An automated crude distillation system for triisopropylsilane and its control method

Abstract

The present invention discloses an automated crude distillation system for triisopropylsilane and its control method, specifically relating to the technical field of extracting triisopropylsilane. The system includes a reaction liquid storage tank, a crude distillation kettle, a crude product storage tank, a crude distillation column, a condensation unit, a reflux ratio regulator, a pre-fraction receiving tank, a solvent receiving tank, and a vacuum unit; the method includes (1) feeding; (2) pre-fraction receiving; (3) solvent receiving; (4) crude product collection. Beneficial effects: The present invention provides an automated crude distillation system for triisopropylsilane and its control method, realizing one-key startup of the system, eliminating the need for personnel operation in the on-site operation state, reducing the frequency of personnel operation in the crude distillation of triisopropylsilane, and reducing production costs; realizing automated process operation and being able to continuously and stably execute, producing qualified crude triisopropylsilane products, and reducing the workload of the subsequent distillation system.

Description

Technical Field

[0001] This invention patent relates to the technical field of extracting triisopropylsilane, and particularly relates to an automated rough distillation system for triisopropylsilane and its control method. Background Art

[0002] Triisopropylsilane is a chemical intermediate, which can be used in the synthesis of sterically hindered organosilicon protecting agents, the preparation of special organosilicon materials and organic synthesis. It is an excellent hydrogen proton donor and is applied to many reduction reactions. Currently, the patent with publication number CN103204869B discloses a method for synthesizing high-purity triisopropylsilane, in which magnesium, a solvent, 2-chloropropane, methylcyclohexane and trichlorosilane are used as raw materials for reaction, and then triisopropylsilane is obtained through vacuum distillation; currently, vacuum distillation generally includes rough distillation and rectification, and the rough distillation is manually controlled, so there are problems such as unstable control process, large fluctuations, increasing the working burden of the rectification system, and ultimately affecting the output and quality of the product. Summary of the Invention

[0003] The purpose of the present invention is to provide an automated rough distillation system for triisopropylsilane and its control method that realizes automated process operation and reduces production costs.

[0004] One object of the present invention is implemented by the following technical solution: An automated rough distillation system for triisopropylsilane, which includes a reaction liquid storage tank, a rough distillation kettle, a crude product storage tank, a rough distillation tower, a condensation 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 communicated with the liquid inlet of the rough 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 rough distillation kettle is communicated with 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 rough distillation kettle; the rough distillation tower is communicated and arranged above the rough distillation kettle, the gas outlet at the top of the rough distillation tower is communicated with the gas inlet of the condensation unit, and the gas outlet of the condensation unit is communicated with the gas inlet of the vacuum unit; a temperature sensor is arranged at the top inside the rough distillation tower, and a pressure sensor is arranged inside the rough distillation tower; the condensate outlet of the condensation 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 rough distillation tower and the liquid inlet end of the total discharge pipe; the liquid outlet end of the total discharge 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 total discharge pipe; a fore-fraction inlet valve is arranged at the liquid inlet of the fore-fraction receiving tank; a solvent inlet valve is arranged at the liquid inlet of the solvent receiving tank; the gas outlets at the tops of the fore-fraction receiving tank and the solvent receiving tank are both communicated with the gas inlet of the vacuum unit; a fore-fraction outlet valve is arranged at the gas outlet of the fore-fraction receiving tank; a solvent outlet valve is arranged at the gas outlet of the solvent receiving tank; the gas outlet end of the steam pipeline is communicated with the gas inlet of the jacket of the rough distillation kettle; a steam cut-off valve is arranged at the gas inlet of the jacket; the water outlet end of the circulating water pipeline is communicated with the water inlet of the jacket of the rough distillation kettle; a circulating water cut-off valve is arranged at the water inlet of the jacket; the gas outlet end of the nitrogen pipeline is communicated with the gas inlet of the rough distillation kettle, and a nitrogen cut-off valve is arranged at the gas inlet of the rough distillation 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 signal connections; 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 signal connections.

[0005] Further, a second liquid level sensor is arranged in the reaction liquid storage tank, and the signal output end of the second liquid level sensor is connected to the signal input end of the controller through a signal connection.

[0006] Further, it further includes a solvent storage tank. The liquid outlet of the solvent receiving tank is communicated with 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 signal-connected to the signal input end of the controller, and the signal output end of the controller is signal-connected to the signal input end of the liquid outlet pump.

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

[0008] Further, the condensation unit includes a water cooler and a salt cooler. The gas outlet of the rough distillation tower is communicated with the gas inlet of the water cooler, the gas outlet of the water cooler is communicated with the gas inlet of the salt cooler, the gas outlet of the salt cooler is communicated with the gas inlet of the vacuum unit, and the condensate outlets of the water cooler and the salt cooler are both communicated with the liquid inlet of the reflux ratio regulator.

[0009] The second object of the present invention is implemented by the following technical solution: A control method for an automatic rough distillation system of triisopropylsilane, which includes the following steps:

[0010] (1) Feeding: With one-key start, the transfer pump starts to operate, and at the same time the feed valve is opened, and the reaction liquid enters the rough distillation kettle. When the liquid level in the rough distillation kettle reaches the upper limit value, the controller controls the transfer pump and the feed valve to close;

[0011] (2) Receiving of fore-fraction: After completing step (1), the controller controls the vacuum unit to start, and at the same time opens the steam cut-off valve. When the temperature at the top of the rough distillation tower rises to 75 °C and the pressure inside is < -0.09 MPa, the controller controls the reflux ratio regulator to open, and all the condensate condensed by the condensation unit flows back into the rough distillation tower. The reflux time is 1.5 - 3.5 h. Then, the controller controls the reflux ratio regulator to adjust the reflux ratio of the condensate flowing back into the rough distillation tower and the condensate drawn out into the fore-fraction receiving tank to 20:1, and at the same time opens the fore-fraction inlet valve and the fore-fraction outlet valve;

[0012] (3) Solvent receiving: When the water content of the liquid drawn out in step (2) < 600 PPM, the controller controls the fore-fraction inlet valve and the fore-fraction outlet valve to close, and at the same time opens the solvent inlet valve and the solvent outlet valve, and controls the reflux ratio regulator to adjust the reflux ratio of the condensate flowing back into the rough distillation tower and the condensate drawn out into the solvent receiving tank to 10:8;

[0013] (4)Crude product collection: When the temperature at the top of the crude distillation tower in step (3) rises to 85 °C, the controller controls the solvent inlet valve and the solvent outlet valve to close. At the same time, it controls the reflux ratio regulator to adjust so that all the condensate flows back into the crude distillation tower. And it controls the steam cut-off valve to close, opens the circulating water cut-off valve, and cools it by introducing cooling water. When the temperature inside the crude distillation tower drops below 50 °C, the controller controls the vacuum unit and the reflux ratio regulator to close. At the same time, it opens the nitrogen cut-off valve, pressurizes the crude distillation kettle to atmospheric pressure and then closes the nitrogen cut-off valve. Then it controls the discharge valve to open and the crude product discharge pump to operate, and transports the crude product in the crude distillation kettle to the crude product storage tank. After the crude product in the crude distillation kettle is emptied, it controls the discharge valve and the crude product discharge pump to close.

[0014] Further, in step (1), it also includes that when the liquid level in the reaction liquid storage tank reaches the lower limit value, the controller controls the transfer pump and the feed valve to close.

[0015] Further, in step (3), it also includes that when the liquid level in the solvent receiving tank reaches the upper limit value, the controller controls the liquid outlet pump to open and transports the solvent in the solvent receiving tank to the solvent storage tank. When the liquid level in the solvent receiving tank reaches the lower limit value, the controller controls the liquid outlet pump to close.

[0016] Advantages of the present invention:

[0017] 1. The present invention provides an automated crude distillation system for triisopropylsilane, realizing one-key start of the system, without the need for personnel operation of the on-site operation status, reducing the frequency of personnel operation for the crude distillation of triisopropylsilane and reducing the production cost.

[0018] 2. The present invention provides a control method for an automated crude distillation system of triisopropylsilane, making judgment control operations based on the set process parameters, realizing automated process operations, and being able to continuously and stably execute, producing qualified crude triisopropylsilane products, reducing the working burden of the subsequent rectification system. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] In order to more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the following will briefly introduce the drawings required for use in the description of the embodiments or the prior art. Obviously, the following drawings are only some embodiments of the present invention. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.

[0020] Figure 1 It is the process system diagram of Embodiment 1 of the present invention.

[0021] Figure 2 It is the control flow chart of Embodiment 1 of the present invention.

[0022] Reaction liquid storage tank 1, rough distillation kettle 2, jacket 201, crude product storage tank 3, rough distillation column 4, condensation 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, total liquid discharge pipe 21, moisture sensor 22, fore-fraction inlet valve 23, solvent inlet valve 24, fore-fraction gas outlet valve 25, solvent gas outlet valve 26, liquid discharge 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 implementation mode

[0023] The present invention will be further described in detail below through embodiments.

[0024] Embodiment 1: As Figure 1 shown, an automated rough distillation system for triisopropylsilane, which includes a reaction liquid storage tank 1, a rough distillation kettle 2, a crude product storage tank 3, a rough distillation column 4, a condensation unit 5, a reflux ratio regulator 6, a fore-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 communicated with the liquid inlet of the rough 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 sequentially arranged on the feed pipe 11; the liquid outlet of the rough distillation kettle 2 is communicated with the feed inlet of the crude product storage tank 3 through a discharge pipe 15, and a discharge valve 16 and a crude product discharge pump 17 are sequentially arranged on the discharge pipe 15; a first liquid level sensor 18 is arranged in the rough distillation kettle 2; a rough distillation column 4 is communicated and arranged above the rough distillation kettle 2, the gas outlet at the top of the rough distillation column 4 is communicated with the gas inlet of the condensation unit 5, the gas outlet of the condensation unit 5 is communicated with the gas inlet of the vacuum unit 9, a temperature sensor 19 is arranged at the top inside the rough distillation column 4, a pressure sensor 20 is arranged inside the rough distillation column 4, and the vacuum unit 9 is a Roots vacuum unit 9.

[0025] The condensate outlet of the condensation unit 5 is communicated with the liquid inlet of the reflux ratio regulator 6. The two liquid outlets of the reflux ratio regulator 6 are respectively communicated with the liquid inlet above the rough distillation column 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 communicated with the inlets of the pre-fraction receiving tank 7 and the solvent receiving tank 8. A moisture sensor 22 is arranged on the liquid outlet main pipe 21. A pre-fraction inlet valve 23 is arranged at the liquid inlet of the pre-fraction receiving tank 7. A solvent inlet valve 24 is arranged at the liquid inlet of the solvent receiving tank 8. The top gas outlets of the pre-fraction receiving tank 7 and the solvent receiving tank 8 are both communicated with the gas inlet of the vacuum unit 9. A pre-fraction gas outlet valve 25 is arranged at the gas outlet of the pre-fraction receiving tank 7. A solvent gas outlet valve 26 is arranged at the gas outlet of the solvent receiving tank 8. The liquid outlet of the solvent receiving tank 8 is communicated with the liquid inlet of the solvent storage tank 10 through a pipeline. A liquid outlet pump 27 is arranged on the pipeline between the solvent receiving tank 8 and the solvent storage tank 10. A third liquid level sensor 28 is arranged in the solvent receiving tank 8.

[0026] The gas outlet end of the steam pipeline 29 is communicated with the gas inlet of the jacket 201 of the rough distillation kettle 2. A steam cut-off valve 30 is arranged at the gas inlet of the jacket 201. The water outlet end of the circulating water pipeline 31 is communicated with the water inlet of the jacket 201 of the rough distillation kettle 2. A circulating water cut-off valve 32 is arranged at the water inlet of the jacket 201. The gas outlet end of the nitrogen pipeline 33 is communicated with the gas inlet of the rough distillation kettle 2. A nitrogen cut-off valve 34 is arranged at the gas inlet of the rough distillation kettle 2.

[0027] 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 with the signal input end of the controller 35 through signals. The signal output end of the controller 35 is respectively connected with 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 pre-fraction inlet valve 23, the solvent inlet valve 24, the pre-fraction gas outlet valve 25, the solvent gas 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.

[0028] The condensation unit 5 includes a water cooler 51 and a salt cooler 52. The gas outlet of the rough distillation column 4 is communicated with the gas inlet of the water cooler 51. The gas outlet of the water cooler 51 is communicated with the gas inlet of the salt cooler 52. The gas outlet of the salt cooler 52 is communicated with the gas inlet of the vacuum unit 9. The condensate outlets of the water cooler 51 and the salt cooler 52 are both communicated with the liquid inlet of the reflux ratio regulator 6.

[0029] Embodiment 2: A control method for an automated rough distillation system of triisopropylsilane, which successively includes the following steps:

[0030] (1)Feeding: With one-key start, the transfer pump 13 starts to operate, and at the same time, the feed valve 14 opens, and the reaction liquid enters the rough distillation kettle 2. When the liquid level in the rough distillation kettle 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.

[0031] (2)Receiving of pre-fraction: After completing step (1), the controller 35 controls the vacuum unit 9 to start, and at the same time, the steam cut-off valve 30 is opened. When the temperature at the top of the rough distillation column 4 rises to 75 °C and the pressure inside is < -0.09 MPa, the reflux ratio regulator 6 is controlled to open. All the condensate condensed by the condensation unit 5 flows back into the rough distillation column 4, and the reflux time is 0.5 h. Then, the reflux ratio regulator 6 is controlled to adjust the reflux ratio of the condensate flowing back into the rough distillation column 4 and the condensate drawn into the pre-fraction receiving tank 7 to 20:1. At the same time, the pre-fraction inlet valve 23 and the pre-fraction outlet gas valve 25 are opened. Under the condition that the column diameter and the packing height remain unchanged, by adjusting the reflux ratio, the separation effect is increased, and n-butyl ether, methanol, light components generated during the synthesis process, and triisopropylsilane are effectively separated. With the above reflux ratio, the separation degree is relatively high; if the reflux ratio is 30:1, the required sampling time will reach 10 h. Although the separation degree is slightly improved, the time consumption is too long and the energy consumption is too high.

[0032] (3)Receiving of solvent: When the water content of the liquid sampled in step (2) < 600 PPM, the controller 35 controls the pre-fraction inlet valve 23 and the pre-fraction outlet gas valve 25 to close, and at the same time, the solvent inlet valve 24 and the solvent outlet gas valve 26 are opened, and the reflux ratio regulator 6 is controlled to adjust the reflux ratio of the condensate flowing back into the rough distillation column 4 and the condensate drawn into the solvent receiving tank 8 to 10:8; Under the condition that the column diameter and the packing height remain unchanged, by adjusting the reflux ratio, the separation effect is increased, 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 open, and transports the solvent in the solvent receiving tank 8 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 close.

[0033] (4)Crude product collection: When the temperature at the top of the crude distillation column 4 in step (3) rises to 85 °C, the controller 35 controls the solvent inlet valve 24 and the solvent outlet valve 26 to close. At the same time, it controls the reflux ratio regulator 6 to adjust so that all the condensate flows back into the crude distillation column 4. And it controls the steam cut-off valve 30 to close and opens the circulating water cut-off valve 32 to introduce cooling water for temperature reduction. When the temperature inside the crude distillation column 4 drops below 50 °C, the controller 35 controls the vacuum unit 9 and the reflux ratio regulator 6 to close. At the same time, it opens the nitrogen cut-off valve 34 to pressurize the crude distillation kettle 2 to atmospheric pressure and then closes the nitrogen cut-off valve 34. After that, it controls the discharge valve 16 to open and the crude product discharge pump 17 to operate 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 emptied, it controls the discharge valve 16 and the crude product discharge pump 17 to close; After detection, the purity of the crude product reaches 98% and the yield reaches 87%.

[0034] The above is the preferred implementation mode of the present invention. For those of ordinary skill in the art of this technology, without departing from the principle of the present invention, several improvements and refinements can be made, and these improvements and refinements should also be regarded as the protection scope of the present invention.

Claims

1. A method for controlling the automated crude distillation of triisopropylsilane, 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.

2. The method for controlling the automated crude distillation of triisopropylsilane according to claim 1, 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.

3. The method for controlling the automated crude distillation of triisopropylsilane according to claim 1, 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.

4. The method for controlling the automated crude distillation of triisopropylsilane according to claim 1, characterized in that: It includes a system for realizing the automated crude distillation control method of triisopropylsilane as claimed in any one of claims 1 to 3, wherein the system 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.

5. The method for controlling the automated crude distillation of triisopropylsilane according to claim 4, 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.

6. The method for controlling the automated crude distillation of triisopropylsilane according to claim 4, 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.

7. The method for controlling the automated crude distillation of triisopropylsilane according to claim 4, characterized in that: The vacuum unit is a Roots vacuum unit.

8. The method for controlling the automated crude distillation of triisopropylsilane according to claim 4, 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.

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