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 PDFInfo
- 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
- Authority
- CN
- China
- Prior art keywords
- flue gas
- oxidation
- fluidized bed
- absorption tower
- ozone
- 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.)
- Pending
Links
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
- B01D53/75—Multi-step processes
-
- 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
- B01D2251/104—Ozone
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/602—Oxides
-
- 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 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
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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711263347.5A CN107983119A (en) | 2017-12-05 | 2017-12-05 | The dry desulfurization method of denitration of oxidation is forced based on ozone |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711263347.5A CN107983119A (en) | 2017-12-05 | 2017-12-05 | The dry desulfurization method of denitration of oxidation is forced based on ozone |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107983119A true CN107983119A (en) | 2018-05-04 |
Family
ID=62035495
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711263347.5A Pending CN107983119A (en) | 2017-12-05 | 2017-12-05 | The dry desulfurization method of denitration of oxidation is forced based on ozone |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107983119A (en) |
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111167299A (en) * | 2020-03-02 | 2020-05-19 | 中晶蓝实业集团有限公司 | Flue gas denitration device based on liquid oxidizing ions and application method thereof |
| CN111495142A (en) * | 2020-05-08 | 2020-08-07 | 北京金大万翔环保科技有限公司 | Automatically-adjustable ozone oxidation and semi-dry desulfurization and denitrification method and equipment |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101036855A (en) * | 2006-03-15 | 2007-09-19 | 洛阳高新博大环保新技术有限公司 | Circled dry phase flow tower flue gas desulphurizaion technique |
| CN102836634A (en) * | 2012-09-11 | 2012-12-26 | 北京世能中晶能源科技有限公司 | Desulfurization denitration method |
| CN103736373A (en) * | 2013-12-31 | 2014-04-23 | 浙江天蓝环保技术股份有限公司 | Flue gas treatment method and flue gas treatment device capable of simultaneous desulfurization, de-nitration and mercury removal through magnesium oxide |
| CN203790810U (en) * | 2014-03-21 | 2014-08-27 | 上海东硕环保科技有限公司 | Device for simultaneously desulfurizing and denitrifying flue gas by using magnesium oxide according to wet process |
| CN104984606A (en) * | 2015-07-10 | 2015-10-21 | 佛山君帝环保科技有限公司 | Synchronous desulphurization and dust removal system shared by multi-tower and multi-kiln and method |
-
2017
- 2017-12-05 CN CN201711263347.5A patent/CN107983119A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101036855A (en) * | 2006-03-15 | 2007-09-19 | 洛阳高新博大环保新技术有限公司 | Circled dry phase flow tower flue gas desulphurizaion technique |
| CN102836634A (en) * | 2012-09-11 | 2012-12-26 | 北京世能中晶能源科技有限公司 | Desulfurization denitration method |
| CN103736373A (en) * | 2013-12-31 | 2014-04-23 | 浙江天蓝环保技术股份有限公司 | Flue gas treatment method and flue gas treatment device capable of simultaneous desulfurization, de-nitration and mercury removal through magnesium oxide |
| CN203790810U (en) * | 2014-03-21 | 2014-08-27 | 上海东硕环保科技有限公司 | Device for simultaneously desulfurizing and denitrifying flue gas by using magnesium oxide according to wet process |
| CN104984606A (en) * | 2015-07-10 | 2015-10-21 | 佛山君帝环保科技有限公司 | Synchronous desulphurization and dust removal system shared by multi-tower and multi-kiln and method |
Non-Patent Citations (1)
| Title |
|---|
| 詹威全: "循环流化床脱硫的技术优势及应用的最新进展", 《中国环保产业》 * |
Cited By (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| CN111167299B (en) * | 2020-03-02 | 2024-02-27 | 中晶环境科技股份有限公司 | Flue gas denitration device based on liquid oxidizing ions and application method thereof |
| CN111167299A (en) * | 2020-03-02 | 2020-05-19 | 中晶蓝实业集团有限公司 | Flue gas denitration device based on liquid oxidizing ions and application method thereof |
| CN111495142A (en) * | 2020-05-08 | 2020-08-07 | 北京金大万翔环保科技有限公司 | Automatically-adjustable ozone oxidation and semi-dry desulfurization and denitrification method and equipment |
| 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 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107983119A (en) | The dry desulfurization method of denitration of oxidation is forced based on ozone | |
| JP6357280B2 (en) | Multi-pollutant removal method using semi-dry simultaneous desulfurization and denitration equipment for sintered flue gas by circulating fluidized bed | |
| CN207667430U (en) | Dry flue gas desulphurization denitrification apparatus | |
| CN102489149A (en) | Flue-gas purification and reclamation system and method thereof | |
| CN1962034A (en) | Method and apparatus for removing sulfur, nitrate and mercury simultaneously from boiler flue gas | |
| CN108176204A (en) | Flue gas and desulfurizing and denitrifying integrated purification system and purification method | |
| CN107456865A (en) | The method of flue gas desulfurization and denitrification | |
| CN107970769A (en) | Flue gas dry desulfurizing method of denitration based on ozone and carbide slag | |
| CN106731585B (en) | Coke oven flue gas dry-type desulfurization device, coke oven flue gas dry-type desulfurization and dust removal integrated system and method | |
| CN110665352A (en) | Dry desulfurization, denitrification and dust removal device and method for low-sulfur flue gas in cement kiln tail | |
| CN107497295A (en) | The method of dry flue gas desulphurization denitration | |
| CN101342459A (en) | Exhuast gas desulfurization, recycle and treatment method and apparatus | |
| CN102233230A (en) | Waste burning smoke purification process and purification system | |
| CN203955012U (en) | The system of boiler completing combustion decarburization and flue gas desulfurization and dedusting | |
| CN104524935A (en) | Single-tower type double-circulation sprinkling composite absorption device and method | |
| CN107899408B (en) | Wet method and dry method combined flue gas desulfurization system and desulfurization method | |
| CN105126567A (en) | Method and device for removing nitric oxide and sulfur oxide from gas flow | |
| CN107824039A (en) | Composite oxidant and the method for dry desulfurization denitration | |
| CN107812441A (en) | Flue gas dry desulfurizing method of denitration based on red mud | |
| WO2021134927A1 (en) | Dry process of integrated flue gas desulfurization and denitration | |
| CN201239608Y (en) | Integrated system for simultaneous desulfuration and denitration using semidry process | |
| CN213668653U (en) | Desulfurization and denitrification device containing moving bed desulfurization and denitrification tower | |
| CN212999279U (en) | Flue gas treatment system for efficiently utilizing carbon monoxide | |
| CN205965464U (en) | Desulphurization of exhaust gas denitration ultra -clean dust removal integrated device | |
| CN112870948A (en) | Heat recovery coke oven flue gas multi-pollutant ultra-clean discharge device and process thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180504 |
|
| RJ01 | Rejection of invention patent application after publication |