CN210656181U - Recovery system of cold hydrogenation tail gas condensate - Google Patents
Recovery system of cold hydrogenation tail gas condensate Download PDFInfo
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- CN210656181U CN210656181U CN201921673694.XU CN201921673694U CN210656181U CN 210656181 U CN210656181 U CN 210656181U CN 201921673694 U CN201921673694 U CN 201921673694U CN 210656181 U CN210656181 U CN 210656181U
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Abstract
The utility model discloses a recovery system of cold hydrogenation tail gas condensate, it includes silicon tetrachloride storage tank, vaporizer, steam heater, primary heater, secondary heater, tertiary heater, fluidized bed reactor, hydrogen source, silica flour storage tank, quench tower, air cooler, water cooler, first freon cooler, chlorosilane storage tank, tail gas drip washing tower, second freon cooler, alkali drip washing tower and controller. Has the advantages that: the utility model has simple connection relation and easy realization, realizes the recovery of the chlorosilane, and avoids the waste of the chlorosilane; the production cost is reduced; the normal operation of the quench tower is ensured, and the working efficiency is further ensured; manual cleaning is not needed, contact between a cleaner and the high polymer is avoided, and safety of the cleaner is guaranteed; meanwhile, the cleaning efficiency is improved.
Description
The technical field is as follows:
the utility model relates to a recovery system, in particular to recovery system of cold hydrogenation tail gas condensate.
Background art:
the process technology for preparing the polysilicon at the present stage in China is basically allIs a siemens process technology, and a very important link in the process technology is the production of trichlorosilane (one of raw materials for preparing polysilicon) by cold hydrogenation of silicon tetrachloride. The cold hydrogenation system is adopted by most domestic manufacturers at present. The system sequentially comprises a silicon tetrachloride storage tank, a vaporizer, a heat exchanger, a primary heater, a secondary heater, a tertiary heater, a fluidized bed reactor, a quench tower, an air cooler, a water cooler and a Freon cooler according to the material trend; the method comprises the following steps that silicon tetrachloride liquid is gasified by a vaporizer in sequence, the heat exchanger, a first-stage heater, a second-stage heater and a third-stage heater are heated to form high-temperature gaseous silicon tetrachloride, then silicon tetrachloride gas, hydrogen and silicon powder are sent to a fluidized bed reactor to be hydrogenated, part of the silicon tetrachloride is converted into trichlorosilane, and the reaction equation is as follows: 3SiCl4+Si+2H2＝4SiHCl3(ii) a The converted mixed gas is sequentially cooled by a quench tower, an air cooler, a water cooler and a Freon cooler to obtain mixed chlorosilane liquid, and the mixed chlorosilane liquid is separated by a separation system to obtain trichlorosilane; the system has the following disadvantages: 1. the noncondensable gas cooled by the Freon cooler is directly sent to an alkali leaching tower for treatment, the treated gas is discharged, and the washed liquid is sent to a sewage treatment station for water treatment, so that chlorosilane contained in the gas is wasted, the sewage treatment capacity is increased, and the production cost is increased; 2. after the reaction in the fluidized bed reactor is finished, chlorosilane gas and a small amount of silicon powder are generated, the chlorosilane gas carries the silicon powder into a quenching tower, and chlorosilane liquid in the quenching tower sprays mixed gas in the quenching tower through a circulating pump to cool and remove the silicon powder; the circulating pump is seriously abraded due to more silicon powder and higher hardness of the silicon powder in the chlorosilane gas entering the quenching tower, the operation cycle of 316 materials is 7-12 days, the operation cycle is 3-5 days under the condition of higher solid content, the operation cycle of special materials is 8-15 days, and the service life is short; the maintenance and replacement period is long, and the normal operation of the quenching tower is seriously influenced; 3. the pipeline of the inlet of present circulating pump is very easily blockked up by solid wastes such as silica flour, and the quench tower that needs the shut down carries out artifical clearance because the solid wastes in the quench tower contains the high polymer, and is flammable and explosive and poisonousTherefore, when cleaning, a cleaning worker has potential safety hazards.
The utility model has the following contents:
an object of the utility model is to provide a relation of connection is simple, has realized that chloroethane retrieves in the tail gas, has guaranteed the recovery system of quench tower normal operating's cold hydrogenation tail gas condensate.
The utility model discloses by following technical scheme implement: a recovery system of cold hydrogenation tail gas condensate comprises a silicon tetrachloride storage tank, a vaporizer, a steam heater, a primary heater, a secondary heater, a tertiary heater, a fluidized bed reactor, a hydrogen source, a silicon powder storage tank, a quench tower, an air cooler, a water cooler, a first freon cooler, a chlorosilane storage tank, a tail gas leaching tower, a second freon cooler, an alkali leaching tower and a controller; the silicon tetrachloride storage tank, the vaporizer, the steam heater, the primary heater, the secondary heater, the tertiary heater and the fluidized bed reactor are sequentially communicated; the discharge hole of the silicon powder storage tank is connected with the feed inlet of the fluidized bed reactor, and the hydrogen source is communicated with the air inlet of the fluidized bed reactor; the fluidized bed reactor, the quenching tower, the air cooler, the water cooler and the first Freon cooler are sequentially communicated; the liquid outlets of the air cooler, the water cooler and the first Freon cooler are communicated with the liquid inlet of the chlorosilane storage tank; the liquid outlet of the chlorosilane storage tank is communicated with the liquid inlet of the tail gas leaching tower through a pipeline; the gas outlet of the first freon cooler is communicated with the gas inlet of the tail gas leaching tower through a pipeline, the liquid outlet of the tail gas leaching tower is respectively communicated with the chlorosilane storage tank and the liquid inlet of the second freon cooler through pipelines, a shut-off valve is arranged on the pipeline between the liquid outlet of the tail gas leaching tower and the liquid inlet of the chlorosilane storage tank, and the liquid outlet of the second freon cooler is communicated with the liquid inlet of the tail gas leaching tower through a pipeline; the gas outlet of the tail gas leaching tower is communicated with the gas inlet of the alkali leaching tower through a pipeline; a first liquid level sensor is arranged in the tail gas leaching tower; the signal output end of the first liquid level sensor is in signal connection with the signal input end of the controller; and the signal output end of the controller is in signal connection with the signal input end of the shutoff valve.
Further, the device also comprises a nitrogen source and a recovery tank; a horizontal pipe is communicated and arranged at the air inlet of the tail gas leaching tower; the air outlet of the first Freon cooler is communicated with the air inlet of the horizontal pipe through a pipeline; a liquid discharge pipe is arranged at the bottom of the horizontal pipe, one end of the liquid discharge pipe is communicated with the horizontal pipe, and the other end of the liquid discharge pipe is communicated with a liquid inlet of the recovery tank through a pipeline; the nitrogen source is communicated with the air inlet of the recovery tank through a pipeline, and a control valve is arranged on the pipeline between the nitrogen source and the recovery tank; a liquid outlet of the recovery tank is communicated with a liquid inlet of the chlorosilane storage tank through a pipeline, a valve is arranged on the pipeline between the recovery tank and the chlorosilane storage tank, and a second liquid level sensor and a pressure sensor are arranged in the recovery tank; the signal output ends of the second liquid level sensor and the pressure sensor are in signal connection with the signal input end of the controller; and the signal output end of the controller is respectively connected with the signal input ends of the control valve and the valve through signals.
Further, the device also comprises a circulating pump, a stripping tower, a hydrogen heater, a third liquid level sensor, a temperature sensor and a slag slurry dryer; a liquid outlet of the chlorosilane storage tank is communicated with a liquid inlet of the quenching tower through a pipeline, and a conveying pump is arranged on the pipeline between the chlorosilane storage tank and the quenching tower; the liquid outlet of the quenching tower is respectively communicated with the liquid inlets of the circulating pump and the stripping tower through pipelines; a liquid outlet of the circulating pump is respectively communicated with liquid inlets of the quenching tower and the stripping tower through pipelines; electromagnetic valves are respectively arranged on a pipeline between the circulating pump and the quenching tower and a pipeline between the circulating pump and the stripping tower, and stop valves are arranged on a pipeline between the quenching tower and the stripping tower; a pipeline between the quenching tower and the stop valve is communicated with one end of a liquid conveying pipe, and the other end of the liquid conveying pipe is communicated with a liquid outlet of the silicon tetrachloride storage tank; a flushing pump is arranged on the infusion tube; the hydrogen source is communicated with the gas inlet of the hydrogen heater through a pipeline, the gas outlet of the hydrogen heater is communicated with the gas inlet of the stripping tower through a pipeline, the gas outlet of the stripping tower is communicated with the gas inlet of the quenching tower through a pipeline, and the slag discharge port of the stripping tower is communicated with the slag inlet of the slag slurry dryer through a pipeline; the signal output ends of the third liquid level sensor and the temperature sensor are in signal connection with the signal input end of the controller; the signal output end of the controller is in signal connection with the signal input ends of the delivery pump, the circulating pump, the electromagnetic valve, the stop valve and the flushing pump.
The utility model has the advantages that: 1. the utility model has simple connection relation and easy realization, realizes the recovery of chlorosilane through the tail gas leaching tower, avoids the waste of chlorosilane, reduces the using amount of alkali liquor in the alkali leaching tower, and further reduces the water treatment capacity of the sewage treatment station; the production cost is reduced; 2. when the circulating pump is overhauled, the waste residue solution at the bottom of the quenching tower can be normally discharged into the stripping tower, the quenching tower does not need to be stopped, the normal operation of the quenching tower is ensured, and the working efficiency is further ensured; 3. the method has the advantages that silicon tetrachloride solution is used as flushing fluid, when a circulating pump is overhauled, the electromagnetic valve is closed, the stop valve and the flushing pump are opened, the silicon tetrachloride solution flushes a pipeline between the quenching tower and the circulating pump, and waste residue solution and the silicon tetrachloride solution in the quenching tower are mixed and conveyed to the stripping tower without manual cleaning, so that a cleaning worker is prevented from contacting with a high polymer, and the safety of the cleaning worker is ensured; meanwhile, the cleaning efficiency is improved.
Description of the drawings:
in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a schematic view of the overall structure of the embodiment of the present invention.
Fig. 2 is a system control diagram according to an embodiment of the present invention.
The system comprises a silicon tetrachloride storage tank 1, a vaporizer 2, a steam heater 3, a primary heater 4, a secondary heater 5, a tertiary heater 6, a fluidized bed reactor 7, a hydrogen source 8, a silicon powder storage tank 9, a quenching tower 10, an air cooler 11, a water cooler 12, a first freon cooler 13, a chlorosilane storage tank 14, a tail gas leaching tower 15, a second freon cooler 16, an alkali leaching tower 17, a controller 18, a nitrogen source 19, a recovery tank 20, a circulating pump 21, a stripping tower 22, a hydrogen heater 23, a third liquid level sensor 24, a temperature sensor 25, a slurry dryer 26, a shut-off valve 27, a first liquid level sensor 28, a horizontal pipe 29, a liquid discharge pipe 30, a control valve 31, a valve 32, a second liquid level sensor 33, a delivery pump 34, an electromagnetic valve 35, a stop valve 36, a liquid conveying pipe 37, a flushing pump 38 and a pressure sensor 39.
The specific implementation mode is as follows:
as shown in fig. 1-2, a recovery system of cold hydrogenation tail gas condensate comprises a silicon tetrachloride storage tank 1, a vaporizer 2, a steam heater 3, a primary heater 4, a secondary heater 5, a tertiary heater 6, a fluidized bed reactor 7, a hydrogen source 8, a silicon powder storage tank 9, a quench tower 10, an air cooler 11, a water cooler 12, a first freon cooler 13, a chlorosilane storage tank 14, a tail gas leaching tower 15, a second freon cooler 16, an alkali leaching tower 17, a controller 18, a nitrogen source 19, a recovery tank 20, a circulating pump 21, a stripping tower 22, a hydrogen heater 23, a third liquid level sensor 24, a temperature sensor 25 and a slag slurry dryer 26; the silicon tetrachloride storage tank 1, the vaporizer 2, the steam heater 3, the primary heater 4, the secondary heater 5, the tertiary heater 6 and the fluidized bed reactor 7 are sequentially communicated; a discharge hole of the silicon powder storage tank 9 is connected with a feed inlet of the fluidized bed reactor 7, and a hydrogen source 8 is communicated with an air inlet of the fluidized bed reactor 7; the fluidized bed reactor 7, the quenching tower 10, the air cooler 11, the water cooler 12 and the first Freon cooler 13 are sequentially communicated; the liquid outlets of the air cooler 11, the water cooler 12 and the first freon cooler 13 are communicated with the liquid inlet of the chlorosilane storage tank 14; a liquid outlet of the chlorosilane storage tank 14 is communicated with a liquid inlet of the tail gas leaching tower 15 through a pipeline; the gas outlet of the first freon cooler 13 is communicated with the gas inlet of the tail gas leaching tower 15 through a pipeline, the liquid outlet of the tail gas leaching tower 15 is respectively communicated with the liquid inlets of the chlorosilane storage tank 14 and the second freon cooler 16 through pipelines, a shut-off valve 27 is arranged on the pipeline between the liquid outlet of the tail gas leaching tower 15 and the liquid inlet of the chlorosilane storage tank 14, and the liquid outlet of the second freon cooler 16 is communicated with the liquid inlet of the tail gas leaching tower 15 through a pipeline; the gas outlet of the tail gas leaching tower 15 is communicated with the gas inlet of the alkali leaching tower 17 through a pipeline; a first level sensor 28 is arranged in the off-gas washing column 15.
A horizontal pipe 29 is communicated with the air inlet of the tail gas leaching tower 15; the air outlet of the first Freon cooler 13 is communicated with the air inlet of the horizontal pipe 29 through a pipeline; the liquid discharge pipe 30 is arranged at the bottom of the horizontal pipe 29, one end of the liquid discharge pipe 30 is communicated with the horizontal pipe 29, and the other end of the liquid discharge pipe 30 is communicated with the liquid inlet of the recovery tank 20 through a pipeline, so that the situation that gas is condensed into liquid and accumulated in the horizontal pipe 29 to block the horizontal pipe 29 when the ambient temperature is low is prevented, the situation that high pressure occurs in the system due to the blocking of the horizontal pipe 29 is avoided, the problem that the shaft seal of the slurry dryer 26 is blocked due to the high pressure is further avoided, and the normal operation of the slurry dryer 26 is ensured; the nitrogen source 19 is communicated with the air inlet of the recovery tank 20 through a pipeline, and a control valve 31 is arranged on the pipeline between the nitrogen source 19 and the recovery tank 20; a liquid outlet of the recovery tank 20 is communicated with a liquid inlet of the chlorosilane storage tank 14 through a pipeline, a valve 32 is arranged on the pipeline between the recovery tank 20 and the chlorosilane storage tank 14, and a second liquid level sensor 33 and a pressure sensor 39 are arranged in the recovery tank 20;
a liquid outlet of the chlorosilane storage tank 14 is communicated with a liquid inlet of the quenching tower 10 through a pipeline, and a conveying pump 34 is arranged on the pipeline between the chlorosilane storage tank 14 and the quenching tower 10; the liquid outlet of the quenching tower 10 is respectively communicated with the liquid inlets of the circulating pump 21 and the stripping tower 22 through pipelines; the liquid outlet of the circulating pump 21 is respectively communicated with the liquid inlets of the quenching tower 10 and the stripping tower 22 through pipelines; electromagnetic valves 35 are respectively arranged on a pipeline between the circulating pump 21 and the quenching tower 10 and a pipeline between the circulating pump 21 and the stripping tower 22, and a stop valve 36 is arranged on a pipeline between the quenching tower 10 and the stripping tower 22; a pipeline between the quenching tower 10 and the stop valve 36 is communicated with one end of a liquid conveying pipe 37, and the other end of the liquid conveying pipe 37 is communicated with a liquid outlet of the silicon tetrachloride storage tank 1; a flushing pump 38 is arranged on the infusion tube 37; the hydrogen source 8 is communicated with the gas inlet of the hydrogen heater 23 through a pipeline, the gas outlet of the hydrogen heater 23 is communicated with the gas inlet of the stripping tower 22 through a pipeline, the gas outlet of the stripping tower 22 is communicated with the gas inlet of the quenching tower 10 through a pipeline, and the slag discharge port of the stripping tower 22 is communicated with the slag inlet of the slag slurry dryer 26 through a pipeline.
The signal output ends of the first liquid level sensor 28, the second liquid level sensor 33, the third liquid level sensor 24, the pressure sensor 39 and the temperature sensor 25 are all connected with the signal input end of the controller 18 through signals; the signal outputs of the controller 18 are connected by signals to the signal inputs of the shut-off valve 27, the control valve 31, the valve 32, the feed pump 34, the circulation pump 21, the solenoid valve 35, the shut-off valve 36 and the flushing pump 38.
The working process is as follows: the raw material silicon tetrachloride liquid is gasified and heated by a vaporizer 2, a steam heater 3, a primary heater 4, a secondary heater 5 and a tertiary heater 6, is sent into a fluidized bed reactor 7, hydrogen and silicon powder are also added into the fluidized bed reactor 7, silicon tetrachloride, the hydrogen and the silicon powder react in the fluidized bed reactor 7 to form high-temperature chlorosilane mixed gas carrying the silicon powder, then the mixed gas enters a quenching tower 10, circulating chlorosilane liquid through a circulating pump 21 to spray and cool the gas and remove silicon powder, conveying the chlorosilane liquid containing the silicon powder at the bottom of the quenching tower 10 into a stripping tower 22 through the circulating pump 21 to perform gas stripping, introducing hydrogen at the temperature of 350 ℃ into the stripping tower 22 to perform gas stripping on the chlorosilane liquid, discharging the slag slurry stripped by the stripping tower 22 out of the stripping tower 22, and then, drying the slag slurry in a slag slurry dryer 26; chlorosilane gas extracted from gas in the stripping tower 22 is sent to the quenching tower 10, spraying and cooling are carried out again, silicon powder is removed, the cooled gas sequentially passes through the air cooler 11, the water cooler 12 and the first freon cooler 13 to be condensed, liquid condensed by the air cooler 11, the water cooler 12 and the first freon cooler 13 is sent to the chlorosilane storage tank 14, non-condensable gas in the first freon cooler 13 is sent to the tail gas leaching tower 15, then chlorosilane liquid at the bottom of the tail gas leaching tower 15 is cooled by the second freon cooler 16 and then is sprayed downwards from the top in the tail gas leaching tower 15, chlorosilane in the non-condensable gas is recovered, the liquid level of the liquid in the tail gas leaching tower 15 is detected by the first liquid level sensor 28 at all times, and signals are transmitted to the controller 18; when the detected liquid level value reaches the set highest value, the controller 18 controls the shut-off valve 27 to be opened, liquid in the tail gas leaching tower 15 is conveyed to the chlorosilane storage tank 14, and when the liquid level value of the liquid in the tail gas leaching tower 15 reaches the set lowest value, the controller 18 controls the shut-off valve 27 to be closed; the liquid accumulated in the horizontal pipe 29 is discharged to the recovery tank 20 from the liquid discharge pipe 30 at the bottom, and the second liquid level sensor 33 detects the liquid level of the liquid in the recovery tank 20 at any moment and transmits a signal to the controller 18; when the detected liquid level value reaches the set maximum value, the controller 18 controls the control valve 31 and the valve 32 to be opened, nitrogen enters the recovery tank 20 to increase the pressure in the recovery tank 20, so that the liquid in the recovery tank 20 is pressed into the chlorosilane storage tank 14, the pressure sensor 39 detects the pressure change in the recovery tank 20 at any moment and transmits a signal to the controller 18, and when the detected pressure value reaches the set value, the controller 18 controls the control valve 31 to be closed, so that the situation that the pressure in the recovery tank 20 is too high and danger is caused is prevented; when the level value detected by the second level sensor 33 reaches a set minimum value, the controller 18 controls the valve 32 to close.
A third level sensor 24 in the quench tower 10 constantly detects the level of the liquid in the quench tower 10 and transmits a signal to the controller 18; when the detected liquid level value is lower than the set lowest value, the controller 18 controls the conveying pump 34 to operate, so that the chlorosilane liquid in the chlorosilane storage tank 14 is supplemented into the quenching tower 10; when the detected liquid level value reaches the set highest value, the controller 18 controls the delivery pump 34 to stop running; the temperature sensor 25 in the quenching tower 10 constantly detects the temperature in the quenching tower 10 and transmits a signal to the controller 18; when the detected temperature is higher than 160 ℃, which indicates that the circulating pump 21 is damaged, the controller 18 controls the circulating pump 21 to stop, the electromagnetic valve 35 to close, and simultaneously controls the flushing pump 38 to start, and the stop valve 36 to open; the maintenance personnel can start to maintain the circulating pump 21, liquid in the quenching tower 10 is directly conveyed into the stripping tower 22 for gas stripping under the action of the silicon tetrachloride solution, the quenching tower 10 does not need to be stopped, the normal operation of the quenching tower 10 is ensured, the working efficiency is further ensured, the silicon tetrachloride solution also washes a pipeline between the quenching tower 10 and the circulating pump 21, manual cleaning is not needed, contact between a cleaning worker and a high polymer is avoided, and the safety of the cleaning worker is ensured; meanwhile, the cleaning efficiency is improved; the utility model discloses the relation of connection is simple, easily realizes.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (3)
1. A recovery system for cold hydrogenation tail gas condensate is characterized by comprising a silicon tetrachloride storage tank, a vaporizer, a steam heater, a primary heater, a secondary heater, a tertiary heater, a fluidized bed reactor, a hydrogen source, a silicon powder storage tank, a quench tower, an air cooler, a water cooler, a first freon cooler, a chlorosilane storage tank, a tail gas leaching tower, a second freon cooler, an alkali leaching tower and a controller; the silicon tetrachloride storage tank, the vaporizer, the steam heater, the primary heater, the secondary heater, the tertiary heater and the fluidized bed reactor are sequentially communicated; the discharge hole of the silicon powder storage tank is connected with the feed inlet of the fluidized bed reactor, and the hydrogen source is communicated with the air inlet of the fluidized bed reactor; the fluidized bed reactor, the quenching tower, the air cooler, the water cooler and the first Freon cooler are sequentially communicated; the liquid outlets of the air cooler, the water cooler and the first Freon cooler are communicated with the liquid inlet of the chlorosilane storage tank; the liquid outlet of the chlorosilane storage tank is communicated with the liquid inlet of the tail gas leaching tower through a pipeline; the gas outlet of the first freon cooler is communicated with the gas inlet of the tail gas leaching tower through a pipeline, the liquid outlet of the tail gas leaching tower is respectively communicated with the chlorosilane storage tank and the liquid inlet of the second freon cooler through pipelines, a shut-off valve is arranged on the pipeline between the gas inlet of the tail gas leaching tower and the liquid inlet of the chlorosilane storage tank, and the liquid outlet of the second freon cooler is communicated with the liquid inlet of the tail gas leaching tower through a pipeline; the gas outlet of the tail gas leaching tower is communicated with the gas inlet of the alkali leaching tower through a pipeline; a first liquid level sensor is arranged in the tail gas leaching tower; the signal output end of the first liquid level sensor is in signal connection with the signal input end of the controller; and the signal output end of the controller is in signal connection with the signal input end of the shutoff valve.
2. A cold hydrogenated tail gas condensate recovery system according to claim 1, further comprising a nitrogen source and a recovery tank; a horizontal pipe is communicated and arranged at the air inlet of the tail gas leaching tower; the air outlet of the first Freon cooler is communicated with the air inlet of the horizontal pipe through a pipeline; a liquid discharge pipe is arranged at the bottom of the horizontal pipe, one end of the liquid discharge pipe is communicated with the horizontal pipe, and the other end of the liquid discharge pipe is communicated with a liquid inlet of the recovery tank through a pipeline; the nitrogen source is communicated with the air inlet of the recovery tank through a pipeline, and a control valve is arranged on the pipeline between the nitrogen source and the recovery tank; a liquid outlet of the recovery tank is communicated with a liquid inlet of the chlorosilane storage tank through a pipeline, a valve is arranged on the pipeline between the recovery tank and the chlorosilane storage tank, and a second liquid level sensor and a pressure sensor are arranged in the recovery tank; the signal output ends of the second liquid level sensor and the pressure sensor are in signal connection with the signal input end of the controller; and the signal output end of the controller is respectively connected with the signal input ends of the control valve and the valve through signals.
3. The recovery system of cold hydrogenation tail gas condensate as claimed in claim 1 or 2, further comprising a circulation pump, a stripping tower, a hydrogen heater, a third liquid level sensor, a temperature sensor and a slurry dryer; a liquid outlet of the chlorosilane storage tank is communicated with a liquid inlet of the quenching tower through a pipeline, and a conveying pump is arranged on the pipeline between the chlorosilane storage tank and the quenching tower; the liquid outlet of the quenching tower is respectively communicated with the liquid inlets of the circulating pump and the stripping tower through pipelines; a liquid outlet of the circulating pump is respectively communicated with liquid inlets of the quenching tower and the stripping tower through pipelines; electromagnetic valves are respectively arranged on a pipeline between the circulating pump and the quenching tower and a pipeline between the circulating pump and the stripping tower, and stop valves are arranged on a pipeline between the quenching tower and the stripping tower; a pipeline between the quenching tower and the stop valve is communicated with one end of a liquid conveying pipe, and the other end of the liquid conveying pipe is communicated with a liquid outlet of the silicon tetrachloride storage tank; a flushing pump is arranged on the infusion tube; the hydrogen source is communicated with the gas inlet of the hydrogen heater through a pipeline, the gas outlet of the hydrogen heater is communicated with the gas inlet of the stripping tower through a pipeline, the gas outlet of the stripping tower is communicated with the gas inlet of the quenching tower through a pipeline, and the slag discharge port of the stripping tower is communicated with the slag inlet of the slag slurry dryer through a pipeline; the signal output ends of the third liquid level sensor and the temperature sensor are in signal connection with the signal input end of the controller; the signal output end of the controller is in signal connection with the signal input ends of the delivery pump, the circulating pump, the electromagnetic valve, the stop valve and the flushing pump.
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| CN201921673694.XU CN210656181U (en) | 2019-10-08 | 2019-10-08 | Recovery system of cold hydrogenation tail gas condensate |
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