CN103055666A - Method for removing nitric oxide in flue gas - Google Patents
Method for removing nitric oxide in flue gas Download PDFInfo
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- CN103055666A CN103055666A CN2011103225501A CN201110322550A CN103055666A CN 103055666 A CN103055666 A CN 103055666A CN 2011103225501 A CN2011103225501 A CN 2011103225501A CN 201110322550 A CN201110322550 A CN 201110322550A CN 103055666 A CN103055666 A CN 103055666A
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- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 title claims abstract description 56
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title abstract description 14
- 239000003546 flue gas Substances 0.000 title abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 29
- 239000007789 gas Substances 0.000 claims abstract description 24
- 238000010521 absorption reaction Methods 0.000 claims abstract description 21
- 238000000034 method Methods 0.000 claims abstract description 20
- 239000007791 liquid phase Substances 0.000 claims abstract description 10
- 239000012071 phase Substances 0.000 claims abstract description 7
- 239000002250 absorbent Substances 0.000 claims description 23
- 230000002745 absorbent Effects 0.000 claims description 23
- 229910052813 nitrogen oxide Inorganic materials 0.000 claims description 22
- CWYNVVGOOAEACU-UHFFFAOYSA-N fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 14
- KCXVZYZYPLLWCC-UHFFFAOYSA-N edta Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 claims description 10
- 239000008246 gaseous mixture Substances 0.000 claims description 10
- 150000001875 compounds Chemical class 0.000 claims description 9
- 235000013495 cobalt Nutrition 0.000 claims description 8
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 6
- 229910052803 cobalt Inorganic materials 0.000 claims description 6
- 239000010941 cobalt Substances 0.000 claims description 6
- QPCDCPDFJACHGM-UHFFFAOYSA-N N,N-bis{2-[bis(carboxymethyl)amino]ethyl}glycine Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(=O)O)CCN(CC(O)=O)CC(O)=O QPCDCPDFJACHGM-UHFFFAOYSA-N 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 5
- 230000002411 adverse Effects 0.000 claims description 4
- 150000001412 amines Chemical class 0.000 claims description 4
- IFQUWYZCAGRUJN-UHFFFAOYSA-N 2-[2-(carboxymethylamino)ethylamino]acetic acid Chemical compound OC(=O)CNCCNCC(O)=O IFQUWYZCAGRUJN-UHFFFAOYSA-N 0.000 claims description 3
- 229960003330 Pentetic Acid Drugs 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims description 2
- 229910001429 cobalt ion Inorganic materials 0.000 claims description 2
- 229940009662 edetate Drugs 0.000 claims description 2
- BTMQKQSSEQVSAS-UHFFFAOYSA-N cobalt;ethane-1,2-diamine Chemical compound [Co].NCCN BTMQKQSSEQVSAS-UHFFFAOYSA-N 0.000 claims 1
- 235000000396 iron Nutrition 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 10
- 230000005484 gravity Effects 0.000 abstract description 5
- 230000001105 regulatory Effects 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 231100000078 corrosive Toxicity 0.000 abstract 1
- 231100001010 corrosive Toxicity 0.000 abstract 1
- 239000001257 hydrogen Substances 0.000 abstract 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract 1
- 229910052739 hydrogen Inorganic materials 0.000 abstract 1
- GQPLMRYTRLFLPF-UHFFFAOYSA-N nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 19
- 238000005516 engineering process Methods 0.000 description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- XSQUKJJJFZCRTK-UHFFFAOYSA-N urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 4
- 238000003916 acid precipitation Methods 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- 239000007792 gaseous phase Substances 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- PIICEJLVQHRZGT-UHFFFAOYSA-N 1,2-ethanediamine Chemical compound NCCN PIICEJLVQHRZGT-UHFFFAOYSA-N 0.000 description 2
- 229910002089 NOx Inorganic materials 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000004202 carbamide Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000016507 interphase Effects 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 206010022114 Injury Diseases 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000000536 complexating Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000003009 desulfurizing Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229940006477 nitrate ion Drugs 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 239000001184 potassium carbonate Substances 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000007619 statistical method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001131 transforming Effects 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium(0) Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Abstract
A method for removing nitric oxide in flue gas belongs to the technical field of super gravity. The method comprises the following steps of: starting a super-gravity reactor, regulating the rotation speed of a rotator to be 100-4000rpm; feeding an absorption liquid and a mixed gas containing NO (nitric oxide) into a super-gravity revolving bed reactor from a liquid phase inlet and a gas phase inlet respectively, wherein the absorption liquid flows from the inner edge of the rotator to the outer edge of the rotator under the action of centrifugal power, is in counter-current or cross-current contact with the gas in the super-gravity revolving bed reactor and carries out reaction, and thus the NO removing process is finished; the pH (potential of hydrogen) value of the absorption liquid is 5-10, the volume flow ratio of the gas and the liquid is (30-300):1, the pressure of the system during the absorption process is 0.1-4.0MPa, the temperature of the system is 10-80 DEG C, and the concentration of the complex absorption solution is 0.005-0.1mol/L. The removing rate of NO in the mixed gas reaches more than 85%. The method provided by the invention is low in equipment investment, is low in energy consumption, is environment-friendly and is non-corrosive to equipment.
Description
Technical field
The present invention relates to a kind of with complex solution as absorbent, utilize high-gravity rotating bedly as reactor, remove the new method of NO in the industrial tail gas.The method can be used for the industrial discharge gas cleaning, is applicable to the separation that removes of NO in thermal power industry flue gas and the process industry tail gas, and belongs to the high-gravity technology field.
Background technology
Nitrogen oxide (NO
x) refer to the compound that is only formed by nitrogen, two kinds of elements of oxygen.Nitrogen oxide as air pollutants often refers to NO and NO
2NOx discharge capacity maximum be heat power station, account for national NO
xMore than 40% of total emission volumn.The nitrogen oxide complicated component of Thermal Power Generation Industry discharging, but wherein 90% direct emission is NO.The Thermal Power Generation Industry nitrogen oxide emission is huge, in the urgent need to control.Statistical analysis according to " the Chinese thermal power plant Emission Controlling Technology of Nitric Oxides project study report " of China environmental protection industry association and organization, the nitrogen oxide total amount of power plant emission in 2007 has increased to 8,400,000 tons, increased closely 40.6% than 597.3 ten thousand tons in 2003, accounted for 35%～40% of national nitrogen oxide emission.National nitrogen oxide emission reached 2,000 ten thousand tons in 2008, became the first in the world discharged nitrous oxides state.According to scholarly forecast, along with the quickening of the national economic development, population growth and urbanization process, Chinese nitrogen oxide emission will continue to increase.If without control, nitrogen oxide emission will reach 3,000 ten thousand tons at the year two thousand twenty, bring huge threat for China's atmospheric environment.Result of study shows that nitrogen oxide also can produce multiple secondary pollution except as the primary pollution injury health.Nitrogen oxide is the major reason that forms regional fine particles pollution and grey haze, has caused China's developed area atmospheric visibility increasingly to descend, and grey haze fate constantly increases.In addition, the increase of nitrogen oxide emission so that China's Acid Rain Pollution by sulfuric acid type to sulfuric acid and the compound transformation of nitric acid, nitrate ion in acid rain shared ratio from 1/10 of the eighties in last century progressively rise in recent years 1/3.The Eleventh Five-Year Plan period, the rapid growth of discharged nitrous oxides has aggravated the degradating trend of regional acid rain, partial offset China in the great efforts of paying aspect the sulfur dioxide reduction of discharging.
Selective catalytic reduction method (SCR) is the denitration method for flue gas of present main application.The method is to utilize the catalyst such as iron, vanadium, chromium, cobalt, nickel and alkali metal to utilize ammonia or urea that NOx is reduced to N when temperature is 200 ℃～450 ℃
2But also there is certain defective in the method, for example contains SO in the flue gas
2, grit and water smoke, all unfavorable to catalytic reaction and catalyst, so adopt the SCR method must at first carry out flue gas ash removal and desulfurization, or select the catalyst that is not subject to the dirty flue gas pollution effect; To make simultaneously catalyst have certain activity, also higher flue-gas temperature must be arranged, so the method energy consumption be higher.Emptyingly after the ammonia that uses in the method in addition or the urea incomplete reaction be easy to cause secondary pollution.
In recent years, adopt complex solution that the wet denitration technical research that nitrogen oxides in effluent removes is extensively carried out.The reaction rate of complex solution and nitrogen oxide is very fast, and the complexing product can decompose and emits nitrogen oxide under certain conditions, thereby realizes that the enrichment utilization of nitrogen oxide and the regeneration cycle of absorbent use.Therefore, use complex solution to carry out the method that nitrogen oxides in effluent removes and be considered to the out of stock technology of a kind of very promising flue gas.Because the reaction rate of complex solution and nitrogen oxide is very fast, the mass transport process in the liquid phase becomes the key factor that affects removal of nitrogen oxide speed.Developing new reactor strengthens the vapour-liquid mass of this process and becomes the important prerequisite of this Technique Popularizing to industrial applications.
High-gravity technology is the new technology of utilizing the Elevated Gravity more much bigger than terrestrial gravitation acceleration that mass transfer, diabatic process and micro mixing are strengthened, produces the Elevated Gravity of simulating by rotation on earth and obtains.It can increase substantially the conversion ratio of reaction and selective, dwindles significantly the volume of reactor, simplifies technique, flow process, implementation procedure energy-efficient, reducing polluted emission.Research and analysis show, under Elevated Gravity, molecular diffusion between different sized molecules and interphase mass transfer process are all than in after the match faster of terrestrial gravitation, produce the contact of flowing in gas one liquid, liquid-liquid, the liquid one solid porous media of two-phase under the Elevated Gravity larger hundreds of times to thousand times than earth gravitational field, huge shearing force makes liquid crushing become nano level film, silk and drips, produce boundary huge and that upgrade fast, make and improve 1～3 order of magnitude in the traditional tower of interphase mass transfer speed ratio, mass transport process is greatly strengthened.About open in the patent (ZL95215430.7) of hypergravity swinging bed device before the applicant (Beijing University of Chemical Technology).On this basis, the applicant is also obtaining important progress aspect the application study of high-gravity technology, this technology from separate, the physical process of desorb is extended to chemical reaction process.As: propose in (CN101168115A) by removing CO in the conversion gas with Hot potassium carbonate solution, sodium hydroxide solution or the potassium hydroxide solution of interpolation activator as absorbent in " a kind of method that removes carbon dioxide in the conversion gas "
2But the employing high-gravity technology uses complex solution to carry out the research of denitrating flue gas as absorbent, and so far there are no both at home and abroad reports.
Summary of the invention
The purpose of this invention is to provide a kind of with supergravity reactor as consersion unit, with complex solution as absorbent, from gaseous mixture, remove the method for NO, the gaseous mixture that contains NO and absorbent adverse current or cross-flow in rotating packed bed reactor contact and react, and finish the subtractive process of NO.Because the NO in the flue gas more than 90%
xBe NO, thus wet denitration for mainly be the removing of NO in the flue gas.
A kind of method that removes nitrogen oxides in effluent of the present invention is characterized in that, may further comprise the steps:
(a) open rotating packed bed reactor, and rotor speed is adjusted to 100～4000 rev/mins of predetermined values;
(b) absorbent and the gaseous mixture that contains NO are sent to the rotating packed bed reactor from liquid phase import and gas phase import respectively, absorbent flows to the rotor outer rim by the rotor inner edge under the effect of centrifugal force, contact with gas adverse current or cross-flow in rotating packed bed reactor and react, finish the subtractive process of NO.The pH value of absorption liquid is 5～10, is preferably 6～8, most preferably is 7.Gas-liquid by volume flow-rate ratio is 30～300: 1, is preferably 50～150: 1, more preferably 60～100: 1.The pressure of system is 0.1～4.0MPa during absorption, is preferably 0.1～1.0MPa, most preferably is 0.1MPa.The temperature of system is preferably 15～40 ℃ at 10～80 ℃, most preferably is 20～30 ℃.The concentration of complex compound absorption liquid is preferably 0.01～0.08mol/L at 0.005～0.1mol/L, most preferably is 0.03～0.05mol/L.
The removing in the separation method of N0 in the gaseous mixture provided by the invention, used is high-gravity rotating bed including, but not limited to hypergravity whirligigs such as RPB, deflector type, helical duct, a fixed rotor, rotating compact discs.The rotating speed of high-gravity rotating bed rotor is 100～4000 rev/mins, is preferably 1500～3500 rev/mins, most preferably is 2500～3200 rev/mins.
Absorbent of the present invention is complex solution or its mixture that contains ferrous iron or cobalt ions.When adopting complex solution as absorbent, used complex compound absorption liquid is including but not limited to [ethylenediamine tetra-acetic acid is ferrous] (Fe
II[EDTA]), [Cobalt Edetate] (Co[EDTA]), [ethylenediamine cobalt] (Co[EN]
2), [amine second three acid ferrous] (Fe
II[NTA]), [amine second three sour cobalts] (Co[NTA]), [EDDA is ferrous] (Fe
II[EDDA]), [diethylene-triamine pentaacetic acid ferrous] (Fe
II[DTPA]) etc.
In addition, when adopting complex solution as absorbent, used absorbent enters waste liquor storage tank through behind the supergravity reactor, prepares regeneration.
The invention effect:
The present invention can effectively remove separation with the NO in the unstripped gas, the removal efficiency of NO can reach more than 85% (volume) in the gaseous mixture, the technical method that removes NO in the absorption gaseous mixture that the present invention proposes, it is few to have equipment investment, that energy consumption is low, equipment takes up space is little, environmentally friendly, to equipment without advantages such as corrosion.
Description of drawings
Fig. 1 is process chart of the present invention
Wherein: 3-is high-gravity rotating bed for the import of 1-liquid phase import 2-gas phase
4-rotor 5-gaseous phase outlet 6-liquid-phase outlet
Specific embodiments
Below in conjunction with drawings and Examples embodiment of the present invention are further specified.Device therefor is publication (ZL95215430.7).
The reaction unit figure of a kind of embodiment of the present invention as shown in Figure 1.Open high-gravity rotating bedly 3, adjusting rotary speed is to desired speed.Absorbent is sprayed the inner edge of high-gravity rotating bed rotor 4 by liquid distribution trough via liquid phase inlet tube 1, the gaseous mixture that contains NO from a upper workshop section enters into rotating packed bed reactor via gas phase inlet tube 2, contact with absorption liquid adverse current or cross-flow in high-gravity rotating bed rotor, under the hypergravity condition, carry out removing of NO, then discharge from gaseous phase outlet 5, enter follow-up workshop section.Absorbent flows out from the liquid-phase outlet 6 that is positioned at the rotating packed bed reactor bottom.Adopt the concentration of NO in the flue gas analyzer on-line analysis rotating packed bed reactor exit gas.
Embodiment 1
Unstripped gas forms: NO and the N of 1000ppm (volume fraction meter)
2The mist that forms.
Absorbent is [ethylenediamine tetra-acetic acid is ferrous] (Fe
II[EDTA]), the pH value is 7, concentration is 0.02mol/L.The regulating system temperature is 20 ℃, pressure is adjusted to 0.1Mpa, start rotating packed bed reactor, the regulating rotary rotor speed is 2825r/m, then open the by-pass valve control of liquid reactor import, absorbent is sprayed the inner edge of high-gravity rotating bed rotor 4 by liquid distribution trough via liquid phase inlet tube 1, the flow of regulating liquid is 2.65L/h, the gaseous mixture that contains NO from a upper workshop section enters into rotating packed bed reactor via gas phase inlet tube 2, with absorption liquid counter current contacting in high-gravity rotating bed rotor, under the hypergravity condition, carry out the capture of NO, then discharge from gaseous phase outlet 5, enter follow-up workshop section.The flow of gas is 0.39m
3/ h.Absorption liquid flows out from the liquid-phase outlet 6 that is positioned at the rotating packed bed reactor bottom.Adopt the concentration of NO in the flue gas analyzer on-line analysis rotating packed bed reactor exit gas.The concentration of exit gas NO is that the removal efficiency of 201, NO reaches 79.9%.
Embodiment 2-19
Technological process and step are with embodiment 1, and flow, rotor speed and the result of the test of the temperature of each embodiment, pressure, absorbent kind, absorbent pH value, concentration of absorbing, gas-liquid see Table 1.
Absorbent is [ethylenediamine tetra-acetic acid is ferrous] (Fe
II[EDTA]), [diethylene-triamine pentaacetic acid ferrous] (Fe
II[DTPA]), [ethylenediamine cobalt] (Co[EN]
2) etc. contain complex solution or its mixture of ferrous iron or cobalt central ion.
Operating temperature is 10～70 ℃, and pressure is 0.01～4MPa, and the pH value of absorbent is 5～10, and the concentration of absorbent is 0.005～0.1mol/L, and the volume flow ratio of absorbent and gaseous mixture is 30～300: 1.
The process conditions of each embodiment of table 1 and experimental result
Claims (10)
1. a method that removes nitrogen oxides in effluent is characterized in that, may further comprise the steps:
(a) open rotating packed bed reactor, and rotor speed is adjusted to 100～4000 rev/mins of predetermined values;
(b) complex compound absorption liquid and the gaseous mixture that contains NO are sent to the rotating packed bed reactor from liquid phase import and gas phase import respectively, absorbent flows to the rotor outer rim by the rotor inner edge under the effect of centrifugal force, contact with gas adverse current or cross-flow in rotating packed bed reactor and react, finish the subtractive process of NO; The pH value of absorption liquid is 5～10, and gas-liquid by volume flow-rate ratio is 30～300: 1, and the pressure of system is 0.1～4.0MPa during absorption, and the temperature of system is at 10～80 ℃, and the concentration of complex compound absorption liquid is at 0.005～0.1mol/L.
2. according to the method for claim 1, it is characterized in that the complex compound absorption liquid is complex solution or its mixture that contains ferrous iron or cobalt ions.
3. according to the method for claim 2, it is characterized in that complex compound is selected from ethylenediamine tetra-acetic acid ferrous iron, Cobalt Edetate, ethylenediamine cobalt, amine second three acid ferrous irons, amine second three sour cobalts, EDDA is ferrous, diethylene-triamine pentaacetic acid is ferrous.
4. according to the method for claim 1, it is characterized in that described high-gravity rotating bed RPB, deflector type, helical duct, a fixed rotor, the rotating compact disc hypergravity whirligig of being selected from.
5. according to the method for claim 1, it is characterized in that the pH value 6～8 of absorption liquid.
6. according to the method for claim 1, it is characterized in that gas-liquid by volume flow-rate ratio is 50～150: 1.
7. according to the method for claim 1, it is characterized in that the pressure of system is 0.1～1.0Mpa during absorption.
8. according to the method for claim 1, it is characterized in that the temperature of system is 15～40 ℃.
9. according to the method for claim 1, it is characterized in that the concentration of complex compound absorption liquid is 0.01～0.08mol/L.
10. according to the method for claim 1, it is characterized in that the rotating speed of high-gravity rotating bed rotor is 1500～3500 rev/mins.
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| CN2011103225501A CN103055666A (en) | 2011-10-21 | 2011-10-21 | Method for removing nitric oxide in flue gas |
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| CN103432889A (en) * | 2013-09-06 | 2013-12-11 | 余国贤 | Method for denitration of complexing ferroporphyrin smoke based on supergravity |
| CN103432879A (en) * | 2013-09-06 | 2013-12-11 | 余国贤 | Method for desulfurization and denitrification of complexing ferroporphyrin smoke based on supergravity |
| CN103521160A (en) * | 2013-09-29 | 2014-01-22 | 北京化工大学 | Multifunctional and multipurpose multistage rotary packed bed reactor device and method for performing multiphase and multicomponent reaction by using device |
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| CN105854542A (en) * | 2016-05-23 | 2016-08-17 | 天津市思茂阁科技有限责任公司 | Method for purifying nitrogen-containing oxide tail gas |
| CN106582239A (en) * | 2016-12-19 | 2017-04-26 | 北京化工大学 | Device for treating hydrazine-containing waste gas in aircraft emergency power system and application of device |
| CN107303459A (en) * | 2016-04-25 | 2017-10-31 | 云南民族大学 | The innoxious removing low concentration of NO of high-gravity technologyxDevice |
| CN107303463A (en) * | 2016-04-25 | 2017-10-31 | 云南民族大学 | The innoxious removing low concentration of NO of high-gravity technologyxMethod |
| TWI613003B (en) * | 2015-12-08 | 2018-02-01 | 國立清華大學 | Apparatus for absorbing a component from a gas mixture |
| CN109200813A (en) * | 2018-11-21 | 2019-01-15 | 安徽工业大学 | A kind of denitrfying agent and preparation method catalytic-reduction denitrified for sintering flue gas |
| CN109200789A (en) * | 2018-11-21 | 2019-01-15 | 安徽工业大学 | A kind of kiln gas low-temperature biological enzymatic reduction denitrification apparatus and method |
| CN111467946A (en) * | 2020-04-22 | 2020-07-31 | 运城学院 | NO in preparation process of molecular sieve catalystxMethod for treating exhaust gas |
| CN112090273A (en) * | 2020-08-28 | 2020-12-18 | 中北大学 | Photocatalyst-loaded filler and its high-gravity NO removalxApparatus and process of |
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