Automatic triisopropyl silane coarse steaming system and control method thereof

Abstract

The invention discloses an automatic triisopropyl silane coarse steaming system and a control method thereof, and particularly relates to the technical field of triisopropyl silane extraction, the system comprises a reaction liquid storage tank, a coarse steaming kettle, a crude product storage tank, a coarse steaming tower, a condensation unit, a reflux ratio regulator, a front fraction receiving tank, a solvent receiving tank and a vacuum unit; the method comprises the following steps: (1) feeding; (2) receiving a front fraction; (3) solvent receiving; and (4) collecting a crude product. The triisopropyl silane automatic coarse steaming system and the control method thereof have the beneficial effects that one-key starting of the system is achieved, personnel operation is not needed in the field operation state, the frequency of personnel operation of triisopropyl silane coarse steaming is reduced, and the production cost is reduced; the process operation automation is realized, the continuous and stable execution can be realized, the qualified triisopropyl silane crude product is produced, and the workload of a subsequent rectification system is reduced.

Description

Technical Field

[0001] The patent of this invention relates to the technical field of extracting triisopropylsilane, and specifically to an automated crude distillation system for triisopropylsilane and a control method thereof. Background Art

[0002] Triisopropylsilane is a chemical intermediate that can be used to synthesize sterically hindered organosilicon protective agents, prepare special organosilicon materials and organic synthesis. It is an excellent hydrogen proton donor and is used in many reduction reactions. The current patent with publication number CN103204869B discloses a method for synthesizing high-purity triisopropylsilane, which discloses the use of magnesium, solvent, 2-chloropropane, methylcyclohexane and trichlorosilane as raw materials for reaction, and then obtains triisopropylsilane by vacuum distillation; currently, vacuum distillation generally includes crude distillation and rectification, wherein crude distillation is manually controlled, so there is an instability in the control process, large fluctuations, increasing the workload of the rectification system, and ultimately affecting the output and quality of the product. Summary of the invention

[0003] The object of the present invention is to provide a triisopropylsilane automated crude steaming system and a control method thereof, which realizes process operation automation and reduces production costs.

[0004] The first object of the present invention is implemented by the following technical scheme: an automated crude distillation system for triisopropylsilane, comprising a reaction liquid storage tank, a crude distillation kettle, a crude product storage tank, a crude distillation tower, a condensing unit, a reflux ratio regulator, a fore fraction receiving tank, a solvent receiving tank and a vacuum unit; the liquid outlet of the reaction liquid storage tank is connected to the liquid inlet of the crude distillation kettle through a feed pipe, and a transfer pump and a feed valve are sequentially arranged on the feed pipe; the liquid outlet of the crude distillation kettle is connected to the feed inlet of the crude product storage tank through a discharge pipe, and a discharge valve and a crude product discharge pump are sequentially arranged on the discharge pipe; a first liquid level sensor is arranged in the crude distillation kettle; and a liquid level sensor is arranged above the crude distillation kettle. The crude distillation tower is characterized in that the top air outlet of the crude distillation tower is communicated with the air inlet of the condensing unit, and the air outlet of the condensing unit is communicated with the air inlet of the vacuum unit; a temperature sensor is arranged at the top of the crude distillation tower, and a pressure sensor is arranged in the crude distillation tower; the condensate outlet of the condensing unit is communicated with the liquid inlet of the reflux ratio regulator, and the two liquid outlets of the reflux ratio regulator are respectively communicated with the liquid inlet above the crude distillation tower and the liquid inlet end of the liquid outlet main pipe; the liquid outlet end of the liquid outlet main pipe is respectively communicated with the liquid inlets of the fore fraction receiving tank and the solvent receiving tank; a moisture sensor is arranged on the liquid outlet main pipe; A fore fraction inlet valve is arranged at the liquid inlet of the tank; a solvent inlet valve is arranged at the liquid inlet of the solvent receiving tank; the top gas outlets of the fore fraction receiving tank and the solvent receiving tank are both connected to the gas inlet of the vacuum unit; a fore fraction gas outlet valve is arranged at the gas outlet of the fore fraction receiving tank; a solvent gas outlet valve is arranged at the gas outlet of the solvent receiving tank; the gas outlet end of the steam pipeline is connected to the gas inlet of the jacket of the crude steam kettle; a steam shut-off valve is arranged at the gas inlet of the jacket; the water outlet end of the circulating water pipeline is connected to the water inlet of the jacket of the crude steam kettle; a circulating water shut-off valve is arranged at the water inlet of the jacket; the gas outlet end of the nitrogen pipeline The controller is connected to the air inlet of the crude steam kettle, and a nitrogen cut-off valve is arranged at the air inlet of the crude steam kettle; the signal output ends of the first liquid level sensor, the temperature sensor, the pressure sensor and the moisture sensor are all connected to the signal input end of the controller through signals; the signal output end of the controller is respectively connected to the signal input ends of the transfer pump, the feed valve, the discharge valve, the crude product discharge pump, the vacuum unit, the reflux ratio regulator, the fore fraction inlet valve, the solvent inlet valve, the fore fraction outlet valve, the solvent outlet valve, the steam cut-off valve, the circulating water cut-off valve and the nitrogen cut-off valve through signals.

[0005] Furthermore, a second liquid level sensor is provided in the reaction liquid storage tank, and a signal output end of the second liquid level sensor is connected to a signal input end of the controller via a signal.

[0006] Furthermore, it also includes a solvent storage tank, the liquid outlet of the solvent receiving tank is connected to the liquid inlet of the solvent storage tank through a pipeline, and a liquid outlet pump is arranged on the pipeline between the solvent receiving tank and the solvent storage tank; a third liquid level sensor is arranged in the solvent receiving tank, the signal output end of the third liquid level sensor is connected to the signal input end of the controller through a signal, and the signal output end of the controller is connected to the signal input end of the liquid outlet pump through a signal.

[0007] Furthermore, the vacuum unit is a Roots vacuum unit.

[0008] Furthermore, the condensing unit includes a water cooler and a salt cooler, the air outlet of the crude distillation tower is connected to the air inlet of the water cooler, the air outlet of the water cooler is connected to the air inlet of the salt cooler, the air outlet of the salt cooler is connected to the air inlet of the vacuum unit, and the condensate outlets of the water cooler and the salt cooler are both connected to the liquid inlet of the reflux ratio regulator.

[0009] The second objective of the present invention is implemented by the following technical solution: a control method for an automated crude distillation system of triisopropylsilane, comprising the following steps: (1) Feeding: One-button start, the feed pump starts running, and the feed valve opens at the same time, and the reaction liquid enters the crude steam kettle. When the liquid level in the crude steam kettle reaches the upper limit, the controller controls the feed pump and the feed valve to close; (2) Receiving the fore fraction: After completing step (1), the controller controls the vacuum unit to start and opens the steam shut-off valve at the same time. When the temperature at the top of the crude distillation tower rises to 75°C and the internal pressure is less than -0.09 MPa, the reflux ratio regulator is controlled to open, and all the condensate condensed by the condensing unit is refluxed into the crude distillation tower. The reflux time is 1.5-3.5 hours. Thereafter, the reflux ratio regulator is controlled to adjust the reflux ratio of the condensate refluxed to the crude distillation tower and the condensate taken out to the fore fraction receiving tank to 20:1. At the same time, the fore fraction inlet valve and the fore fraction outlet valve are opened; (3) Solvent receiving: When the water content of the liquid produced in step (2) is less than 600 PPM, the controller controls the front fraction inlet valve and the front fraction outlet valve to be closed, and simultaneously opens the solvent inlet valve and the solvent outlet valve, and controls the reflux ratio regulator to adjust the reflux ratio of the condensate refluxed to the crude distillation tower and produced into the solvent receiving tank to 10:8; (4) Crude product collection: When the temperature of the crude distillation tower top in step (3) rises to 85°C, the controller controls the solvent inlet valve and the solvent outlet valve to be closed, and controls the reflux ratio regulator to be adjusted, so that all the condensate flows back into the crude distillation tower, and controls the steam shut-off valve to be closed, opens the circulating water shut-off valve, and introduces cooling water for cooling. When the temperature in the crude distillation tower drops to below 50°C, the controller controls the vacuum unit and the reflux ratio regulator to be closed, and opens the nitrogen shut-off valve to pressurize the crude distillation kettle to normal pressure, and then closes the nitrogen shut-off valve. Then, the discharge valve is controlled to be opened, and the crude product discharge pump is operated to transport the crude product in the crude distillation kettle to the crude product storage tank. After the crude product in the crude distillation kettle is discharged, the discharge valve and the crude product discharge pump are controlled to be closed.

[0010] Furthermore, step (1) also includes that when the liquid level in the reaction liquid storage tank reaches a lower limit value, the controller controls the material transfer pump and the feed valve to close.

[0011] Furthermore, step (3) also includes that when the liquid level in the solvent receiving tank reaches an upper limit value, the controller controls the liquid outlet pump to start, and transports the solvent in the solvent receiving tank to the solvent storage tank; when the liquid level in the solvent receiving tank reaches a lower limit value, the controller controls the liquid outlet pump to close.

[0012] Advantages of the present invention: 1. The present invention provides an automated crude steaming system for triisopropylsilane, which realizes one-key system start-up and does not require human operation during on-site operation, thereby reducing the frequency of human operation for crude steaming of triisopropylsilane and reducing production costs.

[0013] 2. The present invention provides a control method for an automated crude distillation system of triisopropylsilane, which performs judgment and control operations based on set process parameters, realizes process operation automation, and can be executed continuously and stably to produce qualified crude triisopropylsilane, thereby reducing the workload of subsequent distillation systems. BRIEF DESCRIPTION OF THE DRAWINGS

[0014] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0015] Figure 1 This is a process system diagram of Example 1 of the present invention.

[0016] Figure 2 This is a control flow chart of Example 1 of the present invention.

[0017] Reaction liquid storage tank 1, crude distillation kettle 2, jacket 201, crude product storage tank 3, crude distillation tower 4, condensing unit 5, water cooler 51, salt cooler 52, reflux ratio regulator 6, fore fraction receiving tank 7, solvent receiving tank 8, vacuum unit 9, solvent storage tank 10, feed pipe 11, second liquid level sensor 12, transfer pump 13, feed valve 14, discharge pipe 15, discharge valve 16, crude product discharge pump 17, first liquid level sensor 18, temperature sensor 19, pressure sensor 20, liquid outlet main pipe 21, moisture sensor 22, fore fraction inlet valve 23, solvent inlet valve 24, fore fraction outlet valve 25, solvent outlet valve 26, liquid outlet pump 27, third liquid level sensor 28, steam pipeline 29, steam cut-off valve 30, circulating water pipeline 31, circulating water cut-off valve 32, nitrogen pipeline 33, nitrogen cut-off valve 34, controller 35. DETAILED DESCRIPTION

[0018] The present invention will be further described in detail below by way of examples.

[0019] Example 1: Figure 1 As shown, an automated crude distillation system for triisopropylsilane comprises a reaction liquid storage tank 1, a crude distillation kettle 2, a crude product storage tank 3, a crude distillation tower 4, a condensing unit 5, a reflux ratio regulator 6, a front fraction receiving tank 7, a solvent receiving tank 8, a vacuum unit 9 and a solvent storage tank 10; the liquid outlet of the reaction liquid storage tank 1 is connected to the liquid inlet of the crude distillation kettle 2 through a feed pipe 11, a second liquid level sensor 12 is arranged in the reaction liquid storage tank 1, and a transfer pump 13 and a feed valve 14 are arranged on the feed pipe 11 in sequence; the liquid outlet of the crude distillation kettle 2 is connected to the crude product storage tank 3, and the feed pipe 11 is connected to the crude product storage tank 3. The feed port of the tank 3 is connected through a discharge pipe 15, on which a discharge valve 16 and a crude product discharge pump 17 are sequentially arranged; a first liquid level sensor 18 is arranged in the crude steam kettle 2; a crude steam tower 4 is arranged above the crude steam kettle 2, and the top air outlet of the crude steam tower 4 is connected to the air inlet of the condensing unit 5, and the air outlet of the condensing unit 5 is connected to the air inlet of the vacuum unit 9, a temperature sensor 19 is arranged on the top of the crude steam tower 4, and a pressure sensor 20 is arranged in the crude steam tower 4, and the vacuum unit 9 is a Roots vacuum unit 9.

[0020] The condensate outlet of the condensing unit 5 is connected to the liquid inlet of the reflux ratio regulator 6, and the two liquid outlets of the reflux ratio regulator 6 are respectively connected to the liquid inlet above the crude distillation tower 4 and the liquid inlet end of the liquid outlet main pipe 21; the liquid outlet end of the liquid outlet main pipe 21 is respectively connected to the liquid inlets of the fore fraction receiving tank 7 and the solvent receiving tank 8; a moisture sensor 22 is arranged on the liquid outlet main pipe 21; a fore fraction inlet valve 23 is arranged at the liquid inlet of the fore fraction receiving tank 7; a solvent inlet valve 24 is arranged at the liquid inlet of the solvent receiving tank 8 Valve 24; the top air outlets of the fore-fraction receiving tank 7 and the solvent receiving tank 8 are both connected to the air inlet of the vacuum unit 9; a fore-fraction air outlet valve 25 is provided at the air outlet of the fore-fraction receiving tank 7; a solvent air outlet valve 26 is provided at the air outlet of the solvent receiving tank 8; the liquid outlet of the solvent receiving tank 8 is connected to the liquid inlet of the solvent storage tank 10 through a pipeline, and a liquid outlet pump 27 is provided on the pipeline between the solvent receiving tank 8 and the solvent storage tank 10; a third liquid level sensor 28 is provided in the solvent receiving tank 8.

[0021] The gas outlet end of the steam pipeline 29 is connected to the gas inlet of the jacket 201 of the rough steam kettle 2; a steam shut-off valve 30 is provided at the gas inlet of the jacket 201; the water outlet end of the circulating water pipeline 31 is connected to the water inlet of the jacket 201 of the rough steam kettle 2; a circulating water shut-off valve 32 is provided at the water inlet of the jacket 201; the gas outlet end of the nitrogen pipeline 33 is connected to the gas inlet of the rough steam kettle 2, and a nitrogen shut-off valve 34 is provided at the gas inlet of the rough steam kettle 2.

[0022] The signal output ends of the first liquid level sensor 18, the temperature sensor 19, the pressure sensor 20, the moisture sensor 22, the second liquid level sensor 12 and the third liquid level sensor 28 are all connected to the signal input end of the controller 35 through signals; the signal output end of the controller 35 is respectively connected to the signal input ends of the transfer pump 13, the feed valve 14, the discharge valve 16, the crude product discharge pump 17, the vacuum unit 9, the reflux ratio regulator 6, the front fraction inlet valve 23, the solvent inlet valve 24, the front fraction outlet valve 25, the solvent outlet valve 26, the steam cut-off valve 30, the circulating water cut-off valve 32, the nitrogen cut-off valve 34 and the liquid outlet pump 27 through signals.

[0023] The condensing unit 5 includes a water cooler 51 and a salt cooler 52. The air outlet of the crude distillation tower 4 is connected to the air inlet of the water cooler 51, the air outlet of the water cooler 51 is connected to the air inlet of the salt cooler 52, the air outlet of the salt cooler 52 is connected to the air inlet of the vacuum unit 9, and the condensate outlets of the water cooler 51 and the salt cooler 52 are both connected to the liquid inlet of the reflux ratio regulator 6.

[0024] Embodiment 2: A control method for an automated crude distillation system of triisopropylsilane, comprising the following steps in sequence: (1) Feeding: Press one button to start, the transfer pump 13 starts running, and the feed valve 14 opens, and the reaction liquid enters the crude steamer 2. When the liquid level in the crude steamer 2 reaches the upper limit value or when the liquid level in the reaction liquid storage tank 1 reaches the lower limit value, the controller 35 controls the transfer pump 13 and the feed valve 14 to close.

[0025] (2) Receiving the fore fraction: After completing step (1), the controller 35 controls the vacuum unit 9 to start and simultaneously opens the steam shut-off valve 30. When the temperature at the top of the crude distillation tower 4 rises to 75°C and the internal pressure is less than -0.09 MPa, the reflux ratio regulator 6 is controlled to open, and all the condensate condensed by the condensing unit 5 is refluxed into the crude distillation tower 4. The reflux time is 0.5 h. Thereafter, the reflux ratio regulator 6 is controlled to adjust the reflux ratio of the condensate refluxed to the crude distillation tower 4 and the condensate taken out into the fore fraction receiving tank 7 to 20:1. At the same time, the fore fraction inlet valve 23 and the fore fraction outlet valve 25 in the fore fraction are opened. When the tower diameter and packing height remain unchanged, the separation effect is increased by adjusting the reflux ratio, and n-butyl ether, methanol, light components produced in the synthesis process and triisopropylsilane are effectively separated. The above reflux ratio has a high degree of separation. If the reflux ratio is 30:1, the required extraction time must reach 10 hours. Although the separation degree is slightly improved, it takes too long and the energy consumption is too high.

[0026] (3) Solvent receiving: When the water content of the liquid produced in step (2) is less than 600 PPM, the controller 35 controls the front fraction inlet valve 23 and the front fraction outlet valve 25 to be closed, and opens the solvent inlet valve 24 and the solvent outlet valve 26 at the same time, and controls the reflux ratio regulator 6 to adjust the reflux ratio of the condensate refluxed to the crude distillation tower 4 and produced into the solvent receiving tank 8 to 10:8; when the tower diameter and the packing height remain unchanged, the separation effect is increased by adjusting the reflux ratio, and n-butyl ether is effectively separated. With the above reflux ratio, the separation degree is relatively high; when the liquid level in the solvent receiving tank 8 reaches the upper limit value, the controller 35 controls the liquid outlet pump 27 to be turned on, and the solvent in the solvent receiving tank 8 is transported to the solvent storage tank 10. When the liquid level in the solvent receiving tank 8 reaches the lower limit value, the controller 35 controls the liquid outlet pump 27 to be turned off.

[0027] (4) Crude product collection: When the temperature of the top of the crude distillation tower 4 in step (3) rises to 85° C., the controller 35 controls the solvent inlet valve 24 and the solvent outlet valve 26 to be closed, and controls the reflux ratio regulator 6 to adjust so that all the condensate flows back into the crude distillation tower 4, and controls the steam cut-off valve 30 to be closed, and opens the circulating water cut-off valve 32 to introduce cooling water for cooling. When the temperature in the crude distillation tower 4 drops to below 50° C., the controller 35 controls the vacuum unit 9 and the reflux ratio regulator 6 to be closed, and opens the nitrogen cut-off valve 34 to pressurize the crude distillation kettle 2 to normal pressure, and then closes the nitrogen cut-off valve 34. Then, the discharge valve 16 is controlled to be opened, and the crude product discharge pump 17 is operated to transport the crude product in the crude distillation kettle 2 to the crude product storage tank 3. After the crude product in the crude distillation kettle 2 is discharged, the discharge valve 16 and the crude product discharge pump 17 are controlled to be closed. After the crude product in the crude distillation kettle 2 is discharged, the purity of the crude product reaches 98% and the yield reaches 87%.

[0028] The above are preferred embodiments of the present invention. For ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principles of the present invention. These improvements and modifications should also be regarded as within the scope of protection of the present invention.

Claims

1. A triisopropylsilane automated crude steaming system, characterized in that: It includes a reaction liquid storage tank, a crude distillation kettle, a crude product storage tank, a crude distillation tower, a condensing unit, a reflux ratio regulator, a front fraction receiving tank, a solvent receiving tank and a vacuum unit; The liquid outlet of the reaction liquid storage tank is connected to the liquid inlet of the crude steam kettle through a feed pipe, and a feed transfer pump and a feed valve are sequentially arranged on the feed pipe; The liquid outlet of the crude steam kettle is connected to the feed port of the crude product storage tank through a discharge pipe, and a discharge valve and a crude product discharge pump are sequentially arranged on the discharge pipe; a first liquid level sensor is arranged in the crude steam kettle; The crude steaming tower is connected to the crude steaming kettle, the top gas outlet of the crude steaming tower is connected to the gas inlet of the condensing unit, and the gas outlet of the condensing unit is connected to the gas inlet of the vacuum unit; a temperature sensor is provided at the top of the crude steaming tower, and a pressure sensor is provided inside the crude steaming tower; The condensate outlet of the condensing unit is connected to the liquid inlet of the reflux ratio regulator, and the two liquid outlets of the reflux ratio regulator are respectively connected to the liquid inlet above the crude distillation tower and the liquid inlet end of the liquid outlet main pipe; The liquid outlet end of the liquid outlet main pipe is connected to the liquid inlet of the fore fraction receiving tank and the liquid inlet of the solvent receiving tank respectively; a moisture sensor is arranged on the liquid outlet main pipe; a fore fraction inlet valve is arranged at the liquid inlet of the fore fraction receiving tank; and a solvent inlet valve is arranged at the liquid inlet of the solvent receiving tank; The top gas outlets of the fore fraction receiving tank and the solvent receiving tank are both connected to the gas inlet of the vacuum unit; a fore fraction gas outlet valve is provided at the gas outlet of the fore fraction receiving tank; and a solvent gas outlet valve is provided at the gas outlet of the solvent receiving tank; The gas outlet end of the steam pipeline is connected to the gas inlet of the jacket of the crude steam kettle; a steam shut-off valve is provided at the gas inlet of the jacket; The water outlet of the circulating water pipeline is connected to the water inlet of the jacket of the crude steam kettle; a circulating water cut-off valve is provided at the water inlet of the jacket; The gas outlet end of the nitrogen pipeline is connected to the gas inlet of the crude steam kettle, and a nitrogen shut-off valve is arranged at the gas inlet of the crude steam kettle; The signal output ends of the first liquid level sensor, the temperature sensor, the pressure sensor and the moisture sensor are all connected to the signal input end of the controller through signals; the signal output end of the controller is respectively connected to the signal input ends of the transfer pump, the feed valve, the discharge valve, the crude product discharge pump, the vacuum unit, the reflux ratio regulator, the fore fraction inlet valve, the solvent inlet valve, the fore fraction outlet valve, the solvent outlet valve, the steam cut-off valve, the circulating water cut-off valve and the nitrogen cut-off valve through signals.

2. The automated crude distillation system for triisopropylsilane according to claim 1, characterized in that: A second liquid level sensor is arranged in the reaction liquid storage tank, and a signal output end of the second liquid level sensor is connected to a signal input end of the controller through a signal.

3. The automated crude distillation system for triisopropylsilane according to claim 1, characterized in that: It also includes a solvent storage tank, the liquid outlet of the solvent receiving tank is connected to the liquid inlet of the solvent storage tank through a pipeline, and a liquid outlet pump is arranged on the pipeline between the solvent receiving tank and the solvent storage tank; a third liquid level sensor is arranged in the solvent receiving tank, the signal output end of the third liquid level sensor is connected to the signal input end of the controller through a signal, and the signal output end of the controller is connected to the signal input end of the liquid outlet pump through a signal.

4. The automated crude distillation system for triisopropylsilane according to claim 1, characterized in that: The vacuum unit is a Roots vacuum unit.

5. The automated crude distillation system for triisopropylsilane according to claim 1, characterized in that: The condensing unit includes a water cooler and a salt cooler, the air outlet of the crude distillation tower is connected to the air inlet of the water cooler, the air outlet of the water cooler is connected to the air inlet of the salt cooler, the air outlet of the salt cooler is connected to the air inlet of the vacuum unit, and the condensate outlets of the water cooler and the salt cooler are both connected to the liquid inlet of the reflux ratio regulator.

6. A control method for a system as claimed in any one of claims 1 to 5, characterized in that: It includes the following steps: (1) Feeding: One-button start, the feed pump starts running, and the feed valve opens at the same time, and the reaction liquid enters the crude steam kettle. When the liquid level in the crude steam kettle reaches the upper limit, the controller controls the feed pump and the feed valve to close; (2) Receiving the fore fraction: After completing step (1), the controller controls the vacuum unit to start and opens the steam shut-off valve at the same time. When the temperature at the top of the crude distillation tower rises to 75°C and the internal pressure is less than -0.09 MPa, the reflux ratio regulator is controlled to open, and all the condensate condensed by the condensing unit is refluxed into the crude distillation tower. The reflux time is 1.5-3.5 hours. Thereafter, the reflux ratio regulator is controlled to adjust the reflux ratio of the condensate refluxed to the crude distillation tower and the condensate taken out to the fore fraction receiving tank to 20:

1. At the same time, the fore fraction inlet valve and the fore fraction outlet valve are opened; (3) Solvent receiving: When the water content of the liquid produced in step (2) is less than 600 PPM, the controller controls the front fraction inlet valve and the front fraction outlet valve to be closed, and simultaneously opens the solvent inlet valve and the solvent outlet valve, and controls the reflux ratio regulator to adjust the reflux ratio of the condensate refluxed to the crude distillation tower and produced into the solvent receiving tank to 10:8; (4) Crude product collection: When the temperature of the crude distillation tower top in step (3) rises to 85°C, the controller controls the solvent inlet valve and the solvent outlet valve to be closed, and controls the reflux ratio regulator to be adjusted, so that all the condensate flows back into the crude distillation tower, and controls the steam shut-off valve to be closed, opens the circulating water shut-off valve, and introduces cooling water for cooling. When the temperature in the crude distillation tower drops to below 50°C, the controller controls the vacuum unit and the reflux ratio regulator to be closed, and opens the nitrogen shut-off valve to pressurize the crude distillation kettle to normal pressure, and then closes the nitrogen shut-off valve. Then, the discharge valve is controlled to be opened, and the crude product discharge pump is operated to transport the crude product in the crude distillation kettle to the crude product storage tank. After the crude product in the crude distillation kettle is discharged, the discharge valve and the crude product discharge pump are controlled to be closed.

7. The control method of a triisopropylsilane automated crude steaming system according to claim 6, characterized in that: Step (1) also includes that when the liquid level in the reaction liquid storage tank reaches a lower limit value, the controller controls the material transfer pump and the feed valve to close.

8. The control method of a triisopropylsilane automated crude steaming system according to claim 6, characterized in that: Step (3) also includes that when the liquid level in the solvent receiving tank reaches an upper limit value, the controller controls the liquid outlet pump to start, and transports the solvent in the solvent receiving tank to the solvent storage tank; when the liquid level in the solvent receiving tank reaches a lower limit value, the controller controls the liquid outlet pump to close.

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