CN205886557U - Redox is with journey SOx/NOx control device - Google Patents
Redox is with journey SOx/NOx control device Download PDFInfo
- Publication number
- CN205886557U CN205886557U CN201620847829.XU CN201620847829U CN205886557U CN 205886557 U CN205886557 U CN 205886557U CN 201620847829 U CN201620847829 U CN 201620847829U CN 205886557 U CN205886557 U CN 205886557U
- Authority
- CN
- China
- Prior art keywords
- circulation fluid
- area
- treatment region
- fluid treatment
- denitrifying
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a redox is with journey SOx/NOx control device, the absorption tower includes the waste gas import, the circulation fluid treatment region, the alkali lye district, synchronous SOx/NOx control district and exhaust outlet, be equipped with oxidation reactor and reduction reactor between waste gas import and the circulation fluid treatment region, waste gas access connection oxidation reactor, oxidation reactor connects reduction reactor, reduction reactor connects the circulation fluid treatment region, synchronous SOx/NOx control district sets up the top at the circulation fluid treatment region, the alkali lye district sets up the side on the absorption tower, synchronous SOx/NOx control district top is equipped with the defroster, the defroster top is equipped with exhaust outlet. Efficient, nitric oxide activated product electronation reaction is fast, has improved the efficiency of system greatly, nitric oxide activated product electronation reaction is thorough, has improved the effect of system greatly, taking up an area of and lacking, the cost is few, and the working costs is low, and application range is wide.
Description
Technical field
This utility model is related to a kind of desulfuring and denitrifying apparatus, more particularly, to a kind of oxidoreduction with journey desulfuring and denitrifying apparatus,
Belong to combustion products process field.
Background technology
Nitrogen oxides are the main causes causing chemical fumes, are also the major reason of acid rain.Sulfur dioxide is acid rain
Main cause.Desulfurization and denitration are two vital tasks of waste gas pollution control and treatment.
Desulfurizing method of exhaust gas mainly has dry type, half dry type and wet type desulfurizing.Dry type desulfurizing feeding lime stone, magnesium oxide etc. are done
Powder desulfurizing agent, directly with waste gas sulfur dioxide react and generate the dry products such as calcium sulfite, magnesium sulfite, then dedusting.Half
The desulfurizer slurries such as dry type desulfurizing feeding lime, magnesium oxide, sodium hydroxide, directly react generation Asia with the sulfur dioxide in waste gas
The dry products such as calcium sulfate, magnesium sulfite, then dedusting.Dry type, the advantage of half dry type desulfurization are not need water, there is not pulp water and divide
From with water recycle problem；Shortcoming is to react not thorough, and efficiency is low, is required for dedusting before and after desulfurization, and repeated construction is serious,
Pressure drop is big, and operating cost is high.Wet type desulfurizing sprays waste gas with doctor solution first, and the sulfur dioxide in waste gas is transferred to shape in water
Become sulfurous acid, then in the alkali liquor such as feeding lime, magnesium oxide, sodium hydroxide and acid doctor solution, desulfurization after slag-liquid separation
Liquid recycles.The advantage of wet type desulfurizing is that sulfur dioxide transfer velocity is fast, efficiency high, and effect is good；Shortcoming is to consume water, desulfurization
Liquid needs slag-liquid separation and recycles.Generally adopt wet type desulfurizing at present, seldom adopt dry type and half dry type desulfurization.
Main flow denitration technology mainly selective catalytic reduction method (scr) and SNCR method (sncr).Its
His technology mainly has electronic beam method (eba), activated coke absorption, normal temperature oxidation reducing process etc..Scr law technology is in catalyst action
Under, reducing agent nh3No in (liquefied ammonia, ammonia, carbamide etc.) and flue gasxReaction, by the no in flue gasxIt is reduced to nitrogen and water.Its
Reactor is arranged between boiler economizer outlet and air preheater entrance, and reaction temperature is typically between 320 DEG C -400 DEG C.
Sncr law technology nh3, the reducing agent such as carbamide spray into the region that in-furnace temperature is 850～1100 DEG C, in reducing agent and flue gas
noxCarry out selective reaction, noxIt is reduced to nitrogen and water.Scr and sncr technology be required for specific reaction temperature condition and
Strict automatically controls, and reducing agent is not enough, and reaction is not thorough, and instead excess generation the escaping of ammonia increases nitrogen oxides, results in process
Effect reduces.Electronic beam method utilizes the high energy particle that electron accelerator produces to irradiate flue gas so as to so2And noxOxidation generates sulphuric acid
And nitric acid, then react generation ammonium sulphate and nitric acid ammonia with the ammonia adding.This technology does not have waste water it is not necessary to catalyst, to flue gas
Condition changes strong adaptability, but power consumption is big, is not also suitable for large-scale application.Active coke absorption method carries out cigarette with activated coke
Desulfurization and denitrogenation while gas.so2Adsorbed by activated coke, by hot recycling, product is converted into the pairs such as sulfur, sulphuric acid, chemical fertilizer
Product.noxIt is under conditions of ammonification, the catalytic action through activated coke generates water and nitrogen enters air again.This technology does not have
Waste water, it is not necessary to catalyst, changes strong adaptability to flue gas condition, but operation is more complicated, and side-product produces complexity, and activated coke disappears
Consumption is big, and tower pressure drop is big.No is first oxidized to no by normal temperature oxidation reducing process2, then by no2Transfer to and in water, become hno3, finally profit
Use h2so3By hno3It is reduced into n2Discharge.This technical matters process similar with desulfurization it is not necessary to reducing agent, flue gas condition is changed
, moreover it is possible to the noxious substance such as simultaneous oxidation two English and remove removing heavy metals etc., operating cost is low for strong adaptability, difficult point be oxidation and
The control of reduction.
Because technique limits, the denitration such as scr, sncr, activated coke absorption synchronously can not possibly be carried out with desulfurization, and both can only make
For separate unit it is impossible to realize technique and the integration of device, floor space is big, and investment is many, and operating cost is high.Only several
Normal temperature oxidation reduction denitration example is also all independent denitration after desulfurization, there is a problem of same.Electronic beam method denitration needs
Produce high energy particle using electron accelerator, energy consumption is very big, is difficult to commercial production.
Content of the invention
The purpose of this utility model is to overcome weak point in prior art, and provides a kind of oxidoreduction with journey desulfurization
Denitrification apparatus.Oxidoreduction makes wet type desulfurizing and normal temperature oxidation reduction denitration same in a reaction tower with journey desulfuring and denitrifying apparatus
Step completes, and substantially increases dust-removal and desulfurizing effect and efficiency, reduces investment row 30-40, reduces operating cost 20-30%, reduces
Floor space 40-45%.
This oxidoreduction with journey desulfuring and denitrifying apparatus, absorption tower include circulation fluid treatment region, alkali liquor area, synchronized desulfuring take off
Nitre area and waste gas outlet, are provided with oxidation reactor and reduction reactor, exhaust gas inlet between exhaust gas inlet and circulation fluid treatment region
Connect oxidation reactor, oxidation reactor connects reduction reactor, reduction reactor connects circulation fluid treatment region, synchronized desulfuring takes off
Nitre area is arranged on the top of circulation fluid treatment region, and alkali liquor area is arranged on the side on absorption tower, and synchronized desulfuring and denitrifying is provided with above area
Demister, is provided with waste gas outlet above demister.
Described circulation fluid treatment region side is provided with dope elevator pump, and circulation fluid treatment region is upper with synchronized desulfuring and denitrifying area
Be provided with circulating pump between side, below alkali liquor area and synchronized desulfuring and denitrifying area between be provided with dosing pump.
It is additionally added strong acid in described reduction reactor.
This utility model advantage is:
1. strong acid microenvironment, sprays strong acid fog together with reducing agent, causes reducing agent to contact with nitric oxide bioactivity product
The ph value of moment is less than 1 microenvironment；
2., with journey desulphurization denitration, by the use of desulfurization product as reducing agent, in desulphurization denitration subsequent process, soda acid, slag liquid divides
From completing it is achieved that with journey desulphurization denitration in a set of facility with recycling etc. of water.
3. efficiency high, nitric oxide bioactivity product reduction reaction speed is fast, substantially increases the efficiency of system；
4. effect is good, and nitric oxide bioactivity product reduction reaction thoroughly, substantially increases the effect of system；
5. take up an area few, with journey desulphurization denitration, save floor space 40-45%；
6. cost is few, saves cost 30-40%；
7. operating cost is low, saves operating cost 20-30%；
8. range is wide, is not only applicable to grassroot project, is also applied for off-the-shelf item and proposes mark transformation, especially land used is nervous
Project with the obvious advantage.
Brief description
Fig. 1 is the structural representation with journey desulfuring and denitrifying apparatus for the oxidoreduction.
In figure labelling: 1- oxidation reactor, 2- reduction reactor, 3- circulating pump, 4- elevator pump, 5- dosing pump, 6- demisting
Device, 7- absorption tower, 8- exhaust gas inlet, 9- circulation fluid treatment region, 10- alkali liquor area, 11- synchronized desulfuring and denitrifying area, 12- waste gas go out
Mouthful.
Specific embodiment
Below in conjunction with the accompanying drawings oxidoreduction is further described with journey desulfuring and denitrifying apparatus.
With journey desulfuring and denitrifying apparatus, absorption tower 7 includes circulation fluid treatment region 9, alkali liquor area 10, synchronously takes off this oxidoreduction
Sulfur denitration region 11 and waste gas outlet 12, are provided with oxidation reactor 1 and reduction reaction between exhaust gas inlet 8 and circulation fluid treatment region 9
Device 2, exhaust gas inlet 8 connects oxidation reactor 1, and oxidation reactor 1 connects reduction reactor 2, and reduction reactor 2 connects circulation fluid
Treatment region 9, synchronized desulfuring and denitrifying area 11 is arranged on the top of circulation fluid treatment region 9, and alkali liquor area 10 is arranged on the side on absorption tower 7
Face, is provided with demister 6, is provided with waste gas outlet 12 above demister 6 above synchronized desulfuring and denitrifying area 11.
Described circulation fluid treatment region 9 side is provided with dope elevator pump 4, circulation fluid treatment region 9 and synchronized desulfuring and denitrifying area
It is provided with circulating pump 3 between 11 top, between alkali liquor area 10 and synchronized desulfuring and denitrifying area 11 lower section, be provided with dosing pump 5.
It is additionally added strong acid in described reduction reactor 2.
Waste gas first passes through exhaust gas inlet 8 and enters oxidation reactor 1, and inertia nitric oxide is oxidized to activated product；So
Enter reduction reactor 2 afterwards, nitric oxide bioactivity product is reduced into nitrogen, and waste gas subsequently enters absorption tower 7；Dosing pump 5 will
The alkali liquor in alkali liquor area 10 uniformly sprays the bottom in the synchronized desulfuring and denitrifying area 11 on absorption tower 7, carries out acid-base neutralization；Circulating pump 3
Circulation fluid is uniformly sprayed to the top in the synchronized desulfuring and denitrifying area 11 on absorption tower 7；Synchronized desulfuring and denitrifying area on absorption tower 7
11, waste gas rises, and circulation fluid declines, and gas-liquid is fully contacted, and soluble gas transfer to circulation fluid；Waste gas is same through absorption tower 7
Continue to rise behind step desulphurization denitration area 11, by demister 6, water smoke is removed, purify waste gas discharge；Circulation fluid falls into circulation fluid
In treatment region 9, circulation fluid treatment region 9 supernatant continues cycling through use, and the dope of circulation fluid treatment region 9 is sent by dope elevator pump 4
Toward processed facility.
This oxidoreduction, with journey desulfuring and denitrifying apparatus, wet type desulfurizing technology and normal temperature oxidation reduction denitration technology phase is tied
Close, define oxidoreduction with journey desulphurization denitration new technology device, desulphurization denitration synchronously carries out in one apparatus, greatly improves
Desulfurization off sulfide effect and efficiency, greatly reduce investment, operating cost and floor space.
Oxidoreduction is extremely complex with journey desulphurization denitration chemical reaction process, mainly the following chemical reaction of generation:
so2+h2o→so3 2-+2h+(1)
(m+n+k) no (gas)+(m+n+k) [o] → mno2+nno2 -+kno-(2)
mno2+nno2 -+kno-+(m+n+k)so3 2-+2(m+n)h+→(m+n+k)n2↑+(m+n+k)so4 2-+(m+n)h2o (3)
4no2+2h2o+2[o]→4no3 -+4h+(4)
2so3 2-+3no3 -→2so4 2-+n2↑+no (liquid) (5)
No (liquid)+[o] → no2(liquid) (6)
4no2(liquid)+2h2o+2[o]→4no3 -+4h+(7)
h++oh-→h2o (8)
Reaction (1) and (4) completes in gas transfer, needs shower water.Reaction (5), (6), (7), (8) are complete in the liquid phase
Become.Reaction (5) produces no (liquid), completes to react (6) and (7) using surplus [o], reaction (5), (6), (7) are repeated, reaction
Relatively slow in fact it could happen that no3 -Accumulation.Reaction (2) and (3) completes in the gas phase, and the response speed of reaction (2) quickly, reacts (3)
Response speed ph value be less than 1 under conditions of quickly, very slow under conditions of more than 2.Reaction (3) will react the product of (2)
Direct-reduction nitrogen, for denitration effect and avoid no3 -Accumulation is all extremely important.The reaction condition how building reaction (3) is
Normal temperature oxidation reduces the key problem in technology of denitration, is also the key problem in technology of the present invention.
Claims (3)
1. a kind of oxidoreduction is with journey desulfuring and denitrifying apparatus, absorption tower (7) include circulation fluid treatment region (9), alkali liquor area (10), with
Step desulphurization denitration area (11) and waste gas outlet (12) it is characterised in that: set between exhaust gas inlet (8) and circulation fluid treatment region (9)
There are oxidation reactor (1) and reduction reactor (2), exhaust gas inlet (8) connects oxidation reactor (1), oxidation reactor (1) connects
Reduction reactor (2), reduction reactor (2) connects circulation fluid treatment region (9), and synchronized desulfuring and denitrifying area (11) are arranged on circulation fluid
The top for the treatment of region (9), alkali liquor area (10) are arranged on the side of absorption tower (7), be provided with and remove above synchronized desulfuring and denitrifying area (11)
Day with fog (6), is provided with waste gas outlet (12) above demister (6).
2. oxidoreduction according to claim 1 with journey desulfuring and denitrifying apparatus it is characterised in that: described circulation fluid is processed
Area (9) side is provided with dope elevator pump (4), is provided between the top of circulation fluid treatment region (9) and synchronized desulfuring and denitrifying area (11)
Circulating pump (3), below alkali liquor area (10) and synchronized desulfuring and denitrifying area (11) between be provided with dosing pump (5).
3. oxidoreduction according to claim 1 with journey desulfuring and denitrifying apparatus it is characterised in that: described reduction reactor
(2) it is additionally added strong acid in.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620847829.XU CN205886557U (en) | 2016-08-08 | 2016-08-08 | Redox is with journey SOx/NOx control device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620847829.XU CN205886557U (en) | 2016-08-08 | 2016-08-08 | Redox is with journey SOx/NOx control device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205886557U true CN205886557U (en) | 2017-01-18 |
Family
ID=57783772
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620847829.XU Expired - Fee Related CN205886557U (en) | 2016-08-08 | 2016-08-08 | Redox is with journey SOx/NOx control device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205886557U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106064017A (en) * | 2016-08-08 | 2016-11-02 | 辽宁信威环保科技有限公司 | Oxidoreduction is with journey desulfuring and denitrifying apparatus |
-
2016
- 2016-08-08 CN CN201620847829.XU patent/CN205886557U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106064017A (en) * | 2016-08-08 | 2016-11-02 | 辽宁信威环保科技有限公司 | Oxidoreduction is with journey desulfuring and denitrifying apparatus |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103301749B (en) | The method of flue gas and desulfurizing and denitrifying | |
| CN102179146B (en) | Smoke desulfuration and denitration system absorbed by dielectric barrier discharge combined lye and process thereof | |
| CN102188897B (en) | Wet flue gas desulfurization and denitrification combined method | |
| WO2017096692A1 (en) | Fuel gas denitration and desulfurization washing system and denitration and desulfurization method | |
| CN104941410B (en) | Flue gas desulfurization and denitrification integrated method and device based on two-step oxidation process of active molecules O3 at low temperature | |
| CN101385943A (en) | Deprivation technique based on semi-dry process | |
| CN106731783B (en) | Integrated flue gas desulfurization and denitrification agent and use method thereof | |
| CN106237851A (en) | A kind of utilize ozone to carry out SCR denitration to carry the System and method for of effect | |
| CN105194991B (en) | Glass kiln flue gas desulfurization and denitrification system and technique | |
| CN110479057A (en) | A kind of method of chemical oxidation absorbing treating smoke pollutant | |
| CN102527224A (en) | Method and device for removing sulfur dioxide and nitrogen oxides from flue gas/ waste gas | |
| CN104524935A (en) | Single-tower type double-circulation sprinkling composite absorption device and method | |
| CN104324575A (en) | Spray absorption type system for simultaneous desulphurization and denitration of sintering flue gas | |
| CN103170228A (en) | Mixed solution for flue gas denitrification and application method of mixed solution | |
| CN112403154A (en) | Flue gas multi-pollutant cooperative purification process and device | |
| CN103100294A (en) | Method for removing oxynitride from flue gas through ozone oxidation method | |
| CN102188889B (en) | Device and method for combined removal of sulphur dioxide (SO2), nitrogen oxide (NOX) and mercury from fume | |
| CN113856441B (en) | Ammonia desulfurization method and ammonia desulfurization apparatus | |
| CN107737520A (en) | The method that coordinated desulfurization denitration is carried out to Flue Gas of Nonferrous Smelting using sodium alkali is circulated | |
| CN204247052U (en) | Single tower type double-cycle spray composite absorption device | |
| CN205886557U (en) | Redox is with journey SOx/NOx control device | |
| CN103933835B (en) | Soda acid waste gas electron beam irradiation intelligent processing system | |
| CN105268294A (en) | Double-tower double-circulation wet oxidation and catalysis combined removal system and method | |
| CN203061046U (en) | Coal-fired flue gas desulfurization and denitrification cooperative control device | |
| CN102423621A (en) | Double-alkali synchronous flue gas desulfurization and denitration process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Liaoning Fenghua Industrial Co., Ltd. Assignor: Liaoning Xinwei Environmental Protection Technology Co. Ltd. Contract record no.: 2017210000033 Denomination of utility model: Redox same-course desulfurization and denitrification apparatus Granted publication date: 20170118 License type: Common License Record date: 20171108 Assignee: Dashiqiao Xinwei Refractory Material Co.,Ltd. Assignor: Liaoning Xinwei Environmental Protection Technology Co. Ltd. Contract record no.: 2017210000032 Denomination of utility model: Redox same-course desulfurization and denitrification apparatus Granted publication date: 20170118 License type: Common License Record date: 20171108 |
|
| EE01 | Entry into force of recordation of patent licensing contract | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20170118 Termination date: 20200808 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |