CN203764107U - Integrated low-temperature flue gas desulfurization and denitrification ammonia removal device - Google Patents
Integrated low-temperature flue gas desulfurization and denitrification ammonia removal device Download PDFInfo
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- CN203764107U CN203764107U CN201420109070.6U CN201420109070U CN203764107U CN 203764107 U CN203764107 U CN 203764107U CN 201420109070 U CN201420109070 U CN 201420109070U CN 203764107 U CN203764107 U CN 203764107U
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- ammonia
- flue gas
- except
- denitration
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 314
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 157
- 239000003546 flue gas Substances 0.000 title claims abstract description 80
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 70
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 30
- 230000023556 desulfurization Effects 0.000 title abstract description 16
- 239000000843 powder Substances 0.000 claims abstract description 27
- 238000002360 preparation method Methods 0.000 claims abstract description 14
- 238000011084 recovery Methods 0.000 claims abstract description 12
- 230000000903 blocking effect Effects 0.000 claims abstract description 11
- 239000003054 catalyst Substances 0.000 claims description 47
- 239000002245 particle Substances 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 26
- 239000000571 coke Substances 0.000 claims description 25
- 239000004744 fabric Substances 0.000 claims description 21
- 238000005507 spraying Methods 0.000 claims description 21
- 239000002131 composite material Substances 0.000 claims description 20
- 239000002912 waste gas Substances 0.000 claims description 19
- 238000007599 discharging Methods 0.000 claims description 15
- 239000000428 dust Substances 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 238000009826 distribution Methods 0.000 claims description 6
- 230000003068 static effect Effects 0.000 claims description 6
- 239000000706 filtrate Substances 0.000 claims description 5
- 239000000779 smoke Substances 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 16
- 235000011114 ammonium hydroxide Nutrition 0.000 abstract description 10
- 238000005243 fluidization Methods 0.000 abstract description 5
- 238000000746 purification Methods 0.000 abstract description 5
- 239000002918 waste heat Substances 0.000 abstract description 5
- 239000013618 particulate matter Substances 0.000 abstract description 4
- 230000009286 beneficial effect Effects 0.000 abstract description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 abstract 1
- 239000002956 ash Substances 0.000 description 20
- 230000008569 process Effects 0.000 description 11
- 238000010438 heat treatment Methods 0.000 description 6
- 239000010410 layer Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 4
- 230000003009 desulfurizing effect Effects 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 2
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 2
- 235000011130 ammonium sulphate Nutrition 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 239000002344 surface layer Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000010882 bottom ash Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000005215 recombination Methods 0.000 description 1
- 230000006798 recombination Effects 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The utility model relates to an integrated low-temperature flue gas desulfurization and denitrification ammonia removal device which comprises an induced draft fan, a dry desulfurization system, an ammonia preparation system, ammonia removal denitrification equipment, a particulate matter recovery system and a compressed air system, wherein the dry desulfurization system, the ammonia preparation system and the ammonia removal denitrification equipment are sequentially connected to a flue gas main pipeline according to the flue gas airflow direction; the induced draft fan is arranged on the flue gas main pipeline behind the ammonia removal denitrification equipment; the ammonia removal denitrification equipment is additionally connected with the particulate matter recovery system; the compressed air system is respectively connected with a pulsed ash removal device in the ammonia removal denitrification equipment, dried powder fluidization equipment in the dry desulfurization system and a closed relief blocking valve at an ash outlet of the ammonia removal denitrification equipment through a connecting pipeline. Compared with the prior art, the device has the beneficial effects that the integrated desulfurization and denitrification ammonia removal efficiency is high, the denitrification mode is unique, the structural force of the equipment is advanced, the energy is saved, residual ammonia water in a gas purification process is fully recycled, and the waste heat is fully recycled.
Description
Technical field
The utility model relates to low-temperature flue gas innoxious process for treating field, relates in particular to a kind of low-temperature flue gas desulphurization denitration except ammonia integrated apparatus.
Background technology
NH
3-SCR method (selective catalytic reduction) denitration technology maturation, reliable, is used widely in power plant.Power-plant flue gas temperature is between 350 DEG C～400 DEG C, and the denitration efficiency under this temperature case can reach 90%, and because flue-gas temperature is high, SO under catalyst action
2change into SO
3amount little, SO
2impact on denitration efficiency is very little.Power plant generally adopts first denitration, flue gas waste heat recovery, rear low-temp desulfurization technique.
Coke-oven plant's coke oven flue EGT is generally between 180 DEG C～250 DEG C; SO
2content is generally 60～150mg/Nm
3, for the higher enterprise of organic sulfur content in feed coal, the SO in its coke oven flue waste gas
2content can reach 350mg/Nm
3; NO
xcontent is at 600～1200mg/Nm
3between; Oxygen content is lower, is about 6%; Water content changes with coke oven heat medium, while adopting coke-stove gas heating, is about 17.25%, while adopting mixed gas heating, is about 6.6%.For meeting coking industry to NO
xand SO
2concentration of emission requirement, must take desulphurization denitration measure to coke oven stack gases.
Coke oven flue EGT is lower, adopts conventional NH
3the denitration of-SCR method, its efficiency is only 50～70%, the NO after denitration
xconcentration cannot meet discharging standards requirement, has a large amount of the escaping of ammonia simultaneously, produces new atmosphere pollution.In this temperature range, SO
2under catalyst effect, very easily change into SO
3, SO
3with NH
3reaction generates ammonium sulfate, after ammonium sulfate deliquescence, is bonded in catalyst surface, not only reduces denitration efficiency, also can reduce catalyst service life.If add traditional sulfur removal technology before denitrification apparatus, because flue-gas temperature decreases, can further reduce denitration efficiency.Although the problems referred to above can solve by heating coke oven flue waste gas, can cause energy waste, increase once investment and operating cost simultaneously.
Summary of the invention
The utility model provides a kind of low-temperature flue gas desulphurization denitration except ammonia integrated apparatus, is applicable to flue-gas temperature and is greater than 180 DEG C, SO
2content is less than 150mg/Nm
3coke oven flue exhuast gas desulfurization denitration, denitration mode uniqueness, device structure form advanced person, fully recycles the remained ammonia in gas purification process, when high-efficiency desulfurization denitration, can control amount of ammonia slip lower than discharging standards value.
In order to achieve the above object, the utility model is realized by the following technical solutions:
A kind of low-temperature flue gas desulphurization denitration is except ammonia integrated apparatus, comprise air-introduced machine, dry method desulfuration system, ammonia preparation system, except ammonia denitration device, particle recovery system and compressed air system, described dry method desulfuration system, ammonia preparation system and access successively flue gas main pipeline by flue gas stream direction except ammonia denitration device, air-introduced machine is arranged on except on the flue gas main pipeline after ammonia denitration device, except ammonia denitration device connects particle recovery system in addition, compressed air system connects respectively except the pulse ash remover in ammonia denitration device by connecting pipe, dry powder fluidizing apparatus in dry method desulfuration system and except the airtight discharge blocking valve of ammonia denitration device ash hole.
Before described flue gas main pipeline, waste gas inlet place, coke oven chimney bottom both sides arranges waste gas inlet volume damper.
Described dry method desulfuration system is made up of dry powder storagetank, frequency conversion dosing equipment and dry powder fluidizing apparatus, and dry powder storagetank discharging opening is provided with frequency conversion dosing equipment, and dry powder fluidizing apparatus connects flue by desulphurization catalyst entrance.
Described ammonia preparation system is made up of tank used for storing ammonia, ammonia spraying evaporator, ammonia surge tank, ammonia-flue gas blender, desulphurization denitration is accessed except the flue after ammonia treatment by pipeline in the two ends of ammonia spraying evaporator, form loop, its pipeline being positioned at before ammonia spraying evaporator is separately established pipeline branch road connection ammonia-flue gas blender, and from other end access flue gas main pipeline.
Described ammonia preparation system and flue gas main pipeline junction are provided with ammonia-spraying grid, and it is also provided with static mixer along flow of flue gas direction front.
Described except ammonia denitration device employing pulse bag type dust collector version, bottom is ash silo, and airtight discharge blocking valve is established in ash silo outlet, cloth bag composite catalyst is established on ash silo top, cloth bag composite catalyst outer surface is high temperature resistant filter bag, and middle for removing ammonia catalyst layer, nexine is filtrate skeleton; Smoke inlet place, composite catalyst side establishes airflow-distribution board, and pulse ash remover is established at cloth bag composite catalyst top.
Described air-introduced machine is furnished with variable-frequency motor.
Described particle recovery system is made up of drag conveyor, chain bucket elevator and particle bunker, described drag conveyor is positioned at the below except ammonia denitration device ash bin discharge port external, its afterbody is by pipeline connection chain bucket elevator underfeed mouth, and chain bucket elevator top discharging opening connects particle bunker.
Described particle bunker below discharging opening is provided with screw push-pull valve.
Compared with prior art, the beneficial effects of the utility model are:
1) integration desulfurization denitration except ammonia efficiency high
This device operation principle is the SO2 in first dry removal flue gas, then adopts except ammonia catalyst carries out denitration and removes ammonia, and its desulfuration efficiency is higher than 90%, and denitration efficiency is higher than 90%, and ammonia react efficiency is higher than 98%.
2) denitration mode uniqueness, device structure form advanced person
Directly adopt except ammonia catalyst carries out denitration and remove ammonia simultaneously, except ammonia denitrification apparatus adopts pulse bag type dust collector version, high temperature resistant filter bag is with compound except ammonia catalyst, and filter bag is used for the NaHCO of filtering flue gas
3, Na
2cO
3, Na
2sO
3in particle and dust, prevent that dust and Particulate Pollution are except ammonia catalyst surface, when flue gas is through filter bag outer surface layer of particulate matter simultaneously, the SO in flue gas
2meeting and NaHCO
3and Na
2cO
3continue reaction, further remove SO
2, under low-sulfur environment, except ammonia catalyst still has very high denitration efficiency to low-temperature flue gas.
3) deashing is simple
Adopt pulse of compressed air purge mode to remove the particle of filter bag outer surface, not only can improve cloth bag efficiency of dust filtration, reduction system running resistance, the dust being mingled with except between ammonia catalyst granules can also blow off, improve except ammonia catalyst except ammonia efficiency and denitration efficiency, extending catalyst service life.
4) save the energy, reduce operating cost and once investment
Adopt desulphurization denitration except ammonia integral process, can be under coke oven flue waste gas worst cold case, directly efficient dry desulfurization, NO_x Reduction by Effective, except ammonia, does not need low temperature coke oven stack gases to take heating measure simultaneously, saves the energy, reduces operating cost and once investment.
5) fully recycle the remained ammonia in gas purification process
The concentration producing in employing gas purification ammonia still process workshop section is about 15%～18% remained ammonia as reducing agent, reduces pollution discharging substrate concentration outside coke-oven plant, reduces simultaneously and processes pollutant operating cost and once investment.
6) fully recycle waste heat
Ammonia evaporation and ammonia mix the coke oven flue waste gas all adopting after denitration, fully recycle the waste heat of stack gases, do not need to set up in addition to add heating agent, greatly save the energy.
Brief description of the drawings
Fig. 1 is the utility model process chart.。
Fig. 2 is except ammonia denitration device side view in the utility model.
Fig. 3 is cloth bag composite catalyst structural representation in the utility model.
In figure: 1a. air-introduced machine 1b. waste gas inlet volume damper 2a. frequency conversion dosing equipment 2b. dry powder fluidizing apparatus 2c. dry powder storagetank 3a. ammoniacal liquor basin 3b. ammoniacal liquor supply pump 3c. ammonia spraying evaporator 3d. ammonia surge tank 3e. ammonia-flue gas blender 3f. ammonia-spraying grid 3g. static mixer 4. is except ammonia denitration device 4a. cloth bag composite catalyst 4a-1. filter bag 4a-2. is except the airtight discharge blocking valve of ammonia catalyst layer 4a-3. filtrate skeleton 4b. pulse ash remover 4c. ash silo 4d. 4e. airflow-distribution board 5. air reservoir 6a. drag conveyor 6b. chain bucket elevator 6c. particle bunker 6d. screw push-pull valves
Detailed description of the invention
Below in conjunction with accompanying drawing, detailed description of the invention of the present utility model is described further:
See Fig. 1, the structural representation of a kind of low-temperature flue gas desulphurization denitration of the utility model except ammonia integrated apparatus, comprise air-introduced machine 1a, dry method desulfuration system, ammonia preparation system, except ammonia denitration device 4, particle recovery system and compressed air system, described dry method desulfuration system, ammonia preparation system and access successively flue gas main pipeline by flue gas stream direction except ammonia denitration device 4, air-introduced machine 1a is arranged on except on the flue gas main pipeline after ammonia denitration device 4, except ammonia denitration device 4 connects particle recovery system in addition, compressed air system connects respectively except the pulse ash remover 4b in ammonia denitration device 4 by connecting pipe, dry powder fluidizing apparatus 2b in dry method desulfuration system and except the airtight discharge blocking valve 4d of ammonia denitration device 4 ash holes.
Before described flue gas main pipeline, waste gas inlet place, coke oven chimney bottom both sides arranges waste gas inlet volume damper 1b.
Described dry method desulfuration system is made up of dry powder storagetank 2c, frequency conversion dosing equipment 2a and dry powder fluidizing apparatus 2b, dry powder storagetank 2c discharging opening is provided with frequency conversion dosing equipment 2a, and dry powder fluidizing apparatus 2b connects flue by desulphurization catalyst entrance.
Described ammonia preparation system is made up of tank used for storing ammonia 3a, ammonia spraying evaporator 3c, ammonia surge tank 3d, ammonia-flue gas blender 3e, desulphurization denitration is accessed except the flue after ammonia treatment by pipeline in the two ends of ammonia spraying evaporator 3c, form loop, its pipeline being positioned at before ammonia spraying evaporator 3c is separately established pipeline branch road connection ammonia-flue gas blender 3e, and from other end access flue gas main pipeline.
Described ammonia preparation system and flue gas main pipeline junction are provided with ammonia-spraying grid 3f, and it is also provided with static mixer 3g along flow of flue gas direction front.
The described ammonia denitration device 4 that removes adopts pulse bag type dust collector version, bottom is ash silo 4c, airtight discharge blocking valve 4d is established in ash silo 4c outlet, cloth bag composite catalyst 4a is established on ash silo top, cloth bag composite catalyst 4a outer surface is high temperature resistant filter bag 4a-1, middle for removing ammonia catalyst layer 4a-2, nexine is filtrate skeleton 4a-3; Smoke inlet place, composite catalyst 4a side establishes airflow-distribution board 4e, and cloth bag composite catalyst 4a establishes pulse ash remover 4b in top.
Described air-introduced machine 1a is furnished with variable-frequency motor.
Described particle recovery system is made up of drag conveyor 6a, chain bucket elevator 6b and particle bunker 6c, described drag conveyor 6a is positioned at the below except ammonia denitration device ash silo 4c discharging opening, its afterbody is by pipeline connection chain bucket elevator 6b underfeed mouth, and chain bucket elevator 6b top discharging opening connects particle bunker 6c.
Described particle bunker 6c below discharging opening is provided with screw push-pull valve 6d.
The operation principle that a kind of low-temperature flue gas desulphurization denitration of the utility model removes ammonia integrated apparatus is: according to fluidization principle, before denitration, first carry out dry desulfurization, the ammonia that the remained ammonia that adopts ammonia still process workshop section of coke-oven plant to produce is evaporated is as reducing agent, utilize cloth bag-except ammonia catalyst composite structure as dedusting and denitration means, when high-efficiency desulfurization denitration, can control amount of ammonia slip lower than discharging standards value.
The course of work that a kind of low-temperature flue gas desulphurization denitration of the utility model removes ammonia integrated apparatus is as follows:
1) low-temperature flue gas was first taked desulfurization measure before denitration, was stored in the NaHCO in dry powder storagetank 2c
3fine powder desulfurizing agent passes through, after compressed air and dry powder fluidizing apparatus 2b fluidisation, to spray into coke oven flue waste gas pipeline road by desulfurizing agent entrance; Fluidization NaHCO
3fine powder contacts with coke oven flue waste gas, and following chemical reaction occurs:
2NaHCO
3->Na
2CO
3+H
2O+CO
2；
Na
2CO
3+SO
2->Na
2SO
3+CO
2；
2NaHCO
3+SO
2->Na
2SO
3+H
2O+2CO
2。
Most NaHCO
3fine powder decomposes the Na that generation fineness is less, specific area is larger, activity degree is higher in hot flue gas
2cO
3, improve SO
2removal efficiency.
2) remained ammonia that concentration gas purification process ammonia still process being produced is 15～18% is piped in ammoniacal liquor basin 3a to be stored, and ammoniacal liquor basin 3a is also for stablizing denitrating system ammoniacal liquor flow and concentration.Ammoniacal liquor weight feed pump 3b sprays into ammonia spraying evaporator 3c by the ammoniacal liquor in ammoniacal liquor basin 3a and evaporates, after evaporation, the ammonia of certain pressure is introduced into ammonia surge tank 3d, then entering ammonia-flue gas blender 3e mixes with the exhaust after a part of denitration, mixed ammonia is evenly sprayed in the coke oven flue gas pipeline after desulfurization by ammonia-spraying grid 3f, static mixer 3g is set after ammonia-spraying grid 3e, ammonia is fully mixed with the oxynitrides in flue gas.
According to NO in coke oven flue waste gas
xcontent and NO
xconcentration of emission requirement, the quantity delivered of adjustable ammoniacal liquor supply pump 3b, to meet the requirement of denitrating system ammonia consumption.
The coke oven flue waste gas of the thermal source of ammonia spraying evaporator 3c after from denitration, makes full use of the waste heat of flue gas, does not need to set up in addition heating system.
Blender 3e plays dilution ammonia concentration, improves the effect of ammonia temperature, can make the ammonia spraying into better mix with flue gases of cock oven, and reduces because ammonia sprays into the flue-gas temperature decline causing.The medium mixing with ammonia adopts the stack gases through desulphurization denitration processing.
After simulation, the ammonia-spraying grid 3f of design is for evenly spraying into ammonia at coke oven flue waste gas, and static mixer 3g can make ammonia further fully mix with flue gases of cock oven.
3) seeing Fig. 2, is the side view except ammonia denitration device 4; Enter except ammonia denitration device 4 carries out denitration and remove ammonia with the even mixed coke oven flue waste gas of ammonia; Flue gas is from entering except ammonia denitration device 4 side bottoms, and the flue gas that removes ammonia through denitration flows out by removing ammonia denitration device 4 side roof parts or top; Enter the flue gas that removes ammonia denitration device 4 after the uniform air-flow of airflow-distribution board 4e, first contact with cloth bag composite catalyst 4a.Seeing Fig. 3, is cloth bag composite catalyst structural representation, and cloth bag composite catalyst 4a outer surface is high temperature resistant filter bag 4a-1, and middle for removing ammonia catalyst layer 4a-2, nexine is filtrate skeleton 4a-3.The Na generating in sweetening process
2sO
3fine powder, the NaHCO that participation is reacted
3and Na
2cO
3the dust containing in fine powder, flue gas is all filtered at cloth bag outer surface by filter bag 4a-1, and flue gas is mandatory through cloth bag under the suction function of air-introduced machine 1a, enters and passes except ammonia catalyst layer 4a-2; Except ammonia catalyst 4a-2 is fine particulate, the oxygen content in coke oven flue waste gas is lower, is about 6%, in low-sulfur, low-temperature flue gas environment, is removing under the catalytic action of ammonia catalyst NH
3preferential and NO
xetc. strong reacted, by NO
xbe reduced into N
2; Denitration efficiency under worst cold case is up to 90%, and ammonia also reacts with small part oxygen and generates N simultaneously
2and water, except the ammonia react efficiency under the effect of ammonia catalyst is up to 98%.
Filter bag 4a-1 is for filtering particle and dust, along with the increase of filter bag 4a-1 surface particles attachment, except ammonia denitration device 4 resistances also can increase, utilize compressed air, by pulse ash remover 4b, cloth bag composite catalyst 4a is carried out to pulse dust cleaning, the particle under removing falls into except ammonia denitration device 4 bottom ash silo 4c; Flue gas when the filter bag 4a-1 outer surface layer of particulate matter, residual SO in flue gas
2with NaHCO
3and Na
2cO
3fine powder continues to react, and further improves desulfuration efficiency.
Air-introduced machine 1a is furnished with variable-frequency motor.By air-introduced machine 1a is carried out to frequency control, and regulate waste gas inlet volume damper 1b, both can ensure the needed negative pressure value of the normal production of coke oven, also can ensure the needed force value of the normal work of desulfurizing and denitrifying process system.
Except establishing airflow-distribution board 4e in ammonia denitration device coke oven flue exhaust gas entrance place, by airflow uniform distribution to cloth bag composite catalyst 4a, because cloth bag recombination catalyst layer has certain resistance, there is certain all pressures effect simultaneously, be beneficial to device interior airflow field and temperature field uniform.
By pulse ash remover 4b reverse gas cleaning, not only can fall clearly the particle that filter bag 4a-1 outer surface adheres to, can remove the dust being mingled with except between ammonia catalyst granules simultaneously, improve service efficiency and service life except ammonia catalyst.
Airtight discharge blocking valve 4d is established in ash silo 4 outlets, prevents that extraneous air from being infiltrated by ash hole imprecision place, reduces flue-gas temperature.
4) remove ammonia overall process stack gases after treatment through desulphurization denitration and reach discharging standards, return to coke oven smoke stack emission; Except particle and the dust of collection in ammonia denitration device 4 pass through, after airtight discharge blocking valve 4d discharge, to be delivered to particle bunker 6c to store by drag conveyor 6a, chain bucket elevator 6b, and regularly outward transport is sold.
Compressed air is for removing ammonia denitration device deashing, the fluidization of desulfurizing agent dry powder, opening and closing airtight discharge blocking valve.
A kind of low-temperature flue gas desulphurization denitration of the present invention, except ammonia integral process, is applicable to flue-gas temperature and is greater than 180 DEG C, SO
2content is less than 150mg/Nm
3coke oven flue exhuast gas desulfurization denitration.
Claims (9)
1. a low-temperature flue gas desulphurization denitration is except ammonia integrated apparatus, it is characterized in that, comprise air-introduced machine, dry method desulfuration system, ammonia preparation system, except ammonia denitration device, particle recovery system and compressed air system, described dry method desulfuration system, ammonia preparation system and access successively flue gas main pipeline by flue gas stream direction except ammonia denitration device, air-introduced machine is arranged on except on the flue gas main pipeline after ammonia denitration device, except ammonia denitration device connects particle recovery system in addition, compressed air system connects respectively except the pulse ash remover in ammonia denitration device by connecting pipe, dry powder fluidizing apparatus in dry method desulfuration system and except the airtight discharge blocking valve of ammonia denitration device ash hole.
2. a kind of low-temperature flue gas desulphurization denitration according to claim 1, except ammonia integrated apparatus, is characterized in that, before described flue gas main pipeline, waste gas inlet place, coke oven chimney bottom both sides arranges waste gas inlet volume damper.
3. a kind of low-temperature flue gas desulphurization denitration according to claim 1 is except ammonia integrated apparatus, it is characterized in that, described dry method desulfuration system is made up of dry powder storagetank, frequency conversion dosing equipment and dry powder fluidizing apparatus, dry powder storagetank discharging opening is provided with frequency conversion dosing equipment, and dry powder fluidizing apparatus connects flue by desulphurization catalyst entrance.
4. a kind of low-temperature flue gas desulphurization denitration according to claim 1 is except ammonia integrated apparatus, it is characterized in that, described ammonia preparation system is made up of tank used for storing ammonia, ammonia spraying evaporator, ammonia surge tank, ammonia-flue gas blender, desulphurization denitration is accessed except the flue after ammonia treatment by pipeline in the two ends of ammonia spraying evaporator, form loop, its pipeline being positioned at before ammonia spraying evaporator is separately established pipeline branch road connection ammonia-flue gas blender, and from other end access flue gas main pipeline.
5. remove ammonia integrated apparatus according to a kind of low-temperature flue gas desulphurization denitration described in claim 1 or 4, it is characterized in that, described ammonia preparation system and flue gas main pipeline junction are provided with ammonia-spraying grid, and it is also provided with static mixer along flow of flue gas direction front.
6. a kind of low-temperature flue gas desulphurization denitration according to claim 1 is except ammonia integrated apparatus, it is characterized in that, described except ammonia denitration device employing pulse bag type dust collector version, bottom is ash silo, airtight discharge blocking valve is established in ash silo outlet, and cloth bag composite catalyst is established on ash silo top, and cloth bag composite catalyst outer surface is high temperature resistant filter bag, middle for removing ammonia catalyst layer, nexine is filtrate skeleton; Smoke inlet place, composite catalyst side establishes airflow-distribution board, and pulse ash remover is established at cloth bag composite catalyst top.
7. a kind of low-temperature flue gas desulphurization denitration according to claim 1, except ammonia integrated apparatus, is characterized in that, described air-introduced machine is furnished with variable-frequency motor.
8. a kind of low-temperature flue gas desulphurization denitration according to claim 1 is except ammonia integrated apparatus, it is characterized in that, described particle recovery system is made up of drag conveyor, chain bucket elevator and particle bunker, described drag conveyor is positioned at the below except ammonia denitration device ash bin discharge port external, its afterbody is by pipeline connection chain bucket elevator underfeed mouth, and chain bucket elevator top discharging opening connects particle bunker.
9. a kind of low-temperature flue gas desulphurization denitration according to claim 8, except ammonia integrated apparatus, is characterized in that, described particle bunker below discharging opening is provided with screw push-pull valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420109070.6U CN203764107U (en) | 2014-03-11 | 2014-03-11 | Integrated low-temperature flue gas desulfurization and denitrification ammonia removal device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420109070.6U CN203764107U (en) | 2014-03-11 | 2014-03-11 | Integrated low-temperature flue gas desulfurization and denitrification ammonia removal device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203764107U true CN203764107U (en) | 2014-08-13 |
Family
ID=51281355
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420109070.6U Expired - Lifetime CN203764107U (en) | 2014-03-11 | 2014-03-11 | Integrated low-temperature flue gas desulfurization and denitrification ammonia removal device |
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| CN (1) | CN203764107U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109266400A (en) * | 2018-09-30 | 2019-01-25 | 垣曲县五龙镁业有限责任公司 | A kind of oven gas negative pressure low-temp desulfurization deamination integrated apparatus |
| CN111389223A (en) * | 2020-04-20 | 2020-07-10 | 上海环境工程设计研究院有限公司 | Flue gas desulfurization and denitrification system and process |
-
2014
- 2014-03-11 CN CN201420109070.6U patent/CN203764107U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109266400A (en) * | 2018-09-30 | 2019-01-25 | 垣曲县五龙镁业有限责任公司 | A kind of oven gas negative pressure low-temp desulfurization deamination integrated apparatus |
| CN111389223A (en) * | 2020-04-20 | 2020-07-10 | 上海环境工程设计研究院有限公司 | Flue gas desulfurization and denitrification system and process |
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