: 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), and the addition amount of activated carbon of any denitration unit (301) is controlled by adjusting the first valve (M1) according to working conditions; and/or
A second valve (M2) is arranged between the third activated carbon conveying device (6) and any one of the desulfurization units (201), and the addition amount of activated carbon of any one of the desulfurization units (201) is controlled by adjusting the second valve (M2) according to working conditions; and/or
The first bypass activated carbon conveying device (7) is provided with a third valve (M3), and the addition amount of activated carbon conveyed to the desulfurizing tower (2) by the first bypass activated carbon conveying device (7) is controlled by adjusting the third valve (M3) according to working conditions; and/or
And a fourth valve (M4) is arranged on the second bypass activated carbon conveying device (10), and the fourth valve (M4) is adjusted according to the working condition to control the activated carbon conveying amount of the second bypass activated carbon conveying device (10) conveyed to the desorption tower (1).
10. The method of claim 9, wherein: setting SO2Concentration discharge standard of CS，mg/Nm3(ii) a Setting NOx concentration emission standard to CN，mg/Nm3(ii) a When C3 is not less than CSThe circulation amount of the activated carbon of the desulfurizing tower (2) is Z1 t/h; when C4 is not less than CNThe circulation amount of the activated carbon in the denitration tower (3) is Z2, t/h; calculating the circulation quantity of the activated carbon in the desulfurizing tower (2):
Z1＝a*q*(c1-Cs)*S1*10-9.. formula I;
wherein 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 (3):
Z2＝b*q*(c2-CN)*S2*10-9… formula II;
wherein b is a second system constant; s2 is the denitration value of the activated carbon, mg/gAC;
setting the circulation quantity of the activated carbon in the analysis tower (1) as Z3; and (4) judging:
when Z1 is greater than Z2, the circulating amount of activated carbon Z3 in the analytical column (1) is adjusted to Z1; opening the first valve (M1), the second valve (M2), the third valve (M3), closing the fourth valve (M4); adjusting the material flow condition of the activated carbon so that the circulation quantity of the activated carbon conveyed to the denitration tower (3) by the first activated carbon conveying device (4) is Z2; the circulation quantity of the activated carbon conveyed to the desulfurizing tower (2) by the first bypass activated carbon conveying device (7) is (Z1-Z2); the circulating quantity of the activated carbon conveyed to the desulfurizing tower (2) by the third activated carbon conveying device (6) is Z2;
when Z1 is Z2, the circulating amount of activated carbon Z3 in the desorption column (1) is adjusted to Z1; opening the first valve (M1), the second valve (M2), closing the third valve (M3), the fourth valve (M4); the material flow condition of the activated carbon is adjusted, so that the activated carbon sequentially passes through a desorption tower (1) → a denitration tower (3) → a desulfurization tower (2);
when Z1 is less than Z2, adjusting the circulating quantity of the activated carbon Z3 to Z2 in the analysis tower (1); opening the first valve (M1), the second valve (M2), the fourth valve (M4), and closing the third valve (M3); adjusting the material flow condition of the activated carbon so that the circulating quantity of the activated carbon conveyed to the denitration tower (3) by the first activated carbon conveying device (4) is Z2, and the circulating quantity of the activated carbon conveyed to the desorption tower (1) by the second bypass activated carbon conveying device (10) is (Z2-Z1); the circulating amount of the activated carbon conveyed to the desulfurizing tower (2) by the third activated carbon conveying device (6) is Z1.
11. The method of claim 10, wherein: the circulation amount of the activated carbon entering the denitration tower (3) is controlled by controlling the unloading time of the denitration tower (3), and the circulation amount of the activated carbon entering the desorption tower (1) is controlled by controlling the unloading time of the desulfurization tower (2); controlling the circulation amount of the activated carbon delivered to the desulfurization tower (2) through the first bypass activated carbon delivery device (7) by controlling the opening time of the third valve (M3); controlling the circulation amount of the activated carbon delivered to the desorption tower (1) through the second bypass activated carbon delivery device (10) by controlling the opening time of the fourth valve (M4); the activated carbon circulation amount in the desorption tower (1) is controlled by controlling the activated carbon blanking time of the desorption tower (1); setting the blanking time of the activated carbon of the analysis tower (1) as T, h; the method specifically comprises the following steps:
when Z1 is more than Z2, the circulating amount of the activated carbon of the denitration tower (3) is Z2, and the circulating amount of the activated carbon of the desulfurization tower (2) is Z1; controlling the first valve (M1) to adjust the discharge time t1 of any denitration unit (301) of the denitration tower (3) as follows: t1 ═ T × Z2/(n × Z1), the opening time T3 for controlling the third valve (M3) is: t3 ═ T (Z1-Z2)/Z1; controlling the second valve (M2) to adjust the discharge time t2 of any desulfurization unit (201) of the desulfurization tower (2) to be: t2 ═ T/m;
when Z1 is Z2, the third valve (M3) and the fourth valve (M4) are closed; controlling the first valve (M1) to adjust the discharge time t1 of any denitration unit (301) of the denitration tower (3) as follows: t1 ═ T/n; controlling the second valve (M2) to adjust the discharge time t2 of any desulfurization unit (201) of the desulfurization tower (2) to be: t2 ═ T/m;
when Z1 is less than Z2, the circulating amount of the activated carbon of the denitration tower (3) is Z2, and the circulating amount of the activated carbon of the desulfurization tower (2) is Z1; controlling the first valve (M1) to adjust the discharge time t1 of any denitration unit (301) of the denitration tower (3) as follows: t1 ═ T/n; the opening time t4 of the fourth valve (M4) is controlled as follows: t4 ═ T (Z2-Z1)/Z2; controlling the second valve (M2) to adjust the discharge time t2 of any desulfurization unit (201) of the desulfurization tower (2) to be: t2 ═ T × Z1/(Z2 × m).
12. The method of claim 11, wherein: a is 0.5 to 3; s1 is 10-30; b is 0.8 to 6; and S2 is 5-10.
13. The method of claim 11, wherein: a is 1-2; s1 is 15-25; b is 1.5 to 4; and S2 is 8-15.
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