CN203577619U - Absorption tower for desulfuration by using wet type calcium method - Google Patents
Absorption tower for desulfuration by using wet type calcium method Download PDFInfo
- Publication number
- CN203577619U CN203577619U CN201320636006.9U CN201320636006U CN203577619U CN 203577619 U CN203577619 U CN 203577619U CN 201320636006 U CN201320636006 U CN 201320636006U CN 203577619 U CN203577619 U CN 203577619U
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- Prior art keywords
- liquid pool
- slurry tank
- absorption
- thin pulp
- pool
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 40
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 18
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims abstract description 12
- 239000011575 calcium Substances 0.000 title claims abstract description 12
- 229910052791 calcium Inorganic materials 0.000 title claims abstract description 12
- 238000000034 method Methods 0.000 title abstract description 5
- 239000002002 slurry Substances 0.000 claims abstract description 69
- 239000007788 liquid Substances 0.000 claims abstract description 65
- 238000005507 spraying Methods 0.000 claims abstract description 23
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 11
- 239000010440 gypsum Substances 0.000 claims abstract description 11
- 238000001816 cooling Methods 0.000 claims description 21
- 230000003647 oxidation Effects 0.000 claims description 9
- 238000007254 oxidation reaction Methods 0.000 claims description 9
- 238000005273 aeration Methods 0.000 claims description 6
- 230000001590 oxidative effect Effects 0.000 claims description 6
- 239000000779 smoke Substances 0.000 claims description 6
- 239000012141 concentrate Substances 0.000 claims description 2
- 238000007789 sealing Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 26
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 18
- 239000003517 fume Substances 0.000 abstract description 5
- 230000009286 beneficial effect Effects 0.000 abstract 1
- 238000000638 solvent extraction Methods 0.000 abstract 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 22
- 239000003546 flue gas Substances 0.000 description 22
- 230000003009 desulfurizing effect Effects 0.000 description 6
- 239000007921 spray Substances 0.000 description 6
- 210000002966 serum Anatomy 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 229920006395 saturated elastomer Polymers 0.000 description 4
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 3
- 235000010261 calcium sulphite Nutrition 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000008021 deposition Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000011800 void material Substances 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical class OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 2
- 206010061876 Obstruction Diseases 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 125000006850 spacer group Chemical group 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model discloses an absorption tower for desulfuration by using a wet type calcium method. The absorption tower comprises a tower body, wherein a slurry tank, a gas cap layer, a plurality of main spraying absorption layers and a plurality of demister layers are sequentially arranged inside the tower body from bottom to top, wherein a fume outlet is formed in the top of the tower body; a fume inlet is formed between the slurry tank and the gas cap layer; the slurry tank is partitioned into a diluted slurry tank and a thick slurry tank by a partitioning plate; the diluted slurry tank is sealed up; a temperature reducing concentration spraying layer is arranged between the slurry tank and the gas cap layer; a nozzle on the temperature reducing concentration spraying layer is communicated with the thick slurry tank through a temperature reducing concentration circulation outlet pipeline; a gypsum slurry discharge hole is formed in the thick slurry tank; the diluted slurry tank is connected with the nozzle of the main absorption spraying layer through a main absorption circulation outlet pipeline; the gas cap layer is connected with the diluted slurry tank through a connecting tube. The absorption tower is very beneficial for absorption of fume sulfur dioxide, the desulfuration efficiency is greatly improved, and under the same condition, the designed gas-liquid ratio can be reduced to a large extent, so that the power consumption of a circulation pump in operation is reduced.
Description
Technical field
The utility model relates to a kind of desulfuration absorbing tower.
Background technology
Fume desulfurating absorption tower is the device of most critical in flue gas desulfurization technique.The reasonability of absorption tower structural design is directly connected to the height of desulfuration efficiency, sorbent utilization, sub-salt oxidation efficiency and plant energy consumption.In calcium method sulfur removal technology, owing to containing more solid matter in slurries, easily fouling, deposition, therefore the spray void towers that adopt more.The feature of spray void tower is that system is less scaling, stop up, flue gas pressure drop is little, but the flue-gas temperature that enters desulfurizing tower is higher, (do not establish in the situation of GGH, flue-gas temperature is general >=and 130 ℃), carry out in the same region in desulfurizing tower that is absorbed in of flue gas cool-down and sulfur dioxide, on the one hand flue-gas temperature is high is unfavorable for the absorption of slurries to sulfur dioxide, circulation absorbs serum density higher (generally at 1.10-1.13g/cm3) on the other hand, slurry viscosity is large, be unfavorable for gas-liquid mass transfer, in order to obtain desirable desulfuration efficiency, just must realize by increasing liquid-gas ratio, this has just increased the operation power consumption of desulphurization system greatly.
In traditional spray void tower, only have a kind of slurries of density, in order to obtain enough slurries time of staying, the serum density of operation is generally higher.Entrance dry flue gas becomes saturated wet flue gas after spray-absorption, and carries a large amount of slurries, and serum density is higher, and the live load of demister is just larger, and the risk that demister fouling is stopped up is also just larger.
In addition, intermediate product calcium sulfite oxidation will along with the rising of serum density, become more difficult, under higher serum density condition, move, the oxidation effectiveness of calcium sulfite is relatively poor, in the gypsum slurries of simultaneously discharging, also wrap some unreacteds desulfurizing agent completely, these all will directly affect the quality of desulfurated plaster.
Summary of the invention
For the technical problem of above-mentioned existence, the utility model provides a kind of absorption tower for wet-type calcium desulfuration, slurry pool is divided into rare, dense two parts, utilize underflow liquid to lower the temperature in advance to flue gas, recycling dilute slurry carries out desulfurization to flue gas, not only improve the absorption efficiency of sulfur dioxide, reduced again the live load of demister.
In order to solve the problems of the technologies described above, the technical solution adopted in the utility model is: a kind of absorption tower for wet-type calcium desulfuration, comprise tower body, described tower body inside is disposed with slurry pool, gas cap layer, some main jets pouring absorbed layer, some demister layers from the bottom to top; Tower body top is provided with exhanst gas outlet, between slurry pool and gas cap layer, is provided with smoke inlet; Described slurry pool is become thin pulp liquid pool and underflow liquid pool by baffle for separating, and described thin pulp liquid pool is sealing; Between slurry pool and gas cap layer, be provided with the concentrated spraying layer of cooling, the shower nozzle on the concentrated spraying layer of described cooling concentrates loop exit pipeline by cooling and is communicated with underflow liquid pool; On described underflow liquid pool, be provided with gypsum slurries and arrange mouth outward; Described thin pulp liquid pool is connected with the shower nozzle of main absorption spraying layer by main absorption cycle outlet conduit; Described gas cap layer is connected with thin pulp liquid pool by tube connector.
As one, improve, in described thin pulp liquid pool and underflow liquid pool, be provided with aeration oxidative system; Thin pulp liquid pool top is provided with oxidation air outlet gas cap.Aeration oxidative system blasts a large amount of air, has made to absorb sulfur dioxide and has been oxidized to sulfate slurries containing the spray liquid of sulphite.
As one, improve, in described thin pulp liquid pool and underflow liquid pool, be provided with side-feeding mixer.Prevent deposition of solids, fouling.
As one, improve, described thin pulp liquid pool is connected by the concentrated loop exit pipeline of dilute slurry delivery pipe and cooling.Slurries in thin pulp liquid pool are added to the circulation of underflow liquid, reduce dense slurry solid content, to reduce the wearing and tearing to circulating line middle pump body.
As above-mentioned improvement, further improve, on described dilute slurry delivery pipe, be provided with control valve.To regulate thin pulp liquid pool to add to the liquid measure of underflow liquid pool.
As one, improve, described dividing plate comprises vertical dividing plate and covers the dividing plate at top; The described dividing plate that covers top is for being obliquely installed, and its higher one end is furnished with flusher.Avoid thin pulp liquid pool top to stop solids accumulation, fouling.
Usefulness of the present utility model is: the absorption tower with said structure, the former flue gas of high temperature that makes to enter absorption tower first enters main absorption spraying layer by gas cap layer again and removes the sulfur dioxide in flue gas after the concentrated spraying layer of lowering the temperature is fully lowered the temperature, because former dry flue gas is humidified, form saturated wet flue gas, and flue-gas temperature is reduced to approximately 60 ℃, extremely be conducive to the absorption of circulated sprinkling slurries to SO 2 from fume, greatly improve desulfuration efficiency, under equal conditions, can significantly reduce design liquid-gas ratio, thereby reduce pump operating cycle power consumption.
In addition, by dense, the thin pulp liquid pool of different densities are set, make circulation absorb slurries and move in low-density, be both conducive to gas-liquid mass transfer, be conducive to again the oxidation of calcium sulfite and the dissolving of desulfurizing agent and fully reaction, also can reduce demister fouling, stop up risk.High/low density slurry pool is arranged in to desulfurizing tower bottom simultaneously, adopts dividing plate to separate, both saved occupation of land, shortened again slurries fed distance, thereby reduce Incrustation of pipe, obstruction risk.
Slurries in underflow liquid pool are because contacting with former flue gas recirculation, and slurry pH value is reduced to a fixed value, under this pH value condition, are more conducive to separate out gypsum crystal.Meanwhile, can suitably improve this section of gypsum slurries density, reduce the slurries amount of discharging, thereby reduce the power consumption of redundance slurries in tower outer circulation, also reduce the operating load of follow-up gypsum slurries solid-liquid separating equipment.The high efficiency of bulk devulcanization system and energy-saving and cost-reducing performance find full expression.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Mark in figure: 1 smoke inlet, 2 gas cap layers, 3 main absorption spraying layers, 4 demisters, 5 exhanst gas outlets, 8 main absorption cycle outlet conduits, 9 main absorbent recirculation pumps, 11 side-feeding mixers, 12 thin pulp liquid pools, 13 flushers, 14 tube connectors, the concentrated spraying layer of 15 cooling, the concentrated loop exit pipeline of 17 cooling, the concentrated circulating pump of 18 cooling, 20 dilute slurry delivery pipes, 21 control valves, 22 aeration oxidative systems, 23 underflow liquid pools, 24 dividing plates, 25 oxidation air outlet gas caps, 26 gypsum slurries are arranged mouth outward, 27 tower bodies.
The specific embodiment
Below in conjunction with accompanying drawing, the utility model is described in detail.
In order to make the purpose of this utility model, technical scheme and advantage clearer, below in conjunction with drawings and Examples, the utility model is further elaborated.Should be appreciated that specific embodiment described herein is only in order to explain the utility model, and be not used in restriction the utility model.
As shown in Figure 1:
The utility model comprises tower body 27, and described tower body 27 inside are disposed with slurry pool, gas cap layer 2, some main jets pouring absorbed layer 3, some demister layers 4 from the bottom to top; Tower body 27 tops are provided with exhanst gas outlet 5, between slurry pool and gas cap layer 2, are provided with smoke inlet 1; Described slurry pool is separated into thin pulp liquid pool 12 and underflow liquid pool 23 by dividing plate 24, and described thin pulp liquid pool 12 is sealed by the dividing plate 24 at the dividing plate 24 of side and top; Between slurry pool and gas cap layer 2, be provided with the concentrated spraying layer 15 of cooling, shower nozzle on the concentrated spraying layer 15 of described cooling is communicated with underflow liquid pool 23 by the concentrated loop exit pipeline 17 of lowering the temperature, and is provided with the concentrated circulating pump 18 of cooling on the concentrated loop exit pipeline 17 of cooling; On described underflow liquid pool 23, be provided with gypsum slurries and arrange mouth 26 outward; Described thin pulp liquid pool 12 is connected with the shower nozzle of main absorption spraying layer 3 by main absorption cycle outlet conduit 8, is provided with main absorbent recirculation pump 9 on main absorption cycle outlet conduit 8; Described gas cap layer 2 is connected with thin pulp liquid pool 12 by tube connector 14.Can be in thin pulp liquid pool 12 and the interior aeration oxidative system 22 that arranges of underflow liquid pool 23; And oxidation air outlet gas cap 25 is set at thin pulp liquid pool 12 tops.The interior side-feeding mixer 11 that is preferably provided with of thin pulp liquid pool 12 and underflow liquid pool 23.Thin pulp liquid pool 12 can also be connected by the concentrated loop exit pipeline 17 of dilute slurry delivery pipe 20 and cooling, and on dilute slurry delivery pipe 20, control valve 21 is set.Described dividing plate 24 comprises vertical dividing plate 24 and covers the dividing plate 24 at top; The described dividing plate 24 that covers top is for being obliquely installed, and its higher one end is furnished with flusher 13.
In the time of work, flue gas enters tower body 27 from smoke inlet 1, upwards at the concentrated spraying layer 15 of cooling, contact with sprayed slurry is reverse, in smoke absorption slurries, unnecessary moisture becomes saturated wet flue gas, flue-gas temperature is significantly reduced (final identical with slurry temperature) simultaneously, saturated wet flue gas after cooling enters main absorption spraying layer 3 and reverse contact of dilute slurry (density is 1.05-1.08mg/cm3) containing desulfurizing agent spraying by gas cap layer 2, sulfur dioxide in flue gas is by spray liquid absorbing and removing, the flue gas that removes sulfur dioxide is discharged from exhanst gas outlet 5 after the moisture that major part carries is removed at demister 4 places.
The spray liquid that has absorbed sulfur dioxide becomes containing the liquid of sulphite and drops to gas cap layer 2, then enters thin pulp liquid pool 12 by gas cap layer 2 and the tube connector 14 of thin pulp liquid pool 12, and the air oxidation being blasted by aeration oxidative system 22 is sulfate slurries.Part of sulfuric acid salt slurries are the supplementary slurries as underflow liquid pool by the concentrated loop exit pipeline 17 of dilute slurry delivery pipe 20 cooling, supplement slurries amount and are automatically controlled by control valve 21; The main absorption cycle outlet conduit 8 of part of sulfuric acid salt slurries is delivered to main absorption spraying layer 3 circulated sprinklings.
Part slurries in underflow liquid pool 23 are drawn out of by the concentrated loop exit pipeline 17 of lowering the temperature that to deliver to the concentrated spraying layer 15 circulated sprinklings coolings of cooling concentrated, and part underflow liquid (1.10-1.13g/cm3) is arranged mouthfuls 26 outward by gypsum slurries and drained into gypsum dehydration system and process.
During operation, start the side-feeding mixer 11 in thin pulp liquid pool and underflow liquid pool, prevent deposition of solids, fouling.Start by set date flusher 13, rinses top spacer 24 simultaneously, prevents solid material accumulation.
The foregoing is only preferred embodiment of the present utility model; not in order to limit the utility model; all any modifications of doing within spirit of the present utility model and principle, be equal to and replace and improvement etc., within all should being included in protection domain of the present utility model.
Claims (6)
1. for an absorption tower for wet-type calcium desulfuration, comprise tower body, described tower body inside is disposed with slurry pool, gas cap layer, some main absorption spraying layers, some demister layers from the bottom to top; Tower body top is provided with exhanst gas outlet, between slurry pool and gas cap layer, is provided with smoke inlet; It is characterized in that: described slurry pool is become thin pulp liquid pool and underflow liquid pool by baffle for separating, described thin pulp liquid pool is sealing; Between slurry pool and gas cap layer, be provided with the concentrated spraying layer of cooling, the shower nozzle on the concentrated spraying layer of described cooling concentrates loop exit pipeline by cooling and is communicated with underflow liquid pool; On described underflow liquid pool, be provided with gypsum slurries and arrange mouth outward; Described thin pulp liquid pool is connected with the shower nozzle of main absorption spraying layer by main absorption cycle outlet conduit; Described gas cap layer is connected with thin pulp liquid pool by tube connector.
2. a kind of absorption tower for wet-type calcium desulfuration according to claim 1, is characterized in that: in described thin pulp liquid pool and underflow liquid pool, be provided with aeration oxidative system; Thin pulp liquid pool top is provided with oxidation air outlet gas cap.
3. a kind of absorption tower for wet-type calcium desulfuration according to claim 1, is characterized in that: in described thin pulp liquid pool and underflow liquid pool, be provided with side-feeding mixer.
4. a kind of absorption tower for wet-type calcium desulfuration according to claim 1, is characterized in that: described thin pulp liquid pool is connected by the concentrated loop exit pipeline of dilute slurry delivery pipe and cooling.
5. a kind of absorption tower for wet-type calcium desulfuration according to claim 4, is characterized in that: on described dilute slurry delivery pipe, be provided with control valve.
6. a kind of absorption tower for wet-type calcium desulfuration according to claim 1, is characterized in that: described dividing plate comprises vertical dividing plate and covers the dividing plate at top; The described dividing plate that covers top is for being obliquely installed, and its higher one end is furnished with flusher.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320636006.9U CN203577619U (en) | 2013-10-16 | 2013-10-16 | Absorption tower for desulfuration by using wet type calcium method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320636006.9U CN203577619U (en) | 2013-10-16 | 2013-10-16 | Absorption tower for desulfuration by using wet type calcium method |
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| Publication Number | Publication Date |
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| CN203577619U true CN203577619U (en) | 2014-05-07 |
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| CN201320636006.9U Expired - Lifetime CN203577619U (en) | 2013-10-16 | 2013-10-16 | Absorption tower for desulfuration by using wet type calcium method |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103495341A (en) * | 2013-10-16 | 2014-01-08 | 四川君和环保工程有限公司 | Absorption tower for wet desulfurization by calcium method |
| CN104174284A (en) * | 2014-09-15 | 2014-12-03 | 江苏峰业科技环保集团股份有限公司 | Single-tower double-loop limestone-gypsum wet-method desulfuration device and method |
| CN109381989A (en) * | 2018-11-05 | 2019-02-26 | 华电电力科学研究院有限公司 | The system and its working method of Multi-stage cooling cooperation-removal multiple pollutant in a kind of tower |
| CN110404394A (en) * | 2019-09-25 | 2019-11-05 | 山东润扬环保设备有限公司 | Ultraviolet catalytic oxidation-Fenton high efficiency composition organic waste gas treatment device and method |
-
2013
- 2013-10-16 CN CN201320636006.9U patent/CN203577619U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103495341A (en) * | 2013-10-16 | 2014-01-08 | 四川君和环保工程有限公司 | Absorption tower for wet desulfurization by calcium method |
| CN104174284A (en) * | 2014-09-15 | 2014-12-03 | 江苏峰业科技环保集团股份有限公司 | Single-tower double-loop limestone-gypsum wet-method desulfuration device and method |
| CN109381989A (en) * | 2018-11-05 | 2019-02-26 | 华电电力科学研究院有限公司 | The system and its working method of Multi-stage cooling cooperation-removal multiple pollutant in a kind of tower |
| CN110404394A (en) * | 2019-09-25 | 2019-11-05 | 山东润扬环保设备有限公司 | Ultraviolet catalytic oxidation-Fenton high efficiency composition organic waste gas treatment device and method |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: SICHUAN JUNHE ENVIRONMENTAL PROTECTION CO., LTD. Free format text: FORMER NAME: SICHUAN JUNHE ENVIRONMENTAL PROTECTION ENGINEERING CO., LTD. |
|
| CP03 | Change of name, title or address |
Address after: 614008 Sichuan high tech Zone in Leshan City, the New South Road, No. 12 Patentee after: SICHUAN JUNHE ENVIRONMENTAL PROTECTION Co.,Ltd. Address before: 614008 World Trade Center, No. 211, Fenghuang Road, central, Sichuan, Leshan, 13 Patentee before: SICHUAN JUNHE ENVIRONMENTAL PROTECTION ENGINEERING Co.,Ltd. |
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| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20140507 |