CN102174336A - Hearth temperature control device and control method for multi-nozzle opposed coal water slurry gasification furnace - Google Patents
Hearth temperature control device and control method for multi-nozzle opposed coal water slurry gasification furnace Download PDFInfo
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Abstract
The invention discloses a hearth temperature advanced control method for a multi-nozzle opposed coal water slurry gasification furnace. The method comprises the following steps of: controlling oxygen-coal proportion of the gasification furnace; controlling temperature of a hearth of the gasification furnace and performing balancing control of nozzles; and controlling temperature of the hearth. By adopting the gasification furnace hearth temperature control scheme, the problems of large oxygen-coal proportion fluctuation of a basic control loop, flow unbalance of four paths of nozzles and deflective flame spouting can be solved; the temperature of the hearth can be stabilized at a set value, the oxygen-coal proportion of each path of nozzle is coordinated and deflective spouting is avoided under the conditions of frequent changing of coals and flow fluctuation of the coal water slurry; therefore, running period of the gasification furnace is obviously prolonged and economic benefit of the coal gasification device is increased.
Description
Technical Field
The invention relates to a hearth temperature control method, in particular to a hearth temperature control device and a hearth temperature control method for a multi-nozzle opposed coal water slurry gasification furnace.
Background
China is rich in coal resources and deficient in oil and gas resources, and the special energy resource structure determines that coal is a main energy source of China for a long time. However, the utilization rate of coal in China is low in overall efficiency and serious in pollution at present. Coal gasification is an important way for clean and efficient utilization of coal resources, is an important technical basis for developing energy industry and chemical industry, and has a leading position in modern coal-based energy and chemical systems. Coal gasification technology can be divided into coal water slurry gasification technology and pulverized coal gasification technology according to the feeding form. The coal water slurry gasification technology is widely applied to systems for chemical synthesis and the like under the condition of coal type permission due to low device investment, reliable operation and high synthesis gas-water/dry gas ratio of a gasification device.
The coal water slurry gasification processes of different production processes are basically the same, and comprise the following steps: the process comprises the steps of coal water slurry preparation, gasification and coal gas primary purification and slag-containing water treatment, and the core is gasification technology. The present invention is directed to a multi-nozzle opposed gasifier (such as the one shown in patent No. 200520047515.3) designed by university of eastern university of china, etc. Compared with GE and Destec coal water slurry gasification technologies and dry coal powder gasification technologies introduced abroad, the multi-nozzle opposed coal water slurry gasification technology has great advantages in the aspects of equipment investment, operation cost, carbon conversion rate, effective gas components and the like.
The opposed multi-nozzle gasifier is based on an impinging stream principle, and water-coal-slurry and oxygen are quickly sprayed into the gasifier through four opposed nozzles and are fully mixed through impingement. In the gasification furnace, oxygen and atomized water-coal-slurry are subjected to the high-temperature radiation action of a refractory lining in the furnace, and then quickly undergo a series of complex physical and chemical processes such as preheating, moisture evaporation, coal dry distillation, volatile matter cracking combustion, carbon gasification and the like, and finally, wet coal gas and molten slag which take carbon monoxide, hydrogen, carbon dioxide and water vapor as main components are generated. The high temperature (1300-1600 ℃), high pressure (3.0-6.5 MPa) operating conditions and partially oxidized reducing atmosphere of the entrained flow coal gasification enable a series of chemical changes in the furnace to be fundamentally different from combustion processes and other gasification processes.
The hearth temperature of the gasification furnace is a key factor influencing the whole coal water slurry gasification process. If the temperature in the gasification furnace is too high, the moisture in the reaction gas is too high firstly, and the operation and the running of the subsequent working section are influenced. In addition, too high furnace temperature may affect the life cycle of the gasifier, causing damage to refractory bricks and the like. Experience shows that when the operating temperature of the gasification furnace is 1400 ℃, the service life of the refractory brick changes by 10% every time the operating temperature changes by 10 ℃, the operating temperature is increased by 50 ℃ for 3-5 days, the service life of the vault furnace brick is obviously reduced, even the vault furnace brick is broken, falls off, cracks in brick joints and the like, and the whole system can be stopped in severe cases. On the contrary, when the temperature in the furnace is too low, the content of CO in the reaction gas is increased, and the operation of the subsequent section and the water balance in the whole system are influenced. Therefore, the control of the proper temperature of the gasification furnace has great significance for prolonging the service life of the refractory bricks and reducing the operation cost.
Although the importance of the furnace temperature of the gasification furnace is very obvious, the automatic control of the furnace temperature is still lacked on site. The operation and control strategy adopted by the multi-nozzle opposed gasification furnace at present is as follows: the flow of the coal water slurry and the oxygen of each nozzle is independently controlled; the temperature of the hearth is controlled by adjusting the set value of the oxygen flow of each nozzle. The Control strategy is implemented on a Distributed Control Systems (DCS) platform on site, and the basic Control function is completed and the production process is monitored. These basic control systems ensure the safe operation of the gasification furnace, but cannot automatically control the temperature of the gasification furnace, and generally cannot adapt to the frequent change of coal types. There are three major problems. First, the basic control scheme does not allow for the ratiometric linkage of the coal-water slurry flow and the oxygen flow for a single nozzle. When the flow of the coal water slurry changes, the oxygen flow needs to be correspondingly adjusted through manual intervention so as to maintain the proper oxygen-coal ratio. Secondly, the temperature and the oxygen-coal ratio are not related to form a control loop, manual intervention is needed, and the hearth temperature is changed by manually adjusting the oxygen injection amount. Thirdly, since each nozzle is individually controlled, the balance of the flame in the furnace cannot be ensured. For the stable long-term operation of the gasification furnace, the approximate balance of the amounts of the coal water slurry and the oxygen sprayed from the four nozzles needs to be ensured. Otherwise, if the injection flow in a single nozzle is too high, the flame in the furnace is inevitably deviated from the center, and the local temperature is too high. Not only can the gasification efficiency be influenced, but also the refractory bricks can be punctured and the nozzle can be burnt out in serious cases. Therefore, the three problems cause that when the coal type changes and the flow rate of the coal slurry changes, an operator needs to manually adjust the oxygen injection amount of the four groups of nozzles for a long time so as to achieve the purposes of stable production again, high operation difficulty and long time, and the efficiency of the whole gasification process is influenced.
Therefore, in order to fully exert the potential of DCS and operation equipment in the gasification device, effectively utilize raw materials and energy sources, increase the economic benefit of the device, combine the process operation characteristics of the gasification production process, comprehensively apply the latest technology in chemical engineering and automatic control science, implement furnace temperature control and nozzle balance control on the gasification furnace, stabilize all process parameters of the gasification furnace in the optimal working state, and have extremely important practical value.
Disclosure of Invention
In order to overcome the defects of the prior art mentioned above, the invention provides a control method of a multi-nozzle opposed gasification furnace, which comprises the following steps:
oxygen-coal ratio control of gasification furnace
According to the operation requirement of the gasification furnace, the ratio of the coal water slurry and the oxygen injected into the gasification furnace by a single nozzle is always stable, so that better combustion and gasification effects are achieved. Fluctuations in the oxygen-to-coal ratio can firstly cause the flame to be off-centre and secondly can cause fluctuations in the furnace temperature, which in turn affects the composition of the synthesis gas. Therefore, the control method in the present invention first requires the ability to stably control the ratio of oxygen to the dry coal injection amount during the operation of the gasification furnace. FIG. 1 shows an oxygen-coal proportional control strategy developed for a single nozzle, with the control modules (slurry flow control and oxygen flow control) and information flow (set points and measurements for both controllers) identified by solid lines all existing basic control loops; the modules and information flows identified by dashed lines add content to the invention. When the method is realized on the DCS, the basic flow control adopts the traditional PID control algorithm. In fig. 1, the dry coal calculation module indirectly calculates the carbon flow entering the gasifier through the nozzle by using the measured values of the coal slurry flow, the coal slurry concentration, the dry coal density and the like as inputs. The oxygen coal proportion control module calculates a set value of the oxygen flow controller according to the calculated dry coal flow and the given oxygen coal ratio:
wherein
The output of the proportional controller of the ith nozzle and the set value of the oxygen flow controller of the ith nozzle,
for the dry coal flow of the ith nozzle, the calculation was made as follows
ρcoalIn order to obtain the density of the dry coal,the flow rate of the coal water slurry of the ith nozzle, ConslurryIs the concentration of the coal water slurry.
Gasifier hearth temperature control and nozzle balance control
Firstly, the furnace temperature control of the invention requires that the furnace temperature is controlled by adjusting the oxygen-coal ratio, the injection quantity of oxygen is increased to improve the temperature when the temperature is lower, and the injection quantity of oxygen is reduced otherwise. However, if the furnace temperature and the proportional control system of each nozzle are directly cascaded for control, the phenomenon of flame deflected spraying in the furnace is easily caused. First, the slurry flow meter and the oxygen flow meter of each nozzle have different deviations. If the output of the temperature controller is directly used as the set value of the proportional controller, the proportional control systems of different nozzles are necessarily required to control the oxygen flow to reach the same set value of the oxygen flow according to the same proportional value (assuming that the coal-water slurry flow of each nozzle is the same). However, due to the deviation of the flow meter, the flow rates of the coal water slurry and the oxygen which are actually sprayed into the hearth from each nozzle are different, so that the deviation spray is caused. The second reason for the offset injection is that when the oxygen-coal ratio of a single furnace tube is adjusted, the injection flow of other nozzles cannot be considered, so that the flow among the nozzles cannot be balanced, and the offset injection is caused. In summary, in designing the control scheme, it is desirable to be able to cascade temperature control and proportional control and control the temperature by relatively adjusting the oxygen-coal ratio of each nozzle, rather than absolutely keeping the flow rate of each nozzle consistent.
In order to solve the problems of temperature control and flow balance of each nozzle, the invention provides a control scheme as shown in figure 2 on the basis of proportional control. In fig. 2, the solid line module is a basic control module and a proportional control module, and the dotted line module is a temperature control and nozzle balance control module according to the present invention. The furnace temperature controller added in the invention is realized on DCS by adopting a traditional PID control module. The output of the furnace temperature controller is a relative value corresponding to the oxygen-to-coal ratio, typically a real number between 0 and 100. The hearth temperature controller changes the output of the equalizing module by adjusting the output of the relative value, and further influences the set value of the oxygen coal proportion control module, thereby achieving the purpose of controlling the hearth temperature. In order to ensure the flow balance among the nozzles, the nozzle balancing module of the invention coordinates the flow balance among the nozzles by adjusting the set value of the oxygen-coal ratio control module of each nozzle. The specific algorithm is as follows:
wherein k is a time point, OPT(k) The output of the temperature controller at time k. a isi(k-1) is the balance coefficient for the ith nozzle used at time k, which is obtained by the ratio of the oxygen-coal ratio of the ith nozzle to the average oxygen-coal ratio of the four nozzles at time k-1, as shown in equation (4). As can be seen in equation (3), the ith oxygen to coal ratio controller set point, i.e., the output of the ith nozzle equalization controller, at the current time k is superimposed by the relative increment of the temperature controller output based on the value at its own time k-1. The influence degree of the output increment of the temperature controller on the oxygen-coal ratio of each nozzle is determined by the balance coefficient of each nozzle and is also related to the ratio of the oxygen-coal ratio of the ith nozzle to the average oxygen-coal ratio at the last moment. By equalizing coefficients, due to flowThe problem of inconsistency of the oxygen-coal ratio of each nozzle caused by measurement errors such as metering and the like can be solved. When the nozzles are balanced, the set value of the hearth temperature is increased or decreased, the output of the temperature controller is increased or decreased, the changed relative value is weighted by a balance coefficient and then is superposed on a proportional controller of the oxygen-coal ratio, and the increase or decrease of the injection quantity of the oxygen is further controlled. For the nozzle with larger oxygen coal ratio caused by the measurement error of the flow meter, the increment or decrement of the set value of the oxygen coal ratio controller is relatively larger through the balance coefficient, and conversely, for the nozzle with smaller oxygen coal ratio, the increment or decrement is relatively smaller when the output of the temperature controller is changed.
According to the hearth temperature control and the nozzle balance control provided by the invention, under the condition that the temperature setting is increased and decreased, the oxygen injection amount of each nozzle is increased and decreased in a balanced manner. Except that can control furnace temperature, can also stop the inclined to one side phenomenon of spouting of flame in the furnace.
Hearth temperature control implementation operation method
By integrating the oxygen-coal ratio control, the hearth temperature control and the nozzle balance control, the control method provided by the invention can achieve the following control effects:
1. the proportion setting of the oxygen-coal proportion controller is determined by a temperature controller and a nozzle balance controller;
2. after the proportion set value of the oxygen-coal proportion controller is stable, the proportion controller keeps the oxygen-coal proportion to reach a set value by adjusting the oxygen injection amount;
3. when the load of the coal water slurry is changed, the proportion controller is firstly operated to adjust the oxygen injection amount so as to maintain the given oxygen-coal ratio. When the change of the load affects the temperature of the hearth, the temperature controller and the nozzle balance control module change the set value of the oxygen-coal ratio control of each nozzle, and when the control is controlled at the set value, the flow of the four nozzles is ensured to be consistent, and the generation of the partial injection is avoided.
In order to ensure that the control method provided by the invention is matched with a basic loop existing on the original DCS to finish the temperature control of the hearth and the balanced control of the nozzles, the invention also provides a corresponding control method switching method.
1. In the basic control loop mode, the oxygen and coal slurry flow controllers are in an automatic control state. The oxygen-coal ratio controller, the nozzle balance controller and the hearth temperature controller are in manual states. In this mode, the output of the oxygen-to-coal ratio controller tracks the set value of the corresponding oxygen flow controller; the set value of the oxygen-coal ratio controller is obtained by dividing the measured value of the oxygen flow by the measured value of the dry coal flow; the output of the furnace temperature controller is set to 50 (assuming that the output range of the temperature controller is 0-100); the output of each nozzle balance controller tracks the set value of the corresponding oxygen-to-coal ratio controller. The operator adjusts the balance between furnace temperature and flow rate of each nozzle by manually changing the set point of each flow controller.
2. After the gasification furnace is controlled stably, the mode of controlling the temperature and the nozzle in a balanced mode can be switched. Firstly, the oxygen-coal ratio controller and the oxygen flow controller are controlled in a cascade mode. At this time, the output of the oxygen/coal ratio controller is set as a set value of the oxygen flow controller, and the control is aimed at maintaining a stable oxygen/coal ratio. The oxygen-to-coal ratio controller setting can still be changed manually. The output of the nozzle balance controller still tracks the set value of the oxygen-to-coal ratio controller. The oxygen to coal ratio controller and nozzle balance controller are then set to cascade mode. At this time, the output value of the nozzle balance controller is calculated according to equations (3) and (4) and is used as the set value of the nozzle balance controller. At this time, the furnace temperature control can be controlled by manually setting the set value of the furnace temperature controller. The load is adjusted by adjusting the spraying amount of the coal water slurry of each nozzle.
3. When the temperature control and nozzle balance control functions are not good, the basic control mode can be switched to ensure the safe operation of the gasification furnace. The nozzle balance controller and the oxygen-to-coal ratio controller are first set to initialize the manual mode and the automatic mode, respectively. The nozzle balance controller outputs the set value of the oxygen-coal ratio controller at this time. The furnace temperature controller is manual and the output is 50. The oxygen-coal ratio controller setting value can still be set manually at this time. Then, the oxygen flow control module is set to be automatic, and the output of the oxygen-coal ratio controller tracks the set value of the oxygen flow control module. The set value of the oxygen-coal ratio controller is obtained by dividing the oxygen flow rate by the dry coal flow rate.
In the invention, the proposed proportion control module, temperature control module, nozzle balancing module and corresponding implementation operation method are combined into a control method for the multi-nozzle opposed coal-water slurry gasification furnace. The proportion control module ensures that the oxygen-coal ratio is controlled at a set value, and the temperature control module ensures that the temperature of the hearth is controlled at the set value by adjusting the set value of the oxygen-coal proportion controller. The nozzle balancing module can ensure that the flow of each group of nozzles is balanced on the basis of controlling the temperature of the hearth, and avoids the deviation of flame from the central position of the hearth. In addition, the implementation operation method provided by the invention can safely add the provided control method on the basis of not changing the original basic control loop, thereby improving the guidance for field implementation.
Drawings
FIG. 1 is a schematic diagram of a single nozzle oxygen to coal ratio control module.
FIG. 2 is a schematic view of a multi-nozzle opposed coal-water slurry gasification furnace hearth temperature control device with multiple equilibrium branches.
FIG. 3 is a configuration diagram of a single nozzle A-way slurry flow controller, a dry coal flow calculation module, an oxygen/coal ratio controller, and an oxygen flow controller implemented by a PKS.
Fig. 4 is a configuration diagram of a furnace temperature control device with multiple equalization branches implemented by the PKS.
Detailed Description
The following examples are given to aid in the understanding of the present invention, but are not intended to limit the scope of the present invention.
The designed control loop is configured using the Process Knowledge System (PKS) of Honeywell. The control system aims at a process of four-nozzle opposed gasification furnaces, and has four nozzle systems of A, B, C and D. In this embodiment, the following functional modules inherent in the PKS are used:
1. each path of coal water slurry flow measurement module FI1203A (B, C, D) _ 1; each path of oxygen flow measuring module FI1303A (B, C, D) _ 1; each path of coal water slurry concentration measuring module FI1403A (B, C, D) _ 1; each path of dry coal density measuring module FI1503A (B, C, D) _ 1; a measurement module TI1304 for the temperature of the hearth;
2. an output module FV1203A (B, C, D) _1 for controlling the opening of each path of coal water slurry flow valve; an output module FV1303A (B, C, D) _1 for controlling the opening of each path of oxygen flow valve;
and 3, the DATAACQ module carries out processing such as filtering clamping, low signal cutoff, alarming and the like on each measured value, and finally converts the measured value into an expected engineering unit output value.
4. A digital multiplication module (COALCCA, COALCB, COALCC, COALCLCD) for calculating the flow of each path of dry coal, which is used for eliminating the disturbance of the coal slurry concentration and the dry coal density of the coal water slurry on the oxygen flow control and manufacture, and can be referred to as a formula (2)
5. A controller module: the controller module used in the scheme comprises a PID control module, a proportional control module and an increment addition controller. The FIC1203A (B, C, D) _1 of each path of coal water slurry flow controller and the FIC1303A (B, C, D) _1 of each path of oxygen flow controller are realized by adopting PID modules. Each path of oxygen/coal proportional controller RATIOCTLA (B, C, D) is a proportional controller and forms cascade control with each path of oxygen flow controller. And the furnace mouth balance controllers FYI _1303A (B, C, D) _1 of each channel and the oxygen/coal ratio controllers of each channel form cascade control, and are realized by adopting an increment addition control module so as to realize the control strategies designed by the formulas (3) and (4). OP in the formula (3)T(k) And OPT(k-1) corresponding to the input value of the previous execution cycle and the input value of the current execution cycle of the tuyere balancing controller, that is, the output value of the current execution cycle and the output value of the previous execution cycle corresponding to the furnace temperature controller TIC 1304; a in the formula (4)iThe scaling factor denoted (k-1) (the equalization coefficient for the ith nozzle used at time k) is implemented by the arithmetic block ENHREGCALCA _ A (B, C, D).
The connection relationship of the control modules is introduced by taking the A-way furnace tube as an example so as to realize the proposed hearth temperature control method. First, the measurement module TI1304 of the furnace temperature obtains a measurement of the furnace temperature through the AI channel, the output of which is taken as input of the module DATAACQ. The furnace temperature measurement signal is converted into a value in engineering quantity units by the DATAACQ module and enters the furnace temperature controller TIC1304 as a measurement value. The other input to the controller TIC1304 is its set point. The output of the temperature controller is connected to the input of the equalization module FYI _1303A, while the other input is the output of the calculation module ENHREGCALCA _ A. The output of block ENHREGCALCA _ A gives the equalization coefficients for the A-way furnace tubes. The output of FYI _1303A is connected to the set point input of the A-way oxygen-coal ratio controller RATIOCTLA. And the other input end of the RATIOCTLA is connected with the output of the A-path dry coal flow calculation module COALCLCLA. The inputs of the modules COALCLCA are the outputs of the measurement modules FI1203A _1, FI1403A, FI1503A through DATAACQ. Wherein the measured value of FI1503A is input as the measured value of the coal-water slurry flow controller FIC1203A through the output of DATAACQ. The other input to the controller module FIC1203A is its set point. The output of the oxygen-coal ratio controller RATIOCTLA is connected to the set point input of an oxygen flow controller FIC 1303A. The measurement input of the FIC1303A comes from the output port of the measurement module FI1303A via DATAACQ. The outputs of the controller FIC1303A and FIC1203A are applied directly to respective control valve modules FV1303A and FV 1203A. The connection relation establishes a part of the oxygen-coal ratio control and the hearth temperature of the A-way furnace tube. Through similar establishment of control systems of other three furnace tubes, the whole hearth temperature control system can be established.
How to switch the established control system with the basic control loop mode is as follows:
1. in the mode of the basic control loop, the oxygen and coal water slurry flow controllers FIC1303A (B, C, D) and FIC1203A (B, C, D) are in an automatic control state. The proportional controller RATIOCTLA (B, C, D), the nozzle equalization controller FYI _1303A (B, C, D), and the furnace temperature controller TIC1304 are in an initial manual state. In this mode, the output of the proportional controller RATIOCTLA (B, C, D) tracks the set point of the corresponding oxygen flow controller FIC1303A (B, C, D), which is determined by dividing the measured value of oxygen flow FI1303A (B, C, D) by the measured value of dry coal flow COALCLCLA (B, C, D); the output of the furnace temperature controller TIC1304 is set to 50 (assuming the temperature controller output is in the range of 0-100); the output of each nozzle balancing controller FYI _1303A (B, C, D) tracks the set point of the corresponding proportional controller RATIOCTLA (B, C, D).
2. After the gasification furnace is controlled stably, the mode of controlling the temperature and the nozzle in a balanced mode can be switched. First, the proportional controller ratiocotla (B, C, D) and the oxygen flow controller FIC1303A (B, C, D) are cascaded. At this time, the output of the ratio controller ratiocotla (B, C, D) is set as the oxygen flow controller FIC1303A (B, C, D), and the control is aimed at maintaining a stable oxygen-coal ratio. The set value of the proportional controller RATIOCTLA (B, C, D) can still be changed manually. The output of the nozzle equalization module FYI _1303A (B, C, D) still tracks the set point of the proportional controller RATIOCTLA (B, C, D). The oxygen to coal ratio controller RATIOCTLA (B, C, D) and nozzle equalization module FYI _1303A (B, C, D) are then set to cascade mode. At this time, the output value of the nozzle equalization module FYI _1303A (B, C, D) is calculated according to equations (3) and (4) and is used as the set value of the proportional control module ratiocotla (B, C, D). At this point, the furnace temperature control may be controlled by manually setting the set point of the temperature control module TIC 1304. The load was adjusted by adjusting the amount of coal-water slurry injected from each nozzle (by adjusting the set value of FIC1203A (B, C, D)).
3. When the temperature control and nozzle balance control functions are not good, the basic control mode can be switched to ensure the safe operation of the gasification furnace. The nozzle equalization control module FYI _1303A (B, C, D) and the proportional control module RATIOCTLA (B, C, D) are first set to initialize manual and automatic modes, respectively. The nozzle equalization module FYI _1303A (B, C, D) outputs a set point that tracks the proportional control module ratio (B, C, D) at this time. The temperature control module TIC1304 is manual and the output is 50. The set-point of the proportional control module RATIOCTLA (B, C, D) can still be set manually at this time. Then, the oxygen flow control module FIC1303A (B, C, D) is set to automatic, at which time the output of the proportional control module ratiocotla (B, C, D) tracks the set value of the oxygen flow control module FIC1303A (B, C, D). The set value of the proportional control module RATIOCTLA (B, C, D) is obtained by dividing the oxygen flow by the dry coal flow.
In summary, the embodiments of the present invention are merely exemplary embodiments, and are not intended to limit the scope of the present invention. That is, all equivalent changes and modifications made according to the content of the claims of the present invention should be within the technical scope of the present invention.
Claims (7)
1. The hearth temperature control device of the opposed coal water slurry gasification furnace of the multiinjector, including a single-nozzle oxygen coal than the control module, this module includes:
the coal slurry flow controller takes a coal slurry flow set value and a measured value as input, and adjusts the valve to enable the flow to reach the set value;
an oxygen flow controller which takes an oxygen flow set value and a measured value as input so as to adjust a valve to enable the flow to reach the set value;
it is characterized by also comprising:
the dry coal flow calculation module takes a water-coal-slurry flow measured value, a water-coal-slurry concentration measured value and a dry coal density measured value as input and carries out the following operations:
wherein
Measured dry coal flow for the ith nozzle, ρcoalAs a measure of the density of the dry coal,
measured value of flow rate of coal water slurry of the ith nozzle, ConslurryThe measured value of the concentration of the coal water slurry is obtained as the flow rate of the obtained dry coal
Is an output;
the module further comprises:
an oxygen-coal ratio controller which takes an oxygen-coal ratio set value and a dry coal flow rate output by the dry coal flow controller as input and performs the following operations:wherein,
the output of the proportional controller of the ith nozzle and the set value of the oxygen flow controller of the ith nozzle,
the dry coal flow rate of the ith nozzle,
is the set value of the oxygen-coal ratio controller.
2. The temperature control device of claim 1, wherein the input end of the single-nozzle oxygen-coal ratio control module is connected with a nozzle balance controller to form a single-nozzle balance branch, and the nozzle balance controller takes the output of the furnace temperature controller as input and performs the following operations:
whereink is a time point, OPT(k) Is the output of the furnace temperature controller at time k, ai(k-1) equilibrium coefficient for the ith nozzle used at time k, in terms of the resulting oxygen-to-coal ratioFor output, the output is sent to an oxygen-coal ratio control module as a set value; the temperature control device is composed of a plurality of branches, the input ends of the branches are connected with a hearth temperature controller, the temperature controller takes a hearth temperature set value and a measured value as input, and the obtained output is transmitted to each nozzle balance controller.
3. A method for controlling the hearth temperature of the opposed multi-nozzle coal-water slurry gasification furnace according to claim 1, comprising the steps of:
step 1, inputting a coal water slurry flow measurement value, a coal water slurry concentration measurement value and a dry coal density measurement value into a dry coal flow module, operating the module, and outputting a dry coal flow value to an oxygen-coal ratio controller;
and 2, inputting the dry coal flow and the oxygen-coal ratio into an oxygen-coal ratio controller, operating the controller, and outputting an oxygen flow set value to an oxygen flow controller.
4. A method for controlling the hearth temperature of the opposed multi-nozzle coal-water slurry gasification furnace according to claim 2, wherein the equilibrium temperature control method comprises the following steps:
step 0, outputting the hearth temperature controller to a nozzle balance controller, operating the controller, and outputting an oxygen-coal ratio set value to an oxygen-coal ratio controller;
step 1, inputting a coal water slurry flow measurement value, a coal water slurry concentration measurement value and a dry coal density measurement value into a dry coal flow module, operating the module, and outputting a dry coal flow value to an oxygen-coal ratio controller;
step 2, inputting the dry coal flow and the oxygen-coal ratio into an oxygen-coal ratio controller, operating the controller, and outputting an oxygen flow set value to an oxygen flow controller;
and 3, controlling the temperature of the hearth by manually setting a set value of the hearth temperature controller.
5. The control method of claim 4, further comprising switching the equalization temperature control method to a basic loop control method, wherein the nozzle equalization controller, the oxygen-to-coal ratio controller, and the oxygen flow controller are in a manual mode, or an automatic mode, wherein an output of the nozzle equalization controller tracks a set value of the oxygen-to-coal ratio controller, an output of the oxygen-to-coal ratio controller tracks a set value of the oxygen flow control module, and the set value of the oxygen-to-coal ratio controller is determined by dividing an oxygen flow by a dry coal flow.
6. The control method of claim 5, wherein the equalization temperature control method switches to a basic loop method, further comprising the steps of:
step 4, setting the nozzle balance controller and the oxygen-coal ratio controller into an initialization manual mode, setting the hearth temperature controller into manual mode, and outputting a preset value;
and 5, setting the oxygen flow and the coal water slurry flow control module to be automatic, namely, the output of the oxygen-coal ratio controller tracks the set value of the oxygen flow control module, and the set value of the oxygen-coal ratio controller is obtained by dividing the oxygen flow by the dry coal flow.
7. The control method of claim 5, wherein the basic loop method is switched to the equilibrium temperature control method, comprising the steps of, before said step 0:
step-2, the output of the oxygen-coal ratio controller is used as a set value of the oxygen flow controller, the oxygen-coal ratio controller keeps a manual mode, namely the oxygen-coal ratio controller oxygen-carbon ratio set value is changed manually, and the nozzle balance controller keeps an automatic mode, namely the nozzle balance controller outputs a set value tracking the oxygen-coal ratio controller;
step-1 the oxygen to coal ratio controller and the nozzle balance controller are set to cascade mode.
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