CN107983119A - The dry desulfurization method of denitration of oxidation is forced based on ozone - Google Patents

The dry desulfurization method of denitration of oxidation is forced based on ozone Download PDF

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Publication number
CN107983119A
CN107983119A CN201711263347.5A CN201711263347A CN107983119A CN 107983119 A CN107983119 A CN 107983119A CN 201711263347 A CN201711263347 A CN 201711263347A CN 107983119 A CN107983119 A CN 107983119A
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China
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flue gas
oxidation
fluidized bed
absorption tower
ozone
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童裳慧
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Microtek Environmental Polytron Technologies Inc
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Microtek Environmental Polytron Technologies Inc
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Priority to CN201711263347.5A priority Critical patent/CN107983119A/en
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/60Simultaneously removing sulfur oxides and nitrogen oxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75Multi-step processes
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/10Oxidants
    • B01D2251/104Ozone
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/40Alkaline earth metal or magnesium compounds
    • B01D2251/402Alkaline earth metal or magnesium compounds of magnesium
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/60Inorganic bases or salts
    • B01D2251/602Oxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2258/00Sources of waste gases
    • B01D2258/02Other waste gases
    • B01D2258/0283Flue gases

Abstract

The invention discloses a kind of dry desulfurization method of denitration that oxidation is forced based on ozone, including:(1) former flue gas is subjected to pre- dust removal process, obtains the flue gas after dedusting;The dustiness in flue gas after the dedusting is 10~30mg/Nm3;(2) flue gas after the dedusting is contacted to carry out pressure oxidation with gas ozoniferous, so as to form oxidation flue gas;(3) absorbent magnesia dry powder is uniformly mixed with the oxidation flue gas in flue, subsequently into recirculating fluidized bed absorption tower, water is sprayed into the recirculating fluidized bed absorption tower, fully forms desulphurization denitration flue gas after reaction;(4) the desulphurization denitration flue gas is subjected to dust removal process, is purified flue gas, accessory substance and the absorbent not reacted completely;(5) absorbent not reacted completely is recycled to the recirculating fluidized bed absorption tower.The method of the present invention can synchronize desulphurization denitration using magnesia dry powder to flue gas.

Description

The dry desulfurization method of denitration of oxidation is forced based on ozone
Technical field
The present invention relates to a kind of flue gas dry desulfurizing method of denitration, more particularly to a kind of dry method that oxidation is forced based on ozone Desulfurization denitration method.
Background technology
Air environmental pollution control problem has caused global great attention.Joint flue gas desulfurization and denitrification technology is Receive significant attention.Traditional joint flue gas desulfurization and denitration technique is to install a set of denitrification apparatus additional behind desulfurizer.It is this Classification administration way not only takes up a large area, but also investment and operating cost are high, and difficulty is brought to large scale application.
On the one hand, input makes extensively in China's every profession and trade stove for large-scale flue gas wet method, semidry method, dry desulfurization device With, but the technique is without denitration ability at the same time.If carrying out denitration process again, take up an area more, and invest and operating cost is high It is high.For flue gas desulfurization technique, at present mainly using calcium base particle as desulfurizing agent, the desulfurization by-product after its gas cleaning Thing component is mainly calcium sulfite.Calcium sulfite is difficult to be recycled, and becomes current dry flue gas desulphurization engineering application In biggest obstacle.For gas denitrifying technology, mainly low NOx NO is used at presentxBurner.Above-mentioned burning skill Art can not meet the environmental requirement of clean flue gas well, and be influenced by factors such as coal characteristic, service conditions.At present The denitrating technique of application includes selective catalytic reduction (SCR methods) and selective non-catalytic reduction method (SNCR methods).SCR methods take off Nitre efficiency is higher, and discharge standard can reach 90%, but complex process, system investments expense and follow-up operation processing cost are high; SNCR method small investments, follow-up operation processing cost is relatively low, but denitration efficiency can only achieve 60%.
On the other hand, current magnesium method flue gas desulphurization denitrating technique is mostly wet processing, difficult to deal with there are sewage Problem.The Chinese patent application of Application No. 200610017524.7 discloses a kind of Circled dry phase flow tower flue gas desulphurizaion Technique:(1) it is sent into first by what industrial production produced containing form waste gas of sulfur dioxide in primary dust removing device, 90% flies in removing flue gas Ash particle thing;(2) flue gas for removing fly ash particulate is sent into circulation dry-phase flow tower and at smoke inlet by pipeline Equally distributed desulfurization absorbent slurries magnesia comes into full contact with, and makes absorbent slurry and the dioxy in flue gas by the power of flue gas Change sulphur to be mixed into tower, multigroup blender is set in tower, mixture is thoroughly mixed reaction, generate magnesium sulfite and sulphur Sour magnesium, reaches desulfurization purpose;(3) flue gas reacted is sent to secondary ash collector by circulation dry-phase flow tower gas-solid separator, The qualified discharge after dedusting again, while reactant is not by accessory substance and complete under the action of bottom of towe particle sorter in tower The desulfurization absorbent particulate matter of full response sorts away, and the desulfurization absorbent particulate matter not reacted completely that can be recycled is led to Cross circulation dry-phase flow tower bottom of towe chain conveyor and send recycle unit, repeated recycling utilize back to.The technique is only used for flue gas desulfurization, It is not used to denitrating flue gas.In addition, the technique mixes magnesia with flue gas in smoke inlet in form of slurry, subsequently into Desulfurizing tower, causes the two not react fully so that desulfuration efficiency is only capable of reaching 90%.
The Chinese patent application of Application No. 201710515142.5 discloses a kind of loaded modified magnesia of monoethanolamine Base flue gas dry desulfurizing adsorbent and preparation method, using magnesia as raw material, magnesium oxide-based adsorbent is prepared using coprecipitation, Roasting initial stage, by pyrolysis, the volatile impurities such as chemical bonding water and carbon therein can be removed, change into absorption and lived The magnesia of property, by the recrystallization of catabolite, also obtains having the magnesium oxide-based of specific crystal formation, grain size and pore structure Adsorbent, increases the specific surface area of magnesium oxide-based adsorbent, and at relatively high temperatures, solid phase reaction, shape also occur for magnesia Into active combined form, the performance of desulfurization also improves therewith, and monoethanolamine finally is carried on adsorbent with infusion process again Surface, for chemisorbed desulfurization, obtained desulfuration adsorbent intensity is high, carries out flue gas dry desulfurizing.This method is needed to oxygen Change magnesium and carry out specially treated, cause desulfurizing agent cost to improve, and can be only used for flue gas desulfurization.
To sum up, at present still without a kind of report that flue gas desulfurization and denitrification is directly carried out using magnesia dry method.
The content of the invention
It is an object of the invention to provide a kind of flue gas dry desulfurizing denitration, it directly uses magnesia dry method, and realizes Flue gas desulfurization and denitrification synchronously carries out.Further, the denitrification efficiency of method of the invention is high, easy to operate, operating cost It is low.
The present invention provides a kind of dry desulfurization method of denitration that oxidation is forced based on ozone, includes the following steps:
(1) former flue gas is subjected to pre- dust removal process, obtains the flue gas after dedusting;The dustiness in flue gas after the dedusting For 10~30mg/Nm3
(2) flue gas after the dedusting is contacted to carry out pressure oxidation with gas ozoniferous, so as to form oxidation cigarette Gas;
(3) absorbent magnesia dry powder is uniformly mixed with the oxidation flue gas in flue, subsequently into circulation Fluid bed absorption tower, the recirculating fluidized bed absorption tower is sprayed into by water, fully forms desulphurization denitration flue gas after reaction;Wherein, it is described Flue is arranged on the outside on the recirculating fluidized bed absorption tower;
(4) the desulphurization denitration flue gas is subjected to dust removal process, is purified flue gas, accessory substance and the suction do not reacted completely Receive agent;
(5) absorbent not reacted completely is recycled to the recirculating fluidized bed absorption tower.
Method in accordance with the invention it is preferred that in step (1), the oxygen content of former flue gas is 10~20vol%.
Method in accordance with the invention it is preferred that in step (1), the temperature of former flue gas is 80~150 DEG C, flow velocity for 2~ 5m/s。
Method in accordance with the invention it is preferred that in step (1), the flow velocity of former flue gas is 2~3.5m/s.
Method in accordance with the invention it is preferred that in step (1), the sulfur dioxide concentration of former flue gas is 1000~3000mg/ Nm3, nitrous oxides concentration is 200~500mg/Nm3
Method in accordance with the invention it is preferred that in step (2), pressure oxidation carries out in ozone oxidation device, should The entrance of ozone oxidation device is provided with spiral board and ozone inlet.
Method in accordance with the invention it is preferred that in step (3), the absorbent is with the oxidation flue gas in the circulation Time of contact in fluid bed absorption tower is more than 30min.
Method in accordance with the invention it is preferred that in step (3), water is sprayed into the recirculating fluidized bed absorption tower, with So that the moisture of magnesia dry powder is 0.1~3.5wt%.
Method in accordance with the invention it is preferred that in step (4), the dust removal process carries out in bag filter.
Method in accordance with the invention it is preferred that in step (5), by the absorbent not reacted completely from the circulation The recirculating fluidized bed absorption tower is sent into the bottom on fluid bed absorption tower.
The method of the present invention forces oxidation using ozone, improves the oxygenation efficiency of lower nitrogen oxides (such as NO), makes its oxygen The higher nitrogen oxides for being more readily absorbed removal are turned to, so that magnesia dry powder denitration is possibly realized.The side of the present invention Method is directly come into full contact with using magnesia dry powder with flue gas, can more efficiently remove sulfur dioxide and nitrogen oxidation in flue gas Thing.Preferable technical solution according to the present invention, desulfuration efficiency more than 93%, denitration efficiency is more than 85%, such as 89% with On.
Embodiment
With reference to specific embodiment, the present invention is further illustrated, but protection scope of the present invention is not limited to This.
The dry desulfurization method of denitration of the present invention is flue gas processing method, it can carry out the comprehensive regulation to flue gas at the same time, So as to remove the sulfur dioxide and nitrogen oxides in flue gas at the same time.The method of the present invention includes pre- dust removal step, force oxidation step Suddenly, desulphurization denitration step, dust removal step and circulation step etc..Introduce in detail below.
<Pre- dust removal step>
The pre- dust removal step of the present invention is that former flue gas is carried out pre- dust removal process, obtains the flue gas after dedusting;The dedusting The dustiness in flue gas afterwards is 10~30mg/Nm3.Pre- dust removal process can use cloth-sack-type dust removal, spiral-flow type dedusting or The method of electric precipitation, and preferably electric precipitation.By pre- dust removal step, particle larger and small in flue gas can be removed.Remove Dustiness is 10~30mg/Nm in flue gas after dirt3, it is preferably 10~20mg/Nm3, more preferably 10~15mg/Nm3.When except When the dustiness in flue gas after dirt is above range, ozone can be made more fully to be reacted with the NO in flue gas, so that shape Into NO2、N2O5Etc. high-valence state nitrogen oxides.
In the present invention, the oxygen content in former flue gas is 10~20vol%, is preferably 12~18vol%.When in flue gas When oxygen content is above range, ozone can be made more fully to react to form NO with the NO in flue gas2、N2O5Etc. high-valence state Nitrogen oxides;The magnesium sulfite that can be formed in subsequent step at the same time is more fully converted into magnesium sulfate.The present invention's The step of method can also include adjusting the oxygen content of flue gas.Specifically, when oxygen content is insufficient in flue gas, can use Oxidation fan adds oxygen-enriched air or oxygen into flue gas, to make oxygen content in flue gas reach above range.The oxygen of flue gas Content control is suitable within the scope of the invention, and oxygen content is too low in flue gas, it is impossible to ensures desulfurization off sulfide effect;Oxygen Too high levels, then increase energy consumption and cost.
In the present invention, the temperature of the former flue gas before pre- dust removal process can be 80~150 DEG C, be preferably 130~150 ℃.The flow velocity of former flue gas is 2~5m/s, is preferably 2~4m/s, more preferably 2~3.5m/s.By flue-gas temperature and flow control In above range, it is more conducive to ozone and forces NO to be oxidized to NO2、N2O5Etc. high-valence state nitrogen oxides, so as to improve denitration effect Rate.
In the present invention, the sulfur dioxide SO of former flue gas2Concentration is 1000~3000mg/Nm3, more preferably 1500~ 2500mg/Nm3.The nitrogen oxides NO of former flue gasxConcentration is 200~500mg/Nm3, more preferably 300~470mg/Nm3.By cigarette The sulfur dioxide and nitrous oxides concentration of gas are controlled in above range, are more conducive to ozone and are forced NO to be oxidized to NO2、N2O5 Etc. high-valence state nitrogen oxides, and be conducive to magnesia and sulfur dioxide and high-valence state reaction of nitrogen oxides, taken off so as to improve desulfurization Nitre efficiency.
<Force oxidation step>
The pressure oxidation step of the present invention is to contact the flue gas after the dedusting to be forced with gas ozoniferous Oxidation, so as to form oxidation flue gas.The present invention, as oxidant, can be sent out rapidly using ozone with the lower nitrogen oxides in flue gas Biochemical reaction, reaction speed is fast, efficient.NO in flue gas is oxidized to NO by ozone2、N2O5Etc. high-valence state nitrogen oxides, just In the absorption of magnesia dry powder.Oxidation step is forced to be carried out in ozone oxidation device.Ozone oxidation device can be arranged on cigarette Gas enter recirculating fluidized bed absorption tower before pipeline on, can so increase the time of contact of ozone and flue gas, so as to promote Ozone reacts the Quick Oxidation of lower nitrogen oxides.For example, ozone oxidation device is absorbed in pre-dedusting device and recirculating fluidized bed On pipeline between tower.
According to embodiment of the present invention, pressure oxidation carries out in ozone oxidation device, the ozone oxidation The entrance of device is provided with spiral board and ozone inlet.Ozone oxidation device can be horizontally-mounted reactor, its entrance is installed There are spiral board and ozone inlet.Spiral board can promote ozone to be uniformly mixed with flue gas, and then improve and force oxidation effectiveness.System Oxygen machine and ozone generator are arranged on the outside of the ozone oxidation device.The oxygen that oxygenerator produces is changed into through ozone generator effect Gas ozoniferous, then discharges through ozone inlet and enters with flue gas inside ozone oxidation device.In gas ozoniferous Ozone concentration is 2~15wt%, is preferably 5~12wt%, more preferably 7~10wt%.Ozone concentration energy using the present invention Enough take into account oxidation effectiveness and save ozone.Ozone inlet can use high pressure atomizing nozzle.The pressure of high pressure atomizing nozzle is 0.7~1.0MPa, is preferably 0.8~0.9MPa.
<Desulphurization denitration step>
The desulphurization denitration step of the present invention is to mix absorbent magnesia dry powder and the oxidation flue gas in flue Close uniformly, subsequently into recirculating fluidized bed absorption tower, water is sprayed into the recirculating fluidized bed absorption tower, fully form desulfurization after reaction Denitration flue gas.In the absorption tower, the presence of water on the one hand can promote magnesia dry powder absorb the sulfur dioxide in flue gas and Nitrogen oxides, is also easy to cause the reunion of magnesia dry powder, so that magnesia dry powder can not be mixed with flue gas but then Uniformly.In the present invention, the flue is arranged on the outside on the recirculating fluidized bed absorption tower.So flue gas and magnesia Dry method can be uniformly mixed before absorption tower is entered, thus can be to avoid the two nothing caused by the interference of moisture in absorption tower Method is uniformly mixed.Such setting can significantly improve flue gas desulfurization and denitrification effect.
In the present invention, time of contact of the absorbent with the oxidation flue gas in the recirculating fluidized bed absorption tower 30min, such as 30~60min can be more than.Magnesia dry powder repeatedly circulates in absorption tower, makes its time of contact with flue gas Increase is general up to more than 30min.Sulfur dioxide and high-valence state nitrogen oxides are reacted with solid absorbent, generate sulfurous acid Magnesium and magnesium nitrate, magnesium sulfite is further oxidized to magnesium sulfate by the oxygen in flue gas at the same time, so as to reach the effect of desulphurization denitration Fruit.Oxygen of the oxygen part in former flue gas in flue gas, a part are formed from ozone oxidation lower valency nitrogen oxides Oxygen.
In the present invention, water is sprayed into the recirculating fluidized bed absorption tower, so that the moisture of magnesia dry powder contains Measure as 0.1~3.5wt%, preferably 1~3wt%.As it was previously stated, suitable moisture is favourable to flue gas desulfurization and denitrification, but It is that excessive moisture then causes magnesia dry powder to be reunited, thus flue gas desulfurization and denitrification effect.
<Dust removal step and circulation step>
The dust removal step of the present invention is that the desulphurization denitration flue gas is carried out dust removal process, is purified flue gas, accessory substance The absorbent not reacted completely.Circulation step is that the absorbent not reacted completely is recycled to the recirculating fluidized bed to absorb Tower.According to embodiment of the present invention, the dust removal process carries out in bag filter.Under gravity, will Magnesium sulfate, the magnesium nitrate of flue gas desulfurization and denitrification formation are separated with the complete absorbent of unreacted.Magnesium sulfate and magnesium nitrate are as secondary Product enters accessory substance storehouse;The complete absorbent of unreacted is reentered in absorption tower and reused;Purifying smoke is arranged through chimney Put.According to embodiment of the present invention, by the absorbent not reacted completely from the recirculating fluidized bed absorption tower The recirculating fluidized bed absorption tower is sent into bottom.
Embodiment 1
(1) former flue gas (oxygen content 15vol%, flow velocity 3.5m/s) is removed into particulate matter using electric precipitation, obtained It is 15mg/Nm to dustiness3Dedusting after flue gas.Former flue gas (inlet flue gas) parameter is as shown in table 1.
(2) flue gas after the dedusting is contacted to carry out pressure oxidation with ozone in ozone oxidation device, so as to be formed Aoxidize flue gas.The entrance of the ozone oxidation device is provided with spiral board and ozone inlet.Spiral board can effectively facilitate ozone with Flue gas is uniformly mixed.Lower valency nitrogen oxides (such as NO) oxidation in flue gas is formed high-valence state nitrogen oxides (such as NO by ozone2With N2O5)。
(3) magnesia dry powder is mixed with oxidation flue gas in the flue being arranged on outside recirculating fluidized bed absorption tower Uniformly, subsequently into recirculating fluidized bed absorption tower.Water is sprayed into by the recirculating fluidized bed absorption tower using sprayer, so that oxidation The moisture of magnesium dry powder is 3wt%.Magnesia dry powder and oxidation flue gas come into full contact with 30min, and react, and form desulfurization Denitration flue gas.
(4) desulphurization denitration flue gas is subjected to dust removal process using bag filter, is purified flue gas, accessory substance and not complete The absorbent of full response.Accessory substance is mainly magnesium sulfate and magnesium nitrate.The parameter of purifying smoke is as shown in table 2.
(5) absorbent not reacted completely is sent into recirculating fluidized bed absorption tower from the bottom on recirculating fluidized bed absorption tower, Recycling.
Table 1, inlet flue gas parameter
Sequence number Parameter Unit Numerical value
1 Inlet flue gas amount (operating mode) m3/h 180000
2 Inlet flue gas amount (mark condition) Nm3/h 120441
3 Inlet flue gas temperature 135
4 Sulfur dioxide entrance concentration mg/Nm3 2500
5 Nitrogen oxides entrance concentration mg/Nm3 450
Table 2, exiting flue gas parameter
Sequence number Project Quantity Unit
1 Exiting flue gas amount (operating mode) 99543 m3/h
2 Exhaust gas temperature 65
3 Sulfur dioxide emissioning concentration 45 mg/Nm3
4 Desulfuration efficiency 98.20 %
5 Discharged nitrous oxides concentration 47 mg/Nm3
6 Denitration efficiency 89.56 %
7 The quantum of output of accessory substance 5.37 t/h
Embodiment 2
In addition to using the former flue gas shown in the former flue gas substitution table 1 shown in table 3, remaining condition is same as Example 1, Gained purifying smoke parameter is referring to table 4.
Table 3, inlet flue gas parameter
Sequence number Parameter Unit Numerical value
1 Inlet flue gas amount (operating mode) m3/h 105000
2 Inlet flue gas amount (mark condition) Nm3/h 67766
3 Inlet flue gas temperature 150
4 Sulfur dioxide entrance concentration mg/Nm3 2200
5 Nitrogen oxides entrance concentration mg/Nm3 470
Table 4, exiting flue gas parameter
Sequence number Project Quantity Unit
1 Exiting flue gas amount (operating mode) 899543 m3/h
2 Exhaust gas temperature 65
3 Sulfur dioxide emissioning concentration 45 mg/Nm3
4 Desulfuration efficiency 97.95 %
5 Discharged nitrous oxides concentration 37 mg/Nm3
6 Denitration efficiency 92.13 %
7 The quantum of output of accessory substance 5.37 t/h
Embodiment 3
In addition to using the former flue gas shown in the former flue gas substitution table 1 shown in table 5, remaining condition is same as Example 1, Gained purifying smoke parameter is referring to table 6.
Table 5, inlet flue gas parameter
Sequence number Parameter Unit Numerical value
1 Inlet flue gas amount (operating mode) m3/h 180000
2 Inlet flue gas amount (mark condition) Nm3/h 120441
3 Inlet flue gas temperature 135
4 Sulfur dioxide entrance concentration mg/Nm3 2000
5 Nitrogen oxides entrance concentration mg/Nm3 400
Table 6, exiting flue gas parameter
Sequence number Project Quantity Unit
1 Desulfurizing tower exiting flue gas amount (operating mode) 99543 m3/h
2 Exhaust gas temperature 75
3 Sulfur dioxide emissioning concentration 35 mg/Nm3
4 Desulfuration efficiency 98.25 %
5 Discharged nitrous oxides concentration 27 mg/Nm3
6 Denitration efficiency 93.25 %
7 The quantum of output of accessory substance 5.36 t/h
Present invention is not limited to the embodiments described above, in the case of without departing substantially from the substantive content of the present invention, this area skill Any deformation, improvement, the replacement that art personnel are contemplated that each fall within the scope of the present invention.

Claims (10)

1. a kind of dry desulfurization method of denitration that oxidation is forced based on ozone, it is characterised in that include the following steps:
(1) former flue gas is subjected to pre- dust removal process, obtains the flue gas after dedusting;The dustiness in flue gas after the dedusting is 10 ~30mg/Nm3
(2) flue gas after the dedusting is contacted to carry out pressure oxidation with gas ozoniferous, so as to form oxidation flue gas;
(3) absorbent magnesia dry powder is uniformly mixed with the oxidation flue gas in flue, subsequently into ciculation fluidized Bed absorption tower, the recirculating fluidized bed absorption tower is sprayed into by water, fully forms desulphurization denitration flue gas after reaction;Wherein, the flue gas Pipeline is arranged on the outside on the recirculating fluidized bed absorption tower;
(4) the desulphurization denitration flue gas is subjected to dust removal process, is purified flue gas, accessory substance and the absorption do not reacted completely Agent;With
(5) absorbent not reacted completely is recycled to the recirculating fluidized bed absorption tower.
2. according to the method described in claim 1, it is characterized in that, in step (1), the oxygen content of former flue gas for 10~ 20vol%.
3. according to the method described in claim 2, it is characterized in that, in step (1), the temperature of former flue gas is 80~150 DEG C, stream Speed is 2~5m/s.
4. according to the method described in claim 3, it is characterized in that, in step (1), the flow velocity of former flue gas is 2~3.5m/s.
5. according to the method described in claim 3, it is characterized in that, in step (1), the sulfur dioxide concentration of former flue gas is 1000 ~3000mg/Nm3, nitrous oxides concentration is 200~500mg/Nm3
6. according to the method described in claim 1, it is characterized in that, in step (2), the pressure is aoxidized in ozone oxidation device Middle progress, the entrance of the ozone oxidation device are provided with spiral board and ozone inlet.
7. according to the method described in claim 6, it is characterized in that, in step (3), the absorbent exists with the oxidation flue gas Time of contact in the recirculating fluidized bed absorption tower is more than 30min.
8. according to the method described in claim 1, it is characterized in that, in step (3), water is sprayed into the recirculating fluidized bed and is inhaled Receive in tower, so that the moisture of magnesia dry powder is 0.1~3.5wt%.
9. according to claim 1~8 any one of them method, it is characterised in that in step (4), the dust removal process is in cloth Carried out in bag dust collector.
10. method according to claims 1 to 8, it is characterised in that in step (5), by the absorption do not reacted completely Agent is sent into the recirculating fluidized bed absorption tower from the bottom on the recirculating fluidized bed absorption tower.
CN201711263347.5A 2017-12-05 2017-12-05 The dry desulfurization method of denitration of oxidation is forced based on ozone Pending CN107983119A (en)

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CN113117487A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Process for simultaneously desulfurizing and denitrifying flue gas
CN113117479A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Semi-dry flue gas desulfurization and denitrification method
CN113117481A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Method for desulfurization and denitrification by using chlorine dioxide
CN113117482A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Method for desulfurization and denitrification by using gas-phase oxidant
CN113117478A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Flue gas desulfurization and denitrification method based on fly ash
CN113117486A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Integrated treatment method for flue gas desulfurization and denitrification and cementing material preparation
CN113117474A (en) * 2019-12-31 2021-07-16 中晶环境科技股份有限公司 Integrated method for dry flue gas desulfurization and denitrification
CN113117493A (en) * 2019-12-31 2021-07-16 中晶环境科技股份有限公司 Method for flue gas desulfurization and denitration by using mixed reducing agent
CN113117480A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Method for flue gas desulfurization and denitration by using calcium-based absorbent
CN113117498A (en) * 2019-12-30 2021-07-16 中晶新材料有限公司 Integrated process for flue gas treatment and cementing material preparation
CN113117483A (en) * 2019-12-30 2021-07-16 中晶新材料有限公司 Integrated method for dry desulfurization and denitrification and cementing material manufacturing
CN113117490A (en) * 2019-12-31 2021-07-16 中晶新材料有限公司 Integrated process for flue gas desulfurization and denitrification and cementing material production
CN113117494A (en) * 2019-12-31 2021-07-16 中晶新材料有限公司 Integrated method for flue gas desulfurization and denitrification and cementing material production
CN113117489A (en) * 2019-12-31 2021-07-16 中晶新材料有限公司 Integrated process for flue gas desulfurization and denitrification and cementing material manufacturing
CN113117492A (en) * 2019-12-31 2021-07-16 中晶环境科技股份有限公司 Semi-dry integrated process for flue gas desulfurization and denitrification

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CN113117480A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Method for flue gas desulfurization and denitration by using calcium-based absorbent
CN113117487A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Process for simultaneously desulfurizing and denitrifying flue gas
CN113117479A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Semi-dry flue gas desulfurization and denitrification method
CN113117481A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Method for desulfurization and denitrification by using chlorine dioxide
CN113117482A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Method for desulfurization and denitrification by using gas-phase oxidant
CN113117478A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Flue gas desulfurization and denitrification method based on fly ash
CN113117486A (en) * 2019-12-30 2021-07-16 中晶环境科技股份有限公司 Integrated treatment method for flue gas desulfurization and denitrification and cementing material preparation
CN113117483A (en) * 2019-12-30 2021-07-16 中晶新材料有限公司 Integrated method for dry desulfurization and denitrification and cementing material manufacturing
CN113117498A (en) * 2019-12-30 2021-07-16 中晶新材料有限公司 Integrated process for flue gas treatment and cementing material preparation
CN113117493A (en) * 2019-12-31 2021-07-16 中晶环境科技股份有限公司 Method for flue gas desulfurization and denitration by using mixed reducing agent
CN113117474A (en) * 2019-12-31 2021-07-16 中晶环境科技股份有限公司 Integrated method for dry flue gas desulfurization and denitrification
CN113117490A (en) * 2019-12-31 2021-07-16 中晶新材料有限公司 Integrated process for flue gas desulfurization and denitrification and cementing material production
CN113117494A (en) * 2019-12-31 2021-07-16 中晶新材料有限公司 Integrated method for flue gas desulfurization and denitrification and cementing material production
CN113117489A (en) * 2019-12-31 2021-07-16 中晶新材料有限公司 Integrated process for flue gas desulfurization and denitrification and cementing material manufacturing
CN113117492A (en) * 2019-12-31 2021-07-16 中晶环境科技股份有限公司 Semi-dry integrated process for flue gas desulfurization and denitrification
CN112807958A (en) * 2021-01-20 2021-05-18 昆明理工大学 Method for simultaneously desulfurizing and denitrifying flue gas by dry method

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