CN113025390B - Control method, storage medium and system for automatic load distribution of gasification device - Google Patents
Control method, storage medium and system for automatic load distribution of gasification device Download PDFInfo
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Abstract
The application provides a control method, a storage medium and a system for automatic load distribution of a gasification device, wherein the method comprises the following steps: establishing a material balance model of an unconverted gas absorption tower and a converted gas absorption tower; obtaining a target load value of the absorption tower without changing the ventilation, a target value of the amount of synthesis gas removed from the absorption tower without changing the ventilation, a target load value of the absorption tower with changing the ventilation, a target value of the amount of synthesis gas removed from the absorption tower with changing the ventilation, a load adjustment rate of the absorption tower without changing the ventilation and a load adjustment rate of the absorption tower with changing the ventilation according to the output adjustment amounts of the first gas and the second gas and the material balance model; and obtaining the synthesis gas removal rate of the unchanged change gas absorption tower and the synthesis gas removal rate of the change gas absorption tower according to the pressure of the first gas pipe network. Above scheme can realize the automatic adjustment to gasification equipment load, compromise the pressure stability of product air pipe network simultaneously, reduces the unloading loss of adjustment in-process product gas, improves device degree of automation, reduces operating personnel working strength.
Description
Technical Field
The application relates to the technical field of load adjustment in chemical product process control, in particular to a control method, a storage medium and a system for automatic load distribution of a gasification device.
Background
Gasification processes are one of the major routes to syngas products, converting solid coal into gaseous syngas through a gasification process. The synthesis gas generated by the gasification device can be divided into a converted gas and an unconverted gas according to the requirements of downstream products, and the two gas flows need to be regulated after load adjustment or downstream requirements change.
In the prior art, gasification units use flow control in the unshifted stream, while the shifted stream uses valve position control. Therefore, the flow of both streams is currently controlled primarily by adjusting the flow of the unconverted air. However, the capacity of adjusting the flow of the unconverted gas is limited, when the valve of the control loop is too large or too small, the flow of the control loop cannot be effectively controlled, and the valve position of the converted gas adjusting valve needs to be adjusted manually, because the control of the two flows of the unconverted gas and the converted gas is mutually coupled, the control of the converted gas flow needs to consider parameters such as the flow, the pressure difference and the like, manual intervention not only cannot adjust in time, but also the accuracy is low, so that the precision of the automatic distribution result of the load is poor.
Disclosure of Invention
The embodiment of the application aims to provide a control method, a storage medium and a system for automatic load distribution of a gasification device, so as to solve the technical problems of low automation degree and poor distribution precision in the load distribution process of the gasification device in the prior art.
To this end, some embodiments of the present application provide a method for controlling automatic load distribution of a gasification device for generating a first gas, a second gas and a synthesis gas, the method comprising the steps of:
establishing a material balance model of an unconverted gas absorption tower and a converted gas absorption tower;
obtaining a target load value of the absorption tower with unchanged ventilation and a target value of the amount of synthesis gas removed from the absorption tower with unchanged ventilation according to the output adjustment amount of the first gas and the material balance model; obtaining a target load value of the conversion gas absorption tower and a target value of the amount of synthesis gas removed from the conversion gas absorption tower according to the output adjustment amount of the second gas and the material balance model;
obtaining the load adjustment rate of the absorption tower of the unconverted gas according to the current load value of the absorption tower of the unconverted gas and the target load value of the absorption tower of the unconverted gas; obtaining the load adjustment rate of the variable gas absorption tower according to the load adjustment rate of the unchanged variable gas absorption tower and a first set proportion;
obtaining the synthetic gas amount adjustment rate of the unchanged ventilation absorption tower according to the pressure of the first gas pipe network; and obtaining the synthesis gas removal amount adjusting rate of the shift gas absorption tower according to the synthesis gas composition limited range and the second set proportion.
In the method for controlling load automatic distribution of a gasification apparatus according to some embodiments of the present application, in the step of establishing a material balance model of the unconverted gas absorption tower and the converted gas absorption tower, the material balance model is:
F1.T×(C11+C12)+F2.T×(C21+C22)＝F1.PV×(C11+C12)+F2.SP×(C21+C22)； (1)
F1.T×C12＝F3.T×C32+F5.T×C52； (2)
F2.T×C11＝F4.T×C41+F6.T×C61； (3)
(F3.T×C32+F4.T×C42-F3.T×C33)/(F3.T×C31+F4.T×C41+F3.T×C33)＝K； (4)
wherein, F1.T is the target load value of the conversion gas absorption tower; f2.T is the target load value of the absorption tower with unchanged ventilation, F1.PV is the current load value of the absorption tower with changed ventilation, and F2.SP is the current load value of the absorption tower with unchanged ventilation;
f3.T is the target value of the amount of synthesis gas removed by the shifted gas absorption tower, F4.T is the target value of the amount of synthesis gas removed by the unchanged shifted gas absorption tower, F5.T is the target value of the second gas output by the shifted gas absorption tower, and F6.T is the target value of the first gas output by the unchanged shifted gas absorption tower, CmnIs the component content of the corresponding gas in the corresponding gas stream, where m is 1,2,3 … … 6; the first gas corresponds to n-1, the second gas corresponds to n-2, and the third gas corresponds to n-3; k is a set proportion.
In some embodiments of the present application, in the method for controlling load automatic distribution of a gasification apparatus, the target load value of a shift gas absorption tower and the target syngas removal amount of the shift gas absorption tower are obtained according to the output adjustment amount of the first gas and the material balance model; in the step of obtaining the target load value of the absorption tower with the unchanged ventilation gas and the target de-synthesis gas amount of the absorption tower with the unchanged ventilation gas according to the output adjustment amount of the second gas and the material balance model, the steps are obtained according to the formulas (1) to (4):
F1.T＝K11×F1.PV+K12×F2.SP+K13×F5.T+K14×F6.T；
F2.T＝K21×F1.PV+K22×F2.SP+K23×F5.T+K24×F6.T；
F3.T＝K31×F1.PV+K32×F2.SP+K33×F5.T+K34×F6.T；
F4.T＝K41×F1.PV+K42×F2.SP+K43×F5.T+K44×F6.T；
wherein, Kij is a correlation coefficient, obtained according to the gas composition in the corresponding gas flow, i is 1,2,3, 4; j is 1,2,3, 4.
In some embodiments of the present application, the step of obtaining the load adjustment rate of the absorption tower with unchanged ventilation according to the current load value of the absorption tower with unchanged ventilation and the target load value of the absorption tower with unchanged ventilation further includes:
acquiring the load adjustment demand rate of the absorption tower with unchanged ventilation input by a user, and acquiring the load adjustment demand rate of the absorption tower with unchanged ventilation according to the load adjustment demand rate of the absorption tower with unchanged ventilation, the current load value of the absorption tower with unchanged ventilation and the target load value of the absorption tower with unchanged ventilation.
In some embodiments of the present application, in the step of obtaining the syngas removal rate adjustment rate of the absorption tower with unchanged ventilation according to the pressure of the first gas pipe network, a relationship between the syngas removal rate f3.t of the absorption tower with unchanged ventilation and the pressure P of the first gas pipe network is as follows:
wherein, Δ F3(t) is the variable quantity of the synthesis gas removal quantity F3.T of the unchanged gas exchange absorption tower at the time t; Δ p (t) is the deviation between the target value and the actual value of the first gas piping pressure at time t; kp is the proportional gain, which is,kp is 0.2-20, Td is integration time, Td is 120-360 s, Ts is differentiation time, and Ts is 1.2-6 s.
The control method for automatic load distribution of the gasification device in some embodiments of the present application further includes the following steps:
when the unconverted gas absorption tower load reaches the unconverted gas absorption tower target load value and the converted gas absorption tower load reaches the converted gas absorption tower target load value, the adjustment of the loads of the unconverted gas absorption tower and the converted gas absorption tower is stopped.
The control method for automatic load distribution of the gasification device in some embodiments of the present application further includes the following steps:
and if the pressure fluctuation amount of the first gas pipe network is in a preset range, the deviation of the actual value of the syngas removal amount of the unchanged scavenging gas absorption tower and the target value of the syngas removal amount of the unchanged scavenging gas absorption tower is smaller than a threshold value, and the deviation of the actual value of the syngas removal amount of the changed scavenging gas absorption tower and the target value of the syngas removal amount of the changed scavenging gas absorption tower is smaller than the threshold value, stopping adjusting the syngas removal amount of the unchanged scavenging gas absorption tower and the changed scavenging gas absorption tower.
Some embodiments of the present application provide a storage medium, in which program instructions are stored, and a computer reads the program instructions and executes the control method for automatic load distribution of a gasification device according to any one of the above.
Some embodiments of the present application provide a control system for automatic load distribution of a gasification device, which includes at least one processor and at least one memory, at least one of the memories stores program instructions, and at least one of the processors reads the program instructions to execute the control method for automatic load distribution of a gasification device as described in any one of the above.
The control system for automatic load distribution of a gasification device in some embodiments of the present application further comprises:
and the pressure gauge is arranged in the first gas pipe network pipeline and used for detecting the pressure of the first gas pipe network and sending the pressure of the first gas pipe network to the processor.
Compared with the prior art, the technical scheme provided by the application at least has the following beneficial effects: the method comprises the steps of establishing a material balance model of an unconverted air absorption tower and a converted gas absorption tower, automatically calculating according to an output adjustment amount of first gas, an output adjustment amount of second gas and the material balance model to obtain a target load value of the unconverted air absorption tower, a target value of the synthesis gas removal amount of the unconverted air absorption tower, a target load value of the converted gas absorption tower and a target value of the synthesis gas removal amount of the converted gas absorption tower, obtaining a load adjustment rate of the unconverted air absorption tower and a load adjustment rate of the converted air absorption tower by combining a current load value of the unconverted air absorption tower, and obtaining a synthesis gas removal adjustment rate of the unconverted air absorption tower and a load adjustment rate of the converted air absorption tower according to the pressure of a first gas pipeline. Above scheme, according to the user demand change of first gas and second gas, combine material balance automatic calculation key parameter target value, and then can realize the automatic adjustment to gasification equipment load, and because the pipe network pressure of introducing first gas is as the auxiliary variable, adjust the speed of load adjustment, can compromise the pressure stability of first gas pipe network when automatic distribution load, reduce the atmospheric loss of first gas and second gas in the adjustment process, improve device degree of automation, reduce operating personnel working strength.
Drawings
The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application.
FIG. 1 is a flow chart illustrating a method for controlling the automatic load distribution of a gasification facility according to an embodiment of the present disclosure;
FIG. 2 is a schematic structural diagram of a gasification apparatus according to an embodiment of the present application;
FIG. 3 is a flow chart illustrating a method for controlling the automatic load distribution of a gasification unit according to another embodiment of the present disclosure;
fig. 4 is a schematic diagram of a connection relationship of a hardware structure of a control system for automatically allocating a load of a gasification apparatus according to an embodiment of the present application.
Wherein the reference numerals have the meanings indicated:
1-gasification furnace; 2-shift gas absorption tower; 3-an unconverted gas absorption tower; 4-changing the air regulating valve; 5-an unconverted gas regulating valve; 6-changing the gas absorption tower to synthesize gas regulating valve; 7-the shift gas absorption tower is used for preparing a hydrogen regulating valve; 8-removing the unconverted gas absorption tower to a synthesis gas regulating valve; 9-preparing a carbon monoxide regulating valve by the unchanged gas absorption tower.
Detailed Description
In the description of the present application, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only used for convenience of description of the present application, and do not indicate or imply that the device or component being referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present application. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present application, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; the two components can be directly connected or indirectly connected through an intermediate medium, and the two components can be communicated with each other. The specific meaning of the above terms in the present application can be understood in a specific case by those of ordinary skill in the art.
The present embodiment provides a method for controlling load automatic distribution of a gasification apparatus for generating a first gas, a second gas and a synthesis gas, as shown in fig. 1, the method comprising the steps of:
s101: and establishing a material balance model of the unconverted gas absorption tower and the converted gas absorption tower. The material weighing calculation is a process for determining the quantitative relation between the material proportion and the material conversion in the chemical production process, and is an important analysis and calculation process in the chemical process calculation. The method aims to calculate the consumption of raw materials, the yield of various intermediate products, products and byproducts and the consumption and composition of each stage in the production process according to the quantitative conversion relation between the raw materials and the products, thereby laying a foundation for heat balance calculation, other process calculation and equipment calculation. The general formula of the material balance is as follows: sigma G is put into a sigma G product, and plus sigma G is recovered and lost; wherein, sigma G is input into the total material amount of the system; sigma G product-the total amount of products and by-products produced by the system; Σ G loss — total amount of material lost in the system; SIG G recovery-total amount of material recovered in the system.
S102: obtaining a target load value of the absorption tower with unchanged ventilation and a target value of the amount of synthesis gas removed from the absorption tower with unchanged ventilation according to the output adjustment amount of the first gas and the material balance model; and obtaining a target load value of the conversion gas absorption tower and a target value of the synthesis gas removal amount of the conversion gas absorption tower according to the output adjustment amount of the second gas and the material balance model. The output adjustment amounts of the first gas and the second gas are determined according to the requirements of users, and the relationship between the tower inlet load and the output product of the converted gas absorption tower and the unconverted gas absorption tower is determined in the material balance model, so that the change of the tower inlet load can be automatically calculated according to the adjustment of the output amount.
S104: obtaining the load adjustment rate of the absorption tower of the unconverted gas according to the current load value of the absorption tower of the unconverted gas and the target load value of the absorption tower of the unconverted gas; and obtaining the load adjustment rate of the converted gas absorption tower according to the load adjustment rate of the unconverted gas absorption tower and the first set proportion. In this step, after the current load value and the target load value of the unconverted gas absorption tower are determined, the adjustment time is determined according to the user requirement, and the load adjustment rate can be calculated. Since the load at the starting end of the gasification apparatus does not change, it is considered that the total load of the shifted gas absorption tower and the non-shifted gas absorption tower should be kept constant, and in this case, the first set ratio may be "-1", that is, when the load of the shifted gas absorption tower changes to increase, the load of the non-shifted gas absorption tower changes to decrease and the amount of decrease is the same as the amount of increase in the load of the shifted gas absorption tower. If the loads of the shifted gas absorption tower and the unvented gas absorption tower have a certain proportional relationship, the proportional relationship is set as a first set proportion.
S105: obtaining the synthetic gas amount adjustment rate of the unchanged ventilation absorption tower according to the pressure of the first gas pipe network; and obtaining the synthesis gas removal amount adjusting rate of the shift gas absorption tower according to the synthesis gas composition limited range and the second set proportion. The amount of synthesis gas removed by the unchanged-change-gas absorption tower is controlled by the pressure of the first gas pipe network, so that the pressure of the first gas pipe network is selected as an auxiliary variable, the emptying of product gas in the load adjustment process can be reduced, and the utilization efficiency and the economic benefit of the product gas are improved.
According to the load distribution scheme of the gasification device, the target value of the key adjustment parameter can be quickly calculated according to the current working condition and the downstream demand change, so that the loads of the downstream devices of the gasification device can be quickly matched, and the fluctuation influence caused by the fact that the key parameter cannot be adjusted in the load adjustment process is reduced; because the downstream load is automatically distributed, the personnel operation amount in the load adjusting process is greatly reduced, and the automation degree and the safety in the load adjusting process are improved.
In the above-described embodiment, the first gas, the second gas, and the synthesis gas are determined according to an actual gasification apparatus. In one specific example, the gasification apparatus is shown in FIG. 2, the first gas is carbon monoxide, the second gas is hydrogen, and the syngas includes hydrogen, carbon monoxide, and carbon dioxide. The product is separated into converted gas and unconverted gas after oxygen and coal enter the gasification furnace 1, the converted gas passes through a converted gas absorption tower 2, the unconverted gas passes through an unconverted gas absorption tower 3, a converted gas regulating valve 4 and a converted gas detecting sensor FI-1001 are arranged in front of the converted gas absorption tower 2, and an unconverted gas regulating valve 5 and an unconverted gas detecting sensor FIC-1002 are arranged in front of the unconverted gas absorption tower 3. The shifted gas regulating valve 4 and the un-shifted gas flow regulating valve 2 are connected by feedback control of the control device.
The shift gas absorption tower 2 outputs two paths of gas flow, wherein one path is hydrogen and the other path is synthesis gas. The synthesis gas enters the gas flow of the synthesis gas after passing through the shift gas absorption tower and going to the synthesis gas regulating valve 6, the synthesis gas output by the shift gas absorption tower 2 is detected by a synthesis gas detection sensor FIC-1003, and the hydrogen output by the shift gas absorption tower 2 is output after passing through the shift gas absorption tower and going to the hydrogen production regulating valve 7 and is detected by a hydrogen detection sensor FI-1005.
The unchanged gas exchange absorption tower 3 outputs two paths of gas flows, wherein one path of gas flow is carbon monoxide, and the other path of gas flow is synthesis gas. The synthesis gas enters the gas flow of the synthesis gas after passing through the unconverted gas absorption tower and going to the synthesis gas regulating valve 8, the synthesis gas output by the unconverted gas absorption tower 3 is detected by a synthesis gas detection sensor FIC-1004, and the carbon monoxide output by the unconverted gas absorption tower 3 is output after passing through the unconverted gas absorption tower and going to a carbon monoxide regulating valve 9 and is detected by a carbon monoxide detection sensor FI-1006.
By adopting the control method for automatically distributing the load, the gasification device produces the carbon monoxide, the hydrogen and the synthesis gas to be supplied to downstream users for use, when the load of the gasification furnace 1 is not changed and the hydrogen or the carbon monoxide required by the downstream users is changed, the load of the carbon monoxide, the hydrogen and the synthesis gas needs to be redistributed, and the composition of the synthesis gas needs to be maintained to be stable. The control method provided by the application can be applied to the system, and each valve is automatically controlled through the load corresponding to each valve obtained through automatic analysis. Therefore, the load is automatically distributed according to the material balance and the proportion limit of the synthesis gas, the target value of the key parameter is calculated according to the downstream requirements on the carbon monoxide and the hydrogen, the automatic load matching is realized by using program control, and the automatic load matching and adjustment of the gasification device are realized by continuously correcting and adjusting the load adjusting rate as the load adjusting rate is matched with the user requirements.
Further, as shown in the figure, a pressure gauge PI-1001 may be provided in the hydrogen pipe network for detecting the pressure of the hydrogen pipe network. A pressure gauge PI-1002 can be arranged in the carbon monoxide pipe network and used for detecting the pressure of the carbon monoxide pipe network. Through carbon monoxide and hydrogen pipe network pressure variation condition, can reduce in the adjustment process carbon monoxide and hydrogen and empty, promote carbon monoxide and hydrogen utilization efficiency and economic benefits.
In some embodiments, the method for controlling automatic load distribution of a gasification device comprises:
F1.T×(C11+C12)+F2.T×(C21+C22)＝F1.PV×(C11+C12)+F2.SP×(C21+C22)； (1)
F1.T×C12＝F3.T×C32+F5.T×C52； (2)
F2.T×C11＝F4.T×C41+F6.T×C61； (3)
(F3.T×C32+F4.T×C42-F3.T×C33)/(F3.T×C31+F4.T×C41+F3.T×C33)＝K； (4)
wherein, F1.T is the target load value of the conversion gas absorption tower; f2.T is the target load value of the absorption tower with unchanged ventilation, F1.PV is the current load value of the absorption tower with changed ventilation, and F2.SP is the current load value of the absorption tower with unchanged ventilation; f3.T is the target value of the amount of synthesis gas removed by the shifted gas absorption tower, F4.T is the target value of the amount of synthesis gas removed by the unchanged shifted gas absorption tower, F5.T is the target value of the second gas output by the shifted gas absorption tower, and F6.T is the target value of the first gas output by the unchanged shifted gas absorption tower, CmnIs the component content of the corresponding gas in the corresponding gas stream, where m is 1,2,3 … … 6; the first gas corresponds to n-1, the second gas corresponds to n-2, and the third gas corresponds to n-3; k is a set proportion. For the device shown in FIG. 2, C1 in the above formula1Represents C1COI.e. the carbon monoxide content detected by FI-1001, C12Represents C1H2I.e. the hydrogen content detected by FI-1001, C21Represents C2COI.e., the carbon monoxide content detected by FIC-1002, C22Represents C2H2I.e., the hydrogen content detected by FIC-1002, C33Represents C3CO2I.e., the carbon dioxide content detected by FIC-1003, and so on, can determine each Cm thereinnThe corresponding gas component content.
According to the material balance model, different control strategies are used according to different intervals where the untransformed air flow regulating valve is located, the untransformed air flow control regulating valve is controlled through the transformed air flow regulating valve, the cooperative control of transformed air flow and untransformed air flow of the gasification furnace is realized, the coupling between the two flows is overcome, the transformed air flow and the untransformed air flow can be regulated quickly and stably according to load change, and the fluctuation of a downstream device due to untimely flow regulation is avoided.
Further, it is obtained according to formulas (1) to (4):
F1.T＝K11×F1.PV+K12×F2.SP+K13×F5.T+K14×F6.T；
F2.T＝K21×F1.PV+K22×F2.SP+K23×F5.T+K24×F6.T；
F3.T＝K31×F1.PV+K32×F2.SP+K33×F5.T+K34×F6.T；
F4.T＝K41×F1.PV+K42×F2.SP+K43×F5.T+K44×F6.T；
wherein, Kij is a correlation coefficient, obtained according to the gas composition in the corresponding gas flow, i is 1,2,3, 4; j is 1,2,3,4, and the correlation coefficient can be obtained by calibration test.
Through the model, the automatic load distribution system can realize automatic distribution of gasification downstream loads, reduce the operation amount of personnel in the load adjustment process and provide the automation degree and the safety of the load adjustment process. Obviously, the values of F1.PV and F2.SP can be directly detected by the detection sensors, and F5.T and F6.T can be obtained by user requirements, so that the values of F1.T, F2.T, F3.T and F4.T can be automatically obtained, and therefore, the target values of the key adjusting parameters can be quickly calculated according to the current working condition and the downstream requirements, the loads of the downstream devices of the gasification device can be quickly matched, and the fluctuation influence caused by the fact that the key parameters cannot be adjusted in place in the load adjusting process can be reduced.
In some embodiments, the unconverted gas absorption column load adjustment rate may be obtained by: acquiring an unconverted gas absorption tower load adjustment demand rate a1 input by a user, and acquiring an unconverted gas absorption tower load adjustment rate according to the unconverted gas absorption tower load adjustment demand rate a1, an unconverted gas absorption tower current load value and an unconverted gas absorption tower target load value. For example, the a1 set by the user may be directly used as the unconverted gas absorption tower load adjustment rate, or the final unconverted gas absorption tower load adjustment rate may be obtained by averaging a2 and a1 obtained by calculation, and the a2 is (target unconverted gas absorption tower load value — current unconverted gas absorption tower load value)/adjustment time, so that the unconverted gas absorption tower load adjustment rate can be brought closer to the user demand.
In some embodiments, the relationship between the amount of unshifted gas absorber de-syngas f3.t and the first gas grid pressure P is:
wherein, Δ F3(t) is the variable quantity of the synthesis gas removal quantity F3.T of the unchanged gas exchange absorption tower at the time t; Δ p (t) is the deviation between the target value and the actual value of the first gas piping pressure at time t; kp is a proportional gain, Kp is 0.2-20, such as 0.2, 1.8, 3.5, 12, 16 or 20, Td is an integration time, Td is 120-360 s, such as 120s, 150s, 280s or 360s, Ts is a differentiation time, Ts is 1.2-6 s, such as 1.2s, 2.4s, 3.8s or 6 s. The above variables can be adaptively adjusted according to actual product conditions.
In the scheme, the carbon monoxide net pressure control loop is additionally arranged, so that the speed of load change can be adjusted in time according to the change of downstream load, the fluctuation of the pipe network pressure is reduced, the matching of upstream and downstream load change is realized, the emptying of product gas in the load adjusting process is reduced, and the product gas utilization efficiency and the economic benefit are improved.
As shown in fig. 3, the method for controlling the load automatic distribution of the gasification device may further include the following steps:
s105: when the unconverted gas absorption tower load reaches the unconverted gas absorption tower target load value and the converted gas absorption tower load reaches the converted gas absorption tower target load value, the adjustment of the loads of the unconverted gas absorption tower and the converted gas absorption tower is stopped. In this step, after the load of the unconverted gas absorption tower is adjusted stably, and when the deviation of the load of the unconverted gas from the target value is less than 3%, the load adjustment of the unconverted gas absorption tower and the load adjustment of the converted gas absorption tower are considered to meet the requirement, so that the accurate and automatic load distribution of the unconverted gas absorption tower and the converted gas absorption tower is realized.
S106: if the pressure fluctuation amount of the first gas pipe network is in a preset range (namely the pressure P of the carbon monoxide pipe network is stable), the deviation of the actual value of the synthesis gas amount removed by the unconverted gas absorption tower and the target value of the synthesis gas amount removed by the unconverted gas absorption tower is smaller than a threshold value, and the deviation of the actual value of the synthesis gas amount removed by the converted gas absorption tower and the target value of the synthesis gas amount removed by the converted gas absorption tower is smaller than the threshold value, the synthesis gas removal amount adjustment of the unconverted gas absorption tower and the converted gas absorption tower is stopped. In the step, when the deviation between the synthesis gas removal amount of the unchanged gas exchange absorption tower and the synthesis gas removal amount of the transformed gas absorption tower and the calculated adjustment target value is less than 3%, the load adjustment is judged to meet the requirement, and the load distribution process is finished, so that the accurate automatic distribution of the synthesis gas removal amount of the unchanged gas exchange absorption tower and the synthesis gas removal amount of the transformed gas absorption tower is realized.
Some embodiments of the present application further provide a storage medium, in which program instructions are stored, and a computer reads the program instructions and executes the control method for automatic load distribution of a gasification device according to any one of the above.
Some embodiments of the present application further provide a control system for automatic load distribution of a gasification device, as shown in fig. 4, including at least one processor 101 and at least one memory 102, at least one of the memories 102 storing program instructions, and at least one of the processors 101 reading the program instructions and then executing the control method for automatic load distribution of a gasification device according to any one of the above aspects. The above chemical product processing control system may further include: an input device 103 and an output device 104. The processor 101, memory 102, input device 103, and output device 104 may be connected by a bus or other means. The system can execute the method provided by the embodiment of the application, and has the corresponding functional modules and beneficial effects of the execution method. For technical details that are not described in detail in this embodiment, reference may be made to the methods provided in the embodiments of the present application.
With reference to fig. 2, the control system for automatic load distribution of a gasification device in the present application further includes a pressure gauge PI-1002, which is disposed in the first gas pipe network pipeline and is configured to detect the pressure of the first gas pipe network and send the pressure of the first gas pipe network to the processor 101.
The control system for automatically distributing the load of the gasification device in the scheme can be a Distributed Control System (DCS), and the DCS is used for collecting the data of the flow and pressure measurement and realizing data communication and man-machine interaction. Inputting the following parameters in a DCS operation screen: and setting a changed gas absorption tower to the hydrogen production pipe network target load F5.T, and setting an unchanged gas absorption tower to the synthesis gas target load F6. T. And calculating a conversion gas absorption tower adjustment target value F1.T, an unchanged conversion gas absorption tower adjustment target value F2.T, a conversion gas absorption tower target load F3.T of the synthesis gas and an unchanged conversion gas absorption tower target load F4.T of the synthesis gas through a material balance model. And setting the load adjustment rate a of the absorption tower which is not converted, determining the absorption load change rate of the converted gas according to the first proportional relation, clicking on a display interface of the DCS system to confirm adjustment, and then adjusting through a sequential control program.
In one specific example, the shifted gas absorption tower load is set at 102000Nm3The flow rate of the synthetic gas removed by the shift gas absorption tower is 52900Nm3The flow rate of the hydrogen production pipe network from the shift gas absorption tower is 35000Nm3The load of the unchanged gas absorption tower is 103500Nm3The flow of a pipe network for producing carbon monoxide by the unchanged gas exchange absorption tower is 28500Nm3The syngas removal load of the unconverted gas absorption column is 56500Nm3H is used as the reference value. The carbon monoxide load needs to be increased by 3000Nm according to the downstream load change demand3And h, combining a conversion gas and unshifted gas composition balance formula and synthesis gas composition limitation, calculating to obtain a target load of 969000Nm of the conversion gas absorption tower3The target load of the synthetic gas flow rate of the shift gas absorption tower is 50092Nm3Perh, target load of the unchanged gas absorption column of 107100Nm3The syngas load of the unchanged gas absorption tower is 52900Nm3/h。
Setting the load adjustment rate of the unchanged air exchange absorption tower to 50Nm according to the downstream load adjustment requirement3H/min, the pressure control set value of the carbon monoxide generating pipe network is 5.15Mpa, Kp is set to be 0.5, Td is 20s and Ts is set to be 2s according to the dynamic relation of proportional-integral-derivative control between the synthesis gas amount removed by the unchanged ventilation gas absorption tower F3.T and the pressure P of the first gas pipe network, the load adjusting process is completed by 1.6h through an automatic load matching system, the adjusting time is reduced by 0.4h compared with the manual adjusting process, and the operation is reducedThe pressure fluctuation of the carbon monoxide production pipe network is reduced from 0.25MPa to 0.15MPa after 105 times of measurement. Obviously, the technical problems of low automation degree and poor distribution precision in the load distribution process of the gasification device are well solved by the scheme in the application.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solutions of the present application, and not to limit the same; although the present application has been described in detail with reference to the foregoing embodiments, it should be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions in the embodiments of the present application.
Claims (9)
1. A method for controlling automatic load distribution in a gasification apparatus for generating a first gas, a second gas and a synthesis gas, the method comprising the steps of:
establishing a material balance model of an unconverted gas absorption tower and a converted gas absorption tower;
obtaining a target load value of the absorption tower with unchanged ventilation and a target value of the amount of synthesis gas removed from the absorption tower with unchanged ventilation according to the output adjustment amount of the first gas and the material balance model; obtaining a target load value of the conversion gas absorption tower and a target value of the amount of synthesis gas removed from the conversion gas absorption tower according to the output adjustment amount of the second gas and the material balance model;
obtaining the load adjustment rate of the absorption tower of the unconverted gas according to the current load value of the absorption tower of the unconverted gas and the target load value of the absorption tower of the unconverted gas; obtaining the load adjustment rate of the variable gas absorption tower according to the load adjustment rate of the unchanged variable gas absorption tower and a first set proportion;
obtaining the synthetic gas amount adjustment rate of the unchanged ventilation absorption tower according to the pressure of the first gas pipe network; obtaining the synthesis gas removal amount adjustment rate of the shift gas absorption tower according to the synthesis gas composition limited range and a second set proportion;
in the step of establishing a material balance model of the unconverted gas absorption tower and the converted gas absorption tower, the material balance model is as follows:
F1.T×(C11+C12)+F2.T×(C21+C22)＝F1.PV×(C11+C12)+F2.SP×(C21+C22)； (1)
F1.T×C12＝F3.T×C32+F5.T×C52； (2)
F2.T×C11＝F4.T×C41+F6.T×C61； (3)
(F3.T×C32+F4.T×C42-F3.T×C33)/(F3.T×C31+F4.T×C41+F3.T×C33)＝K； (4)
wherein, F1.T is the target load value of the conversion gas absorption tower; f2.T is the target load value of the absorption tower with unchanged ventilation, F1.PV is the current load value of the absorption tower with changed ventilation, and F2.SP is the current load value of the absorption tower with unchanged ventilation;
f3.T is the target value of the amount of synthesis gas removed by the shifted gas absorption tower, F4.T is the target value of the amount of synthesis gas removed by the unchanged shifted gas absorption tower, F5.T is the target value of the second gas output by the shifted gas absorption tower, and F6.T is the target value of the first gas output by the unchanged shifted gas absorption tower, CmnIs the component content of the corresponding gas in the corresponding gas stream, where m is 1,2,3 … … 6; the first gas corresponds to n-1, the second gas corresponds to n-2, and the third gas corresponds to n-3; k is a set proportion; wherein the first gas is carbon monoxide, the second gas is hydrogen, and the third gas is carbon dioxide.
2. The method according to claim 1, wherein the target load value of the shift gas absorption tower and the target syngas removal amount of the shift gas absorption tower are obtained according to the output adjustment amount of the first gas and the mass balance model; in the step of obtaining the target load value of the absorption tower with the unchanged ventilation gas and the target de-synthesis gas amount of the absorption tower with the unchanged ventilation gas according to the output adjustment amount of the second gas and the material balance model, the steps are obtained according to the formulas (1) to (4):
F1.T＝K11×F1.PV+K12×F2.SP+K13×F5.T+K14×F6.T；
F2.T＝K21×F1.PV+K22×F2.SP+K23×F5.T+K24×F6.T；
F3.T＝K31×F1.PV+K32×F2.SP+K33×F5.T+K34×F6.T；
F4.T＝K41×F1.PV+K42×F2.SP+K43×F5.T+K44×F6.T；
wherein, Kij is a correlation coefficient, obtained according to the gas composition in the corresponding gas flow, i is 1,2,3, 4; j is 1,2,3, 4.
3. The method of claim 1, wherein the step of obtaining the load adjustment rate of the absorption tower with unchanged gas flow according to the current load value of the absorption tower with unchanged gas flow and the target load value of the absorption tower with unchanged gas flow further comprises:
acquiring the load adjustment demand rate of the absorption tower with unchanged ventilation input by a user, and acquiring the load adjustment demand rate of the absorption tower with unchanged ventilation according to the load adjustment demand rate of the absorption tower with unchanged ventilation, the current load value of the absorption tower with unchanged ventilation and the target load value of the absorption tower with unchanged ventilation.
4. The method of claim 3, wherein in the step of obtaining the adjusted rate of the amount of syngas removed from the absorption tower with unchanged gas as a function of the pressure of the first gas grid, the relationship between the amount of syngas removed from the absorption tower with unchanged gas as F3.T and the pressure of the first gas grid P is:
wherein, Δ F3(t) is the variable quantity of the synthesis gas removal quantity F3.T of the unchanged gas exchange absorption tower at the time t; Δ p (t) is the deviation between the target value and the actual value of the first gas piping pressure at time t; kp is proportional gain, Kp is 0.2-20, Td is integral time, Td is 120-360 s, Ts is differential time, and Ts is 1.2-6 s.
5. The method for controlling load automatic distribution of a gasification apparatus according to any one of claims 1 to 4, further comprising the steps of:
when the unconverted gas absorption tower load reaches the unconverted gas absorption tower target load value and the converted gas absorption tower load reaches the converted gas absorption tower target load value, the adjustment of the loads of the unconverted gas absorption tower and the converted gas absorption tower is stopped.
6. The method of controlling load automatic distribution of a gasification apparatus according to claim 5, further comprising the steps of:
and if the pressure fluctuation amount of the first gas pipe network is in a preset range, the deviation of the actual value of the syngas removal amount of the unchanged scavenging gas absorption tower and the target value of the syngas removal amount of the unchanged scavenging gas absorption tower is smaller than a threshold value, and the deviation of the actual value of the syngas removal amount of the changed scavenging gas absorption tower and the target value of the syngas removal amount of the changed scavenging gas absorption tower is smaller than the threshold value, stopping adjusting the syngas removal amount of the unchanged scavenging gas absorption tower and the changed scavenging gas absorption tower.
7. A storage medium having stored therein program instructions, wherein a computer reads the program instructions and executes the method for controlling gasification apparatus load automatic distribution according to any one of claims 1 to 6.
8. A control system for automatic load distribution of a gasification device, comprising at least one processor and at least one memory, at least one of the memories storing program instructions, wherein the at least one processor reads the program instructions and executes the control method for automatic load distribution of a gasification device according to any one of claims 1 to 6.
9. The system of claim 8, further comprising:
and the pressure gauge is arranged in the first gas pipe network pipeline and used for detecting the pressure of the first gas pipe network and sending the pressure of the first gas pipe network to the processor.
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