CN109126408B - Wet desulfurization device and intelligent control method - Google Patents
Wet desulfurization device and intelligent control method Download PDFInfo
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- CN109126408B CN109126408B CN201811200022.7A CN201811200022A CN109126408B CN 109126408 B CN109126408 B CN 109126408B CN 201811200022 A CN201811200022 A CN 201811200022A CN 109126408 B CN109126408 B CN 109126408B
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 85
- 230000023556 desulfurization Effects 0.000 title claims abstract description 85
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000002002 slurry Substances 0.000 claims abstract description 85
- 238000010521 absorption reaction Methods 0.000 claims abstract description 53
- 238000005457 optimization Methods 0.000 claims abstract description 35
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 74
- 239000003546 flue gas Substances 0.000 claims description 74
- 239000010440 gypsum Substances 0.000 claims description 66
- 229910052602 gypsum Inorganic materials 0.000 claims description 66
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 49
- 239000007787 solid Substances 0.000 claims description 45
- 238000000926 separation method Methods 0.000 claims description 42
- 230000001105 regulatory effect Effects 0.000 claims description 27
- 238000001914 filtration Methods 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 25
- 235000019738 Limestone Nutrition 0.000 claims description 13
- 239000006028 limestone Substances 0.000 claims description 13
- 230000003647 oxidation Effects 0.000 claims description 13
- 238000007254 oxidation reaction Methods 0.000 claims description 13
- 238000004364 calculation method Methods 0.000 claims description 9
- 239000000446 fuel Substances 0.000 claims description 9
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 7
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 7
- 239000004571 lime Substances 0.000 claims description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 230000007175 bidirectional communication Effects 0.000 claims description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 5
- 238000001514 detection method Methods 0.000 claims description 5
- 229910052717 sulfur Inorganic materials 0.000 claims description 5
- 239000011593 sulfur Substances 0.000 claims description 5
- 230000001276 controlling effect Effects 0.000 claims description 4
- 230000003009 desulfurizing effect Effects 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 3
- 230000007423 decrease Effects 0.000 claims 1
- 230000008676 import Effects 0.000 claims 1
- 239000003245 coal Substances 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000000779 smoke Substances 0.000 description 5
- 238000013461 design Methods 0.000 description 4
- 238000011217 control strategy Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000007257 malfunction Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000000844 transformation Methods 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- 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
- B01D53/30—Controlling by gas-analysis apparatus
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/346—Controlling the process
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/608—Sulfates
-
- 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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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
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Abstract
The invention discloses a wet desulfurization device and an intelligent control method, wherein the wet desulfurization device comprises a boiler 1, a desulfurization absorption tower 5, a slurry circulating pump group 7 and intelligent control, wherein the intelligent control comprises a distributed control server and an optimization controller.
Description
Technical Field
The invention relates to a wet desulfurization device, in particular to an intelligent control method of the wet desulfurization device, and belongs to the technical field of flue gas purification.
Background
At present, most of domestic wet desulfurization control systems for power plants realize PID automatic control of the PH value, but the control of the desulfurization rate is still in an open loop regulation state, and the PH value needs to be manually set to control the desulfurization rate, so that great operation burden is brought to operators.
The flue gas reaction of the desulfurization absorption tower is a large-lag and slow-dynamic process, the conventional PID control strategy is not ideal for the PH value control quality, operators can always remove the manual operation, and the blind area of the absorption tower is easy to occur by directly adjusting the limestone slurry flow regulating valve for intervention.
With the increasingly strict environmental protection requirements, the future desulfurization rate and export SO 2 The concentration is checked, however, the conventional control system cannot realize the function of closed-loop control, the desulfurization rate and the SO outlet 2 Multi-target closed loop control of concentration.
Most of the prior desulfurization control optimization systems have some problems, including 1) SO at the inlet and outlet of a desulfurization tower collected by a control system 2 The concentration measurement value is not representative, has larger difference with the average value of the flue gas, and has the phenomenon of inverted hanging of the chimney measurement value and the desulfurizing tower outlet value; 2) As the AGC depth peak regulation is more frequent, the coal types are changeable, the desulfurization system control optimization system continuously worsens along with the time optimization effect, and the optimization target under the multi-factor change can not be met; 3) The prior optimized product mainly reduces the input amount of limestone, and rarely directly and effectively reduces the power consumption; 4) Failure of the sensor or the instrument and partial parameter distortion can cause malfunction of an optimal control system, even occurrence of out-of-standard emission; 5) At present, most slurry circulating pumps of wet desulfurization systems are controlled by switches, when the load and the smoke amount of a boiler are reduced greatly, a water pump is turned off, SO that the slurry circulating flow is suddenly reduced, and the SO at an outlet is further caused 2 Severe fluctuations even exceed the standard.
Disclosure of Invention
The invention aims to: in order to overcome the defects in the prior art, the invention provides a wet desulfurization device which comprises a boiler 1, a desulfurization absorption tower 5 and a slurry circulating pump set 7, wherein a first pipeline 13 branched by a main pipeline 16 of the boiler 1 is connected with a flue gas inlet below the desulfurization absorption tower 5, the lower part of the desulfurization absorption tower 5 extends to a lime slurry tank 10 through a second pipeline 14, fresh slurry in the lime slurry tank 10 enters the desulfurization absorption tower 5 for reaction, and then enters the desulfurization absorption tower 5 for reaction after being circularly treated by the slurry circulating pump set 7 connected with the desulfurization absorption tower 5, the bottom of the desulfurization absorption tower 5 extends to a gypsum filtering liquid pond 12 through a gypsum separation branch 15, the gypsum filtering liquid pond is also a gypsum recovery pond, solid gypsum is left in the pond, and filtrate is circularly used. One side of the desulfurization absorption tower 5 is also connected with a variable-frequency oxidation fan 3 through a pipeline, a variable-frequency booster fan 2 is arranged on a first pipeline 13, a variable-frequency fresh slurry pump 4 is arranged on a second pipeline 14, and a gypsum separation branch electric regulating valve 6 and a gypsum separation water pump 11 are arranged on a gypsum separation branch 15.
Further, the slurry circulating pump set 7 at least comprises three water pumps, wherein any one water pump is a variable-frequency water pump, and the others are common water pumps.
Further, SO is arranged at the flue gas inlet 17 2 Concentration detection device and flue gas flowmeter.
Further, the main pipeline 16 is provided with an induced draft fan 9; the boiler is connected with the chimney 8 through a main pipeline 16; the chimney 8 is also connected with the top of the desulfurization absorption tower 5 for absorbing the flue gas discharged from the desulfurization absorption tower 5.
In order to achieve the purpose of intelligently controlling the wet desulfurization device, the system stable operation requirement can be better met under the condition of changeable coal types by a prediction means, and the technical scheme of the invention further comprises the following steps:
the intelligent control method of the wet desulfurization device is characterized in that a control system of the device comprises a distributed control server which is in bidirectional communication connection with a variable-frequency water pump, a variable-frequency fan and a separation branch electric regulating valve 6, and the distributed control server and an optimization controller also realize bidirectional communication, and the intelligent control method is characterized by comprising the following steps:
controlling step A, SO 2 SO detected by the concentration detection device at the position of the flue gas inlet 17 of the desulfurization absorption tower 5 2 The concentration is a, the flue gas flow detected by the flue gas flowmeter at the position of the flue gas inlet 17 of the desulfurization absorption tower 5 is b, the load flue gas flow of the boiler 1 is c, the distributed control server transmits the parameters a and b to the optimization controller in real time, the optimization controller makes an optimization control command according to the control logic A and transmits the optimization control command to the distributed control server, and the distributed control server turns on or off a common water pump in the slurry circulating pump group 7;
a control step B, when the reduction amplitude of the flue gas flow detected by the flue gas flowmeter exceeds 10%, the optimization controller makes an optimization command according to a control logic B, wherein the control logic B comprises the steps of adjusting the flow of fresh limestone slurry to d, and after a delay time of 10s, the distributed control server respectively controls and adjusts the loads of the variable-frequency booster fan 2, the variable-frequency oxidation fan 3 and the variable-frequency fresh limestone slurry pump 4 in the same proportion;
the control step C, the solid concentration sensor transmits the solid concentration parameter information to the distributed control server, the distributed control server optimizes the parameter information to the controller, and the optimizing controller makes an optimizing command according to the control logic C;
a control step D, wherein the distributed control server respectively controls the air supply quantity L1 of the boiler 1, the fuel mass consumption rate W1 (unit kg/s), and the mass fractions of sulfur, carbon, hydrogen, oxygen and nitrogen elements in the fuel to be Sa, ca, ha, O in real time a 、N a The monitoring data (unit%) are transmitted to an optimization controller, and the boiler air supply quantity L1 (unit m) is obtained through the following calculation formula 3 ) The amount of smoke per second V1 (unit m) 3 ):
V1= (1.867ca+11.2ha+0.7sa+0.8na+ (1-0.21/α) L1) W1; wherein α= (0.0889 (ca+0.375 Sa) +0.265Ha-0.033 Oa)/L1.
The SO in the flue gas is obtained by the following calculation formula 2 Concentration P (unit kg/Nm) 3 )：
P＝3.33Sa*W1/V1；
Wherein V1 is the real-time fuel consumption rate, and V1 is the smoke amount calculated according to the coal quality data;
after the optimization controller obtains P, V data, the flow rate d (unit m) of the limestone slurry is adjusted in advance according to the control step B before the changed flue gas reaches the desulfurizing tower 3 /s)。
Further, the control logic a in the control step a includes the following:
(1) When a is less than 0.7 e c, 1/4 of the total water pump in the circulating slurry pump set is closed;
(2) When a is less than 0.45 e c, 1/2 of the total number of circulating slurry pumps is closed;
(3) When a is less than 0.2 e c, 3/4 of the total number of circulating slurry pumps is closed;
(4) When a is greater than 0.7 e c, 1/4 of the total number of circulating slurry pumps is started;
(5) When a is greater than 0.45 e c, 1/2 of the total number of circulating slurry pumps is started;
(6) When a is equal to b >0.2 e c, 3/4 of the total circulating slurry pumps are started;
wherein a is the SO of the flue gas detected by the sensor at the position of the flue gas inlet 17 of the desulfurization absorption tower 5 2 The concentration b is the flue gas flow detected by the flue gas flowmeter at the position of the flue gas inlet 17 of the desulfurization absorption tower 5, c is the flue gas flow under the design load of the boiler 1, and e is the SO (sulfur separation) combustion flue gas of the boiler 1 design coal 2 Concentration. The closed water pump is a common water pump in the circulating slurry pump set. Calculating the number of closed circulating slurry pumps according to rounding value, namely if the calculated number is 0.25, not closing the water pump in the circulating slurry pump group; if the calculated number is 0.75, the ordinary water pump in a circulating slurry pump set is turned off, and the like.
When the water pump is controlled to start and stop according to the control logic A, when the second water pump in the slurry circulating pump set is required to be closed, the distributed control server starts the variable-frequency water pump firstly, then closes the second water pump, and then gradually reduces the working frequency of the variable-frequency water pump until the variable-frequency water pump is closed, and the variable-frequency water pump plays a role of slow adjustment, so that cliff-type start and stop are avoided.
Further, the calculation formula of d is:
d＝(-0.0000002*a 2 *b 2 +0.0051*a*b-0.1312)*0.25
wherein a is the SO of the flue gas detected by the sensor at the position of the flue gas inlet 17 of the desulfurization absorption tower 5 2 Concentration in mg/Nm 3 B is the flue gas flow detected by the flue gas flowmeter at the position of the flue gas inlet 17 of the desulfurization absorption tower 5, and the unit is Nm 3 。
After 10s delay time, the desulfurization distributed control server adjusts and reduces the loads of the variable-frequency booster fan 2, the variable-frequency oxidation fan 3 and the variable-frequency fresh limestone slurry pump 4 respectively, so that the flue gas flow rate in the desulfurization absorption tower 5 and the CaS0 in the fresh slurry are realized 3 The oxidation rate and the pH of the circulating slurry in the desulfurization absorbing tower 5 are maintained within the designed range, and the pH is in the range of 5.1 to 5.68.
Further, the control logic C in the control step C includes the following:
(1) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid tank 12 is within the range of 13-15%, the distributed control server adjusts and increases the opening of the gypsum separation branch electric regulating valve 6, and increases the flow to 110% of the flow before the separation branch electric regulating valve 6 adjusts, and the flow is I at the moment;
(2) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid tank 12 is in the range of 15-17%, the distributed control server adjusts and increases the opening of the gypsum separation branch electric regulating valve 6, and increases the flow to 110% of the flow I; at this time, the flow rate is II;
(3) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid tank 12 exceeds 17%, the distributed control server adjusts and increases the opening of the gypsum separation branch electric regulating valve (6) and increases the flow rate to 115% of the flow rate II; the flow is III at this time;
(4) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid tank 12 is reduced to be within the range of 15% -17%, the distributed control server adjusts and reduces the opening of the gypsum separation branch electric regulating valve 6, and reduces the flow to 87% of the flow III; the flow is IV at this point;
(5) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid tank 12 is reduced to be within a range of 13-15%, the distributed control server adjusts and reduces the opening of the gypsum separation branch electric regulating valve 6, and reduces the flow to 90.9% of the flow IV; at this time, the flow is V;
(6) When the solid concentration sensor detects that the percentage of the solid volume concentration of the circulating slurry in the gypsum filtration pond 12 is reduced to 13% or less, the distributed control server adjusts and reduces the opening of the gypsum separation branch electric control valve 6, and reduces the flow rate to 90.9% of the flow rate V.
The beneficial effects are that: 1) Through all transforming booster fan, oxidation fan, fresh slurry pump, a slurry circulating pump in the circulating slurry pump group into the frequency conversion, reduce the operation power consumption by a wide margin, make the system adjust operation more steady.
2) The intelligent control algorithm of the predictive control model is added into the existing desulfurization control system, and the requirements of AGC depth peak regulation and variable coal types, system operation stability and export SO are better met through a predictive means 2 The fluctuation standard deviation is reduced, and the SO at the outlet is properly improved under the condition of meeting the emission requirement 2 The consumption of limestone raw materials can be greatly reduced by setting values.
3) Through increasing electric control valve at gypsum separation branch road, effectively reduce equipment wearing and tearing and fault rate, guarantee the purity and the desulfurization rate of accessory product gypsum simultaneously.
4) The intelligent control algorithm of the MPC (predictive control model) has good fault tolerance, and can still enable the control system to stably run under the conditions of equipment parameter distortion and sensor faults, so as to avoid entering blind areas and exceeding emission accidents.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
In the figure: the device comprises a boiler, a booster fan, an oxidation fan, a fresh slurry pump, a desulfurization absorption tower, an electric regulating valve for a gypsum separation branch, a slurry circulating pump set, a chimney, a draught fan, a lime slurry tank, a gypsum separation water pump, a gypsum filtration liquid tank, a first pipeline, a second pipeline, a gypsum separation branch, a main pipeline and a flue gas inlet.
Detailed Description
The invention will be further described with reference to the accompanying drawings.
The invention provides a wet desulfurization device which comprises a boiler 1, a desulfurization absorption tower 5 and a slurry circulating pump set 7, wherein the boiler 1 is connected with a flue gas inlet below the desulfurization absorption tower 5 through a first pipeline 13 branched by a main pipeline 16, the lower part of the desulfurization absorption tower 5 extends to a lime slurry tank 10 through a second pipeline 14, fresh slurry in the lime slurry tank 10 enters the desulfurization absorption tower 5 for reaction, then enters the desulfurization absorption tower 5 for reaction after being circularly treated through the slurry circulating pump set 7 connected with the desulfurization absorption tower 5, the bottom of the desulfurization absorption tower 5 extends to a gypsum filtering liquid pool 12 through a gypsum separation branch 15, the gypsum filtering liquid pool is also a gypsum recovery pool, solid gypsum is left in the pool, and filtrate is recycled. One side of the desulfurization absorption tower 5 is also connected with a variable-frequency oxidation fan 3 through a pipeline, a variable-frequency booster fan 2 is arranged on a first pipeline 13, a variable-frequency fresh slurry pump 4 is arranged on a second pipeline 14, and a gypsum separation branch electric regulating valve 6 and a gypsum separation water pump 11 are arranged on a gypsum separation branch 15. The slurry circulating pump set 7 comprises three water pumps, wherein any one water pump is a variable-frequency water pump, and the other water pumps are common water pumps. SO is arranged at the flue gas inlet 17 2 Concentration detection device and flue gas flowmeter. The main pipeline 16 is provided with an induced draft fan 9; the boiler is connected with the chimney 8 through a main pipeline 16; the chimney 8 is also connected with the top of the desulfurization absorption tower 5 for absorbing the flue gas discharged from the desulfurization absorption tower 5.
The invention also provides an intelligent control method of the wet desulfurization device, the control system of the device comprises a distributed control server which is connected with the variable-frequency water pump in a bidirectional communication way, and the distributed control server and the optimization controller also realize the bidirectional communication, and the intelligent control method is characterized by comprising the following steps:
controlling step A, SO 2 SO detected by the concentration detection device at the position of the flue gas inlet 17 of the desulfurization absorption tower 5 2 The concentration is a, the flue gas flow detected by the flue gas flowmeter at the position of the flue gas inlet 17 of the desulfurization absorption tower 5 is b, the load flue gas flow of the boiler 1 is c, the distributed control server transmits the parameters a and b to the optimization controller in real time, the optimization controller makes an optimization control command according to the control logic A and transmits the optimization control command to the distributed control server, and the distributed control server turns on or off a common water pump in the slurry circulating pump group 7;
(1) When a is less than 0.7 e c, 1/4 of the total water pump in the circulating slurry pump set is closed;
(2) When a is less than 0.45 e c, 1/2 of the total number of circulating slurry pumps is closed;
(3) When a is less than 0.2 e c, 3/4 of the total number of circulating slurry pumps is closed;
(4) When a is greater than 0.7 e c, 1/4 of the total number of circulating slurry pumps is started;
(5) When a is greater than 0.45 e c, 1/2 of the total number of circulating slurry pumps is started;
(6) When a is equal to b >0.2 e c, 3/4 of the total circulating slurry pumps are started;
wherein a is the SO of the flue gas detected by the sensor at the position of the flue gas inlet 17 of the desulfurization absorption tower 5 2 The concentration b is the flue gas flow detected by the flue gas flowmeter at the position of the flue gas inlet 17 of the desulfurization absorption tower 5, c is the flue gas flow under the design load of the boiler 1, and e is the SO (sulfur separation) combustion flue gas of the boiler 1 design coal 2 Concentration. The closed water pump is a common water pump in the circulating slurry pump set. Calculating the number of closed circulating slurry pumps according to rounding value, namely if the calculated number is 0.25, not closing the water pump in the circulating slurry pump group; if the calculated number is 0.75, the ordinary water pump in a circulating slurry pump set is turned off, and the like.
When the water pump is controlled to start and stop according to the control logic A, when the second water pump in the slurry circulating pump set is required to be closed, the distributed control server starts the variable-frequency water pump firstly, then closes the second water pump, and then gradually reduces the working frequency of the variable-frequency water pump until the variable-frequency water pump is closed, and the variable-frequency water pump plays a role of slow adjustment, so that cliff-type start and stop are avoided.
A control step B, when the reduction amplitude of the flue gas flow detected by the flue gas flowmeter exceeds 10%, the optimization controller makes an optimization command according to a control logic B, wherein the control logic B comprises the steps of adjusting the flow of fresh limestone slurry to d, and after a delay time of 10s, the distributed control server respectively controls and adjusts the loads of the variable-frequency booster fan 2, the variable-frequency oxidation fan 3 and the variable-frequency fresh limestone slurry pump 4 in the same proportion;
d has the following calculation formula:
d＝(-0.0000002*a 2 *b 2 +0.0051*a*b-0.1312)*0.25
wherein a is the SO of the flue gas detected by the sensor at the position of the flue gas inlet 17 of the desulfurization absorption tower 5 2 Concentration in mg/Nm 3 B is the flue gas flow detected by the flue gas flowmeter at the position of the flue gas inlet 17 of the desulfurization absorption tower 5, and the unit is Nm 3 。
After 10s delay time, the desulfurization distributed control server adjusts and reduces the loads of the variable-frequency booster fan 2, the variable-frequency oxidation fan 3 and the variable-frequency fresh limestone slurry pump 4 respectively, so that the flue gas flow rate in the desulfurization absorption tower 5 and the CaS0 in the fresh slurry are realized 3 The oxidation rate and the pH of the circulating slurry in the desulfurization absorbing tower 5 are maintained within the designed range, and the pH is in the range of 5.1 to 5.68.
The control step C, the solid concentration sensor transmits the solid concentration parameter information to the distributed control server, the distributed control server optimizes the parameter information to the controller, and the optimizing controller makes an optimizing command according to the control logic C;
the control logic C in the control step C includes the following:
(1) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid tank 12 is within the range of 13-15%, the distributed control server adjusts and increases the opening of the gypsum separation branch electric regulating valve 6, and increases the flow to 110% of the flow before the separation branch electric regulating valve 6 adjusts, and the flow is I at the moment;
(2) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid tank 12 is in the range of 15-17%, the distributed control server adjusts and increases the opening of the gypsum separation branch electric regulating valve 6, and increases the flow to 110% of the flow I; at this time, the flow rate is II;
(3) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid tank 12 exceeds 17%, the distributed control server adjusts and increases the opening of the gypsum separation branch electric regulating valve 6, and increases the flow rate to 115% of the flow rate II; the flow is III at this time;
(4) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid tank 12 is reduced to be within the range of 15% -17%, the distributed control server adjusts and reduces the opening of the gypsum separation branch electric regulating valve 6, and reduces the flow to 87% of the flow III; the flow is IV at this point;
(5) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid tank 12 is reduced to be within a range of 13-15%, the distributed control server adjusts and reduces the opening of the gypsum separation branch electric regulating valve 6, and reduces the flow to 90.9% of the flow IV; at this time, the flow is V;
(6) When the solid concentration sensor detects that the percentage of the solid volume concentration of the circulating slurry in the gypsum filtration pond 12 is reduced to 13% or less, the distributed control server adjusts and reduces the opening of the gypsum separation branch electric control valve 6, and reduces the flow rate to 90.9% of the flow rate V.
A control step D, wherein the distributed control server respectively controls the air supply quantity L1 of the boiler 1, the fuel mass consumption rate W1 (unit kg/S), and the mass fractions of sulfur, carbon, hydrogen, oxygen and nitrogen elements in the fuel to be S in real time a 、C a 、H a 、O a 、N a The monitoring data (unit%) are transmitted to an optimization controller, and the boiler air supply quantity L1 (unit m) is obtained through the following calculation formula 3 ) The amount of smoke per second V1 (unit m) 3 ):
V1= (1.867ca+11.2ha+0.7sa+0.8na+ (1-0.21/α) L1) W1; wherein α= (0.0889 (ca+0.375 Sa) +0.265Ha-0.033 Oa)/L1.
The SO in the flue gas is obtained by the following calculation formula 2 Concentration P (unit kg/Nm) 3 )：
P＝3.33Sa*W1/V1；
Wherein V1 is the real-time fuel consumption rate, and V1 is the smoke amount calculated according to the coal quality data;
after the optimization controller obtains P, V data, the flow rate d (unit m) of the limestone slurry is adjusted in advance according to the control step B before the changed flue gas reaches the desulfurizing tower 3 /s)。
According to the intelligent control method, the intelligent control model and the control loop are added by optimizing the control strategy of the desulfurization system in the optimization controller, meanwhile, part of hardware (fans, water pumps and valves) of the system is modified, and an intelligent closed-loop control algorithm of the predictive control model is added to realize intelligent control of the desulfurization system.
The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be appreciated by persons skilled in the art that the above embodiments are not intended to limit the invention in any way, and that all technical solutions obtained by means of equivalent substitutions or equivalent transformations fall within the scope of the invention.
Claims (4)
1. The utility model provides an intelligent control method of wet flue gas desulfurization device, wet flue gas desulfurization device includes boiler (1), desulfurization absorption tower (5) and thick liquid circulating pump package (7), first pipeline (13) that boiler (1) branch through trunk line (16) divide are connected with flue gas import (17) below desulfurization absorption tower (5), the below of desulfurization absorption tower (5) extends to lime mud pond (10) through second pipeline (14), fresh thick liquid in lime mud pond (10) gets into desulfurization absorption tower (5) after reacting, reentrant desulfurization absorption tower (5) after circulating treatment through thick liquid circulating pump package (7) that are connected with desulfurization absorption tower (5), the bottom of desulfurization absorption tower (5) is through gypsum separation branch road (15) extension to gypsum filtration pond (12), its characterized in that: one side of the desulfurization absorption tower (5) is also connected with a variable-frequency oxidation fan (3) through a pipeline, a variable-frequency booster fan (2) is arranged on the first pipeline (13), a variable-frequency fresh slurry pump (4) is arranged on the second pipeline (14), and a gypsum separation branch electric regulating valve (6) and a gypsum separation water pump (11) are arranged on the gypsum separation branch (15); at least three water pumps are contained in the slurry circulating pump set (7), wherein any one water pump is a variable-frequency water pump, and the others are common water pumps;
the control system of the device comprises a distributed control server which is in bidirectional communication connection with a variable-frequency water pump, a variable-frequency oxidation fan (3), a variable-frequency booster fan (2) and a gypsum separation branch electric regulating valve (6), and the distributed control server and an optimization controller also realize bidirectional communication, and is characterized by comprising the following steps:
controlling step A, SO 2 SO detected by the concentration detection device at the position of a flue gas inlet (17) of the desulfurization absorption tower (5) 2 The concentration is a, the flue gas flow detected by the flue gas flowmeter at the position of a flue gas inlet (17) of the desulfurization absorption tower (5) is b, the load flue gas flow of the boiler (1) is c, the distributed control server transmits parameters a and b to an optimization controller in real time, the optimization controller makes an optimization control command according to a control logic A and transmits the optimization control command to the distributed control server, and the distributed control server starts or closes a common water pump in the slurry circulating pump group (7);
a control step B, when the reduction amplitude of the flue gas flow detected by the flue gas flowmeter exceeds 10%, an optimization controller makes an optimization command according to a control logic B, wherein the control logic B comprises the steps of adjusting the flow d of fresh limestone slurry, and after 10s of delay time, a distributed control server respectively controls and adjusts and reduces the loads of a variable-frequency booster fan (2), a variable-frequency oxidation fan (3) and a variable-frequency fresh slurry pump (4) in the same proportion;
a control step C, wherein a solid concentration sensor detects the solid volume concentration percentage of circulating slurry in a gypsum filtering liquid pond (12) and transmits solid concentration parameter information to a distributed control server, the distributed control server transmits the parameter information to an optimization controller, the optimization controller makes an optimization command according to the control step C, and the distributed control server adjusts and increases or decreases the opening of an electric regulating valve (6) of a gypsum separation branch according to the parameter information;
in the control step D, the distributed control server transmits monitoring data of the air supply quantity L1 of the boiler (1), the fuel mass consumption rate W1 (unit kg/s) and the mass fractions of sulfur, carbon, hydrogen, oxygen and nitrogen elements in fuel as Sa, ca, ha, oa, na (unit%) to the optimization controller in real time, and the air supply quantity L1 (unit m) of the boiler is obtained through the following calculation formula, and the air quantity V1 (unit m) per second entering the desulfurization absorption tower after combustion is obtained:
V1=(1.867Ca+11.2Ha+0.7Sa+0.8Na+（1-0.21/α）L1)W1;
wherein α= (0.0889 (ca+0.375 Sa) +0.265Ha-0.033 Oa)/L1;
the SO in the flue gas is obtained by the following calculation formula 2 Concentration P (unit kg/Nm:
P=3.33Sa*W1/V1；
wherein W1 is the real-time fuel consumption rate;
after the optimizing controller obtains the data of P, V1, the flow d (unit m/s) of the fresh limestone slurry is adjusted in advance according to the control step B before the changed flue gas reaches the desulfurizing tower.
2. The intelligent control method of a wet desulfurization device according to claim 1, characterized by comprising the steps of: the calculation formula of d is as follows:
d=（-0.0000002*a 2 *b 2 +0.0051*a*b-0.1312）*0.25
wherein a is the SO of the flue gas detected by the sensor at the position of the flue gas inlet (17) of the desulfurization absorption tower (5) 2 The concentration is in mg/Nm and b is the flue gas flow detected by the flue gas flowmeter at the position of a flue gas inlet (17) of the desulfurization absorption tower (5), and the unit is Nm.
3. The intelligent control method of a wet desulfurization device according to claim 1, characterized by comprising the steps of: the control logic C in the control step C includes the following:
(1) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid pool (12) is in the range of 13% -15%, the distributed control server adjusts and increases the opening of the gypsum separation branch electric regulating valve (6) and increases the flow to 110% of the flow before the separation branch electric regulating valve (6) adjusts, and the flow is I;
(2) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid pond (12) is in the range of 15% -17%, the distributed control server adjusts and increases the opening of the gypsum separation branch electric regulating valve (6) and increases the flow to 110% of the flow I; at this time, the flow rate is II;
(3) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid pond (12) exceeds 17%, the distributed control server adjusts and increases the opening of the gypsum separation branch electric regulating valve (6) and increases the flow to 115% of the flow II; the flow is III at this time;
(4) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid pond (12) is reduced to be within the range of 15% -17%, the distributed control server adjusts and reduces the opening of the gypsum separation branch electric regulating valve (6) and reduces the flow to 87% of the flow III; the flow is IV at this point;
(5) When the solid concentration sensor detects that the solid volume concentration percentage of the circulating slurry in the gypsum filtering liquid pond (12) is reduced to be within a range of 13-15%, the distributed control server adjusts and reduces the opening of the gypsum separation branch electric regulating valve (6) and reduces the flow to 90.9% of the flow IV; at this time, the flow is V;
(6) When the solid concentration sensor detects that the solid concentration percentage of the circulating slurry in the gypsum filtering liquid tank (12) is reduced to be lower than 13%, the distributed control server adjusts and reduces the opening of the gypsum separation branch electric regulating valve (6) and reduces the flow to 90.9% of the flow V.
4. The intelligent control method of a wet desulfurization device according to claim 1, characterized by comprising the steps of: an induced draft fan (9) is arranged on the main pipeline (16); the boiler is connected with a chimney (8) through a main pipeline (16), and the chimney (8) is also connected with the top of the desulfurization absorption tower (5) to absorb the flue gas discharged from the desulfurization absorption tower (5).
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| CN110090534A (en) * | 2019-04-03 | 2019-08-06 | 红云红河烟草(集团)有限责任公司 | A kind of desulfurizing agent control detection method |
| CN110756036B (en) * | 2019-11-29 | 2024-02-06 | 苏州仕净科技股份有限公司 | Thermal power plant flue gas wet desulfurization system with multi-parameter monitoring function |
| CN111545023B (en) * | 2020-06-18 | 2022-04-01 | 河北化工医药职业技术学院 | Intelligent optimization system for limestone-gypsum wet flue gas desulfurization |
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