Data processing method and data processing device based on circulating fluidized bed boiler

Abstract

The invention provides a data processing method and device based on a circulating fluidized bed boiler, and the method comprises the steps: obtaining the current reaction temperature of the circulating fluidized bed boiler, the type of a reducing agent, and the amount of flue gas flowing through each separator in the circulating fluidized bed boiler; determining a reaction coefficient of the circulating fluidized bed boiler according to the current reaction temperature and the type of the reducing agent; according to the amount of smoke flowing through each separator in the circulating fluidized bed boiler, the smoke coefficient corresponding to each separator is determined; determining a distribution coefficient of the circulating fluidized bed boiler according to the flue gas amount and the flue gas coefficient corresponding to each separator; and calculating the actual denitration efficiency of the circulating fluidized bed boiler according to the reaction coefficient, the distribution coefficient and the designed denitration efficiency. The actual denitration efficiency of the circulating fluidized bed boiler is calculated, operation parameters are adjusted to reduce the consumption of a reducing agent, and the cost is reduced.

Description

Technical Field

[0001] The present application relates to the technical field of boilers, and in particular to a data processing method and a data processing device based on a circulating fluidized bed boiler. Background Art

[0002] At present, the denitrification process of circulating fluidized bed boilers mostly adopts the selective non-catalytic reduction process. Circulating fluidized bed boilers mainly remove NOx through the SNCR process. The reducing agent containing amino groups (such as ammonia water, urea solution, etc.) is sprayed into the furnace in a narrow temperature range of 850-1100°C in a mist form. The reducing agent is rapidly thermally decomposed into NH3 and reacts with NOx in the flue gas to generate N2 and H2O, thereby removing NOx in the flue gas.

[0003] With the strict environmental protection requirements and the influence of coal type fluctuations, the precise control technology of SNCR process removal in circulating fluidized bed boilers has become an important research direction. This technology requires understanding the relationship between SNCR denitrification efficiency and the main influencing factors. Currently, no method has been proposed to evaluate it.

[0004] The challenges are mainly reflected in two aspects. First, the SNCR denitrification efficiency mainly depends on the reaction temperature, the atomization effect of the reducing agent, the uniformity of the reaction mixing, etc.; second, due to the influence of the uneven gas-solid flow of the circulating fluidized bed, there are differences in the NOx concentration, flue gas volume, solid particle concentration, etc. of each cyclone separator. Summary of the invention

[0005] In view of this, the purpose of the present application is to provide a data processing method and a data processing device based on a circulating fluidized bed boiler to overcome at least one of the above-mentioned defects.

[0006] In a first aspect, an embodiment of the present application provides a data processing method based on a circulating fluidized bed boiler, the method comprising: obtaining a current reaction temperature of the circulating fluidized bed boiler, a reducing agent type, and an actual amount of flue gas flowing through each separator in the circulating fluidized bed boiler; determining a reaction coefficient of the circulating fluidized bed boiler according to the current reaction temperature and the reducing agent type; determining a flue gas coefficient corresponding to each separator according to the actual amount of flue gas flowing through each separator in the circulating fluidized bed boiler; determining a distribution coefficient of the circulating fluidized bed boiler according to the actual flue gas amount and the flue gas coefficient corresponding to each separator; calculating an actual denitrification efficiency of the circulating fluidized bed boiler according to the reaction coefficient, the distribution coefficient, and the designed denitrification efficiency, and determining guidance suggestions for the circulating fluidized bed boiler.

[0007] In an optional embodiment of the present application, the reaction coefficient of the circulating fluidized bed boiler is determined in the following manner: according to the type of reducing agent, a target temperature is determined, and the target temperature is the temperature with the highest actual denitrification efficiency in the historical data recorded for the type of reducing agent; according to the spray gun structure of the circulating fluidized bed boiler and the type of reducing agent, an injection mixing coefficient is determined; based on the target temperature, the current reaction temperature and the injection mixing coefficient, the reaction coefficient of the circulating fluidized bed boiler is calculated.

[0008] In an optional embodiment of the present application, the flue gas coefficient of each separator is determined in the following manner: a preset state is determined according to the target temperature and the reducing agent type, and a preset flue gas volume of each separator under the preset state and a first sum of the preset flue gas volumes of all separators are obtained; a first fuel volume of the circulating fluidized bed boiler at the current reaction temperature and a second fuel volume of the circulating fluidized bed boiler under the preset state are determined; a structural coefficient of the circulating fluidized bed boiler is determined according to the hood resistance of the circulating fluidized bed boiler and the resistance of all separators; a dimensionless standard deviation of the circulating fluidized bed boiler is determined according to the first fuel volume, the second fuel volume and the structural coefficient; for each separator, the actual flue gas volume of the separator is compared with a target flue gas threshold, and the flue gas coefficient of the separator is calculated according to the comparison result, wherein the target flue gas threshold is the ratio of the second sum of the actual flue gas volumes of all separators to the total number of all separators.

[0009] In an optional embodiment of the present application, for each separator, the actual smoke volume of the separator is compared with the target smoke volume, and the smoke coefficient of the separator is calculated according to the comparison result, including: for each separator, calculating the ratio of the preset smoke volume of the separator to the first total, the difference between the ratio and a preset constant, and the second product of the difference and the dimensionless standard deviation; for each separator, judging whether the actual smoke volume of the separator is greater than the target smoke threshold; for each separator, if the actual smoke volume of the separator is greater than the target smoke threshold, calculating the difference between the preset constant and the second product, and using the difference as the smoke coefficient of the separator; for each separator, if the actual smoke volume of the separator is not greater than the target smoke threshold, calculating the sum of the preset constant and the second product, and using the sum as the smoke coefficient of the separator.

[0010] In an optional embodiment of the present application, the distribution coefficient of the circulating fluidized bed boiler is determined in the following manner: for each separator, calculating the first product of the flue gas volume of the separator and the corresponding flue gas coefficient; calculating the third sum of the first products of all separators; and determining the distribution coefficient of the circulating fluidized bed boiler based on the ratio of the second sum to the third sum.

[0011] In an optional embodiment of the present application, guidance suggestions for the circulating fluidized bed boiler are determined in the following manner: judging whether the actual denitrification efficiency of the circulating fluidized bed boiler is greater than the preset denitrification efficiency; if the actual denitrification efficiency of the circulating fluidized bed boiler is greater than the preset denitrification efficiency, continuing to calculate the actual denitrification efficiency; if the actual denitrification efficiency of the circulating fluidized bed boiler is not greater than the preset denitrification efficiency, selecting a target coefficient from between the reaction coefficient and the distribution coefficient, the target coefficient being the coefficient with the largest difference from the preset constant between the reaction coefficient and the distribution coefficient; determining guidance suggestions for the circulating fluidized bed boiler based on the target coefficient.

[0012] In an optional embodiment of the present application, the guidance suggestions for the circulating fluidized bed boiler are determined based on the target coefficient, including: if the target coefficient is a reaction coefficient, the guidance suggestions for the circulating fluidized bed boiler are to increase the reaction temperature of the circulating fluidized bed boiler and check the hardware structure of the circulating fluidized bed boiler; if the target coefficient is a distribution coefficient, the guidance suggestions for the circulating fluidized bed boiler are to differentially adjust the input of the reducing agent of each separator according to the distribution coefficient.

[0013] In the second aspect, an embodiment of the present application also provides a data processing device, which includes: a flue gas volume acquisition module, which is used to acquire the current reaction temperature of the circulating fluidized bed boiler, the type of reducing agent and the actual flue gas volume flowing through each separator in the circulating fluidized bed boiler; a reaction coefficient determination module, which is used to determine the reaction coefficient of the circulating fluidized bed boiler according to the current reaction temperature and the type of reducing agent; a flue gas coefficient determination module, which is used to determine the flue gas coefficient corresponding to each separator in the circulating fluidized bed boiler according to the actual flue gas volume flowing through each separator in the circulating fluidized bed boiler; a distribution coefficient determination module, which is used to determine the distribution coefficient of the circulating fluidized bed boiler according to the actual flue gas volume and the flue gas coefficient corresponding to each separator; an actual denitrification efficiency calculation module, which is used to calculate the actual denitrification efficiency of the circulating fluidized bed boiler according to the reaction coefficient, the distribution coefficient and the designed denitrification efficiency, and determine guidance suggestions for the circulating fluidized bed boiler.

[0014] In a third aspect, an embodiment of the present application further provides an electronic device, comprising: a processor, a memory and a bus, wherein the memory stores machine-readable instructions executable by the processor, and when the electronic device is running, the processor and the memory communicate via the bus, and when the machine-readable instructions are executed by the processor, the steps of the method described above are performed.

[0015] In a fourth aspect, an embodiment of the present application further provides a computer-readable storage medium, on which a computer program is stored, and when the computer program is executed by a processor, the steps of the method described above are executed.

[0016] The data processing method and data processing device based on the circulating fluidized bed boiler provided in the embodiment of the present application obtain the current reaction temperature of the circulating fluidized bed boiler, the type of reducing agent, and the amount of flue gas flowing through each separator in the circulating fluidized bed boiler; determine the reaction coefficient of the circulating fluidized bed boiler according to the current reaction temperature and the type of reducing agent; determine the flue gas coefficient corresponding to each separator according to the amount of flue gas flowing through each separator in the circulating fluidized bed boiler; determine the distribution coefficient of the circulating fluidized bed boiler according to the flue gas volume and the flue gas coefficient corresponding to each separator; calculate the actual denitration efficiency of the circulating fluidized bed boiler according to the reaction coefficient, the distribution coefficient, and the designed denitration efficiency. The actual denitration efficiency of the circulating fluidized bed boiler is calculated by the present application, the relationship between the actual denitration efficiency and the main influencing factors of denitration is mastered, and the operating parameters are adjusted to reduce the consumption of the reducing agent and reduce the cost.

[0017] In order to make the above-mentioned objects, features and advantages of the present application more obvious and easy to understand, preferred embodiments are specifically cited below and described in detail with reference to the attached drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings required for use in the embodiments will be briefly introduced below. It should be understood that the following drawings only show certain embodiments of the present application and therefore should not be regarded as limiting the scope. For ordinary technicians in this field, other related drawings can be obtained based on these drawings without paying creative work.

[0019] Figure 1 A flow chart of a data processing method based on a circulating fluidized bed boiler provided in an embodiment of the present application;

[0020] Figure 2 A flow chart for determining the reaction coefficient of a circulating fluidized bed boiler provided in an embodiment of the present application;

[0021] Figure 3 A flow chart for determining the flue gas coefficient of each separator provided in an embodiment of the present application;

[0022] Figure 4 A front view of a circulating fluidized bed boiler provided in an embodiment of the present application;

[0023] Figure 5 A top view of a circulating fluidized bed boiler provided in an embodiment of the present application;

[0024] Figure 6 A schematic diagram of the structure of a data processing device provided in an embodiment of the present application;

[0025] Figure 7 A schematic diagram of the structure of an electronic device provided in an embodiment of the present application. DETAILED DESCRIPTION

[0026] To make the purpose, technical scheme and advantages of the embodiments of the present application clearer, the technical scheme in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application. Obviously, the described embodiments are only a part of the embodiments of the present application, rather than all of the embodiments. The components of the embodiments of the present application usually described and shown in the drawings here can be arranged and designed in various different configurations. Therefore, the following detailed description of the embodiments of the present application provided in the drawings is not intended to limit the scope of the application claimed for protection, but merely represents the selected embodiments of the present application. Based on the embodiments of the present application, each other embodiment obtained by those skilled in the art without making creative work belongs to the scope of protection of the present application.

[0027] First, the application scenarios to which the present application is applicable are introduced. The present application can be applied to the boiler field.

[0028] Research has found that the denitrification process of circulating fluidized bed boilers mostly adopts selective non-catalytic reduction process. Circulating fluidized bed boilers mainly remove NOx through the SNCR process. The amino-containing reducing agent (such as ammonia water, urea solution, etc.) is sprayed into the furnace in a narrow temperature range of 850-1100°C. The reducing agent is rapidly thermally decomposed into NH3 and reacts with NOx in the flue gas to generate N2 and H2O, thereby removing NOx in the flue gas.

[0029] With the strict environmental protection requirements and the influence of coal type fluctuations, the precise control technology of SNCR process removal of circulating fluidized bed boilers has become an important research direction. This technology requires the understanding of the relationship between SNCR denitrification efficiency and the main influencing factors. At present, there is no method proposed for evaluation, and it is impossible to adjust parameters according to the relationship between SNCR denitrification efficiency and the main influencing factors, which wastes energy and has high costs.

[0030] Based on this, the embodiment of the present application provides a data processing method and a data processing device based on a circulating fluidized bed boiler, which obtains the current reaction temperature of the circulating fluidized bed boiler, the type of reducing agent, and the amount of flue gas flowing through each separator in the circulating fluidized bed boiler; according to the current reaction temperature and the type of reducing agent, the reaction coefficient of the circulating fluidized bed boiler is determined; according to the amount of flue gas flowing through each separator in the circulating fluidized bed boiler, the flue gas coefficient corresponding to each separator is determined; according to the flue gas volume corresponding to each separator and the flue gas coefficient, the distribution coefficient of the circulating fluidized bed boiler is determined; according to the reaction coefficient, the distribution coefficient and the designed denitrification efficiency, the actual denitrification efficiency of the circulating fluidized bed boiler is calculated. The actual denitrification efficiency of the circulating fluidized bed boiler is calculated by the present application, the relationship between the actual denitrification efficiency and the main influencing factors of denitrification is mastered, and the operating parameters are adjusted to reduce the consumption of the reducing agent and reduce the cost.

[0031] See also Figure 1 , Figure 1 This is a flow chart of a data processing method based on a circulating fluidized bed boiler provided in an embodiment of the present application. Figure 1 As shown in , the data processing method based on the circulating fluidized bed boiler provided in the embodiment of the present application includes:

[0032] S101. Obtain the current reaction temperature of the circulating fluidized bed boiler, the type of reducing agent, and the actual amount of flue gas flowing through each separator in the circulating fluidized bed boiler.

[0033] Among them, the bed temperature control range of the circulating fluidized bed boiler is usually 780℃ to 1050℃. This range is determined according to different coal qualities, and can be adjusted appropriately according to actual needs. The ideal bed temperature is roughly between 850℃ and 900℃. This temperature range takes into account the NOx and SO2 emission indicators and combustion efficiency. For example, the bed temperature is 840℃ to 880℃ when burning lignite, 860℃ to 900℃ when burning bituminous coal, 870℃ to 920℃ when burning lean coal, and 890℃ to 940℃ when burning anthracite.

[0034] There are three main reducing agents commonly used in SNCR denitration in circulating fluidized bed boilers: liquid ammonia, ammonia water and urea. The selection of reducing agent is one of the main factors affecting denitration efficiency and operating economy. The specific selection of reducing agent depends on factors such as the boiler's denitration system design, operating costs, safety and environmental protection requirements.

[0035] Here, SNCR technology is a method for reducing NOx without a catalyst in the temperature range of 850-1100°C. In this method, ammonia, urea and other amino-containing reducing agents are sprayed into the flue gas without the presence of a catalyst. The reducing agent is rapidly thermally decomposed into NH3 and undergoes SNCR reaction with NOx in the flue gas to generate N2 and H2O.

[0036] The working principle of SNCR technology is to spray the reducing agent containing amino group (such as ammonia water, urea solution, etc.) into the furnace in a narrow temperature range of 850-1100℃ in the form of mist. The reducing agent is rapidly thermally decomposed into NH3 and reacts with NOx in the flue gas to generate N2 and H2O, thereby removing NOx from the flue gas.

[0037] The actual flue gas volume depends on many factors, such as boiler capacity, coal quality, combustion efficiency, and excess air coefficient. Generally speaking, the actual flue gas volume can be calculated by parameters such as boiler fuel consumption, excess air coefficient, and flue gas density.

[0038] S102. Determine the reaction coefficient of the circulating fluidized bed boiler according to the current reaction temperature and the type of reducing agent.

[0039] Specifically, see Figure 2 , Figure 2 This is a flow chart for determining the reaction coefficient of a circulating fluidized bed boiler provided in an embodiment of the present application. Figure 2 As shown in , the data processing method based on the circulating fluidized bed boiler provided in the embodiment of the present application includes:

[0040] S201. Determine a target temperature according to the type of reducing agent.

[0041] The target temperature is the temperature with the highest actual denitration efficiency in the historical data recorded for the reductant type;

[0042] Here, different reducing agents (such as urea, ammonia water, liquid ammonia, etc.) have different reaction activities in the CFB boiler, so their optimal reaction temperatures will also be different. The temperature with the highest actual denitrification efficiency in historical data is set as the target temperature. This is because at this temperature point, the reducing agent reacts most fully with nitrogen oxides (NOx) in the flue gas, and the denitrification efficiency is the highest.

[0043] In order to accurately determine the target temperature, it is necessary to collect a large amount of historical data, including denitrification efficiency, reducing agent consumption, flue gas composition, etc. at different temperatures. Through data analysis, the temperature point with the highest denitrification efficiency corresponding to each reducing agent can be found.

[0044] S202. Determine the injection mixing coefficient according to the injection gun structure and the type of reducing agent of the circulating fluidized bed boiler.

[0045] Specifically, the spray gun structure in the boiler directly affects the spray angle, speed and distribution range of the reducing agent, and further affects the mixing effect of the reducing agent and the flue gas. Different spray gun structures are suitable for different reducing agents and operating conditions of the circulating fluidized bed boiler.

[0046] The injection mixing coefficient is an indicator that comprehensively reflects the injection effect and mixing efficiency. It can be determined through experimental measurement, numerical simulation or empirical formula. Experimental measurement usually involves installing sensors in the circulating fluidized bed boiler to monitor the concentration distribution of the reducing agent after injection; numerical simulation uses computational fluid dynamics (CFD) software to simulate the injection process; and the empirical formula is a simplified calculation method summarized based on a large amount of practical data.

[0047] In an optional embodiment, the injection mixing coefficient is mainly related to the SNCR spray gun structure, the number of spray guns, the spray gun position and the reaction medium, and has nothing to do with the ammonia nitrogen molar ratio, and generally ranges from 0.0003 to 0.001. The value of liquid ammonia or ammonia water is slightly larger than that of urea.

[0048] S203. Calculate the reaction coefficient of the circulating fluidized bed boiler according to the target temperature, the current reaction temperature and the injection mixing coefficient.

[0049] The reaction coefficient is a comprehensive indicator that reflects the denitrification reaction efficiency of a CFB boiler, which takes into account the effects of the target temperature, current reaction temperature, and injection mixing coefficient.

[0050] Specifically, the reaction coefficient of the circulating fluidized bed boiler is determined by the following formula:

[0051] K1=-k1(T 最佳 -T) 2 +1

[0052] Among them, K1 represents the reaction coefficient of the circulating fluidized bed boiler, k1 represents the injection mixing coefficient of the circulating fluidized bed boiler, T 最佳 represents the target temperature of the circulating fluidized bed boiler, and T represents the current temperature of the circulating fluidized bed boiler.

[0053] Preferably, the reaction coefficient mainly depends on the reaction temperature. Different reducing agents have different reaction characteristics and different reaction coefficients.

[0054] S103. Determine a flue gas coefficient corresponding to each separator according to the amount of flue gas flowing through each separator in the circulating fluidized bed boiler.

[0055] Specifically, see Figure 3 , Figure 3 The flowchart for determining the flue gas coefficient of each separator provided in the embodiment of the present application. Figure 3 As shown in , the data processing method based on the circulating fluidized bed boiler provided in the embodiment of the present application includes:

[0056] S301. Determine a preset state according to a target temperature and a reducing agent type, and obtain a preset flue gas volume of each separator and a first sum of the preset flue gas volumes of all separators under the preset state.

[0057] The preset state refers to an ideal state when the CFB boiler (circulating fluidized bed boiler) is operated with a specific reductant type and fuel amount at the target temperature. This state is usually based on historical optimal operating data or experimental data, and this state can be understood as a full load state.

[0058] Under the preset state, a preset flue gas volume needs to be set for each separator. These preset flue gas volumes are determined based on factors such as the overall flue gas flow of the CFB boiler, the design capacity of the separator, and the amount of fuel under the preset state. The preset flue gas volumes of all separators are added together to obtain a first sum, which represents the total flue gas flow of the CFB boiler under the preset state.

[0059] S302, determining a first fuel amount of the circulating fluidized bed boiler at a current reaction temperature and a second fuel amount of the circulating fluidized bed boiler at a preset state.

[0060] The first fuel amount refers to the actual fuel amount of the CFB boiler at the current reaction temperature, while the second fuel amount refers to the corresponding fuel amount under the preset state. The difference between the two fuel amounts reflects the change in fuel amount required for the CFB boiler to adjust from the current state to the preset state.

[0061] In an optional embodiment, the first fuel amount refers to the fuel amount under a random load, each load has a corresponding fuel amount and reaction temperature, and the second fuel amount refers to the fuel amount under full load, which can be understood as the maximum continuous load output of the boiler, that is, full load.

[0062] S303. Determine the structural coefficient of the circulating fluidized bed boiler according to the hood resistance of the circulating fluidized bed boiler and the resistance of all separators.

[0063] The hood of a CFB boiler is a key component for mixing fuel and air, and its resistance will affect the operating efficiency and fuel consumption of the CFB boiler. Similarly, the resistance of the separator will also affect the flow and separation efficiency of flue gas.

[0064] The structural coefficient is an indicator that comprehensively reflects the structural characteristics of the CFB boiler and separator. It can be determined based on the hood resistance, separator resistance and other design parameters of the CFB boiler (such as bed height, bed density, etc.). The structural coefficient is mainly related to the boiler structure such as the hood, furnace, separator, etc., and is of great significance for evaluating the operating efficiency and adjustment strategy of the CFB boiler.

[0065] Specifically, the structural coefficient of the circulating fluidized bed boiler is determined by the following formula:

[0066] k2=f(P 风帽阻力 , P 分离器阻力 )

[0067] Among them, k2 represents the structural coefficient of the circulating fluidized bed boiler, P 风帽阻力 P represents the hood resistance of the circulating fluidized bed boiler. 分离器阻力 Represents the resistance of all separators in a circulating fluidized bed boiler.

[0068] S304: Determine a dimensionless standard deviation of the circulating fluidized bed boiler according to the first fuel amount, the second fuel amount, and the structural coefficient.

[0069] Specifically, the furnace cross-section of the circulating fluidized bed boiler is large, and there is unevenness in the gas-solid flow. The degree of unevenness under different loads is also different. Different separator structures have different resistance distributions, which will affect the distribution of the gas-solid flow.

[0070] Therefore, this application takes the circulating fluidized bed with three separators as an example for analysis. Figure 4 , Figure 5, Figure 4 This is a front view of a circulating fluidized bed boiler provided in an embodiment of the present application. Figure 5 This is a top view of a circulating fluidized bed boiler provided in an embodiment of the present application. Figure 4 As shown in the figure, the front view of the circulating fluidized bed boiler provided in the embodiment of the present application includes: a de-pinning lance 41 and a separator 42, as shown in FIG. Figure 5 As shown in , a top view of a circulating fluidized bed boiler provided in an embodiment of the present application includes: an A separator 51 , a B separator 52 and a C separator 53 .

[0071] Assume that under a certain load, the flue gas volumes of the three separators are a, b, and c respectively, and the second sum of the actual flue gas volumes of the separators is V. The flue gas proportions corresponding to the three separators are a / (a+b+c), b / (a+b+c), and c / (a+b+c), which are dimensionless as a / b, 1, and c / b. The standard deviation of these three dimensionless numbers is σ.

[0072] Dimensionlessness of separators refers to the use of dimensionless methods to represent and analyze performance parameters of separators when studying and designing them, converting parameters with different dimensions or units into the same dimension for unified analysis and comparison. In this application, the actual flue gas volume b of separator B 52 in the circulating fluidized bed boiler is used as a parameter and then converted into the same order of magnitude. In the design and optimization process of separators, dimensionlessness can help eliminate the impact of different dimensions or units on data analysis and improve the accuracy and reliability of analysis.

[0073] The dimensionless standard deviation is an indicator used to evaluate the operating stability of the CFB boiler. It can be calculated based on the first fuel amount, the second fuel amount and the structural coefficient. The smaller the dimensionless standard deviation is, the closer the operating state of the CFB boiler is to the preset state, and the better the operating stability is.

[0074] In summary, the preset flue gas volumes of the three separators under the preset state, that is, under full load, are a BMCR , b BMCR and c BMCR , the total flue gas volume of the separator is V BMCR , the standard deviation of the corresponding dimensionless number can be σ BMCR .

[0075] Specifically, the dimensionless standard deviation of the circulating fluidized bed boiler is determined by the following formula:

[0076]

[0077] Where σ represents the dimensionless standard deviation of the circulating fluidized bed boiler, B represents the first fuel amount of the circulating fluidized bed boiler at the current reaction temperature, and B BMCRrepresents the second fuel amount of the circulating fluidized bed boiler under the preset state, and k2 represents the structural coefficient of the circulating fluidized bed boiler.

[0078] Here, the preset state is a full load state.

[0079] S305 . For each separator, compare the actual smoke volume of the separator with the target smoke threshold, and calculate the smoke coefficient of the separator according to the comparison result.

[0080] The target smoke threshold is the ratio of the second sum of the actual smoke volumes of all separators to the total number of all separators.

[0081] The target flue gas threshold refers to the flue gas volume threshold that each separator should reach under the preset state. This threshold is determined based on the design capacity of the separator and the total flue gas flow of the CFB boiler. Specifically, it is equal to the total actual flue gas volume of the CFB boiler divided by the total number of all separators.

[0082] Here, for each separator, its actual flue gas volume is compared with the target flue gas threshold. If the actual flue gas volume is higher than the target flue gas threshold, it means that the flue gas flow of the separator is too large, which may lead to a decrease in separation efficiency; if the actual flue gas volume is lower than the target flue gas threshold, it means that the flue gas flow of the separator is insufficient, which may cause flue gas short circuit or insufficient separation. Based on the comparison results, a flue gas coefficient can be determined to reflect the flue gas flow status of each separator. This flue gas coefficient can be used to guide the adjustment and optimization strategy of the CFB boiler.

[0083] Specifically, for each separator, a ratio of a preset flue gas volume of the separator to the first sum, a difference between the ratio and a preset constant, and a second product of the difference and the dimensionless standard deviation are calculated;

[0084] First, for each separator, the ratio of its preset flue gas volume to the sum of the preset flue gas volumes of all separators is calculated. This ratio reflects the relative size of the preset flue gas volume of the separator in the system.

[0085] Here, a preset constant (this constant can be set according to system characteristics, design standards or experience) is subtracted from the above ratio to obtain a difference, which reflects the degree of deviation between the preset flue gas volume of the separator and the target value (preset constant).

[0086] Finally, the above difference is multiplied by a dimensionless standard deviation (this standard deviation may reflect the discrete degree of the flue gas volume distribution in the system) to obtain the second product. This product comprehensively considers the influence of the relative size of the separator flue gas volume and the discreteness of the distribution on the coefficient.

[0087] For each separator, determine whether the actual smoke volume of the separator is greater than the target smoke threshold; for each separator, if the actual smoke volume of the separator is greater than the target smoke threshold, calculate the difference between the preset constant and the second product, and use the difference as the smoke coefficient of the separator; for each separator, if the actual smoke volume of the separator is not greater than the target smoke threshold, calculate the sum of the preset constant and the second product, and use the sum as the smoke coefficient of the separator.

[0088] Specifically, for each separator, its actual smoke volume is compared with the target smoke threshold calculated previously. If the actual smoke volume is greater than the target smoke threshold, it means that the separator has assumed a smoke treatment task that exceeds the average level. In order to reflect this additional burden, the difference between the preset constant and the second product is calculated, and this difference is used as the smoke coefficient of the separator.

[0089] If the actual smoke volume is not greater than the target smoke threshold, it means that the smoke treatment task of the separator is at or below the average level. In order to encourage it to take on more tasks or reflect its relatively light burden, the sum of the preset constant and the second product is calculated and used as the smoke coefficient of the separator.

[0090] Specifically, the flue gas coefficient of the A separator 51 is determined in the following manner:

[0091]

[0092] Among them, K a represents the flue gas coefficient of the A separator 51 in the circulating fluidized bed boiler, σ represents the dimensionless standard deviation of the circulating fluidized bed boiler, a BMCR represents the preset flue gas volume of the A separator 51 in the circulating fluidized bed boiler, V BMCR represents the first sum of the preset flue gas volumes of all separators in the circulating fluidized bed boiler, a represents the actual flue gas volume of the A separator 51 in the circulating fluidized bed boiler, and V represents the second sum of the actual flue gas volumes of all separators in the circulating fluidized bed boiler.

[0093] Similarly, the calculation formulas for the smoke coefficient of the B separator 52 and the smoke coefficient of the C separator 53 are as follows:

[0094]

[0095] Among them, K b represents the flue gas coefficient of the B separator 52 in the circulating fluidized bed boiler, σ represents the dimensionless standard deviation of the circulating fluidized bed boiler, and b BMCR represents the preset flue gas volume of the B separator 52 in the circulating fluidized bed boiler, V BMCRrepresents the first sum of the preset flue gas volumes of all separators in the circulating fluidized bed boiler, b represents the actual flue gas volume of the B separator 52 in the circulating fluidized bed boiler, and V represents the second sum of the actual flue gas volumes of all separators in the circulating fluidized bed boiler.

[0096]

[0097] Among them, K c represents the flue gas coefficient of the C separator 53 in the circulating fluidized bed boiler, σ represents the dimensionless standard deviation of the circulating fluidized bed boiler, c BMCR represents the preset flue gas volume of the C separator 53 in the circulating fluidized bed boiler, V BMCR represents the first sum of the preset flue gas volumes of all separators in the circulating fluidized bed boiler, c represents the actual flue gas volume of the C separator 53 in the circulating fluidized bed boiler, and V represents the second sum of the actual flue gas volumes of all separators in the circulating fluidized bed boiler.

[0098] Through the above steps, we can conduct a comprehensive evaluation of the operating status of the CFB boiler and formulate corresponding adjustment and optimization strategies based on the evaluation results to improve the operating efficiency and denitrification efficiency of the CFB boiler.

[0099] S104. Determine the distribution coefficient of the circulating fluidized bed boiler according to the flue gas volume and flue gas coefficient corresponding to each separator.

[0100] The distribution coefficient of the circulating fluidized bed boiler is determined by:

[0101] For each separator, the first product of the flue gas volume of the separator and the corresponding flue gas coefficient is calculated; the third sum of the first products of all separators is calculated; and the distribution coefficient of the circulating fluidized bed boiler is determined according to the ratio of the second sum to the third sum.

[0102] Specifically, the distribution coefficient of the circulating fluidized bed boiler is determined by the following formula:

[0103]

[0104] Among them, K a represents the flue gas coefficient of the A separator 51 in the circulating fluidized bed boiler, K b represents the flue gas coefficient of the B separator 52 in the circulating fluidized bed boiler, K c It represents the flue gas coefficient of the C separator 53 in the circulating fluidized bed boiler, a represents the actual flue gas volume of the A separator 51 in the circulating fluidized bed boiler, b represents the actual flue gas volume of the B separator 52 in the circulating fluidized bed boiler, and c represents the actual flue gas volume of the C separator 53 in the circulating fluidized bed boiler.

[0105] Preferably, the distribution coefficient is related to the boiler flue gas volume and the solid particle concentration, which mainly depends on the load rate of the circulating fluidized bed boiler and the structure of each cyclone separator.

[0106] S105. Calculate the actual denitrification efficiency of the circulating fluidized bed boiler based on the reaction coefficient, the distribution coefficient and the designed denitrification efficiency, and determine guidance suggestions for the circulating fluidized bed boiler.

[0107] The actual denitrification efficiency of the circulating fluidized bed boiler is calculated by the following formula:

[0108] η SNCR =K1K2η SNCR，Design

[0109] Among them, η SNCR represents the actual denitrification efficiency of the circulating fluidized bed boiler, K1 represents the reaction coefficient of the circulating fluidized bed boiler, K2 represents the distribution coefficient of the circulating fluidized bed boiler, η SNCR，Design It indicates the designed denitrification efficiency of the circulating fluidized bed boiler under the preset state.

[0110] Specifically, guidance recommendations for circulating fluidized bed boilers are determined by:

[0111] Determine whether the actual denitrification efficiency of the circulating fluidized bed boiler is greater than the preset denitrification efficiency;

[0112] If the actual denitrification efficiency of the circulating fluidized bed boiler is greater than the preset denitrification efficiency, the actual denitrification efficiency will continue to be calculated;

[0113] If the actual denitration efficiency of the circulating fluidized bed boiler is not greater than the preset denitration efficiency, a target coefficient is selected from the reaction coefficient and the distribution coefficient.

[0114] The target coefficient is the coefficient with the largest difference between the reaction coefficient and the distribution coefficient and the preset constant.

[0115] Here, if the actual denitrification efficiency is not greater than the preset denitrification efficiency, a target coefficient is selected from the reaction coefficient and the distribution coefficient, which respectively reflect the chemical reaction efficiency of the boiler and the rationality of the flue gas distribution.

[0116] Set a preset constant as a reference value, then calculate the difference between the reaction coefficient and the distribution coefficient and the preset constant. This difference can be measured by absolute value or relative value, and select the coefficient with the largest difference from the preset constant as the target coefficient. This means that the aspect represented by the coefficient may be the main reason for the denitrification efficiency not meeting the standard.

[0117] Based on the target coefficients, guidance recommendations for circulating fluidized bed boilers are determined.

[0118] In an optional embodiment, if the target coefficient is the reaction coefficient, the guidance suggestion for the circulating fluidized bed boiler is to increase the reaction temperature of the circulating fluidized bed boiler and check the hardware structure of the circulating fluidized bed boiler.

[0119] Preferably, if the target coefficient is the reaction coefficient and the gap is large, it may mean that the current reaction temperature is not enough to promote the NOx reduction reaction. Therefore, it is recommended to increase the reaction temperature of the CFB boiler to improve the denitrification efficiency. At the same time, it is also necessary to check the operating parameters of the boiler, such as coal feed, air distribution, etc., to ensure that they are in good condition and reasonably configured to support efficient denitrification reactions.

[0120] In another optional embodiment, if the target coefficient is a distribution coefficient, the guidance suggestion for the circulating fluidized bed boiler is to differentially adjust the input of the reducing agent to each separator according to the distribution coefficient.

[0121] Preferably, if the target coefficient is the distribution coefficient, and the difference is large, it means that the current flue gas distribution is uneven, resulting in the reductant of each separator not matching the actual flue gas volume in the optimal range. In this case, it is recommended to adjust the input amount of the reductant of each separator according to the distribution coefficient to optimize the flue gas distribution and avoid unnecessary waste.

[0122] According to the determined guidance suggestions, formulate corresponding implementation plans and arrange professional personnel to implement them. After the implementation of the suggestions, it is necessary to continuously monitor the denitrification efficiency and other relevant parameters of the CFB boiler to ensure the effectiveness of the improvement measures. According to the monitoring results, timely collect feedback and make necessary adjustments to ensure that the CFB boiler can operate stably in the long term and meet environmental protection requirements.

[0123] Through the detailed expansion and implementation of the above steps, we can effectively determine whether the actual denitrification efficiency of the CFB boiler meets the standard, and formulate effective improvement measures accordingly to improve the denitrification performance and operating efficiency of the boiler.

[0124] The data processing method and data processing device based on the circulating fluidized bed boiler provided in the embodiment of the present application obtain the current reaction temperature of the circulating fluidized bed boiler, the type of reducing agent and the amount of flue gas flowing through each separator in the circulating fluidized bed boiler; determine the reaction coefficient of the circulating fluidized bed boiler according to the current reaction temperature and the type of reducing agent; determine the flue gas coefficient corresponding to each separator in the circulating fluidized bed boiler according to the amount of flue gas flowing through each separator in the circulating fluidized bed boiler; determine the distribution coefficient of the circulating fluidized bed boiler according to the flue gas volume and the flue gas coefficient corresponding to each separator; calculate the actual denitrification efficiency of the circulating fluidized bed boiler according to the reaction coefficient, the distribution coefficient and the designed denitrification efficiency, calculate the actual denitrification efficiency of the circulating fluidized bed boiler through the present application, grasp the relationship between the actual denitrification efficiency and the main influencing factors of denitrification, adjust the operating parameters to reduce the consumption of the reducing agent and reduce the cost.

[0125] The present application aims to propose a method for evaluating the actual denitrification efficiency of the SNCR denitrification process of a circulating fluidized bed boiler, to more specifically understand the influence of the main factors on the denitrification efficiency, and to provide guidance for the optimization of the operation control strategy.

[0126] This application reveals how various key factors in the circulating fluidized bed SNCR denitrification process work and affect the denitrification efficiency. This not only provides operators with specific guidance for adjusting and optimizing operations, but also provides a key reference for the refinement of automation control logic.

[0127] Through this application, the influence trend of temperature, load, K1 (spray gun structure, quantity, position), and K2 (separator structure) on denitrification efficiency can be understood, which can be used to optimize control logic, guide operation parameter adjustment, and optimize structure, thereby improving denitrification efficiency and saving reducing agent costs.

[0128] Based on the same inventive concept, a data processing device corresponding to the data processing method based on a circulating fluidized bed boiler is also provided in the embodiment of the present application. Since the principle of solving the problem by the device in the embodiment of the present application is similar to the data processing method based on a circulating fluidized bed boiler in the embodiment of the present application, the implementation of the device can refer to the implementation of the method, and the repeated parts will not be repeated.

[0129] See also Figure 6 , Figure 6 This is a schematic diagram of the structure of the data processing device provided in the embodiment of the present application. Figure 6 As shown in , the data processing device 600 includes:

[0130] The flue gas volume acquisition module 601 is used to acquire the current reaction temperature of the circulating fluidized bed boiler, the type of reducing agent, and the actual flue gas volume flowing through each separator in the circulating fluidized bed boiler;

[0131] A reaction coefficient determination module 602, for determining a reaction coefficient of the circulating fluidized bed boiler according to the current reaction temperature and the type of the reducing agent;

[0132] The flue gas coefficient determination module 603 is used to determine the flue gas coefficient corresponding to each separator according to the actual flue gas volume flowing through each separator in the circulating fluidized bed boiler;

[0133] A distribution coefficient determination module 604 is used to determine the distribution coefficient of the circulating fluidized bed boiler according to the actual flue gas volume and the flue gas coefficient corresponding to each separator;

[0134] The actual denitration efficiency calculation module 605 is used to calculate the actual denitration efficiency of the circulating fluidized bed boiler according to the reaction coefficient, the distribution coefficient and the designed denitration efficiency, and determine guidance suggestions for the circulating fluidized bed boiler.

[0135] See also Figure 7 , Figure 7 This is a schematic diagram of the structure of the electronic device provided in the embodiment of the present application. Figure 7 As shown in , the electronic device 700 includes a processor 710 , a memory 720 and a bus 730 .

[0136] The memory 720 stores machine-readable instructions executable by the processor 710. When the electronic device 700 is running, the processor 710 communicates with the memory 720 via the bus 730. When the machine-readable instructions are executed by the processor 710, the above-mentioned Figure 1 The steps of the data processing method based on the circulating fluidized bed boiler in the method embodiment shown in the figure, and the specific implementation method can be referred to the method embodiment, which will not be described in detail here.

[0137] The present application also provides a computer-readable storage medium on which a computer program is stored. When the computer program is executed by a processor, the computer program can execute the above-mentioned Figure 1 The steps of the data processing method based on the circulating fluidized bed boiler in the method embodiment shown in the figure, and the specific implementation method can be referred to the method embodiment, which will not be described in detail here.

[0138] Those skilled in the art can clearly understand that, for the convenience and brevity of description, the specific working processes of the systems, devices and units described above can refer to the corresponding processes in the aforementioned method embodiments and will not be repeated here.

[0139] In the several embodiments provided in the present application, it should be understood that the disclosed systems, devices and methods can be implemented in other ways. The device embodiments described above are merely schematic. For example, the division of the units is only a logical function division. There may be other division methods in actual implementation. For example, multiple units or components can be combined or integrated into another system, or some features can be ignored or not executed. Another point is that the mutual coupling or direct coupling or communication connection shown or discussed can be through some communication interfaces, and the indirect coupling or communication connection of devices or units can be electrical, mechanical or other forms.

[0140] The units described as separate components may or may not be physically separated, and the components shown as units may or may not be physical units, that is, they may be located in one place or distributed on multiple network units. Some or all of the units may be selected according to actual needs to achieve the purpose of the solution of this embodiment.

[0141] In addition, each functional unit in each embodiment of the present application may be integrated into one processing unit, or each unit may exist physically separately, or two or more units may be integrated into one unit.

[0142] If the functions are implemented in the form of software functional units and sold or used as independent products, they can be stored in a non-volatile computer-readable storage medium that is executable by a processor. Based on this understanding, the technical solution of the present application can essentially be embodied in the form of a software product, or in other words, the part that contributes to the prior art or the part of the technical solution. The computer software product is stored in a storage medium, including several instructions for a computer device (which can be a personal computer, a server, or a network device, etc.) to perform all or part of the steps of the method described in each embodiment of the present application. The aforementioned storage medium includes: various media that can store program codes, such as a USB flash drive, a mobile hard disk, a read-only memory (ROM), a random access memory (RAM), a magnetic disk or an optical disk.

[0143] Finally, it should be noted that the above-described embodiments are only specific implementation methods of the present application, which are used to illustrate the technical solutions of the present application, rather than to limit them. The protection scope of the present application is not limited thereto. Although the present application is described in detail with reference to the above-mentioned embodiments, ordinary technicians in the field should understand that any technician familiar with the technical field can still modify the technical solutions recorded in the above-mentioned embodiments within the technical scope disclosed in the present application, or can easily think of changes, or make equivalent replacements for some of the technical features therein; and these modifications, changes or replacements do not make the essence of the corresponding technical solutions deviate from the spirit and scope of the technical solutions of the embodiments of the present application, and should be included in the protection scope of the present application. Therefore, the protection scope of the present application shall be based on the protection scope of the claims.

Claims

1. A data processing method based on a circulating fluidized bed boiler, characterized in that: include: Obtain the current reaction temperature of the circulating fluidized bed boiler, the type of reducing agent, and the actual flue gas volume flowing through each separator in the circulating fluidized bed boiler; Determining a reaction coefficient of the circulating fluidized bed boiler according to the current reaction temperature and the type of the reducing agent; According to the actual flue gas volume flowing through each separator in the circulating fluidized bed boiler, the flue gas coefficient corresponding to each separator is determined; Determining the distribution coefficient of the circulating fluidized bed boiler according to the actual flue gas volume and the flue gas coefficient corresponding to each separator; According to the reaction coefficient, the distribution coefficient and the designed denitration efficiency, the actual denitration efficiency of the circulating fluidized bed boiler is calculated, and guidance suggestions for the circulating fluidized bed boiler are determined.

2. The method according to claim 1, characterized in that The reaction coefficient of the circulating fluidized bed boiler is determined by: Determining a target temperature according to the reducing agent type, wherein the target temperature is a temperature with the highest actual denitration efficiency in historical data recorded for the reducing agent type; Determine the injection mixing coefficient according to the injection gun structure of the circulating fluidized bed boiler and the type of the reducing agent; The reaction coefficient of the circulating fluidized bed boiler is calculated according to the target temperature, the current reaction temperature and the injection mixing coefficient.

3. The method according to claim 2, characterized in that The flue gas coefficient for each separator is determined by: Determine a preset state according to the target temperature and the type of reducing agent, and obtain a preset flue gas volume of each separator and a first sum of the preset flue gas volumes of all separators under the preset state; Determining a first fuel amount of the circulating fluidized bed boiler at a current reaction temperature and a second fuel amount of the circulating fluidized bed boiler at the preset state; Determining the structural coefficient of the circulating fluidized bed boiler according to the hood resistance of the circulating fluidized bed boiler and the resistance of all separators; determining a dimensionless standard deviation of the circulating fluidized bed boiler according to the first fuel amount, the second fuel amount, and the structural coefficient; For each separator, the actual smoke volume of the separator is compared with the target smoke threshold, and the smoke coefficient of the separator is calculated according to the comparison result. The target smoke threshold is the ratio of the second sum of the actual smoke volumes of all separators to the total number of all separators.

4. The method according to claim 3, characterized in that: For each separator, comparing the actual smoke volume of the separator with the target smoke volume, and calculating the smoke coefficient of the separator according to the comparison result, includes: For each separator, calculating a ratio of a preset flue gas volume of the separator to the first sum, a difference between the ratio and a preset constant, and a second product of the difference and the dimensionless standard deviation; For each separator, determining whether the actual smoke volume of the separator is greater than the target smoke threshold; For each separator, if the actual smoke volume of the separator is greater than the target smoke threshold, a difference between a preset constant and the second product is calculated, and the difference is used as the smoke coefficient of the separator; For each separator, if the actual smoke volume of the separator is not greater than the target smoke threshold, the sum of the preset constant and the second product is calculated, and the sum is used as the smoke coefficient of the separator.

5. The method according to claim 4, characterized in that The distribution coefficient of the circulating fluidized bed boiler is determined by: For each separator, calculating a first product of the smoke volume of the separator and the corresponding smoke coefficient; Calculate the third sum of the first products of all separators; The distribution coefficient of the circulating fluidized bed boiler is determined according to the ratio of the second sum to the third sum.

6. The method according to claim 1, characterized in that The guidance recommendations for the circulating fluidized bed boiler were determined by: Determining whether the actual denitration efficiency of the circulating fluidized bed boiler is greater than a preset denitration efficiency; If the actual denitration efficiency of the circulating fluidized bed boiler is greater than the preset denitration efficiency, then continue to calculate the actual denitration efficiency; If the actual denitration efficiency of the circulating fluidized bed boiler is not greater than the preset denitration efficiency, a target coefficient is selected from the reaction coefficient and the distribution coefficient, and the target coefficient is the coefficient with the largest difference between the reaction coefficient and the distribution coefficient and the preset constant; According to the target coefficient, guidance suggestions for the circulating fluidized bed boiler are determined.

7. The method according to claim 6, characterized in that Determining guidance suggestions for the circulating fluidized bed boiler according to the target coefficient includes: If the target coefficient is a reaction coefficient, the guidance suggestion for the circulating fluidized bed boiler is to increase the reaction temperature of the circulating fluidized bed boiler and check the hardware structure of the circulating fluidized bed boiler; If the target coefficient is a distribution coefficient, the guidance suggestion for the circulating fluidized bed boiler is to differentially adjust the input of the reducing agent to each separator according to the distribution coefficient.

8. A data processing device, characterized in that: include: A flue gas volume acquisition module, used to acquire the current reaction temperature of the circulating fluidized bed boiler, the type of reducing agent, and the actual flue gas volume flowing through each separator in the circulating fluidized bed boiler; A reaction coefficient determination module, used to determine the reaction coefficient of the circulating fluidized bed boiler according to the current reaction temperature and the type of the reducing agent; A flue gas coefficient determination module is used to determine the flue gas coefficient corresponding to each separator according to the actual flue gas volume flowing through each separator in the circulating fluidized bed boiler; A distribution coefficient determination module, used to determine the distribution coefficient of the circulating fluidized bed boiler according to the actual flue gas volume and the flue gas coefficient corresponding to each separator; The actual denitration efficiency calculation module is used to calculate the actual denitration efficiency of the circulating fluidized bed boiler according to the reaction coefficient, the distribution coefficient and the designed denitration efficiency, and determine guidance suggestions for the circulating fluidized bed boiler.

9. An electronic device, characterized in that: include: A processor, a memory and a bus, wherein the memory stores machine-readable instructions executable by the processor, and when the electronic device is running, the processor and the memory communicate via the bus, and the processor executes the machine-readable instructions to perform the steps of any method as claimed in claims 1 to 7.

10. A computer-readable storage medium, characterized in that: The computer-readable storage medium stores a computer program, and when the computer program is executed by a processor, the steps of the method according to any one of claims 1 to 7 are executed.

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