A method and control system for controlling the amount of air introduced into dry quenching coke.

Abstract

This invention discloses a method for controlling the air intake of dry quenching coke, relating to the field of dry quenching technology. The method involves inputting both reference data and actual measurement data into a control system, which then calculates the air intake. This invention utilizes a feedforward method to adjust the air intake. By monitoring factors affecting the air intake of the dry quenching coke system, the required air intake is determined. When disturbances change, the method promptly reflects these changes and adjusts accordingly, avoiding the lag inherent in feedback methods. Furthermore, by employing automated program control of the dry quenching furnace's air intake, manual operation is significantly reduced compared to manual control, improving control accuracy and system automation.

Description

Technical Field

[0001] This invention relates to the field of dry quenching technology, and in particular to a method and control system for controlling the amount of air introduced into the dry quenching coke. Background Technology

[0002] Dry quenching is a quenching method that uses inert gas to cool red-hot coke. It utilizes a low-temperature circulating gas to exchange heat with the red-hot coke in the dry quenching furnace, thereby cooling the red-hot coke. After absorbing the heat from the red-hot coke, the circulating gas enters the dry quenching boiler and transfers the heat to the boiler to generate steam. The circulating gas cooled down by the dry quenching boiler is then blown back into the dry quenching furnace by a circulating fan to continue exchanging heat with the red-hot coke.

[0003] Under normal operating conditions, the circulating gas in dry quenching coke production consists of N2, O2, CO, H2, CO2, H2O, and trace amounts of sulfides and chlorides. H2 and CO are the main combustible gases, generated in four ways: first, residual volatilization from the red-hot coke in the pre-storage chamber of the dry quenching furnace releases gases primarily composed of H2 and CO; second, as the circulating gas passes through the red-hot coke layer, CO2 in the gas reacts with the coke to form CO; third, as the circulating gas passes through the red-hot coke layer, H2O in the gas reacts with the coke to form H2; and fourth, a certain amount of air is drawn into the negative pressure section of the gas circulation system, where O2 reacts with the coke as it passes through the red-hot coke layer of the dry quenching furnace, producing CO and CO2. To ensure the safe operation of the dry quenching coke system, it is essential to control the content of combustible gases in the circulating gas to prevent potential explosions or other hazards.

[0004] There are currently two methods to control the content of combustible gases in the circulating gas. The first method is to introduce air into the circulating gas for combustion and nitrogen dilution. Introducing nitrogen into the dry quenching furnace to dilute the combustible gases in the circulating gas requires a large amount of nitrogen, which increases production costs. The second method is to introduce air into the dry quenching furnace to burn off the combustible gases in the circulating gas. This method is more economical and is currently widely used.

[0005] The main process of introducing air into the dry quenching furnace to burn off the combustible gases in the circulating gas is as follows: A gas composition analyzer is installed on the circulating gas pipeline at the inlet of the dry quenching furnace. Air is introduced into the annular duct of the dry quenching furnace. The air introduction is a system consisting of an air introduction pipeline, a gas distribution device, a regulating valve, and a compensator. One side of the air introduction pipeline is open to the atmosphere, and the other side is connected to the annular duct of the dry quenching furnace. The power for introduction is the negative pressure of the annular duct of the dry quenching furnace to introduce air into the dry quenching furnace. The regulating valve is used to control the amount of air introduced. By introducing air, the combustible gas composition in the dry quenching coke circulating gas is controlled within the safe production range. The typical control indicators are O2 < 1%, H2 < 3%, and CO < 6%.

[0006] However, the commonly used air-introduction combustion method mainly involves the dry quenching coke control operator manually adjusting the amount of air introduced based on the combustible gas composition displayed by the gas analyzer on the inlet pipe of the dry quenching furnace. This operation mode requires the dry quenching coke control operator to observe the changes in the system's combustible components in real time and adjust the amount of air introduced accordingly. Moreover, there is a possibility that the adjustment may not be accurate and repeated adjustments may be necessary. This operation is a feedback method, and the disadvantages of the feedback method are that the adjustment response is lagging, requires real-time adjustment, and is subject to system fluctuations. It not only wastes the operator's energy but also has poor control accuracy.

[0007] Therefore, there is an urgent need for a method to control the amount of dry quenching air that can achieve automated feedforward adjustment, fast response speed, high control accuracy, and save manpower. Summary of the Invention

[0008] The purpose of this invention is to provide a method and control system for controlling the amount of air introduced into dry quenching coke, so as to solve the problems existing in the prior art. After the system acquires data from the data acquisition system, it performs calculations and controls the regulating valve in real time to realize the real-time adjustment of the amount of air introduced, realizes automated feedforward regulation, and also has the advantages of fast response speed, high adjustment accuracy and saving manpower.

[0009] To achieve the above objectives, the present invention provides the following solution: The present invention provides a method for controlling the amount of dry quenching air introduced, comprising the following steps:

[0010] S1: Before using the dry quenching system, set the dry quenching baseline values, including baseline throughput, baseline residual volatile matter in coke, baseline coke discharge temperature, baseline carbon dioxide content in circulating gas, baseline water content in circulating gas, baseline minimum air conductance of the dry quenching furnace, baseline air conductance coefficient of volatile matter in coke, and low material level value of the dry quenching furnace.

[0011] S2: During the use of the dry quenching system, the actual processing capacity, actual coke discharge temperature, actual residual volatile matter in coke, actual carbon dioxide content in the circulating gas, actual water content in the circulating gas, and actual material level are obtained in real time.

[0012] S3: The control system acquires the data from steps S1 and S2 and calculates the air conduction of the dry quenching furnace, and automatically adjusts the regulating valve on the air inlet pipeline to control the amount of air introduced.

[0013] Preferably, the calculation formula used in step S3 is:

[0014] Q 空 =i G i V残 [i T i CO2 iH2O Q min +α(L-L0)]

[0015] In the above formula: Qair represents the air conductivity of the dry quenching furnace; iair G i is the dry quenching capacity coefficient; V The residual value is the correction factor for volatile matter in coke; i T i is the temperature field correction coefficient; CO2 and i H2O Q represents the carbon dioxide and water treatment capacity coefficient of dry quenching; min α is the minimum air conductivity of the dry quenching furnace at the reference coke discharge temperature; L is the air conductivity coefficient of the reference coke volatile matter; L is the real-time material level of the dry quenching furnace; L0 is the low material level value of the dry quenching furnace.

[0016] In the preferred relation,

[0017]

[0018] Where G is the actual dry quenching throughput and G0 is the baseline dry quenching throughput.

[0019] In the preferred relation,

[0020]

[0021] Where V 残 V represents residual volatile matter from coke. 残0 The residual volatile matter in the coke is the baseline.

[0022] In the preferred relation,

[0023]

[0024] Where T is the actual coke discharge temperature and T0 is the reference coke discharge temperature.

[0025] In the preferred relation,

[0026]

[0027] Where V CO2 V represents the actual carbon dioxide content in the dry quenching cycle gas. 0CO2 The carbon dioxide content is the baseline for the dry quenching cycle gas.

[0028] In the preferred relation,

[0029]

[0030] Where V H2O V represents the actual carbon dioxide content in the dry quenching cycle gas. 0H2O The carbon dioxide content is the baseline for the dry quenching cycle gas.

[0031] This invention also provides a control system applying the above-mentioned dry quenching coke air introduction control method, comprising a gas analyzer for acquiring the actual carbon dioxide content and actual water content of the circulating gas, an electronic belt scale for acquiring the actual throughput, a radiation thermometer for acquiring the actual coke discharge temperature, a level gauge for acquiring the actual material level, and a control system. The gas analyzer is installed on the inlet pipe of the dry quenching furnace, the electronic belt scale is installed on the bottom outlet belt conveyor of the dry quenching furnace, the radiation thermometer is installed above the bottom outlet belt conveyor of the dry quenching furnace, and the level gauge is installed inside the dry quenching furnace. The gas analyzer, the electronic belt scale, the radiation thermometer, the level gauge, and the regulating valve on the air introduction pipe are all electrically connected to the control system.

[0032] The present invention achieves the following technical effects compared to the prior art:

[0033] By using the feedforward method to adjust the air intake, the required air intake for the dry quenching system is determined based on monitoring the factors affecting the air intake. When the disturbance changes, the change in air intake is reflected in a timely manner, and adjustments are made accordingly. This avoids the lag of the feedback method. In addition, by using a program to automatically control the air intake of the dry quenching furnace, manual operation is reduced compared to manual control, the control accuracy is improved, and the system automation level is increased. Attached Figure Description

[0034] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0035] Figure 1 This is a logic block diagram of the dry quenching air introduction amount control method of the present invention; Detailed Implementation

[0036] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0037] The purpose of this invention is to provide a method and control system for controlling the amount of air introduced into dry quenching coke, in order to solve the problems existing in the prior art. After the system acquires data from the data acquisition system, it performs calculations and controls the regulating valve in real time to realize the real-time adjustment of the amount of air introduced, achieving automated feedforward regulation. It also has the advantages of fast response speed, high adjustment accuracy, and saving manpower.

[0038] To make the above-mentioned objects, features and advantages of the present invention more apparent and understandable, the present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.

[0039] Please refer to the following: Figure 1 As shown, a method for controlling the amount of air introduced into the dry quenching coke is provided, including the following steps:

[0040] S1: Before using the dry quenching system, preliminary benchmark values ​​for dry quenching are set according to relevant technical indicators such as the "National Second-Class Metallurgical Coke Standard". These include benchmark throughput, benchmark residual volatile matter in coke, benchmark coke discharge temperature, benchmark carbon dioxide content in circulating gas, benchmark water content in circulating gas, minimum space conductivity of the benchmark dry quenching furnace, space conductivity coefficient of benchmark volatile matter in coke, and low material level value of the dry quenching furnace. Each indicator is then input into the control system.

[0041] S2: During the use of the dry quenching system, the actual processing volume, actual coke discharge temperature, actual residual volatile matter in coke, actual carbon dioxide content in circulating gas, actual water content in circulating gas, and actual material level are obtained in real time using data detection equipment, and all data information is input into the control system.

[0042] S3: The control system acquires the data from steps S1 and S2 and calculates the air conduction of the dry quenching furnace. Based on the calculated air conduction of the dry quenching furnace, it automatically adjusts the opening degree of the regulating valve on the air inlet pipe to control the amount of air introduced.

[0043] The calculation formula used in step S3 is:

[0044] Q 空 =i G i V残 [i T i CO2 i H2O Q min +α(L-L0)]

[0045] In the above relation:

[0046] Q 空 Dry quenching furnace air conductivity (m) 3 / h).

[0047] i GThe dry quenching capacity coefficient is the ratio of the actual dry quenching capacity to the baseline dry quenching capacity. It is dimensionless, and the corresponding calculation formula is:

[0048]

[0049] Where G is the actual dry quenching capacity (t / h), which is the amount of coke cooled per unit time under actual conditions. The actual capacity is measured using an electronic belt scale. G0 is the dry quenching baseline capacity (t / h). The baseline capacity is the rated operating condition of the dry quenching system, not the capacity under ideal conditions. The rated dry quenching capacity refers to the amount of coke cooled per unit time by a single dry quenching furnace, corresponding to the normal production capacity of the matching coke oven. This is the baseline capacity, the capacity under the selected rated operating condition.

[0050] i V残 This is the coke volatile matter correction factor, which is the ratio of residual volatile matter in coke to residual volatile matter in reference coke (the residual volatile matter in reference coke is 1.8% as mentioned in the national secondary metallurgical coke standard (GB / t 1996-2017)). It is dimensionless, and the corresponding calculation formula is:

[0051]

[0052] Where V 残 The residual volatile matter (%) of coke is obtained by periodically measuring it using wet quenching sampling. This parameter is periodically input into the control system by system maintenance personnel. 残0 The baseline is the residual volatile matter (%) of coke.

[0053] i T This is the temperature field correction coefficient, which is the ratio of the coke discharge temperature to the reference coke discharge temperature. It is dimensionless, and the corresponding calculation formula is:

[0054]

[0055] Where T is the actual coke discharge temperature (°C), which is measured using a radiation thermometer, and T0 is the reference coke discharge temperature (°C), which is the dry quenching design value of 180°C (water equivalent method).

[0056] i CO2 The carbon dioxide handling capacity coefficient of dry quenching gas is the ratio of the actual carbon dioxide content in the dry quenching circulating gas to the reference carbon dioxide content in the dry quenching circulating gas. It is dimensionless, and the corresponding calculation formula is as follows:

[0057]

[0058] Where V CO2The actual carbon dioxide content (%) of the dry quenching circulating gas is given by V, which is measured using a gas analyzer. 0CO2 The baseline carbon dioxide content (%) of the circulating gas for dry quenching is 12-18% under normal production conditions during dry quenching design.

[0059] i H2O This is the water treatment capacity coefficient of dry quenching gas, i.e., the ratio of the actual water content in the dry quenching circulating gas to the reference water content in the dry quenching circulating gas. It is dimensionless, and the corresponding calculation formula is:

[0060]

[0061] Where V H2O The actual water content (%) of the dry quenching circulating gas is measured using a gas analyzer. V 0H2O The reference water content (%) of the circulating gas in dry quenching is 5-7% under normal production conditions during dry quenching design.

[0062] Q min Minimum air conductivity (m) of dry quenching furnace at the reference coke discharge temperature 3 / h), which is the amount of air introduced under the baseline design parameters.

[0063] α is the space-time conductivity of the volatile matter in the reference coke (m 2 / h), which is the air conductivity coefficient under the reference design parameters.

[0064] L represents the real-time material level (m) in the dry quenching furnace, which is measured using a level gauge.

[0065] L0 is the low material level value (m) of the dry quenching furnace.

[0066] The present invention also provides a control system for applying the above-mentioned dry quenching coke air introduction control method, including a gas analyzer, an electronic belt scale, a radiation thermometer, a level gauge, and a control system. The gas analyzer is used to obtain the actual carbon dioxide content and the actual water content of the circulating gas. The electronic belt scale is used to obtain the actual throughput. The radiation thermometer is used to obtain the actual coke discharge temperature. The level gauge is used to obtain the actual material level. The gas analyzer is installed on the inlet pipe of the dry quenching furnace. The electronic belt scale is installed on the bottom outlet belt conveyor of the dry quenching furnace. The radiation thermometer is installed above the bottom outlet belt conveyor of the dry quenching furnace. The level gauge is installed inside the dry quenching furnace. The gas analyzer, the electronic belt scale, the radiation thermometer, the level gauge, and the regulating valve on the air introduction pipe are all electrically connected to the control system for transmitting the measured data to the control system.

[0067] The control system should have a display screen to show the contents of N2, O2, CO, H2, CO2 and H2O detected by the gas analyzer, the boiler inlet temperature detected by the temperature detector, the boiler internal pressure detected by the pressure sensor, the material level and other data for the staff to view.

[0068] Any adaptive changes made according to actual needs are within the scope of protection of this invention.

[0069] It should be noted that, for those skilled in the art, it is obvious that the present invention is not limited to the details of the exemplary embodiments described above, and that the invention can be implemented in other specific forms without departing from the spirit or essential characteristics of the invention. Therefore, the embodiments should be considered illustrative and non-limiting in all respects, and the scope of the invention is defined by the appended claims rather than the foregoing description. Thus, all variations falling within the meaning and scope of equivalents of the claims are intended to be included within the present invention. No reference numerals in the claims should be construed as limiting the scope of the claims.

[0070] Specific examples have been used to illustrate the principles and implementation methods of this invention. The descriptions of the above embodiments are only for the purpose of helping to understand the method and core ideas of this invention. Furthermore, those skilled in the art will recognize that, based on the ideas of this invention, there will be changes in the specific implementation methods and application scope. Therefore, the content of this specification should not be construed as a limitation of this invention.

Claims

1. A dry quenching air introduction amount control method characterized by, Includes the following steps: S1: Before using the dry quenching system, set the dry quenching baseline values, including baseline throughput, baseline residual volatile matter in coke, baseline coke discharge temperature, baseline carbon dioxide content in circulating gas, baseline water content in circulating gas, baseline minimum air conductance of the dry quenching furnace, baseline air conductance coefficient of volatile matter in coke, and low material level value of the dry quenching furnace. S2: During the use of the dry quenching system, the actual processing capacity, actual coke discharge temperature, actual residual volatile matter in coke, actual carbon dioxide content in the circulating gas, actual water content in the circulating gas, and actual material level are obtained in real time. S3: The control system acquires the data from steps S1 and S2 and calculates the air conduction of the dry quenching furnace, and automatically adjusts the regulating valve on the air inlet pipeline to control the amount of air introduced. The calculation formula used in step S3 is: In the above relation: Q 空 For dry quenching furnace air quantity; i G This is the dry quenching capacity coefficient; i V残 coefficient for coke volatile matter; i T T is the temperature field correction factor; i CO2 andi H2O Kd is the treatment capacity factor for carbon dioxide and water for dry quenching. Q min Q = minimum air flow rate of dry quenching furnace at reference focus temperature Kv is the space-time volatile matter evolution coefficient for the reference coke; L represents the real-time material level in the dry quenching furnace; L0 is the low material level value of the dry quenching furnace.

2. The dry quenching air introduction amount control method according to claim 1, characterized by, In the relation, Where G represents the actual dry quenching throughput, and G0 represents the baseline dry quenching throughput.

3. The dry quenching air introduction amount control method according to claim 1, characterized by, In the relation, where V 残 is coke residual volatile matter, V 残0 is reference coke residual volatile matter.

4. The dry quenching air introduction amount control method according to claim 1, characterized by, In the relation, Where T is the actual coke discharge temperature and T0 is the reference coke discharge temperature.

5. The dry quenching air introduction amount control method according to claim 1, characterized by, In the relation, where V CO2 is the actual carbon dioxide content of the dry quenching cycle gas, V 0CO2 is the reference carbon dioxide content of the dry quenching cycle gas.

6. The dry quenching air introduction amount control method according to claim 1, characterized by, In the relation, Where V H2O V represents the actual water content of the dry quenching cycle gas. 0H2O The reference water content is the circulating gas content for dry quenching.

7. A control system applying the dry quenching air introduction quantity control method as described in any one of claims 1-6, characterized in that, The system includes a gas analyzer for obtaining the actual carbon dioxide and water content of the circulating gas, an electronic belt scale for obtaining the actual throughput, a radiation thermometer for obtaining the actual coke discharge temperature, a level gauge for obtaining the actual material level, and a control system. The gas analyzer is installed on the inlet pipe of the dry quenching furnace, the electronic belt scale is installed on the bottom outlet belt conveyor of the dry quenching furnace, the radiation thermometer is installed above the bottom outlet belt conveyor of the dry quenching furnace, and the level gauge is installed inside the dry quenching furnace. The gas analyzer, the electronic belt scale, the radiation thermometer, the level gauge, and the regulating valve on the air inlet pipe are all electrically connected to the control system.

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