CN116251428B - Wet flue gas desulfurization dust collector based on tympanic bulla unit - Google Patents
Wet flue gas desulfurization dust collector based on tympanic bulla unit Download PDFInfo
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- CN116251428B CN116251428B CN202310296545.0A CN202310296545A CN116251428B CN 116251428 B CN116251428 B CN 116251428B CN 202310296545 A CN202310296545 A CN 202310296545A CN 116251428 B CN116251428 B CN 116251428B
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- flue gas
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 115
- 239000003546 flue gas Substances 0.000 title claims abstract description 111
- 239000000428 dust Substances 0.000 title claims abstract description 52
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 43
- 230000023556 desulfurization Effects 0.000 title claims abstract description 43
- 241000197194 Bulla Species 0.000 title claims description 4
- 208000002352 blister Diseases 0.000 title claims description 4
- 230000005587 bubbling Effects 0.000 claims abstract description 69
- 238000005507 spraying Methods 0.000 claims abstract description 52
- 239000002002 slurry Substances 0.000 claims abstract description 37
- 239000000498 cooling water Substances 0.000 claims abstract description 36
- 239000007788 liquid Substances 0.000 claims abstract description 33
- 239000002245 particle Substances 0.000 claims abstract description 26
- 235000019738 Limestone Nutrition 0.000 claims abstract description 13
- 239000006028 limestone Substances 0.000 claims abstract description 13
- 230000000712 assembly Effects 0.000 claims abstract 3
- 238000000429 assembly Methods 0.000 claims abstract 3
- 238000001816 cooling Methods 0.000 claims description 37
- 239000002918 waste heat Substances 0.000 claims description 21
- 239000007789 gas Substances 0.000 claims description 16
- 238000005057 refrigeration Methods 0.000 claims description 13
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 claims description 6
- 229910010271 silicon carbide Inorganic materials 0.000 claims description 6
- 229910001256 stainless steel alloy Inorganic materials 0.000 claims description 6
- 230000002708 enhancing effect Effects 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 3
- 239000003344 environmental pollutant Substances 0.000 abstract description 8
- 231100000719 pollutant Toxicity 0.000 abstract description 8
- 239000000779 smoke Substances 0.000 abstract description 6
- 239000010410 layer Substances 0.000 description 39
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 13
- 238000000034 method Methods 0.000 description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 239000013618 particulate matter Substances 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 239000003507 refrigerant Substances 0.000 description 7
- 238000007599 discharging Methods 0.000 description 5
- 239000010440 gypsum Substances 0.000 description 5
- 229910052602 gypsum Inorganic materials 0.000 description 5
- 238000005192 partition Methods 0.000 description 5
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000010248 power generation Methods 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 230000002195 synergetic effect Effects 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 239000012717 electrostatic precipitator Substances 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
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- 239000002244 precipitate Substances 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- LVGUZGTVOIAKKC-UHFFFAOYSA-N 1,1,1,2-tetrafluoroethane Chemical compound FCC(F)(F)F LVGUZGTVOIAKKC-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000001154 acute effect Effects 0.000 description 1
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000010261 calcium sulphite Nutrition 0.000 description 1
- JXRVKYBCWUJJBP-UHFFFAOYSA-L calcium;hydrogen sulfate Chemical compound [Ca+2].OS([O-])(=O)=O.OS([O-])(=O)=O JXRVKYBCWUJJBP-UHFFFAOYSA-L 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
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- 230000007613 environmental effect Effects 0.000 description 1
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- HJUFTIJOISQSKQ-UHFFFAOYSA-N fenoxycarb Chemical compound C1=CC(OCCNC(=O)OCC)=CC=C1OC1=CC=CC=C1 HJUFTIJOISQSKQ-UHFFFAOYSA-N 0.000 description 1
- 229920002313 fluoropolymer Polymers 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 229910000856 hastalloy Inorganic materials 0.000 description 1
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/02—Separating dispersed particles from gases, air or vapours by liquid as separating agent by passing the gas or air or vapour over or through a liquid bath
- B01D47/021—Separating dispersed particles from gases, air or vapours by liquid as separating agent by passing the gas or air or vapour over or through a liquid bath by bubbling the gas through a liquid bath
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (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)
- Treating Waste Gases (AREA)
Abstract
The invention provides a wet flue gas desulfurization dust removal device based on a bubbling unit, which belongs to the field of pollutant control and comprises a tower body, and a slurry pool, a spraying layer, the bubbling unit and a demister which are arranged in the tower body from bottom to top, wherein: the side surface of the tower body is provided with a smoke inlet, and the top surface is provided with a smoke outlet; limestone slurry for desulfurization is arranged in the slurry pond; the spraying layer is used for spraying limestone slurry; the bubbling unit comprises a plurality of dust removal assemblies which are arranged in parallel, a flow guide pipe in the dust removal assembly is arranged above the liquid holding bubbling tank and extends into the liquid holding bubbling tank, and cooling water is arranged in the liquid holding bubbling tank; the defroster sets up in the below of flue gas export. The invention uses the cooling water to cool the saturated flue gas, and forms bubbles by bubbling, so that the condensable particles and filterable particles in the flue gas are deeply removed, a wet electric dust collector is not needed, the dust collection cost is effectively reduced, and the invention has a great engineering application value.
Description
Technical Field
The invention belongs to the field of pollutant control, and in particular relates to a wet flue gas desulfurization and dust removal device based on a bubbling unit.
Background
The International Institute of Application and Systems Analysis (IIASA) has shown that large combustion can bring about 10% of particulate emissions worldwide (ECLIPSE V6b global emission fields, 2019). The China is used as a large country of coal-fired power generation, so far, the coal-fired power generation still accounts for more than 60% of the total power generation amount of the China. Meanwhile, the method is not only coal-fired power generation, but also fossil fuels are widely applied to chemical industry and metallurgy in China. Thus, there is a need for controlling particulate emissions during combustion.
The particulate matters generated by combustion can be divided into Filterable Particulate Matters (FPM) and Condensable Particulate Matters (CPM) according to the emission types of the particulate matters, wherein the filterable particulate matters are particulate pollutants in a flue, and are mainly fly ash particulate matters crushed after fire coal is combusted in a hearth; the condensable particulate matter refers to gaseous pollutants in the flue, and when the flue gas is discharged into the atmosphere from the flue, the flue gas is cooled and condensed into the particulate matter. For purifying the coal-fired particulate matters, an electrostatic precipitator (ESP)/cloth bag dust collector (FFs) device is commonly adopted in China, and the filterable particulate matters in the coal-fired flue gas can be reduced to 5mg/m by combining a wet electric precipitator (WESP) device 3 The following is given. However, the traditional test usually ignores the influence of condensable particles, the WESP device has complex equipment, high construction cost and operation cost, the efficiency in the operation process can not reach the design value (more than 90 percent), the dust removal efficiency is only about 60 to 70 percent, and the enterprise is brought with higher efficiencyThe ultra-clean emission is not achieved at the same time of large economic burden.
The flue gas has certain purifying capacity to the particulate matters in the flue gas through a Wet Flue Gas Desulfurization (WFGD) device, but the removing performance is low for PM2.5 particles, so that the particulate matters are cooperatively removed by installing a WESP device after the WFGD in the prior art. After the WFGD system, the temperature of the flue gas is reduced to 40-60 ℃ under the cooling action of the desulfurization slurry, part of condensable particles can be condensed and separated out in the flue gas and then trapped by a WESP device, but the cooling temperature is still higher than the atmospheric temperature. A plurality of tests show that the concentration of condensable particles discharged by the purified coal-fired flue gas is concentrated at 5mg/Nm 3 ～20mg/Nm 3 And is not negligible.
Aiming at the problems that the efficiency of removing particles by a WESP device is low and the CPM cannot be removed efficiently, the existing solution is mainly to arrange a water-cooling heat exchanger above a WFGD spraying layer or in a flue after the WFGD, so that the temperature of flue gas is reduced, and condensable particles are removed through the WESP at the rear end after condensation. For example, CN109737439B discloses a water-cooling-whitening device for removing condensable pollutants and reclaimed water in flue gas, CN104707432B discloses a system and a method for cooperatively removing dust and condensable particles in flue gas, the above systems all utilize the humidification characteristic of WFGD on flue gas, after flue gas is sprayed by the WFGD system, water vapor in flue gas is saturated, and at the outlet of WFGD, a condensation cooling method is adopted to make flue gas in a supersaturated state so as to enable FPM to grow up, and the flue gas is removed by WESP. CPM also adopts the cooling at desulfurizing tower exit to make the flue gas be in supersaturation state and precipitate and nucleate, and is got rid of through WESP. The adoption of the cooling method has certain removal performance for the FPM and CPM, the removal efficiency is determined according to the cooling depth and the particle growth characteristics, but the WESP device has high operation cost and construction cost, and the above methods are finished under the cooperation of the WESP device, so that the problem of high production cost exists.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a wet flue gas desulfurization and dust removal device based on a bubbling unit, and aims to solve the problem that the production cost is too high due to the fact that the existing wet flue gas desulfurization device relies on a wet electric dust removal device to remove particles.
In order to achieve the above purpose, the invention provides a wet flue gas desulfurization and dust removal device based on a bubbling unit, which comprises a tower body, and a slurry pool, a spraying layer, the bubbling unit and a demister which are sequentially arranged in the tower body from bottom to top, wherein: a flue gas inlet is formed in the side face of the tower body, the flue gas inlet is positioned between the slurry pool and the spraying layer, and a flue gas outlet is formed in the top face of the tower body; limestone slurry for desulfurization is arranged in the slurry pool; the spraying layer is used for spraying limestone slurry to realize wet flue gas desulfurization; the bubbling unit comprises a plurality of dust removing components which are arranged in parallel, the dust removing components comprise drainage plates, a bottom plate, a liquid holding bubbling tank, a flow guide plate and a flow guide pipe, and the drainage plates are connected with the upper bottom plate and the lower bottom plate at staggered intervals to form a serpentine flue gas channel; the liquid holding bubbling pond is arranged between two adjacent drainage plates and connected with a bottom plate below, and cooling water is arranged in the liquid holding bubbling pond; the guide plate is provided with holes and is connected with the guide pipe so as to introduce the flue gas into the guide pipe through the guide plate, and meanwhile, the guide plate is arranged above the liquid-holding bubbling pond and is connected with two adjacent guide plates so as to fix the guide pipe; the draft tube stretches into the liquid level of the liquid holding bubbling pond and is used for introducing the flue gas into cooling water and forming bubbles, so that particles are trapped and dust removal is realized; the demister is arranged between the flue gas outlet and the bubbling unit and is used for removing fog drops in flue gas.
Further preferably, the distance between the bottom of the draft tube and the bottom of the liquid holding bubbling tank is 0 mm-10 mm.
As a further preferable mode, the diameter of the flow guide pipe is 20 mm-200 mm, the flow guide pipe is provided with air outlet holes, the aperture of the air outlet holes is 1 mm-10 mm, and the aperture ratio of the flow guide pipe is 15% -50%.
As a further preferred aspect, the wet flue gas desulfurization dust removal device further includes a cooling pipe, the cooling pipe is disposed between the bubbling unit and the spraying layer, and is used for introducing cooling water to realize preliminary cooling of flue gas.
As a further preferred aspect, the cooling tube comprises a plurality of stainless steel alloy tube bundles arranged in parallel, wherein the diameter of the stainless steel alloy tube bundles is 30 mm-300 mm, and the tube spacing is 10 mm-100 mm.
As a further preferred aspect, the wet flue gas desulfurization dust removal device further includes a waste heat refrigeration unit, the waste heat refrigeration unit includes a heat exchange component and a refrigeration component, and the heat exchange component is connected with the flue gas inlet to absorb waste heat of the flue gas; the refrigerating assembly is used for cooling the cooling water by utilizing waste heat.
As a further preferred aspect, the wet flue gas desulfurization dust removal device further comprises a tray, wherein the tray is arranged between the spraying layer and the slurry pool and is used for enhancing the gas-liquid contact time.
As a further preferable mode, the wet flue gas desulfurization dust removal device further comprises a gas collecting ring, wherein the gas collecting ring is arranged below the spraying layer and is used for collecting flue gas towards the center in the tower.
As a further preferable mode, the number of the spraying layers is 1-4, the spraying layers are arranged in a crossing way, the spraying nozzles in the same spraying layer are arranged in concentric circles, and the spraying angle of the spraying nozzles in the spraying layer is 45-135 degrees.
Further preferably, the nozzle is a silicon carbide solid conical nozzle or a silicon carbide hollow conical nozzle, and the coverage rate of the spray layer is 200-300%.
In general, the above technical solutions conceived by the present invention have the following compared with the prior art
The beneficial effects are that:
1. according to the invention, the bubbling unit is arranged between the demister and the spraying layer, so that the flue gas is guided into the honeycomb duct and extends into the liquid-holding bubbling pond to form bubbles, on one hand, the cooling water is used for cooling saturated flue gas, and on the other hand, bubbles are formed through bubbling, so that condensable particles and filterable particles in the flue gas are deeply removed, a wet electric dust collector is not needed, the dust collection cost is effectively reduced, and the method has a large engineering application value;
2. meanwhile, the invention improves the parameters of the bubbling unit, effectively reduces the size of bubbles by using the flow guide pipe, enhances the gas-liquid mass transfer coefficient and enhances the trapping efficiency of particles by the liquid film, thereby enhancing the synergistic removal effect of multiple pollutants;
3. particularly, the cooling pipe is arranged between the bubbling unit and the spraying layer, and cooling water is introduced, so that saturated flue gas can be cooled, long and large condensable particles can be effectively condensed, and the particles which can be filtered are also long and large due to the supersaturation characteristic in the cooling process, so that the particles are easier to remove;
4. in addition, the waste heat refrigerating unit is arranged to cool the cooling water by using the waste heat of the flue gas, so that the recycling of the waste heat of the flue gas can be realized, the energy utilization rate is effectively improved, and the production cost is reduced.
Drawings
Fig. 1 is a schematic structural diagram of a wet flue gas desulfurization dust removal device based on a bubbling unit according to an embodiment of the present invention;
fig. 2 is a schematic structural diagram of a bubbling unit according to an embodiment of the present invention;
fig. 3 is a schematic diagram of a dust removal mechanism of a bubbling unit according to an embodiment of the present invention.
The same reference numbers are used throughout the drawings to reference like elements or structures, wherein:
the device comprises a slurry pond, a 2-tray, a 3-gas gathering ring, a 4-spraying layer, a 5-cooling pipe, a 6-bubbling unit, a 6.1-flow guiding plate, a 6.2-liquid holding bubbling pond, a 6.3-flow guiding pipe, a 6.4-flow guiding plate, 6.5-smoke, a 6.6-bottom plate, a 7-demister, an 8-induced draft fan, a 9-smoke outlet, a 10-waste heat refrigerating unit and an 11-cooling water pond.
Detailed Description
The present invention will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
As shown in fig. 1 and 2, the invention provides a wet flue gas desulfurization and dust removal device based on a bubbling unit, which comprises a tower body, and a slurry pool 1, a spraying layer 4, a bubbling unit 6 and a demister 7 which are sequentially arranged in the tower body from bottom to top, wherein:
the tower body is vertically arranged, the height of the tower body is determined according to the number of 4 layers of spraying layers and the gas residence time which are required to be arranged, and the height is preferably 15-40 m; a flue gas inlet is formed in the side face of the tower body, is positioned between the slurry pond 1 and the spraying layer 4, is connected with a flue gas inlet pipe through a draught fan 8 and is used for introducing flue gas 6.5 to be treated; the included angle between the flue gas inlet and the ground is 5-15 degrees; meanwhile, a flue gas outlet 9 is formed in the top surface of the tower body and is used for discharging the treated flue gas 6.5;
the slurry pond 1 is positioned at the bottom of the wet flue gas desulfurization dust removal device, and internally comprises limestone slurry for desulfurization, a stirrer and a forced oxidation fan, and is connected with a limestone slurry feeding assembly, a gypsum discharging assembly, a slurry circulating pump and a process water adding assembly; the gypsum discharging assembly is used for timely discharging oxidized calcium sulfate crystals, enabling the oxidized calcium sulfate crystals to enter a gypsum storage room for standing after passing through a gypsum cyclone station and a vacuum belt dehydrator, and enabling the humidity of dehydrated gypsum to be less than 10%; the slurry circulating pump is used for pumping limestone slurry in the slurry tank 1 into the spraying layer 4, and preferably a single-suction horizontal centrifugal pump is adopted; the forced oxidation fan is used for forced oxidation of the calcium sulfite and the calcium bisulfate in the slurry pond 1, and is preferably a Roots blower; the stirrer is used for mixing limestone slurry in the slurry pond 1 and strengthening dissolution of calcium carbonate so as to avoid limestone precipitation; monitoring the pH of the slurry pool 1 in the operation process, and adjusting the pH of the slurry pool 1 by adjusting the concentration of limestone in fresh slurry, wherein the pH is preferably 5-5.8, and the calcium-sulfur ratio is 1.03-1.1;
the spraying layers 4 are used for spraying limestone slurry to realize wet flue gas desulfurization, the number of layers of the spraying layers 4 is 1-4, the spraying layers 4 are arranged in a crossing way, all the nozzles in the same spraying layer 4 are arranged in concentric circles, the spraying angle of the nozzles in the spraying layers 4 is 45-135 degrees, the nozzles are silicon carbide solid conical nozzles or silicon carbide hollow conical nozzles, and the coverage rate of the spraying layers 4 is 200-300%;
the bubbling unit 6 comprises a plurality of dust removing components which are arranged in parallel, wherein the dust removing components comprise a bottom plate 6.6, a drainage plate 6.1, a liquid holding bubbling tank 6.2, a guide plate 6.4 and a guide pipe 6.3, the upper bottom plate 6 and the lower bottom plate 6.6 are arranged in a staggered mode in the horizontal direction, and the drainage plate 6.1 is connected with the upper bottom plate 6 and the lower bottom plate 6 at staggered intervals to form a snake-shaped flue gas channel for guiding and guiding flue gas; the liquid-holding bubbling pond 6.2 is arranged between two adjacent drainage plates 6.1 and connected with a bottom plate 6.6 below, cooling water used as particulate matter trapping washing liquid is arranged in the liquid-holding bubbling pond, and a side surface of the liquid-holding bubbling pond 6.2 is provided with holes for ensuring the flow of flue gas 6.5; the guide plate 6.4 is provided with holes and is connected with the guide pipe 6.3 so as to introduce the flue gas into the guide pipe 6.3 through the guide plate 6.4, and meanwhile, the guide plate 6.4 is arranged above the liquid-holding bubbling tank 6.2 and is connected with two adjacent guide plates 6.1 so as to fix the guide pipe 6.3; the flow guide pipe 6.3 stretches into the liquid level of the liquid-holding bubbling pond 6.2 and is used for introducing cooling water into the flue gas 6.5 to form bubbles, so that particles are trapped to realize dust removal, the size of the bubbles can be effectively reduced by the flow guide pipe 6.3, the gas-liquid mass transfer coefficient is enhanced, and meanwhile, the trapping efficiency of the particles by a liquid film is enhanced, so that the synergistic removal effect of multiple pollutants is enhanced;
the demister 7 is arranged between the flue gas outlet and the bubbling unit 6 and is positioned at the top of the tower body and used for efficiently separating desulfurization slurry and partial particulate matters carried by flue gas, and the demister 7 is one or more of a tube bundle demister, a ridge type demister, a wire mesh demister and a baffle plate demister.
Further, the distance between the bottom of the flow guide pipe 6.3 and the bottom of the liquid holding bubbling tank 6.2 is 0 mm-10 mm. The diameter of the flow guide pipe 6.3 is 20 mm-200 mm, the aperture ratio of the flow guide pipe 6.3 on the flow guide plate 6.4 is 30% -50%, the flow guide pipe 6.3 is composed of a plurality of uniformly distributed air outlet holes, the aperture of each air outlet hole is 1 mm-10 mm, in order to fully improve the pollutant purifying effect, the aperture of each air outlet hole is preferably 1/20-1/10 of the diameter of the flow guide pipe, the aperture ratio of the flow guide pipe 6.3 is 15% -50%, and the aperture ratio and the diameter of the flow guide pipe 6.3 are in nonlinear negative correlation. Through the interaction of the parameters, the size of bubbles can be effectively optimized, the gas-liquid mass transfer coefficient is enhanced, meanwhile, the trapping probability of particles by a liquid film is enhanced, the multi-pollution synergistic removal effect is enhanced, and the proper pressure drop is obtained. The aperture ratio of the guide plate 6.4 is maintained to be 40%, the diameter of the guide pipe 6.3 is 40mm, the aperture of the air outlet hole is 10mm, the aperture ratio is 40%, the liquid level height is 50mm, when the guide pipe stretches into the liquid level to be 30mm, the particulate removal efficiency can be realized to be more than 80%, and the pressure drop is lower than 200Pa.
Further, the wet flue gas desulfurization dust removal device further comprises a cooling pipe 5, wherein the cooling pipe 5 is arranged between the bubbling unit 6 and the spraying layer 4 and is used for introducing cooling water to realize preliminary cooling of flue gas. The cooling pipe 5 comprises a preset number of stainless steel alloy pipe bundles which are arranged in parallel, two ends of each pipe bundle transversely penetrate through the tower body, and low-temperature water enters from one end and exits from the other end. The cooling pipes 5 can be arranged in a single layer or in multiple layers, and solution pumps are arranged at two ends of the pipe bundle and used for circulating water in the cooling water pool 11. The diameter of the stainless steel alloy tube bundle is 30 mm-300 mm, and the tube spacing is 10 mm-100 mm. When the multi-layer arrangement is carried out, the different layer tube bundles are arranged in a crossing way, the included angle between the first layer tube bundle and the last layer tube bundle is 90 degrees, and the middle layer tube bundles are arranged in a crossing way. Through setting up cooling tube 5, can make CPM condense and separate out the length greatly, FPM grows up under supersaturated humidity flue gas, particulate matter is by bubble interface entrapment when bubbling unit.
Further, the wet flue gas desulfurization dust removal device further comprises a waste heat refrigeration unit 10, the waste heat refrigeration unit 10 comprises a heat exchange assembly and a refrigeration assembly, the heat exchange assembly is connected with the flue gas inlet so as to absorb waste heat of flue gas, and the refrigeration assembly is used for cooling water by utilizing the waste heat. The material of the heat exchange component is preferably a corrosion resistant material such as fluoroplastic, hastelloy and the like. The refrigeration component adopts an absorption type waste heat refrigeration unit, wherein the refrigerant is a mixed refrigerant formed by R134 and A, R, the liquid high-temperature refrigerant R134A is utilized to condense the gaseous low-temperature refrigerant R32, and the condensed low-temperature refrigerant is utilized to cool the water in the cooling water pool 11, so that the temperature of the cooling water can reach 5-30 ℃. The absorbent adopts M, N Dimethylformamide (DMF), and mixed refrigerant enters a first-stage condenser after being heated, at the moment, the DMF is kept in a liquid state, and after the refrigerant circulates, the refrigerant is mixed again in the absorber and absorbed by the DMF, and is pumped into a heat exchanger by a solution pump to complete a heat exchange process, and then the DMF enters a generator, and heat is used in the heat exchange process of the heat exchanger, and enters the absorber again to complete the circulation.
The cooling water circulating pump pumps the cooling water cooled by the waste heat into the cooling water pool 11, and pumps the cooling water in the cooling water pool 11 into the bubbling unit 6 and the cooling pipe 5, and the cooling water circulating pump is preferably a single-suction horizontal centrifugal pump. The cooling water tank 11 and the waste heat refrigerating unit 10 are provided with temperature measuring points, and the power of the solution pump is controlled by PID/MPC negative feedback to adjust the cold quantity, so that the temperature of the cooling water is kept constant. Meanwhile, an ash discharging component is arranged at the bottom of the cooling water tank 11, and cooling water after ash washing is discharged and enters fresh water periodically.
Further, the wet flue gas desulfurization dust removal device also comprises a tray 2, wherein the tray 2 is arranged between the spraying layer 4 and the slurry pool 1 and is used for enhancing the gas-liquid contact time, effectively improving the uniformity of flue gas distribution and the gas-liquid contact form and enhancing the desulfurization and preliminary dust removal capability. The distance between the tray 2 and the spraying layer 4 is preferably 1 m-3 m, a plurality of trays can be arranged in the tower, and a single tray is arranged below the single spraying layer 4. The tray is a porous sieve plate, the preferred thickness is 1 mm-5 mm, the aperture is preferably 10 mm-50 mm, the aperture ratio is preferably 20% -50%, the hole arrangement is preferably 60-degree staggered triangular arrangement, the hole spacing is preferably 10 mm-50 mm, a plurality of holes in the tray 2 are separated by partition plates, the height of each partition plate is preferably 100 mm-300 mm, the partition plates divide the plurality of holes into squares, the preferred thickness of each partition plate is 1 mm-5 mm, 36-400 holes are preferably arranged as square partition plates, namely 6X 6-20X 20 holes are arranged as squares.
Further, the wet flue gas desulfurization dust removal device also comprises a gas collecting ring 3, wherein the gas collecting ring 3 is arranged below the spraying layer 4 and is used for gathering flue gas towards the center in the tower. The distance between the gas collecting ring 3 and the spraying layer 4 is preferably 0-3 m, and the gas collecting ring 3 can be arranged at a plurality of positions in the tower, so that the gas collecting ring 3 is mainly used for avoiding the escape of the gas from the position close to the wall of the tower, strengthening the gas to be close to the center in the tower, further optimizing the centering arrangement of the nozzles, and reducing the flushing of the slurry sprayed by the nozzles to the tower body. The top of the gas gathering ring 3 is connected with the tower body, the top and the lower wall of the tower body are arranged at an acute angle, the arrangement angle is preferably 0-90 degrees, the bottom of the gas gathering ring 3 is positioned in the space in the tower, the bottom is preferably serrated, and the slurry on the gas gathering ring 3 can be effectively crushed for the second time.
Further, the wet flue gas desulfurization dust removal device also comprises a process water adding component which is used for cleaning a demister 7, a spray layer 4 and the like in the tower, preventing scaling and blocking in the tower and avoiding liquid level in the towerOverflow phenomenon caused by excessive height; the cleaning frequency is determined by the pressure difference of the two sides of the demister 7, when the pressure difference change amplitude of the two sides of the demister 7 is more than 20%, the cleaning is carried out, and the flushing water quantity is preferably 0.1m per MW unit capacity 3 /h～0.2m 3 The rinsing frequency is preferably 1 to 2 h/time.
The invention fully utilizes the waste heat of coal-fired flue gas, adopts a waste heat refrigeration process to prepare low-temperature cooling water, and installs the cooling pipe 5 and the bubbling unit 6 at the top of the tower body, uses the low-temperature cooling water as the cooling agent in the cooling pipe 5 to cool saturated flue gas, so as to condense CPM, precipitate and grow FPM, and then deep cooling and removing the FPM by the bubbling unit 6, thereby achieving ultra-clean removal of particulate matters without installing a WESP device and having the advantages of environmental protection, no harm, cleanness, high efficiency and low cost. The mechanism is shown in fig. 3, after the flue gas with particles enters the bubbling unit 6, the relative humidity RH in the flue gas is more than 100% under the induction of low-temperature cooling water, and the particles in the flue gas move to the inner surface of the bubbles under the action force taking diffusion swimming force as the dominant action force at the moment, so that the flue gas is purified and removed, and the cooling pipe is the primary cooling of the flue gas, so that the flue gas can be cooled to the supersaturation temperature in the bubbling unit. And after the flue gas is supersaturated, water in the flue gas is condensed, CPM is synchronously condensed and separated out, partial water is condensed in a heterogeneous way on the surface of the FPM, so that the FPM is promoted to grow up, and CPM and FPM efficient collaborative removal is realized.
The technical scheme provided by the invention is further described below according to a specific embodiment.
Example 1
Device one, the smoke volume is 1200000Nm 3 Before the bubbling unit 6 and the cooling pipe 5 are installed, the concentration of particles at the outlet of the WFGD is 25mg/Nm 3 ，SO 2 At a concentration of 18mg/Nm 3 The concentration of particulate matter at the WESP outlet was 8mg/Nm 3 ，SO 2 At a concentration of 17mg/Nm 3 After the bubbling unit 6 and the cooling pipe 5 are installed, the temperature of the running cooling water is 15 ℃, and the concentration of the particles at the outlet of the WFGD is 5mg/Nm 3 ，SO 2 At a concentration of 3mg/Nm 3 The particulate concentration at the WESP outlet was 3mg/Nm 3 ，SO 2 At a concentration of 3mg/Nm 3 WFGD apparatus has been implementedUltra-clean emission; the temperature of the operating cooling water is 10 ℃, and the concentration of the particulate matters at the outlet of the WFGD is 3mg/Nm 3 ，SO 2 At a concentration of 3mg/Nm 3 The concentration of particulate matter at the WESP outlet was 2mg/Nm 3 ，SO 2 At a concentration of 3mg/Nm 3 WFGD units have achieved ultra-clean emissions.
Example 2
Device two, the smoke volume is 2100000Nm 3 Before the bubbling unit 6 and the cooling pipe 5 are installed, the concentration of particulate matters at the outlet of the WFGD is 14mg/Nm 3 ，SO 2 At a concentration of 8mg/Nm 3 The particulate concentration at the WESP outlet was 4mg/Nm 3 ，SO 2 At a concentration of 8mg/Nm 3 After the bubbling unit 6 and the cooling pipe 5 are installed, the temperature of the running cold water is 20 ℃, and the concentration of the particulate matters at the WFGD outlet is 3mg/Nm 3 ，SO 2 At a concentration of 3mg/Nm 3 The concentration of particulate matter at the WESP outlet was 2mg/Nm 3 ，SO 2 At a concentration of 3mg/Nm 3 The WFGD device has realized ultra-clean emissions; the temperature of the cold water is 10 ℃, and the concentration of the particulate matters at the outlet of the WFGD is 1mg/Nm 3 ，SO 2 At a concentration of 3mg/Nm 3 The concentration of particulate matter at the WESP outlet was 1mg/Nm 3 ，SO 2 At a concentration of 3mg/Nm 3 WFGD units have achieved ultra-clean emissions.
It will be readily appreciated by those skilled in the art that the foregoing description is merely a preferred embodiment of the invention and is not intended to limit the invention, but any modifications, equivalents, improvements or alternatives falling within the spirit and principles of the invention are intended to be included within the scope of the invention.
Claims (10)
1. The utility model provides a wet flue gas desulfurization dust collector based on tympanic bulla unit, its characterized in that, this wet flue gas desulfurization dust collector includes the tower body and from bottom to top sets gradually at the inside thick liquid pond (1) of tower body, sprays layer (4), tympanic bulla unit (6) and defroster (7), wherein: a flue gas inlet is formed in the side face of the tower body, the flue gas inlet is positioned between the slurry pool (1) and the spraying layer (4), and a flue gas outlet (9) is formed in the top face of the tower body; limestone slurry for desulfurization is arranged in the slurry tank (1); the spraying layer (4) is used for spraying limestone slurry to realize wet flue gas desulfurization; the bubbling unit (6) comprises a plurality of dust removal assemblies which are arranged in parallel, the dust removal assemblies comprise drainage plates (6.1), bottom plates (6.6), a liquid holding bubbling tank (6.2), guide plates (6.4) and guide pipes (6.3), and the drainage plates (6.1) are connected with the upper bottom plates (6.6) and the lower bottom plates at staggered intervals to form a snake-shaped flue gas channel; the liquid-holding bubbling pond (6.2) is arranged between two adjacent drainage plates (6.1) and is connected with a bottom plate (6.6) below, and cooling water is arranged in the liquid-holding bubbling pond; the guide plate (6.4) is provided with holes and is connected with the guide pipe (6.3) so as to introduce the flue gas into the guide pipe (6.3) through the guide plate (6.4), and meanwhile, the guide plate (6.4) is arranged above the liquid-holding bubbling pond (6.2) and is connected with two adjacent guide plates (6.1) so as to fix the guide pipe (6.3); the flow guide pipe (6.3) stretches into the liquid level of the liquid holding bubbling pond (6.2) and is used for introducing cooling water into the flue gas (6.5) and forming bubbles, so that particles are trapped and dust removal is realized; the demister (7) is arranged between the flue gas outlet (9) and the bubbling unit (6) and is used for removing fog drops in flue gas.
2. The wet flue gas desulfurization and dust removal device based on a bubbling unit as claimed in claim 1, wherein the distance between the bottom of the draft tube (6.3) and the bottom of the liquid-holding bubbling tank (6.2) is 0 mm-10 mm.
3. The wet flue gas desulfurization and dust removal device based on a bubbling unit as claimed in claim 1, wherein the diameter of the flow guide pipe (6.3) is 20 mm-200 mm, the flow guide pipe (6.3) is provided with an air outlet hole, the aperture of the air outlet hole is 1 mm-10 mm, and the aperture ratio of the flow guide pipe (6.3) is 15% -50%.
4. Wet flue gas desulfurization and dust removal device based on a bubbling unit according to claim 1, characterized in that the wet flue gas desulfurization and dust removal device further comprises a cooling pipe (5), wherein the cooling pipe (5) is arranged between the bubbling unit (6) and the spraying layer (4) and is used for introducing cooling water to realize preliminary cooling of flue gas.
5. The wet flue gas desulfurization and dust removal device based on a bubbling unit according to claim 4, wherein the cooling pipe (5) comprises a plurality of stainless steel alloy pipe bundles which are arranged in parallel, the diameter of the stainless steel alloy pipe bundles is 30 mm-300 mm, and the pipe spacing is 10 mm-100 mm.
6. Wet flue gas desulfurization and dust removal device based on a bubbling unit according to claim 1, characterized in that the wet flue gas desulfurization and dust removal device further comprises a waste heat refrigeration unit (10), the waste heat refrigeration unit (10) comprises a heat exchange assembly and a refrigeration assembly, and the heat exchange assembly is connected with a flue gas inlet to absorb waste heat of flue gas; the refrigerating assembly is used for cooling the cooling water by utilizing waste heat.
7. Wet flue gas desulfurization and dust removal device based on a bubbling unit according to claim 1, characterized in that it further comprises a tray (2), said tray (2) being arranged between the spraying layer (4) and the slurry tank (1) for enhancing the gas-liquid contact time.
8. The wet flue gas desulfurization and dust removal device based on the bubbling unit as claimed in claim 1, further comprising a gas collecting ring (3), wherein the gas collecting ring (3) is arranged below the spraying layer (4) and is used for collecting flue gas towards the center in the tower.
9. The wet flue gas desulfurization and dust removal device based on a bubbling unit as claimed in claim 1, wherein the number of layers of the spraying layers (4) is 1-4, the spraying layers (4) are arranged in a crossing way, the spraying nozzles in the same spraying layer (4) are arranged in concentric circles, and the spraying angle of the spraying nozzles in the spraying layer (4) is 45-135 degrees.
10. Wet flue gas desulfurization and dust removal device based on a bubbling unit according to any of claims 1-9, characterized in that the nozzle is a silicon carbide solid conical nozzle or a silicon carbide hollow conical nozzle, the coverage of the spray layer (4) is 200% -300%.
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