CN108730968B - Desulfurization control method and device - Google Patents
Desulfurization control method and device Download PDFInfo
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- CN108730968B CN108730968B CN201810619527.0A CN201810619527A CN108730968B CN 108730968 B CN108730968 B CN 108730968B CN 201810619527 A CN201810619527 A CN 201810619527A CN 108730968 B CN108730968 B CN 108730968B
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 42
- 230000023556 desulfurization Effects 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 41
- 235000019738 Limestone Nutrition 0.000 claims abstract description 96
- 239000006028 limestone Substances 0.000 claims abstract description 96
- 239000003245 coal Substances 0.000 claims abstract description 42
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 87
- 238000004590 computer program Methods 0.000 claims description 12
- 230000008569 process Effects 0.000 abstract description 10
- 238000006243 chemical reaction Methods 0.000 description 8
- 230000001276 controlling effect Effects 0.000 description 8
- 238000010586 diagram Methods 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 230000008859 change Effects 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 5
- 230000006870 function Effects 0.000 description 5
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- 239000000292 calcium oxide Substances 0.000 description 4
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 4
- 230000010354 integration Effects 0.000 description 4
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 3
- 238000004364 calculation method Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 230000002452 interceptive effect Effects 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 230000033228 biological regulation Effects 0.000 description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000010355 oscillation Effects 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000009738 saturating Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 230000004069 differentiation Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 230000007363 regulatory process Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
Abstract
The application provides a desulfurization control method and a desulfurization control device, wherein the method comprises the following steps: determining a prediction curve of SO2 discharge amount in a predetermined time period during the coal desulfurization process by the circulating fluidized bed boiler, wherein the prediction curve corresponds to a plurality of predicted values at a plurality of moments in the predetermined time period; and adjusting the limestone input amount of the circulating fluidized bed boiler according to the prediction curve. By adopting the technical scheme, the problem that the input amount of limestone cannot be timely and accurately adjusted when the circulating fluidized bed is used for coal desulfurization in the related technology is solved, the delay of adjusting the input amount of limestone according to the measured value of SO2 detected at a chimney is avoided, and the limestone input amount is properly controlled at each moment.
Description
Technical Field
The application relates to the field of chemical industry, in particular to a desulfurization control method and device.
Background
In the related technology, the most common desulfurizer for desulfurization in the circulating fluidized bed boiler is limestone in the combustion process, and limestone powder is conveyed into a hearth through a limestone feeder and a pipeline to carry out chemical reaction in the operation process so as to remove sulfur dioxide generated by coal combustion. The temperature in the circulating fluidized bed boiler is usually 830-900 ℃ in the operation process, limestone can fully generate roasting reaction at the temperature, calcium carbonate is decomposed into calcium oxide, and the calcium oxide and sulfur dioxide generated by coal combustion are subjected to salinization reaction to generate calcium sulfate which is discharged in a solid form to achieve the aim of desulfurization.
Limestone calcinations reaction equation:
CaCO3＝CaO+CO2heat quantity Q
The desulfurization reaction equation:
CaO+SO2+1/2O2＝CaSO4+ Heat quantity Q
FIG. 1 is a block diagram illustrating a conventional automatic in-furnace desulfurization control scheme of a circulating fluidized bed boiler according to the present application, and as shown in FIG. 1, the automatic in-furnace desulfurization control model generally adopted in the circulating fluidized bed boiler is a single-loop control scheme, which is controlled by a regulator pair SO2Target value "and" measured SO2And comparing the concentrations, performing PID (proportion integration differentiation) operation according to the deviation, outputting a corresponding control value to an operator, and outputting the control value to a limestone variable-frequency feeder through the operator.
Aiming at the problem that the input amount of limestone cannot be timely and accurately adjusted when a circulating fluidized bed is used for coal desulfurization in the related technology, no effective solution is available at present.
Disclosure of Invention
The embodiment of the application provides a desulfurization control method and device, which at least solve the problem that the input amount of limestone cannot be timely and accurately adjusted when a circulating fluidized bed is used for coal desulfurization in the related art.
According to an embodiment of the present application, there is provided a method of controlling desulfurization, including: determining a prediction curve of SO2 discharge amount of a predetermined time period in the coal desulfurization process through a circulating fluidized bed boiler, wherein the prediction curve corresponds to a plurality of predicted values at a plurality of moments of the predetermined time period; and adjusting the limestone input amount of the circulating fluidized bed boiler according to the prediction curve.
According to another embodiment of the present application, there is also provided a method of controlling desulfurization, the method further including: the control device of the circulating fluidized bed boiler detects the discharge amount of SO2 at regular time in each preset time interval of the desulfurization process; increasing limestone input to the circulating fluidized bed boiler upon determining that the amount of SO2 emissions exceeds an index.
According to another embodiment of the present application, there is also provided a desulfurization control apparatus including: the determining module is used for determining a prediction curve of SO2 discharge amount of a preset time period aiming at the circulating fluidized bed boiler, wherein a plurality of moments of the preset time period of the prediction curve correspond to a plurality of predicted values; and the adjusting module is used for adjusting the limestone input amount of the circulating fluidized bed boiler according to the prediction curve.
According to a further embodiment of the present application, there is also provided a storage medium having a computer program stored therein, wherein the computer program is arranged to perform the steps of any of the above method embodiments when executed.
According to yet another embodiment of the present application, there is also provided an electronic device, comprising a memory in which a computer program is stored and a processor arranged to run the computer program to perform the steps of any of the above method embodiments.
According to the method, a prediction curve of SO2 emission amount of a preset time period is determined in the coal desulfurization process of the circulating fluidized bed boiler, wherein the prediction curve corresponds to a plurality of prediction values at a plurality of moments of the preset time period; and adjusting the limestone input amount of the circulating fluidized bed boiler according to the prediction curve. By adopting the technical scheme, the problem that the input amount of limestone cannot be timely and accurately adjusted when the circulating fluidized bed is used for coal desulfurization in the related technology is solved, the delay of adjusting the input amount of limestone according to the measured value of SO2 detected at a chimney is avoided, and the limestone input amount is properly controlled at each moment.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this application, illustrate embodiment(s) of the application and together with the description serve to explain the application and not to limit the application. In the drawings:
FIG. 1 is a schematic block diagram of a conventional automatic in-furnace desulfurization control of a circulating fluidized bed boiler according to the present application;
FIG. 2 is a flow chart of a method of controlling desulfation according to an embodiment of the present application;
FIG. 3 is a schematic view of a furnace desulfurization control model of a circulating fluidized bed boiler according to the present application;
FIG. 4 is a schematic diagram of a target value intelligence given module according to the present application;
FIG. 5 is a schematic diagram of a look ahead prediction module according to the present application.
Detailed Description
The present application will be described in detail below with reference to the accompanying drawings in conjunction with embodiments. It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict.
It should be noted that the terms "first," "second," and the like in the description and claims of this application and in the drawings described above are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order.
The solution in the present document can be applied to the coal desulfurization scenario in industry, but is not limited thereto.
Example one
In the present embodiment, a method for controlling desulfurization is provided, which can be applied to an industrial automation controller, and fig. 2 is a flowchart of a method for controlling desulfurization according to an embodiment of the present application, and as shown in fig. 2, the flowchart includes the following steps:
step S202, determining a prediction curve of SO2 emission in a preset time period in the process of coal desulfurization by a circulating fluidized bed boiler, wherein the prediction curve corresponds to a plurality of prediction values at a plurality of moments in the preset time period;
the prediction curve of the current time period can be determined according to the emission of the SO2 before the preset time period, and the emission of the SO2 of the current time period can be used as the prediction basis of the future time period.
And step S204, adjusting the limestone input amount of the circulating fluidized bed boiler according to the prediction curve.
Optionally, the execution sequence of step S202 and step S204 may be interchanged, that is, step S204 may be executed first, and then step S202 may be executed.
Through the steps, determining a prediction curve of SO2 discharge amount of a preset time period in the coal desulfurization process of the circulating fluidized bed boiler, wherein the prediction curve corresponds to a plurality of prediction values at a plurality of moments of the preset time period; and adjusting the limestone input amount of the circulating fluidized bed boiler according to the prediction curve. By adopting the technical scheme, the problem that the input amount of limestone cannot be timely and accurately adjusted when the circulating fluidized bed is used for coal desulfurization in the related technology is solved, the delay of adjusting the input amount of limestone according to the measured value of SO2 detected at a chimney is avoided, and the limestone input amount is properly controlled at each moment.
Optionally, adjusting the limestone input of the circulating fluidized bed boiler according to the prediction curve comprises: acquiring an actual measurement value of SO2 emission at a moment; estimating a second value of the SO2 emission amount after a preset value is minutes according to the measured value at the moment; and adjusting the limestone input amount of the circulating fluidized bed boiler after a preset value is minutes according to the second value and a predicted value on a prediction curve of the second value at the same time.
The second value after the predetermined number of minutes is estimated by using the measured value of one time, which may be equivalent to the hysteresis module in the following embodiments.
Optionally, before the limestone input amount of the circulating fluidized bed boiler is adjusted, acquiring a target value of SO2 discharge amount of the preset time period; adjusting the limestone input of the circulating fluidized bed boiler comprises the following steps: and determining the limestone input amount at the current moment according to the prediction curve and the target value.
The predicted value in the prediction curve can be used to determine a value after deviation calculation with the target value, and then the limestone amount input at the current moment can be determined.
Optionally, adjusting the limestone input of the circulating fluidized bed boiler according to the prediction curve comprises: adjusting the limestone input of the circulating fluidized bed boiler according to the prediction curve and at least one of the following parameters of the circulating fluidized bed boiler: the coal quantity at the present moment, the bed temperature of the circulating fluidized bed and the air quantity entering the circulating fluidized bed boiler. The parameter of the air volume can be replaced by the oxygen volume entering the circulating fluidized bed boiler.
Optionally, adjusting the limestone input of the circulating fluidized bed boiler based on the prediction curve and at least one of the following parameters of the circulating fluidized bed boiler, including at least one of: when the coal amount is increased, increasing the limestone input amount according to the first corresponding relation; when the bed temperature of the circulating fluidized bed is increased, the input amount of the limestone is reduced according to the second corresponding relation; when the air volume increases, the limestone input amount is reduced according to the third correspondence relationship. In a specific embodiment, the limestone input amount can also be determined by comprehensively considering the three factors.
Optionally, the prediction curve is determined by a first regulator, and the prediction curve is input to a second regulator; regulating the limestone input amount by the second regulator according to the prediction curve and at least one of the parameters, and controlling an operator to input limestone to the circulating fluidized bed boiler according to the limestone input amount;
a first feedback device is arranged between the second regulator and the first regulator and used for feeding back the working state of the second regulator to the first regulator; and a second feedback device is arranged between the operator and the second regulator and used for feeding back the working state of the operator to the second regulator. The first feedback may prevent the main regulator from saturating with integration, and the second feedback may prevent the sub-regulator from saturating with integration.
According to another embodiment of the present application, there is also provided a method of controlling desulfurization, including the steps of:
step one, in each preset time interval of the desulfurization process, a control device of the circulating fluidized bed boiler regularly detects the emission of SO 2;
and step two, increasing limestone input of the circulating fluidized bed boiler when determining that the discharge amount of SO2 exceeds the standard.
By adopting the scheme, if the emission before the timing detection within a preset time interval exceeds the standard, the limestone input is immediately increased, the total SO2 emission within the preset time interval is reduced, the national detection standard is met, the problem that the emission of SO2 within a certain time period, such as 1 hour, in the related technology exceeds the standard is solved, and the emission of the circulating fluidized bed boiler reaches the standard is ensured.
The automatic control model for desulfurization generally adopted by the circulating fluidized bed boiler in the related art is single-loop control (see fig. 1), and the control principle is that a "regulator" is used for comparing a "target value of SO 2" with a "measured SO2 concentration", then PID (Proportion integration Differential, abbreviated as PID) operation is carried out according to the deviation, a corresponding control value is output to an "operator", and then the control value is output to a "limestone variable frequency feeder" through the "operator". This control method mainly has the following disadvantages:
1, a certain distance is reserved between a limestone feeder and a hearth; a certain distance is reserved between the hearth and an SO2 concentration measuring point at the chimney; the chemical reaction between the sprayed limestone powder and SO2 takes a certain time. Due to the three factors, a long time (usually 4-6 minutes) is required for the change of the concentration of the SO2 from the change of the rotating speed of the limestone feeder (namely, after the change of the amount of limestone) to the chimney, SO that a large delay exists in the measured SO2 concentration detected by the regulator, and the delay can cause the problems of oscillation of a control system, long time of the regulating process, large control deviation and the like.
2, SO2 generated in the combustion process of the circulating fluidized bed boiler mainly comes from coal, namely, is related to the quantity of the coal; the amount of the concentration value of SO2 carried in the flue gas is also related to the ratio (or oxygen amount) of the air volume to the coal amount; the efficiency of the limestone chemical reaction with SO2 is related to the "bed temperature". The traditional control model does not consider the factors as the lead values, so the timeliness of the control is poor.
3, limestone flow (or feeder rotational speed) does not participate in the control of the intermediate flow in the traditional single-loop control, belongs to semi-open loop control, and can not be identified by a control system in time when faults such as feeder jamming, limestone conveying system blockage, feeder nonlinearity and the like occur, so that the quality of the control system is easy to become poor or the control system cannot be put into operation.
4, SO in conventional Single Loop control2Target value is manually set by operator, because of SO by environmental protection department2The hourly mean value is critical (SO in 60 minutes per hour)2Average emission should not exceed environmental limits), when operators are in order to save limestone pairs "SO2Target value "set higher, and SO at the end of a certain hour2When the average value is higher, the final hour average value is possibly out of standard, so that the method is subjected to environmental protection examination.
In the conventional control method, the target value is generally set to be low, so that more limestone is used and the economy is poor.
The application designs a more reliable automatic control model for desulphurization in a circulating fluidized bed boiler, which can effectively avoid the problems.
The utility model designs a novel automatic control model of desulfurization in circulating fluidized bed boiler stove, and figure 3 is according to the control model schematic diagram of desulfurization in circulating fluidized bed boiler stove of this application, as shown in figure 3, the model comprises several parts such as "target value intelligence gives the module", "advance prediction module", "two-stage regulator control", "coal volume, bed temperature, the mutual operation basic value of amount of wind are given", "off limit discernment".
Fig. 4 is a schematic diagram of a target value intelligent setting module according to the present application, as shown in fig. 4, the system time can be identified, a signal of the switching value 1 is sent out at 45 th minute of each hour, if the concentration of the SO2 emission exceeds the standard, a numerical value is output through a broken line function generator according to the strength of the exceeding standard, a smaller value is output after deviation calculation is carried out with the target value as the target value of the control system, thereby rapidly increasing limestone input, preventing the average value of the hour from exceeding the standard, and the target value is restored to the original target value after one hour is over. The design can ensure that operators can set the target value to be larger with confidence, and can prevent the standard exceeding of the hour mean value while saving limestone.
Fig. 5 is a schematic diagram of a lead prediction module according to the present application, as shown in fig. 5, the lead prediction module may simulate a variation trend value of SO2 at a chimney through an inertia module when an output of a main regulator varies, perform a deviation operation on the value and an actual measured value of SO2 to obtain a feedback value of SO2 of the main regulator, input a concentration value of SO2 emissions into a lag module, perform a lag operation in the lag module, and output the value through the lag module after a certain time and perform a deviation operation on the value and an output of the inertia module to achieve smooth regulation. The addition of the module can effectively reduce the problems of oscillation, slow adjustment, large adjustment deviation and the like caused by hysteresis in the adjustment process of the system, and can shorten the adjustment time by one fifth under an ideal condition.
The 'two-stage regulator control', namely the 'main regulator' and the 'auxiliary regulator' are in linkage control, and the main regulator receives the target value of the 'target value intelligent given module' and the predicted value of the 'advanced prediction module' to perform deviation operation and then outputs a limestone flow instruction to the auxiliary regulator. The auxiliary regulator receives the limestone flow comprehensive instruction (namely the sum of the output of the main regulator and the interactive operation basic value of the coal quantity, bed temperature and air quantity) and limestone flow feedback, performs deviation operation, outputs a feeder frequency instruction, and outputs the instruction to the feeder through the operator.
The "coal amount, bed temperature and air volume interactive operation basic value giving" is that a comprehensive operation numerical value after a "coal amount real-time value" x "bed temperature" x (boiler total air volume divided by coal amount real-time value) is added to the output of a main regulator and then is given to the input end of a secondary regulator as a target value of the secondary regulator. Almost all SO2 generated in the combustion process of the circulating fluidized bed boiler comes from coal entering a hearth, the higher the bed temperature is, the lower the chemical reaction efficiency of limestone and SO2 is, namely, the same amount of coal needs more limestone to react to ensure the environmental protection index; if the air quantity is not changed, when the 'ratio of the air quantity to the coal quantity' is changed, namely the air quantity is changed, the measured SO2 concentration value is increased if the air quantity is small, limestone investment needs to be increased, and limestone investment needs to be reduced if the air quantity is small; if the air quantity is not changed, when the 'ratio of the air quantity to the coal quantity' is changed, namely the coal quantity is changed, the measured SO2 concentration value is increased if the coal quantity is large, limestone input needs to be increased, and limestone input needs to be reduced if the coal quantity is large; in addition, the change of the bed temperature and the proportioning of the air quantity and the coal quantity have interaction. Therefore, a multiplication relation is adopted among the real-time coal value, the bed temperature, the total air quantity of the boiler and the real-time coal value. It should be noted here that "total air volume of boiler divided by real-time value of coal volume" will ultimately reflect the value of "oxygen volume" of boiler, and here, no "oxygen volume" is taken to participate in the calculation because the change of "oxygen volume" will lag behind "total air volume of boiler divided by real-time value of coal volume" for about one minute, and taking "total air volume of boiler divided by real-time value of coal volume" to participate in the control will make the adjustment faster than taking "oxygen volume" to participate in the control. After the coal quantity, bed temperature and air quantity interactive operation basic value setting is added at the input end of the auxiliary regulator, the auxiliary regulator can quickly output instructions to increase and decrease limestone at the first time of parameter change, and the system can be more stable while advanced regulation is realized.
The function of the out-of-limit identification 1 module is to increase and decrease the main regulator in a closed mode when the output of the auxiliary regulator exceeds the upper limit or the lower limit, and the integral saturation of the main regulator is prevented; the "out-of-limit identification 2" module functions to place the secondary regulator into a tracking state when the output of the operator exceeds an upper or lower limit, preventing integral saturation of the secondary regulator.
This application automatic control model of desulfurization in circulating fluidized bed boiler stove is more superior than traditional control model, can effectively avoid this book of handing over 4.1, 4.2, 4.3, 4.4, the problem of mentioning in the 4.5 clauses and subclauses, make control system process more stable, quick and accurate, make the input that whole control system can be stable for a long time, can also the greatly reduced lime stone quantity simultaneously, reduce the number of times that environmental protection index exceeds standard.
For the automatic control model for the in-furnace desulfurization of the circulating fluidized bed boiler, when in use, the model can be configured according to the block diagram shown in the book at the bottom of the text, tests are carried out under various working conditions of the boiler, relevant parameters in logic are determined, and finally the control system is better.
Through the above description of the embodiments, those skilled in the art can clearly understand that the method according to the above embodiments can be implemented by software plus a necessary general hardware platform, and certainly can also be implemented by hardware, but the former is a better implementation mode in many cases. Based on such understanding, the technical solutions of the present application may be embodied in the form of a software product, which is stored in a storage medium (e.g., ROM/RAM, magnetic disk, optical disk) and includes instructions for enabling a terminal device (e.g., a mobile phone, a computer, a server, or a network device) to execute the method according to the embodiments of the present application.
Example two
In this embodiment, a desulfurization control device is further provided, and the device is used to implement the foregoing embodiments and preferred embodiments, and the description of the device that has been already made is omitted. As used below, the term "module" may be a combination of software and/or hardware that implements a predetermined function. Although the means described in the embodiments below are preferably implemented in software, an implementation in hardware, or a combination of software and hardware is also possible and contemplated.
According to an embodiment of the present application, there is also provided a control apparatus of desulfurization, including:
the determining module is used for determining a prediction curve of the SO2 discharge amount of a preset time period aiming at the circulating fluidized bed boiler, wherein a plurality of moments of the preset time period of the prediction curve correspond to a plurality of predicted values;
and the adjusting module is used for adjusting the limestone input amount of the circulating fluidized bed boiler according to the prediction curve.
Optionally, the adjusting module is further configured to adjust the limestone input of the circulating fluidized bed boiler according to the prediction curve, and includes: acquiring an actual measurement value of SO2 emission at a moment; estimating a second value of the SO2 emission amount after a preset value is minutes according to the measured value at the moment;
and adjusting the limestone input amount of the circulating fluidized bed boiler after a preset value is minutes according to the second value and a predicted value on a prediction curve of the second value at the same time.
Optionally, before the limestone input of the circulating fluidized bed boiler is adjusted, the adjusting module is further used for obtaining a target value of SO2 discharge amount of the preset time period; adjusting the limestone input of the circulating fluidized bed boiler comprises the following steps: and determining the limestone input amount at the current moment according to the prediction curve and the target value.
Optionally, the adjusting module further comprises: adjusting the limestone input of the circulating fluidized bed boiler according to the prediction curve and at least one of the following parameters of the circulating fluidized bed boiler: the coal quantity at the present moment, the bed temperature of the circulating fluidized bed and the air quantity entering the circulating fluidized bed boiler.
Optionally, the adjusting module adjusts the limestone input of the circulating fluidized bed boiler based on the prediction curve and at least one of the following parameters of the circulating fluidized bed boiler, including at least one of: when the coal amount is increased, increasing the limestone input amount according to the first corresponding relation; when the bed temperature of the circulating fluidized bed is increased, the input amount of the limestone is reduced according to the second corresponding relation; when the air volume increases, the limestone input amount is reduced according to the third correspondence relationship.
Optionally, a first regulator, a second regulator and an operator are arranged in the regulating module, and the functions of the first regulator, the second regulator and the operator are as follows: determining the prediction curve by a first regulator, and inputting the prediction curve into a second regulator; regulating the limestone input amount by the second regulator according to the prediction curve and at least one of the parameters, and controlling an operator to input limestone to the circulating fluidized bed boiler according to the limestone input amount; a first feedback device is arranged between the second regulator and the first regulator and used for feeding back the working state of the second regulator to the first regulator; and a second feedback device is arranged between the operator and the second regulator and used for feeding back the working state of the operator to the second regulator.
It should be noted that, the above modules may be implemented by software or hardware, and for the latter, the following may be implemented, but not limited to: the modules are all positioned in the same processor; alternatively, the modules are respectively located in different processors in any combination.
EXAMPLE III
According to a further embodiment of the present application, there is also provided a storage medium having a computer program stored therein, wherein the computer program is arranged to perform the steps of any of the above-described method embodiments when executed.
According to yet another embodiment of the present application, there is also provided an electronic device comprising a memory having a computer program stored therein and a processor configured to execute the computer program to perform the steps of any of the above method embodiments.
It will be apparent to those skilled in the art that the modules or steps of the present application described above may be implemented by a general purpose computing device, they may be centralized on a single computing device or distributed across a network of multiple computing devices, and alternatively, they may be implemented by program code executable by a computing device, such that they may be stored in a storage device and executed by a computing device, and in some cases, the steps shown or described may be performed in an order different than that described herein, or they may be separately fabricated into individual integrated circuit modules, or multiple ones of them may be fabricated into a single integrated circuit module. Thus, the present application is not limited to any specific combination of hardware and software.
The above description is only a preferred embodiment of the present application and is not intended to limit the present application, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.
Claims (8)
1. A method for controlling desulfurization, comprising:
determining sulfur dioxide SO for a predetermined period of time during coal desulfurization by a circulating fluidized bed boiler2A prediction curve of the discharge amount, wherein the prediction curve corresponds to a plurality of prediction values at a plurality of moments of the predetermined period;
according to the prediction curve, adjusting the limestone input amount of the circulating fluidized bed boiler;
wherein, according to the prediction curve, the limestone input amount of the circulating fluidized bed boiler is adjusted, and the method comprises the following steps: obtaining SO of a moment2Measured values of emissions; estimating the SO after a preset value is minutes according to the measured value of the moment2A second value of emissions; and adjusting the limestone input amount of the circulating fluidized bed boiler after a preset value is minutes according to the second value and a predicted value on a prediction curve of the second value at the same time.
2. The method of claim 1,
obtaining SO of the preset time period before the limestone input of the circulating fluidized bed boiler is adjusted2A target value of the discharge amount;
adjusting the limestone input of the circulating fluidized bed boiler, comprising: and determining the limestone input amount at the current moment according to the prediction curve and the target value.
3. The method of claim 1, wherein adjusting the limestone input to the circulating fluidized bed boiler based on the predictive curve comprises:
adjusting the limestone input of the circulating fluidized bed boiler according to the prediction curve and at least one of the following parameters of the circulating fluidized bed boiler:
the coal quantity at the current moment, the bed temperature of the circulating fluidized bed and the air quantity entering the circulating fluidized bed boiler.
4. A method according to claim 3, characterized in that the limestone input of the circulating fluidized bed boiler is adjusted in dependence of the prediction curve and at least one of the following parameters of the circulating fluidized bed boiler, including at least one of:
when the coal amount is increased, increasing the limestone input amount according to a first corresponding relation;
when the bed temperature of the circulating fluidized bed is increased, reducing the input amount of the limestone according to a second corresponding relation;
and when the air volume is increased, reducing the input amount of the limestone according to a third corresponding relation.
5. The method of claim 3,
determining the prediction curve by a first regulator, inputting the prediction curve into a second regulator;
adjusting the limestone input amount by the second adjuster according to the prediction curve and at least one of the parameters, and controlling an operator to input limestone to the circulating fluidized bed boiler according to the limestone input amount;
a first feedback device is arranged between the second regulator and the first regulator and used for feeding back the working state of the second regulator to the first regulator;
and a second feedback device is arranged between the operator and the second regulator and is used for feeding back the working state of the operator to the second regulator.
6. A desulfurization control apparatus, comprising:
a determination module for determining SO for a predetermined period of time for a circulating fluidized bed boiler2A prediction curve of the emission amount, wherein a plurality of moments of the prediction curve in the predetermined time period correspond to a plurality of predicted values;
the adjusting module is used for adjusting the limestone input amount of the circulating fluidized bed boiler according to the prediction curve;
wherein the adjusting module is further configured to obtain the SO at a moment2Measured values of emissions; estimating the SO after a preset value is minutes according to the measured value of the moment2A second value of emissions;
and adjusting the limestone input amount of the circulating fluidized bed boiler after a preset value is minutes according to the second value and a predicted value on a prediction curve of the second value at the same time.
7. A storage medium, in which a computer program is stored, wherein the computer program is arranged to perform the method of any of claims 1 to 5 when executed.
8. An electronic device comprising a memory and a processor, wherein the memory has stored therein a computer program, and wherein the processor is arranged to execute the computer program to perform the method of any of claims 1 to 5.
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| CN111306536A (en) * | 2020-02-12 | 2020-06-19 | 神华国能集团有限公司 | Method and device for controlling sulfur dioxide emission of circulating fluidized bed boiler |
| CN111957190A (en) * | 2020-08-29 | 2020-11-20 | 无锡雪浪环境科技股份有限公司 | Feeding control method and system for deacidification atomizer |
| CN112711232B (en) * | 2020-12-23 | 2022-08-09 | 天津水泥工业设计研究院有限公司 | Based on preposed SO 2 Method and system for controlling predicted usage amount of desulfurizing agent |
| CN113007703B (en) * | 2021-03-17 | 2022-12-27 | 新奥数能科技有限公司 | Method and device for controlling feeding amount of desulfurizer in circulating fluidized bed boiler |
| CN113058393A (en) * | 2021-04-16 | 2021-07-02 | 新奥数能科技有限公司 | Method and device for controlling pH value of slurry in desulfurization system |
| CN113648802B (en) * | 2021-09-10 | 2024-01-09 | 南方电网电力科技股份有限公司 | Flue gas desulfurization diagnosis method and device for thermal power generating unit |
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| CN105116855B (en) * | 2015-07-22 | 2018-04-10 | 华北电力大学 | A kind of optimal control method of flue gas circulating fluidized bed desulfurization |
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