CN116658819A - SF6 recovery device and method with recovery rate measurement function - Google Patents
SF6 recovery device and method with recovery rate measurement function Download PDFInfo
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- CN116658819A CN116658819A CN202310549069.9A CN202310549069A CN116658819A CN 116658819 A CN116658819 A CN 116658819A CN 202310549069 A CN202310549069 A CN 202310549069A CN 116658819 A CN116658819 A CN 116658819A
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- 238000005259 measurement Methods 0.000 title claims description 18
- 239000007788 liquid Substances 0.000 claims abstract description 14
- 238000012544 monitoring process Methods 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims 16
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- 230000033228 biological regulation Effects 0.000 description 2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/02—Pipe-line systems for gases or vapours
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/20—Arrangements or systems of devices for influencing or altering dynamic characteristics of the systems, e.g. for damping pulsations caused by opening or closing of valves
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D3/00—Arrangements for supervising or controlling working operations
- F17D3/01—Arrangements for supervising or controlling working operations for controlling, signalling, or supervising the conveyance of a product
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D5/00—Protection or supervision of installations
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Abstract
An SF6 recovery device and method with recovery rate measuring function, the device includes: the device comprises a first buffer tank, a second buffer tank, an external liquid storage tank and a PLC controller, wherein an input port of the first buffer tank is connected with an air charging and discharging interface through a first pipeline, and a temperature sensor, a first pressure sensor, a first electromagnetic valve and a first compressor are arranged on the first pipeline; the output port of the first buffer tank is connected with the input port of the second buffer tank through a second pipeline and a third pipeline, and a second electromagnetic valve, a pressure reducing valve, a mass flow controller and a fourth electromagnetic valve are sequentially arranged on the second pipeline; a third electromagnetic valve and a fifth electromagnetic valve are sequentially arranged on the third pipeline; the output port of the second buffer tank is connected with an external liquid storage tank through a fourth pipeline, and the fourth pipeline is provided with a proportional valve and a second compressor. The invention can accurately measure the recovery rate, the air chamber air volume, the effective volume and other data without reducing the recovery speed, and can completely calculate the recovery rate and the recovery amount in the whole recovery process.
Description
Technical Field
The invention relates to the field of SF6 gas recovery, in particular to an SF6 recovery device and method with a recovery rate measurement function.
Background
The recovery rate of SF6 gas in the recovery process is accurately mastered, and the data such as the gas quantity and the effective volume of the gas chamber of the inflating equipment are obtained, so that the SF6 gas management and control is enhanced, and an important way for realizing the full life cycle lean management of the SF6 gas is provided. As shown in figure 1, the method for measuring recovery rate in the prior art mainly comprises the steps of connecting a recovery rate measuring device in series between an air chamber inflation and deflation interface and an SF6 recovery device connecting pipeline, detecting the pressure and the temperature of the air chamber and the pressure of the SF6 recovery device in each recovery stage, and calculating the data of recovery rate, air chamber gas quantity, effective volume and the like according to the output gas quantity of a mass flow controller and combining Betty-Bridgman (Bettie-Bridgman) empirical formulas. The pressure at the front end of the mass flow controller cannot be too high, so that the pressure reducing valve is designed. After a period of recovery, the pressure in the air chamber is reduced, the pressure difference between the front end and the rear end of the mass flow controller does not meet the requirement, the output gas cannot be controlled normally, the electromagnetic valve 2 is required to be opened, and the gas flows out from the bypass.
The prior art mainly has the following problems:
(1) Reducing the recovery speed: the core module of the recovery rate measuring device is a built-in mass flow controller, and plays a role in controlling the SF6 gas flow. In order to realize accurate flow control, the pressure difference of the front end and the rear end of the mass flow controller needs to be kept stable. As the recovery process proceeds, the SF6 gas pressure in the chamber gradually decreases, and therefore a pressure reducing valve is required to be disposed at the front end to fix the front end pressure of the mass flow controller at a certain value. Compared with the air chamber inflation and deflation interface which is directly connected with the SF6 recovery device, the existence of the pressure reducing valve can reduce the recovery speed. In addition, the mass flow controller can control the SF6 gas flow and simultaneously can have an effect of blocking the gas flow, so that the recovery speed is reduced.
(2) The measurement error is larger: the pressure difference between the front end and the rear end of the mass flow controller affects the flow control error, the front end can keep stable pressure by the pressure reducing valve, but the rear end is connected with the SF6 recovery device, and the pressure difference between the front end and the rear end of the flowmeter is unstable due to the fact that the pressure of the rear end of the flowmeter is unstable as the recovery process (the internal pressure of the recovery device increases) and the flow control error is large.
(3) All recovery rates could not be accurately measured: when the pressure of the air chamber is reduced to a certain degree, the pressure reducing valve and the mass flow controller can seriously disturb the recovery speed, and only the pipelines where the pressure reducing valve and the mass flow controller are located can be bypassed, so that the gas cannot be calculated from a bypass, and the measurement result is inaccurate.
Disclosure of Invention
The invention provides an SF6 recovery device and method with recovery rate measurement function, which can accurately measure recovery rate, air chamber air volume, effective volume and other data without reducing recovery rate; in addition, the pressure difference between the front end and the rear end of the mass flow controller is kept stable in the whole process, the flow control is accurate, and the recovery rate and the recovery quantity in the whole recovery process can be completely calculated.
The SF6 recovery device with the recovery rate measurement function comprises a first buffer tank, a second buffer tank, an external liquid storage tank and a PLC controller, wherein an input port of the first buffer tank is connected with an inflation and deflation interface through a first pipeline, a temperature sensor, a first pressure sensor, a first electromagnetic valve and a first compressor are arranged on the first pipeline, and a second pressure sensor is arranged on the first buffer tank; the output port of the first buffer tank is connected with the input port of the second buffer tank through a second pipeline and a third pipeline, a second electromagnetic valve, a pressure reducing valve, a mass flow controller and a fourth electromagnetic valve are sequentially arranged on the second pipeline, and a third pressure sensor is arranged on the second buffer tank; a third electromagnetic valve and a fifth electromagnetic valve are sequentially arranged on the third pipeline; the output port of the second buffer tank is connected with an external liquid storage tank through a fourth pipeline, and the fourth pipeline is provided with a proportional valve and a second compressor; the temperature sensor, the pressure sensors, the electromagnetic valves, the compressors, the pressure reducing valve, the mass flow controller and the proportional valve are all connected with the PLC.
Further, the temperature sensor and the first pressure sensor are respectively used for measuring the initial temperature T of the air chamber of the air charging equipment 0 And an initial pressure P 0 The PLC is used for controlling the initial temperature T of the air chamber of the air charging equipment according to the measurement 0 And an initial pressure P 0 The gas density rho of the gas chamber before recovery is calculated by a Di-Bridgman empirical formula 0 。
Further, the second pressure sensor 8 is used for monitoring the pressure P of the first buffer tank in real time during the recovery process b If a first buffer tankMedium pressure P b Below (P) a +0.05) MPa, the PLC controls the second electromagnetic valve, the fourth electromagnetic valve and the mass flow controller to be closed until the pressure P in the first buffer tank b Above (P) a +0.05) MPa restart, wherein P a Is the pressure after the pressure is reduced by the pressure reducing valve.
Further, the third pressure sensor is used for monitoring the pressure P of the second buffer tank in real time in the recovery process c The PLC is used for monitoring the pressure P of the second buffer tank according to the third pressure sensor c Controlling the size of the internal aperture of the proportional valve to enable the pressure P of the second buffer tank c The conditions are satisfied: (P) d -0.03)＜P c ＜(P d +0.03) Mpa, where P d Taking 0.1Mpa.
Further, the PLC is also used for controlling the pressure P in the first buffer tank after SF6 recovery is finished b Below (P) a +0.05) MPa, closing the second electromagnetic valve and the fourth electromagnetic valve, removing the pressure reducing valve and the mass flow controller from the gas path, and calculating the recovery rate, the gas amount and the effective volume.
9. Further, the PLC calculates the recovery rate, the gas amount and the effective volume, and the specific steps include:
the PLC controller is internally provided with a timer, and the output gas time t of the mass flow controller is recorded 1 Output gas volume V 1 ＝t 1 Q, SF6 gas density at normal pressure is ρ SF6 ＝6.0886kg/m 3 The amount of recovered gas in this period of time is m k1 ＝V 1 ×ρ SF6 ；
At t in the first buffer tank 1 Time gas pressure P c1 Temperature is equal to the temperature T of the gas in the gas chamber at the moment 1 Calculating the gas density rho in the first buffer tank by combining an empirical formula c1 The first buffer tank volume V is known c Mass of gas m in the first buffer tank k2 ＝V c ×ρ c1 ；
Calculating the recovery start t 1 Within the time, the gas in the gas chamber is reduced by m s1 ＝m k1 +m k2 ；
According to the temperature T of the air chamber after recovery 1 And pressure P 1 Calculating the gas density rho of the recovered gas chamber by combining an empirical formula 1 The effective volume V of the air chamber can be further calculated:
V＝m s1 /(ρ 0 -ρ 1 )；
the gas amount: m=v×ρ 0 ；
Recovery rate: ζ=m s1 /m。
An SF6 recovery method with recovery measurement function, which is performed by the above device, the method comprising:
(1) Temperature sensor and first pressure sensor measure initial temperature T of inflation device air chamber 0 And an initial pressure P 0 Calculating the gas density rho of the gas chamber before recovery according to a Di-Bridgman empirical formula 0 ；
(2) Opening the first electromagnetic valve, the second electromagnetic valve and the fourth electromagnetic valve, opening the pressure reducing valve and the proportional valve 18, and starting the first compressor and the second compressor; wherein the pressure after the pressure reduction by the pressure reducing valve is set to be P a The output flow of the mass flow controller is Qm 3 /h；
(3) The second pressure sensor and the third pressure sensor respectively monitor the pressure of the first buffer tank and the pressure of the second buffer tank in real time in the recovery process, if the pressure P in the first buffer tank b Below (P) a +0.05) MPa, closing the second electromagnetic valve, the fourth electromagnetic valve and the mass flow controller until the pressure P in the first buffer tank b Above (P) a +0.05) MPa re-opening; the PLC monitors the pressure P of the second buffer tank according to the third pressure sensor c Controlling the size of the internal aperture of the proportional valve to enable the pressure P of the second buffer tank c The conditions are satisfied: (P) d -0.03)＜P c ＜(P d +0.03) Mpa, where P d Taking 0.1Mpa;
(4) After SF6 recovery is completed, and the pressure P in the first buffer tank b Below (P) a +0.05) MPa, closing the second electromagnetic valve and the fourth electromagnetic valve, removing the pressure reducing valve and the mass flow controller from the gas path, and calculatingRecovery rate, gas amount and effective volume;
(5) After the calculation is completed, the third electromagnetic valve and the fifth electromagnetic valve are opened, and residual gas in the first buffer tank is completely recovered into the liquid storage tank by the second compressor for liquefaction and storage.
Further, the PLC calculates the recovery rate, the gas amount and the effective volume, and the specific steps include:
the PLC controller is internally provided with a timer, and the output gas time t of the mass flow controller is recorded 1 Output gas volume V 1 ＝t 1 Q, SF6 gas density at normal pressure is ρ SF6 ＝6.0886kg/m 3 The amount of recovered gas in this period of time is m k1 ＝V 1 ×ρ SF6 ；
At t in the first buffer tank 1 Time gas pressure P c1 Temperature is equal to the temperature T of the gas in the gas chamber at the moment 1 Calculating the gas density rho in the first buffer tank by combining an empirical formula c1 The first buffer tank volume V is known c Mass of gas m in the first buffer tank k2 ＝V c ×ρ c1 ；
Calculating the recovery start t 1 Within the time, the gas in the gas chamber is reduced by m s1 ＝m k1 +m k2 ；
According to the temperature T of the air chamber after recovery 1 And pressure P 1 Calculating the gas density rho of the recovered gas chamber by combining an empirical formula 1 The effective volume V of the air chamber can be further calculated:
V＝m s1 /(ρ 0 -ρ 1 )；
the gas amount: m=v×ρ 0 ；
Recovery rate: ζ=m s1 /m。
Further, a vacuum gauge and a vacuum pump are arranged on a pipeline between the third electromagnetic valve and the fifth electromagnetic valve, the output end of the vacuum pump is communicated with the exhaust port, and the vacuum gauge and the vacuum pump are connected with the PLC.
Further, if the device needs to be vacuumized, the second electromagnetic valve and the fourth electromagnetic valve are closed, the first electromagnetic valve, the third electromagnetic valve and the fifth electromagnetic valve are opened, the vacuum pump is started to discharge residual gas, and vacuumizing is stopped when the pressure of the vacuum gauge is detected to be lower than 10 Pa.
According to the invention, through dual regulation and control of the pressure reducing valve and the proportional valve, the stability of the pressure difference between the front end and the rear end of the mass flow controller is ensured, and the flow output accuracy is improved; the front end of the pressure reducing valve is provided with a first buffer tank, and the recovery gas firstly enters the first buffer tank without reducing the pressure of the pressure reducing valve, so that the recovery speed is not reduced; the pressure of the front end of the pressure reducing valve is always kept in a set range, the mass flow controller can still output gas even when the air pressure of the air chamber in the later recovery period is low, the gas quantity of all the recovered gas can be measured, and the recovery rate and recovery quantity of the whole process can be completely calculated.
Drawings
FIG. 1 is a schematic diagram of a prior art SF6 recovery measurement device and SF6 recovery device combined;
fig. 2 is a schematic structural diagram of an SF6 recovery apparatus with recovery measurement function according to an embodiment of the present invention.
Reference numerals in the drawings are described as follows: 1-first buffer tank, 2-second buffer tank, 3-external liquid storage tank, 4-temperature sensor, 5-first pressure sensor, 6-first solenoid valve, 7-first compressor, 8-second pressure sensor, 9-second solenoid valve, 10-relief valve, 11-mass flow controller, 12-fourth solenoid valve, 13-third pressure sensor, 14-third solenoid valve, 15-fifth solenoid valve, 16-vacuum gauge, 17-vacuum pump, 18-proportional valve, 19-vacuum pump, 20-PLC controller.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
As shown in fig. 2, the embodiment of the invention provides an SF6 recovery device with recovery rate measurement function, a recovery rate measurement module is built in the SF6 recovery device, gas is recovered into recovery equipment, recovery rate measurement is performed, and meanwhile, the pressure stability of the front end and the rear end of a mass flow controller 11 is controlled through a pressure reducing valve 10 and a proportional valve 18 respectively, so that flow control errors are reduced.
The SF6 recovery device comprises a first buffer tank 1, a second buffer tank 2, an external liquid storage tank 3 and a PLC (programmable logic controller) 20, wherein an input port of the first buffer tank 1 is connected with an air charging and discharging interface through a first pipeline, a temperature sensor 4, a first pressure sensor 5, a first electromagnetic valve 6 and a first compressor 7 are arranged on the first pipeline, and a second pressure sensor 8 is arranged on the first buffer tank 1;
the output port of the first buffer tank 1 is connected with the input port of the second buffer tank 2 through a second pipeline and a third pipeline, a second electromagnetic valve 9, a pressure reducing valve 10, a mass flow controller 11 and a fourth electromagnetic valve 12 are sequentially arranged on the second pipeline, and a third pressure sensor 13 is arranged on the second buffer tank 2; the third pipeline is sequentially provided with a third electromagnetic valve 14 and a fifth electromagnetic valve 15, a vacuum gauge 16 and a vacuum pump 17 are arranged on the pipeline between the third electromagnetic valve 14 and the fifth electromagnetic valve 15, and the output end of the vacuum pump 17 is communicated with the exhaust port.
The output port of the second buffer tank 2 is connected with the external liquid storage tank 3 through a fourth pipeline, and the fourth pipeline is provided with a proportional valve 18 and a second compressor 19.
The SF6 recovery device has the following working principle:
(1) The air charging and discharging interface and the recovery device of the air charging equipment are connected through a special pipeline, and the temperature sensor 4 and the first pressure sensor 5 measure the initial temperature T of the air chamber of the air charging equipment 0 And an initial pressure P 0 The gas density ρ of the gas chamber before recovery is calculated according to the empirical formula (1) of Ti-Bridgman 0 。
P＝56.2ρT(1+B)- ρ 2 A (1)
A＝74.9(1-0.727×10 -3 ρ)
B＝2.51×10 -3 ρ(1-0.846×10 -3 ρ)
Wherein:
absolute pressure of P-SF 6 gas, unit is MPa;
density of rho-SF 6 gas in kg/m 3 ；
R-gas constant, unit is J, (kg. K), SF6 is 56.2J/(kg. K)
The thermodynamic temperature of the T-SF 6 gas is given in K.
(2) Opening the first electromagnetic valve 6, the second electromagnetic valve 9 and the fourth electromagnetic valve 12, opening the pressure reducing valve 10 and the proportional valve 18, and starting the first compressor 7 and the second compressor 19; wherein the pressure after the depressurization of the pressure reducing valve 10 is set to P a (typically 0.2 MPa), the mass flow controller 11 outputs a flow of Qm 3 And/h (a value in a standard state, the flow rate is required to be larger than the SF6 recovery speed, and the air inlet speed of the first buffer tank 1 is prevented from being larger than the air outlet speed).
(3) The second pressure sensor 8 and the third pressure sensor 13 respectively monitor the pressure of the first buffer tank 1 and the pressure of the second buffer tank 2 in real time in the recovery process, and if the pressure P in the first buffer tank 1 is the same b Below (P) a +0.05) MPa, the second solenoid valve 9, the fourth solenoid valve 12 and the mass flow controller 11 are closed until the pressure P in the first surge tank 1 b Above (P) a +0.05) MPa re-opening;
if the pressure P in the second buffer tank 2 c (equal to the mass flow controller 11 back end pressure) is present: (P) d -0.03)＜P c ＜(P d +0.03) MPa, where P d The pressure difference between the front end and the rear end is generally 0.1MPa, and the aperture of the proportional valve 18 is not required to be adjusted and controlled by the control system; if P c ＞(P d +0.03), the pressure in the second buffer tank 2 is higher, the pressure difference between the front end and the rear end of the mass flow controller 11 is too small, the control system controls the proportional valve 18, the internal aperture is increased, the gas in the second buffer tank 2 is pressurized, liquefied and stored in the liquid storage tank by the second compressor 19, and the pressure P of the gas in the second buffer tank 2 is reduced c Thereby reducing the pressure difference between the front and rear ends of the mass flow controller 11; if P c ＜(P d +0.03), the pressure in the second buffer tank 2 is lower, and the mass flow is controlledThe pressure difference between the front end and the rear end of the preparation device 11 is overlarge, the control system controls the proportional valve 18 to reduce the internal aperture, slow down the pressurizing, liquefying and storing of the gas in the second buffer tank 2 by the second compressor 19 into the liquid storage tank, and improve the gas pressure P in the second buffer tank 2 c Thereby increasing the pressure differential across the mass flow controller 11.
(4) After SF6 recovery is completed and the pressure P in the first buffer tank 1 b Below (P) a +0.05) MPa, closing the second electromagnetic valve 9 and the fourth electromagnetic valve 12, removing the pressure reducing valve 10 and the mass flow controller 11 from the gas path, and calculating the recovery rate, the gas amount and the effective volume:
the PLC controller 20 is internally provided with a timer, and records the output gas time t of the mass flow controller 11 1 Output gas volume V 1 ＝t 1 Q, SF6 gas density at normal pressure is ρ SF6 ＝6.0886kg/m 3 The amount of recovered gas in this period of time is m k1 ＝V 1 ×ρ SF6 。
At t in the first buffer tank 1 1 Time gas pressure P c1 Temperature is equal to the temperature T of the gas in the gas chamber at the moment 1 (which can be regarded as a constant gas temperature during recovery), the gas density ρ in the first buffer tank 1 is calculated in combination with an empirical formula c1 The first buffer tank 1 volume V is known c (m 3 ) The mass of gas m in the first buffer tank 1 k2 ＝V c ×ρ c1 。
Thereby calculating the recovery start t 1 Within the time, the gas in the gas chamber is reduced by m s1 ＝m k1 +m k2 。
According to the temperature T of the air chamber after recovery 1 And pressure P 1 Calculating the gas density rho of the recovered gas chamber by combining an empirical formula 1 The effective volume V of the air chamber can be further calculated:
V＝m s1 /(ρ 0 -ρ 1 )
gas amount: m=v×ρ 0
Recovery rate: ζ=m s1 /m
(5) After the data calculation is completed, the third electromagnetic valve 14 and the fifth electromagnetic valve 15 are opened, and all residual gas in the first buffer tank 1 is recovered into the external liquid storage tank 3 by the second compressor 19 for liquefaction and storage.
(6) If the device needs to be vacuumized, the second electromagnetic valve 9 and the fourth electromagnetic valve 12 are closed, the first electromagnetic valve 6, the third electromagnetic valve 14 and the fifth electromagnetic valve 15 are opened, the vacuum pump 17 is started to discharge residual gas, and when the pressure of the vacuum gauge 16 is detected to be lower than 10Pa, the vacuumizing is stopped.
The invention has the following beneficial effects:
(1) The pressure difference at the front end and the rear end of the mass flow controller 11 is ensured to be stable through the dual regulation and control of the pressure reducing valve 10 and the proportional valve 18, and the flow output accuracy is improved;
(2) The front end of the pressure reducing valve 10 is provided with a first buffer tank 1, and the recovery gas firstly enters the first buffer tank 1 without reducing the pressure of the pressure reducing valve 10 and the recovery speed;
(3) The pressure at the front end of the pressure reducing valve 10 is always kept within a set range, the mass flow controller 11 can still output gas even if the air pressure of the air chamber is lower in the later recovery period, all the gas quantity of the recovered gas can be measured, and the recovery rate and recovery quantity of the whole process can be completely calculated;
(4) The recovery device and the measurement device are integrated into one device, so that the device is convenient to use on site.
The foregoing is merely illustrative embodiments of the present invention, and the present invention is not limited thereto, and any changes or substitutions that may be easily contemplated by those skilled in the art within the scope of the present invention should be included in the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the protection scope of the claims.
Claims (10)
1. An SF6 recovery device with recovery rate measurement function, which is characterized in that: the device comprises a first buffer tank, a second buffer tank, an external liquid storage tank and a PLC (programmable logic controller), wherein an input port of the first buffer tank is connected with an inflation and deflation interface through a first pipeline, a temperature sensor, a first pressure sensor, a first electromagnetic valve and a first compressor are arranged on the first pipeline, and a second pressure sensor is arranged on the first buffer tank; the output port of the first buffer tank is connected with the input port of the second buffer tank through a second pipeline and a third pipeline, a second electromagnetic valve, a pressure reducing valve, a mass flow controller and a fourth electromagnetic valve are sequentially arranged on the second pipeline, and a third pressure sensor is arranged on the second buffer tank; a third electromagnetic valve and a fifth electromagnetic valve are sequentially arranged on the third pipeline; the output port of the second buffer tank is connected with an external liquid storage tank through a fourth pipeline, and the fourth pipeline is provided with a proportional valve and a second compressor; the temperature sensor, the pressure sensors, the electromagnetic valves, the compressors, the pressure reducing valve, the mass flow controller and the proportional valve are all connected with the PLC.
2. The SF6 recycling apparatus with recycling rate measuring function according to claim 1, wherein: the temperature sensor and the first pressure sensor are respectively used for measuring the initial temperature T of the air chamber of the air charging equipment 0 And an initial pressure P 0 The PLC is used for controlling the initial temperature T of the air chamber of the air charging equipment according to the measurement 0 And an initial pressure P 0 The gas density rho of the gas chamber before recovery is calculated by a Di-Bridgman empirical formula 0 。
3. The SF6 recycling apparatus with recycling rate measuring function according to claim 2, wherein: the second pressure sensor 8 is used for monitoring the pressure P of the first buffer tank in real time in the recovery process b If the pressure P in the first buffer tank b Below (P) a +0.05) MPa, the PLC controls the second electromagnetic valve, the fourth electromagnetic valve and the mass flow controller to be closed until the pressure P in the first buffer tank b Above (P) a +0.05) MPa restart, wherein P a Is the pressure after the pressure is reduced by the pressure reducing valve.
4. The SF6 recycling apparatus with recycling rate measuring function according to claim 1, wherein: the third pressure sensor is used for monitoring the pressure P of the second buffer tank in real time in the recovery process c The PLC is used for monitoring the pressure of the second buffer tank according to the third pressure sensorP c Controlling the size of the internal aperture of the proportional valve to enable the pressure P of the second buffer tank c The conditions are satisfied: (P) d -0.03)＜P c ＜(P d +0.03) Mpa, where P d Taking 0.1Mpa.
5. The SF6 recycling apparatus with recycling rate measuring function according to claim 3, wherein: the PLC is also used for controlling the pressure P in the first buffer tank after SF6 recovery is finished b Below (P) a +0.05) MPa, closing the second electromagnetic valve and the fourth electromagnetic valve, removing the pressure reducing valve and the mass flow controller from the gas path, and calculating the recovery rate, the gas amount and the effective volume.
6. The SF6 recycling apparatus with recycling rate measuring function according to claim 5, wherein: the PLC calculates the recovery rate, the gas quantity and the effective volume, and the specific steps include:
the PLC controller is internally provided with a timer, and the output gas time t of the mass flow controller is recorded 1 Output gas volume V 1 ＝t 1 Q, SF6 gas density at normal pressure is ρ SF6 ＝6.0886kg/m 3 The amount of recovered gas in this period of time is m k1 ＝V 1 ×ρ SF6 ；
At t in the first buffer tank 1 Time gas pressure P c1 Temperature is equal to the temperature T of the gas in the gas chamber at the moment 1 Calculating the gas density rho in the first buffer tank by combining an empirical formula c1 The first buffer tank volume V is known c Mass of gas m in the first buffer tank k2 ＝V c ×ρ c1 ；
Calculating the recovery start t 1 Within the time, the gas in the gas chamber is reduced by m s1 ＝m k1 +m k2 ；
According to the temperature T of the air chamber after recovery 1 And pressure P 1 Calculating the gas density rho of the recovered gas chamber by combining an empirical formula 1 The effective volume V of the air chamber can be further calculated:
V＝m s1 /(ρ 0 -ρ 1 )；
the gas amount: m=v×ρ 0 ；
Recovery rate: ζ=m s1 /m。
7. A SF6 recovery method with recovery measurement function, characterized in that it is performed with the device according to any of claims 1-6, said method comprising:
(1) Temperature sensor and first pressure sensor measure initial temperature T of inflation device air chamber 0 And an initial pressure P 0 Calculating the gas density rho of the gas chamber before recovery according to a Di-Bridgman empirical formula 0 ；
(2) Opening the first electromagnetic valve, the second electromagnetic valve and the fourth electromagnetic valve, opening the pressure reducing valve and the proportional valve 18, and starting the first compressor and the second compressor; wherein the pressure after the pressure reduction by the pressure reducing valve is set to be P a The output flow of the mass flow controller is Qm 3 /h；
(3) The second pressure sensor and the third pressure sensor respectively monitor the pressure of the first buffer tank and the pressure of the second buffer tank in real time in the recovery process, if the pressure P in the first buffer tank b Below (P) a +0.05) MPa, closing the second electromagnetic valve, the fourth electromagnetic valve and the mass flow controller until the pressure P in the first buffer tank b Above (P) a +0.05) MPa re-opening; the PLC monitors the pressure P of the second buffer tank according to the third pressure sensor c Controlling the size of the internal aperture of the proportional valve to enable the pressure P of the second buffer tank c The conditions are satisfied: (P) d -0.03)＜P c ＜(P d +0.03) Mpa, where P d Taking 0.1Mpa;
(4) After SF6 recovery is completed, and the pressure P in the first buffer tank b Below (P) a +0.05) MPa, closing the second electromagnetic valve and the fourth electromagnetic valve, removing the pressure reducing valve and the mass flow controller from the gas path, and calculating the recovery rate, the gas amount and the effective volume;
(5) After the calculation is completed, the third electromagnetic valve and the fifth electromagnetic valve are opened, and residual gas in the first buffer tank is completely recovered into the liquid storage tank by the second compressor for liquefaction and storage.
8. The SF6 recycling method with recycling rate measuring function according to claim 7, wherein: the PLC calculates the recovery rate, the gas quantity and the effective volume, and the specific steps include:
the PLC controller is internally provided with a timer, and the output gas time t of the mass flow controller is recorded 1 Output gas volume V 1 ＝t 1 Q, SF6 gas density at normal pressure is ρ SF6 ＝6.0886kg/m 3 The amount of recovered gas in this period of time is m k1 ＝V 1 ×ρ SF6 ；
At t in the first buffer tank 1 Time gas pressure P c1 Temperature is equal to the temperature T of the gas in the gas chamber at the moment 1 Calculating the gas density rho in the first buffer tank by combining an empirical formula c1 The first buffer tank volume V is known c Mass of gas m in the first buffer tank k2 ＝V c ×ρ c1 ；
Calculating the recovery start t 1 Within the time, the gas in the gas chamber is reduced by m s1 ＝m k1 +m k2 ；
According to the temperature T of the air chamber after recovery 1 And pressure P 1 Calculating the gas density rho of the recovered gas chamber by combining an empirical formula 1 The effective volume V of the air chamber can be further calculated:
V＝m s1 /(ρ 0 -ρ 1 )；
the gas amount: m=v×ρ 0 ；
Recovery rate: ζ=m s1 /m。
9. The SF6 recycling method with recycling rate measuring function according to claim 7, wherein: and a vacuum gauge and a vacuum pump are arranged on a pipeline between the third electromagnetic valve and the fifth electromagnetic valve, the output end of the vacuum pump is communicated with the exhaust port, and the vacuum gauge and the vacuum pump are connected with the PLC.
10. The SF6 recycling method with recycling rate measuring function according to claim 9, wherein: if the device needs to be vacuumized, the second electromagnetic valve and the fourth electromagnetic valve are closed, the first electromagnetic valve, the third electromagnetic valve and the fifth electromagnetic valve are opened, the vacuum pump is started to discharge residual gas, and vacuumizing is stopped when the pressure of the vacuum gauge is detected to be lower than 10 Pa.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117053095A (en) * | 2023-10-11 | 2023-11-14 | 国网江苏省电力有限公司电力科学研究院 | Device and method for changing SF6 pure gas in equipment into SF6-N2 mixed gas |
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- 2023-05-12 CN CN202310549069.9A patent/CN116658819A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117053095A (en) * | 2023-10-11 | 2023-11-14 | 国网江苏省电力有限公司电力科学研究院 | Device and method for changing SF6 pure gas in equipment into SF6-N2 mixed gas |
| CN117053095B (en) * | 2023-10-11 | 2023-12-26 | 国网江苏省电力有限公司电力科学研究院 | Device and method for changing SF6 pure gas in equipment into SF6-N2 mixed gas |
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