CN106110860A - A kind of oxidative absorption high gravity desulfurization denitrating system and method - Google Patents
A kind of oxidative absorption high gravity desulfurization denitrating system and method Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 62
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 38
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 34
- 230000023556 desulfurization Effects 0.000 title claims abstract description 29
- 230000005484 gravity Effects 0.000 title claims abstract description 28
- 230000001590 oxidative effect Effects 0.000 title claims abstract description 11
- 239000003814 drug Substances 0.000 claims abstract description 62
- 239000003546 flue gas Substances 0.000 claims abstract description 38
- 239000007789 gas Substances 0.000 claims abstract description 37
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000012425 OXONE® Substances 0.000 claims abstract description 22
- HJKYXKSLRZKNSI-UHFFFAOYSA-I pentapotassium;hydrogen sulfate;oxido sulfate;sulfuric acid Chemical compound [K+].[K+].[K+].[K+].[K+].OS([O-])(=O)=O.[O-]S([O-])(=O)=O.OS(=O)(=O)O[O-].OS(=O)(=O)O[O-] HJKYXKSLRZKNSI-UHFFFAOYSA-I 0.000 claims abstract description 22
- 238000012856 packing Methods 0.000 claims abstract description 20
- 239000000945 filler Substances 0.000 claims abstract description 19
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 18
- 238000010992 reflux Methods 0.000 claims abstract description 8
- 230000008676 import Effects 0.000 claims abstract description 7
- 239000000243 solution Substances 0.000 claims description 21
- 230000001276 controlling effect Effects 0.000 claims description 7
- 239000008155 medical solution Substances 0.000 claims description 5
- 239000000835 fiber Substances 0.000 claims description 4
- 239000000395 magnesium oxide Substances 0.000 claims description 4
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 4
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 238000013459 approach Methods 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims description 2
- 239000012530 fluid Substances 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims 1
- 239000000463 material Substances 0.000 claims 1
- 238000012545 processing Methods 0.000 abstract description 8
- 238000002360 preparation method Methods 0.000 abstract 1
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 18
- 230000008569 process Effects 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 10
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 9
- 238000007254 oxidation reaction Methods 0.000 description 7
- 230000003647 oxidation Effects 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 5
- 238000010894 electron beam technology Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000010531 catalytic reduction reaction Methods 0.000 description 3
- 239000003638 chemical reducing agent Substances 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 3
- 150000003254 radicals Chemical class 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000003915 air pollution Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 1
- 208000019901 Anxiety disease Diseases 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical group N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000036506 anxiety Effects 0.000 description 1
- 210000001367 artery Anatomy 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 235000013877 carbamide Nutrition 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010668 complexation reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- JZBWUTVDIDNCMW-UHFFFAOYSA-L dipotassium;oxido sulfate Chemical compound [K+].[K+].[O-]OS([O-])(=O)=O JZBWUTVDIDNCMW-UHFFFAOYSA-L 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- -1 hydroxyl radical free radical Chemical class 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 238000004080 punching Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 210000002700 urine Anatomy 0.000 description 1
- 210000003462 vein Anatomy 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The present invention provides a kind of oxidative absorption high gravity desulfurization denitrating system and method, described system is made up of doser and supergravity reactor, described doser includes medicament pond, and the medicine liquid outlet in medicament pond connects dosing pump import, and dosing pump outlet is connected with the medicament inlet of supergravity reactor；Described supergravity reactor includes that housing, enclosure interior are provided with annular packing rotor, and housing is provided with gas feed, gas outlet, medicament inlet and agent outlet, and described gas outlet is connected with air-introduced machine, and agent outlet is connected with the refluxing opening in medicament pond.The processing step of described method includes: preparation mass concentration is the potassium monopersulfate solutions of 1 ~ 10 ‰；Being continually introduced by potassium monopersulfate solutions inside the filler of supergravity reactor annular packing rotor, and the mixed flue gas of dedusting introduces supergravity reactor, control annular packing rotor at the uniform velocity rotates and mixed flue gas is carried out desulphurization denitration；Control the flow velocity of gas control valve, the flue gas after desulphurization denitration is emptied.
Description
Technical field
The present invention relates to environmental technology field, be specifically related to a kind of oxidation-absorption high gravity desulfurization denitrating system and method.
Background technology
State Council in 2013 issues three files continuously with regard to energy-saving and emission-reduction problem: " ten measures of prevention and control of air pollution ", " state
Business institute is about the suggestion accelerating development energy-conserving and environment-protective industry " and " prevention and control of air pollution action plan ", to energy-saving and emission-reduction, air dirt
Dye control proposes requirements at the higher level.
The method processing nitrogen oxides and/or sulfide the most both at home and abroad mainly has: SNCR method
(SNCR), at selective catalytic reduction (SCR), high energy electron active oxidation method, solution absorption method, oxidative absorption method, biology
Logos etc..Non-selective catalytic reduction (SNCR method) and selective catalytic reduction (SCR method) are mainly used to process nitrogen oxidation
Thing.
SNCR method is containing NHxAfter the reducing agent of base sprays into the region that fire box temperature is 850～1100 DEG C, heat point rapidly
Solution becomes NH3 and other by-product, subsequently NH3With the NO in flue gasxCarry out SNCR reaction and generate N2, the method is inefficient,
Between 40-50%, advantage be invest the fewest；SCR method is under the effect of catalyst, utilizes reducing agent (such as NH3, liquefied ammonia, urine
Element) come " selectivity " with the NO in flue gasxReact and generate the N of nontoxic pollution-free2And H2O, high than SNCR method of its efficiency,
About 80%, but the catalyst costs of SCR method typically constitutes about the 40% of SCR system initial outlay, and its operating cost is the biggest
Affected by catalyst life in degree, thus investment is higher.SNCR method and SCR method all must utilize ammonia as reducing agent, and
Denitration enterprise often build the place that comparison is remote in mostly, and the expense purchasing, transport and preserving liquefied ammonia or carbamide is high, also has
Bigger danger.
High energy electron active oxidation method is different according to the producing method of high energy electron, is divided into again electron beam irradiation method (EBA)
With impulse electric corona plasma method (PPCP).Electron beam irradiation method (EBA) is a kind of desulphurization denitration new technology, and advantage is dry method
Processing procedure, does not produce waste water and dregs；System is simple, and easy to operate, process is easily controllable；For different sulfur content flue gas and
The well adapting to property of change of exhaust gas volumn and Steam Generator in Load Follow；Side-product is ammonium sulfate and ammonium nitrate mixture, can be used as
Fertile.The Chengdu steam power plant of China introduced this electron beam irradiation technology in 1997, and actual motion desulfurization degree reaches more than 80%, but
Denitration efficiency is less than 20%, it is seen that electron beam irradiation method still has a lot of work to do as wanted widespread adoption in industrially desulfurized denitration.
Impulse electric corona plasma method grows up on the basis of electron beam irradiation method, and its advantage is high energy electron
Produced by corona discharge self, from without expensive electron gun, be also not required to radiation shield；Finished product can be used as fertilizer, does not produces
Raw secondary pollution；Within Ultra-short pulse action time, electronics obtains acceleration, and the ion big to the inertia not producing free radical
Do not accelerate, thus the method has the biggest potentiality at energy-conservation aspect；The safe operation of station boiler is not the most affected by it.But
It is that the power consumption of this technology is higher, accounts for about the 3-5% of power plant's gross generation.In addition the arteries and veins high-power, narrow of this high-voltage pulse power source
The key problems such as punching, long-life how realization have to be solved.
Solution absorption method utilizes the characteristic that nitrogen oxides and sulfide are sour gas, by alkaline solution in waste gas
Nitrogen oxides and sulfide remove, and can remove SO under certain condition simultaneously2And NOx.The advantage of the method is to reach
To SO2And NOxPreferably removal effect；Shortcoming be the specific denitrating system used often exist catalyst surface fouling and in
The phenomenon of poison[1], cause obstruction and the corrosion of air preheater/gas heat exchanger.Additionally, due to the NO in nitrogen oxides be difficult to by
Solution absorbs, and also needs the methods such as combination oxidation and complexation to NO process, and technical process is relatively complicated.
Oxidative absorption method is frequently with ozone, H2O2、NaClO2Deng oxidant to SO2And NOxCarry out oxidation removal.The method is gone
Except efficiency is higher, and can simultaneously desulfurization, it is easy to operation, but the ozone used and NaClO are expensive, cause its desulfurization simultaneously
The high cost of denitration.Although H2O2Cheap, but reaction temperature reaches H when more than 60 DEG C2O2Start acutely to decompose, because of
This, under conditions of industrial high temperature flue gas produces, it is necessary to flue gas is carried out cooling process, and investment cost is higher, is unfavorable for
Industrialization[2]。
Biological treatment is dry method, the semi-dry process flue gas desulphurization denitration technology developed in recent years, but due to these skills
Art is still in laboratory development, and its desulphurization denitration mechanism waits research, thus does not the most possess the ability of actual application.
In sum, all there are the pluses and minuses of himself in various process nitrogen oxides, the method for sulfide, single method
Use and can not meet reality need, thus associating removing sulfuldioxide is increasingly becoming countries in the world research institution, focus of attention
Focus.The development of this kind of technology is trend of the times, but how de-real ripe technology be actually rare so far.
List of references
[1] Yao Wei, Liu little Feng etc..SCR catalyst poisoning and correlative protection measure [J].Modern chemical industry, 2015,35(6): 22-
25。
[2] Lin Binfan, Yang Lan etc..The progress [J] of liquid phase oxidation absorption process simultaneous SO_2 and NO removal technology.Coal Chemical Industry,
2015,43(5): 24-27.
Summary of the invention
The problem existed for existing desulphurization denitration technology, the present invention provides a kind of oxidation-absorption high gravity desulfurization denitration
System and method.The technical scheme is that
A kind of oxidation-absorption high gravity desulfurization denitrating system, is made up of doser and supergravity reactor, described doser
Including medicament pond, the medicine liquid outlet in medicament pond connects dosing pump import, dosing pump outlet and the medicament inlet of supergravity reactor
It is connected；Described supergravity reactor includes that housing, enclosure interior are provided with annular packing rotor, and housing is provided with gas feed, gas
Body outlet, medicament inlet and agent outlet, described gas outlet is connected with air-introduced machine, the refluxing opening phase in agent outlet and medicament pond
Even.
On the pipeline that the medicine liquid outlet in described medicament pond is connected with dosing pump import, the agent outlet of supergravity reactor
On the pipeline being connected with medicament pond refluxing opening and dosing pump exports the pipe that is connected with the medicament inlet of supergravity reactor
It is equipped with liquid control valve on road, is used for regulating fluid flow and flow velocity.
The pipeline that the gas outlet of described supergravity reactor is connected with air-introduced machine is provided with gas control valve and temperature
Table, wherein gas control valve is for regulating the flow and flow velocity discharging gas, and the temperature of gas discharged by thermometer for monitoring.
Described annular packing rotor is connected with motor by rotating shaft.
Described supergravity reactor gas feed is positioned in housing sidewall, and its set-up mode in housing sidewall with
Making flue gas approach axis is to be as the criterion along the tangential line direction of annular packing rotor.
Described supergravity reactor medicament inlet lower end is provided with flow-stopping plate, and flow-stopping plate and horizontal angle are 30 ~ 45 °,
Purpose is to make medicament uniformly and sufficiently flow into inside the filler of filler rotor from medicament inlet, prevents medicament to be directly sprayed onto and turns
In rotating shaft within Zi and owing to gravity flows back in medicament pond along rotating shaft, reduce the service efficiency of medicament.
A kind of oxidation-absorption high gravity desulfurization method of denitration, is to use said system, and processing step includes:
(1) with Potassium Monopersulfate for oxidative absorption agent, medical solution pool is configured to the solution that mass concentration is 1 ~ 10 ‰；
(2) control the flow velocity of liquid control valve, potassium monopersulfate solutions is continually introduced supergravity reactor annular packing and turns
Inside the filler of son, and open air-introduced machine, the mixed flue gas of dedusting is introduced supergravity reactor, control annular packing rotor even
Speed rotates and mixed flue gas is carried out desulphurization denitration, and the potassium monopersulfate solutions by supergravity reactor bottom deposit is continuous simultaneously
Lead back to medicament pond；
(3) control the flow velocity of gas control valve, the flue gas after desulphurization denitration is emptied.
In said method, the rotating speed that described step (2) control annular packing rotor at the uniform velocity rotates is 400 ~ 1000r/min,
Filler uses magnesium oxide and the mixture of activated fibre.
In said method, potassium monopersulfate solutions can recycle in the entire system, and Potassium Monopersulfate is molten
Liquid is after medicament pond introduces supergravity reactor, and potassium monopersulfate solutions enters after deflection plate is by strong force field pulverizing, dispersion
Inside filler, react with flue gas, and be the most automatically scattered, then in agent outlet flows back into medicament pond.
The oxidation-absorption high gravity desulfurization denitrating system of the present invention and method, owing to Potassium peroxysulfate itself produces sulphuric acid
Root free radical S04 •- (E0=2.5V-3.1V), and free radical is with extremely strong standard electrode EMF, almost with hydroxyl radical free radical
(E0=2.7V-2.8V) there is the oxidability of equivalent, so strong oxidizer Potassium Monopersulfate can be by NO and SO2Respectively
It is oxidized to the NO of high-valence statex(NO2、N2O5、N2O3Deng nitrogen oxides) and SO3, the hypergravity that recycling is provided with active filler layer is anti-
Answer device to improve NO and SO2Oxidation, adsorb and absorb removal effect.Supergravity reactor is rotor by centrifugal principle
Internal flushing liquor is pulverized so that it is can NO effectively and in flue gasxAnd SO2Efficiently quickly mix, contact, react, remove；Turn
On the one hand the active filler layer (magnesium oxide and activated fibre) set in son plays absorption NO and SO2It is allowed to continue to be oxidized to high-valence state
NOxAnd SO3Effect, on the other hand play a part the most again to increase gas-to-liquid contact interface, make the NO in flue gasxAnd SO2Can fill
Oxidized dose of (Potassium Monopersulfate) oxidative absorption is divided to remove.
Beneficial effects of the present invention: the oxidation-absorption high gravity desulfurization denitrating system simple in construction of the present invention, can be at cigarette
Temperature improves desulphurization denitration less than desulphurization denitration under conditions of 160 DEG C, process simplification while reducing production cost
Efficiency, wherein desulfuration efficiency reaches more than 95%, and denitration efficiency reaches more than 80%.Additionally, and existing desulfuring and denitrifying apparatus phase
Ratio, the system processing power of the present invention reaches greatly to process flue gas 10000-100000m/h, and energy consumption is low, safety is high, body
(more existing system for desulfuration and denitration takes up an area to amass little, to be suitable for land used anxiety while reducing occupation area of equipment environment
Area reduces 7-10 times).
Accompanying drawing explanation
Fig. 1 is the overall structure schematic diagram of the oxidation-absorption high gravity desulfurization denitrating system of the present invention；
Wherein, 1-supergravity reactor housing；2-annular packing rotor；3-supergravity reactor gas feed；4-hypergravity is anti-
Ying Qi gas outlet；5-supergravity reactor medicament inlet pipe；6-supergravity reactor agent outlet pipe；7-air-introduced machine；8-medicine
Agent pond；9-dosing pump；10-medicament regulation valve；11-rotating shaft；12-medicament pond refluxing opening；13-medicament pond medicine liquid outlet；14-baffle
Plate；15-thermometer, 16-gas control valve, 17-motor.
Detailed description of the invention
The mixed flue gas that the embodiment of the present invention is used is from Shenyang smelter, Anshan smelter, Shenyang
Chemical enterprise.
Combine accompanying drawing below by way of specific embodiment the specific implementation process of the present invention is described, but embodiment is interior
Hold and be not limiting as protection scope of the present invention.
Embodiment 1
A kind of oxidation-absorption high gravity desulfurization denitrating system, its structure is as it is shown in figure 1, by doser and supergravity reactor
Composition, described doser includes medicament pond 8, and the medicine liquid outlet 13 in medicament pond connects dosing pump 9 import, dosing pump 9 outlet with
The medicament inlet medicament inlet of supergravity reactor is connected, and medicament inlet is provided with medicament inlet pipe 5；Described supergravity reactor
Including housing 1, enclosure interior is provided with annular packing rotor 2, housing 1 be provided with gas feed 3, gas outlet 4, medicament inlet and
Agent outlet, described gas outlet 4 is connected with air-introduced machine 7, and agent outlet is provided with agent outlet pipe 6, with the refluxing opening in medicament pond 8
12 are connected.
The size of described supergravity reactor is: diameter 0.9m, high 1.0m.
On the pipeline that the medicine liquid outlet 13 in described medicament pond 8 is connected with dosing pump 9 import, the medicament of supergravity reactor
On the pipeline that outlet 6 is connected with medicament pond refluxing opening 12 and dosing pump 9 outlet and the medicament inlet of supergravity reactor
Liquid control valve 10 it is equipped with on the pipeline that pipe 5 is connected.
The pipeline that the gas outlet 4 of described supergravity reactor is connected with air-introduced machine 7 be provided with gas control valve 16 and
Thermometer 15(TG002).
Described annular packing rotor 2 is connected with motor 17 by rotating shaft 11, rotor exterior ring diameter 0.8m, annular diameters
0.65m, filler uses magnesium oxide and the mixture of activated fibre.
Described supergravity reactor gas feed 3 is positioned on housing 1 sidewall, gas feed and the angle of housing horizontal center line
Degree is 90 °.
Described supergravity reactor medicament inlet lower end is provided with flow-stopping plate 14, a size of 60mm × 60mm, flow-stopping plate 14 with
Horizontal angle is 45 °.
Use said system, the mixed flue gas of Shenyang smelter is carried out oxidation-absorption high gravity desulfurization denitration side
Method, processing step includes:
(1) with Potassium Monopersulfate for oxidative absorption agent, medical solution pool is configured to the solution that mass concentration is 5 ‰；
(2) flow velocity controlling liquid control valve is 3m/s, potassium monopersulfate solutions is continually introduced supergravity reactor ring-type
In the filler of filler rotor, and open air-introduced machine, the mixed flue gas of dedusting is introduced supergravity reactor, control annular packing and turn
Son at the uniform velocity rotates and mixed flue gas is carried out desulphurization denitration, simultaneously by the potassium monopersulfate solutions of supergravity reactor bottom deposit
Constantly leading back to medicament pond, the rotating speed the most at the uniform velocity rotated is 800r/min；
(3) flow velocity controlling gas control valve is 10m/s, is emptied by the flue gas after desulphurization denitration.
The system of the present embodiment processes the ability of this enterprise's mixed flue gas and reaches 10000 m/h, and desulfuration efficiency is 97 ~
100%, denitration efficiency 80 ~ 90%, and energy consumption is low, safety is high, volume is little.
The size of the former desulfurizer of this enterprise is: desulfurizing tower: diameter d=3m, high h=15m；Denitrification apparatus: floor space 20
m³；Total floor space of these equipment is 10 times of the oxidation-absorption high gravity desulfurization denitrating system floor space of the present embodiment.
Embodiment 2
The oxidation-absorption high gravity desulfurization denitrating system of the present embodiment is with embodiment 1, and distinctive points is the chi of supergravity reactor
Very little being: diameter 1.8m, high 2.0m, the size of flow-stopping plate 14 is 100mm × 100mm, filler rotor exterior ring diameter=1.5 ~ 1.6m,
Annular diameters 1.3 ~ 1.4m.
Use said system, the mixed flue gas of Anshan smelter is carried out oxidation-absorption high gravity desulfurization denitration side
Method, processing step includes:
(1) with Potassium Monopersulfate for oxidative absorption agent, medical solution pool is configured to the solution that mass concentration is 6 ‰；
(2) flow velocity controlling liquid control valve is 4m/s, potassium monopersulfate solutions is continually introduced supergravity reactor ring-type
In the filler of filler rotor, and open air-introduced machine, the mixed flue gas of dedusting is introduced supergravity reactor, control annular packing and turn
Son at the uniform velocity rotates and mixed flue gas is carried out desulphurization denitration, simultaneously by the potassium monopersulfate solutions of supergravity reactor bottom deposit
Constantly leading back to medicament pond, the rotating speed the most at the uniform velocity rotated is 800r/min；
(3) flow velocity controlling gas control valve is 12m/s, is emptied by the flue gas after desulphurization denitration.
The system of the present embodiment processes the ability of this enterprise's mixed flue gas and reaches 60000 m/h, and desulfuration efficiency is 97 ~
100%, denitration efficiency 80 ~ 85%, and energy consumption is low, safety is high, volume is little.
Embodiment 3
The oxidation-absorption high gravity desulfurization denitrating system of the present embodiment is with embodiment 1, and distinctive points is the chi of supergravity reactor
Very little it is: diameter 2.4m, high 2.6m, the size of flow-stopping plate 14 is 120mm × 120mm, filler rotor exterior ring diameter=2.0m, internal ring
Diameter 1.75m.
Use said system, the mixed flue gas of Shenyang chemical enterprise is carried out oxidation-absorption high gravity desulfurization denitration side
Method, processing step includes:
(1) with Potassium Monopersulfate for oxidative absorption agent, medical solution pool is configured to the solution that mass concentration is 6 ‰；
(2) flow velocity controlling liquid control valve is 5m/s, potassium monopersulfate solutions is continually introduced supergravity reactor ring-type
In the filler of filler rotor, and open air-introduced machine, the mixed flue gas of dedusting is introduced supergravity reactor, control annular packing and turn
Son at the uniform velocity rotates and mixed flue gas is carried out desulphurization denitration, simultaneously by the potassium monopersulfate solutions of supergravity reactor bottom deposit
Constantly leading back to medicament pond, the rotating speed the most at the uniform velocity rotated is 800r/min；
(3) flow velocity controlling gas control valve is 15m/s, is emptied by the flue gas after desulphurization denitration.
The system of the present embodiment processes the ability of this enterprise's mixed flue gas and reaches 100000 m/h, and desulfuration efficiency is 95 ~
100%, denitration efficiency 80 ~ 85%, and energy consumption is low, safety is high, volume is little.
When the mixed flue gas amount processed is more than 100000m, if using single device to require higher to power of motor, go out
Consideration in terms of safety and energy consumption, the oxidation-absorption high gravity desulfurization denitrating system that can use the multiple stage present invention is used in parallel,
More preferable removal effect can be reached.
Claims (8)
1. an oxidation-absorption high gravity desulfurization denitrating system, it is characterised in that described system is anti-by doser and hypergravity
Answering device to form, described doser includes medicament pond, and the medicine liquid outlet in medicament pond connects dosing pump import, and dosing pump outlet is with super
The medicament inlet of gravity reactor is connected；Described supergravity reactor includes that housing, enclosure interior are provided with annular packing rotor, shell
Body is provided with gas feed, gas outlet, medicament inlet and agent outlet, and described gas outlet is connected with air-introduced machine, and medicament goes out
Mouth is connected with the refluxing opening in medicament pond.
A kind of oxidation-absorption high gravity desulfurization denitrating system the most according to claim 1, it is characterised in that described medicament pond
The pipeline that is connected with dosing pump import of medicine liquid outlet on, the agent outlet of supergravity reactor is connected with medicament pond refluxing opening
It is equipped with for regulating on the pipeline connect and on the dosing pump pipeline that is connected with the medicament inlet of supergravity reactor of outlet
Fluid flow and the liquid control valve of flow velocity.
A kind of oxidation-absorption high gravity desulfurization denitrating system the most according to claim 1, it is characterised in that described gas goes out
The pipeline that mouth is connected with air-introduced machine is provided with for regulating the flow and the gas control valve of flow velocity and thermometer discharging gas.
A kind of oxidation-absorption high gravity desulfurization denitrating system the most according to claim 1, it is characterised in that described gas enters
Mouth is positioned in housing sidewall, and its set-up mode in housing sidewall is so that flue gas approach axis is for turn along annular packing
The tangential line direction of son is as the criterion.
A kind of oxidation-absorption high gravity desulfurization denitrating system the most according to claim 1, it is characterised in that described ring-type fill out
Material rotor is connected with motor by rotating shaft.
6. according to the arbitrary described a kind of oxidation-absorption high gravity desulfurization denitrating system of claim 1 ~ 5, it is characterised in that described
Medicament inlet lower end is provided with flow-stopping plate, and flow-stopping plate and horizontal angle are 30 ~ 45 °.
7. an oxidation-absorption high gravity desulfurization method of denitration, is to use system described in claim 1, it is characterised in that technique
Step includes:
(1) with Potassium Monopersulfate for oxidative absorption agent, medical solution pool is configured to the solution that mass concentration is 1 ~ 10 ‰；
(2) control the flow velocity of liquid control valve, potassium monopersulfate solutions is continually introduced supergravity reactor annular packing and turns
Inside the filler of son, and open air-introduced machine, the mixed flue gas of dedusting is introduced supergravity reactor, control annular packing rotor even
Speed rotates and mixed flue gas is carried out desulphurization denitration, and the potassium monopersulfate solutions by supergravity reactor bottom deposit is continuous simultaneously
Lead back to medicament pond；
(3) control the flow velocity of gas control valve, the flue gas after desulphurization denitration is emptied.
A kind of oxidation-absorption high gravity desulfurization method of denitration the most according to claim 7, it is characterised in that described step
(2) controlling the rotating speed that at the uniform velocity rotates of annular packing rotor is 400 ~ 1000r/min, and filler uses the mixed of magnesium oxide and activated fibre
Compound.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107141251A (en) * | 2017-03-17 | 2017-09-08 | 江苏中邦制药有限公司 | A kind of method for directly synthesizing nanometer small particle ZPT |
| CN107638792A (en) * | 2017-09-26 | 2018-01-30 | 大连理工大学 | A kind of compound flue gas denitration oxidizing agent and application process |
| CN109847566A (en) * | 2019-04-22 | 2019-06-07 | 四川恒创博联科技有限责任公司 | The dust removal integrated laminar reactor of desulphurization denitration |
| CN110420551A (en) * | 2019-08-06 | 2019-11-08 | 浙江工业大学 | A kind of removing higher concentration NOXThe device and method of flue gas |
| CN111467946A (en) * | 2020-04-22 | 2020-07-31 | 运城学院 | NO in preparation process of molecular sieve catalystxMethod for treating exhaust gas |
| CN112915786A (en) * | 2021-01-22 | 2021-06-08 | 中国船舶重工集团公司第七一一研究所 | Tail gas desulfurization and denitrification system and tail gas desulfurization and denitrification treatment process |
| CN114259867A (en) * | 2021-12-09 | 2022-04-01 | 中北大学 | Device and method for simultaneously desulfurizing and denitrifying coal-fired flue gas |
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| CN114768509A (en) * | 2022-04-01 | 2022-07-22 | 中北大学 | Method and device for removing multi-component pollutants in flue gas based on supergravity technology |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100035751A1 (en) * | 2007-03-14 | 2010-02-11 | Semali Priyanthi Perera | Regenerable adsorption unit |
| CN101913845A (en) * | 2010-08-04 | 2010-12-15 | 姜辉 | Ceramic packing with high iron content for wet-method gas desulfurization |
| CN102974181A (en) * | 2012-11-14 | 2013-03-20 | 江苏中显集团有限公司 | Flue gas dedusting and desulfurization and denitrification craft and special device thereof |
| CN105126587A (en) * | 2015-09-01 | 2015-12-09 | 北京蓝天宇恒环保科技有限公司 | Method for removing sulfur dioxide in flue gas |
| CN105771600A (en) * | 2016-04-12 | 2016-07-20 | 刘杨先 | Method and device for integrally removing multiple pollutants in tail gas through plant ash seriflux |
| CN205965476U (en) * | 2016-08-17 | 2017-02-22 | 沈阳汇川环境工程有限公司 | Oxidation absorb hypergravity SOx/NOx control system |
-
2016
- 2016-08-17 CN CN201610675581.8A patent/CN106110860A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100035751A1 (en) * | 2007-03-14 | 2010-02-11 | Semali Priyanthi Perera | Regenerable adsorption unit |
| CN101913845A (en) * | 2010-08-04 | 2010-12-15 | 姜辉 | Ceramic packing with high iron content for wet-method gas desulfurization |
| CN102974181A (en) * | 2012-11-14 | 2013-03-20 | 江苏中显集团有限公司 | Flue gas dedusting and desulfurization and denitrification craft and special device thereof |
| CN105126587A (en) * | 2015-09-01 | 2015-12-09 | 北京蓝天宇恒环保科技有限公司 | Method for removing sulfur dioxide in flue gas |
| CN105771600A (en) * | 2016-04-12 | 2016-07-20 | 刘杨先 | Method and device for integrally removing multiple pollutants in tail gas through plant ash seriflux |
| CN205965476U (en) * | 2016-08-17 | 2017-02-22 | 沈阳汇川环境工程有限公司 | Oxidation absorb hypergravity SOx/NOx control system |
Non-Patent Citations (1)
| Title |
|---|
| 焦纬洲: "《超重力强化甲醇柴油乳化燃料制备技术》", 31 December 2013, 国防工业出版社 * |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107141251A (en) * | 2017-03-17 | 2017-09-08 | 江苏中邦制药有限公司 | A kind of method for directly synthesizing nanometer small particle ZPT |
| CN107638792A (en) * | 2017-09-26 | 2018-01-30 | 大连理工大学 | A kind of compound flue gas denitration oxidizing agent and application process |
| CN107638792B (en) * | 2017-09-26 | 2019-12-27 | 大连理工大学 | Composite flue gas denitration oxidant and application method thereof |
| CN109847566A (en) * | 2019-04-22 | 2019-06-07 | 四川恒创博联科技有限责任公司 | The dust removal integrated laminar reactor of desulphurization denitration |
| CN110420551A (en) * | 2019-08-06 | 2019-11-08 | 浙江工业大学 | A kind of removing higher concentration NOXThe device and method of flue gas |
| CN111467946A (en) * | 2020-04-22 | 2020-07-31 | 运城学院 | NO in preparation process of molecular sieve catalystxMethod for treating exhaust gas |
| CN114588761A (en) * | 2020-12-03 | 2022-06-07 | 中国石油天然气股份有限公司 | Device and method for absorbing sulfur trioxide in sulfonated tail gas |
| CN112915786A (en) * | 2021-01-22 | 2021-06-08 | 中国船舶重工集团公司第七一一研究所 | Tail gas desulfurization and denitrification system and tail gas desulfurization and denitrification treatment process |
| CN114259867A (en) * | 2021-12-09 | 2022-04-01 | 中北大学 | Device and method for simultaneously desulfurizing and denitrifying coal-fired flue gas |
| CN114768509A (en) * | 2022-04-01 | 2022-07-22 | 中北大学 | Method and device for removing multi-component pollutants in flue gas based on supergravity technology |
| CN114768509B (en) * | 2022-04-01 | 2023-12-01 | 中北大学 | Method and device for removing multi-component pollutants in flue gas based on supergravity technology |
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Application publication date: 20161116 |