Organic silicon rectification coupling system

Abstract

The utility model discloses an organic silicon rectification coupling system which comprises a material steam distribution cylinder, a top exhaust port of the binary upper tower is communicated with a gas inlet of a material steam distribution cylinder, and a gas outlet of the material steam distribution cylinder is respectively communicated with reboiler material steam inlets of the high component removal tower, the low component removal tower, the light component removal tower, the hydrogen-containing tower, the azeotropic tower and the trimethyl tower; a condensate outlet of the reboiler of each tower is respectively communicated with a reflux tank of the binary tower; a bottom liquid outlet of the binary tower reflux tank is communicated with an inlet of a reflux pump, and an outlet of the reflux pump is communicated with the top of the binary upper tower through a reflux pipeline. The tower system has the advantages that the total amount of water vapor consumed by the tower system is greatly reduced, and the production cost is effectively reduced; the material steam generated by the binary upper tower is used as a heating medium of reboilers of the high component removal tower, the low component removal tower, the light component removal tower, the hydrogen-containing tower, the azeotropic tower and the trimethyl tower for heat exchange, so that the tower kettle temperature of each tower can be ensured, the heat of the material steam is recycled, and the heat loss is reduced.

Description

Technical Field:

[0001] The utility model relates to the technical field of silicone production, and particularly relates to a silicone rectification coupling system. Background Art:

[0002] In the process of silicone production, raw material methyl chloride and silicon powder are used in a fluidized bed reactor to synthesize a mixed monomer of methylchlorosilane under the action of a catalyst. Its main components include low boilers, methyl dichlorosilane, silicon tetrachloride, trimethylchlorosilane, methyltrichlorosilane, dimethyldichlorosilane, and high boilers.

[0003] At present, most silicone rectification for separating the mixed monomer of methylchlorosilane generally adopts eight - tower separation, namely a high - boiling tower, a low - boiling tower, a binary tower, a light - component tower, a hydrogen - containing tower, an azeotropic tower, and a trimethyl tower, using high - temperature steam to rectify and separate the components of the mixed monomer of methylchlorosilane.

[0004] In the current rectification separation process, the steam consumption of the binary tower is 20 tons per hour, and the total steam consumption of the other towers is 25.1 tons per hour. The steam consumption is large, and almost no heat is recovered during the rectification process. After the overhead material steam is condensed by the condensation unit at the top of the tower, part is used as reflux liquid and part is taken out as the overhead product. The heat of the overhead material steam is not recovered, resulting in serious heat loss.

[0005] In addition, each tower kettle of each tower system is equipped with a separate reboiler. The reboiler uses steam medium to exchange heat with the kettle material medium. Due to the large temperature difference between the two media in the reboiler, the thermal stress is large. After long - term operation, the reboiler has the phenomenon of damage and leakage, shortening its service life, especially the reboiler of the high - boiling tower is more serious. Summary of the Utility Model:

[0006] The purpose of the utility model is to provide a silicone rectification coupling system that can effectively recover and utilize the heat of the material steam and extend the service life of the reboiler.

[0007] The utility model is implemented by the following technical solutions: An organosilicon rectification coupling system, which includes a high tower, a low tower, a binary lower tower, a binary upper tower, a light tower, a hydrogen-containing tower, an azeotropic tower, a trimethyl tower and a high-boiling tower; it also includes a material steam distribution cylinder and a binary tower reflux tank; the top exhaust port of the binary upper tower is communicated with the air inlet of the material steam distribution cylinder, and the air outlet of the material steam distribution cylinder is respectively communicated with the reboiler material steam inlet of the high tower, the reboiler material steam inlet of the low tower, the reboiler material steam inlet of the light tower, the reboiler material steam inlet of the hydrogen-containing tower, the reboiler material steam inlet of the azeotropic tower, and the reboiler material steam inlet of the trimethyl tower; the reboiler condensate outlet of the high tower, the reboiler condensate outlet of the low tower, the reboiler condensate outlet of the light tower, the reboiler condensate outlet of the hydrogen-containing tower, the reboiler condensate outlet of the azeotropic tower, and the reboiler condensate outlet of the trimethyl tower are respectively communicated with the binary tower reflux tank; the bottom liquid outlet of the binary tower reflux tank is communicated with the inlet of the reflux pump, and the outlet of the reflux pump is communicated with the top of the binary upper tower through a reflux pipeline.

[0008] Further, a gas-liquid separator is installed between the pipeline at the material steam inlet of each reboiler and the pipeline at the corresponding condensate outlet.

[0009] Further, a first liquid level sensor is installed on the gas-liquid separator, and the first liquid level sensor is electrically connected to an electric valve on the pipeline at the bottom condensate outlet of the gas-liquid separator.

[0010] Further, a first pressure transmitter is installed on the material steam distribution cylinder, and the first pressure transmitter is electrically connected to an electric valve on the pipeline at the reboiler material steam inlet of the high tower.

[0011] Further, a steam trap is installed at the bottom of the material steam distribution cylinder, and the bottom liquid outlet of the steam trap is communicated with the binary tower reflux tank.

[0012] Further, a nitrogen inlet pipeline and a vent pipeline are communicated with the binary tower reflux tank, and a second pressure transmitter is installed on the binary tower reflux tank. The second pressure transmitter is electrically connected to the electric valve on the nitrogen inlet pipeline and the electric valve on the vent pipeline.

[0013] Further, a monomethyl product extraction pipeline is communicated with the reflux pipeline at the outlet of the reflux pump, a flow transmitter is installed on the monomethyl product extraction pipeline, and a second liquid level sensor is installed on the binary tower reflux tank. The second liquid level sensor and the flow transmitter are both electrically connected to the electric valve on the monomethyl product extraction pipeline.

[0014] Further, the top outlets of the de-high tower, de-low tower, de-light tower, hydrogen-containing tower, azeotropic tower, trimethyl tower and high-boiling tower are all connected with a condensation unit; the condensation unit includes a reflux drum and a first condenser and a second condenser connected in series in sequence. The top liquid discharge ports of the first condenser and the second condenser are communicated with the reflux drum. The top gas outlet of the second condenser is connected with a non-condensable gas pipeline. A third pressure transmitter is installed on the reflux drum, and the third pressure transmitter is electrically connected with an electric valve on the non-condensable gas pipeline.

[0015] Further, the bottom of the de-high tower is communicated with the high-boiling tower through a pump, and the liquid outlet of the reflux drum of the de-high tower is respectively communicated with the tops of the de-low tower and the de-high tower through a pump; the bottom of the de-low tower is communicated with the binary upper tower through a pump, and the liquid outlet of the reflux drum of the de-low tower is respectively communicated with the tops of the de-light tower and the de-low tower through a pump; the top material outlet of the binary lower tower is communicated with the lower inlet of the binary upper tower, and the bottom outlet of the binary upper tower is communicated with the top of the binary lower tower through a pump; the bottom of the de-light tower is communicated with the hydrogen-containing tower through a pump, the bottom of the hydrogen-containing tower is communicated with the azeotropic tower through a pump, the bottom of the azeotropic tower is communicated with the trimethyl tower through a pump, the bottom of the trimethyl tower is communicated with the de-light tower through a pump, and the liquid outlet of the reflux drum of the high-boiling tower is respectively communicated with the tops of the de-high tower and the high-boiling tower through a pump.

[0016] Advantages of the present utility model: In the present utility model, only the binary lower tower and the high-boiling tower use water vapor as a heat source for heat exchange in the reboiler. Among them, the consumption of the binary lower tower is 26 tons per hour, and the consumption of the high-boiling tower is 0.4 tons per hour, with a total of 26.4 tons per hour. In the prior art, the steam consumption of the binary tower is 20 tons per hour, and the total steam consumption of the other towers is 25.1 tons per hour, with a total of 45.1 tons per hour. Therefore, compared with the prior art, the total amount of water vapor consumed by the tower system of the present utility model is greatly reduced, effectively reducing the production cost.

[0017] The present utility model utilizes the material steam generated by the binary upper tower as a heating medium for heat exchange in the reboilers of the de-high tower, de-low tower, de-light tower, hydrogen-containing tower, azeotropic tower and trimethyl tower, which can not only ensure the tower bottom temperature of each tower, but also realize the heat recovery and utilization of the material steam, reducing heat loss.

[0018] Compared with the prior art, the temperature difference between the two media exchanging heat with each other in the reboiler of each tower in the system of the present utility model is smaller, which is beneficial to reducing thermal stress and prolonging its service life. Description of the drawings:

[0019] Figure 1 It is a structural schematic diagram of the present utility model.

[0020] Figure 2 This is a schematic structural diagram of the condensation unit of the present utility model.

[0021] Figure 3 is Figure 1 a partially enlarged view of A.

[0022] The markings of each component in the attached drawings are as follows: high-boiling tower 1, low-boiling tower 2, binary lower tower 3, binary upper tower 4, light-component removal tower 5, hydrogen-containing tower 6, azeotropic tower 7, trimethyl tower 8, high-boiling tower 9, material vapor distribution cylinder 10, reboiler 11, binary tower reflux tank 12, reflux pump 13, reflux pipeline 14, gas-liquid separator 15, first liquid level sensor 16, first pressure transmitter 17, steam trap 18, nitrogen inlet pipeline 19, vent pipeline 20, second pressure transmitter 21, monomethyl product extraction pipeline 22, flow transmitter 23, second liquid level sensor 24, condensation unit 25, first condenser 26, second condenser 27, reflux tank 28, non-condensable gas pipeline 29, third pressure transmitter 30, air cooler 31. Specific embodiments:

[0023] Next, the technical solutions in the embodiments of the present utility model will be clearly and completely described in conjunction with the attached drawings in the embodiments of the present utility model. Obviously, the described embodiments are only a part of the embodiments of the present utility model, rather than all of the embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present utility model.

[0024] As Figures 1 to 3 shown, this embodiment provides an organosilicon rectification coupling system, which includes a high-boiling tower 1, a low-boiling tower 2, a binary lower tower 3, a binary upper tower 4, a light-component removal tower 5, a hydrogen-containing tower 6, an azeotropic tower 7, a trimethyl tower 8, and a high-boiling tower 9; the bottom of the high-boiling tower 1, the low-boiling tower 2, the binary lower tower 3, the light-component removal tower 5, the hydrogen-containing tower 6, the azeotropic tower 7, the trimethyl tower 8, and the high-boiling tower 9 are all connected to a reboiler 11, and the top outlets of the high-boiling tower 1, the low-boiling tower 2, the light-component removal tower 5, the hydrogen-containing tower 6, the azeotropic tower 7, the trimethyl tower 8, and the high-boiling tower 9 are all connected to a condensation unit 25.

[0025] The condensation unit 25 includes a reflux drum 28, a first condenser 26 and a second condenser 27 connected in series in sequence. The top drain outlets of the first condenser 26 and the second condenser 27 are communicated with the reflux drum 28. The feed inlet of the first condenser 26 is communicated with the top discharge outlet of the corresponding tower. A non-condensable gas pipeline 29 is connected to the top gas outlet of the second condenser 27. In order to improve the cooling efficiency, in actual production, an air cooler 31 can be connected in series before the feed of the first condenser 26. However, considering the site space problem, in the present utility model, the air cooler 31 is only connected to the top discharge outlets of the low-boiling tower 2 and the binary upper tower 4. That is, the material is first cooled by the air cooler 31, and the non-condensable gas after cooling then enters the first condenser 26 for cooling. The condensate directly enters the reflux drum 28. The overhead material of the tower without the air cooler 31 directly enters the first condenser 26. The condensate water of the first condenser 26 enters the reflux drum 28. The non-condensable gas enters the second condenser 27 for continuous cooling, and the condensate water enters the reflux drum 28. A small amount of non-condensable gas is discharged into the subsequent tail gas treatment system through the non-condensable gas pipeline 29.

[0026] A third pressure transmitter 30 is installed on the reflux drum 28. The third pressure transmitter 30 is electrically connected to the electric valve on the non-condensable gas pipeline 29. The pressure in the reflux drum 28 is detected in real time by the third pressure transmitter 30, and the signal is transmitted to the controller. When the pressure exceeds the set range value, the opening degree of the electric valve on the non-condensable gas pipeline 29 is controlled by the controller to stabilize the pressure in the reflux drum 28.

[0027] The bottom of the high-boiling tower 1 is communicated with the high-boiling tower 9 through a pump. The methylchlorosilane mixed monomer is first sent to the high-boiling tower 1. After separating part of the dimethyldichlorosilane and high-boiling substances from the mixed monomer at the bottom of the tower, it is sent to the high-boiling tower 9. The remaining components enter the reflux drum 28 after being cooled by the condensation unit 25 from the top of the tower. The liquid outlet of the reflux drum 28 of the high-boiling tower 1 is communicated with the tops of the low-boiling tower 2 and the high-boiling tower 1 through pumps respectively. Part of the condensate in the reflux drum 28 is sent back to the high-boiling tower 1 as reflux liquid, and the other part is sent to the low-boiling tower 2. Its components include low-boiling substances, methyl dichlorosilane, silicon tetrachloride, trimethylchlorosilane, methyltrichlorosilane, and dimethyldichlorosilane.

[0028] The bottom of the low-boiling tower 2 is communicated with the binary upper tower 4 through a pump. The liquid outlet of the reflux drum 28 of the low-boiling tower 2 is communicated with the tops of the light-boiling tower 5 and the low-boiling tower 2 through pumps respectively. The methyltrichlorosilane and dimethyldichlorosilane extracted from the bottom of the low-boiling tower 2 are sent to the binary upper tower 4. Part of the condensate after cooling from the top of the low-boiling tower 2 is sent back to the low-boiling tower 2 as reflux liquid, and the other part is sent to the light-boiling tower 5. Its components include low-boiling substances, methyl dichlorosilane, silicon tetrachloride, trimethylchlorosilane, and a small amount of methyltrichlorosilane.

[0029] The top material outlet of the binary lower column 3 is connected to the lower inlet of the binary upper column 4, and the bottom outlet of the binary upper column 4 is connected to the top of the binary lower column 3 through a pump; the heating medium introduced into the reboiler 11 of the binary lower column 3 is steam, with a steam consumption of 26 tons per hour, and the temperature of the introduced steam is 159 °C. The dimethyldichlorosilane product is withdrawn from the bottom of the binary lower column 3, and the monomethyltrichlorosilane product is produced at the top of the binary upper column 4. Without cooling, it is directly sent to the material steam distribution cylinder 10 as the heat exchange material steam for the reboilers 11 of other columns except the high-boiling column 9.

[0030] The bottom of the light component removal column 5 is connected to the hydrogen-containing column 6 through a pump. The light components are separated from the top of the light component removal column 5, and the remaining materials are withdrawn from the bottom of the column and enter the hydrogen-containing column 6, with components including monomethyldichlorosilane, silicon tetrachloride, trimethylchlorosilane, and a small amount of monomethyltrichlorosilane.

[0031] The bottom of the hydrogen-containing column 6 is connected to the azeotropic column 7 through a pump. The monomethyl hydrogen-containing product is separated from the top of the hydrogen-containing column 6, and the remaining materials are withdrawn from the bottom of the column and enter the azeotropic column 7, with components including silicon tetrachloride, trimethylchlorosilane, and a small amount of monomethyltrichlorosilane.

[0032] The bottom of the azeotropic column 7 is connected to the trimethyl column 8 through a pump. The azeotropic product (where the silicon tetrachloride content < 45% and the trimethylchlorosilane content > 50%) is separated from the top of the azeotropic column 7, and the remaining materials are withdrawn from the bottom of the column and enter the trimethyl column 8, including trimethylchlorosilane and a small amount of monomethyltrichlorosilane.

[0033] The bottom of the trimethyl column 8 is connected to the light component removal column 5 through a pump. The trimethylchlorosilane product is produced at the top of the trimethyl column 8, and the remaining materials are withdrawn from the bottom of the column and enter the low-boiling component removal tower 2 for recovery, including a small amount of trimethylchlorosilane and a small amount of monomethyltrichlorosilane.

[0034] The liquid outlet of the reflux drum 28 of the high-boiling column 9 is connected to the top of the high-boiling component removal tower 1 and the high-boiling column 9 respectively through a pump. The dimethyldichlorosilane is produced at the top of the high-boiling column 9 and enters the high-boiling component removal tower 1 for recovery. A small amount of dimethyldichlorosilane and high-boiling substances are withdrawn from the bottom of the column and sent to high-boiling cracking; the heating medium of the reboiler 11 of the high-boiling column 9 is steam, the steam consumption of the reboiler 11 of the high-boiling column 9 is 0.4 tons per hour, and the temperature of the introduced steam is 184 °C.

[0035] It also includes a material steam distribution cylinder 10 and a binary tower reflux tank 12; the top exhaust port of the binary upper tower 4 is communicated with the air inlet of the material steam distribution cylinder 10. The monomethyltrichlorosilane product produced at the top of the binary upper tower 4 enters the material steam distribution cylinder 10. The temperature of the material steam is 110 °C, which is used as the heat exchange medium for the corresponding reboiler 11, controlling the temperature of the bottom of the de-high tower 1 at 90 °C, the temperature of the bottom of the de-low tower 2 at 89.7 °C, the temperature of the bottom of the de-light tower 5 at 77.6 °C, the temperature of the bottom of the hydrogen-containing tower 6 at 64.7 °C, the temperature of the bottom of the azeotropic tower 7 at 65.8 °C, and the temperature of the bottom of the trimethyl tower 8 at 67.9 °C; thus, it also meets the process requirement that the temperature difference between the heat exchange medium of the reboiler 11 and the bottom material is greater than 15 °C.

[0036] Before the improvement, the temperature of the steam used in the de-high tower 1 was 184 °C, and the temperatures of the steam used in the de-low tower 2, de-light tower 5, hydrogen-containing tower 6, azeotropic tower 7, and trimethyl tower 8 were all 159 °C. The bottom temperatures of each tower were the same as those after the improvement. It can be seen that the temperature difference between the two media exchanging heat with each other in the reboiler 11 of the above-mentioned towers after the improvement is smaller, which is beneficial to reducing thermal stress and prolonging its service life.

[0037] The air outlet of the material steam distribution cylinder 10 is respectively communicated with the material steam inlet of the reboiler 11 of the de-high tower 1, the material steam inlet of the reboiler 11 of the de-low tower 2, the material steam inlet of the reboiler 11 of the de-light tower 5, the material steam inlet of the reboiler 11 of the hydrogen-containing tower 6, the material steam inlet of the reboiler 11 of the azeotropic tower 7, and the material steam inlet of the reboiler 11 of the trimethyl tower 8; among them, the bottom temperature of the de-high tower 1 is 90 °C, that is, through the heat exchange of the 110 °C material steam, the bottom temperature of the de-high tower 1 can be controlled at 90 °C required by the process, and the top pressure of the de-high tower 1 corresponding to this is 0.05 MPa; before the improvement, 184 °C steam was used for heat exchange, the bottom temperature was controlled at 120 °C, and the top pressure of the de-high tower 1 corresponding to this was 0.2 MPa.

[0038] The binary lower tower 3 uses steam with a temperature of 159 °C to control the bottom temperature at 115 °C. The top pressure of the corresponding binary upper tower 4 is 0.25 MPa, and the reflux flow rate is 300 tons per hour. Before the improvement, the binary lower tower 3 used steam with a temperature of 159 °C to control the bottom temperature at 96.8 °C. The lower the tower pressure, the lower the boiling point of the material in the tower. The top pressure of the corresponding binary upper tower 4 was controlled at 0.1 MPa, and the reflux flow rate was 230 tons per hour.

[0039] A first pressure transmitter 17 is installed on the material steam distribution cylinder 10, and the first pressure transmitter 17 is electrically connected to an electric valve on the pipeline at the material steam inlet of the reboiler 11 of the stripping column 1; the pressure inside the material steam distribution cylinder 10 needs to be maintained in a stable state to avoid affecting the tower pressure of the binary upper column 4, so as to ensure the stable operation of the binary upper column 4 and the binary lower column 3; therefore, the first pressure transmitter 17 detects the pressure inside the material steam distribution cylinder 10 in real time and feeds it back to the controller. When the detected pressure is greater than the set upper limit value, the opening degree of the corresponding electric valve is increased, and vice versa, decreased, to ensure the stable pressure inside the material steam distribution cylinder 10.

[0040] A steam trap 18 is installed at the bottom of the material steam distribution cylinder 10. The bottom liquid outlet of the steam trap 18 is communicated with the binary tower reflux tank 12. The condensate carried by the material steam entering the material steam distribution cylinder 10 enters the binary tower reflux tank 12 through the steam trap 18.

[0041] The condensate outlets of the reboilers 11 of the stripping column 1, the deethanizer column 2, the debutanizer column 5, the hydrogen-containing column 6, the azeotropic column 7, and the trimethylamine column 8 are respectively communicated with the binary tower reflux tank 12; the bottom liquid outlet of the binary tower reflux tank 12 is communicated with the inlet of the reflux pump 13, and the outlet of the reflux pump 13 is communicated with the top of the binary upper column 4 through the reflux pipeline 14; the condensate generated after the material steam passing through the above reboilers 11 is heat-exchanged enters the binary tower reflux tank 12 and returns to the binary upper column 4 through the reflux pump 13, and the reflux flow rate is 300 tons per hour, greatly increasing the reflux ratio and being beneficial to the rectification separation of the materials in the tower.

[0042] A gas-liquid separator 15 is installed between the pipeline at the material steam inlet of each reboiler 11 and the pipeline at the corresponding condensate outlet. The condensate of the material steam after heat exchange in the reboiler 11 first enters the gas-liquid separator 15. The non-condensable gas separated from the condensate returns upward to the material steam inlet of the reboiler 11, and the separated condensate enters the binary tower reflux tank 12; a first liquid level sensor 16 is installed on the gas-liquid separator 15, and the first liquid level sensor 16 is electrically connected to an electric valve on the pipeline at the bottom condensate outlet of the gas-liquid separator 15; the liquid level inside the gas-liquid separator 15 is detected in real time by the first liquid level sensor 16 and the signal is fed back to the controller. When the liquid level value exceeds the set value, the controller increases the opening degree of the electric valve to stabilize the liquid level value inside the gas-liquid separator 15.

[0043] A nitrogen inlet pipeline 19 and a vent pipeline 20 are connected to the binary tower reflux tank 12. A second pressure transmitter 21 is installed on the binary tower reflux tank 12. The second pressure transmitter 21 is electrically connected to the electric valves on the nitrogen inlet pipeline 19 and the vent pipeline 20. According to process requirements, the pressure in the binary tower reflux tank 12 also needs to be maintained in a stable state. The second pressure transmitter 21 detects the pressure in the binary tower reflux tank 12 in real time and feeds back the signal to the controller. When the pressure drops to the set lower limit value, the controller controls the electric valve on the nitrogen inlet pipeline 19 to open and send in nitrogen to achieve nitrogen sealing. When the pressure in the binary tower reflux tank 12 is higher than the set upper limit value, the controller controls the electric valve on the vent pipeline 20 to open and discharge a part to maintain a stable state.

[0044] A first methyl product extraction pipeline 22 is connected to the reflux pipeline 14 at the outlet of the reflux pump 13. A flow transmitter 23 is installed on the first methyl product extraction pipeline 22. A second liquid level sensor 24 is installed on the binary tower reflux tank 12. The second liquid level sensor 24 and the flow transmitter 23 are both electrically connected to the electric valve on the first methyl product extraction pipeline 22. The second liquid level sensor 24 detects the liquid level in the binary tower reflux tank 12 in real time and feeds back the signal to the controller in real time. When the liquid level is higher than the set upper limit value, the controller controls the opening degree of the electric valve on the first methyl product extraction pipeline 22 to increase, increasing the extraction amount of the first methyl product to stabilize the liquid level in the binary tower reflux tank 12. At the same time, in order to ensure the stable flow of the extracted product, the flow transmitter 23 monitors the passing flow value in real time and feeds it back to the controller. Thus, on the premise of ensuring the stable liquid level in the binary tower reflux tank 12, the controller adjusts the opening degree of the electric valve to ensure stable extraction.

[0045] In the present utility model, only the binary lower tower 3 and the high-boiling tower 9 use steam as the heat source for heat exchange in the reboiler 11. Among them, the consumption of the binary lower tower 3 is 26 tons per hour, and the consumption of the high-boiling tower 9 is 0.4 tons per hour, with a total of 26.4 tons per hour. In the prior art, the steam consumption of the binary tower is 20 tons per hour, and the total steam consumption of the other towers is 25.1 tons per hour, with a total of 45.1 tons per hour. Thus, compared with the prior art, the total amount of steam consumed by the tower system of the present utility model is greatly reduced, effectively reducing the production cost.

[0046] The present utility model utilizes the material steam generated by the binary upper tower 4 as the heating medium for heat exchange in the reboilers 11 of the de-high tower 1, de-low tower 2, de-light tower 5, hydrogen-containing tower 6, azeotropic tower 7, and trimethyl tower 8, which can not only ensure the bottom temperature of each tower but also realize the heat recovery and utilization of the material steam, reducing heat loss.

[0047] The above are only the preferred embodiments of the present utility model and are not intended to limit the present utility model. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present utility model shall be included within the protection scope of the present utility model.

Claims

1. An organic silicon distillation coupling system, which includes a high removal tower, a low removal tower, a binary lower tower, a binary upper tower, a light removal tower, a hydrogen-containing tower, an azeotropic tower, a tertiary tower and a high boiling tower; It is characterized in that It also includes a material vapor distribution cylinder and a binary tower reflux tank; The top exhaust port of the binary upper tower is communicated with the air inlet of the material steam distribution cylinder, and the air outlet of the material steam distribution cylinder is respectively communicated with the reboiler material steam inlet of the high-removal tower, the reboiler material steam inlet of the low-removal tower, the reboiler material steam inlet of the light-removal tower, the reboiler material steam inlet of the hydrogen-containing tower, the reboiler material steam inlet of the azeotropic tower, and the reboiler material steam inlet of the triple-carboxylic acid tower; The reboiler condensate outlet of the high-removal tower, the reboiler condensate outlet of the low-removal tower, the reboiler condensate outlet of the light-removal tower, the reboiler condensate outlet of the hydrogen-containing tower, the reboiler condensate outlet of the azeotropic tower, and the reboiler condensate outlet of the triple-methane tower are respectively connected to the binary tower reflux tank; The bottom liquid outlet of the binary tower reflux tank is connected to the inlet of the reflux pump, and the outlet of the reflux pump is connected to the top of the binary upper tower through a reflux pipeline.

2. The organic silicon distillation coupling system according to claim 1, characterized in that: A gas-liquid separator is installed between the pipeline at the material steam inlet of each reboiler and the pipeline at the corresponding condensate outlet.

3. The organic silicon distillation coupling system according to claim 2, characterized in that: A first liquid level sensor is installed on the gas-liquid separator, and the first liquid level sensor is electrically connected to an electric valve on a pipeline at a bottom condensate outlet of the gas-liquid separator.

4. The organic silicon distillation coupling system according to claim 1, characterized in that: A first pressure transmitter is installed on the material steam distribution cylinder, and the first pressure transmitter is connected to the electric valve on the pipeline at the material steam inlet of the reboiler of the degassing tower via an electrical signal.

5. The organic silicon distillation coupling system according to claim 1, characterized in that: A steam trap is installed at the bottom of the material steam distribution cylinder, and the bottom liquid outlet of the steam trap is communicated with the binary tower reflux tank.

6. The organic silicon distillation coupling system according to claim 1, characterized in that: The binary tower reflux tank is connected with a nitrogen inlet pipeline and a venting pipeline. A second pressure transmitter is installed on the binary tower reflux tank. The second pressure transmitter is electrically signal-connected with the electric valve on the nitrogen inlet pipeline and the electric valve on the venting pipeline.

7. The organic silicon distillation coupling system according to claim 1, characterized in that: The reflux pipeline at the outlet of the reflux pump is connected to a product A production pipeline, a flow transmitter is installed on the product A production pipeline, a second liquid level sensor is installed on the binary tower reflux tank, and the second liquid level sensor and the flow transmitter are both connected to the electric signal of the electric valve on the product A production pipeline.

8. An organic silicon distillation coupling system according to any one of claims 1 to 7, characterized in that: The top outlets of the high-pressure removal tower, low-pressure removal tower, light-pressure removal tower, hydrogen-containing tower, azeotropic tower, triple-carbon tower and high-boiling tower are all connected to condensation units; The condensing unit includes a reflux tank and a first condenser and a second condenser connected in series in sequence. The top drain ports of the first condenser and the second condenser are connected to the reflux tank. The top gas outlet of the second condenser is connected to a non-condensable gas pipeline. A third pressure transmitter is installed on the reflux tank, and the third pressure transmitter is connected to an electric valve electrical signal on the non-condensable gas pipeline.

9. The organic silicon distillation coupling system according to claim 8, characterized in that: The bottom of the high degassing tower is connected to the high boiling tower through a pump, and the liquid outlet of the reflux tank of the high degassing tower is connected to the top of the low degassing tower and the high degassing tower respectively through a pump; The bottom of the degassing tower is connected to the binary upper tower through a pump, and the liquid outlet of the reflux tank of the degassing tower is connected to the top of the degassing tower and the degassing tower respectively through a pump; The top material outlet of the binary lower tower is connected to the lower inlet of the binary upper tower, and the bottom outlet of the binary upper tower is connected to the top of the binary lower tower through a pump; The bottom of the light-removal tower is connected to the hydrogen-containing tower through a pump, the bottom of the hydrogen-containing tower is connected to the azeotropic tower through a pump, the bottom of the azeotropic tower is connected to the tertiary tower through a pump, the bottom of the tertiary tower is connected to the light-removal tower through a pump, and the liquid outlet of the reflux tank of the high boiling tower is connected to the top of the high-boiling tower and the high boiling tower respectively through a pump.

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