A process for deaerating feedwater for a heating boiler and a control system therefor

Abstract

The application belongs to the technical field of chemical industry and provides a heating boiler feed water deoxidization process and a control system thereof. The application realizes the solution of boiler feed water and cold slag machine heat exchange temperature linkage control, can stably control the cold slag machine heat exchange temperature, ensures the safe operation of the cold slag machine, and can fully recover the low variable excess heat of the slag preheating and synthetic ammonia device. The inlet water temperature of the deaerator after waste heat recovery reaches 110 DEG C, which can realize the purpose of removing oxygen without additional steam.

Description

Technical Field

[0001] This application belongs to the field of chemical control technology, and in particular relates to a deoxygenation process for feedwater in a heating boiler and its control system. Background Technology

[0002] In heating systems, drum slag coolers are commonly used to recover the physical heat of the slag and lower the temperature of the boiler bottom ash, providing a safe working environment for slag removal. Slag coolers typically use demineralized water as the cooling medium, which recovers heat from the slag and increases the temperature of the demineralized water, reducing steam consumption in the deoxygenation process. The demineralized water, heated by the slag cooler, is then sent to the deaerator to remove oxygen before being used as boiler feedwater.

[0003] However, since the advent of the drum slag cooler, the outlet temperature of the slag cooler has been difficult to control stably. If the temperature of the heat exchange cooling water is too high, a large amount of steam will be generated rapidly and the pressure will rise sharply. If the pressure exceeds the pressure that the cooling water chamber of the slag cooler can withstand, a large amount of energy will be released instantly and converted into mechanical energy, thus causing an explosion.

[0004] When the demineralized water enters the parallel slag cooler for heat exchange, the operator needs to adjust the flow controller FIC001 according to the boiler load. The heat exchange temperature of the slag cooler is determined by both the slag discharge rate and the amount of hot water exchanged in the slag cooler.

[0005] When the hot water exchange volume of the slag cooler is constant, a sudden increase in the slag volume will cause the heat exchange temperature to rise rapidly. If human intervention is not timely, the slag cooler may be at risk of overheating and explosion. Therefore, it is necessary to implement linkage to reduce safety hazards. Summary of the Invention

[0006] This application provides a boiler feedwater deaeration process and its control system, which can fully recover waste heat from the slag and significantly reduce the steam consumption of the deaerator, thus ensuring the safe operation of the slag cooler and reducing the energy consumption of the equipment.

[0007] In a first aspect, embodiments of this application provide a deaeration process for boiler feedwater, including four slag coolers, four boilers, and two deaerators. The deaerators further include deaerators. The steps are as follows:

[0008] Medium-pressure steam is added, and after being reduced to low-pressure steam through pipeline A, it is split into two streams and enters deaerator A and deaerator B respectively.

[0009] The condensate enters deaerator A and deaerator B through pipeline B;

[0010] Add demineralized water, which flows through pipeline C. Pipeline C splits into two paths: one path enters deaerator A, and the other path passes through four parallel slag coolers for heat exchange before converging and splitting into two paths: one path flows through pipeline F into deaerator A, and the other path flows through pipeline E into deaerator B.

[0011] The urea condensate is added through a one-way valve connected to the demineralized water pipeline D. After mixing, the mixture enters the low-level heat recovery equipment of the ammonia synthesis unit for heat exchange before being sent out into pipelines F and E.

[0012] A gas-liquid connection is provided between deaerator A and deaerator B. The water processed by deaerator A and deaerator B flows out as boiler feedwater.

[0013] After being heated by the slag cooler, the demineralized water is mixed with the condensate from the urea unit and then sent to the ammonia synthesis unit for heat exchange with the low-temperature gas, raising the temperature to 110°C. It is then sent to the deaerator for oxygen removal.

[0014] Secondly, this application also provides a control system for implementing the process of the first aspect, comprising:

[0015] Pressure gauges are installed on deaerator A and pipeline A, respectively, and a pressure controller PIC01 for deaerator A is connected to the pressure gauges in communication.

[0016] Pressure gauges are installed in deaerator B and pipeline A respectively, and a pressure controller PIC02 for deaerator B is connected to the pressure gauges in communication.

[0017] Inside deaerator A, at the front end of deaerator A and pipeline F, there are level sensors and a deaerator A level controller LIC01 that is communicatively connected to the level sensors.

[0018] A deaerator B level controller LIC02 is installed on pipeline E.

[0019] Deaerator B is equipped with a liquid level sensor and a deaerator liquid level controller LIC03 that is communicatively connected to the liquid level sensor; the deaerator liquid level controller LIC03 is associated with the deaerator B liquid level controller LI02.

[0020] A flow meter is installed at the front end of pipeline C, and a demineralized water controller FIC001 is connected to the flow meter in communication.

[0021] Four temperature sensors, TI01, TI02, TI03 and TI04, are installed at the rear end of the slag cooler and are connected to the slag cooler temperature controller, TIC001, for communication.

[0022] It also includes a condensate conductivity AI803 installed on pipe B, and a condensate flow controller FIC02 installed at its rear end;

[0023] Temperature sensors TI05 and TI06 are also installed in deaerator A and deaerator B.

[0024] TI05 and TI06 are connected to the system.

[0025] The system also includes: the over-temperature control of the slag cooler is applied to the demineralized water flow control in pipeline C after the temperature controller of the slag cooler reaches the safety warning setting.

[0026] The system also includes deaerator A and deaerator B with pressure control at 0.02-0.04 MPa and water temperature ≥100℃.

[0027] The control system includes valves or solenoid valves installed in the pipeline for use in control.

[0028] The beneficial effects of the embodiments in this application compared with the prior art are:

[0029] This boiler feedwater deaeration process achieves coordinated control of the boiler feedwater and slag cooler heat exchanger temperatures. It can stably control the slag cooler's heat exchanger temperature, ensuring its safe operation, while also fully recovering excess heat from slag preheating and the ammonia synthesis unit. After waste heat recovery, the deaerator inlet water temperature reaches 110℃, enabling the deaerator to remove oxygen without the need for additional steam.

[0030] Operators can set relevant control logic through the slag cooler heat exchanger temperature controller on the operating interface to achieve automatic switching control of boiler feedwater. This boiler feedwater deoxygenation process has the characteristics of high automation, convenient use, stable control, and high waste heat recovery utilization rate. It can effectively eliminate the problem of overheating and explosion of the slag cooler and can significantly reduce the energy consumption of the equipment. Attached Figure Description

[0031] To more clearly illustrate the technical solutions in the embodiments of this application, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0032] Figure 1 This is a schematic diagram of a system provided in an embodiment of this application;

[0033] Figure 2 This is a block diagram of an adjustment method provided in an embodiment of this application;

[0034] Figure 3 This is the diagram showing the relationship between the over-temperature interlock commands of the slag cooler provided in this application. Detailed Implementation

[0035] In the following description, specific details such as particular system architectures and techniques are set forth for illustrative purposes and not for limitation, in order to provide a thorough understanding of the embodiments of this application. However, those skilled in the art will understand that this application may also be implemented in other embodiments without these specific details. In other instances, detailed descriptions of well-known systems, apparatuses, circuits, and methods have been omitted so as not to obscure the description of this application with unnecessary detail.

[0036] It should be understood that, when used in this application specification and the appended claims, the term "comprising" indicates the presence of the described features, integrals, steps, operations, elements and / or components, but does not exclude the presence or addition of one or more other features, integrals, steps, operations, elements, components and / or a collection thereof.

[0037] It should also be understood that the term “and / or” as used in this application specification and the appended claims means any combination of one or more of the associated listed items and all possible combinations, and includes such combinations.

[0038] As used in this application specification and the appended claims, the term "if" may be interpreted, depending on the context, as "when," "once," "in response to determination," or "in response to detection." Similarly, the phrase "if determined" or "if detected [the described condition or event]" may be interpreted, depending on the context, as meaning "once determined," "in response to determination," "once detected [the described condition or event]," or "in response to detection [the described condition or event]."

[0039] Furthermore, in the description of this application and the appended claims, the terms "first," "second," "third," etc., are used only to distinguish descriptions and should not be construed as indicating or implying relative importance.

[0040] References to "one embodiment" or "some embodiments" as described in this specification mean that one or more embodiments of this application include a specific feature, structure, or characteristic described in connection with that embodiment. Therefore, the phrases "in one embodiment," "in some embodiments," "in other embodiments," "in still other embodiments," etc., appearing in different parts of this specification do not necessarily refer to the same embodiment, but rather mean "one or more, but not all, embodiments," unless otherwise specifically emphasized. The terms "comprising," "including," "having," and variations thereof mean "including but not limited to," unless otherwise specifically emphasized.

[0041] like Figure 1As shown, this embodiment provides a deaeration process for boiler feedwater, including 4 slag coolers, 4 boilers, and 2 deaerators. The deaerators further include a deaerator unit. The steps are as follows:

[0042] Medium-pressure steam is added, and after being reduced to low-pressure steam through pipeline A, it is split into two streams and enters deaerator A and deaerator B respectively.

[0043] The condensate enters deaerator A and deaerator B through pipeline B;

[0044] Add demineralized water, which flows through pipeline C. Pipeline C splits into two paths: one path enters deaerator A, and the other path passes through four parallel slag coolers for heat exchange before converging and splitting into two paths: one path flows through pipeline F into deaerator A, and the other path flows through pipeline E into deaerator B.

[0045] The urea condensate is added through a one-way valve connected to the demineralized water pipeline D. After mixing, the mixture enters the low-level heat recovery equipment of the ammonia synthesis unit for heat exchange before being sent out into pipelines F and E.

[0046] A gas-liquid connection is provided between deaerator A and deaerator B. The water processed by deaerator A and deaerator B flows out as boiler feedwater.

[0047] After being heated by the slag cooler, the demineralized water is mixed with the condensate from the urea unit and then sent to the ammonia synthesis unit for heat exchange with the low-temperature gas, raising the temperature to 110°C. It is then sent to the deaerator for oxygen removal.

[0048] This embodiment provides a control system for the deoxygenation process of feedwater in a heating boiler, including:

[0049] Pressure gauges are installed on deaerator A and pipeline A, respectively, and a pressure controller PIC01 for deaerator A is connected to the pressure gauges in communication.

[0050] Pressure gauges are installed in deaerator B and pipeline A respectively, and a pressure controller PIC02 for deaerator B is connected to the pressure gauges in communication.

[0051] Inside deaerator A, at the front end of deaerator A and pipeline F, there are level sensors and a deaerator A level controller LIC01 that is communicatively connected to the level sensors.

[0052] A deaerator B level controller LIC02 is installed on pipeline E.

[0053] Deaerator B is equipped with a liquid level sensor and a deaerator liquid level controller LIC03 that is communicatively connected to the liquid level sensor; the deaerator liquid level controller LIC03 is associated with the deaerator B liquid level controller LI02.

[0054] A flow meter is installed at the front end of pipeline C, and a demineralized water controller FIC001 is connected to the flow meter in communication.

[0055] Four temperature sensors, TI01, TI02, TI03 and TI04, are installed at the rear end of the slag cooler and are connected to the slag cooler temperature controller, TIC001, for communication.

[0056] It also includes a condensate conductivity AI803 installed on pipe B, and a condensate flow controller FIC02 installed at its rear end;

[0057] Temperature sensors TI05 and TI06 are also installed in deaerator A and deaerator B.

[0058] TI05 and TI06 are connected to the system.

[0059] The control system also includes: the over-temperature control of the slag cooler is applied to the demineralized water flow control of pipeline C after the temperature controller of the slag cooler reaches the safety warning setting.

[0060] The control system also includes pressure control of deaerator A and deaerator B at 0.02-0.04 MPa and water temperature ≥100℃.

[0061] The control system includes valves or solenoid valves installed in the pipeline for use in control.

[0062] This application also provides a computer-readable storage medium storing a computer program that, when executed by a processor, performs the following steps:

[0063] The parameters are set, and detailed explanations are provided:

[0064] A TIC001 software control system was added to the PKS operation interface of the boiler feedwater system. The opening degree of FV001 is automatically switched and controlled by TIC001 and FIC001 after "selecting the larger value".

[0065] When the outlet heat exchange temperatures TI01 / 02 / 03 / 04 of the four slag coolers are not high, the SP value of FIC001 is given to control the opening of FV001, and the boiler feedwater is adjusted to meet the boiler's production water needs. When any one of the outlet heat exchange temperatures TI01 / 02 / 03 / 04 of the four slag coolers exceeds 60℃ and the OP value of TIC001 is greater than the OP value of FIC001, the system automatically switches to TIC001 to control the opening of FV001, and the boiler feedwater is adjusted to reduce the heat exchange temperature of the slag cooler. (See the control system block diagram.) Figure 2 The demineralized water, after being heated by the slag cooler, is mixed with the condensate from the urea unit and then sent to the ammonia synthesis unit for heat exchange with the low-temperature gas, raising the temperature to 110°C. It is then sent to the deaerator for oxygen removal.

[0066] I. Operation of FIC001 and TIC001 Control Systems

[0067] 1. A TIC001 software control system was added to the PKS operation interface of the boiler feedwater system. The opening degree of FV001 is automatically switched between TIC001 and FIC001 after "selecting the larger value". When the outlet heat exchange temperatures of the four slag coolers (TI01 / 02 / 03 / 04) are not high, the opening degree of FV001 is controlled by setting the SP value of FIC001, adjusting the boiler feedwater flow to meet the boiler's production water needs. When any one of the outlet heat exchange temperatures of the four slag coolers (TI01 / 02 / 03 / 04) exceeds 60℃ and the OP value of TIC001 is greater than the OP value of FIC001, the system automatically switches to TIC001 to control the opening degree of FV001, adjusting the boiler feedwater flow to reduce the heat exchange temperature of the slag coolers. The block diagram of the control system is as follows. Figure 2 .

[0068] Regulation system logic description:

[0069] (1) SW001 is a module in the PKS backend, always in the "CAS" position. The opening degree of FV001 is automatically switched and controlled by TIC001 and FIC001 after "selecting the larger one".

[0070] (2) When FIC001 is set to “MAN”, the boiler feedwater can be manually adjusted. Its output OP value must be greater than the OP value of TIC001 in order to take effect.

[0071] (3) When FIC001 is set to “AUTO”, its SP can be changed to adjust the boiler feedwater flow rate. Its output value OP must also be greater than the OP value of TIC001 in order to take effect.

[0072] (4) When TIC001 is set to “MAN”, the boiler feedwater can also be manually adjusted, but its output OP value must be greater than the OP value of FIC001 in order to take effect.

[0073] (5) When TIC001 is set to “AUTO”, SP is set to 60°C. The output will only take effect when the PV value of TIC001 exceeds 60°C and the OP value of TIC001 is greater than the OP value of FIC001.

[0074] 2. Operating requirements:

[0075] 1) In principle, TIC001 should be set to "AUTO" control and should not be set to "MAN" arbitrarily. Its SP setting is 60°C and only computer engineers have the authority to modify it.

[0076] 2) Under normal circumstances, FIC001 is set to "AUTO" control.

[0077] 3. After the demineralized water after heat exchange in the slag cooler is mixed with the condensate from the urea unit, it is first sent to the ammonia synthesis unit to exchange heat with the synthetic low-temperature gas, raising the temperature to 110℃, and then sent to the deaerator for oxygen removal.

[0078] This process can, firstly, recover the waste heat from the low-temperature gas transformation of the ammonia synthesis unit, significantly reducing the steam consumption for deaerator heating; secondly, the demineralized water and condensate are very clean, which can avoid problems such as scaling caused by circulating water cooling, while reducing the energy and water consumption of the cooling tower.

[0079] II. Low-grade heat recovery operation:

[0080] Low-grade heat recovery system operation:

[0081] (1) Adjust the relevant liquid level of the deaerator to manual operation and maintain the normal liquid level.

[0082] (2) Adjust the relevant pressure of the deaerator to manual operation and maintain normal pressure.

[0083] (3) Contact the dispatcher to confirm that the ammonia synthesis unit is ready for operation.

[0084] (4) Remove the pressure gauge in front of the demineralized water valve from the low-level heat recovery equipment of the ammonia synthesis unit to the heating unit, and slightly open the demineralized water valve from the heating unit to the low-level heat recovery equipment of the ammonia synthesis unit to send water to the newly added demineralized water pipeline to prevent the deaerator from being not watered enough due to excessive opening and causing the liquid level to fluctuate.

[0085] The high-point exhaust valve at the outlet of the low-level heat recovery equipment of the ammonia synthesis unit is closed after exhausting the steam; the root valve is closed and the pressure gauge is restored after the steam is exhausted at the pressure gauge joint before the demineralized water valve from the low-level heat recovery equipment of the ammonia synthesis unit to the heating unit.

[0086] (5) Fully open the demineralized water valve from the heating unit to the low-level heat recovery equipment of the ammonia synthesis unit, slowly fully open the demineralized water valve from the low-level heat recovery equipment of the ammonia synthesis unit to the heating unit to supply water to the deaerator, and gradually close the shut-off valve from the original cold slag machine outlet demineralized water main to the new and old deaerators. The new deaerator can be deaerator A or deaerator B.

[0087] During the switchover, pay attention to controlling the deaerator liquid level and pressure to prevent the deaerator liquid level from being too low, too high, or overpressured.

[0088] (6) After the switchover is completed, the temperature of the demineralized water in the ammonia synthesis unit is gradually increased to 110°C. During the heating period, monitoring should be strengthened and the pressure and liquid level of the deaerator should be well controlled.

[0089] (7) After the demineralized water temperature at the outlet of the low-temperature heat exchanger rises to normal, the newly added demineralized water pipeline is inspected along the pipeline laying route to confirm whether there are any abnormalities (such as water hammer, air lock, or leakage). If there are any abnormalities, appropriate measures should be taken immediately according to the specific situation.

[0090] Routine maintenance:

[0091] (1) Control the deaerator pressure to 0.02-0.04 MPa and the water temperature to ≥100℃; maintain a stable influent flow rate and ensure normal liquid level.

[0092] (2) In order to prevent the deaerator pressure from fluctuating significantly when the demineralized water or condensate fluctuates, the demineralized water temperature at the outlet of the low-temperature heat exchanger should not exceed 110°C.

[0093] (3) When the temperature of the demineralized water at the outlet of the low-temperature heat recovery equipment of the ammonia synthesis unit fluctuates significantly, the deaerator pressure should be immediately adjusted to manual control. When the deaerator pressure returns to a stable state, it should be gradually switched to automatic control.

[0094] Normal resection:

[0095] (1) Adjust the deaerator level and pressure to manual control to maintain normal level and pressure.

[0096] (2) Contact the dispatcher to confirm that after the synthesis unit cuts off the low heat exchanger, the heating supply should be slowly opened to the shut-off valves of the demineralized water main pipe from the outlet of the original cold slag machine to the new and old deaerators, and the demineralized water supply valve and return valve from the heating unit to the low heat exchanger should be gradually closed.

[0097] (3) Adjust the pressure of the low-pressure steam system, control the pressure and temperature of the deaerator within the normal range, and start it automatically after stabilization.

[0098] Handling abnormal situations:

[0099] (1) When the synthesis unit is shut down or the pipeline and valve of the demineralized water system of the low heat utilization of the ammonia synthesis unit are seriously leaking and need to be repaired, the low heat utilization system of the ammonia synthesis unit shall be shut down in accordance with the normal shutdown operation.

[0100] (2) When the heating unit experiences a complete power outage, acid or alkali leakage of demineralized water, or pipe bursts in the inlet and outlet demineralized water pipelines of the cold slag machine, and it is necessary to reduce or cut off the demineralized water, the demineralized water overflow should be maintained first. Then, the dispatching and fertilizer workshop should be contacted immediately. The demineralized water can only be reduced or cut off after the fertilizer workshop cuts off the low-level heat recovery equipment of the ammonia synthesis unit.

[0101] Urea Compressed Condensate Dosing Operation

[0102] 1. Commissioning Operation:

[0103] (1) After the dispatching notice is given to put the urea compression condensate into use, the amount of demineralized water used is reduced according to the outlet water temperature of the slag cooler, and the amount of condensate used is reduced according to the liquid level of the urea condensate storage tank (FIC02 metering).

[0104] (2) Adjust the pressure of the low-pressure steam system or cut off the 0.8MPa low-pressure steam in a timely manner according to the pressure and temperature of the deaerator. If the pressure of the low-pressure steam pipeline is high, open the drain of the low-pressure steam system to release pressure and avoid overpressure.

[0105] 2. Deaerator makeup water control:

[0106] (1) By limiting the inlet valve of the cold slag machine demineralized water, the demineralized water at the outlet of the cold slag machine of the operating boiler is balanced and the water temperature is controlled at 35-50℃. The amount of demineralized water should be reduced as much as possible under the premise that the demineralized water temperature at the outlet of the cold slag machine does not exceed 50℃.

[0107] (2) When the urea condensate storage tank level exceeds 100%, it will overflow and cause waste. Urea condensate should be used in a timely manner according to the urea condensate storage tank level and changes, and the condensate storage tank level should be controlled between 60% and 90%.

[0108] (4) The liquid levels of deaerator A and deaerator B are stabilized by controlling the liquid level controllers LIC01 and LIC02.

[0109] When the deaerator liquid level is high, the discharge is controlled by controller LIC03. LIC01 and LIC02 are set to manual or automatic control to adjust the urea compressor condensate, and FIC001 is used to adjust the demineralized water volume.

[0110] (5) When the bed pressure rises and the opening of the cold slag machine increases due to reasons such as continuous slag discharge pipe blockage and unblocking, bed pressure reduction, load increase, air volume adjustment and coal quality deterioration, etc., the amount of demineralized water used should be increased in a timely manner according to the demineralized water temperature at the outlet of the cold slag machine.

[0111] 3. Resection procedure

[0112] Upon receiving the dispatch notification to shut down the technical upgrade, promptly increase the amount of condensate and demineralized water used, and adjust the pressure of the low-pressure steam system and the deaerator in a timely manner.

[0113] Over-temperature interlock of slag cooler Figure 3 As shown,

[0114] Interlocking instructions

[0115] a. Interlocking input

[0116] TI01PVHHFL: CO1 Outlet water temperature is too high.

[0117] PB01: Manual click on PB01 interlock

[0118] b. Interlocking output

[0119] HIS123_1: C01 Stop Button

[0120] HIS123_2: C01 Stop Button

[0121] c. Interlocking Operation Description

[0122] (1) When the outlet water temperature TI01 of CO1 reaches the high high alarm, TI01PVHHFL=ON;

[0123] (2) When TI01 reports a high high, PB01 activates, triggering HIS123, and DO points HIS123_1 and HIS123_2 become ON;

[0124] (3) Set the BYPASS parameter of PB01 to ON to bypass the corresponding interlocking conditions, but the button itself cannot be bypassed.

[0125] The above process uses TIC software to perform controllable modifications on specific devices.

[0126] The above-described embodiments are only used to illustrate the technical solutions of this application, and are not intended to limit them. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of this application, and should all be included within the protection scope of this application.

Claims

1. A deaeration process for boiler feedwater, comprising 4 slag coolers, 4 boilers, and 2 deaerators, characterized in that, The steps are as follows: Medium-pressure steam is added, and the pressure is reduced to low-pressure steam through pipeline A. The steam is then divided into two streams and enters deaerator A and deaerator B respectively. The condensate enters deaerator A and deaerator B through pipeline B respectively. Add demineralized water, which flows through pipeline C. Pipeline C splits into two paths: one path enters deaerator A, and the other path flows through four parallel slag coolers for heat exchange before converging and splitting into two paths: one path flows through pipeline F into deaerator A, and the other path flows through pipeline E into deaerator B. Connected in parallel with the four slag coolers is pipeline D. The pipeline containing urea condensate is connected to the one-way valve of pipeline D for mixing and then enters the low-level heat recovery equipment of the ammonia synthesis unit for heat exchange before being sent out into pipelines F and E. A gas-liquid connection is provided between deaerator A and deaerator B. After treatment by deaerator A and deaerator B, the water flows out as boiler feedwater. The demineralized water after heat exchange by the slag cooler is mixed with the condensate from the urea unit and first sent to the ammonia synthesis unit for heat exchange with the low-level shift gas, raising the temperature to 110°C, and then sent to the deaerator for oxygen removal.

2. A control system implementing claim 1, characterized in that, include: Pressure gauges are installed on deaerator A and pipeline A, respectively, and a pressure controller PIC01 for deaerator A is connected to the pressure gauges in communication. Pressure gauges are installed in deaerator B and pipeline A respectively, and a pressure controller PIC02 for deaerator B is connected to the pressure gauges in communication. Inside deaerator A, at the front end of deaerator A and pipeline F, there are level sensors and a deaerator A level controller LIC01 that is communicatively connected to the level sensors. A deaerator B level controller LIC02 is installed on pipeline E. Deaerator B is equipped with a liquid level sensor and a deaerator liquid level controller LIC03 that is communicatively connected to the liquid level sensor; the deaerator liquid level controller LIC03 is associated with the deaerator B liquid level controller LI02. A flow meter is installed at the front end of pipeline C, and a demineralized water controller FIC001 is connected to the flow meter in communication. Four temperature sensors, TI01, TI02, TI03 and TI04, are installed at the rear end of the slag cooler and are connected to the slag cooler temperature controller, TIC001, for communication. It also includes a condensate conductivity AI803 installed on pipe B, and a condensate flow controller FIC02 installed at its rear end; Temperature sensors TI05 and TI06 are also installed in deaerator A and deaerator B. TI05 and TI06 are connected to the system.

3. The control system according to claim 2, characterized in that, Also includes: The over-temperature control of the slag cooler is applied to the demineralized water flow control in pipeline C after the temperature controller of the slag cooler reaches the safety warning setting.

4. The control system according to claim 2, characterized in that, It also includes controlling the pressure of deaerator A and deaerator B at 0.02-0.04 MPa and the water temperature at ≥100℃.

5. The control system according to claim 2, characterized in that, This includes valves or solenoid valves installed in pipelines for control purposes.

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