CN203108372U - Device for removing microparticles in cooperation with wet flue gas desulfurization - Google Patents

Device for removing microparticles in cooperation with wet flue gas desulfurization Download PDF

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Publication number
CN203108372U
CN203108372U CN 201220632657 CN201220632657U CN203108372U CN 203108372 U CN203108372 U CN 203108372U CN 201220632657 CN201220632657 CN 201220632657 CN 201220632657 U CN201220632657 U CN 201220632657U CN 203108372 U CN203108372 U CN 203108372U
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CN
China
Prior art keywords
flue
flue gas
outlet
wet
desulfurization
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CN 201220632657
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Chinese (zh)
Inventor
高继贤
洪小松
阎冬
张小娟
杨春琪
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上海龙净环保科技工程有限公司
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Priority to CN 201220632657 priority Critical patent/CN203108372U/en
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Publication of CN203108372U publication Critical patent/CN203108372U/en

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Abstract

The utility model discloses a device for removing microparticles in cooperation with wet flue gas desulfurization. The device can be used for effectively controlling emission of microparticles, such as PM2.5. The device is characterized in that the outlet of an absorption tower is connected with a diverging pipe at the inlet end of a desulfurized clean gas flue; the outlet end of the desulfurized clean gas flue is connected with a reducing pipe of the flue outlet; and a flue gas distributor, a steam spray nozzle, a clapboard, a washing process water spray nozzle, a flue water collecting port and a flue demister are sequentially arranged between the outlet end of the desulfurized clean gas flue and the reducing pipe of the flue outlet along the flowing direction of flue gas. As the wet desulfuration device is improved, a steam phase change area is built in the desulfurized clean gas flue, the microparticles, such as PM2.5 are coagulated to grow; and meanwhile, an impinging stream technology is utilized, so that microparticles in oversaturated flue gas further collide and coagulate to grow and are finally removed by the flue demister arranged in the flue. According to the device disclosed by the utility model, the desulfurized clean gas flue of the wet desulfuration device is subjected to simple modification, so that the removal effect of the microparticles is good, no new reactor is increased, and the equipment investment and building cost are saved.

Description

A kind of device of wet process of FGD cooperation-removal subparticle
Technical field
The utility model belongs to the control technology field of fine particle in the flue gas, particularly a kind of device of wet process of FGD cooperation-removal fine particle.
Background technology
In wet process of FGD (WFGD) process, on the one hand, but by the particle in the cleaning function cooperation-removal flue gas of desulfurization slurry; Simultaneously, the desulfurization slurry atomizing is carried secretly, the desulfurization product crystallization is separated out owing to exist, and the SO in desulfurizing agent/fine particle and the flue gas 2Deng the complicated heterogeneous reaction process between the gaseous component, itself may form the PM that diameter is less than or equal to 2.5 microns again 2.5Fine particle.And PM 2.5Fine particle is though particle diameter is little, bigger to the influence of health and atmosphere quality.In February, 2012, State Council is agreed in " ambient air quality " of issue PM 2.5Classify one of monitoring index as.But, at present in the common wet process of FGD engineering in coal-burning power plant to PM 2.5Treatment effect often not good.
Mechanism according to steam phase transforming impels fine particle to condense to grow up combines the steam phase transforming technology with existing coal-burning boiler wet process of FGD technology, can effectively control the discharging of subparticle in the flue gas.The technology of growing up but this promotion flue gas desulfurization fine particle condenses, usually need increase smoke moisture conditioning chamber and phase transformation condensing chamber in the smoke-gas wet desulfurization device existing the setting, yet the indoor steam of phase transformation and contain the fine particle flue gas and mix inhomogeneous, not only increased cost of equipment, fail in the fine particle surface condensation because of many steam simultaneously, and cause fine particle directly to be taken away by flue gas.
Summary of the invention
The purpose of this utility model is: the device and method that removes that fine particle in a kind of wet process of FGD is provided, take full advantage of the existing clean flue of desulfurization space, applying steam phase transformation and percussion flow technology are impelled fine particle to condense to grow up the subparticle in the cooperation-removal wet process of FGD.
For achieving the above object, the technical scheme that Bian uses is: a kind of device of wet process of FGD cooperation-removal subparticle, comprise wet flue gas desulfurization absorption tower, it is characterized in that: the desulfuration absorbing tower outlet is connected with the clean chimney intake end of desulfurization increaser, the clean flue outlet end of described desulfurization is connected with the flue outlet reducing pipe, is disposed with flue gas even distribution device, steam jet, dividing plate, cleaning (operating) water nozzle, flue inlet and flue demister along flue gas flow direction therebetween; Interface has carried out the long-pending fractionation of uiform section, has engaged before and after the described flue gas even distribution device, flue gas is evenly expanded flow to the flue enlarged area; Described dividing plate inclined-plane and flow of flue gas angular separation are the α angle lapping and tiltedly arrange.
Described α angle is between 15 °~45 °, or between 135 °~165 °.
At least 3 on the described dividing plate that is obliquely installed is etc. the equidistant setting of gradient.
Interface is crisscross grid-like fractionation, amalgamation before and after the described flue gas even distribution device, and it is 4 that each cross section vertical with flue gas flow direction splits the zone minimum.
Described device carries out the method for cooperation-removal subparticle, it is characterized in that:
⑴ former flue gas enters the clean flue of desulfurization from the desulfuration absorbing tower outlet after wet desulphurization, after the flue gas even distribution device is uniform, evenly mix with the saturated vapor that injects flue, and flue gas reaches hypersaturated state, and the subparticle in the flue gas condenses and grows up;
⑵ the while, when the supersaturation flue gas passed through the area of diaphragm that is obliquely installed, surface condensation had the fine particle of moisture film that bump mutually takes place between dividing plate, fine particle is further condensed grow up;
⑶ flow velocity control is at 2~7m/s during flue gas process flue demister, and the fine particle that the flue demister is grown up to condensing effectively catches, and discharges from flue outlet then.
Described wet fuel gas desulfurizing technology refers to any one in limestone-gypsum method, two alkaline process, seawater method, soda method, magnesium oxide method, the ammonia process.Its flue gas after desulfurization of such technology all has very high moisture content, sprays into a spot of saturated vapor by the steam jet that is arranged in the clean flue of desulfurization, sets up PM 2.5Deng the subparticle supersaturated vapor environment of growing up required that condenses, fine particle is condensed grow up.
The beneficial effects of the utility model are: by wet desulphurization device is improved, set up a steam phase transforming district in the clean flue of desulfurization, spray into a spot of saturated vapor from steam jet, set up PM 2.5Deng the subparticle supersaturated vapor environment of growing up required that condenses, utilize the percussion flow technology simultaneously, at flue gas and the even Mixed Zone of supersaturated vapor dividing plate is set, make the fine particle in the supersaturation flue gas that collision mutually take place between dividing plate, fine particle is further condensed grow up, removed by the flue demister that is arranged in the flue at last.The utility model is set up steam phase transforming district and collision coalescence district by to simply transforming in the clean flue of the desulfurization of wet desulphurization device, and it is effective to remove subparticle, equipment investment and cost saving.
Description of drawings
Below in conjunction with accompanying drawing and case study on implementation, the utility model is described in further detail.
Fig. 1 is the apparatus structure schematic diagram of cooperation-removal subparticle in a kind of wet process of FGD of the utility model;
Fig. 2 be among Fig. 1 flue gas even distribution device A-A to the cross section structure schematic diagram;
Fig. 3 be among Fig. 1 flue gas even distribution device B-B to the cross section structure schematic diagram;
Fig. 4 is that buffler tilt alpha angle arranges the structural configuration schematic diagram among Fig. 1;
Fig. 5 be among Fig. 1 buffler C-C to the cross section structure schematic diagram.
Among the figure, the 1-desulfuration absorbing tower; 2-absorbent entrance; 3-absorbent circulating pump; The former smoke inlet of 4-; The 5-spraying layer; Demister cleaning (operating) water nozzle in the 6-tower; Demister in the 7-tower; The clean flue of 8-desulfurization; 9-flue gas even distribution device; The 10-steam jet; The 11-dividing plate; 12-flue demister cleaning (operating) water nozzle; 13-flue inlet; 14-flue demister; The 15-flue outlet.
The specific embodiment
Fig. 1 is the apparatus structure schematic diagram of a kind of wet process of FGD cooperation-removal of the utility model subparticle, as shown in the figure, this device comprises wet flue gas desulfurization absorption tower 1, it is characterized in that: desulfuration absorbing tower 1 outlet is connected with the clean flue 8 entrance point increasers of desulfurization, clean flue 8 ports of export of described desulfurization are connected with flue outlet 15 reducing pipes, are disposed with flue gas even distribution device 9, steam jet 10, dividing plate 11, cleaning (operating) water nozzle 12, flue inlet 13 and flue demister 14 along flue gas flow direction therebetween; Described flue gas even distribution device 9 front and back interfaces have carried out the long-pending fractionation of uiform section, have engaged, and flue gas is evenly expanded flow to the flue enlarged area; Described dividing plate inclined-plane and flow of flue gas angular separation are the α angle lapping and tiltedly arrange.
Former flue gas enters the SO of desulfurizing tower 1 from the smoke inlet 4 of desulfuration absorbing tower 1 2The uptake zone II, the SO in the flue gas 2Be desulfurized the desulfurization absorbent absorption that absorption tower 1 spraying layer 5 sprays out, and it is oxidized in reaction zone I at the bottom of the tower, desulfurization absorbent adds from reaction zone I bottom absorbent entrance 2, pump into spraying layer through absorbent circulating pump 3, flue gas after the desulfurization after demister 7 demists, enters the clean flue 8 of desulfurization through flue gas even distribution device 9 in desulfurizing tower, evenly mix with the saturated vapor that injects from steam jet 10, reach hypersaturated state, the fine particle in the flue gas condenses and grows up; Simultaneously, when the supersaturation flue gas through 3 dividing plates 11 that being arranged in the clean flue 8 of desulfurization, surface condensation has the fine particle of moisture film to produce bump on 11 on 3 dividing plates, fine particle further condenses and grows up, and the fine particle of growing up that condenses is removed by flue demister 14 captures that are arranged in the clean flue 8 of desulfurization; The cleaning water of flue demister cleaning (operating) water nozzle 12 ejections flows out from flue inlet 13 behind the cleaning flue.
The visible described flue gas even distribution device 9 of Fig. 1 is arranged between the expansion district interface of desulfuration absorbing tower 1 outlet and the clean chimney intake end of desulfurization increaser, and interface is crisscross grid-like fractionation, amalgamation before and after the described flue gas even distribution device.Fig. 2, Fig. 3 are the cross section structure schematic diagram at described flue gas even distribution device 9 two ends, for making flue gas can evenly diffuse to the flue enlarged area preferably, described flue gas even distribution device 9 front and back interfaces have carried out the long-pending fractionation of uiform section, engage, and its fractionation zone of Fig. 2 and diagram shown in Figure 3 is 16.It is 4 that each cross section vertical with flue gas flow direction splits the zone minimum.
Described buffler 11, be arranged at clean flue gas and the even Mixed Zone of supersaturated vapor (Fig. 1) in the clean flue 8 of desulfurization, Fig. 4 and visible buffler shown in Figure 5 11 are tilting, and and flow of flue gas angular separation α is between 15 °~45 °, or between 135 °~165 °, for strengthening the fine particle impact effects, dividing plate 11 quantity arrange 3 at least, and material is selected for use and is polypropylene plastics anticorrosion corrosion resistant materials such as (PP).
Described flue demister 14 is arranged in clean flue 8 ports of export of desulfurization, and flue gas is controlled at 2-5m/s by the flow velocity of this demister, and flue demister 14 can adopt baffle plate demister, eddy flow plate demister or mesh mist eliminator.
In order to further specify system effect of the present utility model, we have carried out the case design:
Embodiment 1:
Serve as to handle object with certain fire coal boiler fume, this flue gas exhaust gas volumn is 1.0 * 10 5Nm 3/ h, former flue gas cigarette temperature is 118 ℃, desulfurizing tower import flue dust mass concentration is 70mg/Nm 3, SO 2Concentration 1747 mg/Nm 3, be absorbent with the lime stone slurry, clean flue gas uniform device 9 cross sections are divided into 16 by homalographic, and to be provided with 3 be 30 ° of bufflers 11 with the flow of flue gas angular separation, and spraying into quantity of steam in the steam phase transforming district is 0.04kg/Nm 3Flue gas after treatment, chimney breast cigarette temperature is 49 ℃, the flue dust mass concentration is 28mg/Nm 3, reach smoke dust discharge concentration that " thermal power plant's air pollution emission standard " (GB13233-2011) stipulate less than 30mg/Nm 3Discharge standard, SO 2Concentration 68mg/Nm 3, desulfuration efficiency is 96.1%, fine particle concentration is 1.23 * 10 in the flue gas 7Individual/cm 3
Comparative Examples 1:
Adopt embodiment 1 used flue gas, flue is not carried out any transformation, after the desulfurization, outlet flue gas flue dust mass concentration is 60mg/Nm 3, do not reach smoke dust discharge concentration that " thermal power plant's air pollution emission standard " (GB13233-2011) stipulate less than 30mg/Nm 3Discharge standard, SO 2Concentration 70mg/Nm 3, desulfuration efficiency is 96%, fine particle concentration is 4.53 * 10 in the flue gas 7Individual/cm 3
Comparative Examples 2:
Adopt embodiment 1 used flue gas, set up a steam phase transforming zone at flue, but flue gas even distribution device and buffler are not set, flue gas after treatment, outlet flue gas flue dust mass concentration is 35mg/Nm 3, do not reach smoke dust discharge concentration that " thermal power plant's air pollution emission standard " (GB13233-2011) stipulate less than 30mg/Nm 3Discharge standard, SO 2Concentration 68mg/Nm 3, desulfuration efficiency is 96.1%, fine particle concentration is 1.94 * 10 in the flue gas 7Individual/cm 3
As seen embodiment 1 compares with Comparative Examples 1, the utility model is by to simply transforming in the clean flue 8 of the desulfurization of wet desulphurization device, take full advantage of the existing clean flue of desulfurization space, set up steam phase transforming district and collision coalescence district, applying steam phase transformation and percussion flow technology are impelled fine particle to condense to grow up, subparticle in the cooperation-removal wet process of FGD, effective, low equipment investment.Comparative Examples 2 is only set up a steam phase transforming zone at flue, but flue gas even distribution device and buffler are not set, and is poor slightly with embodiment 1 contrast effect.

Claims (3)

1. the device of a wet process of FGD cooperation-removal subparticle, comprise wet flue gas desulfurization absorption tower, it is characterized in that: the desulfuration absorbing tower outlet is connected with the clean chimney intake end of desulfurization increaser, the clean flue outlet end of described desulfurization is connected with the flue outlet reducing pipe, is disposed with flue gas even distribution device, steam jet, dividing plate, cleaning (operating) water nozzle, flue inlet and flue demister along flue gas flow direction therebetween; Interface has carried out the long-pending fractionation of uiform section, has engaged before and after the described flue gas even distribution device, flue gas is evenly expanded flow to the flue enlarged area; Described dividing plate inclined-plane and flow of flue gas angular separation are the α angle lapping and tiltedly arrange, and described α angle is between 15 °~45 °, or between 135 °~165 °.
2. according to the device of the described a kind of wet process of FGD cooperation-removal subparticle of claim 1, it is characterized in that: at least 3 on the described dividing plate that is obliquely installed, etc. the equidistant setting of gradient.
3. according to the device of the described a kind of wet process of FGD cooperation-removal subparticle of claim 1, it is characterized in that: interface is crisscross grid-like fractionation, amalgamation before and after the described flue gas even distribution device, and it is 4 that each cross section vertical with flue gas flow direction splits the zone minimum.
CN 201220632657 2012-11-27 2012-11-27 Device for removing microparticles in cooperation with wet flue gas desulfurization CN203108372U (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102961943A (en) * 2012-11-27 2013-03-13 上海龙净环保科技工程有限公司 Method and device for synergistically removing fine particles via wet-process flue gas desulfurization
CN106362535A (en) * 2016-11-03 2017-02-01 东南大学 Device and method for building supersaturation field based on phase transformation strengthening

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102961943A (en) * 2012-11-27 2013-03-13 上海龙净环保科技工程有限公司 Method and device for synergistically removing fine particles via wet-process flue gas desulfurization
CN102961943B (en) * 2012-11-27 2015-03-11 上海龙净环保科技工程有限公司 Method and device for synergistically removing fine particles via wet-process flue gas desulfurization
CN106362535A (en) * 2016-11-03 2017-02-01 东南大学 Device and method for building supersaturation field based on phase transformation strengthening
CN106362535B (en) * 2016-11-03 2019-03-05 东南大学 A kind of device and method based on the building of steam phase transformation strengthening supersaturation field

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Granted publication date: 20130807

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