CN112090379B - Heating furnace drying temperature control method - Google Patents
Heating furnace drying temperature control method Download PDFInfo
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- CN112090379B CN112090379B CN202010862338.3A CN202010862338A CN112090379B CN 112090379 B CN112090379 B CN 112090379B CN 202010862338 A CN202010862338 A CN 202010862338A CN 112090379 B CN112090379 B CN 112090379B
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Abstract
The invention discloses a heating furnace drying temperature control method, which comprises the steps of installing a hearth temperature controller and a hearth temperature transmitter, configuring a control system main loop, arranging a hearth fuel gas flow sensor, a hearth fuel gas flow transmitter and a hearth fuel gas flow regulating valve on a hearth fuel gas pipeline, and configuring the hearth fuel gas flow transmitter with a hearth fuel gas flow controller; hearth fuel gas flow transducer, hearth fuel gas flow controller, hearth fuel gas flow regulating valve constitute control system secondary circuit, and hearth temperature controller output value is hearth fuel gas flow controller given value, and the hearth is adjusted: the invention can overcome the problems of the prior art, ensure the furnace drying effect under the conditions of not changing the design parameters and the flow of the device and not increasing additional investment and prolong the service life of the heating furnace.
Description
Technical Field
The invention relates to a temperature control method, in particular to a heating furnace drying temperature control method, and belongs to the field of petrochemical industry.
Background
Tubular heating furnace wide application in oil refining chemical plant, the heating furnace is in the work progress, and inside lining brick brickwork and refractory castable contain a large amount of free water, crystal water and remaining bound water, for avoiding that the furnace wall spalling, tympanic bulla, deformation or even furnace wall collapses because of the quick vaporization inflation of moisture in the in-process of putting into production, must carry out the baker to the heating furnace before putting into production, make free water, crystal water and remaining bound water slowly evaporate and separate out to carry out the sintering to the furnace wall castable under high temperature. In the process of baking the furnace, the furnace needs to be slowly and uniformly heated according to a baking curve corresponding to the characteristics of a castable product, the highest temperature of a hearth needs to be raised to 550 ℃ and kept at the constant temperature for 18 hours (the temperature rising curve of the hearth is shown in figure 1), in the process of baking the furnace, a burner in the hearth needs to be used for supplying heat to the hearth, the flame intensity of the burner is controlled by adjusting fuel (usually fuel gas or fuel oil) supplied to the burner so as to control the temperature of the hearth to be at a target temperature, at the moment, the heat radiation of the flame of the burner and the heat radiation of the inner wall of the hearth can raise the temperature of a furnace tube in the hearth, in order to prevent the furnace tube from being damaged due to the fact that the temperature of the furnace tube exceeds the designed temperature during baking, a heat-carrying medium needs to be introduced into the furnace tube to reduce the temperature of the furnace tube, two baking methods are generally adopted at present, the first is that medium-pressure steam is used as the heat-carrying medium for baking the furnace tube, and the steam is introduced from the inlet of the furnace tube, a silencer arranged at the outlet of the furnace tube directly exhausts the air; the second method is to use oil-carried material or nitrogen as the heat-carrying medium of the oven. The hydrogenation device needs to be synchronously carried out for shortening the startup period, the drying of the reaction heating furnace and the drying of the reaction system, the reaction heating furnace can only use nitrogen as a heat carrying medium, the low-temperature nitrogen flowing in the furnace tube is used for absorbing the heat of the furnace tube to reduce the temperature of the furnace tube, and the nitrogen in the furnace tube enters a subsequent reactor and a heat exchanger after rising in temperature and is circulated back to the inlet of the furnace tube after being cooled by air cooling and then being boosted by a compressor. For a hydrofining device, a reaction heating furnace usually adopts a double-hearth tubular furnace, a furnace inlet pipeline is divided into two branch pipes in front of the furnace, the two branch pipes respectively enter a hearth and are heated and then converged outside the furnace to form a furnace outlet pipeline (the two heating furnaces are connected in parallel), the temperature of the two hearths is synchronously raised during furnace baking, the design temperature of a hydrofining reactor is usually 400 ℃, the temperature of nitrogen at the furnace outlet cannot exceed the design temperature during furnace baking, otherwise, the high-temperature nitrogen enters the reactor to cause the overtemperature damage of the reactor.
When nitrogen is used as a heat-carrying medium for baking, a nitrogen circulation flow needs to be established, and the nitrogen circulation flow is as follows (see fig. 2):
compressor → shell side of reaction product/reaction feed heat exchanger → heating furnace → tube side of reaction product/reaction feed heat exchanger → air cooling → separator of reaction product → liquid separation tank at inlet of compressor → compressor.
When the reaction product/reaction feeding heat exchanger is a common thread locking ring type heat exchanger, the heat exchange efficiency of the thread locking ring type heat exchanger is relatively low, the temperature of nitrogen entering the inlet of the furnace tube after heat exchange is also low, when the temperature of a hearth is raised to 550 ℃, the temperature of nitrogen at the outlet of the furnace is less than 400 ℃, the temperature of a reactor is not higher than the designed value, and the furnace drying requirement can be met.
However, when the reaction product/reaction feed heat exchanger is a wound tube heat exchanger, the heat exchange efficiency of the wound tube heat exchanger is very high, so that the temperature of nitrogen circulating to the furnace inlet is high, when the temperature of a hearth is increased to 450 ℃ in the furnace baking process, the temperature of the nitrogen at the furnace inlet reaches 320 ℃, the temperature of the nitrogen at the furnace outlet reaches about 395 ℃, and is close to the design temperature of the reactor of 400 ℃, if the temperature of the hearth is continuously increased, the temperature of the reactor exceeds the design temperature, so that the reactor is damaged, the temperature of the hearth cannot be continuously increased according to a furnace baking curve, the furnace baking process cannot be continuously performed, the furnace baking effect cannot be ensured, and the service life of the heating furnace is influenced.
The existing heating furnace is only provided with a furnace temperature transmitter, the temperature of the furnace can be monitored only during the furnace baking process, the disturbance of the temperature of the furnace can be formed when the fuel gas pressure, the flow and the furnace tube can carry the heat medium amount to fluctuate, the fluctuation of the temperature of the furnace is large, the control of the quality of the furnace baking is not facilitated, the opening of a fuel gas regulating valve needs to be frequently and manually adjusted, and the labor intensity of personnel is high.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides the heating furnace drying temperature control method which has the technical characteristics of ensuring the drying effect and prolonging the service life of the heating furnace without changing the design parameters and the flow of the device and increasing the additional investment.
In order to achieve the purpose, the invention is realized by the following technical scheme:
a heating furnace drying temperature control method is characterized by comprising the following steps:
step 1): installing a furnace A temperature controller TIC1A (PID adjusting module 1) and a furnace A temperature transmitter TE1A (thermocouple) and connecting the two in configuration to form a main loop of a control system, arranging a furnace A fuel gas flow sensor FE1A (pore plate), a furnace A fuel gas flow transmitter FT1A (differential pressure transmitter) and a furnace A fuel gas flow adjusting valve FV1A on a furnace A fuel gas pipeline, and connecting the configuration of the furnace A fuel gas flow transmitter FT1A (differential pressure transmitter) with a furnace A fuel gas flow controller FIC1A (PID adjusting module 2); a hearth fuel gas flow transmitter FT1A (differential pressure transmitter), A hearth fuel gas flow controller FIC1A (PID adjusting module 2) and A hearth fuel gas flow adjusting valve FV1A form a control system secondary loop, a distributed control system DCS is adopted to realize configuration connection of the A hearth temperature controller TIC1A and the A hearth fuel gas flow controller FIC1A, and the output value (OP) of the A hearth temperature controller TIC1A is used as the given value (SP) of the A hearth fuel gas flow controller FIC1A to form an A hearth temperature cascade control system;
step 2): installing a B hearth temperature controller TIC1B (PID adjusting module 3) and a B hearth temperature transmitter TE1B (thermocouple) and connecting the two in configuration to form a control system main loop, arranging a flow sensor FE1B (orifice plate), a B hearth fuel gas flow transmitter FT1B (differential pressure transmitter), a B hearth fuel gas flow adjusting valve FV1B and a B hearth fuel gas flow transmitter FT1B (differential pressure transmitter) in a B hearth fuel gas flow controller FIC1B (PID adjusting module 4) in a B hearth fuel gas pipeline; a furnace B fuel gas flow transmitter FT1B (a differential pressure transmitter), a furnace B fuel gas flow controller FIC1B (a PID adjusting module 4) and a furnace B fuel gas flow adjusting valve FV1B form a control system secondary loop, a distributed control system DCS is adopted to realize configuration connection of a furnace B temperature controller TIC1B and a furnace B fuel gas flow controller FIC1B, and an output value OP of the furnace B temperature controller TIC1B is used as a given value SP of the furnace B fuel gas flow controller FIC1B to form a furnace B temperature cascade control system;
step 3): a, automatic adjustment of a hearth: the method is characterized in that a hearth temperature A is used as a control point to establish a control loop, two control parameters are provided in the automatic regulation process, one is a hearth temperature TIA, the other is a hearth fuel gas flow FIA, the hearth temperature TIA is used as a main loop TICA, the fuel gas flow FIA of the hearth is used as a secondary loop FICA to form cascade control, the fault position of a hearth fuel gas flow regulating valve FV1A is 'FC', the hearth fuel gas flow controller FIC1A adopts reaction, the hearth temperature controller TIC1A adopts reaction, the opening of the hearth fuel gas flow regulating valve FV1A, the hearth fuel gas flow FIA of the hearth and the hearth temperature of the A are in relation: the opening degree of a furnace A fuel gas flow regulating valve FV1A is increased, the furnace A fuel gas flow FIA is increased, and the furnace A temperature TIA is increased; the opening degree of a furnace hearth fuel gas flow regulating valve FV1A is reduced, the furnace hearth fuel gas flow FIA is reduced, and the furnace hearth temperature TIA is reduced; when the automatic control is put into use, firstly making the A hearth fuel gas flow controller FIC1A and the A hearth temperature controller TIC1A into Manual (MAN) control, controlling the temperature through the A hearth fuel gas flow controller FIC1A, making the A hearth fuel gas flow FIA into Cascade (CAS) after the A hearth temperature TIA is stable, and then making the A hearth temperature controller TIC1A into Automatic (AUTO);
the hearth self-control process comprises the following steps: when the fluctuation of the fuel gas flow FIA of the hearth A is increased, the fuel gas flow controller FIC1A of the hearth A reacts, the output value OP of the fuel gas flow controller FIC1A of the hearth A is reduced, the fuel gas flow regulating valve FV1A of the hearth A is turned down, and the fuel gas flow FIA of the hearth A is reduced; when the fluctuation of the fuel gas flow FIA of the hearth A is reduced, the fuel gas flow controller FIC1A of the hearth A reacts, the output value OP of the fuel gas flow controller FIC1A of the hearth A is increased, the fuel gas flow regulating valve FV1A of the hearth A is opened greatly, and the fuel gas flow FIA of the hearth A is increased; when the temperature TIA of the furnace A rises in a fluctuating way, the output value OP of the temperature controller TIC1A of the furnace A is reduced, the given value SP given to the fuel gas flow controller FIC1A of the furnace A is reduced, the fuel gas flow FIA of the furnace A is reduced, and the temperature TIA of the furnace A is reduced; when the fluctuation of the temperature TIA of the hearth A is reduced, the temperature controller TIC1A of the hearth A reacts, the output value OP of the temperature controller TIC1A of the hearth A is increased, the given value SP on the fuel gas flow controller FIC1A of the hearth A is increased, the fuel gas flow FIA of the hearth A is increased, the temperature TIA of the hearth A is increased, and the stable control of the temperature TIA of the hearth A is finally realized;
the self-control process of the hearth B is the same as that of the hearth A.
Preferably, the relationship between the furnace fuel gas flow control valve opening, the fuel gas flow rate and the furnace temperature is as follows: the opening of the valve is increased, the flow of the fuel gas is increased, and the temperature of the hearth is increased; the opening of the valve is reduced, the flow of the fuel gas is reduced, and the temperature of the hearth is reduced.
Preferably, the A hearth and the B hearth can be independently controlled in temperature, and the B hearth is reserved when the A hearth is heated or the A hearth is reserved when the B hearth is heated.
Has the advantages that: the existing heating furnace is only provided with a furnace temperature transmitter, the furnace temperature can be monitored only during the furnace drying period, the disturbance of the furnace temperature can be formed when the fuel gas pressure, the flow and the furnace tube can carry the heat medium amount to fluctuate, the furnace temperature fluctuation is large, the control of the furnace drying quality is not facilitated, the opening degree of a fuel gas regulating valve needs to be frequently and manually adjusted, the labor intensity of personnel is high, the invention can overcome the problems of the prior art, the furnace drying effect is ensured under the conditions of not changing the design parameters and the flow of the device and not increasing additional investment, and the service life of the heating furnace is prolonged.
Drawings
FIG. 1 is a graph of a prior art furnace temperature increase.
FIG. 2 is a flow diagram of a prior art nitrogen recycle.
FIG. 3 is a temperature rise curve chart of the hearth A and the hearth B of the invention.
Fig. 4 is a schematic structural diagram of the present invention.
FIG. 5 is a block diagram of an oven temperature control system of the present invention.
Detailed Description
The present invention will be further described with reference to the drawings attached to the specification, but the present invention is not limited to the following examples.
Preparation work before oven drying: after the construction of the heating furnace is finished, natural ventilation drying is carried out for more than 5 days at the ambient temperature, or natural ventilation drying is carried out for more than 10 days at the ambient temperature of more than 5 ℃, the installation and debugging of equipment and pipelines required for establishing nitrogen circulation are finished, during the furnace drying period, the temperature rising stage of 350-550 ℃ and the constant temperature stage of 550 ℃ of two hearths are alternately carried out, the temperature of the furnace outlet nitrogen obtained by mixing the high-temperature nitrogen of the furnace outlet branch pipe of the high-temperature hearth and the lower-temperature nitrogen of the furnace outlet branch pipe of the low-temperature hearth is controlled not to exceed 400 ℃, and a specific temperature rising curve is shown in figure 3.
Example 1: as shown in fig. 1-5, a method for controlling the baking temperature of a heating furnace includes the following steps:
step 1): installing a furnace A temperature controller TIC1A (PID adjusting module 1) and a furnace A temperature transmitter TE1A (thermocouple) and connecting the two in configuration to form a main loop of a control system, arranging a furnace A fuel gas flow sensor FE1A (pore plate), a furnace A fuel gas flow transmitter FT1A (differential pressure transmitter) and a furnace A fuel gas flow adjusting valve FV1A on a furnace A fuel gas pipeline, and connecting the configuration of the furnace A fuel gas flow transmitter FT1A (differential pressure transmitter) with a furnace A fuel gas flow controller FIC1A (PID adjusting module 2); a hearth fuel gas flow transmitter FT1A (differential pressure transmitter), A hearth fuel gas flow controller FIC1A (PID adjusting module 2) and A hearth fuel gas flow adjusting valve FV1A form a control system secondary loop, a distributed control system DCS is adopted to realize configuration connection of the A hearth temperature controller TIC1A and the A hearth fuel gas flow controller FIC1A, and the output value (OP) of the A hearth temperature controller TIC1A is used as the given value (SP) of the A hearth fuel gas flow controller FIC1A to form an A hearth temperature cascade control system;
step 2): installing a B hearth temperature controller TIC1B (PID adjusting module 3) and a B hearth temperature transmitter TE1B (thermocouple) and connecting the two in configuration to form a control system main loop, arranging a flow sensor FE1B (orifice plate), a B hearth fuel gas flow transmitter FT1B (differential pressure transmitter), a B hearth fuel gas flow adjusting valve FV1B and a B hearth fuel gas flow transmitter FT1B (differential pressure transmitter) in a B hearth fuel gas flow controller FIC1B (PID adjusting module 4) in a B hearth fuel gas pipeline; a furnace B fuel gas flow transmitter FT1B (a differential pressure transmitter), a furnace B fuel gas flow controller FIC1B (a PID adjusting module 4) and a furnace B fuel gas flow adjusting valve FV1B form a control system secondary loop, a distributed control system DCS is adopted to realize configuration connection of a furnace B temperature controller TIC1B and a furnace B fuel gas flow controller FIC1B, and an output value OP of the furnace B temperature controller TIC1B is used as a given value SP of the furnace B fuel gas flow controller FIC1B to form a furnace B temperature cascade control system;
step 3): a, automatic adjustment of a hearth: the control loop is established by taking the temperature of the hearth A as a control point, two control parameters exist in the automatic regulation process, one is the temperature TIA of the hearth A, the other is the fuel gas flow FIA of the hearth A, the temperature TIA of the hearth A is taken as a main loop (TICA), the fuel gas flow FIA of the hearth A is taken as a secondary loop (FICA), the two form cascade control, the fault position of the fuel gas flow regulating valve FV1A of the hearth A is 'FC', the fuel gas flow controller FIC1A of the hearth A adopts a reaction, the temperature controller TIC1A of the hearth A adopts a reaction, the opening of the fuel gas flow regulating valve FV1A of the hearth A, the fuel gas flow FIA of the hearth A and the temperature of the hearth are in a relation: the opening degree of a furnace A fuel gas flow regulating valve FV1A is increased, the furnace A fuel gas flow FIA is increased, and the furnace A temperature TIA is increased; the opening degree of a furnace hearth fuel gas flow regulating valve FV1A is reduced, the furnace hearth fuel gas flow FIA is reduced, and the furnace hearth temperature TIA is reduced; when the automatic control is put into use, firstly making the A hearth fuel gas flow controller FIC1A and the A hearth temperature controller TIC1A into Manual (MAN) control, controlling the temperature through the A hearth fuel gas flow controller FIC1A, making the A hearth fuel gas flow FIA into Cascade (CAS) after the A hearth temperature TIA is stable, and then making the A hearth temperature controller TIC1A into Automatic (AUTO);
the hearth self-control process comprises the following steps: when the fluctuation of the fuel gas flow FIA of the hearth A is increased, the fuel gas flow controller FIC1A of the hearth A reacts, the output value OP of the fuel gas flow controller FIC1A of the hearth A is reduced, the fuel gas flow regulating valve FV1A of the hearth A is turned down, and the fuel gas flow FIA of the hearth A is reduced; when the fluctuation of the fuel gas flow FIA of the hearth A is reduced, the fuel gas flow controller FIC1A of the hearth A reacts, the output value OP of the fuel gas flow controller FIC1A of the hearth A is increased, the fuel gas flow regulating valve FV1A of the hearth A is opened greatly, and the fuel gas flow FIA of the hearth A is increased; when the temperature TIA of the furnace A rises in a fluctuating way, the output value OP of the temperature controller TIC1A of the furnace A is reduced, the given value SP given to the fuel gas flow controller FIC1A of the furnace A is reduced, the fuel gas flow FIA of the furnace A is reduced, and the temperature TIA of the furnace A is reduced; when the fluctuation of the temperature TIA of the hearth A is reduced, the temperature controller TIC1A of the hearth A reacts, the output value OP of the temperature controller TIC1A of the hearth A is increased, the given value SP on the fuel gas flow controller FIC1A of the hearth A is increased, the fuel gas flow FIA of the hearth A is increased, the temperature TIA of the hearth A is increased, and the stable control of the temperature TIA of the hearth A is finally realized; the hearth self-control process of the B hearth is the same as that of the A hearth;
because the main control target in the normal production process is the temperature control of the furnace outlet pipeline, not the hearth temperature, when the furnace outlet temperature is selected, the furnace outlet temperature and the fuel gas flow FIA form a cascade loop, and when the hearth temperature is selected, the hearth temperature and the fuel gas flow FIA form a cascade loop.
The hearth A and the hearth B can be independently controlled in temperature, and when the hearth A is heated, the hearth B is reserved, or when the hearth B is heated, the hearth A is reserved.
The Distributed Control System DCS is called a Distributed Control System, and it uses several controllers (process stations) to Control many Control points in a production process, and the controllers are connected through network and can exchange data, and the operation uses computer operation station, and is connected with the controllers through network, collects production data, and transmits operation instructions, so the Distributed Control System DCS mainly uses Distributed Control centralized management;
structurally, the distributed control system DCS comprises a process level, an operation level and a management level, wherein the process level mainly comprises a process control station, an I/O unit and a field instrument and is a main implementation part of a system control function; the operation stage comprises an operator station and an engineer station for completing the operation and configuration of the system; the management level mainly refers to a plant management information system (MIS system). The process control station of DCS is a complete computer system, mainly composed of power supply, CPU, network interface and I/O; I/O, the control system needs to establish the input and output channels of the signal; I/O in DCS is generally modular, one I/O module has one or more I/O channels for connecting sensors and actuators (regulating valves); an I/O unit, wherein one process control station is generally composed of a plurality of racks, and each rack can be used for placing a certain number of modules; the rack where the CPU is located is called a CPU unit, only one CPU unit can be located in the same process station, and other racks which are only used for placing the I/O modules are the I/O units.
Example 2: as shown in fig. 1-5, a method for controlling the baking temperature of a heating furnace includes the following steps:
step 1): installing a B hearth temperature controller TIC1B (PID adjusting module 3) and a B hearth temperature transmitter TE1B (thermocouple) and connecting the two in configuration to form a control system main loop, arranging a flow sensor FE1B (orifice plate), a B hearth fuel gas flow transmitter FT1B (differential pressure transmitter), a B hearth fuel gas flow adjusting valve FV1B and a B hearth fuel gas flow transmitter FT1B (differential pressure transmitter) in a B hearth fuel gas flow controller FIC1B (PID adjusting module 4) in a B hearth fuel gas pipeline; a furnace B fuel gas flow transmitter FT1B (a differential pressure transmitter), a furnace B fuel gas flow controller FIC1B (a PID adjusting module 4) and a furnace B fuel gas flow adjusting valve FV1B form a control system secondary loop, a distributed control system DCS is adopted to realize configuration connection of a furnace B temperature controller TIC1B and a furnace B fuel gas flow controller FIC1B, and an output value OP of the furnace B temperature controller TIC1B is used as a given value SP of the furnace B fuel gas flow controller FIC1B to form a furnace B temperature cascade control system;
step 2): installing a furnace A temperature controller TIC1A (PID adjusting module 1) and a furnace A temperature transmitter TE1A (thermocouple) and connecting the two in configuration to form a main loop of a control system, arranging a furnace A fuel gas flow sensor FE1A (pore plate), a furnace A fuel gas flow transmitter FT1A (differential pressure transmitter) and a furnace A fuel gas flow adjusting valve FV1A on a furnace A fuel gas pipeline, and connecting the configuration of the furnace A fuel gas flow transmitter FT1A (differential pressure transmitter) with a furnace A fuel gas flow controller FIC1A (PID adjusting module 2); a hearth fuel gas flow transmitter FT1A (differential pressure transmitter), A hearth fuel gas flow controller FIC1A (PID adjusting module 2) and A hearth fuel gas flow adjusting valve FV1A form a control system secondary loop, a distributed control system DCS is adopted to realize configuration connection of the A hearth temperature controller TIC1A and the A hearth fuel gas flow controller FIC1A, and the output value (OP) of the A hearth temperature controller TIC1A is used as the given value (SP) of the A hearth fuel gas flow controller FIC1A to form an A hearth temperature cascade control system;
step 3): a, automatic adjustment of a hearth: the control loop is established by taking the temperature of the hearth A as a control point, two control parameters exist in the automatic regulation process, one is the temperature TIA of the hearth A, the other is the fuel gas flow FIA of the hearth A, the temperature TIA of the hearth A is taken as a main loop (TICA), the fuel gas flow FIA of the hearth A is taken as a secondary loop (FICA), the two form cascade control, the fault position of the fuel gas flow regulating valve FV1A of the hearth A is 'FC', the fuel gas flow controller FIC1A of the hearth A adopts a reaction, the temperature controller TIC1A of the hearth A adopts a reaction, the opening of the fuel gas flow regulating valve FV1A of the hearth A, the fuel gas flow FIA of the hearth A and the temperature of the hearth are in a relation: the opening degree of a furnace A fuel gas flow regulating valve FV1A is increased, the furnace A fuel gas flow FIA is increased, and the furnace A temperature TIA is increased; the opening degree of a furnace hearth fuel gas flow regulating valve FV1A is reduced, the furnace hearth fuel gas flow FIA is reduced, and the furnace hearth temperature TIA is reduced; when the automatic control is put into use, firstly making the A hearth fuel gas flow controller FIC1A and the A hearth temperature controller TIC1A into Manual (MAN) control, controlling the temperature through the A hearth fuel gas flow controller FIC1A, making the A hearth fuel gas flow FIA into Cascade (CAS) after the A hearth temperature TIA is stable, and then making the A hearth temperature controller TIC1A into Automatic (AUTO);
the hearth self-control process comprises the following steps: when the fluctuation of the fuel gas flow FIA of the hearth A is increased, the fuel gas flow controller FIC1A of the hearth A reacts, the output value OP of the fuel gas flow controller FIC1A of the hearth A is reduced, the fuel gas flow regulating valve FV1A of the hearth A is turned down, and the fuel gas flow FIA of the hearth A is reduced; when the fluctuation of the fuel gas flow FIA of the hearth A is reduced, the fuel gas flow controller FIC1A of the hearth A reacts, the output value OP of the fuel gas flow controller FIC1A of the hearth A is increased, the fuel gas flow regulating valve FV1A of the hearth A is opened greatly, and the fuel gas flow FIA of the hearth A is increased; when the temperature TIA of the furnace A rises in a fluctuating way, the output value OP of the temperature controller TIC1A of the furnace A is reduced, the given value SP given to the fuel gas flow controller FIC1A of the furnace A is reduced, the fuel gas flow FIA of the furnace A is reduced, and the temperature TIA of the furnace A is reduced; when the fluctuation of the temperature TIA of the hearth A is reduced, the temperature controller TIC1A of the hearth A reacts, the output value OP of the temperature controller TIC1A of the hearth A is increased, the given value SP on the fuel gas flow controller FIC1A of the hearth A is increased, the fuel gas flow FIA of the hearth A is increased, the temperature TIA of the hearth A is increased, and the stable control of the temperature TIA of the hearth A is finally realized; the hearth self-control process of the B hearth is the same as that of the A hearth;
because the main control target in the normal production process is the temperature control of the furnace outlet pipeline, not the hearth temperature, when the furnace outlet temperature is selected, the furnace outlet temperature and the fuel gas flow FIA form a cascade loop, and when the hearth temperature is selected, the hearth temperature and the fuel gas flow FIA form a cascade loop.
The hearth A and the hearth B can be independently controlled in temperature, and when the hearth A is heated, the hearth B is reserved, or when the hearth B is heated, the hearth A is reserved.
A specific oven drying step comprises the following steps:
the method comprises the following steps: the reaction system starts a circulation compressor to establish nitrogen circulation.
Step two: igniting a heating furnace nozzle to increase the temperature of the hearth, controlling the temperature of the hearth by controlling the fuel gas amount of the A/B hearth nozzle, and increasing the temperature of the A/B hearth to 150 ℃ at a temperature rise speed of not more than 15 ℃/h;
step three: controlling the temperature of the A/B hearth at 150 ℃, keeping the temperature for 20 hours, and removing natural water;
step four: after dehydration at the constant temperature of 150 ℃, the A/B hearth is heated to 250 ℃ at the speed of not more than 15 ℃/h;
step five: the temperature of the A/B hearth is controlled to be 250 ℃, and the temperature is kept for 24 hours;
step six: after the constant temperature of 250 ℃ is finished, the A/B hearth is heated to 350 ℃ at the speed of not more than 15 ℃/h;
step seven: controlling the temperature of the A/B hearth to 350 ℃, and keeping the temperature for 24 hours to remove crystal water;
step eight: after the dehydration at the constant temperature of 350 ℃, controlling the hearth A to heat up to 550 ℃ at the speed of not more than 15 ℃/h, and keeping the hearth B at the constant temperature of 350 ℃ at this stage. Controlling the temperature of nitrogen at the outlet of the furnace not to exceed 400 ℃ at this stage;
step nine: and (A) controlling the furnace hearth to be 550 ℃ and keeping the temperature for 18 hours for sintering. In the stage, the hearth of the furnace B is continuously kept at the constant temperature of 350 ℃, and the temperature of nitrogen at the outlet of the furnace is controlled not to exceed 400 ℃ in the stage;
step ten: after the furnace A is sintered at the constant temperature of 550 ℃, controlling the furnace A to cool to 350 ℃ at the speed of not more than 25 ℃/h, simultaneously controlling the furnace B to heat from 350 ℃ to 550 ℃ at the speed of not more than 15 ℃/h, and controlling the temperature of nitrogen at the outlet of the furnace to be not more than 400 ℃ at the stage;
step eleven: the furnace B is controlled to be sintered for 18 hours at the constant temperature of 550 ℃, and the furnace A is controlled to be at the constant temperature of 350 ℃. Controlling the temperature of nitrogen at the outlet of the furnace not to exceed 400 ℃ at this stage;
step twelve: after the furnace B finishes the sintering at the constant temperature of 550 ℃, controlling the furnace B to cool to 350 ℃ at a speed of not more than 25 ℃/h, and controlling the furnace A to keep the constant temperature of 350 ℃ at the stage;
step thirteen: synchronously cooling the A/B hearth to 200 ℃ at the speed of not more than 25 ℃/h, extinguishing a fire nozzle of the heating furnace, closing a flue baffle, stopping a blowing fan, and closing the furnace;
fourteen steps: and when the temperature of the A/B hearth is reduced to 100 ℃, opening the air door and the flue baffle plate, and naturally cooling to normal temperature to finish the furnace drying.
The quality detection method for the qualified oven comprises the steps of placing a castable test block in advance in a hearth before oven drying, analyzing the water content after oven drying is finished, and determining that the oven is qualified when the water content is lower than 1%.
In front of the oven, a castable test block 1 and a castable test block 2 are placed in the middle of a hearth A, and a castable test block 3 and a castable test block 4 are placed in the middle of a hearth B.
After the oven is finished and the hearth is cooled to normal temperature, taking out the test block, and detecting the water content, wherein the detection data is as follows:
| name of test block | Test block 1 | Test block 2 | Test block 3 | Test block 4 |
| Water content% | 0.51％ | 0.55％ | 0.90％ | 0.62％ |
According to the detection result, the furnace drying method can reach the furnace drying quality standard.
Finally, it should be noted that the present invention is not limited to the above embodiments, and many variations are possible. All modifications which can be derived or suggested by a person skilled in the art from the disclosure of the present invention are to be considered within the scope of the invention.
Claims (3)
1. A heating furnace drying temperature control method is characterized by comprising the following steps:
step 1): a hearth temperature controller TIC1A and a hearth temperature transmitter TE1A are installed and connected in a configuration mode to form a main loop of a control system, a hearth fuel gas flow sensor FE1A, a hearth fuel gas flow transmitter FT1A and a hearth fuel gas flow adjusting valve FV1A are sequentially arranged on a hearth fuel gas pipeline A, and a hearth fuel gas flow transmitter FT1A is connected in a configuration mode with a hearth fuel gas flow controller FIC 1A; a hearth fuel gas flow transmitter FT1A, A hearth fuel gas flow controller FIC1A and A hearth fuel gas flow regulating valve FV1A form a control system secondary loop, an A hearth temperature controller TIC1A and the A hearth fuel gas flow controller FIC1A are configured and connected, and the output value OP of the A hearth temperature controller TIC1A is used as the given value SP of the A hearth fuel gas flow controller FIC1A to form an A hearth temperature cascade control system;
step 2): a B hearth temperature controller TIC1B and a B hearth temperature transmitter TE1B are installed and connected in a configuration mode to form a main loop of a control system, a flow sensor FE1B, a B hearth fuel gas flow transmitter FT1B and a B hearth fuel gas flow regulating valve FV1B are sequentially arranged on a B hearth fuel gas pipeline, and the B hearth fuel gas flow transmitter FT1B is configured with a B hearth fuel gas flow controller FIC 1B; a B hearth fuel gas flow transmitter FT1B, a B hearth fuel gas flow controller FIC1B and a B hearth fuel gas flow regulating valve FV1B form a control system secondary loop, a B hearth temperature controller TIC1B and a B hearth fuel gas flow controller FIC1B are configured and connected, and an output value OP of the B hearth temperature controller TIC1B is used as a given value SP of the B hearth fuel gas flow controller FIC1B to form a B hearth temperature cascade control system;
step 3): a, automatic adjustment of a hearth: establishing a control loop by taking the temperature of the hearth A as a control point, wherein two control parameters exist in the automatic adjustment process, one control parameter is the temperature TIA of the hearth A, and the other control parameter is the fuel gas flow FIA of the hearth A; the hearth self-control process comprises the following steps: when the fluctuation of the fuel gas flow FIA of the hearth A is increased, the fuel gas flow controller FIC1A of the hearth A reacts, the output value OP of the fuel gas flow controller FIC1A of the hearth A is reduced, the fuel gas flow regulating valve FV1A of the hearth A is turned down, and the fuel gas flow FIA of the hearth A is reduced; when fluctuation of the fuel gas flow FIA of the hearth A is reduced, the fuel gas flow controller FIC1A of the hearth A reacts, the output value OP of the fuel gas flow controller FIC1A of the hearth A is increased, the fuel gas flow regulating valve FV1A of the hearth A is opened greatly, and the fuel gas flow FIA of the hearth A is increased; when the temperature TIA of the furnace A rises in a fluctuating way, the output value OP of the temperature controller TIC1A of the furnace A is reduced, the given value SP given to the fuel gas flow controller FIC1A of the furnace A is reduced, the fuel gas flow FIA of the furnace A is reduced, and the temperature TIA of the furnace A is reduced; when the fluctuation of the temperature TIA of the hearth A is reduced, the temperature controller TIC1A of the hearth A reacts, the output value OP of the temperature controller TIC1A of the hearth A is increased, the given value SP on the fuel gas flow controller FIC1A of the hearth A is increased, the fuel gas flow FIA of the hearth A is increased, the temperature TIA of the hearth A is increased, and the stable control of the temperature TIA of the hearth A is finally realized;
the self-control process of the hearth B is the same as that of the hearth A.
2. The heating furnace baking temperature control method according to claim 1, characterized in that: the relationship among the opening of the furnace fuel gas flow control valve, the fuel gas flow and the furnace temperature is as follows: the opening of the valve is increased, the flow of the fuel gas is increased, and the temperature of the hearth is increased; the opening of the valve is reduced, the flow of the fuel gas is reduced, and the temperature of the hearth is reduced.
3. The heating furnace baking temperature control method according to claim 1, characterized in that: the hearth A and the hearth B can be independently controlled in temperature, and when the hearth A is heated, the hearth B is reserved, or when the hearth B is heated, the hearth A is reserved.
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| CN112066736B (en) * | 2020-08-25 | 2022-03-15 | 浙江石油化工有限公司 | Method for baking double-hearth tubular heating furnace |
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