CN117563395A - Based on SF in exhaust gas 6 Content statistics SF 6 System and method for membrane separation - Google Patents
Based on SF in exhaust gas 6 Content statistics SF 6 System and method for membrane separation Download PDFInfo
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- 238000000926 separation method Methods 0.000 title claims abstract description 89
- 239000012528 membrane Substances 0.000 title claims abstract description 88
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000002156 mixing Methods 0.000 claims abstract description 17
- 230000001105 regulatory effect Effects 0.000 claims abstract description 17
- 239000003513 alkali Substances 0.000 claims abstract description 9
- 229910018503 SF6 Inorganic materials 0.000 claims description 11
- 229920006254 polymer film Polymers 0.000 claims description 11
- SFZCNBIFKDRMGX-UHFFFAOYSA-N sulfur hexafluoride Chemical compound FS(F)(F)(F)(F)F SFZCNBIFKDRMGX-UHFFFAOYSA-N 0.000 claims description 11
- 229920005597 polymer membrane Polymers 0.000 claims description 10
- 238000000746 purification Methods 0.000 claims description 8
- 238000005057 refrigeration Methods 0.000 claims description 8
- 238000004364 calculation method Methods 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 229960000909 sulfur hexafluoride Drugs 0.000 claims description 5
- 238000001035 drying Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 230000008569 process Effects 0.000 claims description 3
- 230000006872 improvement Effects 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 64
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000007788 liquid Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000002120 nanofilm Substances 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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Abstract
The invention discloses a SF in exhaust gas 6 Content statistics SF 6 A system and a method for membrane separation, a first branch is connected in parallel between a first flowmeter and an alkali liquor tank, and the first branch is connected with the alkali liquor tank according to the following modeThe gas flow direction is sequentially connected with a first SF of a first adjusting needle valve in series 6 /N 2 Comprehensive detector for acquiring SF of intake air 6 /N 2 Mixing ratio; a third branch is led out between the second flowmeter and the second osmosis port, and a second regulating needle valve and a second SF are connected in series in sequence in a third bypass 6 /N 2 Comprehensive detector for acquiring SF of tail gas 6 /N 2 Mixing ratio. SF based on air inlet and tail gas 6 /N 2 And (3) calculating the membrane separation efficiency under the current air inlet pressure and temperature conditions by mixing ratio, comprehensively judging whether the current membrane separation efficiency reaches the optimum according to the standard membrane separation efficiency, and if not, dynamically adjusting the air inlet pressure and temperature to obtain the optimum membrane separation efficiency.
Description
Technical Field
The invention relates to SF 6 /N 2 The technical field of mixed gas separation, in particular to a method based on SF in exhaust tail gas 6 Content statistics SF 6 Membrane separation amount.
Background
Along with the proposal of the 'double carbon' target, SF is gradually adopted by power grid enterprises 6 /N 2 Mixed gas to replace pure SF 6 Gas to reduce strong greenhouse gas SF 6 Used amount and discharge amount of the catalyst. Standard Q/GDW 11921.2-2 SF with rated voltage 72.5kV and above 6 /N 2 Part 2 of the gas-insulated metal-enclosed switchgear: the operation and maintenance standards specify that equipment needs maintenance or SF 6 /N 2 The mixed gas quality does not reach the standard, and the gas is required to be separated and recovered. SF (sulfur hexafluoride) 6 /N 2 N in the mixed gas 2 The duty ratio is about 30%, and the concentration is far higher than that of the traditional pure SF 6 Trace amount of N mixed in gas 2 (generally not more than 0.2%), the prior art generally adopts membrane separation technology to carry out the method for separating high concentration N in the mixed gas 2 Primary filtering, and separating to obtain SF 6 The gas ratio is more than 95%. The membrane separation technology utilizes the difference of diffusion rates of different gas molecules in a high molecular membrane to divide the gas into fast gas and slow gas which flow out from a permeation port and a discharge port respectively. The membrane separation efficiency is mainly related to the gas temperature (which is inversely related to the membrane separation efficiency) and the gas pressure (which is positively related to the membrane separation efficiency), and if the separation efficiency is lower than an expected value due to the change of environmental conditions in the field application process, the trace N at the rear end is increased 2 Purifying module workload and may cause final purified SF 6 The purity of the gas does not meet the intended target. However, at present, a method for counting the membrane separation amount in real time in the separation process does not exist, and the current membrane separation work efficiency cannot be accurately controlled; and, in case SF cannot be obtained 6 Under the condition of the gas membrane separation amount, optimal regulation and control of temperature and pressure are difficult to realize, and then poor separation effect is caused.
Disclosure of Invention
The technical problem to be solved by the invention is how to solve in SF 6 /N 2 And acquiring the current membrane separation energy efficiency in the mixed gas separation process, and adjusting the air inlet pressure and the temperature in real time according to the current membrane separation energy efficiency.
The invention solves the technical problems by the following technical means:
SF (sulfur hexafluoride) in exhaust 6 Content statistics SF 6 A method of membrane separation comprising the steps of:
s1, acquiring SF of intake air in real time 6 /N 2 Mixing ratio a%: b% and flow Q 1 And a mixing ratio c% after separation: d% and flow Q 2 The method comprises the steps of carrying out a first treatment on the surface of the Recording the current air inlet temperature and pressure;
s2, calculating membrane separation efficiency:
wherein V is 1 For the volume of intake, V 2 The smaller the value of K is, the lower the SF6 content in the discharged tail gas is, and the higher the membrane separation efficiency is;
s3, dynamically adjusting the pressure and the temperature of the membrane separation air inlet according to the k value.
The invention counts the separation amount and efficiency of the membrane through the front and back comprehensive detectors and the flowmeter; and the air inlet temperature and pressure are adjusted in real time according to the membrane separation efficiency, so that the self-membrane separation effect is obtained, and the membrane separation result is ensured to meet the requirements.
Further, also comprises calculating SF 6 The specific calculation process of the membrane separation amount is as follows:
real-time statistics of SF separated by membrane 6 The gas volume is:
V SF6 ＝V 1 *a％-V 2 *c％
calculation of Density according to Beattie-Bridgman equation
R＝56.5902×10 -5
Wherein:is SF 6 Absolute pressure of gas, unit: MPa; />Is SF 6 Density of gas, unit: kg/m 3 ；Is SF 6 Thermodynamic temperature of gas, unit: k, performing K;
SF is calculated by a mass formula 6 Gas amount:
further, the method for dynamically adjusting the pressure and the temperature of the membrane separation inlet air in the step S3 specifically comprises the following steps:
assuming that the initial intake pressure and temperature are P respectively 0 And T 0 At this time, the membrane separation efficiency was K 0 The method comprises the steps of carrying out a first treatment on the surface of the Regulating output pressure of compressor, raising set value air inlet pressure, at this time P 1 And the refrigerating module is lowered to lower the air inlet temperature by a set value T 1 The pressure and temperature stabilize to the set value P 1 And T 1 At this time, the membrane separation efficiency was K 1 The method comprises the steps of carrying out a first treatment on the surface of the The pressure and the temperature after the pressure rise and the temperature drop are respectively P after the pressure rise and the temperature drop are analogically conducted for n times n And T n The membrane separation efficiency is K n 。
Further, the membrane separation efficiency is K n The specific judgment of whether the requirements are met is as follows:
1) If 0 is less than or equal to K n -K n-1 If the ratio is less than or equal to 0.5%, the efficiency is not obviously improved, (1) if K is the same at the moment n More than or equal to 94 percent, the air inlet pressure and the temperature are further improved, and K is judged n More than or equal to 95 percent, if K is within the limit value n If the pressure is more than or equal to 95%, stopping boosting and cooling, otherwise, sending out membrane separation warning information; (2) if K n Less than 94%, directly sending out membrane separation warning information;
2) If K n -K n-1 More than 0.5%, the membrane separation efficiency is obviously improved, (1) the inlet pressure and the temperature are further improved, and the efficiency K is improved after the nth time of improvement n -K n-1 Less than or equal to 0.5 percent, the efficiency is not obviously improved at the moment, if K n More than or equal to 95 percent, and keeping the pressure and the temperature unchanged; (2) if K 1 < 95%, refer to step 1).
The invention also provides a method for removing SF in the tail gas 6 Content statistics SF 6 The membrane separation amount system comprises a mixed gas inlet 1, an electromagnetic valve 2, a first flowmeter 19, an alkali liquid pool 5, a drying tower 6, a buffer tank 7, a compressor 8, a first polymer membrane 9, a second polymer membrane 11 and a post-purification treatment module 13 which are sequentially connected in series according to the air inlet direction; the second polymer membrane 11 comprises a second air inlet 111, a second permeation port 112 and a second air outlet 113; the second air outlet 113 is connected with the inlet of the post-purification treatment module 13;
a first branch is connected in parallel between the first flowmeter 19 and the alkali liquor tank 5, and the first branch is connected in series with a first regulating needle valve 3 and a first SF in sequence according to the gas flow direction 6 /N 2 Comprehensive detector 4 for acquiring SF of intake air 6 /N 2 Mixing ratio; a second branch is led out from the second permeation port 112, and a second flowmeter 20, an exhaust gas purifying module 17 and an exhaust gas discharge port 18 are sequentially connected in series on the second branch. A third branch is led out between the second flowmeter 20 and the second osmosis port, and a second regulating needle valve 15 and a second SF are connected in series in sequence in a third bypass 6 /N 2 Comprehensive detector 16 for acquiring SF of tail gas 6 /N 2 Mixing ratio.
Further, the first polymer membrane 9 further includes a first air inlet 91, a first permeation port 92, and a first air outlet 93, the outlet of the compressor 8 is connected to the first air inlet 91, the first permeation port 92 is connected to the inlet of the buffer tank 7, and the first air outlet 93 is connected to the second air inlet 111.
Further, the first polymer film 9 and the second polymer film 11 supply cooling energy through the first refrigeration module 10 and the second refrigeration module 12, respectively.
The invention has the advantages that:
SF based on inlet air and tail gas 6 /N 2 The mixing ratio, the membrane separation efficiency under the current air inlet pressure and temperature conditions is calculated, then whether the current membrane separation efficiency reaches the optimal or not is comprehensively judged according to the standard membrane separation efficiency,if not, the optimal membrane separation efficiency is obtained by dynamically adjusting the inlet pressure and temperature. The membrane separation efficiency is counted in real time, the air inlet pressure and the air inlet temperature are regulated, the optimal membrane separation efficiency is obtained under the condition of saving electric power, the membrane separation effect is ensured to meet the requirement, and SF is reduced 6 And (5) discharging gas.
Meanwhile, SF (sulfur hexafluoride) separated by the membrane can be counted in real time 6 The gas quantity makes up for the current SF 6 /N 2 The mixed gas purifying device has the disadvantage of statistics of the membrane separation amount.
Drawings
Fig. 1 is a schematic diagram of a system according to an embodiment of the present invention.
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 in the embodiments of the present invention will be clearly and completely described in the following in conjunction with 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. 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.
Example 1
As shown in fig. 1, this embodiment describes a method based on SF in exhaust 6 Content statistics SF 6 The membrane separation amount system is sequentially connected with a mixed gas inlet 1, an electromagnetic valve 2, a first flowmeter 19, an alkali liquid pool 5, a drying tower 6, a buffer tank 7, a compressor 8, a first polymer membrane 9, a second polymer membrane 11 and a post-purification treatment module 13 in series according to the air inlet direction; the first polymer film 9 and the second polymer film 11 provide cooling energy through the first refrigeration module 10 and the second refrigeration module 12, respectively.
The first polymer film 9 further comprises a first air inlet 91, a first permeation port 92 and a first air outlet 93, and the second polymer film 11 comprises a second air inlet 111, a second permeation port 112 and a second air outlet 113; the outlet of the compressor 8 is connected with a first air inlet 91, a first penetration port 92 is connected with the inlet of the buffer tank 7, a first air outlet 93 is connected with a second air inlet 111, and a second air outlet 113 is connected with the inlet of the post-purification treatment module 13.
In the embodiment, a first branch is connected in parallel between the first flowmeter 19 and the alkali liquor tank 5, and the first branch is connected in series with a first regulating needle valve 3 and a first SF in turn according to the gas flow direction 6 /N 2 Comprehensive detector 4 for acquiring SF of intake air 6 /N 2 Mixing ratio. A second branch is led out from the second permeation port 112, and a second flowmeter 20, an exhaust gas purifying module 17 and an exhaust gas discharge port 18 are sequentially connected in series on the second branch. A third branch is led out between the second flowmeter 20 and the second osmosis port, and a second regulating needle valve 15 and a second SF are connected in series in sequence in a third bypass 6 /N 2 Comprehensive detector 16 for acquiring SF of tail gas 6 /N 2 Mixing ratio.
Based on the above system, the working steps of this embodiment are:
(1) Opening the electromagnetic valve 2 to purify SF 6 /N 2 The mixed gas enters from the mixed gas inlet 1, and the first flowmeter 19 detects the gas flow rate as Q 1 L/min, regulating the flow of the first regulating needle valve 3 to 300ml/min, and regulating the first SF 6 /N 2 The comprehensive detector 4 detects that the mixing ratio is a%: b, the gas quantity V of the gas entering the purifying device in the process 1 (20℃，0.1MPa)：
t 1 For the total intake time, Δt is the flow time of the mixed gas in the pipeline and the flow time in the polymer film after the mixed gas is metered by the first flowmeter 19.
(2) The gas to be purified enters an alkali liquid pool 5 to remove acidic substances (prevent damage to a polymer film), then enters a drying tower 6 to remove water (the loss is negligible because the impurity in the mixed gas does not exceed 0.1 percent), then sequentially enters a buffer tank 7, is pressurized by a compressor 8, and has initial pressurizing pressure P 0 Is set to 0.3MPa, and the first refrigeration module 10 and the second refrigeration module 12 respectively correspond to the first polymer film 10 and the second polymer filmMolecular film 11 is cooled down, initial temperature T 0 Set to 20 ℃ (generally, the lower the temperature, the higher the pressure, the better the membrane separation effect).
(3) The first permeate port 92 contains mainly nitrogen, but at this time there is still a small amount of SF 6 The gas is introduced into the front buffer tank 7; the first air outlet 93 mainly contains SF 6 There is still a small amount of nitrogen, and the second membrane group 11 is added, while SF is in the second permeate port 111 6 The content is extremely low, and the waste gas enters a tail gas treatment part; SF in the second air outlet 113 6 The ratio of the water to the water is extremely high, and the water enters a post-purification module 13 (which can be an adsorption tower, a cryogenic module, a rectification module and the like).
(4) The high-concentration nitrogen entering the tail gas treatment part is firstly provided with a flow rate of 300ml/min by a regulating needle valve 15, and a second SF 6 /N 2 The integrated detector 16 detects the mixing ratio c% after the membrane separation: d, the second flowmeter 20 measures the flow rate Q 2 The gas then enters an exhaust gas purification module 17 (typically activated carbon, activated alumina, 13X molecular sieve, etc. to remove SO 2 Adsorbent of CO gas impurity), and discharging from 18 ports after innocent treatment; the volume of the gas after membrane separation is:
(5) Calculation of
1) Real-time statistics of SF separated by membrane 6 The gas volume is:
V SF6 ＝V 1 *a％-V 2 *c％
the volume is 20 ℃ and 0.1MPa
Calculation of Density according to Beattie-Bridgman equation
R＝56.5902×10 -5
Wherein:is SF 6 Absolute pressure of gas, unit: MPa; />Is SF 6 Density of gas, unit: kg/m 3 ；Is SF 6 Thermodynamic temperature of gas, unit: K.
calculating SF6 gas amount by a mass formula:
2) Real-time calculation of high molecular film separation efficiency
The smaller the value of K is, the SF in the exhaust gas is discharged 6 The lower the content, the higher the membrane separation efficiency.
(6) Dynamic adjustment of membrane separation inlet pressure and temperature according to K value
The initial intake pressure and temperature are respectively P 0 And T 0 At this time, the membrane separation efficiency was K 0 The method comprises the steps of carrying out a first treatment on the surface of the The output pressure of the compressor is regulated, the air inlet pressure of 0.3MPa is increased, and the pressure is P 1 And the refrigerating module is lowered to lower the temperature of the inlet air by 5 ℃, at the moment, T 1 The pressure and temperature stabilize to the set value P 1 And T 1 At this time, the membrane separation efficiency was K 1 The method comprises the steps of carrying out a first treatment on the surface of the The pressure and the temperature after the pressure rise and the temperature drop are respectively P after the pressure rise and the temperature drop are analogically conducted for n times n And T n The membrane separation efficiency is K n Further analysis and judgment:
1) If 0 is less than or equal to K n -K n-1 If the ratio is less than or equal to 0.5%, the efficiency is not obviously improved, (1) if K is the same at the moment n If the pressure is more than or equal to 94%, the air inlet pressure and the temperature are further increased, the pressure is increased by 0.3MPa and the temperature is reduced by 5 ℃ each time (the upper pressure limit is 5.0MPa, the lower temperature limit is-20 ℃), and K is judged n More than or equal to 95 percent, if K is within the limit value n If the pressure is more than or equal to 95%, stopping boosting and cooling, otherwise, sending out membrane separation warning information; (2) if K n Less than 94%, and directly sending out membrane separation warning information.
2) If K n -K n-1 More than 0.5%, the membrane separation efficiency is obviously improved, (1) the air inlet pressure and the air inlet temperature are further improved, the pressure is increased by 0.3MPa each time, the temperature is reduced by 5 ℃, and the efficiency K is improved after the nth time n -K n-1 Less than or equal to 0.5 percent, the efficiency is not obviously improved at the moment, if K n More than or equal to 95 percent, and keeping the pressure and the temperature unchanged; (2) if K 1 < 95%, refer to step 1).
The optimal membrane separation efficiency can be obtained through the above steps.
The working principle of the embodiment is as follows:
SF based on inlet air and tail gas 6 /N 2 And (3) calculating the membrane separation efficiency under the current air inlet pressure and temperature conditions by mixing ratio, comprehensively judging whether the current membrane separation efficiency reaches the optimum according to the standard membrane separation efficiency, and if not, dynamically adjusting the air inlet pressure and temperature to obtain the optimum membrane separation efficiency.
The above embodiments are only for illustrating the technical solution of the present invention, and are not limiting; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit and scope of the technical solutions of the embodiments of the present invention.
Claims (7)
1. SF (sulfur hexafluoride) in exhaust 6 Content statistics SF 6 The membrane separation quantity system is characterized by comprising a mixed gas inlet (1), an electromagnetic valve (2), a first flowmeter (19), an alkali liquor tank (5), a drying tower (6), a buffer tank (7), a compressor (8), a first polymer membrane (9), a second polymer membrane (11) and a post-purification treatment module (13) which are sequentially connected in series according to the air inlet direction; the second polymer membrane (11) comprises a second air inlet (111), a second permeation port (112) and a second air outlet (113); the second air outlet (113) is connected with the inlet of the post-purification treatment module (13);
a first branch is connected in parallel between the first flowmeter (19) and the alkali liquor tank (5), and a first regulating needle valve 3 and a first SF are connected in series in sequence according to the gas flow direction on the first branch 6 /N 2 Comprehensive detector (4) for acquiring SF of intake air 6 /N 2 Mixing ratio; a second branch is led out from the second permeation port (112), and a second flowmeter (20), a tail gas purifying module (17) and a tail gas discharging port (18) are sequentially connected in series on the second branch; a third branch is led out between the second flowmeter (20) and the second permeation port (112), and a second regulating needle valve (15) and a second SF are connected in series in the third bypass 6 /N 2 Comprehensive detector (16) for acquiring SF of tail gas 6 /N 2 Mixing ratio.
2. An SF based on exhaust gas according to claim 1 6 Content statistics SF 6 The membrane separation amount system is characterized in that the first polymer membrane (9) further comprises a first air inlet (91), a first permeation port (92) and a first air outlet (93), the outlet of the compressor 8 is connected with the first air inlet (91), the first permeation port (92) is connected with the inlet of the buffer tank 7, and the first air outlet (93) is connected with a second air inlet (111).
3. An exhaust tail gas based on SF according to claim 1 or 2 6 Content statistics SF 6 System of Membrane separation amountThe system is characterized in that the first polymer film (9) and the second polymer film (11) respectively provide cold energy through the first refrigeration module (10) and the second refrigeration module (12).
4. SF (sulfur hexafluoride) in exhaust 6 Content statistics SF 6 A method of membrane separation, comprising the steps of:
s1, acquiring SF of intake air in real time 6 /N 2 Mixing ratio a%: b), and the mixing ratio c% after separation: d, d; recording the current air inlet temperature and pressure;
s2, calculating membrane separation efficiency:
wherein V is 1 For the volume of intake, V 2 The smaller the K value of the volume of the tail gas after membrane separation is, the SF in the tail gas is discharged 6 The lower the content, the higher the membrane separation efficiency;
s3, dynamically adjusting the pressure and the temperature of the membrane separation air inlet according to the k value and the current air inlet temperature and pressure.
5. An exhaust tail gas based on SF according to claim 4 6 Content statistics SF 6 A method for membrane separation, characterized by further comprising the step of calculating SF 6 The specific calculation process of the membrane separation amount is as follows:
real-time statistics of SF separated by membrane 6 The gas volume is:
V SF6 ＝V 1 *a％-V 2 *c％
calculation of Density according to Beattie-Bridgman equation
R＝56.5902×10 -5
Wherein:is SF 6 Absolute pressure of gas, unit: MPa; />Is SF 6 Density of gas, unit: kg/m 3 ；/>Is SF 6 Thermodynamic temperature of gas, unit: k, performing K;
SF is calculated by a mass formula 6 Gas amount:
6. an SF-based exhaust gas treatment system as claimed in claim 4 6 Content statistics SF 6 The method for regulating the membrane separation amount is characterized in that the method for regulating the inlet pressure and the temperature of the membrane separation in the step S3 specifically comprises the following steps:
assuming that the initial intake pressure and temperature are P respectively 0 And T 0 At this time, the membrane separation efficiency was K 0 The method comprises the steps of carrying out a first treatment on the surface of the Regulating output pressure of compressor, raising set value air inlet pressure, at this time P 1 And the refrigerating module is lowered to lower the air inlet temperature by a set value T 1 The pressure and temperature stabilize to the set value P 1 And T 1 At this time, the membrane separation efficiency was K 1 The method comprises the steps of carrying out a first treatment on the surface of the The pressure and the temperature after the pressure rise and the temperature drop are respectively P after the pressure rise and the temperature drop are analogically conducted for n times n And T n The membrane separation efficiency is K n 。
7. A method according to claim 6, wherein the SF is based on statistics of SF6 content in the exhaust gas 6 A method for separating a membrane by a membrane separation amount, characterized in that the membrane separation efficiency is K n The specific judgment of whether the requirements are met is as follows:
1) If 0 is less than or equal to K n -K n-1 If the ratio is less than or equal to 0.5%, the efficiency is not obviously improved, (1) if K is the same at the moment n More than or equal to 94 percent, the air inlet pressure and the temperature are further improved, and K is judged n More than or equal to 95 percent, if K is within the limit value n If the pressure is more than or equal to 95%, stopping boosting and cooling, otherwise, sending out membrane separation warning information; (2) if K n Less than 94%, directly sending out membrane separation warning information;
2) If K n -K n-1 More than 0.5%, the membrane separation efficiency is obviously improved, (1) the inlet pressure and the temperature are further improved, and the efficiency K is improved after the nth time of improvement n -K n-1 Less than or equal to 0.5 percent, the efficiency is not obviously improved at the moment, if K n More than or equal to 95 percent, and keeping the pressure and the temperature unchanged; (2) if K 1 < 95%, refer to step 1).
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