CN203525549U - Equipment used for flue gas desulfurization and denitrification - Google Patents
Equipment used for flue gas desulfurization and denitrification Download PDFInfo
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- CN203525549U CN203525549U CN201320723142.1U CN201320723142U CN203525549U CN 203525549 U CN203525549 U CN 203525549U CN 201320723142 U CN201320723142 U CN 201320723142U CN 203525549 U CN203525549 U CN 203525549U
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- pipe
- flue gas
- absorption tower
- slurry
- denitrification
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- 239000003546 flue gas Substances 0.000 title claims abstract description 64
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 61
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 52
- 230000023556 desulfurization Effects 0.000 title abstract description 33
- 239000002002 slurry Substances 0.000 claims abstract description 91
- 239000001257 hydrogen Substances 0.000 claims abstract description 60
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 60
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 56
- 238000010521 absorption reaction Methods 0.000 claims abstract description 37
- 238000004519 manufacturing process Methods 0.000 claims abstract description 32
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 210000000481 breast Anatomy 0.000 claims description 15
- 230000001105 regulatory effect Effects 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 6
- 230000000740 bleeding effect Effects 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000000428 dust Substances 0.000 abstract description 13
- 230000008901 benefit Effects 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 3
- 239000007788 liquid Substances 0.000 abstract 1
- 239000003595 mist Substances 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 24
- 238000000034 method Methods 0.000 description 22
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 13
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 12
- 229910052757 nitrogen Inorganic materials 0.000 description 12
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 10
- 150000004767 nitrides Chemical class 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 8
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 8
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 7
- 239000002893 slag Substances 0.000 description 7
- 229910002089 NOx Inorganic materials 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 5
- 239000000571 coke Substances 0.000 description 5
- 239000008187 granular material Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000000746 purification Methods 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 239000002250 absorbent Substances 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 239000000284 extract Substances 0.000 description 4
- 239000010881 fly ash Substances 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- 238000010793 Steam injection (oil industry) Methods 0.000 description 3
- 229910052802 copper Inorganic materials 0.000 description 3
- 239000010949 copper Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Inorganic materials O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 description 3
- 229910017464 nitrogen compound Inorganic materials 0.000 description 3
- 150000002830 nitrogen compounds Chemical class 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 241001062472 Stokellia anisodon Species 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- ZWWCURLKEXEFQT-UHFFFAOYSA-N dinitrogen pentaoxide Chemical compound [O-][N+](=O)O[N+]([O-])=O ZWWCURLKEXEFQT-UHFFFAOYSA-N 0.000 description 2
- WFPZPJSADLPSON-UHFFFAOYSA-N dinitrogen tetraoxide Chemical compound [O-][N+](=O)[N+]([O-])=O WFPZPJSADLPSON-UHFFFAOYSA-N 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000001272 nitrous oxide Substances 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- MGWGWNFMUOTEHG-UHFFFAOYSA-N 4-(3,5-dimethylphenyl)-1,3-thiazol-2-amine Chemical compound CC1=CC(C)=CC(C=2N=C(N)SC=2)=C1 MGWGWNFMUOTEHG-UHFFFAOYSA-N 0.000 description 1
- DDFHBQSCUXNBSA-UHFFFAOYSA-N 5-(5-carboxythiophen-2-yl)thiophene-2-carboxylic acid Chemical group S1C(C(=O)O)=CC=C1C1=CC=C(C(O)=O)S1 DDFHBQSCUXNBSA-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229940095054 ammoniac Drugs 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- PRORZGWHZXZQMV-UHFFFAOYSA-N azane;nitric acid Chemical compound N.O[N+]([O-])=O PRORZGWHZXZQMV-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- -1 can arrive 90% Substances 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000006184 cosolvent Substances 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- LZDSILRDTDCIQT-UHFFFAOYSA-N dinitrogen trioxide Chemical compound [O-][N+](=O)N=O LZDSILRDTDCIQT-UHFFFAOYSA-N 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 235000003891 ferrous sulphate Nutrition 0.000 description 1
- 239000011790 ferrous sulphate Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 238000006902 nitrogenation reaction Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model relates to the field of purifying equipment and discloses equipment used for flue gas desulfurization and denitrification. The equipment used for flue gas desulfurization and denitrification comprises an air intake pipe, a hydrogenation pipe, a first multi-purpose reactor, an absorption tower, a second multi-purpose reactor, a circulation slurry pool, a hydrogen production tank, a steam temperature control device, a slurry discharge device, a slurry liquid circulation device, a gassing pipeline, a chimney pipeline and a mist eliminator. The equipment used for flue gas desulfurization and denitrification has the advantages that the structure is novel, and the effects of desulfurization and denitrification, and dust removal on flue gas produced by burning are good.
Description
Technical field
The utility model relates to air cleaning facility field, and especially a kind of flue gas producing for purified industrial burning makes the equipment of flue gas desulfuration and denitrification.
Background technology
The industrial smoke that industrial fuel burning produces mainly refers to a large amount of flue gases and the dust that the burning of Industrial Boiler produces, in China, what SO2 mainly discharged from fired coal combustion accounts for 90%, NOx90% is from fuel combustion, in Thermal Power Enterprises and metal smelt enterprise production process, all can produce a large amount of flue gases, so desulfurization removing nitric is that China administers the main target that pollution that caused by coal burning improves atmospheric environment.For example the steel mill in metal smelt, includes oxysulfide, nitrogen oxide, carbide slag and other waste residue dust etc. in the flue gas of its discharge; In the flue gas that firepower electrical plant is discharged, include carbide, oxysulfide, nitrogen oxide and flyash etc.
Purifying industrial smoke is mainly denitrogenation, desulfurization and dedusting at present, and desulfurization and dedusting are all generally to adopt traditional water to drench method.After burning, flue-gas denitrification is the important method of controlling NOx discharge, NOx in most of flue gas processes by this method, after existing burning, flue-gas denitrification desulfur technology has following several: (1) combined method, with the de-SO2(FGD of limestone-gypsum method wet type) and the technology that combines of the de-NOx of selective catalytic reduction (SCR), Germany, Japan, the national majority such as the U.S. is adopted in this way, in this combination technique, wet desulphurization efficiency is high, reach 90%～98%, in this combination technique, with ammonia, reduce denitrogenation, shortcoming is that the catalyst maintenance of denitrogenation is cumbersome, do not want the different nitrogen that adds.(2) electronic beam method (EBA), electronic beam method is to utilize the high energy particle that electron accelerator produces to irradiate, make its SO2 and NOx oxidation generate sulfuric acid and nitric acid, generate sulfate of ammoniac and nitric acid ammonia with the ammonia react adding again, the advantage of electronic beam method smoke treatment is with a process energy while desulfurization removing nitric, and removal efficiency is high, without catalyst, so there is not catalyst poisoning, affect the problem in service life, device structure is simple, flue gas condition is changed to strong adaptability, easily control, the deficiency existing is that power consumption is large, the operating cost accounting for is thus very high, gas radiation device is not also suitable for large-scale application system, still there is discharge nitrogen in the flue gas after processing, the possibility of sulfuric acid and nitrous oxide.(3) active coke absorption method, desulfurization and denitrogenation when carrying out flue gas by activated coke, SO2 is the micropore catalytic adsorption effect by activated coke, generating sulfuric acid is stored in coke micropore, NOx is under the condition of ammonification, catalytic action generation water and nitrogen through activated coke enter atmosphere again, advantage is that desulfurization degree is high, (100～200 ℃) can obtain high denitrification percent (80%) at low temperatures, thereby do not need heat riser, water not in process, without treating apparatus, there is no secondary pollution problem, weak point is the adsorbent attrition that has been in operation, use cost is high, adsorbance is little, when in flue gas, NOx content is high, adsorbent consumption is many, consume large, equipment volume is huge, so apply not extensive.Equipment or the method at present with desulphurization and denitrification functions are mainly divided into two kinds simultaneously, a kind of as China Patent Publication No. be " CN103041688A " " a kind of method of simultanously desulfurizing and denitrification producing ammonium sulfate byproduct ", or as China Patent Publication No. be " the desulfurization removing nitric deduster " of " CN103028301A ", all by ammonia nitrogen and desulfurization, flue-gas temperature is very high, generally all surpass 100 degrees Celsius, to adopt exactly water to drench method the waste residue dust removal in flue gas and cooling best bet, during actual use, nitrogen is very easily water-soluble, therefore adopt ammonia nitrogen and desulfurization not only to need complicated equipment and process, and very difficult very high denitrification percent and the desulfurization degree of simultaneously obtaining.Another as China Patent Publication No. be a kind of " CN102078760A " " flue gas desulfuration and denitrification method ", utilize H2O2 nitrogen and desulfurization, its advantage is that denitrification percent is high, weak point is that H2O2 is used as a kind of absorbent, desulfurization degree is undesirable, H2O2 needs ceaselessly from outside, to add absorption tower, and while using on a large scale, not only cost of material is high, and operation and maintenance is all not inconvenient.
Summary of the invention
Goal of the invention of the present utility model is simultanously desulfurizing and denitrification to be purified to the deficiency existing in order to solve the equipment of above-mentioned existing flue gas desulfuration and denitrification, a kind of novel structure is provided, can to flue gas, carry out desulfurization removing nitric purified treatment simultaneously, and denitrification percent and desulfurization degree are high, the equipment for flue gas desulfuration and denitrification that use cost is low.
In order to realize above-mentioned object, the utility model has adopted following technical scheme:
For an equipment for flue gas desulfuration and denitrification, comprise air inlet pipe, hydrogenation pipe, the first multinomial reactor, absorption tower, the second multinomial reactor, circulation slurry pool, hydrogen manufacturing groove, steam temperature regulating device, slip discharger, slurries EGR, outlet pipe, chimney breast and demister; Air inlet pipe is connected with top, absorption tower, and the first multinomial reactor is arranged in air inlet pipe, and the second multinomial reactor is arranged in absorption tower, the bottom of circulation slurry pool in absorption tower; The inlet end of outlet pipe is connected on absorption tower, and its position is between recycle slurry material pond and the second multinomial reactor, and the outlet side of outlet pipe is connected on the bottom of chimney breast; Demister is arranged in chimney breast, and the top of the outlet side of the position of demister in outlet pipe; Slip discharger is connected with circulation slurry pool; Hydrogen manufacturing groove communicates with circulation slurry pool, and the venthole of steam temperature regulating device is in hydrogen manufacturing groove; Slurries EGR comprises slip charging aperture, slurry circulating pump and slurry pipe, slurry circulating pump and slip charging aperture are connected on slurry pipe, one end of slurry pipe connects hydrogen manufacturing groove, the other end of slurry pipe is in absorption tower, and slurry pipe is connected in the top in the second multinomial reactor, position on absorption tower; The import of hydrogenation pipe is connected on hydrogen manufacturing groove, and the outlet of hydrogenation pipe is connected in air inlet pipe, and hydrogenation pipe was connected in position in air inlet pipe before the first multinomial reactor, and hydrogenation pipe is provided with the control valve of bleeding.
As preferably, for the equipment of flue gas desulfuration and denitrification, also comprise cage, cage is arranged in the absorption tower between the second multinomial reactor and circulation slurry pool, and the position of the inlet end of outlet pipe is between recycle slurry material pond and cage; Further, described cage is up big and down small taper ring, cage top lateral wall and absorption tower madial wall are fixedly linked, the position of outlet pipe inlet end on absorption tower is between cage top and cage bottom, the position of the structure of cage and outlet pipe inlet end cooperatively interacts, and has guaranteed the purifying rate of flue gas.
As preferably, the first multinomial reactor is identical with the second multinomial structure of reactor, and by a plurality of taper rings with the combination of a plurality of cone block is equipped forms, the vertex of a cone of cone block is facing to taper ring, and the bottom surface diameter of cone block is not less than taper ring osculum diameter; Thereby the first multinomial reactor of said structure can make nitride in air contact fully with hydrogen the efficiency that improves reaction with the second multinomial reactor, thereby can also make sulfide improve the efficiency of reacting with sufficient contact of water and hydrogen.
As preferably, demister comprises water shower device and the 3rd multinomial reactor, air is by the multinomial reactor in chimney breast and carry out water pouring processing, air through purifying is carried out demist cooling and again filtered, hydrogen carries out last purification to remaining trace nitrogen compound in the air through purifying, remaining micro-dust granules is swept away by water, through the air of final purification, by chimney breast, is discharged.
Adopted a kind of equipment for flue gas desulfuration and denitrification of above-mentioned technical scheme, by hydrogenation pipe extract in hydrogen manufacturing groove, be mixed with hydrogen air to air inlet pipe, flue gas enters air inlet pipe and just reacts with hydrogen, by hydrogen, flue gas is carried out to denitrogenation processing, and by the first multinomial reactor, with the second multinomial reactor, flue gas is contacted closely with hydrogen, accelerated the speed of reaction, by slurries EGR to flue gas cool-down desulfurization process, and make solid-state dust granules and sulfide chance slurries fall into circulation slurry pool, further by the slurries in circulation slurry pool, carry out desulfurization processing, the hydrogen that carries out denitrogenation processing is spontaneous in hydrogen manufacturing groove due to desulfurization processing, the integrated treatment of its desulfurization removing nitric is very environmental protection and orderly, the quantity of processing the hydrogen producing by desulfurization can control by steam temperature regulating device, the mode of adjusting temperature by steam injection is controlled quantity and the progress that hydrogen produces, additionally add the method for H2O2 to have the different of essence from existing needs, not only environmental protection production cost is low, and safeguard very convenient, by circulation slurry pool, bleed on slip discharger and the hydrogenation pipe cooperation of control valve, use safety very.In sum, this advantage for the equipment of flue gas desulfuration and denitrification is novel structure, and flue gas desulfuration and denitrification and dust removal effect that burning is produced are good, to the desulfurization degree of flue gas, can arrive 98%, to the denitrification percent of flue gas, can arrive 90%, the dust clarifier of fine particle PM2.5 is reached to 95%.
Accompanying drawing explanation
Fig. 1: the structural representation of the utility model embodiment 1.
Fig. 2: the structural representation of the utility model embodiment 2.
The specific embodiment
Below in conjunction with Fig. 1 and Fig. 2, the specific embodiment of the present utility model is made a detailed explanation.
Embodiment 1
A kind of equipment for flue gas desulfuration and denitrification as shown in Figure 1, comprises air inlet pipe 1, the multinomial reactor 3 of hydrogenation pipe 2, first, the multinomial reactor 6 in absorption tower 4, second, cage 11, circulation slurry pool 7, hydrogen manufacturing groove 10, steam temperature regulating device 9, slip discharger 8, slurries EGR 5, outlet pipe 12, chimney breast 13 and demister 14.
Air inlet pipe 1 is connected with 4 tops, absorption tower, and the first multinomial reactor 3 is arranged in air inlet pipe 1, and the second multinomial reactor 6 is arranged in absorption tower 4, and circulation slurry pool 7 is 4 bottom in absorption tower.Cage 11 is arranged in the absorption tower 4 between the second multinomial reactor 6 and circulation slurry pool 7.The inlet end of outlet pipe 12 is connected on absorption tower 4, its position is between recycle slurry material pond 7 and cage 11, specifically cage 11 is up big and down small taper rings, cage 11 top lateral walls and absorption tower 4 madial walls are fixedly linked, the position of outlet pipe 12 inlet ends on absorption tower 4 is between cage 11 tops and cage 11 bottoms, the position of the structure of cage 11 and outlet pipe 12 inlet ends cooperatively interacts, and has guaranteed the purifying rate of flue gas.The outlet side of outlet pipe 12 is connected on the bottom of chimney breast 13, and demister 14 is arranged in chimney breast 13, and the top of the outlet side of the position of demister 14 in outlet pipe 12.
In circulation slurry pool 7, be provided with slurries 71, slip discharger 8 is connected with circulation slurry pool 7, and slurries 71 are mainly mixed by blast furnace slag or copper smelter slag or flyash and water, and the concentration of slurries 71 is between 5%-20%.Hydrogen manufacturing groove 10 is by communicating with circulation slurry pool 7, slurries 71 are in piping flows into hydrogen manufacturing groove 10, the venthole of steam temperature regulating device 9 is in hydrogen manufacturing groove 10, and the temperature of controlling hydrogen manufacturing groove 10 interior slurries 71 to the interior steam injection of hydrogen manufacturing groove 10 by steam temperature regulating device 9 remains between 45-80 degree Celsius.
Slurries EGR 5 comprises slip charging aperture 53, slurry circulating pump 52 and slurry pipe 51, slurry circulating pump 52 and slip charging aperture 53 are all connected on slurry pipe 51, one end of slurry pipe 51 connects hydrogen manufacturing groove 10, the other end of slurry pipe 51 is in absorption tower 4, and slurry pipe 51 is connected in the top in the second multinomial reactor 6, position on absorption tower 4, slurry circulating pump 52 is controlled slurries 71 circulation successively between absorption tower 4, circulation slurry pool 7, hydrogen manufacturing groove 10 and slurry pipe 51.The import of hydrogenation pipe 2 is connected in the top of hydrogen manufacturing groove 10, the outlet of hydrogenation pipe 2 is connected in air inlet pipe 1, and hydrogenation pipe 2 was connected in position in air inlet pipe 1 before the first multinomial reactor 3, hydrogenation pipe 2 is provided with the control valve 2 of bleeding, the control valve 2 of bleeding is controlled the amount of hydrogen that extracts from hydrogen manufacturing groove 10, in air inlet pipe 1, by volume densimeter hydrogen is the 0.01-3% of air, the concrete amount of hydrogen is adjusted by the nitrogen content and the volume that enter flue gas in air inlet pipe 1, be the extraction amount of hydrogen actual be that the content of nitride in flue gas determines, in flue gas, the hydrogen of the high input of the content of nitride is just many, above-mentioned nitride mainly refers to nitrogen oxide, as nitrous oxide, nitric oxide, nitrogen dioxide, nitrogen trioxide, dinitrogen tetroxide and dinitrogen pentoxide etc.
Above-mentioned the first multinomial reactor 3 is identical with the second multinomial reactor 6 structures, by a plurality of taper rings and the equipped formation of a plurality of cone block combination, the vertex of a cone of cone block is facing to taper ring, the bottom surface diameter of cone block is not less than taper ring osculum diameter, and cone block is generally pressed the center in absorption tower 4 by gripper shoe.The combination of taper ring and cone block is various, can freely select.Thereby the first multinomial reactor 3 can make nitride in air contact fully with hydrogen the efficiency that improves reaction with the second multinomial reactor 6, thereby can also make sulfide improve the efficiency of reacting with sufficient contact of water and hydrogen.
During use, the temperature of flue gas is different, generally between 100-500 degree Celsius, press the temperature gas that by hydrogenation pipe 2 extracts hydrogen in corresponding hydrogen manufacturing groove 10 different from nitrogenate input quantity of flue gas, when general flue-gas temperature is high, the gas ratio of suction is low, because the efficiency that the high hydrogen of flue-gas temperature reacts with nitride is just high.The flue gas of high temperature mixes with the air of hydrogen in hydrogenation pipe 2, through the first multinomial reactor 3, nitride in flue gas and hydrogen mix fully to contact and react and produce nitrogen G&W, flue gas continues by the second multinomial reactor 6, nitride in flue gas and hydrogen mix fully to contact and continue reaction and produce nitrogen G&W, slurries 71 in slurry pipe 51 on absorption tower the 4 interior flue gases to high temperature lower the temperature, solid-state dust granules and sulfide are met slurries 71 after cure things and are carried out desulphurization reaction, solid-state dust granules and sulfide fall into the circulation slurry pool 7 of 4 bottoms, absorption tower, sulfide falls into the interior dissolving of circulation slurry pool 7 and with further and slurries 71, chemical reactions occurs, nitride is mainly sulfur dioxide, sulfur dioxide is dissolved in slurries 71 and reaction generation dilute sulfuric acid completes flue gas desulfurization, dilute sulfuric acid makes slurries 71 be acid, pH value is between 4.5-6.Slurries 71 are in piping flows into hydrogen manufacturing groove 10, by steam temperature regulating device 9, to hydrogen manufacturing groove 10 steam injections, slurries 71 being carried out to heat treatment remains between 45-80 degree Celsius the temperature of the interior slurries 71 of hydrogen manufacturing groove 10, dilute sulfuric acid reacts with the active metal in slurries 71 and generates hydrogen, active metal is the iron in blast furnace slag or copper smelter slag, or the aluminium in flyash.Hydrogen is transported in air inlet pipe 1 by hydrogenation pipe 2, is cycled to repeat above-mentioned action.The outlet pipe 12 of the air of processing through desulfurization removing nitric between cage 11 tops and cage 11 bottoms discharged and delivered in chimney breast 13, through the demister 14 in chimney breast 13, directly discharges.
Sulfide in flue gas has reacted desulfurization with slurries 71, sediment together with slurries 71 by 8 recyclings of slip discharger, dust contacts the first multinomial reactor 3 and the second multinomial reactor 6 meets slurries 71 and depositing in water enters to circulate in slurry pool 7, also by slip discharger 8, reclaimed, nitride and sulfide desulfurization and the hydrogen reaction that produces generates nitrogen G&W, water mixes with slurries 71, nitrogen is directly discharged, in the air through purification of discharging, comprised hydrogen and the nitrogen through cooling, by the above-mentioned equipment for flue gas desulfuration and denitrification, to the desulfurization degree of flue gas, can arrive 98%, to the denitrification percent of flue gas, can arrive 90%, dust clarifier to fine particle PM2.5 reaches 95%.Owing to containing hydrogen in the air entering in outlet pipe 12, therefore from outlet pipe 12 to all positions between chimney breast 13 tops, hydrogen is remaining trace nitrogen compound in eliminating air all, efficiencies of nitrogen removal is very good, hydrogen also can be done reduction reaction to the sulfide in slurries, is convenient to it and collects.Use after a period of time, by slip discharger 8, take out and comprise fixing sedimentary slurries, and inject slurries 71 by slip charging aperture 53.
By steam temperature regulating device 9, can control the temperature of the interior slurries 71 of hydrogen manufacturing groove 10, can control the progress of hydrogen manufacturing simultaneously.In order to accelerate dissolution velocity, can in slurries 71, add flux, cosolvent is ammonium fluoride, in order to accelerate the reaction speed of sulfide and to be convenient to follow-up sediment, extract, can add mixed catalyst to make, mixed catalyst is comprised of pyrolusite and the ferrous sulfate of MnO2 grade >=35%.
The demister of the water-flushed zone wire netting that above-mentioned demister 14 is this area routines.
Slurries 71 in above-mentioned circulation slurry pool 7 and hydrogen manufacturing groove 10 are equivalent to absorbent.The inventor of this patent has applied for multinomially take respectively blast furnace slag, copper smelter slag and flyash and adding water and be modulated into slurries as absorbent, for absorbing the sulfur dioxide of flue gas, by special absorbent, carry out the technique of desulfurization, the patent No. comprises ZL200710079615.8, ZL201010123046.4, ZL201010137024.3.The equipment of the flue gas desulfuration and denitrification of this patent is on the basis of aforementioned invention, and under the prerequisite that does not significantly increase cost, through suitable improvement, the equipment of just having realized has the function of desulfurization removing nitric and dedusting simultaneously, and desulfurization degree and denitrification percent all very high.
Embodiment 2
A kind of equipment for flue gas desulfuration and denitrification as shown in Figure 2, other structure and parameter is identical with embodiment 1, difference is only that demister 14 consists of water shower device 15 and the 3rd multinomial reactor 16, the top of water shower device 15 positions in the 3rd multinomial reactor 16, the structure of the 3rd multinomial reactor 16 is identical with the first multinomial reactor 3, the 3rd multinomial reactor 16 is set can further carry out demist cooling and again filter the air through purifying, hydrogen carries out last purification to remaining trace nitrogen compound in the air through purifying, remaining micro-dust granules is swept away by water, air through final purification is discharged by chimney breast, nitric efficiency is better.
Claims (5)
1. for an equipment for flue gas desulfuration and denitrification, it is characterized in that comprising air inlet pipe, hydrogenation pipe, the first multinomial reactor, absorption tower, the second multinomial reactor, circulation slurry pool, hydrogen manufacturing groove, steam temperature regulating device, slip discharger, slurries EGR, outlet pipe, chimney breast and demister; Air inlet pipe is connected with top, absorption tower, and the first multinomial reactor is arranged in air inlet pipe, and the second multinomial reactor is arranged in absorption tower, the bottom of circulation slurry pool in absorption tower; The inlet end of outlet pipe is connected on absorption tower, and its position is between recycle slurry material pond and the second multinomial reactor, and the outlet side of outlet pipe is connected on the bottom of chimney breast; Demister is arranged in chimney breast, and the top of the outlet side of the position of demister in outlet pipe; Slip discharger is connected with circulation slurry pool; Hydrogen manufacturing groove communicates with circulation slurry pool, and the venthole of steam temperature regulating device is in hydrogen manufacturing groove; Slurries EGR comprises slip charging aperture, slurry circulating pump and slurry pipe, slurry circulating pump and slip charging aperture are connected on slurry pipe, one end of slurry pipe connects hydrogen manufacturing groove, the other end of slurry pipe is in absorption tower, and slurry pipe is connected in the top in the second multinomial reactor, position on absorption tower; The import of hydrogenation pipe is connected on hydrogen manufacturing groove, and the outlet of hydrogenation pipe is connected in air inlet pipe, and hydrogenation pipe was connected in position in air inlet pipe before the first multinomial reactor, and hydrogenation pipe is provided with the control valve of bleeding.
2. a kind of equipment for flue gas desulfuration and denitrification according to claim 1, characterized by further comprising cage, cage is arranged in the absorption tower between the second multinomial reactor and circulation slurry pool, and the position of the inlet end of outlet pipe is between recycle slurry material pond and cage.
3. a kind of equipment for flue gas desulfuration and denitrification according to claim 2, it is characterized in that described cage is up big and down small taper ring, cage top lateral wall and absorption tower madial wall are fixedly linked, and the position of outlet pipe inlet end on absorption tower is between cage top and cage bottom.
4. a kind of equipment for flue gas desulfuration and denitrification according to claim 1, it is characterized in that the first multinomial reactor is identical with the second multinomial structure of reactor, by a plurality of taper rings and the equipped formation of a plurality of cone block combination, the vertex of a cone of cone block is facing to taper ring, and the bottom surface diameter of cone block is not less than taper ring osculum diameter.
5. a kind of equipment for flue gas desulfuration and denitrification according to claim 1, is characterized in that demister comprises water shower device and the 3rd multinomial reactor.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320723142.1U CN203525549U (en) | 2013-11-13 | 2013-11-13 | Equipment used for flue gas desulfurization and denitrification |
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| CN201320723142.1U CN203525549U (en) | 2013-11-13 | 2013-11-13 | Equipment used for flue gas desulfurization and denitrification |
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| CN203525549U true CN203525549U (en) | 2014-04-09 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105413439A (en) * | 2015-11-19 | 2016-03-23 | 史汉祥 | Device for desulfurization and denitrification of flue gas |
| CN105435617A (en) * | 2015-11-19 | 2016-03-30 | 史汉祥 | Device for flue gas desulfurization and denitrification |
-
2013
- 2013-11-13 CN CN201320723142.1U patent/CN203525549U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105413439A (en) * | 2015-11-19 | 2016-03-23 | 史汉祥 | Device for desulfurization and denitrification of flue gas |
| CN105435617A (en) * | 2015-11-19 | 2016-03-30 | 史汉祥 | Device for flue gas desulfurization and denitrification |
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