A control method for DCS system of titanium sponge production

Abstract

The present invention discloses a control method of a DCS system for sponge titanium production, which relates to the technical field of sponge titanium production, including a horizontal tank, a reactor and a control computer. A high-level tank is installed on the right side of the horizontal tank through a pipeline, and a feeding pump and a feeding valve are installed in sequence between the horizontal tank and the high-level tank, and one side of the high-level tank is connected to an automatic feeding system through a pipeline. The control method of the DCS system for sponge titanium production mainly includes automatic control of the reduction process, automatic control of the distillation process, and automatic control of the cooling process; the reduction process can realize automatic feeding, automatic filling and discharge of argon gas, furnace temperature detection feedback and automatic control of the cooling fan and valve opening; the distillation process can realize automatic control of the water level and water volume of the cold end reactor, automatic opening of the vacuum system, automatic cleaning of the aisle pipe, and temperature setting and required time of each stage of distillation; the cooling process can realize automatic argon filling protection, automatic introduction of indirect water and direct water cooling, and automatic water discharge after cooling.

Description

Technical Field

[0001] The invention relates to the technical field of titanium sponge production, and in particular to a control method for a titanium sponge production DCS system. Background Art

[0002] Sponge titanium is a sponge-like titanium produced by metal thermal reduction, and is the main raw material for making industrial titanium alloys. Sponge titanium production is the basic link of the titanium industry, and it is the raw material for titanium materials, titanium powder and other titanium components. Turn ilmenite into titanium tetrachloride, then put it in a sealed stainless steel tank, fill it with argon gas, and react with magnesium metal to get "sponge titanium".

[0003] At present, all links of titanium sponge production are manually observed and operated, resulting in uneven and unstable temperature control during reduction. The distillation process uses manual control to open each vacuum pump in the vacuum system, resulting in high labor intensity. At the same time, the manual observation data has large observation errors and poor timeliness, which can easily affect the quality of titanium sponge products. For this reason, we propose a control method for the DCS system of titanium sponge production. Summary of the invention

[0004] In view of the deficiencies in the prior art, the present invention provides a control method for a DCS system for sponge titanium production, which solves the problems raised in the above background technology that all links in the current sponge titanium production are manually observed and operated, resulting in uneven and unstable temperature control during reduction, and the distillation process adopts manual control to open each vacuum pump in the vacuum system, resulting in high labor intensity for personnel. At the same time, the manual observation data has large observation errors and poor timeliness of observation, which can easily affect the quality of sponge titanium products.

[0005] To achieve the above objectives, the present invention is implemented through the following technical solutions: a control method for a DCS system for sponge titanium production, comprising a horizontal tank, a reactor and a control computer, a high-level tank is installed on the right side of the horizontal tank through a pipeline, and a feeding pump and a feeding valve are installed in sequence between the horizontal tank and the high-level tank, one side of the high-level tank is connected to an automatic feeding system through a pipeline, and a feeding valve is installed between the high-level tank and the automatic feeding system, the reactor is placed on one side of the automatic feeding system through a pipeline, and a feeding valve is installed between the automatic feeding system and the reactor, a reduction thermocouple and a cooling fan are arranged on the left side of the reactor used for the reduction stage, and an air inlet valve is installed between the cooling fan and the reactor, a pressure transmitter is arranged on the right side of the reactor used for the reduction stage, and the control computer is electrically connected to one end of the feeding pump.

[0006] Optionally, a cold end reactor is installed on one side of the reactor used in the distillation stage through a pipeline, and a water outlet valve and a water inlet valve are respectively installed on the outside of the cold end reactor, a distillation thermocouple and an automatic aisle cleaning device are installed on the left side of the reactor used in the distillation stage, a main control valve is installed on the right side of the reactor used in the distillation stage, and a vacuum unit is installed on one side of the main control valve through a sub-control valve.

[0007] Optionally, an automatic argon flushing system is installed on one side of the reactor used in the cooling stage through a pipeline, and a cooling argon filling valve is arranged between the automatic argon flushing system and the reactor, a water drain valve is installed on the left side of the reactor used in the cooling stage, and an indirect water valve and a direct water valve are respectively installed on the right side of the reactor used in the cooling stage.

[0008] Optionally, the control method comprises the following stages:

[0009] A. Reduction stage;

[0010] B. Distillation stage;

[0011] C. Cooling stage.

[0012] Optionally, the A, reduction stage includes the following specific steps:

[0013] A1. During the reduction process, the liquid level in the high-level tank can be automatically transmitted to the control computer. When the high-level tank needs to be replenished with raw materials, the operator can automatically open the material pump and material valve through the control computer to replenish the raw materials from the horizontal tank to the high-level tank;

[0014] A2. The raw materials in the high-level tank are transferred to the automatic feeding system through the feeding valve, and the automatic feeding system adds the raw materials into the reactor through the feeding valve; before the reduction feeding, the material speed of each stage of reduction is input through the control computer, and the automatic feeding system operates normally after the feeding starts. The automatic feeding system can accumulate the total feeding amount and display the current material speed. When each reduction stage ends, the feeding valve is automatically closed, and the next stage of feeding is carried out after the magnesium chloride is discharged;

[0015] A3. The reduction thermocouple can measure the temperature of each section of the reactor and automatically feed it back to the control computer. When the reduction temperature is higher than the set upper limit, the cooling fan and the air inlet valve are automatically started to cool the reactor. As the temperature decreases, the cooling fan frequency is automatically adjusted. When the temperature reaches the lower limit, the air inlet valve is automatically closed. During the reduction process, the pressure in the reactor can be transmitted to the control computer through the pressure transmitter, and it can be automatically deflated when the pressure is higher than the upper limit.

[0016] Optionally, the B, distillation stage comprises the following specific steps:

[0017] B1. During the distillation process, the volatiles are transferred from the reactor to the cold end reactor. The cold end reactor has an automatic water inlet valve and a water outlet valve. When the water level of the cold end reactor needs to be raised or lowered, the control computer can automatically open the water inlet valve and automatically adjust the opening angle of the water outlet valve.

[0018] B2. The time and temperature required for each stage of distillation can be input through the control computer, and the distillation thermocouple can feedback the current temperature data in real time; the vacuum pump required for each stage of distillation can be input through the control computer, and the vacuum unit and the main control valve and sub-control valve can automatically switch the vacuum pump according to the set time, and automatically switch the vacuum pump and the corresponding control valve when the time is up;

[0019] B3. During distillation, the cleaning interval of the automatic aisle cleaning device is input into the control computer, and the automatic aisle cleaning device automatically cleans the aisle to ensure the smooth progress of the distillation process.

[0020] Optionally, the C. cooling stage includes the following specific steps:

[0021] C1. During the cooling process, when the pressure in the reactor is lower than the lower limit, the automatic argon flushing system automatically replenishes argon gas to the cooling reactor. When the pressure reaches the upper limit, the cooling argon filling valve automatically closes and stops the pressure replenishment.

[0022] C2. During the cooling period, the opening time of the indirect water valve and the direct water valve is set by the control computer, and water is automatically passed to cool the reactor. When the cooling is completed, the drain valve automatically opens and the water inlet valve automatically closes to complete the cooling process.

[0023] Optionally, during the reduction stage, the control computer is used to set the reactor tank pressure range to 0.005-0.025 MPa, the tube pressure to 0.25-0.05 MPa, and the temperature range of the reduction observation point in the reactor to 750-850°C.

[0024] Optionally, during the distillation stage, the temperature of each section of the reactor is set at 950-970° C. by a control computer.

[0025] Optionally, during the cooling stage, the pressure in the reactor is set to a range of 0.03-0.05 MPa by a control computer.

[0026] The present invention provides a control method for a DCS system for titanium sponge production, which has the following beneficial effects:

[0027] The control method of the DCS system for sponge titanium production, the DCS control system, mainly includes automatic control of the reduction process, automatic control of the distillation process, and automatic control of the cooling process; the reduction process can realize automatic feeding, automatic filling and discharge of argon, furnace temperature detection feedback and automatic control of the cooling fan and valve opening; the distillation process can realize automatic control of the water level and water volume of the cold end reactor, automatic opening of the vacuum system, automatic cleaning of the aisle pipe, temperature setting and required time of each stage of distillation; the cooling process can realize automatic argon filling protection, automatic introduction of indirect water and direct water cooling, and automatic water discharge after cooling; it solves the problems that the current sponge titanium production process is all manual operation and manual measurement, the operation process is prone to deviation, and lack of precision.

[0028] The control method of the DCS system for sponge titanium production further improves the degree of automation in the sponge titanium production process and gradually reduces the intensity of manual labor. The DCS control system for sponge titanium production includes automatic feeding of high-level tanks, automatic feeding during reduction, automatic control of reduction ventilation and cooling, automatic monitoring of the liquid level in the reduction reactor, automatic weighing of magnesium chloride emissions, automatic control of reduction tank pressure and pipe pressure, automatic unblocking of distillation channels during distillation, automatic control of cooling water valves during distillation, automatic water cooling during product cooling, and automatic collection of electricity in each section of the resistance furnace.

[0029] The control method of the DCS system for sponge titanium production is as follows: during operation, multiple resistance furnaces at the operation station are controlled by one computer; during reduction, the material speed of each stage of the reduction of multiple materials, the feeding amount of each stage, the temperature control range of each stage, and the total feeding amount of this batch of sponge titanium are input at one time, and the high-level tank is first automatically replenished from the horizontal tank to ensure the production of this batch of sponge titanium; then, the valves of each feeding pipeline are automatically opened to realize automatic feeding, and when the temperature during reduction reaches the upper temperature limit input in this stage, the ventilation blind plate is automatically opened, and the fan valve is automatically opened to realize automatic control of frequency air supply; during distillation, the various stages of distillation and the controlled temperature, the opening time of the vacuum pump at each stage, and the water level and the opening amount of the water inlet valve corresponding to the condensate temperature are first input; during the cooling period after the product distillation is finished, indirect water and direct water are automatically introduced, the water is automatically discharged after the cooling is finished, and argon gas is automatically protected during the cooling period; while the above operations are automatically performed, each operation signal is fed back to the control computer of the operation station in real time, so that the control personnel of the operation station can grasp the current situation in time, and when an abnormal situation occurs, each node can timely alarm to remind the control personnel. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 This is a system control schematic diagram of a control method for a DCS system for sponge titanium production according to the present invention.

[0031] In the figure: 1. horizontal tank; 2. charging pump; 3. charging valve; 4. high-level tank; 5. charging valve; 6. automatic charging system; 7. feeding valve; 8. reduction thermocouple; 9. cooling fan; 10. air inlet valve; 11. reactor; 12. pressure transmitter; 13. water outlet valve; 14. cold end reactor; 15. water inlet valve; 16. distillation thermocouple; 17. automatic aisle cleaning device; 18. main control valve; 19. sub-control valve; 20. vacuum unit; 21. automatic argon flushing system; 22. cooling and argon filling valve; 23. indirect water valve; 24. direct water valve; 25. drain valve; 26. control computer. DETAILED DESCRIPTION

[0032] See also Figure 1 The present invention provides a technical solution: a control method for a DCS system for sponge titanium production, a control method for a DCS system for sponge titanium production, comprising a horizontal tank 1, a reactor 11 and a control computer 26, a high-level tank 4 is installed on the right side of the horizontal tank 1 through a pipeline, and a feeding pump 2 and a feeding valve 3 are installed in sequence between the horizontal tank 1 and the high-level tank 4, one side of the high-level tank 4 is connected to an automatic feeding system 6 through a pipeline, and a feeding valve 5 is installed between the high-level tank 4 and the automatic feeding system 6, the reactor 11 is arranged on one side of the automatic feeding system 6 through a pipeline, and a feeding valve 7 is installed between the automatic feeding system 6 and the reactor 11, a reduction thermocouple 8 and a cooling fan 9 are arranged on the left side of the reactor 11 used for the reduction stage, and an air inlet valve 10 is installed between the cooling fan 9 and the reactor 11, a pressure transmitter 12 is arranged on the right side of the reactor 11 used for the reduction stage, and the control computer 26 is electrically connected to one end of the feeding pump 2. A cold end reactor 14 is installed on one side of the reactor 11 used in the distillation stage through a pipeline, and a water outlet valve 13 and a water inlet valve 15 are installed on the outside of the cold end reactor 14, a distillation thermocouple 16 and an automatic aisle cleaning device 17 are installed on the left side of the reactor 11 used in the distillation stage, a main control valve 18 is installed on the right side of the reactor 11 used in the distillation stage, and a vacuum unit 20 is installed on one side of the main control valve 18 through a sub-control valve 19. An automatic argon flushing system 21 is installed on one side of the reactor 11 used in the cooling stage through a pipeline, and a cooling argon filling valve 22 is arranged between the automatic argon flushing system 21 and the reactor 11, a water drain valve 25 is installed on the left side of the reactor 11 used in the cooling stage, and an indirect water valve 23 and a direct water valve 24 are installed on the right side of the reactor 11 used in the cooling stage.

[0033] The control method includes the following stages:

[0034] A. Reduction stage;

[0035] B. Distillation stage;

[0036] C. Cooling stage.

[0037] A. The restoration phase includes the following specific steps:

[0038] A1. During the reduction process, the liquid level in the high-level tank 4 can be automatically transmitted to the control computer 26. When the high-level tank 4 needs to be replenished with raw materials, the operator can automatically start the feeding pump 2 and the feeding valve 3 through the control computer 26 to replenish the raw materials from the horizontal tank 1 to the high-level tank 4;

[0039] A2, the raw materials in the header tank 4 are transferred to the automatic feeding system 6 through the feeding valve 5, and the automatic feeding system 6 adds the raw materials to the reactor 11 through the feeding valve 7; the material rate of each stage of reduction is input through the control computer 26 before the reduction feeding, and the automatic feeding system 6 operates normally after the feeding starts. The automatic feeding system 6 can accumulate the total feeding amount, display the current material rate, and when each reduction stage ends, the feeding valve 7 is automatically closed, and the next stage of feeding is carried out after the magnesium chloride is discharged;

[0040] A3. The reduction thermocouple 8 can measure the temperature of each section of the reactor 11 and automatically feed back to the control computer 26. When the reduction temperature is higher than the set upper limit, the cooling fan 9 and the air inlet valve 10 are automatically started to cool the reactor 11. As the temperature decreases, the frequency of the cooling fan 9 is automatically adjusted. When the temperature reaches the lower limit, the air inlet valve 10 is automatically closed. During the reduction process, the pressure in the reactor 11 can be transmitted to the control computer 26 through the pressure transmitter 12, and can be automatically deflated when the pressure is higher than the upper limit.

[0041] During the reduction stage, the control computer 26 sets the tank pressure range of the reactor 11 to 0.005-0.025 MPa, the tube pressure to 0.25-0.05 MPa, and the temperature range of the reduction observation point in the reactor 11 to 750-850°C.

[0042] B. The distillation stage includes the following specific steps:

[0043] B1, distillation process, volatiles are transferred from the reactor 11 to the cold end reactor 14, the cold end reactor 14 has an automatic water inlet valve 15 and a water outlet valve 13, when the cold end reactor 14 needs to raise or lower the water level, the control computer 26 can automatically open the water inlet valve 15 and automatically adjust the opening angle of the water outlet valve 13;

[0044] B2. The time and temperature required for each stage of distillation can be input through the control computer 26, and the distillation thermocouple 16 can feedback the current temperature data in real time; the vacuum pump required for each stage of distillation can be input through the control computer 26, and the vacuum unit 20 and the main control valve 18 and the sub-control valve 19 can automatically switch the vacuum pump according to the set time, and automatically switch the vacuum pump and the corresponding control valve after the time is up;

[0045] B3. During distillation, the cleaning interval of the automatic aisle cleaning device 17 is input through the control computer 26, and the automatic aisle cleaning device 17 automatically cleans the aisle to ensure that the distillation process proceeds smoothly.

[0046] During the distillation stage, the temperature of each section of the reactor 11 is set at 950-970°C by the control computer 26.

[0047] C. The cooling stage includes the following specific steps:

[0048] C1, cooling process, when the pressure in the reactor 11 is lower than the lower limit, the automatic argon flushing system 21 automatically replenishes argon gas to the cooling reactor 11, and when the pressure reaches the upper limit, the cooling argon filling valve 22 is automatically closed to stop the pressure replenishment;

[0049] C2. During the cooling period, the opening time of the indirect water valve 23 and the direct water valve 24 are set by the control computer 26, and water is automatically passed to cool the reactor 11. When the cooling is completed, the drain valve 25 automatically opens and the water inlet valve 15 automatically closes to complete the cooling process.

[0050] During the cooling stage, the pressure in the reactor 11 is set to a range of 0.03-0.05 MPa by the control computer 26 .

[0051] In summary, the control method of the titanium sponge production DCS system includes the following specific steps when used:

[0052] A. Restoration phase

[0053] A1. During the reduction process, the liquid level in the high-level tank 4 can be automatically transmitted to the control computer 26. When the high-level tank 4 needs to be supplemented with raw materials, the operator can automatically start the feeding pump 2 and the feeding valve 3 through the control computer 26 to supplement the raw materials from the horizontal tank 1 to the high-level tank 4. The high-level tank 4 is automatically supplemented with 26 tons of raw materials through the control computer 26, and the feeding valve 3 is closed after the liquid level is reached;

[0054] A2, the raw materials in the header tank 4 are transferred to the automatic feeding system 6 through the feeding valve 5, and the automatic feeding system 6 adds the raw materials to the reactor 11 through the feeding valve 7; the material rate of each stage of reduction is input through the control computer 26 before the reduction feeding, and the automatic feeding system 6 operates normally after the feeding starts. The automatic feeding system 6 can accumulate the total feeding amount, display the current material rate, and when each reduction stage ends, the feeding valve 7 is automatically closed, and the next stage of feeding is carried out after the magnesium chloride is discharged;

[0055] A3, the reduction thermocouple 8 can measure the temperature of each section of the reactor 11 and automatically feed back to the control computer 26. The control computer 26 sets the temperature range of the reduction observation point in the reactor 11 to 750-850°C. When the reduction temperature is higher than the set upper limit, the cooling fan 9 and the air inlet valve 10 are automatically started to cool the reactor 11. As the temperature decreases, the frequency of the cooling fan 9 is automatically adjusted. When the temperature reaches the lower limit, the air inlet valve 10 is automatically closed; during the reduction process, the pressure in the reactor 11 can be transmitted to the control computer 26 through the pressure transmitter 12. The control computer 26 sets the tank pressure range of the reactor 11 to 0.005-0.025Mpa and the pipe pressure to 0.25-0.05Mpa. When the pressure is higher than the upper limit, it can be automatically deflated;

[0056] B. Distillation stage

[0057] B1, during the distillation process, the volatiles are transferred from the reactor 11 to the cold end reactor 14. The cold end reactor 14 has an automatic water inlet valve 15 and a water outlet valve 13. When the water level of the cold end reactor 14 needs to be raised or lowered, the water inlet valve 15 can be automatically opened by the control computer 26, and the opening angle of the water outlet valve 13 can be automatically adjusted. During the distillation, the cold end reactor 14 is set to use the 2# water level. When the temperature is abnormal, it is adjusted to the 1# water level by the control computer 26;

[0058] B2. The time and temperature required for each stage of distillation can be input through the control computer 26. The temperature of each section of the reactor 11 is set to 950-970°C through the control computer 26, and the distillation thermocouple 16 can feedback the current temperature data in real time; the vacuum pump required for each stage of distillation can be input through the control computer 26, and the 1# vacuum pump is set to be used from the start of distillation to 12 hours, the 2# vacuum pump is used from 13 to 33 hours, and the 3# and 4# vacuum pumps are used after 35 hours. The vacuum unit 20 and the main control valve 18 and the sub-control valve 19 can automatically switch the vacuum pump according to the set time, and automatically switch the vacuum pump and the corresponding control valve after the time is up;

[0059] B3, during distillation, the cleaning interval of the automatic aisle cleaning device 17 is input through the control computer 26, and the automatic aisle cleaning device 17 automatically cleans the aisle to ensure that the distillation process proceeds smoothly;

[0060] C. Cooling stage

[0061] C1, cooling process, the pressure range of the reactor 11 is set to 0.03-0.05Mpa by the control computer 26, when the pressure in the reactor 11 is lower than the lower limit, the automatic argon flushing system 21 opens the cooling argon filling valve 22 to automatically replenish argon gas to the cooling reactor 11, when the pressure reaches the upper limit of 0.05Mpa, the cooling argon filling valve 22 is automatically closed to stop the pressure replenishment;

[0062] C2. During the cooling period, the opening time of the indirect water valve 23 and the direct water valve 24 are set by the control computer 26, and water is automatically passed to cool the reactor 11. Indirect water cooling is used for 1-20 hours, and the indirect water valve 23 is opened. Direct water cooling is used for 20-60 hours, and the direct water valve 24 is opened. When the cooling is completed, the drain valve 25 is automatically opened, and the water inlet valve 15 is automatically closed to complete the cooling process.

Claims

1. A control method for a DCS system for titanium sponge production, characterized in that: The invention comprises a horizontal tank (1), a reactor (11) and a control computer (26); a high-level tank (4) is installed on the right side of the horizontal tank (1) via a pipeline, and a feeding pump (2) and a feeding valve (3) are installed in sequence between the horizontal tank (1) and the high-level tank (4); one side of the high-level tank (4) is connected to an automatic feeding system (6) via a pipeline, and a feeding valve (5) is installed between the high-level tank (4) and the automatic feeding system (6); the reactor (11) is placed on the automatic feeding system via a pipeline. (6), and a feed valve (7) is installed between the automatic feeding system (6) and the reactor (11), a reduction thermocouple (8) and a cooling fan (9) are arranged on the left side of the reactor (11) used in the reduction stage, and an air inlet valve (10) is installed between the cooling fan (9) and the reactor (11), a pressure transmitter (12) is arranged on the right side of the reactor (11) used in the reduction stage, and the control computer (26) is electrically connected to one end of the feed pump (2); A cold end reactor (14) is installed on one side of the reactor (11) used in the distillation stage through a pipeline, and a water outlet valve (13) and a water inlet valve (15) are installed on the outside of the cold end reactor (14), a distillation thermocouple (16) and an automatic aisle cleaning device (17) are installed on the left side of the reactor (11) used in the distillation stage, and a main control valve (18) is installed on the right side of the reactor (11) used in the distillation stage, and a vacuum unit (20) is installed on one side of the main control valve (18) through a sub-control valve (19); An automatic argon flushing system (21) is installed on one side of the reactor (11) used in the cooling stage through a pipeline, and a cooling argon filling valve (22) is arranged between the automatic argon flushing system (21) and the reactor (11), a water discharge valve (25) is installed on the left side of the reactor (11) used in the cooling stage, and an indirect water valve (23) and a direct water valve (24) are respectively installed on the right side of the reactor (11) used in the cooling stage; The control method comprises the following stages: A. Reduction phase; B. Distillation stage; C. Cooling stage; The A. reduction phase includes the following specific steps: A1. During the reduction process, the liquid level in the high-level tank (4) can be automatically transmitted to the control computer (26). When the high-level tank (4) needs to be replenished with raw materials, the operator can automatically start the material pump (2) and the material valve (3) through the control computer (26) to replenish the raw materials from the horizontal tank (1) to the high-level tank (4); A2. The raw materials in the high-level tank (4) are transferred to the automatic feeding system (6) through the feeding valve (5), and the automatic feeding system (6) feeds the raw materials into the reactor (11) through the feeding valve (7); before the reduction feeding, the material rate of each reduction stage is input through the control computer (26), and after the feeding starts, the automatic feeding system (6) operates normally. The automatic feeding system (6) can accumulate the total feeding amount and display the current material rate. When each reduction stage ends, the feeding valve (7) is automatically closed, and the magnesium chloride is discharged and then the next stage of feeding is carried out; A3. The reduction thermocouple (8) can measure the temperature of each section of the reactor (11) and automatically feed back to the control computer (26). When the reduction temperature is higher than the set upper limit, the cooling fan (9) and the air inlet valve (10) are automatically started to cool the reactor (11). As the temperature decreases, the frequency of the cooling fan (9) is automatically adjusted. When the temperature reaches the lower limit, the air inlet valve (10) is automatically closed. During the reduction process, the pressure in the reactor (11) can be transmitted to the control computer (26) through the pressure transmitter (12). When the pressure is higher than the upper limit, it can be automatically deflated. The B. distillation stage includes the following specific steps: B1. During the distillation process, the volatiles are transferred from the reactor (11) to the cold end reactor (14). The cold end reactor (14) has an automatic water inlet valve (15) and a water outlet valve (13). When the water level of the cold end reactor (14) needs to be raised or lowered, the water inlet valve (15) is automatically opened and the opening angle of the water outlet valve (13) is automatically adjusted by the control computer (26); B2. The time and temperature required for each stage of distillation can be input through the control computer (26), and the distillation thermocouple (16) can provide real-time feedback of current temperature data; the vacuum pump required for each stage of distillation can be input through the control computer (26), and the vacuum unit (20) and the main control valve (18) and the sub-control valve (19) can automatically switch the vacuum pump according to the set time, and automatically switch the vacuum pump and the corresponding control valve when the time is up; B3. During distillation, the automatic aisle cleaning device (17) is input through the control computer (26) to clean the interval time, and the automatic aisle cleaning device (17) automatically cleans the aisle to ensure the smooth distillation process; The C. cooling stage includes the following specific steps: C1. During the cooling process, when the pressure in the reactor (11) is lower than the lower limit, the automatic argon flushing system (21) automatically replenishes argon gas to the cooling reactor (11). When the pressure reaches the upper limit, the cooling argon filling valve (22) automatically closes to stop the pressure replenishment; C2. During the cooling period, the opening time of the indirect water valve (23) and the direct water valve (24) is set by the control computer (26), and water is automatically passed to cool the reactor (11). When the cooling is completed, the drain valve (25) automatically opens and the water inlet valve (15) automatically closes, completing the cooling process.

2. The control method of a DCS system for titanium sponge production according to claim 1, characterized in that: During the reduction stage, the control computer (26) sets the tank pressure range of the reactor (11) to 0.005-0.025 MPa, the tube pressure to 0.25-0.05 MPa, and the temperature range of the reduction observation point in the reactor (11) to 750-850°C.

3. The control method of a DCS system for titanium sponge production according to claim 1, characterized in that: During the distillation stage, the temperature of each section of the reactor (11) is set to 950-970°C by the control computer (26).

4. The control method of a DCS system for titanium sponge production according to claim 1, characterized in that: During the cooling stage, the pressure in the reactor (11) is set to a range of 0.03-0.05 MPa by means of a control computer (26).

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