CN203556273U - Absorption tower for flue gas desulfurization through ammonia process - Google Patents
Absorption tower for flue gas desulfurization through ammonia process Download PDFInfo
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- CN203556273U CN203556273U CN201320559889.8U CN201320559889U CN203556273U CN 203556273 U CN203556273 U CN 203556273U CN 201320559889 U CN201320559889 U CN 201320559889U CN 203556273 U CN203556273 U CN 203556273U
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- Prior art keywords
- oxidation air
- pipe
- absorption tower
- tower
- oxidation
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 47
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 28
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 239000003546 flue gas Substances 0.000 title claims abstract description 17
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 14
- 238000000034 method Methods 0.000 title abstract description 13
- 238000006477 desulfuration reaction Methods 0.000 title abstract description 3
- 230000023556 desulfurization Effects 0.000 title abstract description 3
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 81
- 230000003647 oxidation Effects 0.000 claims abstract description 80
- 239000002893 slag Substances 0.000 claims abstract description 13
- 238000005507 spraying Methods 0.000 claims abstract description 8
- 239000007921 spray Substances 0.000 claims description 14
- 230000003009 desulfurizing effect Effects 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 9
- 238000003756 stirring Methods 0.000 claims description 7
- 230000008676 import Effects 0.000 claims description 5
- 230000001590 oxidative effect Effects 0.000 claims description 4
- 239000007788 liquid Substances 0.000 abstract description 18
- 239000002002 slurry Substances 0.000 abstract description 15
- 239000007787 solid Substances 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 3
- 238000002156 mixing Methods 0.000 abstract description 3
- 239000002245 particle Substances 0.000 abstract description 2
- 230000000903 blocking effect Effects 0.000 abstract 1
- 230000005484 gravity Effects 0.000 abstract 1
- 239000007791 liquid phase Substances 0.000 abstract 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 238000005299 abrasion Methods 0.000 description 4
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 description 3
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 3
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 3
- 235000011130 ammonium sulphate Nutrition 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 2
- 239000013505 freshwater Substances 0.000 description 2
- 238000005272 metallurgy Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000003916 acid precipitation Methods 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
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Abstract
The utility model discloses an absorption tower for flue gas desulfurization through an ammonia process. The absorption tower comprises a tower body, wherein an air inlet is arranged at the middle part of the tower body; an air outlet is arranged at the upper end of the tower body; a slag outlet is arranged at the lower end of the tower body; a spraying layer is arranged between the air inlet and the air outlet; an oxidation layer is arranged between the air inlet and the slag outlet. The absorption tower is characterized in that an inclined tower board is mounted at the bottom of the tower body; an included angle alpha of the tower body and a horizontal face is more than or equal to 3 degrees and is less than or equal to 30 degrees; the slag outlet is arranged at the lowest position of the tower board. The absorption tower provided by the utility model adopts an inclined type absorption tower board structure and is provided with two layers of oxidation air pipes in a staggered manner, so that the back-mixing and the turbulence of gas-liquid phase contact can be greatly improved, and the uniform mixing in an entire circular slurry basin is guaranteed; solid particles separated from slurry are accumulated to the lowest position of the bottom of the absorption tower under the effect of gravity and the disturbance of oxidation air and then are pumped into a product after-treatment section by a slurry pump, so that the probability of blocking equipment, pipelines and nozzles by circular absorption liquid is greatly reduced.
Description
Technical field
The utility model relates to a kind of absorption tower device for ammonia process wet desulfurizing process, is particularly useful for the smoke gas treatment field of electric power, metallurgy and chemical field.
Background technology
Sulfur dioxide is one of main component forming in atmosphere acid rain, and ammonia process wet desulfurizing process is widely used in the treating tail gas of electric power, metallurgy and chemical industry, effectively reduces the SO in tail gas
2concentration is obvious to the improvement effect of environment.
In traditional ammonia process Wet Flue Gas Desulfurization Technique, absorption tower the first half is for absorbing spray district, and the latter half is recycle slurry liquid pool.Flue gas self-absorption tower middle part enters absorption tower,, with the absorption liquid counter current contacting of self-absorption top of tower spraying layer spray, Gas-Liquid Absorption reaction occurs from bottom to top, removes SO
2after the chimney of flue gas self-absorption top of tower enter atmosphere.
Absorbed SO
2absorption liquid absorbed the heat in former flue gas simultaneously, absorption liquid flows into after recycle slurry liquid pool, in slurry pool, the concentration of ammonium sulfite and ammonium sulfate is further concentrated.In actual moving process, because the parameter controls such as the pH value of slurry pool, total salt (being mainly ammonium sulfite and ammonium sulfate) concentration are more difficult, cause ammonium sulfate and ammonium sulfite supersaturation in absorption tower system, separate out solid, and then cause the shower nozzle of slurry circulating pump abrasion, spraying layer to stop up, greatly reduce the service life of desulphurization plant, also have influence on the absorption efficiency of sulfur dioxide.
Summary of the invention
Technical problem: technical problem to be solved in the utility model is for above-mentioned the deficiencies in the prior art, and a kind of absorption tower of the ammonia type flue gas desulfurizing that has reduced circulating absorption solution abrasion, occluding device, pipeline, nozzle equally likely possibility is provided.
Technical scheme: the utility model solves the technical scheme that its technical problem adopts and is:
A kind of absorption tower of ammonia type flue gas desulfurizing, comprise tower body, middle part at described tower body is provided with air inlet, in the upper end of tower body, is provided with gas outlet, in the lower end of tower body, is provided with slag notch, between described air inlet and gas outlet, be provided with spraying layer, between air inlet and slag notch, be provided with oxide layer, it is characterized in that: in described tower body bottom, tilting column plate is installed, the angle of column plate and horizontal plane is α, 3 °≤α≤30 °, described slag notch is arranged on this column plate lowest part.
Described oxide layer comprises two-layer oxidation air pipe, two-layer oxidation air pipe is vertical dislocation and arranges, the air inlet pipe of the air inlet pipe of upper strata oxidation air pipe and lower floor's oxidation air pipe is connected in parallel to an inlet manifold, the volume that wherein enters upper strata oxidation air pipe air inlet pipe oxidation air accounts for 50～80% of total oxidation air amount, and the volume that enters the oxidation air of lower floor's oxidation air pipe air inlet pipe accounts for 20～50% of total oxidation air amount.
Described two-layer oxidation air pipe includes multiple arms that are arranged in parallel, the oxidation air of the air inlet pipe of upper strata oxidation air pipe and lower floor's oxidation air air inlet pipe disperses to enter each arm by annular spread pipe, and Mei Gen arm import department establishes to regulate the flow control valve of each arm oxidation air flow.
Lower floor's oxidation air pipe is parallel to tilting column plate; The arm bottom of lower floor's oxidation air pipe arranges one group of jet pipe, and the angle of jet pipe and vertical direction is β, wherein β=α; The arm left and right sides is also provided with some spray orifices, and left side spray orifice, right side spray orifice and bottom jet pipe are dislocation and arrange.
Upper strata oxidation air pipe is parallel to horizontal plane to be arranged, in arm bottom and the left and right sides dislocation of upper strata oxidation air pipe, offers spray orifice.
0.5～2m place above the oxidation air pipe of upper strata, installs stirring system, and stirring system is comprised of m agitator, wherein 2≤m≤6; Agitator power is 30～50% of conventional torch-type mode of oxidizing.
Beneficial effect: the utility model adopts in bottom, absorption tower tilting column plate is installed, bottom and the horizontal plane on absorption tower are angled, the solid precipitation of separating out in absorption liquid, at the bottom of tower, can flow to voluntarily absorption tower lowest part under the effect of self gravitation and absorption liquid buoyancy.The oxidation tube of lower level in the recycle slurry liquid pool of absorption tower, oxidation air jet pipe has been installed, the flow perturbation of the oxidation air of ejection to tilting column plate portion, the solid-phase crystallization that is trapped in tower basal surface can be blown to absorption tower lowest part, and then squeeze into treatment and finishing section by slag stock pump, in case bring slurry circulating pump into, strengthen obstruction and abrasion to system.Oxidative system adopts two-layer oxidation air pipe to arrange, two-layer oxidation air constantly collides with absorption liquid in the process rising, and has increased the turbulence of gas-liquid two-phase, has improved the efficiency of oxidation; Side-feeding mixer is located at the upside of higher level oxidation tube, oxidation air is in floating-upward process, under the mechanical disturbance of agitator paddle, further broken, increased the specific area of oxidation air, further increase the contact area of gas-liquid two-phase, be conducive to the raising of efficiency, also improved the utilization rate of oxidation air simultaneously.Owing to having adopted two-layer oxidation air pipe arrangement, the disturbance of oxidation air has increased the uniformity that absorption liquid mixes greatly, and the type selecting that therefore power ratio of side-feeding mixer is traditional is much smaller, has significantly saved stirring energy consumption.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the utility model is further illustrated.
Fig. 1 is the utility model front view.
Fig. 2 is the utility model A-A place agitator top view.
Fig. 3 is the utility model B-B place oxidation air pipe top view.
Fig. 4 is the utility model C-C place oxidation air pipe top view.
Fig. 5 is the top view of support column at the bottom of absorbing tower.
Fig. 6 is the enlarged drawing of H in Fig. 1.
Fig. 7 is the enlarged drawing of J in Fig. 1.
Wherein: 1, tower body, 2, air inlet, 3, gas outlet, 4, slag notch, 5, spraying layer, 6, oxide layer, 61, upper strata oxidation air pipe, 62, lower floor's oxidation air pipe, 63, annular spread pipe, 64, arm, 7, agitator, 8, column plate, 9, slag stock pump.
The specific embodiment
Below in conjunction with drawings and Examples, the utility model is illustrated.
Former flue gas enters absorption tower by middle part, absorption tower, with the absorption liquid counter current contacting from spraying layer (number of plies of spraying layer is by determining according to requirement of engineering), SO
2be absorbed by liquid absorption, former flue gas process fresh water (FW) supplemental layers, then pass through two-stage demister, by absorption tower outlet, enter chimney and enter atmosphere.
In the present embodiment, tilting column plate is installed in bottom, absorption tower, the angle of column plate and horizontal plane is that one group of oxidation air pipe that is parallel to column plate is arranged in α (3≤α≤30 °) column plate top, its structure as Figure 1 and Figure 4, parallel to each other between oxidation air pipe, its quantity determines by loop slurry pool size, oxidation air pipe bottom design one group of jet pipe, the angle of jet pipe and vertical direction is β (β=α), and the number of jet pipe is determined by the quantity that is oxidized air quantity and oxidation air pipe.Except bottom is provided with jet pipe, the oxidation air pipe left and right sides is also provided with some spray orifices, and left side spray orifice, right side spray orifice and bottom jet pipe are dislocation to be arranged, to increase axial backmixing, promotes the oxidation of ammonium salt.In slurries, separate out solid particle under the disturbance of self gravitation and jet pipe oxidation air, accumulate to bottom, absorption tower lowest part, via slag stock pump, squeeze into product treatment and finishing section, reduced the possibility of circulating absorption solution abrasion, occluding device, pipeline, nozzle etc.
In the present embodiment, stirring system is comprised of the individual agitator of m (2≤m≤6), and the numerical value of m is by slurry pool, and the setting height(from bottom) of agitator determines by slurry pool height, and arrangement is referring to Fig. 2.Agitator power is 30～50% of conventional torch-type mode of oxidizing.
0.5～2m place below stirring system～, arrange another layer of oxidation air pipe layer, this layer of oxidation air pipe is parallel with horizontal plane, and is square crossing layout with the oxidation air pipe of lower level, and offers spray orifice in bottom and left and right sides dislocation.
The oxidation air of oxidation fan outlet is divided into two strands, flow to respectively the import (in figure shown in K, L) of two-layer oxidation air pipe, the volume that wherein enters mouth of pipe K oxidation air accounts for 50～80% of total oxidation air amount, and the volume that enters mouth of pipe L oxidation air accounts for 20～50% of total oxidation air amount.Oxidation air enters respectively after import K, L, by annular spread pipe, is disperseed to enter each arm, and Mei Gen arm import department establishes flow control valve V, to regulate each arm oxidation air flow.
The dislocation arrangement of double-deck oxidation air pipe of the present utility model, in conjunction with low power agitator system, guaranteed the uniformity of whole slurry pool mixed atmosphere, back-mixing and the turbulence of Gas-Liquid Contacting have greatly been improved, small-power agitator has increased the specific area of gas phase especially to the fragmentation of bubble, promote the gas-liquid mass transfer of oxidation reaction process, improved the utilization rate of oxidation air, reduced energy consumption.
Claims (6)
1. the absorption tower of an ammonia type flue gas desulfurizing, comprise tower body, middle part at described tower body is provided with air inlet, in the upper end of tower body, is provided with gas outlet, in the lower end of tower body, is provided with slag notch, between described air inlet and gas outlet, be provided with spraying layer, between air inlet and slag notch, be provided with oxide layer, it is characterized in that: in described tower body bottom, tilting column plate is installed, the angle of column plate and horizontal plane is α, 3≤α≤30 °, described slag notch is arranged on this column plate lowest part.
2. the absorption tower of ammonia type flue gas desulfurizing according to claim 1, it is characterized in that: described oxide layer comprises two-layer oxidation air pipe, two-layer oxidation air pipe is vertical dislocation and arranges, the air inlet pipe of the air inlet pipe of upper strata oxidation air pipe and lower floor's oxidation air pipe is connected in parallel to an inlet manifold, the volume that wherein enters upper strata oxidation air pipe air inlet pipe oxidation air accounts for 50～80% of total oxidation air amount, and the volume that enters the oxidation air of lower floor's oxidation air pipe air inlet pipe accounts for 20～50% of total oxidation air amount.
3. the absorption tower of ammonia type flue gas desulfurizing according to claim 2, it is characterized in that: described two-layer oxidation air pipe includes multiple arms that are arranged in parallel, the oxidation air of the air inlet pipe of upper strata oxidation air pipe and lower floor's oxidation air air inlet pipe disperses to enter each arm by annular spread pipe, and Mei Gen arm import department establishes to regulate the flow control valve of each arm oxidation air flow.
4. the absorption tower of ammonia type flue gas desulfurizing according to claim 3, is characterized in that: lower floor's oxidation air pipe is parallel to tilting column plate; The arm bottom of lower floor's oxidation air pipe arranges one group of jet pipe, and the angle of jet pipe and vertical direction is β, wherein β=α; The arm left and right sides is also provided with some spray orifices, and left side spray orifice, right side spray orifice and bottom jet pipe are dislocation and arrange.
5. the absorption tower of ammonia type flue gas desulfurizing according to claim 3, is characterized in that: upper strata oxidation air pipe is parallel to horizontal plane to be arranged, in arm bottom and the left and right sides dislocation of upper strata oxidation air pipe, offers spray orifice.
6. the absorption tower of ammonia type flue gas desulfurizing according to claim 2, is characterized in that: 0.5～2m place above the oxidation air pipe of upper strata, stirring system is installed, and stirring system is comprised of m agitator, wherein 2≤m≤6; Agitator power is 30～50% of conventional torch-type mode of oxidizing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320559889.8U CN203556273U (en) | 2013-09-10 | 2013-09-10 | Absorption tower for flue gas desulfurization through ammonia process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320559889.8U CN203556273U (en) | 2013-09-10 | 2013-09-10 | Absorption tower for flue gas desulfurization through ammonia process |
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| Publication Number | Publication Date |
|---|---|
| CN203556273U true CN203556273U (en) | 2014-04-23 |
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| CN201320559889.8U Expired - Fee Related CN203556273U (en) | 2013-09-10 | 2013-09-10 | Absorption tower for flue gas desulfurization through ammonia process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104307331A (en) * | 2014-10-08 | 2015-01-28 | 泰州明锋资源再生科技有限公司 | Exhaust purification and discharge device in stainless steel acid washing sludge treatment process |
-
2013
- 2013-09-10 CN CN201320559889.8U patent/CN203556273U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104307331A (en) * | 2014-10-08 | 2015-01-28 | 泰州明锋资源再生科技有限公司 | Exhaust purification and discharge device in stainless steel acid washing sludge treatment process |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140423 |
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| CF01 | Termination of patent right due to non-payment of annual fee |