CN114377532A - A integration processing apparatus that is used for rock wool cupola flue gas desulfurization denitration - Google Patents
A integration processing apparatus that is used for rock wool cupola flue gas desulfurization denitration Download PDFInfo
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- CN114377532A CN114377532A CN202111507070.2A CN202111507070A CN114377532A CN 114377532 A CN114377532 A CN 114377532A CN 202111507070 A CN202111507070 A CN 202111507070A CN 114377532 A CN114377532 A CN 114377532A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 239000003546 flue gas Substances 0.000 title claims abstract description 60
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 35
- 230000023556 desulfurization Effects 0.000 title claims abstract description 35
- 239000011490 mineral wool Substances 0.000 title claims abstract description 10
- 230000010354 integration Effects 0.000 title description 2
- 230000003647 oxidation Effects 0.000 claims abstract description 42
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 42
- 230000001590 oxidative effect Effects 0.000 claims abstract description 24
- 239000007800 oxidant agent Substances 0.000 claims abstract description 23
- 238000005192 partition Methods 0.000 claims abstract description 16
- 239000002002 slurry Substances 0.000 claims abstract description 8
- 238000005507 spraying Methods 0.000 claims abstract description 7
- 239000000498 cooling water Substances 0.000 claims abstract description 6
- 238000009792 diffusion process Methods 0.000 claims description 11
- 238000007789 sealing Methods 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 5
- 239000000919 ceramic Substances 0.000 claims description 4
- 230000008602 contraction Effects 0.000 claims 3
- 238000010276 construction Methods 0.000 claims 1
- 230000003009 desulfurizing effect Effects 0.000 abstract description 6
- 239000006185 dispersion Substances 0.000 abstract description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 35
- 239000000428 dust Substances 0.000 description 13
- 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 8
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 8
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 8
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 description 6
- 239000002893 slag Substances 0.000 description 6
- 239000000779 smoke Substances 0.000 description 6
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- ZWWCURLKEXEFQT-UHFFFAOYSA-N dinitrogen pentaoxide Chemical compound [O-][N+](=O)O[N+]([O-])=O ZWWCURLKEXEFQT-UHFFFAOYSA-N 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 4
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical group [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 3
- 239000000920 calcium hydroxide Substances 0.000 description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 2
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 2
- 235000010261 calcium sulphite Nutrition 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 1
- 239000005708 Sodium hypochlorite Substances 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007123 defense Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000012286 potassium permanganate Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/76—Gas phase processes, e.g. by using aerosols
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Dispersion Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses an integrated treatment device for desulfurization and denitrification of rock wool cupola flue gas, which comprises an oxidation tower and a desulfurization tower, wherein the bottoms of the oxidation tower and the desulfurization tower are communicated; a nozzle is arranged above the tapered pipe and used for spraying cooling water into the first inner cavity; an oxidant ejector is arranged in the tapered pipe; the vortex device comprises a partition plate and a vortex tube, wherein the partition plate is arranged in the first inner cavity, the vortex tube is positioned on the lower side of the partition plate, the vortex tube comprises an inlet tube and an outlet tube, the inlet tube is connected to the partition plate and upwards penetrates through the partition plate, and the outlet tube downwards extends; and a desulfurizer sprayer is arranged in the second inner cavity of the desulfurizing tower and is used for spraying alkaline slurry into the second inner cavity. In this application, utilize taper pipe and swirler, not only can improve the dispersion homogeneity of oxidant in the flue gas, improve oxidation efficiency, can also avoid the escape of oxidant.
Description
Technical Field
The invention relates to an integrated treatment device for desulfurization and denitrification of flue gas of a rock wool cupola furnace.
Background
In the production process of rock wool, the cupola furnace utilizes the heat energy generated by coke combustion to melt various raw materials, and a large amount of flue gas containing pollutants such as sulfur dioxide, nitrogen oxide, particulate matters and the like is generated in the furnace. The main fuel in the cupola is coke, the main pollutant components in the generated smoke are similar to those of a coal-fired boiler of a power station, but the treatment of the smoke pollution of the cupola used for producing rock wool is obviously lagged, and the pollution has important influence on the quality of the environmental air, so that the purification treatment of the smoke of the cupola is an important measure for winning the blue-sky defense.
At present, the treatment technology for rock wool cupola flue gas is mainly introduced from the flue gas treatment technology of a power station boiler or an industrial boiler, single desulfurization, denitration and dust removal transformation are basically adopted, and the whole pollutant treatment facility occupies a large area and has high energy consumption. How to realize the high-efficiency and economic cooperative integrated treatment of multiple pollutants is the key research point at present.
Disclosure of Invention
In order to solve the problems, the invention provides an integrated treatment device for desulfurization and denitrification of rock wool cupola flue gas, which comprises an oxidation tower and a desulfurization tower, wherein the bottom of the oxidation tower and the bottom of the desulfurization tower are communicated, the oxidation tower and the desulfurization tower both extend in the vertical direction, a flue gas inlet is formed in the top of the oxidation tower, a flue gas outlet is formed in the top of the desulfurization tower, a tapered pipe and a swirler are installed in a first inner cavity of the oxidation tower, and the tapered pipe is positioned above the swirler; a nozzle is arranged above the tapered pipe and used for spraying cooling water into the first inner cavity; an oxidant ejector is arranged in the tapered pipe;
the vortex device comprises a partition plate arranged in a first inner cavity and a plurality of vortex tubes, wherein the vortex tubes are positioned at the lower side of the partition plate, each vortex tube comprises an inlet tube and an outlet tube, the inlet tube is connected to the partition plate and upwards penetrates through the partition plate, and the outlet tubes extend downwards; and a desulfurizer sprayer is arranged in the second inner cavity of the desulfurization tower and is used for spraying alkaline slurry into the second inner cavity so as to perform semi-dry desulfurization and denitrification in the second inner cavity.
This application is when operation, and cooling water spouts into first inner chamber through the nozzle, carries out the humidification cooling to the flue gas, and the flue gas mixes with the strong oxidant of oxidant sprayer spun when the awl reducing pipe, and strong oxidant oxidizes the nitrogen oxide in the flue gas, and the flue gas utilizes swirl effect to improve the mixed effect of flue gas and strong oxidant when passing through the swirler, has further improved the oxidation effect to nitrogen oxide in the flue gas, with low valence state nitrogen oxide oxidation to nitrogen pentoxide.
When the oxidant is used for oxidizing the low-valence nitrogen oxide, sulfur dioxide is also oxidized to generate sulfur trioxide. The flue gas after being oxidized enters a second inner cavity of the desulfurizing tower, and the alkaline desulfurizing liquid sprayed from the desulfurizing agent sprayer absorbs sulfur dioxide and sulfur trioxide in the flue gas to generate sulfite and sulfate, and simultaneously absorbs dinitrogen pentoxide to generate nitrate. The flue gas outlet of the desulfurizing tower is connected with a bag-type dust remover, and when the flue gas passes through the bag-type dust remover, dust in the flue gas and sulfite, sulfate and nitrate adsorbed on the dust are removed by a bag.
In this application, utilize taper pipe and swirler, not only can improve the dispersion homogeneity of oxidant in the flue gas, improve oxidation efficiency, can also avoid the escape of oxidant, but the oxidant preferred adopts ozone, also can adopt hydrogen peroxide solution, sodium hypochlorite or potassium permanganate etc.. The nitrogen oxide in the flue gas is converted into nitrogen dioxide, the converted nitrogen dioxide is taken as a reference, and the addition amount of ozone is determined according to the nitrogen oxide removal efficiency required by a project and is usually 1.1-2.5 times of the mole number of the nitrogen dioxide.
Specifically, every vortex tube all is including being the annular vortex portion of spiral, and the both ends of this vortex portion are above-mentioned import pipe and outlet pipe respectively, and the central axis of this vortex portion extends along the horizontal direction, observes along this central axis direction, and this vortex portion is the ring form. After entering the vortex device, the flue gas is distributed into each vortex tube, passes through the vortex tubes and continues to flow downwards, and when the flue gas passes through the vortex tubes, the vortex part is in a spiral ring shape, so that the flow direction of the flue gas is continuously changed in the flowing process of the flue gas in the vortex part, the oxidant in the flue gas can be further uniformly diffused into the flue gas, the low-valence nitrogen oxides are oxidized into high-valence nitrogen oxides, and the low-valence nitrogen oxides are removed in the subsequent semi-dry desulfurization or wet desulfurization.
Furthermore, in order to ensure the service life of the vortex tube, the vortex tube is a ceramic tube with an integral structure. The abrasion caused by dust particles in the flue gas is reduced by utilizing the abrasion resistance of the ceramic. Meanwhile, the vortex tube adopts a threaded connection mode, so that the vortex tube is convenient to disassemble and handle, and the vortex tube is convenient to stop operation and maintain and prevent blockage in the vortex tube.
Furthermore, in order to avoid large consumption on the pressure of the flue gas and enable the flue gas to generate large pressure drop, the inner diameter of the vortex tube is 80-120 mm. The flow velocity of the flue gas in the cooling tower is controlled to be about 3-5 m/s, the flow velocity of the flue gas in the vortex tube is controlled to be 5-10 m/s, and the flow velocity of the flue gas in the vortex tube is controlled to be 1.5-2 times of the flow velocity of the flue gas in the cooling tower.
Further, in order to reduce the boundary effect, the baffle plate comprises a conical pipe with the small end facing upwards and a circular plate arranged at the lower end of the conical pipe, and an inlet pipe of the vortex pipe penetrates through the circular plate upwards in a threaded connection mode. Utilize the taper pipe, make the flue gas collect to the central zone of oxidation tower gradually, avoid a right angle dead gas district between the inner wall of division board and oxidation tower, make a large amount of dusts pile up in this region.
Furthermore, in order to avoid causing the liquid drop to be too big and prevent the spray water from being incapable of being completely vaporized, so that partial cooling water is adhered to the inner wall of the oxidation tower and the cooling effect is reduced, the nozzle adopts a double-phase flow atomization nozzle, and the grain diameter of the sprayed liquid drop is 50-120 mu m.
Further, in order to realize oxidation of nitrogen oxides and subsequent desulfurization, the temperature of the flue gas passing through the tapered pipe is reduced to 100-120 ℃.
Specifically, the tapered pipe comprises a necking pipe, a shrinkage pipe connected to the upper side of the necking pipe and a diffusion pipe connected to the lower side of the necking pipe, the shrinkage pipe is in a tapered shape with the small end facing downwards, and the edge of the upper end of the shrinkage pipe is connected to the inner wall of the oxidation tower in a sealing mode; the diffusion pipe is in a conical shape with the small end facing upwards, the edge of the lower end of the diffusion pipe is connected to the inner wall of the oxidation tower in a sealing mode, and the oxidant ejector is installed in the necking pipe. In the necking pipe, the flow area is reduced, a negative pressure area is formed, the diffusion of the oxidant in the flue gas is favorably improved, and meanwhile, when the flue gas enters the diffusion pipe, a vortex can be formed, the uniform distribution of the oxidant in the flue gas is favorably improved, and the oxidation efficiency is improved.
Further, the clear distance between the conical reducing pipe and the vortex device is 1-2 times of the inner diameter of the oxidation tower. In the distance range, the flue gas can be fully diffused in the first inner cavity of the oxidation tower, and the improvement of the uniformity of entering each vortex tube is facilitated.
Furthermore, a manhole is arranged on the oxidation tower, so that when the operation is stopped, workers can enter the oxidation tower to overhaul.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
Fig. 2 is an enlarged view of a portion a in fig. 1.
Detailed Description
Referring to fig. 1 and 2, the integrated treatment device for desulfurization and denitrification of flue gas of a rock wool cupola furnace comprises an oxidation tower 10 and a desulfurization tower 50, wherein the bottom of the oxidation tower and the bottom of the desulfurization tower are connected together through a connecting air duct 40. The oxidation tower 10 and the desulfurization tower 50 both extend along the vertical direction, a flue gas inlet 18 is arranged at the top of the oxidation tower 10, a flue gas outlet 53 is arranged at the top of the desulfurization tower 50, a tapered pipe 20 and a swirler 30 are arranged in a first inner cavity 111 of the oxidation tower, and the tapered pipe 20 is positioned above the swirler 30. The connection air channel extends along the horizontal direction, a slag container 41 is arranged on the bottom plate of the connection air channel, a slag discharge pipe 43 is arranged at the bottom of the slag container, a gate valve 42 is arranged on the slag discharge pipe, when smoke passes through the connection air channel, natural sedimentation occurs due to reduction of flow speed, partial dust carried in the smoke can be settled in the slag container, the gate valve is periodically opened, and the dust in the slag container is discharged.
The tapered pipe 20 comprises a necked pipe 22, a contracted pipe 21 connected to the upper side of the necked pipe and a diffusion pipe 23 connected to the lower side of the necked pipe, the contracted pipe is in a conical shape with the small end facing downwards, and the edge of the upper end of the contracted pipe is connected to the inner wall of the oxidation tower in a sealing manner; the diffusion pipe is in a conical shape with the small end facing upwards, and the edge of the lower end of the diffusion pipe is connected to the inner wall of the oxidation tower in a sealing mode.
The swirler 30 comprises a partition plate 12 arranged in a first inner cavity and a number of swirl tubes 39, the swirl tubes 39 being located at the lower side of the partition plate 12. The partition plate 12 comprises a conical pipe 121 having a small end directed upward and a circular plate 122 installed at the lower end of the conical pipe, the conical pipe being connected to the inner wall of the oxidation tower. The circular plate 122 is formed with a tapered hole 123 having a small end facing downward, a tapered pipe 124 is inserted into the tapered hole from the upper side to the lower side and fixed to the circular plate, and an external thread is formed at the lower end of the tapered pipe 124.
Each vortex tube 39 includes a vortex portion 32 in the shape of a spiral ring, the two ends of the vortex portion are respectively an inlet tube 31 and an outlet tube 33, the central axis of the vortex portion extends along the horizontal direction, the vortex portion is in the shape of a ring encircling by taking the central axis as an axis when viewed along the direction of the central axis, and the inlet tube 31 and the outlet tube 33 both extend along the vertical direction. The vortex tube 39 has a first inner diameter S of 100 mm. In the present application, the pitch diameter F of the vortex portion is controlled to be 200-400 mm, and in the present embodiment, the pitch diameter F of the vortex portion is specifically controlled to be 300 mm.
The inlet tube 31 is internally threaded and the flow tube is screwed onto the external thread of the cone to mount the vortex tube 39 to the barrier 12. I.e. each vortex tube comprises an inlet tube connected to and extending upwardly through the barrier and an outlet tube extending downwardly. In this embodiment, the vortex tube is a ceramic tube with an integral structure. A manhole 17 is arranged on the oxidation tower, and an operator can enter the oxidation tower 10 through the manhole 17 to overhaul and maintain the interior of the tower, so that the vortex tube can be replaced conveniently or the problems of failure and the like can be solved conveniently.
The clear distance H between the tapered pipe 20 and the swirler 30 is 1.5 times of the second inner diameter D of the oxidation tower. The clear distance H is the distance between the lower end of the diffuser pipe 23 and the upper end of the cone 121.
The inlet pipe 13 projects into the first interior space, and a nozzle 14 for spraying cooling water into the first interior space, i.e. into the oxidation tower, is attached to the end of the inlet pipe projecting into the first interior space. The nozzle 14 is a two-phase flow atomizing nozzle, and the particle diameter of the ejected liquid drop is 80-100 μm.
The oxidant pipe 15 extends into the neck pipe, and an oxidant nozzle 16 is mounted on the end of the oxidant pipe extending into the neck pipe, and the oxidant nozzle 16 is an oxidant injector.
The temperature of the smoke passing through the tapered pipe is reduced to 110-115 ℃. In the embodiment, the flow velocity of the flue gas in the cooling tower is controlled to be about 4 +/-0.5 m/s, and the flow velocity of the flue gas in the vortex tube is controlled to be 7 +/-0.5 m/s.
Semi-dry desulfurization is performed in the desulfurization tower 50, and a desulfurizer injector 52 for injecting alkaline desulfurization slurry into the second cavity is installed at the lower part of the second cavity 51 of the desulfurization tower, so as to perform semi-dry desulfurization on the flue gas. In the embodiment, the alkaline desulfurization slurry is calcium hydroxide slurry, and in order to enhance the alkalinity, sodium hydroxide may be supplemented to the calcium hydroxide slurry in other embodiments.
In the desulfurizing tower, dinitrogen pentoxide in the flue gas is absorbed by calcium hydroxide slurry to generate calcium nitrate, the calcium nitrate is adsorbed on dust along with the evaporation of moisture, and sulfur dioxide and sulfur trioxide in the flue gas generate calcium sulfite and calcium sulfate. The flue gas discharged from the flue gas outlet 53 enters the bag-type dust collector for dust removal, dust including calcium nitrate, calcium sulfite and calcium sulfate is removed, and the flue gas after dust removal enters a chimney through a draught fan to be discharged at high altitude.
When the embodiment is operated, the addition amount of ozone is 1.5 times of the mole number of nitrogen dioxide, the nitrogen dioxide is the amount obtained by converting both nitrogen monoxide and nitrogen dioxide in the flue gas into nitrogen dioxide, and the nitrogen dioxide is not detected at the flue gas outlet by adopting the addition amount of ozone.
Claims (9)
1. The integrated treatment device for desulfurization and denitrification of the flue gas of the rock wool cupola is characterized by comprising an oxidation tower and a desulfurization tower, wherein the bottom parts of the oxidation tower and the desulfurization tower are communicated, the oxidation tower and the desulfurization tower extend along the vertical direction, a flue gas inlet is formed in the top part of the oxidation tower, a flue gas outlet is formed in the top part of the desulfurization tower, a tapered pipe and a swirler are installed in a first inner cavity of the oxidation tower, and the tapered pipe is located above the swirler; a nozzle is arranged above the tapered pipe and used for spraying cooling water into the first inner cavity; an oxidant ejector is arranged in the tapered pipe;
the vortex device comprises a partition plate arranged in a first inner cavity and a plurality of vortex tubes, wherein the vortex tubes are positioned at the lower side of the partition plate, each vortex tube comprises an inlet tube and an outlet tube, the inlet tube is connected to the partition plate and upwards penetrates through the partition plate, and the outlet tubes extend downwards; and a desulfurizer sprayer is arranged in the second inner cavity of the desulfurization tower and is used for spraying alkaline slurry into the second inner cavity so as to perform semi-dry desulfurization and denitrification in the second inner cavity.
2. The integrated processing apparatus according to claim 1, wherein each of the vortex tubes includes a vortex portion having a spiral ring shape, the inlet tube and the outlet tube are provided at both ends of the vortex portion, respectively, a central axis of the vortex portion extends in a horizontal direction, and the vortex portion has a ring shape as viewed along the central axis.
3. The integrated processing device according to claim 1, wherein the vortex tube is a ceramic tube of unitary construction.
4. The integrated processing apparatus of claim 1,
the inner diameter of the vortex tube is 80-120 mm.
5. The integrated processing apparatus of claim 1,
the baffle plate comprises a conical pipe with the small end facing upwards and a circular plate arranged at the lower end of the conical pipe, and an inlet pipe of the vortex pipe penetrates through the circular plate upwards.
6. The integrated processing apparatus of claim 1,
the nozzle adopts a double-phase flow atomizing nozzle, and the grain diameter of the sprayed liquid drop is 50-120 mu m.
7. The integrated processing device according to claim 1, wherein the temperature of the flue gas passing through the tapered pipe is reduced to 100-120 ℃.
8. The integrated processing apparatus of claim 1,
the tapered pipe comprises a necking pipe, a contraction pipe connected to the upper side of the necking pipe and a diffusion pipe connected to the lower side of the necking pipe, the contraction pipe is in a tapered shape with the small end facing downwards, and the edge of the upper end of the contraction pipe is connected to the inner wall of the oxidation tower in a sealing mode; the diffusion pipe is in a conical shape with the small end facing upwards, the edge of the lower end of the diffusion pipe is connected to the inner wall of the oxidation tower in a sealing mode, and the oxidant ejector is installed in the necking pipe.
9. The integrated processing apparatus of claim 1,
the clear distance between the tapered pipe and the vortex device is 1-2 times of the inner diameter of the oxidation tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111507070.2A CN114377532A (en) | 2021-12-10 | 2021-12-10 | A integration processing apparatus that is used for rock wool cupola flue gas desulfurization denitration |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111507070.2A CN114377532A (en) | 2021-12-10 | 2021-12-10 | A integration processing apparatus that is used for rock wool cupola flue gas desulfurization denitration |
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| CN114377532A true CN114377532A (en) | 2022-04-22 |
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5193341A (en) * | 1989-06-01 | 1993-03-16 | Hkk Hanseatisches Kreativ Kontor Gesellschaft Fur Entwicklung Und Vertrieb Mbh | Arrangement for removing oxidizable or combustible particles from exhaust gases |
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