Gasification furnace control method, storage medium and electronic equipment

Abstract

The invention discloses a gasification furnace control method, a storage medium and electronic equipment, and the control method comprises the following steps: obtaining real-time gasification furnace state information of a gasification furnace, the real-time gasifier state information comprises real-time coal slurry flow, real-time coal slurry concentration, real-time oxygen flow, real-time oxygen concentration, real-time oxygen-coal ratio, real-time gasifier temperature and real-time effective methane content of a gasifier outlet; obtaining a target gasifier temperature of the gasifier according to the real-time gasifier state information and a preset gasifier temperature optimization model; calculating a target oxygen-coal ratio set value of at least one nozzle of the gasifier according to the target gasifier temperature; calculating a target oxygen flow set value according to the target oxygen-coal ratio set value and the real-time gasifier state information; and controlling the opening degree of an oxygen valve of the gasification furnace according to the target oxygen flow set value. According to the method, the gasification furnace can operate under the safe, stable and economic comprehensive optimal working condition, and the safety is improved.

Description

Technical Field

[0001] The present invention relates to the technical field of gasifiers, and in particular to a gasifier control method, a storage medium and an electronic device. Background Art

[0002] Coal-water slurry gasifier is a device that uses coal-water slurry as raw material for gasification. Raw coal and water are crushed and mixed into coal-water slurry (coal concentration is ), water-coal slurry and oxygen enter the gasifier, and are converted into synthesis gas (CO, H2, CO2, CH4, etc.) through gasification, combustion, water-gas reaction, etc. in the gasifier and enter the downstream conversion system. The incombustible components of the coal (such as inorganic salts) are discharged from the lower slag outlet in the gasifier in a molten form.

[0003] The risk of water-coal slurry gasification furnace operation is relatively high. If the raw material oxygen is excessive, it will cause the gasification furnace to overheat, affecting the service life of the furnace bricks. In severe cases, the unreacted oxygen and synthesis gas will enter the downstream system to form an explosive atmosphere, causing an over-oxygen explosion. Insufficient raw material oxygen will cause the gasification furnace temperature to be low, the slag fluidity to decrease, and in severe cases, the gasification furnace will be blocked and stopped. In addition, improper control of the gasification furnace will also lead to a part of the effective gas production loss.

[0004] At present, the existing gasifier control system manually judges the actual operating status of the gasifier, such as the gasifier temperature and effective gas composition, and then intervenes by manually adjusting the valve position of the main oxygen valve according to the deviation between the actual operating status of the gasifier and the ideal status judged by production experience. There are problems such as large amount of personnel operation, unstable control of key parameters of the gasifier, and untimely discovery of gasifier anomalies. Summary of the invention

[0005] The purpose of the present invention is to overcome the deficiencies of the prior art and provide a gasifier control method, storage medium and electronic equipment to ensure that the gasifier operates under safe, stable and economically optimal conditions, reduce the labor intensity of operators and improve safety.

[0006] The technical solution of the present invention provides a gasifier control method, comprising:

[0007] Acquire real-time gasifier status information of the gasifier, wherein the real-time gasifier status information includes real-time coal slurry flow, real-time coal slurry concentration, real-time oxygen flow, real-time oxygen concentration, real-time oxygen-coal ratio, real-time gasifier temperature and real-time effective methane content at the gasifier outlet;

[0008] Obtaining a target gasifier temperature of the gasifier according to the real-time gasifier state information and a preset furnace temperature optimization model;

[0009] Calculating a target oxygen-coal ratio setting value of at least one nozzle of the gasifier according to the target gasifier temperature;

[0010] Calculating a target oxygen flow rate setting value according to the target oxygen-coal ratio setting value and the real-time gasifier state information;

[0011] The oxygen valve opening of the gasifier is controlled according to the target oxygen flow setting value.

[0012] Furthermore, the furnace temperature optimization model is obtained by the following method:

[0013] Acquire historical gasifier state information of the gasifier, wherein the historical gasifier state information includes a first historical gasifier temperature, a first historical effective gas methane content, a historical oxygen-coal ratio, a historical gasifier load, and a historical gasifier pressure;

[0014] The historical gasification furnace state information is trained using a random forest algorithm to obtain the furnace temperature optimization model.

[0015] Furthermore, obtaining the target gasifier temperature of the gasifier according to the real-time gasifier state information and a preset furnace temperature optimization model includes:

[0016] Decomposing the real-time oxygen-coal ratio into a plurality of sub-real-time oxygen-coal ratios according to a preset range;

[0017] Inputting the plurality of sub-real-time oxygen-coal ratios and the real-time gasifier state information into the furnace temperature optimization model to obtain a plurality of furnace temperature optimization indicators and sub-target gasifier temperatures, wherein the furnace temperature optimization indicator refers to a comprehensive operating indicator of the operating stability and effective gas yield of the gasifier;

[0018] The sub-target gasifier temperature corresponding to the maximum furnace temperature optimization index among the furnace temperature optimization indexes is used as the target gasifier temperature.

[0019] Furthermore, the real-time gasifier temperature corresponding to the maximum furnace temperature optimization index is used as the target gasifier temperature, and then the following is further included:

[0020] Using a first-order exponential decay algorithm to decompose the target gasifier temperature into a plurality of sub-target gasifier temperatures according to a preset number of decomposition steps;

[0021] sequentially adjusting the temperature of the gasifier according to the plurality of sub-target gasifier temperatures;

[0022] If the furnace temperature setting value is the same as the target gasification furnace temperature, the temperature adjustment of the gasification furnace is stopped.

[0023] Furthermore, the target gasifier temperature of the gasifier is obtained according to the real-time gasifier state information and a preset furnace temperature optimization model, and the method further includes:

[0024] If the real-time gasifier status information does not meet the following conditions, stop the optimization;

[0025]

[0026] Where n is time; C i is the historical gasifier status information before the i-th moment; C i+1 is the gasifier status information at the i+1th moment; is the average value of the real-time gasifier status information within the time; Q is a preset constant.

[0027] Further, the target oxygen-coal ratio setting value of the nozzle of the gasifier is calculated according to the target gasifier temperature, including:

[0028] Acquire historical gasifier state information of the gasifier under various operating conditions, wherein the historical gasifier state information includes a first historical gasifier temperature, a historical effective methane content, and a historical oxygen-coal ratio setting value;

[0029] Performing model identification according to the historical gasifier state information to obtain transfer functions in different time periods, wherein the transfer functions include a gain coefficient, a lag time, and a time constant;

[0030] The transfer function is classified according to the gain coefficient, the lag time and the time constant to obtain a gasifier operation control matrix corresponding to the historical gasifier state information, wherein the gasifier operation control matrix is ​​a correspondence matrix between the first historical gasifier temperature and / or the historical effective methane content and the transfer function and the oxygen-coal ratio set value;

[0031] If the real-time gasifier temperature and / or the real-time effective methane content are consistent with the first historical gasifier temperature and / or the historical effective methane content in the gasifier operation control matrix, the oxygen-coal ratio set value corresponding to the first historical gasifier temperature and / or the historical effective methane content is used as the target oxygen-coal ratio set value.

[0032] Furthermore, the number of the nozzles is multiple, and the target oxygen-coal ratio setting value is obtained according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix, and then the following further includes:

[0033] If the target oxygen-coal ratio setting value meets the following conditions, the target oxygen flow rate setting value is calculated according to the target oxygen-coal ratio setting value and the real-time gasifier state information:

[0034]

[0035] Where n is the number of nozzles; MV xis the target oxygen-coal ratio setting value of any nozzle; MV x+1 For MV x The target oxygen-coal ratio setting value of the next adjacent nozzle; MV n is the target oxygen-coal ratio setting value of the nth nozzle; D is a preset constant.

[0036] Further, obtaining the target oxygen-coal ratio setting value according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix includes:

[0037] Within a preset time period, calculating the furnace temperature average value of the real-time gasification furnace temperature and / or the methane content average value of the real-time effective methane content according to a preset calculation cycle;

[0038] The target oxygen-coal ratio setting value is obtained according to the average furnace temperature and / or the average methane content and the gasifier operation control matrix.

[0039] Further, obtaining the target oxygen-coal ratio setting value according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix includes:

[0040] Acquire a second historical gasifier temperature adjacent to the real-time gasifier temperature;

[0041] If the difference between the real-time gasifier temperature and the second historical gasifier temperature is greater than or equal to the preset minimum gasifier temperature threshold, the difference between the real-time gasifier temperature and the second historical gasifier temperature is less than or equal to the preset maximum gasifier temperature threshold, the real-time gasifier temperature is greater than or equal to the preset minimum gasifier confidence threshold, and the real-time gasifier temperature is less than or equal to the preset maximum gasifier confidence threshold, the target oxygen-coal ratio setting value is obtained according to the real-time gasifier temperature and the gasifier operation control matrix.

[0042] Further, obtaining the target oxygen-coal ratio setting value according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix includes:

[0043] Acquire a second historical effective gas methane content adjacent to the real-time effective gas content;

[0044] If the difference between the real-time effective gas methane content and the second historical effective gas methane content is greater than or equal to the preset minimum effective gas content threshold, the difference between the real-time effective gas methane content and the second historical effective gas methane content is less than or equal to the preset maximum effective gas content threshold, the real-time effective methane content is greater than or equal to the preset minimum confidence value of the effective gas content, and the real-time effective methane content is less than or equal to the preset maximum confidence value of the effective gas content, the target oxygen-coal ratio setting value is obtained according to the real-time effective methane content and the gasifier operation control matrix.

[0045] Furthermore, the number of the nozzles is multiple, the real-time oxygen flow rate includes a real-time main pipe oxygen flow rate, the real-time coal slurry flow rate includes a real-time main pipe coal slurry flow rate, the target oxygen-coal ratio setting value includes a target main pipe oxygen-coal ratio setting value and a target central pipe oxygen-coal ratio setting value, the target oxygen flow rate setting value includes a target main pipe oxygen flow rate setting value and a target central pipe oxygen flow rate setting value, and the target oxygen flow rate setting value is calculated according to the target oxygen-coal ratio setting value and the real-time gasifier state information, including:

[0046] Arrange the real-time main pipe coal slurry flow rates in ascending order to obtain the middle main pipe coal slurry flow rate;

[0047] Calculate the product of the target main pipe oxygen-coal ratio setting value, the intermediate main pipe coal slurry flow rate and the real-time coal slurry concentration, and divide the result by the real-time oxygen concentration to obtain the target main pipe oxygen flow rate setting value;

[0048] Arrange the real-time main pipe oxygen flow rates in ascending order to obtain the middle main pipe oxygen flow rate in the middle;

[0049] The product of the target central tube oxygen-coal ratio setting value and the intermediate main tube oxygen flow rate is calculated to obtain the target central tube oxygen flow rate setting value.

[0050] Furthermore, the real-time oxygen flow rate also includes the real-time central pipe oxygen flow rate, the oxygen valve opening includes the main pipe oxygen valve opening and the central pipe oxygen valve opening, and the oxygen valve opening of the gasifier is controlled according to the target oxygen flow rate setting value, including:

[0051] Calculating the deviation between the target main pipe oxygen flow setting value and the intermediate main pipe oxygen flow to obtain a main pipe deviation value;

[0052] Arrange the real-time central tube oxygen flow rates in ascending order to obtain the middle central tube oxygen flow rate;

[0053] Calculating the deviation between the target central tube oxygen flow rate setting value and the intermediate central tube oxygen flow rate to obtain a central tube deviation value;

[0054] The main pipe deviation value and the central pipe deviation value are calculated using a proportional-integral-differential algorithm to obtain the main pipe oxygen valve opening value and the central pipe oxygen valve opening value respectively;

[0055] The main pipe oxygen valve opening and the central pipe oxygen valve opening are controlled respectively according to the main pipe oxygen valve opening value and the central pipe oxygen valve opening value.

[0056] Furthermore, the oxygen valve opening of the gasifier is controlled according to the target oxygen flow setting value, and then further includes:

[0057] According to the real-time gasifier status information and a preset fault warning model, it is determined whether the gasifier fails. The fault warning model is used to store corresponding fault features when the gasifier fails.

[0058] The technical solution of the present invention further provides a storage medium, which stores computer instructions. When a computer executes the computer instructions, it is used to execute all the steps of the gasifier control method as described above.

[0059] The technical solution of the present invention further provides an electronic device, comprising:

[0060] at least one processor; and,

[0061] a memory communicatively connected to the at least one processor; wherein,

[0062] The memory stores instructions that can be executed by the at least one processor. The instructions are executed by the at least one processor so that the at least one processor can perform the gasifier control method as described above.

[0063] The adoption of the above technical scheme has the following beneficial effects: by acquiring the real-time gasifier status information of the gasifier in real time, the target gasifier temperature of the gasifier is obtained according to the real-time gasifier status information and a preset furnace temperature optimization model, the target oxygen-coal ratio setting value of at least one nozzle of the gasifier is calculated according to the target gasifier temperature, the target oxygen flow rate setting value is calculated according to the target oxygen-coal ratio setting value and the real-time gasifier status information, and the oxygen valve opening of the gasifier is controlled according to the target oxygen flow rate setting value, thereby ensuring that the gasifier operates under safe, stable and economically optimal conditions, reducing the labor intensity of operators and improving safety. BRIEF DESCRIPTION OF THE DRAWINGS

[0064] The disclosure of the present invention will become more easily understood with reference to the accompanying drawings. It should be understood that these drawings are only for illustrative purposes and are not intended to limit the scope of protection of the present invention. In the drawings:

[0065] Figure 1 A flowchart of a gasifier control method provided in Example 1 of the present invention;

[0066] Figure 2 A working flow chart of a gasifier control method provided in Embodiment 2 of the present invention;

[0067] Figure 3 A working flow chart of a gasifier control method provided in Embodiment 3 of the present invention;

[0068] Figure 4 A working flow chart of a gasifier control method provided in Embodiment 4 of the present invention;

[0069] Figure 5 It is a structural schematic diagram of the gasifier system of Example 1 and Example 2;

[0070] Figure 6 Optimize flow charts for scrolling;

[0071] Figure 7 A schematic diagram of the hardware structure of an electronic device for controlling a gasifier provided in Example 6 of the present invention. DETAILED DESCRIPTION

[0072] The specific implementation of the present invention will be further described below in conjunction with the accompanying drawings.

[0073] It is easy to understand that according to the technical solution of the present invention, without changing the essential spirit of the present invention, a variety of structural modes and implementation modes that can be replaced by those skilled in the art can be replaced with each other. Therefore, the following specific implementation modes and drawings are only exemplary descriptions of the technical solution of the present invention, and should not be regarded as the whole of the present invention or as a limitation or restriction to the technical solution of the invention.

[0074] The directional terms such as up, down, left, right, front, back, front, back, top, bottom, etc. mentioned or may be mentioned in this specification are defined relative to the structures shown in the drawings. They are relative concepts and may change accordingly according to different positions and different usage conditions. Therefore, these or other directional terms should not be interpreted as restrictive terms.

[0075] Embodiment 1

[0076] like Figure 1 As shown, a gasifier control method provided by Embodiment 1 of the present invention includes:

[0077] Step S101: acquiring real-time gasifier status information of the gasifier, the real-time gasifier status information including real-time coal slurry flow, real-time coal slurry concentration, real-time oxygen flow, real-time oxygen concentration, real-time oxygen-coal ratio, real-time gasifier temperature and real-time effective methane content at the gasifier outlet;

[0078] Step S102: obtaining a target gasifier temperature of the gasifier according to the real-time gasifier state information and a preset furnace temperature optimization model;

[0079] Step S103: calculating a target oxygen-coal ratio setting value of at least one nozzle of the gasifier according to the target gasifier temperature;

[0080] Step S104: Calculate a target oxygen flow rate setting value according to the target oxygen-coal ratio setting value and the real-time gasifier state information;

[0081] Step S105: controlling the opening of the oxygen valve of the gasifier according to the target oxygen flow setting value.

[0082] Specifically, when the gasifier is running, first, the controller executes step S101 to obtain the real-time gasifier state information of the gasifier in real time, and the real-time gasifier state information includes real-time coal slurry flow, real-time coal slurry concentration, real-time oxygen flow, real-time oxygen concentration, real-time oxygen-coal ratio, real-time gasifier temperature and real-time effective methane (CH4) content at the outlet of the gasifier; secondly, the controller executes step S102 to obtain the target gasifier temperature of the gasifier according to the real-time gasifier state information and a preset furnace temperature optimization model, and the furnace temperature optimization model refers to a model of the gasifier operation state and the optimal operation temperature of the gasifier; then, the controller executes step S103 to obtain the target gasifier temperature of the gasifier according to the real-time gasifier state information and a preset furnace temperature optimization model; A target oxygen-coal ratio setting value of at least one nozzle of the gasifier is calculated according to the target gasifier temperature. The number of nozzles is at least one. When the number of nozzles is multiple, the target oxygen-coal ratio setting value of each nozzle is calculated according to the target gasifier temperature; then, the controller executes step S104 to calculate the target oxygen flow rate setting value according to the target oxygen-coal ratio setting value and real-time gasifier status information; finally, the controller executes step S105 to control the oxygen valve opening of the gasifier according to the target oxygen flow rate setting value, thereby ensuring that the gasifier operates under the safe, stable and economically optimal working conditions, reducing the labor intensity of operators and improving safety.

[0083] According to an embodiment of the present invention, real-time gasifier status information of the gasifier is acquired in real time, a target gasifier temperature of the gasifier is obtained according to the real-time gasifier status information and a preset furnace temperature optimization model, a target oxygen-coal ratio setting value of at least one nozzle of the gasifier is calculated according to the target gasifier temperature, a target oxygen flow rate setting value is calculated according to the target oxygen-coal ratio setting value and the real-time gasifier status information, and the oxygen valve opening of the gasifier is controlled according to the target oxygen flow rate setting value, thereby ensuring that the gasifier operates under safe, stable and economically optimal working conditions, reducing the labor intensity of operators and improving safety.

[0084] In one embodiment, the furnace temperature optimization model is obtained by the following method:

[0085] Acquire historical gasifier state information of the gasifier, the historical gasifier state information including a first historical gasifier temperature, a first historical effective gas methane content, a historical oxygen-coal ratio, a historical gasifier load, and a historical gasifier pressure;

[0086] The historical gasifier state information is trained using the random forest algorithm to obtain the furnace temperature optimization model.

[0087] Specifically, historical gasifier state information of the gasifier is obtained, where the historical gasifier state information refers to the gasifier state information of the gasifier under normal and safe operation conditions;

[0088] Construct a random forest algorithm model, including input layer and output layer. The input layer is the first layer and is set to nozzle 1. Nozzle n oxygen-coal ratio, nozzle 1 Nozzle n center oxygen flow, coal slurry concentration, gasifier temperature, gasifier pressure, nozzle 1 The nozzle n pressure difference, gasifier outlet temperature, gasifier liquid level, furnace temperature, ambient temperature, and raw coal calorific value are (11+3n) variables in total. The output layer is the second layer, which is set to the optimal operating temperature of the gasifier. The historical gasifier state information is input into the input layer, and the random forest algorithm is used for training to obtain the furnace temperature optimization model.

[0089] Among them, the split characteristics of the random forest algorithm model construction process are Preferably The random forest size is Preferably

[0090] In one embodiment, step S102 includes:

[0091] Decomposing the real-time oxygen-coal ratio into a plurality of sub-real-time oxygen-coal ratios according to a preset range;

[0092] Input multiple sub-real-time oxygen-coal ratios and real-time gasifier state information into the furnace temperature optimization model to obtain multiple furnace temperature optimization indicators and sub-target gasifier temperatures. The furnace temperature optimization indicator refers to a comprehensive operating indicator of the gasifier's operating stability and effective gas yield.

[0093] The sub-target gasifier temperature corresponding to the maximum furnace temperature optimization index in the furnace temperature optimization index is used as the target gasifier temperature.

[0094] Specifically, the output layer of the random forest algorithm model is also set as the furnace temperature optimization index, which adjusts the real-time oxygen-coal ratio according to the preset range (such as ) is split into multiple sub-real-time oxygen-coal ratios, and the multiple sub-real-time oxygen-coal ratios and the real-time gasifier state information are input into the furnace temperature optimization model to obtain the furnace temperature optimization index and sub-target gasifier temperature corresponding to each sub-real-time oxygen-coal ratio, and the sub-target gasifier temperature corresponding to the maximum furnace temperature optimization index is used as the target gasifier temperature.

[0095] Preferably, the furnace temperature optimization index is calculated using the following formula:

[0096] G=W1×Y+W2×V1+W3×V2

[0097] Among them, G is the furnace temperature optimization index; W1 is the yield weight of the real-time effective methane content; Y is the effective gas yield; W2 is the steady-state index weight of the gasifier; V1 is the steady-state judgment index of the key parameters of the gasifier at the future time T1; W3 is the fault probability index weight of the gasifier; V2 is the fault probability of the gasifier at the future time T2.

[0098] In one embodiment, step S102 further includes:

[0099] A first-order exponential decay algorithm is used to decompose the target gasifier temperature into multiple sub-target gasifier temperatures according to a preset number of decomposition steps;

[0100] adjusting the temperature of the gasifier in sequence according to the multiple sub-target gasifier temperatures;

[0101] If the furnace temperature setting value is the same as the target gasifier temperature, stop adjusting the temperature of the gasifier.

[0102] Specifically, a first-order exponential decay algorithm is used to optimize the target gasifier temperature, and the temperature of the gasifier is adjusted until the furnace temperature set value is the same as the target gasifier temperature. Then, the adjustment of the temperature of the gasifier is stopped. The target gasifier temperature is decomposed into a temperature optimization route, and the temperature of the gasifier is gradually adjusted according to the temperature optimization route, thereby achieving stable adjustment of the temperature of the gasifier and further improving stability and safety.

[0103] The following example takes the furnace temperature optimization target value as T(e), the furnace temperature setting value before optimization as T(0), and the decomposition frequency as n as an example to explain the optimization of the gasifier temperature. That is, from T(0) to T(e) is divided into n steps. The sub-target gasifier temperature of each step after decomposition using the first-order exponential decay algorithm is as follows:

[0104] T(1) (first step to optimize furnace temperature) = T(e) + [T(0) - T(e)] * e -0.125 ) / (e -0.125 +e -0.25 +...+e -0.125*n );

[0105] T(2) (second step to optimize furnace temperature) = T(1) + [T(0) - T(e)] * e -0.25 / (e -0.125 +e -0.25 +...+e -0.125*n ); ...

[0107] T(n) (optimized furnace temperature in step n) = T(n-1) + [T(0)-T(e)]*e -0.125*n / (e -0.125 +e -0.25 +...+e -0.125*n ),

[0108] If T(n) is equal to the furnace temperature setting value, stop adjusting the temperature of the gasifier.

[0109] In one embodiment, step S102, before that, also includes:

[0110] If the real-time gasifier status information does not meet the following conditions, stop the optimization;

[0111]

[0112] Where n is time; C i is the historical gasifier status information before the i-th moment; C i+1 is the gasifier status information at the i+1th moment; is the average value of the real-time gasifier status information within the time; Q is a preset constant.

[0113] Specifically, in order to ensure that the gasifier is in a stable state, the controller determines whether each parameter measurement value in the real-time gasifier state information satisfies the above-mentioned condition (1). If so, the gasifier is considered to be in a stable state and the optimization can continue. If not, the optimization is stopped.

[0114] Embodiment 2

[0115] Based on the first embodiment, Figure 2 As shown, a gasifier control method provided by Embodiment 2 of the present invention includes:

[0116] Step S201: Acquire historical gasifier state information of the gasifier under various operating conditions, wherein the historical gasifier state information includes a first historical gasifier temperature, a historical effective methane content, and a historical oxygen-coal ratio setting value;

[0117] Step S202: Perform model identification based on historical gasifier state information to obtain transfer functions in different time periods, where the transfer functions include a gain coefficient, a lag time, and a time constant;

[0118] Step S203: Classifying the transfer function according to the gain coefficient, the lag time and the time constant to obtain a gasifier operation control matrix corresponding to the historical gasifier state information, wherein the gasifier operation control matrix is ​​a correspondence matrix between the first historical gasifier temperature and / or the historical effective methane content and the transfer function and the target oxygen-coal ratio setting value;

[0119] Step S204: If the real-time gasifier temperature and / or the real-time effective methane content are consistent with the first historical gasifier temperature and / or the historical effective methane content in the gasifier operation control matrix, the oxygen-coal ratio set value corresponding to the first historical gasifier temperature and / or the historical effective methane content is used as the target oxygen-coal ratio set value.

[0120] Specifically, since the gasifier has strong nonlinearity, in order to ensure good control effects under different operating conditions and improve the robustness of the gasifier, first, the controller executes step S201 to obtain historical gasifier state information of the gasifier under various operating conditions. Different types of gasifiers have different operating conditions, and different operating conditions can be set according to the load. The historical gasifier state information refers to the gasifier state information of the gasifier in a stable state under different operating conditions;

[0121] Next, step S202 is executed to input the historical gasifier state information into the transfer function model. Preferably, the transfer function model is: Among them, G is the gain coefficient, D is the lag time, T is the time constant, and s is the time unit second. Inputting the historical gasifier state information into the transfer function model, the corresponding relationship between the three variables G, D, and T in the transfer function model is obtained, thereby obtaining the transfer function in different time periods; then, executing step S203 to classify the transfer function according to the gain coefficient, lag time, and time constant, such as m types (m≥1) of different gasifier operating conditions can be divided according to the gain coefficient, lag time, and time constant, each condition corresponds to a set of control matrices of the gasifier temperature and / or effective gas CH4 content to the nozzle oxygen-coal ratio setting value, and the m control matrices constitute a main control matrix group, the control matrix includes controlled variables and operating variables, wherein the controlled variables are gasifier indicators to be controlled, including the gasifier temperature (CV1) and the effective gas CH4 content (CV2); the operating variables are gasifier parameters that have an effect on the controlled variables and can be used to adjust the controlled variables. When the number of nozzles is n, the operating variables include the target oxygen-coal ratio setting values ​​(MV1, MV2, ..., MVn) of nozzle 1, nozzle 2, ..., nozzle n, and the specific form of the main control matrix group can be as follows:

[0122]

[0123]

[0124] …

[0125]

[0126] in, They are control matrix 1 Control matrix m gasifier furnace temperature to nozzle 1 Transfer function of nozzle n oxygen-coal ratio, They are control matrix 1 Control matrix m gasifier effective gas CH4 content to nozzle 1 Transfer function of nozzle n oxygen-coal ratio;

[0127] Finally, step S204 is executed to determine the target oxygen-coal ratio setting value according to the acquired real-time gasifier temperature and / or real-time effective methane content. For example, when the real-time gasifier temperature and / or real-time effective methane content are consistent with CV1 and / or CV2 in the control matrix 1 in the above-mentioned main control matrix group, the corresponding MV1 in the control matrix 1 is set as the target oxygen-coal ratio setting value. The real-time gasifier temperature and / or real-time effective methane content are matched with the target oxygen-coal ratio setting value in the form of a control matrix, thereby realizing adaptive judgment of the target oxygen-coal ratio setting value, improving accuracy, and further improving stability and safety.

[0128] In one embodiment, the number of nozzles is multiple, and step S204 further includes:

[0129] If the target oxygen-coal ratio setting value meets the following conditions, the target oxygen flow setting value is calculated based on the target oxygen-coal ratio setting value and the real-time gasifier status information:

[0130]

[0131] Where n is the number of nozzles; MV x is the target oxygen-coal ratio setting value of any nozzle; MV x+1 For MV x The target oxygen-coal ratio setting value of the next adjacent nozzle; MV n is the target oxygen-coal ratio setting value of the nth nozzle; D is a preset constant.

[0132] Specifically, when there are multiple nozzles, in order to prevent the oxygen flow deviation of multiple nozzles from being too large and affecting the flow field balance in the gasifier, the controller calculates the square value of the difference between the target oxygen-coal ratio setting values ​​of any two nozzles, and determines whether the value of MV1-MVn in the main control matrix group is allowed to be the final value. If it is greater than the preset constant D, the oxygen flow valve opening will not be adjusted and the status quo will be maintained. Otherwise, the target oxygen flow setting value is calculated based on the target oxygen-coal ratio setting value and the real-time gasifier status information, and the oxygen flow valve opening is adjusted according to the target oxygen flow setting value.

[0133] In one embodiment, obtaining the target oxygen-coal ratio setting value according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix includes:

[0134] Within a preset time period, calculating the furnace temperature average value of the real-time gasification furnace temperature and / or the methane content average value of the real-time effective methane content according to a preset calculation cycle;

[0135] The target oxygen-coal ratio setting value is obtained according to the average furnace temperature and / or the average methane content and the gasifier operation control matrix.

[0136] Specifically, in order to prevent high-frequency disturbances in the real-time gasifier temperature and / or the real-time effective methane content, which may lead to misadjustment, the controller uses the following formula to calculate the average furnace temperature and / or the average methane content:

[0137]

[0138]

[0139] CV1 i : The measured value of gasifier temperature before the i-th minute;

[0140] n1: preset moving average value of gasification furnace temperature, preferably 2-10;

[0141] CV2 i : The measured value of effective gas CH4 content before the i-th minute

[0142] n2: preset moving average value of effective gas CH4 content, preferably 2-10.

[0143] Among them, n1 and n2 can be set according to the instrument performance.

[0144] Among them, the preset calculation cycle can be set according to the instrument noise cycle. Different instruments have different noises, and the preset calculation cycle needs to cover the instrument noise cycle.

[0145] In one embodiment, obtaining the target oxygen-coal ratio setting value according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix includes:

[0146] Acquire a second historical gasifier temperature adjacent to the real-time gasifier temperature;

[0147] If the difference between the real-time gasifier temperature and the second historical gasifier temperature is greater than or equal to the preset minimum gasifier temperature threshold, the difference between the real-time gasifier temperature and the second historical gasifier temperature is less than or equal to the preset maximum gasifier temperature threshold, the real-time gasifier temperature is greater than or equal to the preset minimum gasifier confidence threshold, and the real-time gasifier temperature is less than or equal to the preset maximum gasifier confidence threshold, the target oxygen-coal ratio setting value is obtained according to the real-time gasifier temperature and the gasifier operation control matrix.

[0148] Specifically, in order to prevent the real-time gasifier temperature measuring instrument from indicating abnormalities and causing misadjustment, the controller uses the following judgment conditions to monitor whether the real-time gasifier temperature is valid. If it is valid, it indicates that it can operate normally. According to the real-time gasifier temperature and the gasifier operation control matrix, the target oxygen-coal ratio setting value is obtained, and the oxygen-coal ratio setting value of the nozzle is adjusted. Otherwise, the oxygen-coal ratio setting value of the nozzle is not adjusted.

[0149] The furnace temperature effectiveness monitoring conditions are as follows:

[0150]

[0151] A3≤CV1≤A4

[0152] n: preset gasification furnace temperature effectiveness judgment time domain, preferably 2-20;

[0153] A1: The sum of the minimum allowable deviations of the preset gasification furnace temperature, preferably 1-10°C;

[0154] A2: The sum of the maximum allowable deviations of the preset gasification furnace temperature, preferably 5-50°C;

[0155] A3: preset the minimum confidence value of the gasification furnace temperature, preferably 1000-1200℃;

[0156] A4: Preset the maximum confidence value of the gasification furnace temperature, preferably 1200-1400°C.

[0157] In one embodiment, obtaining the target oxygen-coal ratio setting value according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix includes:

[0158] Acquire a second historical effective gas methane content adjacent to the real-time effective gas content;

[0159] If the difference between the real-time effective gas methane content and the second historical effective gas methane content is greater than or equal to the preset minimum effective gas content threshold, the difference between the real-time effective gas methane content and the second historical effective gas methane content is less than or equal to the preset maximum effective gas content threshold, the real-time effective methane content is greater than or equal to the preset minimum confidence value of the effective gas content, and the real-time effective methane content is less than or equal to the preset maximum confidence value of the effective gas content, the target oxygen-coal ratio setting value is obtained according to the real-time effective methane content and the gasifier operation control matrix.

[0160] Specifically, in order to prevent the real-time effective methane content measurement instrument from indicating abnormalities and causing misadjustment, the controller uses the following judgment conditions to monitor whether the real-time effective methane content is valid. If it is valid, it indicates normal operation. According to the real-time effective methane content and the gasifier operation control matrix, the target oxygen-coal ratio setting value is obtained and the oxygen-coal ratio setting value of the nozzle is adjusted. Otherwise, the oxygen-coal ratio setting value of the nozzle is not adjusted:

[0161]

[0162] A7≤CV2≤A8

[0163] n: preset effective gas CH4 content validity judgment time domain, preferably 2-20;

[0164] A5: The sum of the minimum allowable deviations of the CH4 content in the preset effective gas, preferably 0-30ppm;

[0165] A6: The sum of the maximum allowable deviations of the CH4 content in the preset effective gas is preferably 40-100ppm;

[0166] A7: Preset the minimum confidence value of effective gas CH4 content, preferably 100-300ppm;

[0167] A8: Preset the maximum confidence value of effective gas CH4 content, preferably 1000-1300ppm.

[0168] Embodiment 3

[0169] On the basis of Example 1-Example 2, Figure 3 As shown, a gasifier control method provided by Embodiment 3 of the present invention includes:

[0170] Step S301: arranging the real-time main pipe coal slurry flow rates in ascending order, and obtaining the middle main pipe coal slurry flow rate in the middle;

[0171] Step S302: Calculate the product of the target main pipe oxygen-coal ratio setting value, the intermediate main pipe coal slurry flow rate and the real-time coal slurry concentration, and divide the quotient by the real-time oxygen concentration to obtain the target main pipe oxygen flow rate setting value;

[0172] Step S303: Arrange the real-time main pipe oxygen flow rates in ascending order, and obtain the middle main pipe oxygen flow rate in the middle;

[0173] Step S304: Calculate the product of the target central tube oxygen-coal ratio setting value and the intermediate main tube oxygen flow rate to obtain the target central tube oxygen flow rate setting value.

[0174] Specifically, the real-time oxygen flow rate includes the real-time main pipe oxygen flow rate, the real-time coal slurry flow rate includes the real-time main pipe coal slurry flow rate, the target oxygen-coal ratio setting value includes the target main pipe oxygen-coal ratio setting value and the target central pipe oxygen-coal ratio setting value. When the number of nozzles is multiple (set to n), the gasifier control system includes m1 coal slurry flow sensors, m2 main pipe oxygen flow sensors, m3 central oxygen flow sensors, 1 coal slurry concentration sensor, 1 oxygen concentration sensor, 1 main pipe oxygen regulating valve, 1 central oxygen regulating valve and at least 1 controller. The controller first executes step S301-step S302 to calculate the target main pipe oxygen flow setting value of each nozzle using the following formula:

[0175] FT1=[RT1×MID(FM11,…,FM1m1)×AM]÷AO;

[0176] FT2=[RT2×MID(FM21,…,FM2m1)×AM]÷AO;

[0177] …

[0178] FTn=[RTn×MID(FMn1,…,FMnm1)×AM]÷AO;

[0179] Nozzle 1 Target manifold oxygen flow setting value for nozzle n;

[0180] Nozzle 1 Target main pipe oxygen-coal ratio setting value for nozzle n;

[0181] Nozzle 1 Line 1 The real-time main coal slurry flow of m1;

[0182] Nozzle 2 Line 1 The real-time main coal slurry flow of m1;

[0183] Nozzle n Line 1 The real-time main coal slurry flow of m1;

[0184] AM: real-time coal slurry concentration;

[0185] AO: Real-time oxygen concentration.

[0186] Then, step S303-step S304 is executed to calculate the target central tube oxygen flow setting value of each nozzle using the following formula:

[0187] FC1=RC1×MID(FO11,…,FO1m2);

[0188] FC2=RC2×MID(FO21,…,FO2m2);

[0189] …

[0190] FCn=RCn×MID(FOn1,…,FOnm2);

[0191] Nozzle 1 Target central tube oxygen flow setting value for nozzle n;

[0192] Nozzle 1 The target center tube oxygen-coal ratio setting value of nozzle n;

[0193] Nozzle 1 Line 1 The oxygen flow rate of the intermediate main pipe of m2;

[0194] Nozzle 2 Line 1 The oxygen flow rate of the intermediate main pipe of m2;

[0195] Nozzle n Line 1 The oxygen flow rate of the intermediate main pipe of m2.

[0196] The order of step S301 - step S302 and step S303 - step S304 can be interchanged or performed simultaneously without affecting the actual effect of this embodiment.

[0197] The embodiment of the present invention obtains the intermediate main pipe coal slurry flow rate and the intermediate main pipe oxygen flow rate, and respectively calculates the target main pipe oxygen flow rate setting value and the target central pipe oxygen flow rate setting value according to the target main pipe oxygen-coal ratio setting value, the real-time coal slurry concentration, and the target central pipe oxygen-coal ratio setting value, thereby controlling the valve openings of the main pipe oxygen regulating valve and the central oxygen regulating valve, thereby ensuring that the gasifier operates under the safe, stable, and economically optimal working conditions, reducing the labor intensity of operators and improving safety.

[0198] In one embodiment, the real-time oxygen flow rate also includes the real-time central pipe oxygen flow rate, the oxygen valve opening includes the main pipe oxygen valve opening and the central pipe oxygen valve opening, and the oxygen valve opening of the gasifier is controlled according to the target oxygen flow rate setting value, including:

[0199] Calculate the deviation between the target main pipe oxygen flow setting value and the intermediate main pipe oxygen flow rate to obtain the main pipe deviation value;

[0200] Arrange the real-time central tube oxygen flow rates in ascending order, and obtain the middle central tube oxygen flow rate in the middle;

[0201] Calculate the deviation between the target central tube oxygen flow rate setting value and the intermediate central tube oxygen flow rate to obtain the central tube deviation value;

[0202] The main pipe deviation value and the central pipe deviation value are calculated using the proportional-integral-differential algorithm to obtain the main pipe oxygen valve opening value and the central pipe oxygen valve opening value respectively;

[0203] The main pipe oxygen valve opening and the central pipe oxygen valve opening are controlled respectively according to the main pipe oxygen valve opening value and the central pipe oxygen valve opening value.

[0204] Specifically, the controller uses the PID algorithm to calculate the main pipe oxygen valve opening value and the central pipe oxygen valve opening value. The specific calculation formula is as follows:

[0205]

[0206] P(t): opening value of main pipe oxygen valve or central pipe oxygen valve;

[0207] t: current time;

[0208] e(t): total pipe deviation value or center pipe deviation value;

[0209] k e : Preset proportionality factor, preferably

[0210] T i : Preset integral coefficient, preferably

[0211] T d : The preset differential coefficient, preferably

[0212] In the embodiment of the present invention, a PID algorithm is used to calculate the main pipe oxygen valve opening value and the central pipe oxygen valve opening value, and the main pipe oxygen valve opening value and the central pipe oxygen valve opening value are controlled according to the main pipe oxygen valve opening value and the central pipe oxygen valve opening value, thereby improving accuracy, further ensuring that the gasifier operates under safe, stable and economically optimal working conditions, reducing the labor intensity of operators and improving safety.

[0213] Embodiment 4

[0214] On the basis of Embodiment 1 to Embodiment 3, Figure 4 As shown, a gasifier control method provided by a fourth embodiment of the present invention includes:

[0215] Step S401: obtaining real-time gasifier status information of the gasifier;

[0216] Step S402: judging whether the gasifier has a fault according to the real-time gasifier state information and a preset fault warning model, wherein the fault warning model is used to store the corresponding fault characteristics when the gasifier has a fault;

[0217] Step S403: Send a fault warning signal.

[0218] Specifically, in order to further ensure the stability and safety of the gasifier, the controller monitors the real-time gasifier status information of the gasifier in real time. If the real-time gasifier status information is consistent with the fault characteristics in the fault warning model, it is judged that the gasifier has a fault and a fault warning signal is issued.

[0219] Preferably, the fault warning model is obtained by the following method:

[0220] The historical fault types of the gasifier and the fault characteristics during the corresponding fault occurrence period are obtained, the historical fault types and fault characteristics are matched one by one, and a fault early warning model is established.

[0221] Historical fault types include false triggering of interlock signal, furnace wall overtemperature, gasifier overpressure, slag blockage, abnormal coal slurry pump flow, abnormal oxygen flow, abnormal stirring of large coal slurry tank, abnormal large coal slurry pump, abnormal small coal slurry pump, burner cooling water leakage, burner blockage, liquid level meter failure and bubble breaker slag blockage; the fault characteristic refers to the operating data when the corresponding fault occurs in the gasifier.

[0222] The following examples are used to illustrate the workflow and beneficial effects that can be achieved by using the gasifier control method provided by the present invention:

[0223] Example 1

[0224] Take a coal gasification unit with three four-nozzle water-coal slurry gasifiers of the same shape and a syngas output of 100,000 Nm3 / h as an example. The existing operation mode is two in operation and one in standby. The nozzle of the gasifier is in the form of three channels, the inner channel is oxygen, the middle channel is water-coal slurry, and the outer channel is oxygen. Each nozzle uses an independent water-coal slurry and oxygen pipeline, where the oxygen pipeline is divided into two routes near the gasifier, and a small part (about 10% of the total oxygen of the nozzle) is used for the oxygen pipeline. ) enter the inner oxygen channel of the nozzle, and the rest enter the outer oxygen channel of the nozzle. The inner oxygen, water-coal slurry and outer oxygen are all equipped with flow monitoring instruments; the inner oxygen and outer oxygen are both equipped with flow regulating valves, and form a simple control loop with the flow detection instrument. However, due to concerns about the risk of control loop failure caused by upstream and downstream fluctuations, instrument failure and other reasons, the above-mentioned oxygen flow loop has been unused for a long time. The operator manually adjusts the opening of the oxygen valve to maintain the stability of the oxygen flow, and manually adjusts the oxygen flow to intervene when the gasifier operation shows obvious fluctuations (such as furnace temperature and outlet effective gas composition deviate from process indicators). Under stable load conditions, the temperature fluctuation amplitude of the gasifier of the device is The fluctuation range of effective gas CH4 content is The manual operation volume reaches 300 times / day.

[0225] The implementation steps of the gasifier control method provided by the present invention are as follows:

[0226] (1) Optimize the bottom control loop of the gasifier and design four sets of identical complex control loops, corresponding to the four nozzles of the gasifier. Take nozzle No. 1 as an example. Figure 5 As shown, the loop includes 3 identical coal slurry flow sensors, 3 identical main pipe oxygen flow sensors, 1 central oxygen flow sensor, 1 coal slurry concentration sensor, 1 oxygen concentration sensor, 1 main pipe oxygen regulating valve, 1 central oxygen regulating valve, 1 main pipe oxygen flow controller, 1 central oxygen flow controller, 1 central oxygen ratio controller and 1 oxygen-coal ratio controller.

[0227] The main pipe oxygen flow controller adopts PID form. The main pipe oxygen flow set value is calculated by the oxygen-coal ratio controller. The PID controller adjusts the main pipe oxygen regulating valve opening according to the deviation between the set value and the middle value of the measured values ​​of the three main pipe oxygen flow sensors.

[0228] The central oxygen flow controller adopts PID form. The central oxygen flow set value is calculated by the central oxygen proportional controller. The PID controller adjusts the opening of the central oxygen regulating valve according to the deviation between the set value and the measured value of the central oxygen flow sensor.

[0229] The oxygen-coal ratio controller adopts proportional control. The branch balance module calculates the nozzle oxygen-coal ratio loop set value. The oxygen-coal ratio controller adjusts the oxygen flow controller set value according to the oxygen-coal ratio controller set value and the actual value of the coal slurry flow.

[0230] The adjustment formula of the main pipe oxygen-coal ratio controller is:

[0231] FT1=[RT1×MID(FM11, FM12, FM13)×AM]÷AO;

[0232] FT2=[RT2×MID(FM21, FM22, FM23)×AM]÷AO;

[0233] FT3=[RT3×MID(FM31,FM32,FM33)×AM]÷AO;

[0234] FT4=[RT4×MID(FM41, FM42, FM43)×AM]÷AO;

[0235] Nozzle 1 Nozzle 4 main pipe oxygen flow setting value;

[0236] Nozzle 1 Nozzle 4 oxygen-coal ratio setting value;

[0237] AM: actual value of coal slurry concentration sensor;

[0238] AO: actual value of oxygen concentration sensor;

[0239] Actual value of coal slurry flow sensor of three main pipes of nozzle 1 pipeline;

[0240] Actual value of coal slurry flow sensor of 3 main pipes of nozzle 2 pipeline;

[0241] Actual value of coal slurry flow sensor of 3 main pipes of nozzle 3 pipeline;

[0242] Actual value of coal slurry flow sensor of 3 main pipes of nozzle 4 pipeline;

[0243] The central oxygen controller adopts proportional control. The operator manually sets the set value of the nozzle central oxygen proportional loop. The central oxygen proportional controller adjusts the set value of the central oxygen flow controller according to the set value of the central oxygen proportional controller and the actual value of the main pipe oxygen flow.

[0244] The adjustment formula of the central oxygen ratio controller is:

[0245] FC1=RC1×MID(FO11,FO12,FO13);

[0246] FC2=RC2×MID(FO21,FO22,FO23);

[0247] FC3=RC3×MID(FO31,FO32,FO33);

[0248] FC4=RC4×MID(FO41,FO42,FO43);

[0249] Nozzle 1-Nozzle 4 center oxygen flow setting value;

[0250] Nozzle 1-Nozzle 4 center oxygen ratio setting value;

[0251] Actual value of oxygen flow sensor of 3 main pipes of nozzle 1 pipeline;

[0252] Actual value of oxygen flow sensor of nozzle 2 pipeline 3 main pipes;

[0253] Actual value of oxygen flow sensor of 3 main pipes of nozzle 3 pipeline;

[0254] Actual value of oxygen flow sensor of 3 main pipes of nozzle 4 pipeline;

[0255] (2) After completing the optimization of the underlying loop, an advanced control module is constructed, including the main control matrix group, the model adaptive switching program, the branch balance constraint program, the moving average calculation program, and the instrument effectiveness monitoring program.

[0256] The main control matrix group includes three control matrices. The controlled variables of each control matrix are the gasifier temperature (CV1) and the effective gas CH4 content (CV2), and the operating variables are the oxygen-coal ratio loop set values ​​of nozzle 1, nozzle 2, nozzle 3, and nozzle 4 (MV1, MV2, MV3, and MV4).

[0257] The dynamic control matrix between the variables is determined by step test as follows:

[0258]

[0259]

[0260]

[0261] The three control matrices are adaptively switched according to the following conditions:

[0262] 1) Select control matrix (I) for control;

[0263] 2) Select control matrix (II) for control;

[0264] 3) Select control matrix (III) for control;

[0265] At the same time, four protection programs are set up, namely the branch balance constraint program, the moving average calculation program, the furnace temperature effectiveness monitoring program and the effective gas CH4 content effectiveness monitoring program.

[0266] The branch balance constraint program formula is as follows:

[0267]

[0268] The moving average procedure formula is as follows:

[0269]

[0270]

[0271] CV1 i : The measured value of gasifier temperature before the i-th minute;

[0272] CV2 i : The measured value of effective gas CH4 content before the i-th minute;

[0273] The furnace temperature effectiveness monitoring conditions are as follows:

[0274]

[0275] 1150℃≤CV1≤1350℃

[0276] The monitoring conditions for the effectiveness of effective gas CH4 content are as follows:

[0277]

[0278] 200ppm≤CV2≤1200ppm

[0279] (3) After completing the advanced control optimization, the historical operating data of the gasifier in the past three years was extracted, and the safety optimization model of the gasifier was obtained through the random forest algorithm. The model includes an input layer and an output layer. The split feature of the model construction process is 4, and the random forest size is 150. The input layer includes nozzle 1 Nozzle 4 oxygen-coal ratio, Nozzle 1 Nozzle 4 center oxygen flow, coal slurry concentration, gasifier temperature, gasifier pressure, nozzle 1 There are 23 variables in total, including nozzle 4 pressure difference, gasifier outlet temperature, gasifier liquid level, furnace temperature, ambient temperature, and raw coal calorific value; the output layer includes two variables, namely, the optimal operating temperature of the gasifier and the safety optimization index. The calculation formula of the safety optimization index is as follows:

[0280] G=0.4×Y+6×V1+8.4×V2

[0281] G: comprehensive optimal operating index of gasifier;

[0282] Y: effective gas production rate of gasifier (effective gas is the sum of H2 and CO in the synthesis gas at the outlet of gasifier), (Nm3 / h) / (100kg standard coal);

[0283] V1: steady-state judgment index of key parameters of gasifier in the next 1 hour;

[0284] V2: probability of gasifier failure within the next 3 hours;

[0285] A rolling optimization program is set up based on the safety optimization model to safely and stably assign the calculation results of the safety optimization model to the advanced controller of the gasifier. The rolling optimization process is as follows: Figure 6 shown.

[0286] (4) To ensure that the gasifier operates under safe and stable conditions, a gasifier steady-state detection module and a gasifier fault online diagnosis module were designed based on the historical operation of the gasifier in the past three years.

[0287] The gasifier steady-state detection module detects the nozzle 1 in the gasifier system. Nozzle 4 coal slurry flow, nozzle 1 Nozzle 4 oxygen flow, Nozzle 1 The moving average, moving variance and trend judgment of 23 key process parameters within 10 minutes, including nozzle 4 pressure difference, gasifier pressure, slag outlet pressure difference, gasifier outlet process gas temperature, water scrubber outlet process gas temperature, cyclone separator outlet process gas temperature, water scrubber inlet pressure, cyclone separator inlet pressure, effective gas CH4 content, effective gas CO content, effective gas CO2 content, effective gas H2 content and gasifier liquid level, are calculated and judged. The trend judgment formula is as follows:

[0288]

[0289] C i : parameter measurement value before the i-th minute;

[0290] Average measurement value of the parameter within n minutes;

[0291] Q: parameter trend judgment indicator;

[0292] The judgment criteria for each judgment-related parameter are shown in the following table:

[0293]

[0294] After the gasifier was optimized through intelligent control, the effective gas production rate increased by 1 (Nm3 / h) / (100kg standard coal), the frequency of abnormal shutdowns dropped from 3 times / year to 0, and the operation volume dropped from 300 times / day to 15 times / day.

[0295] Example 2

[0296] A coal gasification unit has two single-nozzle water-coal slurry gasifiers of the same shape with a syngas output of 80,000 Nm3 / h. The operation mode is one on and one on standby. The nozzle of the gasifier is a three-channel form, with the inner channel for oxygen, the middle channel for water-coal slurry, and the outer channel for oxygen. The oxygen pipeline is divided into two routes near the gasifier, and a small part (about 10% of the total oxygen in the nozzle) is used to generate oxygen. ) enter the inner oxygen channel of the nozzle, and the rest enter the outer oxygen channel of the nozzle. The inner oxygen, water-coal slurry and outer oxygen are all equipped with flow monitoring instruments; the inner oxygen and outer oxygen are both equipped with flow regulating valves. The gasifier lacks an automatic control circuit. The operator manually adjusts the opening of the oxygen valve to maintain a stable oxygen flow rate, and manually adjusts the oxygen flow rate to intervene when there are obvious fluctuations in the operation of the gasifier (such as the furnace temperature and the outlet effective gas composition deviate from the process indicators). Under stable load conditions, the temperature fluctuation range of the gasifier of this device is The fluctuation range of effective gas CH4 content is The manual operation volume reaches 150 times / day.

[0297] The implementation steps of this plan in the chemical plant are as follows:

[0298] (1) Optimize the bottom control loop of the gasifier and design a complex control loop, such as Figure 5 As shown, the circuit includes 3 identical coal slurry flow sensors, 3 identical main pipe oxygen flow sensors, 1 central oxygen flow sensor, 1 coal slurry concentration sensor, 1 oxygen concentration sensor, 1 main pipe oxygen regulating valve, 1 central oxygen regulating valve, 1 main pipe oxygen flow controller, 1 central oxygen flow controller, 1 central oxygen ratio controller and 1 oxygen-coal ratio controller.

[0299] The main pipe oxygen flow controller adopts PID form. The main pipe oxygen flow set value is calculated by the oxygen-coal ratio controller. The PID controller adjusts the main pipe oxygen regulating valve opening according to the deviation between the set value and the middle value of the measured values ​​of the three main pipe oxygen flow sensors.

[0300] The central oxygen flow controller adopts PID form. The central oxygen flow set value is calculated by the central oxygen proportional controller. The PID controller adjusts the opening of the central oxygen regulating valve according to the deviation between the set value and the measured value of the central oxygen flow sensor.

[0301] The oxygen-coal ratio controller adopts proportional control. The branch balance module calculates the nozzle oxygen-coal ratio loop set value. The oxygen-coal ratio controller adjusts the oxygen flow controller set value according to the oxygen-coal ratio controller set value and the actual value of the coal slurry flow.

[0302] The adjustment formula of the main pipe oxygen-coal ratio controller is:

[0303] FT=[RT×MID(FM1,FM2,FM3)×AM]÷AO

[0304] FT: Main pipe oxygen flow setting value;

[0305] RT: oxygen-coal ratio setting value;

[0306] AM: actual value of coal slurry concentration sensor;

[0307] AO: actual value of oxygen concentration sensor;

[0308] Actual values ​​of 3 main pipe coal slurry flow sensors;

[0309] The central oxygen controller adopts proportional control. The operator manually sets the set value of the nozzle central oxygen proportional loop. The central oxygen proportional controller adjusts the set value of the central oxygen flow controller according to the set value of the central oxygen proportional controller and the actual value of the main pipe oxygen flow.

[0310] The adjustment formula of the central oxygen ratio controller is:

[0311] FC=RC×MID(FO1,FO2,FO3);

[0312] FC: central oxygen flow setting value;

[0313] RC: central oxygen ratio setting value;

[0314] Actual value of oxygen flow sensor of 3 main pipes of nozzle 1 pipeline;

[0315] (2) After completing the optimization of the underlying loop, an advanced control module is constructed, including the main control matrix group, the model adaptive switching program, the branch balance constraint program, the moving average calculation program, and the instrument effectiveness monitoring program.

[0316] The main control matrix group includes 4 control matrices. The controlled variables of each control matrix are the gasifier temperature (CV1) and the effective gas CH4 content (CV2), and the operating variable is the oxygen-coal ratio loop set value (MV1).

[0317] The dynamic control matrix between the variables is determined by step test as follows:

[0318]

[0319]

[0320]

[0321]

[0322] The three control matrices are adaptively switched according to the following conditions:

[0323] ① Gasifier pressure ≥ 6.5MPa, select control matrix (IV) for control;

[0324] ②6.32MPa≤gasifier pressure<6.5MPa, select control matrix (V) for control;

[0325] ③6.1MPa≤gasifier pressure<6.32MPa, select control matrix (VI) for control;

[0326] ④ When the gasifier pressure is less than 6.1 MPa, select control matrix (VII) for control;

[0327] In addition to the main control matrix, three protection programs are set up, namely the moving average calculation program, the furnace temperature effectiveness monitoring program and the effective gas CH4 content effectiveness monitoring program.

[0328] The moving average program formula is as follows:

[0329]

[0330]

[0331] CV1 i : The measured value of gasifier temperature before the i-th minute;

[0332] CV2 i : The measured value of effective gas CH4 content before the i-th minute;

[0333] The furnace temperature effectiveness monitoring program formula is as follows:

[0334]

[0335] 1050℃≤CV1≤1300℃

[0336] The formula for monitoring the effectiveness of effective gas CH4 content is as follows:

[0337]

[0338] 800ppm≤CV2≤3000ppm

[0339] (3) After completing the advanced control optimization, the historical operating data of the gasifier in the past three years was extracted, and the safety optimization model of the gasifier was obtained through the random forest algorithm. The model includes an input layer and an output layer. The split feature of the model construction process is 3, and the random forest size is 120. The input layer includes 11 variables, including oxygen-coal ratio, central oxygen flow, coal slurry concentration, gasifier temperature, gasifier pressure, nozzle pressure difference, gasifier outlet temperature, gasifier liquid level, furnace temperature, ambient temperature, and raw coal calorific value; the output layer includes two variables, namely, the optimal operating temperature of the gasifier and the safety optimization index. The calculation formula of the safety optimization index is as follows:

[0340] G=0.34×Y+7.2×V1+8×V2

[0341] G: comprehensive optimal operating index of gasifier;

[0342] Y: effective gas production rate of gasifier (effective gas is the sum of H2 and CO in the synthesis gas at the outlet of gasifier), (Nm3 / h) / (100kg standard coal);

[0343] V1: steady-state judgment index of key parameters of gasifier in the next 1 hour;

[0344] V2: probability of gasifier failure within the next 3 hours;

[0345] A rolling optimization program is set up based on the safety optimization model to safely and stably assign the calculation results of the safety optimization model to the advanced controller of the gasifier. The rolling optimization process is as follows: Figure 6 shown.

[0346] (4) To ensure that the gasifier operates under safe and stable conditions, a gasifier steady-state detection module and a gasifier fault online diagnosis module were designed based on the historical operation of the gasifier in the past three years.

[0347] The gasifier steady-state detection module calculates and judges the moving mean, moving variance and trend judgment of 15 key process parameters in the gasifier system, including coal slurry flow, oxygen flow, nozzle pressure difference, gasifier pressure, slag mouth pressure difference, gasifier outlet process gas temperature, water scrubber outlet process gas temperature, cyclone separator outlet process gas temperature, water scrubber inlet pressure, cyclone separator inlet pressure, effective gas CH4 content, effective gas CO content, effective gas CO2 content, effective gas H2 content, and gasifier liquid level within 10 minutes. The trend judgment formula is as follows:

[0348]

[0349] C i : parameter measurement value before the i-th minute;

[0350] Average measurement value of the parameter within n minutes;

[0351] Q: parameter trend judgment indicator;

[0352] The judgment criteria for each judgment-related parameter are shown in the following table:

[0353]

[0354] After the gasifier was optimized through intelligent control, the effective gas production rate increased by 0.8 (Nm3 / h) / (100kg standard coal), the frequency of abnormal shutdowns was reduced from 6 times / year to 1 time / year, and the operation volume was reduced from 150 times / day to 10 times / day.

[0355] Embodiment 5

[0356] Embodiment 5 of the present invention provides a storage medium, wherein the storage medium is used to store computer instructions. When a computer executes the computer instructions, the storage medium is used to execute all steps of the gasifier control method in any of the method embodiments described above.

[0357] Embodiment 6

[0358] like Figure 7 As shown, a hardware structure diagram of an electronic device for gasifier control provided by Embodiment 6 of the present invention includes:

[0359] at least one processor 701; and,

[0360] A memory 702 is communicatively connected to at least one processor 701; wherein,

[0361] The memory 702 stores instructions that can be executed by at least one processor 701 . The instructions are executed by the at least one processor 701 so that the at least one processor 701 can execute the gasifier control method as described above.

[0362] Figure 7 A processor 701 is taken as an example.

[0363] The electronic device is preferably an Electronic Control Unit (ECU).

[0364] The electronic device may further include: an input device 703 and an output device 704 .

[0365] The processor 701, the memory 702, the input device 703 and the output device 704 may be connected via a bus or other means, and the figure takes the connection via a bus as an example.

[0366] The memory 702 is a non-volatile computer-readable storage medium that can be used to obtain non-volatile software programs, non-volatile computer executable programs and modules, such as program instructions / modules corresponding to the gasifier control method in the embodiment of the present application, for example, Figure 1-Figure 4 The processor 701 executes various functional applications and data processing by running the non-volatile software programs, instructions and modules acquired in the memory 702, that is, the gasifier control method in the above embodiment is implemented.

[0367] The memory 702 may include an acquisition program area and an acquisition data area, wherein the acquisition program area may acquire an operating system and an application required by at least one function; the acquisition data area may acquire data created according to the use of the gasifier control method, etc. In addition, the memory 702 may include a high-speed random access memory, and may also include a non-volatile memory, such as at least one disk storage device, a flash memory device, or other non-volatile solid-state storage device. In some embodiments, the memory 702 may optionally include a memory remotely arranged relative to the processor 701, and these remote memories may be connected to the device for executing the gasifier control method via a network. Examples of the above-mentioned network include, but are not limited to, the Internet, an intranet, a local area network, a mobile communication network, and combinations thereof.

[0368] The input device 703 can receive user clicks and generate signal inputs related to user settings and function controls of the gasifier control method. The output device 704 can include display devices such as a display screen.

[0369] The one or more modules are acquired in the memory 702, and when executed by the one or more processors 701, the gasifier control method in any of the above method embodiments is executed.

[0370] The above-mentioned product can execute the method provided in the embodiment of the present application, and has the functional modules and beneficial effects corresponding to the execution method. For technical details not fully described in this embodiment, please refer to the method provided in the embodiment of the present application.

[0371] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the embodiments of the present invention, rather than to limit them. Although the embodiments of the present invention have been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or make equivalent replacements for some of the technical features therein. However, these modifications or replacements do not deviate the essence of the corresponding technical solutions from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. A gasifier control method, characterized in that: include: Acquire real-time gasifier status information of the gasifier, wherein the real-time gasifier status information includes real-time coal slurry flow, real-time coal slurry concentration, real-time oxygen flow, real-time oxygen concentration, real-time oxygen-coal ratio, real-time gasifier temperature and real-time effective methane content at the gasifier outlet; Obtaining a target gasifier temperature of the gasifier according to the real-time gasifier state information and a preset furnace temperature optimization model; Calculating a target oxygen-coal ratio setting value of at least one nozzle of the gasifier according to the target gasifier temperature; Calculating a target oxygen flow rate setting value according to the target oxygen-coal ratio setting value and the real-time gasifier state information; The oxygen valve opening of the gasifier is controlled according to the target oxygen flow setting value.

2. The gasifier control method according to claim 1, characterized in that: The furnace temperature optimization model is obtained by the following method: Acquire historical gasifier state information of the gasifier, wherein the historical gasifier state information includes a first historical gasifier temperature, a first historical effective gas methane content, a historical oxygen-coal ratio, a historical gasifier load, and a historical gasifier pressure; The historical gasification furnace state information is trained using a random forest algorithm to obtain the furnace temperature optimization model.

3. The gasifier control method according to claim 2, characterized in that: The step of obtaining a target gasifier temperature of the gasifier according to the real-time gasifier state information and a preset furnace temperature optimization model includes: Decomposing the real-time oxygen-coal ratio into a plurality of sub-real-time oxygen-coal ratios according to a preset range; Inputting the plurality of sub-real-time oxygen-coal ratios and the real-time gasifier state information into the furnace temperature optimization model to obtain a plurality of furnace temperature optimization indicators and sub-target gasifier temperatures, wherein the furnace temperature optimization indicator refers to a comprehensive operating indicator of the operating stability and effective gas yield of the gasifier; The sub-target gasifier temperature corresponding to the maximum furnace temperature optimization index among the furnace temperature optimization indexes is used as the target gasifier temperature.

4. The gasifier control method according to claim 3, characterized in that: The method further comprises: taking the real-time gasifier temperature corresponding to the maximum furnace temperature optimization index as the target gasifier temperature; Using a first-order exponential decay algorithm to decompose the target gasifier temperature into a plurality of sub-target gasifier temperatures according to a preset number of decomposition steps; sequentially adjusting the temperature of the gasifier according to the plurality of sub-target gasifier temperatures; If the furnace temperature setting value is the same as the target gasification furnace temperature, the temperature adjustment of the gasification furnace is stopped.

5. The gasifier control method according to any one of claims 1 to 4, characterized in that: The step of obtaining the target gasifier temperature of the gasifier according to the real-time gasifier state information and a preset furnace temperature optimization model further includes: If the real-time gasifier status information does not meet the following conditions, stop the optimization; Where n is time; C i is the historical gasifier status information before the i-th moment; C i+1 is the gasifier status information at the i+1th moment; is the average value of the real-time gasifier status information within the time; Q is a preset constant.

6. The gasifier control method according to claim 1, characterized in that: The step of calculating a target oxygen-coal ratio setting value of a nozzle of the gasifier according to the target gasifier temperature comprises: Acquire historical gasifier state information of the gasifier under various operating conditions, wherein the historical gasifier state information includes a first historical gasifier temperature, a historical effective methane content, and a historical oxygen-coal ratio setting value; Performing model identification according to the historical gasifier state information to obtain transfer functions in different time periods, wherein the transfer functions include a gain coefficient, a lag time, and a time constant; The transfer function is classified according to the gain coefficient, the lag time and the time constant to obtain a gasifier operation control matrix corresponding to the historical gasifier state information, wherein the gasifier operation control matrix is ​​a correspondence matrix between the first historical gasifier temperature and / or the historical effective methane content and the transfer function and the oxygen-coal ratio set value; If the real-time gasifier temperature and / or the real-time effective methane content are consistent with the first historical gasifier temperature and / or the historical effective methane content in the gasifier operation control matrix, the oxygen-coal ratio set value corresponding to the first historical gasifier temperature and / or the historical effective methane content is used as the target oxygen-coal ratio set value.

7. The gasifier control method according to claim 6, characterized in that: The number of the nozzles is multiple, and the target oxygen-coal ratio setting value is obtained according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix, and then the following further includes: If the target oxygen-coal ratio setting value meets the following conditions, the target oxygen flow rate setting value is calculated according to the target oxygen-coal ratio setting value and the real-time gasifier state information: Where n is the number of nozzles; MV x is the target oxygen-coal ratio setting value of any nozzle; MV x+1 For MV x The target oxygen-coal ratio setting value of the next adjacent nozzle; MV n is the target oxygen-coal ratio setting value of the nth nozzle; D is a preset constant.

8. The gasifier control method according to claim 6, characterized in that: The step of obtaining the target oxygen-coal ratio setting value according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix includes: Within a preset time period, calculating the furnace temperature average value of the real-time gasification furnace temperature and / or the methane content average value of the real-time effective methane content according to a preset calculation cycle; The target oxygen-coal ratio setting value is obtained according to the average furnace temperature and / or the average methane content and the gasifier operation control matrix.

9. The gasifier control method according to claim 6, characterized in that: The step of obtaining the target oxygen-coal ratio setting value according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix includes: Acquire a second historical gasifier temperature adjacent to the real-time gasifier temperature; If the difference between the real-time gasifier temperature and the second historical gasifier temperature is greater than or equal to the preset minimum gasifier temperature threshold, the difference between the real-time gasifier temperature and the second historical gasifier temperature is less than or equal to the preset maximum gasifier temperature threshold, the real-time gasifier temperature is greater than or equal to the preset minimum gasifier confidence threshold, and the real-time gasifier temperature is less than or equal to the preset maximum gasifier confidence threshold, the target oxygen-coal ratio setting value is obtained according to the real-time gasifier temperature and the gasifier operation control matrix.

10. The gasifier control method according to claim 6, characterized in that: The step of obtaining the target oxygen-coal ratio setting value according to the real-time gasifier temperature and / or the real-time effective methane content and the gasifier operation control matrix includes: Acquire a second historical effective gas methane content adjacent to the real-time effective gas content; If the difference between the real-time effective gas methane content and the second historical effective gas methane content is greater than or equal to the preset minimum effective gas content threshold, the difference between the real-time effective gas methane content and the second historical effective gas methane content is less than or equal to the preset maximum effective gas content threshold, the real-time effective methane content is greater than or equal to the preset minimum confidence value of the effective gas content, and the real-time effective methane content is less than or equal to the preset maximum confidence value of the effective gas content, the target oxygen-coal ratio setting value is obtained according to the real-time effective methane content and the gasifier operation control matrix.

11. The gasifier control method according to claim 1, characterized in that: The number of the nozzles is multiple, the real-time oxygen flow rate includes the real-time main pipe oxygen flow rate, the real-time coal slurry flow rate includes the real-time main pipe coal slurry flow rate, the target oxygen-coal ratio setting value includes the target main pipe oxygen-coal ratio setting value and the target central pipe oxygen-coal ratio setting value, the target oxygen flow rate setting value includes the target main pipe oxygen flow rate setting value and the target central pipe oxygen flow rate setting value, and the target oxygen flow rate setting value is calculated according to the target oxygen-coal ratio setting value and the real-time gasifier state information, including: Arrange the real-time main pipe coal slurry flow rates in ascending order to obtain the middle main pipe coal slurry flow rate; Calculate the target main pipe oxygen-coal ratio setting value, the product of the intermediate main pipe coal slurry flow rate and the real-time coal slurry concentration, and divide the result by the real-time oxygen concentration to obtain the target main pipe oxygen flow rate setting value; Arrange the real-time main pipe oxygen flow rates in ascending order to obtain the middle main pipe oxygen flow rate in the middle; The product of the target central tube oxygen-coal ratio setting value and the intermediate main tube oxygen flow rate is calculated to obtain the target central tube oxygen flow rate setting value.

12. The gasifier control method according to claim 11, characterized in that: The real-time oxygen flow rate also includes the real-time central pipe oxygen flow rate, the oxygen valve opening includes the main pipe oxygen valve opening and the central pipe oxygen valve opening, and the oxygen valve opening of the gasifier is controlled according to the target oxygen flow rate setting value, including: Calculating the deviation between the target main pipe oxygen flow setting value and the intermediate main pipe oxygen flow to obtain a main pipe deviation value; Arrange the real-time central tube oxygen flow rates in ascending order to obtain the middle central tube oxygen flow rate; Calculating the deviation between the target central tube oxygen flow rate setting value and the intermediate central tube oxygen flow rate to obtain a central tube deviation value; The main pipe deviation value and the central pipe deviation value are calculated using a proportional-integral-differential algorithm to obtain the main pipe oxygen valve opening value and the central pipe oxygen valve opening value respectively; The main pipe oxygen valve opening and the central pipe oxygen valve opening are controlled respectively according to the main pipe oxygen valve opening value and the central pipe oxygen valve opening value.

13. The gasifier control method according to claim 1, characterized in that: The step of controlling the oxygen valve opening of the gasifier according to the target oxygen flow setting value further comprises: According to the real-time gasifier status information and a preset fault warning model, it is determined whether the gasifier fails. The fault warning model is used to store corresponding fault features when the gasifier fails.

14. A storage medium, characterized in that: The storage medium stores computer instructions, and when a computer executes the computer instructions, it is used to execute all steps of the gasifier control method according to any one of claims 1 to 13.

15. An electronic device, characterized in that: include: at least one processor; as well as, a memory communicatively connected to the at least one processor; wherein, The memory stores instructions that can be executed by the at least one processor, and the instructions are executed by the at least one processor so that the at least one processor can execute the gasifier control method according to any one of claims 1 to 13.

Images