Carbonization chamber pressure control model of riser flap pressure regulating system, construction method and computer medium

Abstract

The invention provides a carbonization chamber pressure control model of a riser flap pressure regulating system and a construction method thereof, and the specific method comprises the following steps: carrying out a coking experiment according to collected coke oven process parameters to obtain a raw gas generation flow curve, then determining segments and average flow values, establishing a table corresponding to the flow values and flap opening degrees, and calculating the pressure of the riser flap pressure regulating system according to the table. And establishing a table for each coke oven to complete a control model, compiling the model into a pressure regulating control system PLC (Programmable Logic Controller) control system for calculation, and finally adjusting the opening degree of the turning plate to a specified position. According to the method, along with the change of coking time, the change of a coal blending scheme can cause the change of a gas generation amount curve, and the model is subdivided into a plurality of flap opening control schemes, so that fine adjustment is realized.

Description

Technical Field

[0001] The present invention belongs to the technical field of coke oven carbonization chamber pressure control, and in particular relates to a carbonization chamber pressure control model and construction method of a riser tube flap pressure regulating system, and a computer medium. Background Art

[0002] In the structural design of a traditional coke oven, the carbonization chamber's riser is connected to a flap valve via a bridge pipe, thereby achieving connectivity with the gas collection pipe. As a simple two-position control element, the flap valve has only two operating states: open and closed. Because the coking process of coal within the carbonization chamber generates periodic fluctuations in the amount of raw gas, the pressure at the bottom of each carbonization chamber exhibits inconsistencies. To achieve these two operating states, the gas collection pipe pressure is set to a constant value during traditional coke oven operation.

[0003] Specifically, during the coking phase, the flap valve remains fully open. In the early stages of coking, due to the high volume of gas generated, the pressure at the bottom of the carbonization chamber rises accordingly, making it easy for raw gas to leak out of the furnace door or penetrate into the combustion chamber through gaps in the furnace wall. However, toward the end of the coking phase, gas production decreases, and the pressure at the bottom of the carbonization chamber may drop to a negative state, allowing outside air to infiltrate the carbonization chamber. Therefore, achieving real-time regulation of the carbonization chamber pressure would have significant industrial benefits. Summary of the Invention

[0004] Technical Solution: To solve the above technical problems, the present invention aims to control the riser flap pressure regulating system by using a PLC system to control the flap opening size and change the area of ​​the raw gas introduction channel to the gas collecting pipe, thereby adjusting the raw gas outlet volume to achieve the purpose of regulating the bottom pressure of the carbonization chamber. Specifically, a method for constructing a carbonization chamber pressure control model of the riser flap pressure regulating system is provided, and the specific steps are as follows:

[0005] Step 1: Collect the process parameters of the coke oven;

[0006] Step 2: Conduct a coking experiment based on the collected parameters to obtain a raw gas flow curve under the corresponding parameters;

[0007] Step 3: Mark the raw gas flow curve with the corresponding coal loading time and coke pushing time;

[0008] Step 4: From the time of coal loading to the time of coking, the flow curve of a coking cycle is divided into 10 to 18 time periods. The number of sections is determined according to the flow change and the coking time. The flow fluctuation in each curve does not exceed 10%;

[0009] Step 5: Calculate the average flow rate value in each curve segment and establish a corresponding table of flow rate value and flap opening, which includes the applicable coal blending volatile content range and planned coking time range;

[0010] Step 6: Repeat steps 1 to 5 to create a set of tables for a coke oven. This set of tables should cover the volatile content range of all coal blends used in the coke oven and the planned coking time range; this set of tables is the carbonization chamber pressure control model of the riser flap pressure regulating system;

[0011] Step 7: The carbonization chamber pressure control model obtained in step 6 is incorporated into the pressure regulating control system PLC control system for calculation;

[0012] Step 8: When the riser flap pressure regulating system is in operation, the PLC control system sends a signal to adjust the flap opening to the specified position based on the current volatile content of the coal blend, the opening adjustment table corresponding to the planned coking time, and the coking time schedule.

[0013] As an improvement, the process parameters in step one include one or more of the following: coke oven type, carbonization chamber height, carbonization chamber width, coal blending scheme, coal volatile content, and planned coking time.

[0014] As an improvement, in step 4, 15 stages are provided, the coking time is 18.5 to 19.5 hours, and the volatile matter is 26 to 27%.

[0015] As an improvement, the coking time percentage and flap opening percentage of the 15 stages are as follows: first stage 0-20%, 100.00%; second stage 20-40%, 75.00%; third stage 40-50%, 50.00%; fourth stage 50-60%, 40.00%; fifth stage 60-70%, 30.00%; sixth stage 70-76%, 20.00%; seventh stage 76-80% , 16.00%; the eighth stage 80-84%, 12.00%;; the ninth stage 84-88%, 11.50%; the tenth stage 88-90%, 10.90%; the eleventh stage 90-92%, 9.8%; the twelfth stage 92-94%, 9.3%; the thirteenth stage 94-96%, 8.60%; the fourteenth stage 96-98%, 8.10%; the fifteenth stage 98-100%, 7.50%.

[0016] As an improvement, 15 stages are provided, the coking time is 18.5 to 23 hours, and the volatile matter is 24 to 28%.

[0017] As an improvement, in step 4, there are 15 stages of coking time percentage and flap opening percentage, which are as follows: first stage 0-15%, 100.00%; second stage 15-35%, 40.00%; third stage 35-50%, 22.00%; fourth stage 50-65%, 20.00%; fifth stage 65-70%, 18.50%; sixth stage 70-74%, 17.00%; seventh stage 74-78%, 12.50%; eighth stage 78-83%, 11.00%; ninth stage 83-86%, 9.0%; tenth stage 86-88%, 8.0%; eleventh stage 88-91%, 7.0%; twelfth stage 91-94%, 6.5%; thirteenth stage 94-96%, 6.20%; fourteenth stage 96-98%, 6.0%; fifteenth stage 98-100%, 5.50%.

[0018] At the same time, as another specific embodiment of the present invention, a computer medium is also provided, in which a carbonization chamber pressure control model for realizing a riser flap pressure regulating system is stored, and any of the above-mentioned construction methods is executed when the model is constructed.

[0019] Beneficial effects: The carbonization chamber pressure control model of the riser flap pressure regulating system proposed in the present invention is a carbonization chamber pressure control model for a riser flap pressure regulating system corresponding to each group of coke ovens. The model can cause changes in the gas generation curve according to changes in coking time and coal blending scheme, and can be subdivided into several flap opening control schemes to achieve fine adjustment.

[0020] At the same time, the model can adjust the flap opening in sections according to the change law of the gas generation curve, so that the pressure at the bottom of the carbonization chamber can maintain a slightly positive pressure during the coking cycle. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] Figure 1 It is a structural schematic diagram of the present invention.

[0022] Figure 2 This is the flow curve of raw gas generation in Example 1 of the present invention. DETAILED DESCRIPTION

[0023] The technical solutions in the embodiments of the present invention will be described clearly and completely below so that those skilled in the art can better understand the advantages and features of the present invention and thus more clearly define the scope of protection of the present invention. The embodiments described in the present invention are only some of the embodiments of the present invention, not all of them. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without making any creative work shall fall within the scope of protection of the present invention.

[0024] See Figure 1 As shown, the method for constructing the model of the present invention specifically includes: step 1, collecting the process parameters of the coke oven.

[0025] Step 2: Conduct a coking experiment based on the collected parameters to obtain the raw gas flow curve under the corresponding parameters. The coke oven raw gas flow curve has significant periodicity, intermittency, and volatility. Its characteristics are mainly determined by the coke oven type, turnover time (coking time), the ratio and volatile content of the incoming coal, and the rhythm of the coke pushing and coal loading operation. Therefore, the morphological characteristics of the coking coal resource flow curve will vary depending on the coke oven type and coking coal resource flow curve, so coking experiments should be conducted to obtain the raw gas flow curve under the corresponding parameters.

[0026] Step 3: Mark the raw gas flow curve with the corresponding coal loading time and coke pushing time; specifically, the horizontal axis of the raw gas flow curve is time, and the coal loading time and coke pushing time collected by the four coke oven cars are marked on the horizontal axis.

[0027] Step 4: From the time of coal loading to the time of coking, the flow curve of a coking cycle is divided into 10 to 18 time periods. The number of sections is determined according to the flow change and the coking time.

[0028] As a specific embodiment of the present invention, when dividing the flow curve, it is based on the fluctuation characteristics of the flow curve. In the initial stage of coal loading, the flow fluctuates greatly, and the number of divided curve segments is large; the flow is stable in the middle stage of coking, and the number of divided curve segments is small; at the end of coking, the coal pyrolysis reaction is basically completed, the amount of volatile matter generated is significantly reduced, and the raw coal gas flow drops sharply to 10-20% of the initial value, or even lower, and the number of divided curve segments is large, wherein the flow in each curve segment fluctuates by no more than 10%.

[0029] Step 5: Calculate the average flow rate value in each curve segment, that is, calculate the average value of the measured flow rate of each curve segment, and establish a corresponding table of flow rate value and flap opening. The table has the applicable coal blending volatile matter range and planned coking time range.

[0030] As another specific embodiment of the present invention, the specific method of step five is to select a possible coal blending volatile matter range and a planned coking time range based on the furnace type and turnover time range of the coke oven production and the coal blending structure, and conduct multiple groups of coking tests. The flow curve obtained from each group of coking tests corresponds to the volatile matter and coking time parameters of this group of coking tests, and the corresponding applicable range is selected in actual production.

[0031] Step 6. Repeat steps 1 to 5 to create a set of tables for a coke oven. This set of tables should cover the volatile content range of all coal blends used in the coke oven and the planned coking time range; this set of tables is the carbonization chamber pressure control model of the riser flap pressure regulating system.

[0032] Step 7: The carbonization chamber pressure control model obtained in step 6 is incorporated into the pressure regulating control system PLC control system for calculation.

[0033] Step 8: When the riser flap pressure regulating system is in operation, the PLC control system sends a signal to adjust the flap opening to the specified position based on the current volatile content of the coal blend, the opening adjustment table corresponding to the planned coking time, and the coking time schedule.

[0034] As another specific embodiment of the present invention, the present invention also provides a computer medium, in which a carbonization chamber pressure control model for realizing a riser flap pressure regulating system is stored, and any of the above-mentioned construction methods is executed when constructing the model.

[0035] The method for controlling the pressure of the carbonization chamber of the present invention is introduced and described below through specific embodiments.

[0036] Example 1

[0037] This example uses a 6-meter coke oven with 110 holes at a coking plant as an example. The coke oven process parameters are collected, including: oven type, carbonization chamber height, carbonization chamber width, coal blending scheme, coal volatile content, and planned coking time. Specifically, the parameters include a JN60-6 coke oven with a carbonization chamber height of 6.0 meters, a carbonization chamber width of 0.45 meters, a coal blending scheme of 45% coking coal, 10% fat coal, 15% gas coal, 20% 1 / 3 coking coal, and 10% lean coal, a coal volatile content of 24.6%, and a planned coking time of 19.5 hours.

[0038] According to the collected parameters, a coking experiment was conducted to obtain the raw gas flow curve under the corresponding parameters; specifically, when the coking time was 19 hours and the volatile matter was 26.5%, a coking experiment was conducted to obtain the raw gas flow curve as follows Figure 2 shown.

[0039] The raw gas flow curve is marked with the corresponding coal loading time and coke pushing time; then the flow curve of a coking cycle from the coal loading time to the coke pushing time is divided into 15 time periods. The number of segments is determined according to the flow change size and coking time. The flow fluctuation in each curve does not exceed 10%.

[0040] Calculate the average flow value in each curve segment and establish a corresponding table of flow value and flap opening. The table includes the applicable coal blending volatile content range and planned coking time range, as shown in Table 1.

[0041] Table 1 shows the data obtained by the final calculation of Example 1

[0042]

[0043] Example 2

[0044] In this example, coke oven process parameters are first collected, including: coke oven type, carbonization chamber height, carbonization chamber width, coal blending scheme, coal blending volatile content, and planned coking time. Specifically, the parameters are: JN60-6 coke oven, carbonization chamber height 6.0 meters, carbonization chamber width 0.45 meters, coal blending scheme: 40% coking coal, 10% fat coal, 15% gas coal, 23% 1 / 3 coking coal, 12% lean coal, coal blending volatile content 26.3%, and planned coking time 19 hours.

[0045] Then follow steps 3 to 5 above to create a table, as shown in Table 2.

[0046] Table 2 shows the data obtained from the final calculation of Example 2

[0047]

[0048] Repeating the above process, a set of tables was generated, covering coking times from 18.5 to 23 hours and coal blends with volatile content ranging from 24 to 28%. This set of tables became the carbonization chamber pressure control model for the coke oven's riser flap pressure regulating system. This model was then incorporated into the PLC control system for calculations.

[0049] When the riser flap pressure regulating system is in operation, the PLC control system sends a signal to adjust the flap opening to the specified position based on the current volatile content of the coal blend, the opening adjustment table corresponding to the planned coking time, and the coking time progress.

[0050] The above-described embodiments merely illustrate several implementations of the present invention, and while their descriptions are relatively specific and detailed, they should not be construed as limiting the scope of the patent. It should be noted that a person skilled in the art would be able to make numerous variations and improvements without departing from the spirit of the present invention, all of which fall within the scope of protection of the present invention. Therefore, the scope of protection of the patent for this invention shall be determined by the appended claims.

Claims

1. A method for constructing a carbonization chamber pressure control model for a riser flap pressure regulating system, characterized by: The specific steps are: Step 1: Collect the process parameters of the coke oven; Step 2: Conduct a coking experiment based on the collected parameters to obtain a raw gas flow curve under the corresponding parameters; Step 3: Mark the raw gas flow curve with the corresponding coal loading time and coke pushing time; Step 4: From the time of coal loading to the time of coking, the flow curve of a coking cycle is divided into 10 to 18 time periods. The number of sections is determined according to the flow change and the coking time. The flow fluctuation in each curve does not exceed 10%; Step 5: Calculate the average flow rate value in each curve segment and establish a corresponding table of flow rate value and flap opening, which includes the applicable coal blending volatile content range and planned coking time range; Step 6: Repeat steps 1 to 5 to create a set of tables for a coke oven. This set of tables should cover the volatile content range of all coal blends used in the coke oven and the planned coking time range; this set of tables is the carbonization chamber pressure control model of the riser flap pressure regulating system; Step 7: The carbonization chamber pressure control model obtained in step 6 is incorporated into the pressure regulating control system PLC control system for calculation; Step 8: When the riser flap pressure regulating system is in operation, the PLC control system sends a signal to adjust the flap opening to the specified position based on the current volatile content of the coal blend, the opening adjustment table corresponding to the planned coking time, and the coking time schedule.

2. The method for constructing a carbonization chamber pressure control model of a riser flap pressure regulating system according to claim 1, characterized in that: The process parameters in step 1 include one or more of the following: coke oven type, carbonization chamber height, carbonization chamber width, coal blending scheme, coal volatile matter, and planned coking time.

3. The method for constructing a carbonization chamber pressure control model of a riser flap pressure regulating system according to claim 1, characterized in that: In step 4, 15 stages are set, the coking time is 18.5 to 19.5 hours, and the volatile matter of the coal blend is 26 to 27%.

4. The method for constructing a carbonization chamber pressure control model for a riser flap pressure regulating system according to claim 3, characterized in that: The coking time percentage and flap opening percentage of the 15 stages are as follows: 0-20%, 100.00% in the first stage; 20-40%, 75.00% in the second stage; 40-50%, 50.00% in the third stage; 50-60%, 40.00% in the fourth stage; 60-70%, 30.00% in the fifth stage; 70-76%, 20.00% in the sixth stage; 76-80%, 1 6.00%; the eighth stage 80-84%, 12.00%; the ninth stage 84-88%, 11.50%; the tenth stage 88-90%, 10.90%; the eleventh stage 90-92%, 9.8%; the twelfth stage 92-94%, 9.3%; the thirteenth stage 94-96%, 8.60%; the fourteenth stage 96-98%, 8.10%; the fifteenth stage 98-100%, 7.50%.

5. The method for constructing a carbonization chamber pressure control model of a riser tube flap pressure regulating system according to claim 1, characterized in that: There are 15 stages, the coking time is 18.5 to 23 hours, and the volatile matter of the coal is 24 to 28%.

6. The method for constructing a carbonization chamber pressure control model for a riser tube flap pressure regulating system according to claim 5, characterized in that: In step 4, there are 15 stages of coking time percentage and flap opening percentage, which are as follows: first stage 0-15%, 100.00%; second stage 15-35%, 40.00%; third stage 35-50%, 22.00%; fourth stage 50-65%, 20.00%; fifth stage 65-70%, 18.50%; sixth stage 70-74%, 17.00%; seventh stage 74- 78%, 12.50%; the eighth stage 78-83%, 11.00%; the ninth stage 83-86%, 9.0%; the tenth stage 86-88%, 8.0%; the eleventh stage 88-91%, 7.0%; the twelfth stage 91-94%, 6.5%; the thirteenth stage 94-96%, 6.20%; the fourteenth stage 96-98%, 6.0%; the fifteenth stage 98-100%, 5.50%.

7. A computer medium storing a carbonization chamber pressure control model for realizing a riser flap pressure regulating system, wherein the construction method according to any one of claims 1 to 5 is executed when constructing the model.

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