CN206295780U - A kind of pouring-in simultaneous SO_2 and NO removal mercury removal device - Google Patents
A kind of pouring-in simultaneous SO_2 and NO removal mercury removal device Download PDFInfo
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- CN206295780U CN206295780U CN201621430913.8U CN201621430913U CN206295780U CN 206295780 U CN206295780 U CN 206295780U CN 201621430913 U CN201621430913 U CN 201621430913U CN 206295780 U CN206295780 U CN 206295780U
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- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 229910052753 mercury Inorganic materials 0.000 title claims abstract description 48
- 239000007789 gas Substances 0.000 claims abstract description 85
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 58
- 239000003546 flue gas Substances 0.000 claims abstract description 58
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000001514 detection method Methods 0.000 claims abstract description 9
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000012159 carrier gas Substances 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims 1
- 239000002245 particle Substances 0.000 abstract description 13
- 230000006641 stabilisation Effects 0.000 abstract description 11
- 238000011105 stabilization Methods 0.000 abstract description 11
- 239000000203 mixture Substances 0.000 abstract description 8
- 238000000034 method Methods 0.000 abstract description 5
- 230000007797 corrosion Effects 0.000 abstract description 2
- 238000005260 corrosion Methods 0.000 abstract description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 28
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- 239000003344 environmental pollutant Substances 0.000 description 9
- 231100000719 pollutant Toxicity 0.000 description 9
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 8
- 239000003245 coal Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 238000007254 oxidation reaction Methods 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000004868 gas analysis Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- 238000003916 acid precipitation Methods 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- 230000033228 biological regulation Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000007689 inspection Methods 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- 239000002243 precursor Substances 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 231100000614 poison Toxicity 0.000 description 2
- 230000007096 poisonous effect Effects 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 231100000693 bioaccumulation Toxicity 0.000 description 1
- 239000003181 biological factor Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000003851 corona treatment Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000005684 electric field Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 235000013619 trace mineral Nutrition 0.000 description 1
- 239000011573 trace mineral Substances 0.000 description 1
Abstract
A kind of pouring-in simultaneous SO_2 and NO removal mercury removal device, is related to the desulphurization denitration removal of mercury.Pouring-in simultaneous SO_2 and NO removal mercury removal device is provided with coal-fired flue-gas generating unit, vapor generating unit, plasma generating unit, gas mixing units and detection unit.Coal-fired flue-gas generating unit is provided with O2、NO、SO2And N2Gas cylinder and Hg0Osmos tube and thermostat water bath；Vapor generating unit is made up of thermostat water bath, Drexel bottle；Plasma generating unit is provided with power supply and plasma reactor；Gas mixing units are provided with gas mixer chamber；Detection unit is provided with flue gas analyzer and mercury vapourmeter.The pouring-in simultaneous SO_2 and NO removal method for removing hydrargyrum uses pouring-in simultaneous SO_2 and NO removal mercury removal device.Can easily and fast, stabilization produce active particle, and due to using it is pouring-in flue gas system introduce active particle, the corrosion and loss of flue gas composition article on plasma reactor according can be avoided.
Description
Technical field
The utility model is related to the desulphurization denitration removal of mercury, more particularly, to a kind of pouring-in simultaneous SO_2 and NO removal mercury removal device.
Background technology
The existing coal group of motors level of China falls behind, and gross coal consumption rate is high, and flue dust, sulphur are contained in the flue gas that coal burning is produced
Oxide (SOx), nitrogen oxides (NOx), carbon monoxide (CO), carbon dioxide (CO2) and the air such as poisonous heavy metal element it is dirty
Dye thing, the balance that these materials can not only destroy air causes environmental pollution, and health can be caused harm.
SO2And NOxCan form secondary with other materials in environment under physics, chemistry or biological factor after entering air
Pollutant, causes acid rain and photochemical fog etc. to pollute, and causes even more serious harm.It is big that current China has become the world three
First of Acid Rain Zone, to health, building, lake and ecological environment cause greatly harm to acid rain；And photochemical fog
In specific geographical position, the meteorological condition of inversion and unfavorable diffusion is run into, then easily cause zonal ozone and granular pattern
Pollution so that regional air quality degradation.
Mercury belongs to trace element, with very strong toxicity.Although content of the mercury in coal is relatively low, due to CHINESE COAL
Charcoal consumption is big, and total emission volumn is very big, and mercury is volatile, and under the effect of bioaccumulation and amplification, mercury can be in food
Concentration higher is enriched in the organism of thing chain higher level, so as to bring serious harm to biological and health.
The principle of corona treatment pollutant is that under DC Electric Field, a large amount of the taking that electric discharge is produced can electron bombardment
Contaminant molecule, makes its ionization, dissociates and excite, so as to trigger the physical and chemical reaction of a series of complex so that macromolecular
Pollutant is changed into simple small molecule safe material, or poisonous and harmful substance is changed into the low harmful thing of nontoxic or low toxicity
Matter, finally enables pollutant degrade and removes.Plasma flue gas purifying technology has been applied to nitrogen oxides and sulfur dioxide
Purification process, and achieve good effect.
At this stage due to factors such as technology or costs, dedusting, desulphurization and denitration and demercuration are past in domestic and international flue gases purification
Toward being respectively completed in multiple independent systems, existing integrated treatment technology is not also due to the reason such as technology treatment effect
It is highly desirable.In order to reduce the cost of gas cleaning, the new technology and new technology that exploitation multiple pollutant is removed simultaneously turn into flue gas
New development trend in purification techniques field.
(Chen Tianbing, Wu Jianjun, Korea Spro's first industry pollutions that caused by coal burning present situation and its Treatment process summary coals, 2006,15 such as Chen Tianbing
(2):1~4) report pollution that caused by coal burning present situation and its Treatment process summary.Cheng Ke etc. (Cheng Ke, Wang Yan, Xue Zhigang, Tian Hong, easily
Roc《Fossil-fuel power plant atmospheric pollutant emission standard》Implement the influence Research of Environmental Sciences to coal-burning power plant's Mercury In The Air emission reduction
.2015,28(9)：1369~1374) report《Fossil-fuel power plant atmospheric pollutant emission standard》Implementation subtracts to coal-burning power plant's Mercury In The Air
The influence of row.
The content of the invention
The purpose of this utility model is to provide a kind of pouring-in simultaneous SO_2 and NO removal mercury removal device.
The utility model is provided with coal-fired flue-gas generating unit, vapor generating unit, plasma generating unit, gas and mixes
Close unit and detection unit.
The coal-fired flue-gas generating unit is provided with O2Gas cylinder, NO gas cylinders, SO2Gas cylinder, N2Gas cylinder, Hg0Osmos tube and flue gas are sent out
Raw thermostat water bath；
There is thermostat water bath, Drexel bottle and connecting line by vapor and constitute in the vapor generating unit；
The plasma generating unit is provided with high voltage power supply and plasma reactor；
The gas mixing units are made up of gas mixer chamber (can use column glass container) and connecting line, and periphery twines
There is heating tape；
The detection unit is provided with flue gas analysis unit (flue gas analyzer) and Hg0Analytic unit (mercury vapourmeter)；
Vapor is produced by the Drexel bottle equipped with water being positioned in vapor generation thermostat water bath, is connected with Drexel bottle
The stripping carrier gas O of constant flow rate2；
The O2Cylinder outlet is respectively equipped with an O2Gas mass flow controller and the 2nd O2Gas mass flow controller,
The NO cylinder outlets are provided with NO gas mass flow controllers, the SO2Cylinder outlet is provided with SO2Gas mass flow controller, institute
State N2Cylinder outlet is provided with a N2Gas mass flow controller and the 2nd N2Gas mass flow controller；
First O2Gas mass flow controller output end and Drexel bottle connect plasma reactor, the 2nd O2Gas mass flow
Controller output end connects Drexel bottle, and Drexel bottle is located at vapor to be occurred in thermostat water bath, the output of NO gas mass flow controller
End, SO2Gas mass flow controller output end, a N2Gas mass flow controller output end and Hg0Osmos tube output end is distinguished
Connect gas mixer chamber, the 2nd N2Gas mass flow controller output termination Hg0Osmos tube, Hg0Osmos tube is located at flue gas and constant temperature occurs
In water-bath, the output end of gas mixer chamber connects flue gas analyzer, mercury vapourmeter and exhaust gas processing device respectively.
KCl bottles and tube furnace can be sequentially provided with the import of mercury vapourmeter.
The method for carrying out the pouring-in simultaneous SO_2 and NO removal removal of mercury using the utility model is as follows：
1) flow of mass flow controller is respectively set to O2 400 1#、O2 100 2#、SO2 80、NO 66、N2
854, unit is mL/min；
2) open flue gas and thermostat water bath occurs, open N2Gas cylinder, makes Hg0Osmos tube is in constant bath temperature 57.5
DEG C, the stabilization 2h under constant flow rate 0.2L/min carrier gas strippings obtains the mercury release rate of stabilization；
3) steam evaporator is opened, it is produced the aqueous O of steady concentration2, open temperature control box and set its temperature as
140 DEG C, heating tape is set to be stably held in 140 DEG C；
4) O is opened2Gas cylinder and mass flow controller and valve, O2Enter plasma reactor (plasma with vapor
Reactor according is closed), the flow of gas mixer chamber is entered by pump control, mix in gas mixing room with simulated flue gas component
It is even, by flue gas analysis unit (flue gas analyzer) and Hg0Flue gas composition concentration in analytic unit (mercury vapourmeter) detecting system (NO,
SO2) and Hg0Concentration, if surveyed Hg0Concentration is 50 μ g/m3, then step 5 can be carried out), otherwise wait for Hg0Osmos tube stabilization；
5) high voltage power supply is opened, regulation voltage makes O to 5kV2With vapor by produced after plasma discharge reaction
Active particle reacted in gas mixing room by with simulated flue gas component, by flue gas analyzer and mercury vapourmeter detecting system
NO、SO2And Hg0Concentration, after measured result contrast, you can obtain the active oxidation particle of ion precursor reactant generation for NO, SO2
And Hg0Oxidation efficiency；
6) flue gas absorbs Hg respectively by KCl solution and NaOH alkali lye2+After sour gas, by flue gas analyzer and survey mercury
The pollutant concentration of instrument inspection system outlet, draws the efficiency of the system desulphurization denitration removal of mercury.
The beneficial effects of the utility model are：Can easily and fast, stabilization generation active particle, and due to using note
Enter formula and introduce active particle in flue gas system, the corrosion and loss of flue gas composition article on plasma reactor according can be avoided.This practicality
It is new that O is introduced in discharge system2And vapor, electric discharge atmosphere it is pure, be conducive to electric discharge to carry out, and produce active particle group
Into controllable with concentration, OH, O, O are mainly produced3Deng with the active particle compared with strong oxidizing property, be conducive to the oxidation of mixed flue gas.
The active particle that discharge system is produced is via injection mode and fully compositional simulation coal-fired flue-gas in gas mixing units
Mixing, and realized to NO, SO by equipment such as flue gas analyzer and mercury vapourmeters2And Hg0Real-time monitoring.System design is convenient real
With, pipeline using acidproof, high temperature resistant (<200 DEG C) material.
Brief description of the drawings
Fig. 1 is the structure composition schematic diagram of the utility model embodiment.
Specific embodiment
Referring to Fig. 1, the utility model is provided with coal-fired flue-gas generating unit, vapor generating unit 2, plasma and list occurs
Unit, gas mixing units and detection unit.
The coal-fired flue-gas generating unit is provided with O2Gas cylinder 11, NO gas cylinders 12, SO2Gas cylinder 13, N2Gas cylinder 14, Hg0Osmos tube
16 and flue gas occur thermostat water bath 17；
There is thermostat water bath 21, Drexel bottle 22 and connecting line by vapor and constitute in the vapor generating unit；
The plasma generating unit is provided with high voltage power supply 31 and plasma reactor 32；
The gas mixing units are made up of gas mixer chamber 4 (can use column glass container) and connecting line, periphery
It is tied with heating tape；
The detection unit is provided with flue gas analysis unit (flue gas analyzer 51) and Hg0Analytic unit (mercury vapourmeter 52)；
Vapor is produced by the Drexel bottle 22 equipped with water being positioned in vapor generation thermostat water bath 21, Drexel bottle 22
Inside it is connected with the stripping carrier gas O of constant flow rate2；
The O2The outlet of gas cylinder 11 is respectively equipped with an O2The O of gas mass flow controller 111 and the 2nd2Gas mass flow control
Device processed 112, the outlet of NO gas cylinders 12 is provided with NO gas mass flow controller 121, the SO2The outlet of gas cylinder 13 is provided with SO2Makings
Amount flow controller 131, the N2The outlet of gas cylinder 14 is provided with a N2The N of gas mass flow controller 141 and the 2nd2Gas quality stream
Amount controller 142；
First O2The output end of gas mass flow controller 111 and Drexel bottle 22 connect plasma reactor 32, the 2nd O2Makings
The amount output termination Drexel bottle 22 of flow controller 112, Drexel bottle 22 is located at vapor to be occurred in thermostat water bath 21, NO makings amounts
The output end of flow controller 121, SO2The output end of gas mass flow controller 131, a N2Gas mass flow controller 141 is exported
End and Hg0The output end of osmos tube 16 connects gas mixer chamber 4, the 2nd N respectively2The output termination of gas mass flow controller 142 Hg0Ooze
Saturating pipe 16, Hg0Osmos tube 16 is located at flue gas to be occurred in thermostat water bath 17, the output end difference cigarette receiving qi leel of gas mixer chamber 4
Analyzer 51, mercury vapourmeter 52 and exhaust gas processing device 55.
KCl bottles 53 and tube furnace 54 can be sequentially provided with the import of mercury vapourmeter 52.
The method for carrying out the pouring-in simultaneous SO_2 and NO removal removal of mercury using the utility model is as follows：
1) flow of mass flow controller is respectively set to O2 400 1#、O2 100 2#、SO2 80、NO 66、N2
854, unit is mL/min；
2) open flue gas and thermostat water bath occurs, open N2Gas cylinder, makes Hg0Osmos tube is in constant bath temperature 57.5
DEG C, the stabilization 2h under constant flow rate 0.2L/min carrier gas strippings obtains the mercury release rate of stabilization；
3) steam evaporator is opened, it is produced the aqueous O of steady concentration2, open temperature control box and set its temperature as
140 DEG C, heating tape is set to be stably held in 140 DEG C；
4) O is opened2Gas cylinder and mass flow controller and valve, O2Enter plasma reactor (plasma with vapor
Reactor according is closed), the flow of gas mixer chamber is entered by pump (see the mark A in Fig. 1) control, with simulated flue gas component in gas
It is well mixed in body mixing chamber, by flue gas analysis unit (flue gas analyzer 51) and Hg0Analytic unit (mercury vapourmeter 52) detection system
Flue gas composition concentration (NO, SO in system2) and Hg0Concentration, if surveyed Hg0Concentration is 50 μ g/m3, then step 5 can be carried out), otherwise etc.
Treat Hg0Osmos tube stabilization；
5) high voltage power supply is opened, regulation voltage makes O to 5kV2With vapor by produced after plasma discharge reaction
Active particle reacted in gas mixing room by with simulated flue gas component, by flue gas analyzer and mercury vapourmeter detecting system
NO、SO2And Hg0Concentration, after measured result contrast, you can obtain the active oxidation particle of ion precursor reactant generation for NO, SO2
And Hg0Oxidation efficiency；
6) flue gas absorbs Hg respectively by KCl solution and NaOH alkali lye2+After sour gas, by flue gas analyzer and survey mercury
The pollutant concentration of instrument inspection system outlet, draws the efficiency of the system desulphurization denitration removal of mercury.
1. each part is assembled into the device of the complete pouring-in simultaneous SO_2 and NO removal removal of mercury by Fig. 1, is used in the system
To solution be matching while using.
2. producing simulation coal-fired flue-gas (the 50 μ g/m3Hg at 140 DEG C containing typical concentration component0, 9% moisture, 300ppm
NO、300ppm SO2) as a example by, operate as follows：
The flow of mass flow controller shown in Fig. 1 is respectively set to (unit by 3：mL/min)O2 400 1#、O2 100
2#、SO2 80、NO 66、N2 854。
4. water-bath is opened, N is opened2, mercury osmos tube is in 57.5 DEG C constant of bath temperature, in constant flow rate
Stabilization 2h obtains the mercury release rate of stabilization under 0.2L/min carrier gas strippings.Steam evaporator is opened, it is produced steady concentration
Aqueous O2.Open temperature control box and set its temperature as 140 DEG C, heating tape is stably held in 140 DEG C.
5. O is opened2Gas cylinder and mass flow controller and valve, O2Enter plasma reactor (plasma with vapor
Reactor according is closed), the flow of route 1 is entered by pump control, extract 450mL/min, remaining 50mL/min route vias 1 and mould out
Intend flue gas composition (1L/min) to be well mixed in mixing chamber, flue gas composition concentration (NO and SO in detecting system2) and Hg0Concentration.
If surveyed Hg0Concentration is 50 μ g/m3, then next step can be carried out, otherwise wait mercury pipe stabilization.
6. turn on the power, slow regulation voltage makes O to 5kV2With vapor by produced after plasma discharge reaction
Active particle fully reacted in mixing chamber with simulated flue gas component (1L/min) by route 1, by flue gas analyzer and survey mercury
NO, SO in instrument detecting system2And Hg0Concentration.By with 2.3 in measured result contrasted, you can obtain ion precursor reactant generation
Active oxidation particle for NO, SO2And Hg0Oxidation efficiency.
7. flue gas absorbs Hg respectively by KCl solution and NaOH alkali lye in system2+After sour gas, by flue gas analyzer
The pollutant concentration exported with mercury vapourmeter inspection system, draws the efficiency of the system desulphurization denitration removal of mercury.
Claims (3)
1. a kind of pouring-in simultaneous SO_2 and NO removal mercury removal device, it is characterised in that be provided with coal-fired flue-gas generating unit, vapor hair
Raw unit, plasma generating unit, gas mixing units and detection unit；
The coal-fired flue-gas generating unit is provided with O2Gas cylinder, NO gas cylinders, SO2Gas cylinder, N2Gas cylinder, Hg0Osmos tube and flue gas occur permanent
Warm water bath；
There is thermostat water bath, Drexel bottle and connecting line by vapor and constitute in the vapor generating unit；
The plasma generating unit is provided with high voltage power supply and plasma reactor；
The gas mixing units are made up of gas mixer chamber and connecting line, and periphery is tied with heating tape；
The detection unit is provided with flue gas analyzer and mercury vapourmeter；
Vapor is produced by the Drexel bottle equipped with water being positioned in vapor generation thermostat water bath, is connected with Drexel bottle constant
The stripping carrier gas O of flow2；
The O2Cylinder outlet is respectively equipped with an O2Gas mass flow controller and the 2nd O2Gas mass flow controller, it is described
NO cylinder outlets are provided with NO gas mass flow controllers, the SO2Cylinder outlet is provided with SO2Gas mass flow controller, the N2
Cylinder outlet is provided with a N2Gas mass flow controller and the 2nd N2Gas mass flow controller；First O2Gas mass flow control
Device output end processed and Drexel bottle connect plasma reactor, the 2nd O2The output termination Drexel bottle of gas mass flow controller, gas washing
Bottle is located at vapor to be occurred in thermostat water bath, NO gas mass flow controllers output end, SO2Gas mass flow controller is exported
End, a N2Gas mass flow controller output end and Hg0Osmos tube output end connects gas mixer chamber, the 2nd N respectively2Makings amount
Flow controller output termination Hg0Osmos tube, Hg0Osmos tube is located at flue gas to be occurred in thermostat water bath, the output of gas mixer chamber
End connects flue gas analyzer, mercury vapourmeter and exhaust gas processing device respectively.
2. as claimed in claim 1 a kind of pouring-in simultaneous SO_2 and NO removal mercury removal device, it is characterised in that in the import of mercury vapourmeter
It is sequentially provided with KCl bottles and tube furnace.
3. as claimed in claim 1 a kind of pouring-in simultaneous SO_2 and NO removal mercury removal device, it is characterised in that the gas mixer chamber
Periphery is tied with heating tape.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621430913.8U CN206295780U (en) | 2016-12-23 | 2016-12-23 | A kind of pouring-in simultaneous SO_2 and NO removal mercury removal device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621430913.8U CN206295780U (en) | 2016-12-23 | 2016-12-23 | A kind of pouring-in simultaneous SO_2 and NO removal mercury removal device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206295780U true CN206295780U (en) | 2017-07-04 |
Family
ID=59204199
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|---|---|---|---|
| CN201621430913.8U Expired - Fee Related CN206295780U (en) | 2016-12-23 | 2016-12-23 | A kind of pouring-in simultaneous SO_2 and NO removal mercury removal device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106492601A (en) * | 2016-12-23 | 2017-03-15 | 厦门大学 | A kind of pouring-in simultaneous SO_2 and NO removal method for removing hydrargyrum |
| CN109647124A (en) * | 2018-11-19 | 2019-04-19 | 华中科技大学 | A kind of plasma flame method lead occurs and adsorption reaction integral system and method |
| CN113354016A (en) * | 2021-05-06 | 2021-09-07 | 浦恩远 | Water sample mercury vapor stripping and concentrating device |
-
2016
- 2016-12-23 CN CN201621430913.8U patent/CN206295780U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106492601A (en) * | 2016-12-23 | 2017-03-15 | 厦门大学 | A kind of pouring-in simultaneous SO_2 and NO removal method for removing hydrargyrum |
| CN109647124A (en) * | 2018-11-19 | 2019-04-19 | 华中科技大学 | A kind of plasma flame method lead occurs and adsorption reaction integral system and method |
| CN113354016A (en) * | 2021-05-06 | 2021-09-07 | 浦恩远 | Water sample mercury vapor stripping and concentrating device |
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