CN112999839A - Flue gas desulfurization system of drying tower kiln - Google Patents
Flue gas desulfurization system of drying tower kiln Download PDFInfo
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- CN112999839A CN112999839A CN202110323625.1A CN202110323625A CN112999839A CN 112999839 A CN112999839 A CN 112999839A CN 202110323625 A CN202110323625 A CN 202110323625A CN 112999839 A CN112999839 A CN 112999839A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 88
- 239000003546 flue gas Substances 0.000 title claims abstract description 88
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 35
- 230000023556 desulfurization Effects 0.000 title claims abstract description 35
- 238000001035 drying Methods 0.000 title claims abstract description 19
- 239000002002 slurry Substances 0.000 claims abstract description 106
- 238000010521 absorption reaction Methods 0.000 claims abstract description 91
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 27
- 239000010440 gypsum Substances 0.000 claims abstract description 27
- 238000005507 spraying Methods 0.000 claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 25
- 239000000428 dust Substances 0.000 claims abstract description 8
- 230000003647 oxidation Effects 0.000 claims description 27
- 238000007254 oxidation reaction Methods 0.000 claims description 27
- 239000007921 spray Substances 0.000 claims description 25
- 238000001816 cooling Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 230000007246 mechanism Effects 0.000 claims description 11
- 238000003756 stirring Methods 0.000 claims description 10
- 239000000919 ceramic Substances 0.000 claims description 7
- 238000005273 aeration Methods 0.000 claims description 6
- 230000018044 dehydration Effects 0.000 abstract description 4
- 238000006297 dehydration reaction Methods 0.000 abstract description 4
- 238000000605 extraction Methods 0.000 abstract 2
- 230000000694 effects Effects 0.000 description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 4
- 235000011941 Tilia x europaea Nutrition 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000004571 lime Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 238000005457 optimization Methods 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 239000011324 bead Substances 0.000 description 2
- 238000005094 computer simulation Methods 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 230000001706 oxygenating effect Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 230000001376 precipitating effect Effects 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 206010039509 Scab Diseases 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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- 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D53/502—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 solution or suspension
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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)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a flue gas desulfurization system of a drying tower kiln, which comprises a flue gas system, an SO2 absorption system and a gypsum dehydration system, wherein the flue gas system comprises a raw flue gas conveying pipe, a clean flue gas conveying pipe and a lower-level dust removal device, the raw flue gas conveying pipe and the clean flue gas conveying pipe are respectively arranged at a flue gas input end of an SO2 absorption system and a flue gas output end of an SO2 absorption system, the SO2 absorption system comprises an absorption tower, a slurry supply device and a slurry spraying device, the slurry spraying device is arranged at the upper part of an inner cavity of the absorption tower, a liquid outlet of the slurry supply device is connected with a liquid inlet of the slurry spraying device, the gypsum dehydration system comprises a gypsum extraction pump and a vacuum dehydration device, a feed inlet of the gypsum extraction pump is connected with a gypsum discharge port at the lower part of the absorption tower through a pipeline, and. The problems that the existing drying tower furnace flue gas desulfurization system is low in desulfurization efficiency and incomplete in desulfurization are solved.
Description
Technical Field
The invention relates to the field of flue gas desulfurization in ceramic production, in particular to a flue gas desulfurization system of a drying tower kiln.
Background
A drying tower furnace flue gas desulfurization system is a commonly used flue gas treatment system, in a wet flue gas desulfurization system, alkaline substances (usually an alkaline solution, more usually an alkaline slurry) meet flue gas in a spray tower, SO2 in the flue gas is dissolved in water to form a dilute acid solution, and then the dilute acid solution and the alkaline substances dissolved in the water are subjected to a neutralization reaction, and sulfite and sulfate generated by the reaction are separated out from the aqueous solution, and the separation condition depends on the relative solubilities of different salts existing in the solution.
However, the existing drying tower furnace flue gas desulfurization system generally has the problems of low desulfurization efficiency and incomplete desulfurization.
Disclosure of Invention
The invention aims to provide a drying tower kiln flue gas desulfurization system, which solves the problems of low desulfurization efficiency and incomplete desulfurization of the existing drying tower kiln flue gas desulfurization system.
In order to solve the technical problems, the invention adopts the following technical scheme:
the utility model provides a dry tower kiln flue gas desulfurization system, includes flue gas system, SO2 absorption system and gypsum dewatering system, flue gas system includes former flue gas conveyer pipe, clean flue gas conveyer pipe and subordinate dust collecting equipment, former flue gas conveyer pipe and clean flue gas conveyer pipe set up the flue gas output end at SO2 absorption system's flue gas input and SO2 absorption system respectively, SO2 absorption system includes absorption tower, thick liquid feeding device and thick liquid spray set, thick liquid spray set sets up the upper portion at the absorption tower inner chamber, and thick liquid feeding device's liquid outlet links to each other with thick liquid spray set's inlet, gypsum dewatering system includes that the gypsum pump out and vacuum dewatering device, and the feed inlet of gypsum pump out passes through the pipeline and links to each other with the gypsum discharge port of absorption tower lower part, and the discharge gate of gypsum pump is then continuous with vacuum dewatering device.
The flue gas which is not desulfurized is sent into the absorption tower under the action of the original flue gas conveying pipe of the flue gas system, the absorption tower at the moment is filled with slurry fog sprayed by the slurry spraying device, the flue gas which is not desulfurized reacts with the slurry fog after entering, the flue gas is desulfurized, the desulfurized flue gas is discharged from the flue gas output end of the SO2 absorption system and is sent into lower-level dust removal equipment through a clean flue gas conveying pipe to complete dust removal, the size and the internal components of the absorption tower are designed by adopting the auxiliary design function of CFD simulation (computer simulation), and the solid content of the slurry is 20-30% (wt), SO that the optimal absorption effect can be ensured.
In a further preferred embodiment of the present invention, a demister is further provided above the absorption tower.
The fog removing device is arranged to remove fog beads in smoke and ensure the absorption effect.
In a further preferred embodiment of the present invention, the demister has two or more layers.
The defogging effect of the defogger with more than two layers is better.
As a further preferable mode of the present invention, the SO2 absorption system further comprises a slurry circulation system, the slurry circulation system comprises a slurry circulation pump and a circulation spray device, the slurry circulation pump is disposed at one side outside the absorption tower, a liquid inlet of the slurry circulation pump is connected to a slurry circulation outlet at the lower part of the absorption tower through a pipeline, a liquid outlet of the slurry circulation pump is connected to a liquid inlet of the circulation spray device through a pipeline, and the circulation spray device is also disposed at the upper part of the inner cavity of the absorption tower.
The absorption tower slurry circulating system provides a larger-flow adsorbent for the absorption tower, can ensure the sufficient contact of gas phase and liquid phase, improves the absorption efficiency of SO2, and calculates the growth and retention time of gypsum particles (crystal seeds) according to the following formula for ensuring the optimal cost performance design of the oxygen/sulfur ratio:
RT=（V×ρ×SC）/TSP
wherein RT-residence time (min); TSP-gypsum finished product (dry basis) (kg/min), V-size of slurry pool (m 3); ρ -slurry density (kg/m 3); SC-slurry solid (%).
The residence time for lime dissolution is calculated according to the following formula:
T=V/（N×RF）
wherein T-residence time (min); v-slurry pool volume (m 3); n-number of circulating pumps; RF-Single cycle Pump flow rate (m 3/h).
Preferably, the lower part of the absorption tower is provided with two or more oxidation fans, one for one, an air outlet pipe bank of the oxidation fans is inserted into the inner cavity of the absorption tower, the air outlet pipe bank of the oxidation fans comprises an inner tower part and an outer tower part, and a cooling spraying mechanism is arranged above the outer tower part of the air outlet pipe bank of the oxidation fans.
The oxidation fan of chooseing for use is the roots's fan, can provide oil-free oxidation air, and the cooling spraying mechanism who sets up then can prevent the thick liquid scale deposit on the air-out calandria.
In a further preferred embodiment of the present invention, the slurry supply device includes a slurry tank and a stirring device, and the stirring blade of the stirring device is inserted into the slurry tank.
As a further preferable mode of the present invention, the slurry tank is further provided with a two-layer oxidation mechanism, the two-layer oxidation mechanism comprises a branched perforated pipe arranged at the bottom of the slurry tank and a branched ceramic aeration pipe arranged at a lower position in the middle of the slurry tank, and the sizes of the air bubbles of the branched perforated pipe and the branched ceramic aeration pipe are controlled to be 10-15 μm.
The size of the bubbles directly influences the air absorption efficiency of the slurry and the conversion efficiency of CaSo3, and causes great waste to energy sources, so the size of the bubbles in the slurry is controlled to be 10-15 mu m to ensure that the air absorption rate is not lower than 50 percent and the oxygen conversion rate is not lower than 50 percent, and simultaneously a reasonable turbulent flow interval is formed in the slurry to ensure that CaSo3 is converted to CaSo4, and oxygen sprayed from the branched perforated pipes can play a role in stirring the bottom layer while oxygenating the slurry tank, thereby preventing the bottom layer slurry from precipitating.
As a further preference of the invention, the inflow of flue gas introduced into the absorption column is from 3.6 to 3.9 m/s.
The larger the flue gas flow velocity is, the larger the absorption tower resistance is, the power consumption of the induced draft fan is increased, but the gas-liquid mass transfer is good, the desulfurization effect is enhanced, the flow rate of the slurry circulating pump can be reduced, the power consumption of the slurry circulating pump is reduced, the smaller the flue gas flow velocity is, the smaller the absorption tower resistance is, the power consumption of the induced draft fan is reduced, but the gas-liquid mass transfer is poor, and the flow rate of the slurry circulating pump needs to be increased, so that the power consumption of the slurry circulating pump is increased, the inflow of the flue gas introduced into the absorption tower after optimization is.
As a further optimization of the invention, the slurry spraying device comprises more than 3 layers of spraying pipes, the spraying pipes of all layers are arranged in a staggered mode, nozzles on a spraying pipe on the inner wall surface area of an inner cavity wall surface area of the absorption tower are denser than nozzles on a spraying pipe in the central area, the nozzles are efficient atomizing nozzles, and a non-blocking type hollow nozzle design is adopted.
The staggered arrangement can ensure the best contact between the flue gas and the slurry in the absorption tower, and can reduce the liquid-gas ratio, and because of the wall effect, namely the wall surface of the absorption tower is easy to form flue gas short circuit, the nozzles on the spray pipes on the wall surface area of the inner wall of the inner cavity of the absorption tower are more dense than the nozzles on the spray pipes in the central area, so that the occurrence probability of the situation can be reduced.
In a further preferred embodiment of the present invention, a water cooling pipe is provided on an outer wall of the pipe connecting the slurry supply device and the slurry spray device, and the water cooling pipe is connected to the cold water supply tank.
This prevents the slurry from crusting on the shower pipes.
Compared with the prior art, the invention can at least achieve one of the following beneficial effects:
1. the desulfurization effect is good, the desulfurization guarantee rate is more than 90%, the discharge concentration of SO2 at the outlet is less than 50mg/Nm3, the consumption of lime powder in a desulfurization system is less than 0.1t/h, the mesh number of the lime powder adopted for preparing the absorbent is 250 meshes, and the moisture content of the dehydrated desulfurization byproduct is less than 15%.
2. The spraying pipe is not easy to scab.
3. The air outlet calandria is not easy to scale.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Specific example 1:
FIG. 1 shows a flue gas desulfurization system of a drying tower kiln, which comprises a flue gas system, an SO2 absorption system and a gypsum dehydration system, the flue gas system comprises a raw flue gas conveying pipe 1, a clean flue gas conveying pipe 2 and lower-level dust removing equipment, the original flue gas conveying pipe 1 and the clean flue gas conveying pipe 2 are respectively arranged at the flue gas input end of the SO2 absorption system and the flue gas output end of the SO2 absorption system, the SO2 absorption system comprises an absorption tower 3, a slurry supply device 4 and a slurry spraying device 5, the slurry spraying device 5 is arranged at the upper part of the inner cavity of the absorption tower 3, the liquid outlet of the slurry supply device 4 is connected with the liquid inlet of the slurry spraying device 5, the gypsum dewatering system comprises a gypsum pump 6 and a vacuum dewatering device 7, a feed inlet of the gypsum pump 6 is connected with a gypsum discharge port at the lower part of the absorption tower 3 through a pipeline, and a discharge outlet of the gypsum pump 6 is connected with the vacuum dewatering device 7.
The flue gas which is not desulfurized is sent into the absorption tower under the action of the original flue gas conveying pipe of the flue gas system, the absorption tower at the moment is filled with slurry fog sprayed by the slurry spraying device, the flue gas which is not desulfurized reacts with the slurry fog after entering, the flue gas is desulfurized, the desulfurized flue gas is discharged from the flue gas output end of the SO2 absorption system and is sent into lower-level dust removal equipment through a clean flue gas conveying pipe to complete dust removal, the size and the internal components of the absorption tower are designed by adopting the auxiliary design function of CFD simulation (computer simulation), and the solid content of the slurry is 20-30% (wt), SO that the optimal absorption effect can be ensured.
Specific example 2:
in this embodiment, a demister is added to the specific embodiment 1, and a demister 8 is further provided above the absorption tower 3.
The fog removing device is arranged to remove fog beads in smoke and ensure the absorption effect.
Specific example 3:
in this embodiment, the number of the defoggers 8 is further described based on the specific embodiment 2, and the defoggers 8 have two or more layers.
The defogging effect of the defogger with more than two layers is better.
Specific example 4:
in this embodiment, an SO2 absorption system is further described on the basis of specific embodiment 1, the SO2 absorption system further includes a slurry circulation system, the slurry circulation system includes a slurry circulation pump 9 and a circulation spray device 10, the slurry circulation pump 9 is disposed at one side of the outside of the absorption tower 3, a liquid inlet of the slurry circulation pump 9 is connected to a slurry circulation outlet at the lower part of the absorption tower 3 through a pipeline, a liquid outlet of the slurry circulation pump 9 is connected to a liquid inlet of the circulation spray device 10 through a pipeline, and the circulation spray device 10 is also disposed at the upper part of the inner cavity of the absorption tower 3.
The absorption tower slurry circulating system provides a larger-flow adsorbent for the absorption tower, can ensure the sufficient contact of gas phase and liquid phase, improves the absorption efficiency of SO2, and calculates the growth and retention time of gypsum particles (crystal seeds) according to the following formula for ensuring the optimal cost performance design of the oxygen/sulfur ratio:
RT=（V×ρ×SC）/TSP
wherein RT-residence time (min); TSP-gypsum finished product (dry basis) (kg/min), V-size of slurry pool (m 3); ρ -slurry density (kg/m 3); SC-slurry solid (%).
The residence time for lime dissolution is calculated according to the following formula:
T=V/（N×RF）
wherein T-residence time (min); v-slurry pool volume (m 3); n-number of circulating pumps; RF-Single cycle Pump flow rate (m 3/h).
Specific example 5:
in this embodiment, an oxidation fan 11 is additionally provided on the basis of specific embodiment 1, the lower portion of the absorption tower 3 is provided with the oxidation fan 11, the oxidation fan 11 has more than two oxidation fans 11, one oxidation fan is used as standby, an air outlet pipe bank of the oxidation fan 11 is inserted into the inner cavity of the absorption tower 3, the air outlet pipe bank of the oxidation fan 11 includes an inner tower portion and an outer tower portion, and a cooling spraying mechanism 12 is arranged above the air outlet pipe bank of the oxidation fan 11.
The oxidation fan of chooseing for use is the roots's fan, can provide oil-free oxidation air, and the cooling spraying mechanism who sets up then can prevent the thick liquid scale deposit on the air-out calandria.
Specific example 6:
in this embodiment, a slurry supply apparatus 4 is further described in relation to embodiment 1, and the slurry supply apparatus 4 includes a slurry tank and a stirring device having a stirring blade inserted into the slurry tank.
Specific example 7:
this embodiment is further described with reference to specific example 6, in which a two-layer oxidation mechanism is further disposed in the slurry tank, the two-layer oxidation mechanism includes a branched perforated pipe disposed at the bottom of the slurry tank and a branched ceramic aeration pipe disposed at a lower position in the middle of the slurry tank, and the sizes of the air bubbles in the branched perforated pipe and the branched ceramic aeration pipe are controlled to be 10-15 μm.
The size of the bubbles directly influences the air absorption efficiency of the slurry and the conversion efficiency of CaSo3, and causes great waste to energy sources, so the size of the bubbles in the slurry is controlled to be 10-15 mu m to ensure that the air absorption rate is not lower than 50 percent and the oxygen conversion rate is not lower than 50 percent, and simultaneously a reasonable turbulent flow interval is formed in the slurry to ensure that CaSo3 is converted to CaSo4, and oxygen sprayed from the branched perforated pipes can play a role in stirring the bottom layer while oxygenating the slurry tank, thereby preventing the bottom layer slurry from precipitating.
Specific example 8:
this example further illustrates the flow rate of the introduced flue gas of the absorption tower 3 on the basis of the specific example 1, wherein the inflow of the introduced flue gas of the absorption tower 3 is 3.6-3.9 m/s.
The larger the flue gas flow velocity is, the larger the absorption tower resistance is, the power consumption of the induced draft fan is increased, but the gas-liquid mass transfer is good, the desulfurization effect is enhanced, the flow rate of the slurry circulating pump can be reduced, the power consumption of the slurry circulating pump is reduced, the smaller the flue gas flow velocity is, the smaller the absorption tower resistance is, the power consumption of the induced draft fan is reduced, but the gas-liquid mass transfer is poor, and the flow rate of the slurry circulating pump needs to be increased, so that the power consumption of the slurry circulating pump is increased, the inflow of the flue gas introduced into the absorption tower after optimization is.
Specific example 9:
the present embodiment is further described with respect to a slurry spraying device 5 on the basis of specific embodiment 1, where the slurry spraying device 5 includes more than 3 layers of spraying pipes, the spraying pipes in each layer are arranged in a staggered manner, and nozzles on a spray pipe in a wall surface area of an inner wall of an inner cavity of an absorption tower 3 are more dense than nozzles on a spray pipe in a central area, and the nozzles are high-efficiency atomizing nozzles, and simultaneously adopt a non-clogging hollow nozzle design.
The staggered arrangement can ensure the best contact between the flue gas and the slurry in the absorption tower, and can reduce the liquid-gas ratio, and because of the wall effect, namely the wall surface of the absorption tower is easy to form flue gas short circuit, the nozzles on the spray pipes on the wall surface area of the inner wall of the inner cavity of the absorption tower are more dense than the nozzles on the spray pipes in the central area, so that the occurrence probability of the situation can be reduced.
Specific example 10:
in this embodiment, a water cooling pipeline 13 is additionally provided on the basis of embodiment 1, a water cooling pipeline 13 is provided on the outer wall of the pipeline connecting the slurry supply device 4 and the slurry spray device 5, and the water cooling pipeline 13 is connected to a cold water supply tank.
This prevents the slurry from crusting on the shower pipes.
Although the invention has been described herein with reference to a number of illustrative embodiments thereof, it should be understood that numerous other modifications and embodiments can be devised by those skilled in the art that will fall within the spirit and scope of the principles of this disclosure. More specifically, various variations and modifications are possible in the component parts and/or arrangements of the subject combination arrangement within the scope of the disclosure, the drawings and the appended claims. In addition to variations and modifications in the component parts and/or arrangements, other uses will also be apparent to those skilled in the art.
Claims (10)
1. The utility model provides a dry tower kiln flue gas desulfurization system, includes flue gas system, SO2 absorption system and gypsum dewatering system, its characterized in that: the flue gas system comprises a raw flue gas conveying pipe (1), a clean flue gas conveying pipe (2) and lower-level dust removing equipment, the original flue gas conveying pipe (1) and the clean flue gas conveying pipe (2) are respectively arranged at the flue gas input end of the SO2 absorption system and the flue gas output end of the SO2 absorption system, the SO2 absorption system comprises an absorption tower (3), a slurry supply device (4) and a slurry spraying device (5), the slurry spraying device (5) is arranged at the upper part of the inner cavity of the absorption tower (3), the liquid outlet of the slurry supply device (4) is connected with the liquid inlet of the slurry spraying device (5), the gypsum dewatering system comprises a gypsum pump (6) and a vacuum dewatering device (7), wherein a feed inlet of the gypsum pump (6) is connected with a gypsum discharge port at the lower part of the absorption tower (3) through a pipeline, and a discharge outlet of the gypsum pump (6) is connected with the vacuum dewatering device (7).
2. The drying tower kiln flue gas desulfurization system of claim 1, wherein: the upper part of the absorption tower (3) is also provided with a demister (8).
3. The drying tower kiln flue gas desulfurization system according to claim 2, characterized in that: the demister (8) has more than two layers.
4. The drying tower kiln flue gas desulfurization system of claim 1, wherein: SO2 absorption system has still included slurry circulation system, slurry circulation system includes slurry circulation pump (9) and circulation spray set (10), slurry circulation pump (9) set up in the outside one side of absorption tower (3), and the inlet of slurry circulation pump (9) passes through the pipeline and links to each other with the slurry circulation export of absorption tower (3) lower part, and the play liquid mouth of slurry circulation pump (9) then links to each other through the inlet of pipeline with circulation spray set (10), circulation spray set (10) also set up the upper portion at absorption tower (3) inner chamber.
5. The drying tower kiln flue gas desulfurization system of claim 1, wherein: the lower part of absorption tower (3) is equipped with oxidation fan (11), and oxidation fan (11) have more than two, one is equipped with one, and the air-out calandria of oxidation fan (11) is inserted and is established in the inner chamber of absorption tower (3), and the air-out calandria of oxidation fan (11) includes tower internal portion and tower outer part, the air-out calandria of oxidation fan (11) outside the tower part's top is equipped with cooling and sprays mechanism (12).
6. The drying tower kiln flue gas desulfurization system of claim 1, wherein: the slurry supply device (4) comprises a slurry tank and a stirring device, and stirring blades of the stirring device are inserted into the slurry tank.
7. The drying tower kiln flue gas desulfurization system of claim 6, wherein: the slurry tank is also internally provided with two layers of oxidation mechanisms, each two layers of oxidation mechanisms comprise a branched perforated pipe arranged at the bottom of the slurry tank and a branched ceramic aeration pipe arranged at the lower part of the middle part of the slurry tank, and the sizes of the bubbles of the branched perforated pipes and the branched ceramic aeration pipes are controlled to be 10-15 mu m.
8. The drying tower kiln flue gas desulfurization system of claim 1, wherein: the inflow of the flue gas introduced by the absorption tower (3) is 3.6-3.9 m/s.
9. The drying tower kiln flue gas desulfurization system of claim 1, wherein: slurry spray set (5) include the shower more than 3 layers, staggered arrangement between each layer shower, and the nozzle on the inner wall surface district spray tube of absorption tower (3) inner chamber is denser than the nozzle on the center district spray tube, the nozzle is high-efficient atomizing nozzle, adopts the design of non-clogging formula cavity nozzle simultaneously.
10. The drying tower kiln flue gas desulfurization system of claim 1, wherein: and a water cooling pipeline (13) is arranged on the outer wall of the pipeline connecting the slurry supply device (4) and the slurry spraying device (5), and the water cooling pipeline (13) is connected with a cold water supply tank.
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| CN202110323625.1A CN112999839A (en) | 2021-03-26 | 2021-03-26 | Flue gas desulfurization system of drying tower kiln |
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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