CN110465168A - Coke oven flue gas dry desulfurization and middle low-temperature denitration technology - Google Patents
Coke oven flue gas dry desulfurization and middle low-temperature denitration technology Download PDFInfo
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- B01D53/34—Chemical or biological purification of waste gases
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Abstract
The invention discloses a kind of coke oven flue gas dry desulfurization and middle low-temperature denitration technology, including desulfurization, dedusting, SCR system denitration, waste heat recycling, wherein desulphurization system adsorbs desulfurization using dry state adsorbent；Dry state adsorbent is the mixture or magnesium hydroxide of sodium bicarbonate and silica；Dry state adsorbent is powdered, and fineness D90 < 20 μm, to guarantee that there is adsorbent enough specific surface areas to reach higher reactivity；Dry state adsorbent is selected to adsorb sulfide in inventive desulfurization process, dry desulfurization is easy to operate, and it is smaller to invest to build cost；It can guarantee that sulfur compounds adsorption is complete using the dry state absorbent powder of particular fineness, for dedirt again via SCR denitration system denitration, final nitrogen oxide removal efficiency reaches 88% or more to sulfide removal rate after 95% or more, desulfurization.
Description
Technical field
The present invention relates to a kind of industrial waste gas processing techniques, more particularly, to a kind of coke oven flue gas dry desulfurization denitration skill
Art.
Background technique
SO2, NOx be to form one of main matter of acid rain, caused by atmosphere pollution and acid rain problem get worse, to people
Class health and ecosystem harm are serious, SO2, NOx pollution have become restrict China's sustainable development of socio-economy it is important
Factor.It is detected according to environmental protection administration, particulate matter, sulfur dioxide, benzo (a) pyrrole, nitrogen oxides that domestic existing coke oven is discharged
Concentration be not able to satisfy existing " the coking chemistry emission of industrial pollutants standard " GB16172-2012 of country mostly.According to the mark
Newly-built enterprise and 1 Qi existing enterprise January in 2015 from alignment request on October 1st, 2012, the granular material discharged concentration of coke oven chimney
30mg/Nm3, sulfur dioxide 50mg/Nm3, nitrogen oxides 500mg/Nm3, benzo (a) pyrrole 0.3ug/Nm3；Special limit value is particle
Object concentration of emission 15mg/Nm3, sulfur dioxide 30mg/Nm3, nitrogen oxides 150mg/Nm3, benzo (a) pyrrole 0.3ug/Nm3, herein
Under background, develops and coking industry economy, feasible desulfurizing and denitrifying process technology is suitble to be industry development inexorable trends, meet country
The demand of environmental protection.Existing desulfurization technology is broadly divided into wet process of FGD, dry flue gas desulphurization and semidry method by process characteristic
Flue gas desulfurization, wherein dry method is easy to operate, invests to build that cost is relatively low, and dry process mainly cooperates adsorbent to cigarette by fluidized bed
Gas carries out adverse current or fair current spray completes desulfurization, and adsorbent is mainly lime (calcium base) in mature technology at present, adsorbs desulfurization
Efficiency highest is generally 80% or so；The main now industrial widely applied technology of denitration is SCR (selective catalytic reduction
Method) and SNCR (selective non-catalytic reduction method), wherein SNCR denitration needs high-temperature area, and coke oven production process is difficult to realize,
SNCR method can be impacted to coke oven production technology in burner hearth internal spray reducing agent simultaneously, and the production technology of coke oven is special
Point does not allow to carry out gametic fertility in the inside of coke oven, therefore SNCR method is not suitable for the denitration of coke oven flue gas, therefore coke oven cigarette
Qi exhaustion nitre uses SCR technology.But current coke oven flue gas dry desulfurization denitration technology still needs on treatment effeciency and effect
It improves.
Summary of the invention
In order to solve the above technical problems, to provide a kind of denitrification efficiency high by the present invention, and it is easy to operate invest to build cost compared with
Low coke oven flue gas desulfurizing and denitrifying process.
The technical solution of the present invention is to provide a kind of coke oven flue gas dry desulfurization denitration technologies, include the following steps:
S1. coke oven flue gas enters desulphurization system desulfurization, and desulphurization system adsorbs desulfurization using dry state adsorbent, enters dedusting afterwards
System；Dry state adsorbent is the mixture or magnesium hydroxide of sodium bicarbonate and silica；Dry state adsorbent is powdered, and
Fineness D90 < 20 μm, to guarantee that there is adsorbent enough specific surface areas to reach higher reactivity；
S2. the coke oven flue gas of desulfurization and dedusting is passed through SCR denitration system denitration, after to flue gas carry out waste heat recycling, it is up to standard
Discharge；
Further, in step S1 when dry state adsorbent is made of sodium bicarbonate and silica, the mass ratio of the two
For sodium bicarbonate: silica=5~8:1.
Further, in step S1 dry state absorbent powder fineness be distributed as < 10 μm: 10~20 μm: 20~35 μm=3~
7:90:3~7 carry out controlling to fineness distribution the temperature range for being conducive to adsorbent in coke oven flue gas with highest absorption work
Property, can comparatively fast be reacted with sulfide completion absorption, and fineness it is meticulous it is more demanding for attrition process will increase production cost,
Slightly adsorbent activity reduces adsorption effect variation to fineness within the scope of flue-gas temperature excessively, furthermore controls adsorbent fineness and also helps
Subsequent dust removal step.
Further, dry state absorbent powder is transported in step S1 with gas mode of movement and to pass through multiple nozzles directly logical
Enter in flue gas, to guarantee that dry state absorbent powder is sufficiently spread and smoke reaction.
Cyclone structure is arranged in nozzle interior, which is the rotational structure that multiple blades surround that rotary shaft is formed, and
The angle that the blade face of blade and rotary shaft are formed is 15~25 °, is additionally provided on the blade face of each blade along the more of injection direction
Guide groove.
Every processing 180000Nm in step S13The dry state adsorbent of flue gas supplement 5~10%.
Catalyst in step S2 in SCR denitration system include following weight percentage components titanium dioxide 75~
80%, tungstic acid 7~10%, manganese dioxide 2~3%, molybdenum trioxide 0.5~1%, vanadic anhydride 1~3%, titanium dioxide
Silicon 5~8%, gama-alumina 1~2%, calcium oxide 0.5~1.5%, sodium oxide molybdena 0.05~0.1%, potassium oxide 0.05~
0.1%.
The advantages of the present invention: dry state adsorbent is selected in sweetening process to adsorb sulfide, dry method is de-
Sulphur is easy to operate, and it is smaller to invest to build cost；It can guarantee that sulfur compounds adsorption is complete using the dry state absorbent powder of particular fineness, sulphur
Again via SCR denitration system denitration, final nitrogen oxide removal efficiency reaches dedirt compound removal rate after 95% or more, desulfurization
88% or more.
Detailed description of the invention
Fig. 1 is coke oven flue gas dry desulfurization denitrating technique flow diagram of the present invention.
Fig. 2 is the schematic elevation view of nozzle interior cyclone structure of the invention.
Fig. 3 is the schematic top plan view of nozzle interior cyclone structure of the invention.
Specific embodiment
The invention will be further described With reference to embodiment.
Embodiment 1
The present invention provides a kind of coke oven flue gas dry desulfurization denitration technology, includes the following steps:
S1. coke oven flue gas (temperature be 220-260 DEG C) enters desulfurizing tower from tower bottom, at the top of desulfurizing tower by spraying system to
Dry state absorbent powder is sprayed in flue gas；It is sodium bicarbonate: silica=6:1 that dry state adsorbent, which forms mass ratio,；Dry state is inhaled
Attached dose of powdered fineness is distributed as < 10 μm: 10~20 μm: 20~35 μm=3:90:7, to guarantee that adsorbent has enough ratios
Surface area reaches higher reactivity, carries out control to fineness distribution and is conducive to adsorbent in the temperature range tool of coke oven flue gas
There is highest adsorption activity, completion absorption can be comparatively fast reacted with sulfide, and fineness is meticulous more demanding for attrition process
Production cost will be increased, slightly adsorbent activity reduces adsorption effect variation to fineness within the scope of flue-gas temperature excessively, and furthermore control is inhaled
Attached dose of fineness also helps subsequent dust removal step；Every processing 180000Nm3Flue gas supplement 5~10% dry state adsorbent；
S2. the flue gas Jing Guo desulfurization is passed through dust pelletizing system, will form largely after adsorbing sulfide due to dry state adsorbent
Dust, it is therefore necessary to flue gas is dusted before flue gas enters denitrating system；Bag filter dedusting, cloth bag are used herein
On filter cake can be used as the clean second stage of flue gas because filter cake is by reaction product, unreacted adsorbent and flying dust group
At, thus the especially unreacted adsorbent of the ingredient when flue gas passes through filter cake in filter cake can adsorb remaining sulfide from
And achieve the effect that the secondary removing of sulfide；
S3. the coke oven flue gas of desulfurization and dedusting is passed through SCR denitration system denitration, after to flue gas carry out waste heat recycling, it is up to standard
Discharge；Wherein catalyst includes titanium dioxide 78% following weight percentage components, tungstic acid 8.4%, manganese dioxide
3%, molybdenum trioxide 0.5%, vanadic anhydride 1.5%, silica 7%, gama-alumina 1%, calcium oxide 0.5%, sodium oxide molybdena
0.05%, potassium oxide 0.05%；
Wherein cyclone structure is arranged in the nozzle interior of spraying system in step S1, which is that multiple blades 2 surround
The rotational structure that rotary shaft 1 is formed, and the angle theta that the blade face of blade 2 and rotary shaft 1 are formed is 25 °, the blade face of each blade 2
On be additionally provided with a plurality of guide groove 21 along injection direction.When dry state absorbent powder reaches nozzle, since blade is by powder
The impact cyclone structure of last air-flow starts to rotate, therefore rotation is scattered when powder jetting nozzle and increases dry state adsorbent
The diffusion of powder can come into full contact with flue gas；And the emission direction that guide groove can limit powder air-flow makes multiple sprays
The powder air-flow that mouth sprays, which crosses to form part turbulent flow and increase contact of the dry state absorbent powder with coke oven flue gas, improves absorption effect
Fruit.
During above-mentioned desulphurization denitration, sulfur dioxide (SO in entrance coke oven flue gas2) concentration be 500mg/Nm3, nitrogen oxygen
The concentration of compound (NOx) is 600mg/Nm3, after the processing of above-mentioned desulfurizing and denitrifying process, detect sulfur dioxide (SO2) concentration be
10mg/Nm3, removal efficiency 98%, the concentration of nitrogen oxides (NOx) is 60mg/Nm3, removal efficiency 90%.
Embodiment 2
The present invention provides a kind of coke oven flue gas dry desulfurization denitration technology, includes the following steps:
S1. coke oven flue gas (temperature be 220-260 DEG C) enters desulfurizing tower from tower bottom, at the top of desulfurizing tower by spraying system to
Dry state absorbent powder is sprayed in flue gas；It is sodium bicarbonate: silica=8:1 that dry state adsorbent, which forms mass ratio,；Dry state is inhaled
Attached dose of powdered fineness is distributed as < 10 μm: 10~20 μm: 20~35 μm=3:90:3, to guarantee that adsorbent has enough ratios
Surface area reaches higher reactivity, carries out control to fineness distribution and is conducive to adsorbent in the temperature range tool of coke oven flue gas
There is highest adsorption activity, completion absorption can be comparatively fast reacted with sulfide, and fineness is meticulous more demanding for attrition process
Production cost will be increased, slightly adsorbent activity reduces adsorption effect variation to fineness within the scope of flue-gas temperature excessively, and furthermore control is inhaled
Attached dose of fineness also helps subsequent dust removal step；Every processing 180000Nm3Flue gas supplement 5~10% dry state adsorbent；
S2. the flue gas Jing Guo desulfurization is passed through dust pelletizing system, will form largely after adsorbing sulfide due to dry state adsorbent
Dust, it is therefore necessary to flue gas is dusted before flue gas enters denitrating system；Bag filter dedusting, cloth bag are used herein
On filter cake can be used as the clean second stage of flue gas because filter cake is by reaction product, unreacted adsorbent and flying dust group
At, thus the especially unreacted adsorbent of the ingredient when flue gas passes through filter cake in filter cake can adsorb remaining sulfide from
And achieve the effect that the secondary removing of sulfide；
S3. the coke oven flue gas of desulfurization and dedusting is passed through SCR denitration system denitration, after to flue gas carry out waste heat recycling, it is up to standard
Discharge；Wherein catalyst includes titanium dioxide 77% following weight percentage components, tungstic acid 9%, manganese dioxide 2%,
Molybdenum trioxide 0.8%, vanadic anhydride 2%, silica 6%, gama-alumina 1.5%, calcium oxide 1.5%, sodium oxide molybdena
0.1%, potassium oxide 0.1%；
Wherein cyclone structure is arranged in the nozzle interior of spraying system in step S1, which is that multiple blades 2 surround
The rotational structure that rotary shaft 1 is formed, and the angle theta that the blade face of blade 2 and rotary shaft 1 are formed is 20 °, the blade face of each blade 2
On be additionally provided with a plurality of guide groove 21 along injection direction.When dry state absorbent powder reaches nozzle, since blade is by powder
The impact cyclone structure of last air-flow starts to rotate, therefore rotation is scattered when powder jetting nozzle and increases dry state adsorbent
The diffusion of powder can come into full contact with flue gas；And the emission direction that guide groove can limit powder air-flow makes multiple sprays
The powder air-flow that mouth sprays, which crosses to form part turbulent flow and increase contact of the dry state absorbent powder with coke oven flue gas, improves absorption effect
Fruit.
During above-mentioned desulphurization denitration, sulfur dioxide (SO in entrance coke oven flue gas2) concentration be 700mg/Nm3, nitrogen oxygen
The concentration of compound (NOx) is 700mg/Nm3, after the processing of above-mentioned desulfurizing and denitrifying process, detect sulfur dioxide (SO2) concentration be
21mg/Nm3, removal efficiency 97%, the concentration of nitrogen oxides (NOx) is 84mg/Nm3, removal efficiency 88%.
Embodiment 3
The present invention provides a kind of coke oven flue gas dry desulfurization denitration technology, includes the following steps:
S1. coke oven flue gas (temperature be 220-260 DEG C) enters desulfurizing tower from tower bottom, at the top of desulfurizing tower by spraying system to
Dry state absorbent powder is sprayed in flue gas；It is sodium bicarbonate: silica=5:1 that dry state adsorbent, which forms mass ratio,；Dry state is inhaled
Attached dose of powdered fineness is distributed as < 10 μm: 10~20 μm: 20~35 μm=5:90:6, to guarantee that adsorbent has enough ratios
Surface area reaches higher reactivity, carries out control to fineness distribution and is conducive to adsorbent in the temperature range tool of coke oven flue gas
There is highest adsorption activity, completion absorption can be comparatively fast reacted with sulfide, and fineness is meticulous more demanding for attrition process
Production cost will be increased, slightly adsorbent activity reduces adsorption effect variation to fineness within the scope of flue-gas temperature excessively, and furthermore control is inhaled
Attached dose of fineness also helps subsequent dust removal step；Every processing 180000Nm3Flue gas supplement 5~10% dry state adsorbent；
S2. the flue gas Jing Guo desulfurization is passed through dust pelletizing system, will form largely after adsorbing sulfide due to dry state adsorbent
Dust, it is therefore necessary to flue gas is dusted before flue gas enters denitrating system；Bag filter dedusting, cloth bag are used herein
On filter cake can be used as the clean second stage of flue gas because filter cake is by reaction product, unreacted adsorbent and flying dust group
At, thus the especially unreacted adsorbent of the ingredient when flue gas passes through filter cake in filter cake can adsorb remaining sulfide from
And achieve the effect that the secondary removing of sulfide；
S3. the coke oven flue gas of desulfurization and dedusting is passed through SCR denitration system denitration, after to flue gas carry out waste heat recycling, it is up to standard
Discharge；Wherein catalyst includes titanium dioxide 80% following weight percentage components, tungstic acid 7%, manganese dioxide 2%,
Molybdenum trioxide 0.9%, vanadic anhydride 1%, silica 7%, gama-alumina 1%, calcium oxide 1%, sodium oxide molybdena 0.05%,
Potassium oxide 0.05%；
Wherein cyclone structure is arranged in the nozzle interior of spraying system in step S1, which is that multiple blades 2 surround
The rotational structure that rotary shaft 1 is formed, and the angle theta that the blade face of blade 2 and rotary shaft 1 are formed is 15 °, the blade face of each blade 2
On be additionally provided with a plurality of guide groove 21 along injection direction.When dry state absorbent powder reaches nozzle, since blade is by powder
The impact cyclone structure of last air-flow starts to rotate, therefore rotation is scattered when powder jetting nozzle and increases dry state adsorbent
The diffusion of powder can come into full contact with flue gas；And the emission direction that guide groove can limit powder air-flow makes multiple sprays
The powder air-flow that mouth sprays, which crosses to form part turbulent flow and increase contact of the dry state absorbent powder with coke oven flue gas, improves absorption effect
Fruit.
During above-mentioned desulphurization denitration, sulfur dioxide (SO in entrance coke oven flue gas2) concentration be 600mg/Nm3, nitrogen oxygen
The concentration of compound (NOx) is 600mg/Nm3, after the processing of above-mentioned desulfurizing and denitrifying process, detect sulfur dioxide (SO2) concentration be
12mg/Nm3, removal efficiency 98%, the concentration of nitrogen oxides (NOx) is 67mg/Nm3, removal efficiency 89%.
Embodiment 4
The present invention provides a kind of coke oven flue gas dry desulfurization denitration technology, includes the following steps:
S1. coke oven flue gas (temperature be 220-260 DEG C) enters desulfurizing tower from tower bottom, at the top of desulfurizing tower by spraying system to
Dry state absorbent powder is sprayed in flue gas；It is sodium bicarbonate: silica=7:1 that dry state adsorbent, which forms mass ratio,；Dry state is inhaled
Attached dose of powdered fineness is distributed as < 10 μm: 10~20 μm: 20~35 μm=3:90:7, to guarantee that adsorbent has enough ratios
Surface area reaches higher reactivity, carries out control to fineness distribution and is conducive to adsorbent in the temperature range tool of coke oven flue gas
There is highest adsorption activity, completion absorption can be comparatively fast reacted with sulfide, and fineness is meticulous more demanding for attrition process
Production cost will be increased, slightly adsorbent activity reduces adsorption effect variation to fineness within the scope of flue-gas temperature excessively, and furthermore control is inhaled
Attached dose of fineness also helps subsequent dust removal step；Every processing 180000Nm3Flue gas supplement 5~10% dry state adsorbent；
S2. the flue gas Jing Guo desulfurization is passed through dust pelletizing system, will form largely after adsorbing sulfide due to dry state adsorbent
Dust, it is therefore necessary to flue gas is dusted before flue gas enters denitrating system；Bag filter dedusting, cloth bag are used herein
On filter cake can be used as the clean second stage of flue gas because filter cake is by reaction product, unreacted adsorbent and flying dust group
At, thus the especially unreacted adsorbent of the ingredient when flue gas passes through filter cake in filter cake can adsorb remaining sulfide from
And achieve the effect that the secondary removing of sulfide；
S3. the coke oven flue gas of desulfurization and dedusting is passed through SCR denitration system denitration, after to flue gas carry out waste heat recycling, it is up to standard
Discharge；Wherein catalyst includes titanium dioxide 75% following weight percentage components, tungstic acid 10%, manganese dioxide
2.5%, molybdenum trioxide 1%, vanadic anhydride 3%, silica 5%, gama-alumina 2%, calcium oxide 1.4%, sodium oxide molybdena
0.06%, potassium oxide 0.04%；
Wherein cyclone structure is arranged in the nozzle interior of spraying system in step S1, which is that multiple blades 2 surround
The rotational structure that rotary shaft 1 is formed, and the angle theta that the blade face of blade 2 and rotary shaft 1 are formed is 25 °, the blade face of each blade 2
On be additionally provided with a plurality of guide groove 21 along injection direction.When dry state absorbent powder reaches nozzle, since blade is by powder
The impact cyclone structure of last air-flow starts to rotate, therefore rotation is scattered when powder jetting nozzle and increases dry state adsorbent
The diffusion of powder can come into full contact with flue gas；And the emission direction that guide groove can limit powder air-flow makes multiple sprays
The powder air-flow that mouth sprays, which crosses to form part turbulent flow and increase contact of the dry state absorbent powder with coke oven flue gas, improves absorption effect
Fruit.
During above-mentioned desulphurization denitration, sulfur dioxide (SO in entrance coke oven flue gas2) concentration be 500mg/Nm3, nitrogen oxygen
The concentration of compound (NOx) is 700mg/Nm3, after the processing of above-mentioned desulfurizing and denitrifying process, detect sulfur dioxide (SO2) concentration be
10mg/Nm3, removal efficiency 98%, the concentration of nitrogen oxides (NOx) is 70mg/Nm3, removal efficiency 90%.
Embodiment 5
The present invention provides a kind of coke oven flue gas dry desulfurization denitration technology, includes the following steps:
S1. coke oven flue gas (temperature be 220-260 DEG C) enters desulfurizing tower from tower bottom, at the top of desulfurizing tower by spraying system to
Dry state absorbent powder is sprayed in flue gas；Dry state adsorbent group becomes magnesium hydroxide；Dry state absorbent powder shape fineness is distributed as <
It 10 μm: 10~20 μm: 20~35 μm=7:90:7, is lived with guaranteeing that there is adsorbent enough specific surface areas to reach higher reaction
Property, to fineness distribution carry out control be conducive to adsorbent coke oven flue gas temperature range have highest adsorption activity, can
Completion absorption is comparatively fast reacted with sulfide, and fineness is meticulous more demanding for attrition process will increase production cost, fineness mistake
Slightly adsorbent activity reduces adsorption effect variation within the scope of flue-gas temperature, furthermore controls adsorbent fineness and also helps subsequent remove
Dirt step；Every processing 180000Nm3Flue gas supplement 5~10% dry state adsorbent；
S2. the flue gas Jing Guo desulfurization is passed through dust pelletizing system, will form largely after adsorbing sulfide due to dry state adsorbent
Dust, it is therefore necessary to flue gas is dusted before flue gas enters denitrating system；Bag filter dedusting, cloth bag are used herein
On filter cake can be used as the clean second stage of flue gas because filter cake is by reaction product, unreacted adsorbent and flying dust group
At, thus the especially unreacted adsorbent of the ingredient when flue gas passes through filter cake in filter cake can adsorb remaining sulfide from
And achieve the effect that the secondary removing of sulfide；
S3. the coke oven flue gas of desulfurization and dedusting is passed through SCR denitration system denitration, after to flue gas carry out waste heat recycling, it is up to standard
Discharge；Wherein catalyst includes titanium dioxide 75% following weight percentage components, tungstic acid 10%, manganese dioxide
2.5%, molybdenum trioxide 1%, vanadic anhydride 3%, silica 5%, gama-alumina 2%, calcium oxide 1.4%, sodium oxide molybdena
0.06%, potassium oxide 0.04%；
Wherein cyclone structure is arranged in the nozzle interior of spraying system in step S1, which is that multiple blades 2 surround
The rotational structure that rotary shaft 1 is formed, and the angle theta that the blade face of blade 2 and rotary shaft 1 are formed is 20 °, the blade face of each blade 2
On be additionally provided with a plurality of guide groove 21 along injection direction.When dry state absorbent powder reaches nozzle, since blade is by powder
The impact cyclone structure of last air-flow starts to rotate, therefore rotation is scattered when powder jetting nozzle and increases dry state adsorbent
The diffusion of powder can come into full contact with flue gas；And the emission direction that guide groove can limit powder air-flow makes multiple sprays
The powder air-flow that mouth sprays, which crosses to form part turbulent flow and increase contact of the dry state absorbent powder with coke oven flue gas, improves absorption effect
Fruit.
During above-mentioned desulphurization denitration, sulfur dioxide (SO in entrance coke oven flue gas2) concentration be 600mg/Nm3, nitrogen oxygen
The concentration of compound (NOx) is 700mg/Nm3, after the processing of above-mentioned desulfurizing and denitrifying process, detect sulfur dioxide (SO2) concentration be
18mg/Nm3, removal efficiency 97%, the concentration of nitrogen oxides (NOx) is 78mg/Nm3, removal efficiency 89%.
Comparative example 1
Using plain nozzle rather than the nozzle of cyclone structure is installed, other are the same as embodiment 1.
During desulphurization denitration, sulfur dioxide (SO in entrance coke oven flue gas2) concentration be 500mg/Nm3, nitrogen oxides
(NOx) concentration is 600mg/Nm3, after the processing of above-mentioned desulfurizing and denitrifying process, detect sulfur dioxide (SO2) concentration be 50mg/
Nm3, removal efficiency 90%, the concentration of nitrogen oxides (NOx) is 270mg/Nm3, removal efficiency 55%.In the process, by
Be not unable to fully contact with coke oven flue gas in dry state absorbent powder, lead to sulfur compounds adsorption effect deviation, and at this time due to
Entering after SCR denitration system in coke oven flue gas after desulfurization still with a large amount of sulfide leads to catalyst poisoning, therefore serious
Affect denitration effect.
Comparative example 2~5
Comparative example 2~5 is as follows to adjust separately dry state absorbent powder shape fineness in embodiment 1:
| Comparative example | Fineness of powder | Fineness of powder distribution |
| Comparative example 2 | < 10 μm: 10~20 μm: 20~35 μm | 2:90:2 |
| Comparative example 3 | < 10 μm: 10~20 μm: 20~35 μm | 1:90:8 |
| Comparative example 4 | < 10 μm: 10~20 μm: 20~35 μm | 8:90:1 |
| Comparative example 5 | < 10 μm: 10~20 μm: 20~35 μm | 8:90:8 |
Other are the same as embodiment 1.
During desulphurization denitration, sulfur dioxide (SO in entrance coke oven flue gas2) concentration be 500mg/Nm3, nitrogen oxides
(NOx) concentration is 600mg/Nm3, after the processing of above-mentioned desulfurizing and denitrifying process, sulfide in flue gas and nitrous oxides concentration knot
Fruit is as follows:
| Comparative example | SO2Concentration | SO2Removal efficiency | NOx concentration | NOx removal efficiency |
| Comparative example 2 | 110mg/Nm3 | 78% | 300mg/Nm3 | 50% |
| Comparative example 3 | 100mg/Nm3 | 80% | 294mg/Nm3 | 51% |
| Comparative example 4 | 90mg/Nm3 | 82% | 252mg/Nm3 | 58% |
| Comparative example 5 | 100mg/Nm3 | 80% | 288mg/Nm3 | 52% |
Change the specific surface area that dry state absorbent powder fineness is distributed and changes dry state adsorbent, is unable to reach absorption two
The optimum state of sulfur oxide can not make flue gas and dry state adsorbent contact effect best, so as to cause absorption sulfur dioxide effect
Difference further affects subsequent SCR adsorbent to the adsorption effect of nitrogen oxides；Furthermore change dry state absorbent powder fineness point
After cloth, when dry state adsorbent is injected into desulfurizing tower, dry state adsorbent can not be in tower due to hot-air and the work of gravity
The layered distribution for being suitable for formation, therefore can not be come into full contact with flue gas, to further affect the effect of absorption sulfur dioxide
Fruit.Comparative example 6~9
Comparative example 6~9 is to adjust the mass ratio of the sodium bicarbonate of dry state adsorbent and silica in embodiment 1 such as
Under:
| Comparative example | Dry state adsorbent forms mass ratio |
| Comparative example 6 | Sodium bicarbonate: silica=4:1 |
| Comparative example 7 | Sodium bicarbonate: silica=3:2 |
| Comparative example 8 | Sodium bicarbonate: silica=9:1 |
| Comparative example 9 | Sodium bicarbonate: silica=10:1 |
Other are the same as embodiment 1.
During desulphurization denitration, sulfur dioxide (SO in entrance coke oven flue gas2) concentration be 500mg/Nm3, nitrogen oxides
(NOx) concentration is 600mg/Nm3, after the processing of above-mentioned desulfurizing and denitrifying process, sulfide in flue gas and nitrous oxides concentration knot
Fruit is as follows:
The mass ratio of sodium bicarbonate and silica is too low in dry state adsorbent, then by carbon when smoke contacts dry state adsorbent
The amount that sour hydrogen sodium decomposes the high activity sodium carbonate of generation at high temperature is insufficient, i.e., it is complete can not to be carbonated sodium for the sulfur dioxide in flue gas
Full response absorption；And when the mass ratio of sodium bicarbonate and silica is excessively high in dry state adsorbent, first is that fineness of powder is processed
Difficulty is higher, and powder is difficult to be uniformly mixed, second is that silica, which can not play, alleviates high-temperature flue gas and sodium bicarbonate contact process
Effect, cause sodium bicarbonate to decompose too fast and can not instantaneously decompose the high activity sodium carbonate and dioxy of generation using sodium bicarbonate
Change sulphur and carry out reaction absorption, that is, the reactivity of the sodium carbonate and sulfur dioxide that have generated substantially reduces, and affects desulfurization effect
Fruit, so that making excessive sulfur dioxide enter SCR denitration system influences denitration effect.
The present embodiments relate to the material arrived, reagent and experimental facilities, are to meet industrial waste gas unless otherwise instructed
The commercial product of process field.
The above is merely a preferred embodiment of the present invention, it is noted that for those skilled in the art
For, under the premise of not departing from core of the invention technology, improvements and modifications can also be made, these improvements and modifications are also answered
Belong to scope of patent protection of the invention.With any change in the comparable meaning and scope of claims of the present invention, all
It is considered as being included within the scope of the claims.
Claims (8)
1. coke oven flue gas dry desulfurization and middle low-temperature denitration technology, it is characterised in that include the following steps:
S1. coke oven flue gas enters desulphurization system desulfurization, and the desulphurization system adsorbs desulfurization using dry state adsorbent, enters dedusting afterwards
System；The dry state adsorbent is the mixture or magnesium hydroxide of sodium bicarbonate and silica；The dry state adsorbent is
Powdered and fineness D90 < 20 μm；
S2. the coke oven flue gas of desulfurization and dedusting is passed through SCR denitration system denitration, after to flue gas carry out waste heat recycling, qualified discharge.
2. coke oven flue gas dry desulfurization according to claim 1 and middle low-temperature denitration technology, it is characterised in that the step
Dry state adsorbent is made of sodium bicarbonate and silica in S1, and the mass ratio of the two is sodium bicarbonate: silica=5~8:
1。
3. coke oven flue gas dry desulfurization according to claim 1 and middle low-temperature denitration technology, it is characterised in that the step
Dry state absorbent powder fineness is distributed as < 10 μm: 10~20 μm: 20~35 μm=3~7:90:3~7 in S1.
4. coke oven flue gas dry desulfurization according to claim 1 and middle low-temperature denitration technology, it is characterised in that the step
Dry state absorbent powder is transported with gas mode of movement and passes through multiple nozzles and is passed directly into flue gas in S1.
5. coke oven flue gas dry desulfurization according to claim 4 and middle low-temperature denitration technology, it is characterised in that the nozzle
Inside setting cyclone structure, the cyclone structure are the rotational structure that multiple blades surround that rotary shaft is formed, each blade
Blade face on injection direction is provided with a plurality of guide groove.
6. coke oven flue gas dry desulfurization according to claim 5 and middle low-temperature denitration technology, it is characterised in that the blade
Blade face and the rotary shaft formed angle theta be 15~25 °.
7. coke oven flue gas dry desulfurization according to claim 1 and middle low-temperature denitration technology, it is characterised in that the step
The dry state adsorbent of every processing 180000Nm3 flue gas supplement 5~10% in S1.
8. coke oven flue gas dry desulfurization according to claim 1 and middle low-temperature denitration technology, it is characterised in that the step
Catalyst in S2 in SCR denitration system includes titanium dioxide 75~80% following weight percentage components, and tungstic acid 7~
10%, manganese dioxide 2~3%, molybdenum trioxide 0.5~1%, vanadic anhydride 1~3%, silica 5~8%, gamma oxidation
Aluminium 1~2%, calcium oxide 0.5~1.5%, sodium oxide molybdena 0.05~0.1%, potassium oxide 0.05~0.1%.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113797752A (en) * | 2021-10-29 | 2021-12-17 | 宜兴市苏哈电力设备有限公司 | A high-efficient dry process SOx/NOx control system for flue gas is handled |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006021204A (en) * | 2005-10-03 | 2006-01-26 | Mitsui Eng & Shipbuild Co Ltd | Exhaust gas treating agent and method and apparatus for treating exhaust gas by using the same |
| CA2290138C (en) * | 1997-05-14 | 2007-07-24 | Solvay (Societe Anonyme) | Reactive powder composition and method for purifying gas |
| CN103768903A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Regeneration flue gas denitration process for FCC apparatus |
| CN204768240U (en) * | 2015-03-20 | 2015-11-18 | 湖南凌峰环保科技有限公司 | Novel desulfurization spray tube |
| CN106861350A (en) * | 2017-04-21 | 2017-06-20 | 上海市机电设计研究院有限公司 | The biomass electric power plant gas cleaning handling process and system of dry desulfurization and low-temperature denitration |
-
2018
- 2018-05-11 CN CN201810446811.2A patent/CN110465168A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2290138C (en) * | 1997-05-14 | 2007-07-24 | Solvay (Societe Anonyme) | Reactive powder composition and method for purifying gas |
| JP2006021204A (en) * | 2005-10-03 | 2006-01-26 | Mitsui Eng & Shipbuild Co Ltd | Exhaust gas treating agent and method and apparatus for treating exhaust gas by using the same |
| CN103768903A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Regeneration flue gas denitration process for FCC apparatus |
| CN204768240U (en) * | 2015-03-20 | 2015-11-18 | 湖南凌峰环保科技有限公司 | Novel desulfurization spray tube |
| CN106861350A (en) * | 2017-04-21 | 2017-06-20 | 上海市机电设计研究院有限公司 | The biomass electric power plant gas cleaning handling process and system of dry desulfurization and low-temperature denitration |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113797752A (en) * | 2021-10-29 | 2021-12-17 | 宜兴市苏哈电力设备有限公司 | A high-efficient dry process SOx/NOx control system for flue gas is handled |
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