CN111135704A - High-temperature industrial flue gas comprehensive treatment system and treatment method - Google Patents
High-temperature industrial flue gas comprehensive treatment system and treatment method Download PDFInfo
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- CN111135704A CN111135704A CN201911314999.6A CN201911314999A CN111135704A CN 111135704 A CN111135704 A CN 111135704A CN 201911314999 A CN201911314999 A CN 201911314999A CN 111135704 A CN111135704 A CN 111135704A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 141
- 239000003546 flue gas Substances 0.000 title claims abstract description 141
- 238000000034 method Methods 0.000 title claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 172
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 82
- 239000000428 dust Substances 0.000 claims abstract description 81
- 229910052751 metal Inorganic materials 0.000 claims abstract description 55
- 239000002184 metal Substances 0.000 claims abstract description 55
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 41
- 230000008878 coupling Effects 0.000 claims abstract description 27
- 238000010168 coupling process Methods 0.000 claims abstract description 27
- 238000005859 coupling reaction Methods 0.000 claims abstract description 27
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 27
- 230000023556 desulfurization Effects 0.000 claims abstract description 27
- 238000002156 mixing Methods 0.000 claims abstract description 22
- 238000000746 purification Methods 0.000 claims abstract description 9
- 238000010438 heat treatment Methods 0.000 claims abstract description 7
- 238000010531 catalytic reduction reaction Methods 0.000 claims abstract 2
- 239000002002 slurry Substances 0.000 claims description 77
- 238000005507 spraying Methods 0.000 claims description 58
- 239000007788 liquid Substances 0.000 claims description 35
- 238000007664 blowing Methods 0.000 claims description 34
- 239000004744 fabric Substances 0.000 claims description 32
- 239000002245 particle Substances 0.000 claims description 24
- 239000007921 spray Substances 0.000 claims description 24
- 239000000443 aerosol Substances 0.000 claims description 11
- -1 polytetrafluoroethylene Polymers 0.000 claims description 11
- 239000000779 smoke Substances 0.000 claims description 10
- 238000009826 distribution Methods 0.000 claims description 9
- 239000012212 insulator Substances 0.000 claims description 9
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 9
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 230000005684 electric field Effects 0.000 claims description 8
- 239000007789 gas Substances 0.000 claims description 8
- 238000005192 partition Methods 0.000 claims description 8
- 239000005997 Calcium carbide Substances 0.000 claims description 6
- 229910000765 intermetallic Inorganic materials 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 5
- 229910052602 gypsum Inorganic materials 0.000 claims description 5
- 239000010440 gypsum Substances 0.000 claims description 5
- 238000002347 injection Methods 0.000 claims description 5
- 239000007924 injection Substances 0.000 claims description 5
- 238000009827 uniform distribution Methods 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 4
- 238000002485 combustion reaction Methods 0.000 claims description 4
- 239000003595 mist Substances 0.000 claims description 4
- 229910000838 Al alloy Inorganic materials 0.000 claims description 3
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 3
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims description 3
- KCZFLPPCFOHPNI-UHFFFAOYSA-N alumane;iron Chemical compound [AlH3].[Fe] KCZFLPPCFOHPNI-UHFFFAOYSA-N 0.000 claims description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 3
- 239000010962 carbon steel Substances 0.000 claims description 3
- 229910001039 duplex stainless steel Inorganic materials 0.000 claims description 3
- 230000005611 electricity Effects 0.000 claims description 3
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims description 3
- 239000002893 slag Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 239000013589 supplement Substances 0.000 claims description 3
- 238000003466 welding Methods 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims 1
- 230000003009 desulfurizing effect Effects 0.000 claims 1
- 230000003301 hydrolyzing effect Effects 0.000 claims 1
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052753 mercury Inorganic materials 0.000 abstract description 2
- 239000002956 ash Substances 0.000 description 13
- 239000003054 catalyst Substances 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000009950 felting Methods 0.000 description 3
- 239000010419 fine particle Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000005299 abrasion Methods 0.000 description 2
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 210000004911 serous fluid Anatomy 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000012719 wet electrostatic precipitator Substances 0.000 description 2
- 229910006069 SO3H Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000003491 array Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000029219 regulation of pH Effects 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 125000000020 sulfo group Chemical group O=S(=O)([*])O[H] 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Images
Classifications
-
- 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
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- 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
-
- 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
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- 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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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Treating Waste Gases (AREA)
Abstract
The system comprises an ammonia mixing device, an SCR (selective catalytic reduction) denitration device, an air preheater, a heat medium water plate type front heat exchanger, an electrostatic dust removal device, a flue tube type heat exchanger, a WFGD desulfurization system, a metal electric bag coupling device, a circulating water treatment device, a heat medium water plate type rear heat exchange device, a first heat medium water tube type heat exchange device and a second heat medium water tube type heat exchange device, wherein the ammonia mixing device, the SCR denitration device, the air preheater, the heat medium water plate type front heat exchanger, the electrostatic dust removal device, the flue tube type heat exchanger, the WFGD desulfurization system and the metal electric bag coupling device are sequentially connected. The boiler is connected with the ammonia mixing device and the air preheater, and the heat medium water plate type rear heat exchange device is connected with the chimney. The flue gas discharged by the boiler is sequentially subjected to denitration, dust removal, desulfurization, deep purification and heating treatment, so that the dust and mercury emission and the moisture content of the flue gas are finally reduced, and the high-efficiency comprehensive treatment of the flue gas is realized. The invention has high purification efficiency and stable operation, and greatly reduces the environmental pollution.
Description
Technical Field
The invention relates to the field of industrial flue gas pollution treatment, in particular to a high-temperature industrial flue gas comprehensive treatment system and a method for comprehensively treating high-temperature industrial flue gas by adopting the high-temperature industrial flue gas comprehensive treatment system.
Background
The high-temperature flue gas is widely generated in the production processes of various industrial boilers. Various pollutants such as NOx, SOx, aerosol and the like in high-temperature flue gas generated in the production process of various industrial boilers, kilns and coal-fired boilers and formed fine particulate matters (PM 2.5) are one of main causes of air pollution, and comprehensive treatment of the high-temperature industrial flue gas multi-pollutants is an important direction for improving the environment in the future.
The existing high-temperature flue gas treatment equipment mainly comprises an ammonia spraying device, an SCR denitration device, a limestone-gypsum wet desulphurization device, a WFGD mechanical demister, a wet electrostatic precipitator and the like. However, the above-mentioned existing high-temperature flue gas treatment equipment has the following problems when flue gas treatment is performed: (1) ammonia spraying deviceSCR denitrification facility all adopts conventional static mixing device, mostly has the inhomogeneous phenomenon of serious mixture, and operation process operating personnel spouts the ammonia volume for guaranteeing denitration efficiency needs constantly increase to ammonia escape volume increase produces a large amount of ammonium bisulfate and blocks the catalyst and influence its activity on the catalyst surface, and ammonium bisulfate's viscidity makes it firmly to adhere and causes the heat exchange efficiency to descend on heat exchange element. In addition, the dust content of high-dust arrangement adopted by SCR denitration is even as high as 30-40 g, and a large amount of dust easily causes abrasion and blockage of a denitration catalyst, so that normal operation of a denitration device is influenced. (2) The limestone-gypsum wet desulphurization removes large-size fly ash particles and generates a large amount of PM2.5 fine particles at the same time: about 1% of the sulfur in coal combustion is oxidized to SO3，SO3H is mixed with water in the dust remover and the wet desulphurization process2SO4The aerosol particles exist in the form of aerosol particles, and when the size of the colloidal particles is small to a certain extent, the processing capacity of the WFGD mechanical mist eliminator for droplets formed by the colloidal particles is reduced, SO that about 50% of SO which is difficult to remove still remains3Discharging fine particles, fine dust and the like to form a precursor of PM2.5 fine particles in the atmosphere. (3) The conventional wet electrostatic dust collector or the rotary converging coupling device of the desulfurization system has strict requirements on the concentration of inlet flue gas: dust at the inlet<80mg/m3Inlet droplet<75mg/m3The wet electrostatic precipitator has higher requirements on the dust removal and demisting devices at the front end, once the concentration of the flue gas at the inlet exceeds the standard, the realization of ultralow emission cannot be ensured, and meanwhile, due to the trend of efficiency attenuation, the fog drops are not thoroughly removed, and white smoke at the mouth of a chimney cannot be eliminated.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide a high-temperature industrial flue gas comprehensive treatment system and a high-temperature industrial flue gas comprehensive treatment method.
The technical scheme of the invention is as follows: the high-temperature industrial flue gas comprehensive treatment system comprises an ammonia mixing device, an SCR denitration device, an air preheater, a heat medium water plate type front heat exchanger, an electrostatic dust removal device, a flue pipe type heat exchanger, a WFGD desulfurization system, a metal electric bag coupling device, a circulating water treatment device, a heat medium water plate type rear heat exchanger, a first heat medium water pipe type heat exchange device and a second heat medium water pipe type heat exchange device.
A double-blade fixed flow disturbing column, a central shaft seat, a four-blade rotating flow guide column, a flow guide light pipe and an ammonia spraying device are arranged in a box body of the ammonia mixing device; the included angle of two blades of the double-blade fixed turbulence column is 90 degrees, and a plurality of turbulence holes for smoke to pass through are formed in the blades according to the size of the smoke; the four double-blade fixed flow disturbing columns, the five central shaft seats and the four light guide tubes are fixed on a bottom plate of the box body side by side through welding, the five four-blade rotating flow guide columns are respectively installed on a shaft rod of the central shaft seat, the ammonia spraying device is installed at the upper end of the box wall of the box body, and the position of the ammonia spraying device is higher than the heights of the double-blade fixed flow disturbing columns, the four-blade rotating flow guide columns and the light guide tubes.
The SCR denitration device comprises two layers of dust removal units with high-temperature injection valves for back blowing, and the dust removal units are arranged in a front flue of the denitration device.
The plate of the heat medium water plate type front heat exchanger is perpendicular to the flue, and a circulating water pump is arranged on a connecting pipeline of the heat medium water plate type front heat exchanger.
The electrostatic dust removal device comprises a double-layer porous airflow uniform distribution plate arranged at an inlet and a plurality of layers of baffle plates arranged at an outlet.
The WFGD desulfurization system comprises a main spray tower, a primary circulating water pump and a secondary circulating slurry tank; the primary circulating water pump and the secondary circulating slurry tank are arranged outside the main spraying tower, a liquid inlet of the primary circulating water pump is connected with a liquid outlet pipe at the lower part of the main spraying tower through a pipeline, and a liquid outlet of the primary circulating water pump is connected with the primary circulating spraying coil pipe through a pipeline.
The high-efficiency demister, the plate-type demister, the tubular demister, the primary circulating spray coil, the liquid collecting hopper, the secondary circulating spray coil and the double-cyclone tube array are sequentially arranged in the main spray tower from top to bottom; the double-cyclone tube array is composed of a plurality of double-cyclone tubes, and each double-cyclone tube comprises a tube body and blades which are positioned at two ends of the tube body and have opposite rotation directions.
The second-stage circulating slurry pool comprises a heat medium water heat exchange tube arranged on the inner wall and an agitator arranged on the second-stage circulating slurry pool, and a second-stage circulating water pump, wherein a first liquid inlet of the second-stage circulating slurry pool is connected with a liquid collecting funnel in the main spray tower through a pipeline, a liquid inlet of the second-stage circulating water pump on the second-stage circulating slurry pool is connected with the pipeline, the pipeline is inserted into the second-stage circulating slurry pool, a liquid outlet of the second-stage circulating water pump is connected with a first-stage circulating spray coil pipe through the pipeline, a second liquid inlet of the second-stage circulating slurry pool is connected with a return pipe on the lower portion of the main spray tower through the pipeline, and an electromagnetic valve is arranged on the pipeline connected.
The metal electric bag coupling device comprises a shell, an insulator box, a blowing ash removal pipeline, a cathode wire fixing plate, a cathode wire, a sleeve mounting plate, a metal cloth bag, a sleeve and a partition plate; the insulator box is arranged on the outer top of the shell; the blowing and dust removing pipeline is arranged at the upper part in the shell, one end of the blowing and dust removing pipeline extends out of the shell and is connected with the gas path pipeline, a plurality of blowing valves are arranged on the blowing and dust removing pipeline, a cathode wire fixing plate is arranged below the blowing and dust removing pipeline, a plurality of cathode wires are uniformly and fixedly arranged below the cathode wire fixing plate, each cathode wire consists of a cathode wire main pipe and a puncture needle, the puncture needles are spirally arranged along the axis direction of the cathode wire main pipe, and the cathode wire fixing plate is connected with an insulator box with hot air blowing function through a hot air pipe; the sleeve mounting plate is arranged below the cathode ray fixing plate, a plurality of sleeves are uniformly and fixedly arranged on the sleeve mounting plate, a plurality of airflow holes are formed in the wall of each sleeve, the sleeves and the cathode rays on the cathode ray fixing plate are arranged at intervals, the metal cloth bags are fixedly sleeved on the sleeves, the sleeve mounting plate is provided with a plurality of fan-shaped water distribution nozzles with fan-shaped angles of 120 degrees, and the fan-shaped water distribution nozzles are externally connected with water pipes; the baffle is arranged below the cathode wire and the metal cloth bag, and a plurality of through holes are arranged on the baffle.
The heat medium water plate type rear heat exchanger plate is arranged perpendicular to the flue, and a circulating water pump is arranged on a connecting pipeline of the heat medium water plate type rear heat exchanger.
The flue gas outlet end of the ammonia mixing device is connected with the flue gas inlet end of the SCR denitration device through a pipeline, the outlet end of the SCR denitration device is connected with the first inlet of the air preheater through a pipeline, the first outlet of the air preheater is connected with the flue gas inlet end of the heat medium water plate type front heat exchanger through a pipeline, the flue gas outlet end of the heat medium water plate type front heat exchanger is connected with the flue gas inlet end of the electrostatic dust removal device through a pipeline, the flue gas outlet end of the electrostatic dust removal device is connected with the flue gas inlet end of a flue tube type heat exchanger through a pipeline, the flue gas outlet end of the flue tube type heat exchanger is connected with the flue gas inlet end of the WFGD desulfurization system through a pipeline, the flue gas outlet end of the WFGD desulfurization system is connected with the flue gas inlet end of the metal electric bag coupling device through a pipeline, and the flue, the water outlet of the metal electric bag coupling device shell is connected with a circulating water treatment device through a pipeline, a heat medium water plate type front heat exchanger is connected with a heat medium water plate type rear heat exchanger through a pipeline, a first heat medium water pipe type heat exchange device is connected with a flue pipe type heat exchanger through a pipeline, and a second heat medium water pipe type heat exchange device is connected with a heat medium water heat exchange pipe on the inner wall of the secondary circulating slurry pool through a pipeline.
The further technical scheme of the invention is as follows: the electrostatic dust removal device is powered by a 100KV high-frequency high-voltage power supply, the anode is a 480C type plate made of carbon steel, the cathode is an RS bur line, and the cathode line of the last electric field is a stainless steel needle-prick line, so that the collection of fine dust is improved.
The invention further adopts the technical scheme that: the elevation angle of the blades of the double cyclone tubes is 20-25 degrees, the radial angle of the blades is 16-18 degrees, the number of the blades is 20-24, the thickness of the blades is 6-12mm, and the tube body and the blades are made of PP, polytetrafluoroethylene or C276.
The invention further adopts the technical scheme that: the flue pipe type heat exchanger is a light pipe without fins, and the light pipe is made of polytetrafluoroethylene; the first heat medium water pipe type heat exchange device and the second heat medium water pipe type heat exchange device are both return light pipes without fins, the return light pipes are made of polytetrafluoroethylene materials, and the return light pipes are perpendicular to the flue.
The invention further adopts the technical scheme that: the cathode wire main pipe and the puncture needle are made of 2205 duplex stainless steel materials; the metal cloth bag is a cylindrical intermetallic compound, one end of the metal cloth bag is open, the other end of the metal cloth bag is closed, the main component of the intermetallic compound is iron-aluminum alloy, and the thickness of a cloth layer of the metal cloth bag is 1 mm.
The invention provides a treatment method applied to the high-temperature industrial flue gas comprehensive treatment system, which comprises the following processes,
A. system connection: the flue gas outlet end of the boiler is connected with the flue gas inlet end of the ammonia mixing device through a pipeline, the primary and secondary combustion-supporting air S of the boiler is connected with the second inlet of the air preheater through a pipeline, the air inlet of the boiler is connected with the second outlet of the air preheater through a pipeline, the flue gas outlet end of the heat medium water plate type rear heat exchange device is connected with the flue gas inlet end of the chimney through a pipeline, and the first heat medium water pipe type heat exchange device and the second heat medium water pipe type heat exchange device are installed at the upper end of the top of the chimney.
B. Denitration and cooling treatment: the start-up system, the high temperature flue gas that the boiler produced gets into ammonia mixing arrangement through the pipeline, spouts ammonia volume according to NOx concentration adjustment in the flue gas to spout the ammonia device for get into SCR deNOx systems after high temperature flue gas and ammonia intensive mixing and carry out denitration treatment, flue gas after the denitration carries out the heat transfer cooling through air preheater and the first secondary combustion-supporting wind S heat exchange of boiler, and the reentrant heat medium water plate formula front heat exchanger carries out the heat exchange and further cools down.
C. And (3) dust removal treatment: the cooled flue gas enters an electrostatic dust removal device, dust content is reduced through electrostatic dust removal, and the flue gas after dust removal enters a flue tube type heat exchanger for further cooling.
D. And (3) desulfurization treatment: after entering a WFGD desulfurization system, the cooled flue gas is subjected to two-stage circulating spraying through a double-cyclone tube array, a primary circulating spraying coil and a secondary circulating spraying coil, and then a tubular demister, a plate demister and a high-efficiency demister are used for respectively removing large-particle gypsum slurry, large-particle liquid drops and aerosol particles carried in the flue gas; when primary circulating spraying is carried out, a primary circulating water pump pumps slurry containing a desulfurizer in the spraying main tower into a primary circulating spraying coil pipe to carry out primary spraying on the flue gas; when the secondary circulating spraying is carried out, the slurry containing the desulfurizer in the secondary circulating slurry pool is pumped into the secondary circulating spraying coil pipe through a secondary circulating water pump on the secondary circulating slurry pool to carry out secondary spraying on the flue gas, the slurry sprayed by the secondary circulating spraying flows into the secondary circulating slurry pool through a liquid collecting funnel, and when the slurry in the secondary circulating slurry pool is lack, the electromagnetic valve is opened to supplement the slurry in the spraying main tower into the secondary circulating slurry pool.
The desulfurizer adopts calcium carbide to hydrolyze calcium carbide slag which is obtained after acetylene gas is obtained and takes calcium hydroxide as a main component, the pH value of slurry in the spraying main tower is 5, and the pH value of slurry in the secondary circulating slurry tank is 6.1.
E. Deep purification treatment: the desulfurized flue gas enters a metal electric bag coupling device, 110Kv direct-current high-voltage electricity is applied between a metal cloth bag and a cathode wire, under the action of a strong electric field, dust particles, slurry and aerosol particles in the flue gas are gathered to the surface of the metal cloth bag, are sprayed and washed by a water distribution nozzle on a sleeve mounting plate, fall into the lower part of a shell through a through hole on a partition plate, and enter a circulating water treatment device from a water outlet at the bottom of the shell.
When the resistance in the metal electric bag coupling device reaches a set value, a blowing valve on a blowing ash removal pipeline is opened to blow compressed air to remove ash in the metal electric bag coupling device, and auxiliary water mist in the blowing ash removal pipeline is opened to blow.
F. And (3) heating and discharging: the flue gas after deep purification treatment enters a heat medium water plate type rear heat exchanger to be heated and then enters a chimney to be discharged, the top of the chimney is further heated by a first heat medium water pipe type heat exchange device and a second heat medium water pipe type heat exchange device, and the heated flue gas is discharged from the top end of the chimney.
Compared with the prior art, the invention has the following characteristics:
the comprehensive treatment system for the high-temperature industrial flue gas provided by the invention has the advantages of thorough purification of the high-temperature flue gas generated by the industrial boiler, high efficiency, stable and reliable operation, great reduction of environmental pollution and realization of stable and long-acting ultralow emission of the industrial boiler through a comprehensive treatment method.
The detailed structure of the present invention will be further described with reference to the accompanying drawings and the detailed description.
Drawings
FIG. 1 is a schematic diagram of the system of the present invention;
FIG. 2 is a schematic view of the structure of an ammonia mixing device;
FIG. 3 is a cross-sectional view A-A of FIG. 2;
FIG. 4 is a schematic view of a WFGD desulfurization system;
FIG. 5 is a schematic diagram of a structure of a double cyclone tube array;
FIG. 6 is a top view of FIG. 5;
FIG. 7 is a schematic structural diagram of a metal electric bag coupling device;
fig. 8 is an enlarged view of a portion I of fig. 7.
Detailed Description
In the first embodiment, as shown in fig. 1 to 8, the high-temperature industrial flue gas comprehensive treatment system includes an ammonia mixing device 1, an SCR denitration device 2, an air preheater 3, a heat medium water plate type front heat exchanger 4, an electrostatic dust removal device 5, a flue pipe heat exchanger 6, a WFGD desulfurization system 7, a metal electric bag coupling device 8, a circulating water treatment device 9, a heat medium water plate type rear heat exchange device 10, a first heat medium water pipe heat exchanger 11, and a second heat medium water pipe heat exchanger 12.
A double-blade fixed flow disturbing column 1-1, a central shaft seat 1-2, a four-blade rotating flow guide column 1-3, a flow guide light pipe 1-4 and an ammonia spraying device 1-6 are arranged in a box body 1-5 of the ammonia mixing device 1.
The included angle of two blades of the double-blade fixed flow disturbing column 1-1 is 90 degrees, and a plurality of flow disturbing holes 1-1-1 for smoke to pass through are formed in the blades according to the size of the smoke.
Four double-blade fixed flow disturbing columns 1-1, five central shaft seats 1-2 and four flow guide light tubes 1-3 are fixed on a bottom plate of a box body 1-5 in parallel by welding, five four-blade rotating flow guide columns 1-3 are respectively arranged on a shaft rod of the central shaft seat 1-2, when smoke passes through, blades on the four-blade rotating flow guide columns 1-3 rotate around the shaft rod of the central shaft seat 1-2 under the action of smoke flow impact, an ammonia spraying device 1-6 is arranged at the upper end of the box wall of the box body 1-5, and the position of the ammonia spraying device 1-6 is higher than the heights of the double-blade fixed flow disturbing columns 1-1, the four-blade rotating flow guide columns 1-3 and the flow guide light tubes 1-4.
The SCR denitration device 2 comprises two layers of dust removal units 2-1 with high-temperature injection valves for back blowing, and the dust removal units 2-1 are arranged in a front flue of the SCR denitration device 2.
The dust removal unit 2-1 is used for pretreating large-particle dust at the inlet of the SCR denitration device 2, so that the dust content is reduced, the scouring abrasion of the dust on the denitration catalyst is reduced, the blockage is prevented, the service life of the denitration catalyst is prolonged, and meanwhile, the reduction of the dust amount reduces the electric field quantity of the rear-end electrostatic dust removal device 5, so that the investment and the operation cost of the electrostatic dust removal device 5 are reduced.
The air preheater 3 adopts a heat storage exchange mode, high-temperature flue gas discharged by the boiler 14 enters the air preheater 3 from an outlet of the SCR denitration device 2 to heat primary and secondary combustion air S entering the boiler 14, the heated air is sent into the boiler 14 through a blower at a first outlet on the air preheater 3, and the flue gas after heat exchange enters the heat medium water plate type front heat exchanger 4 through a second outlet on the air preheater 3.
The heat medium water plate type front heat exchanger 4 is used for absorbing heat of flue gas discharged by the air preheater 3, the temperature of the flue gas discharged by the heat medium water plate type front heat exchanger 4 is controlled within 100 ℃, plates in the heat medium water plate type front heat exchanger 4 are installed perpendicular to a flue, possibility of ash collection is avoided, and a connecting pipeline of the heat medium water plate type front heat exchanger 4 is provided with a circulating water pump (not shown in the figure).
The electrostatic dust collection device 5 comprises a double-layer porous airflow uniform distribution plate 5-1 arranged at an inlet and a multilayer baffle plate 5-2 arranged at an outlet.
The double-layer porous airflow uniform distribution plate 5-1 is simulated by a CFD flow field so as to keep the uniform distribution coefficient of the flue gas entering an electric field area to be about 0.15. The multilayer baffle plate 5-2 is used for collecting secondary dust escaping in the dust removal vibration process of the dust remover. The electrostatic dust removal device 5 is powered by a 100KV high-frequency high-voltage power supply, the anode is a 480C-shaped plate made of carbon steel, the cathode is an RS burred wire, and the cathode wire of the final electric field is a stainless steel needle-pricked wire, so that the collection of fine dust is improved.
A dust removal unit 2-1 and a heat medium water plate type front heat exchanger 4 in the SCR denitration device 2 respectively make the water enter an electrostatic dust removal deviceThe dust content of the flue gas in the device 5 is reduced, the temperature is reduced, and the specific dust collecting area of the electrostatic dust collector 5 is 110m2/m3The/s is reduced to 90m2/m3And the manufacturing cost, the occupied area and the running power consumption of the electrostatic dust collection device 5 are greatly reduced.
The flue pipe type heat exchanger 6 is a light pipe without fins, and the light pipe is made of polytetrafluoroethylene and has strong wear-resisting and corrosion-resisting properties. The flue pipe type heat exchanger 6 is used for reducing the temperature of the flue gas at the outlet of the electrostatic dust removal device 5 from about 100 ℃ to about 70 ℃, thereby greatly reducing the water consumption of a desulfurization system, the power consumption of a circulating pump and the carrying of the flue gas on evaporation liquid drops.
The WFGD desulfurization system 7 comprises a main spray tower 7-1, a primary circulating water pump 7-9 and a secondary circulating slurry tank 7-10.
The spraying main tower 7-1 is internally provided with a high-efficiency demister 7-2, a plate-type demister 7-3, a tubular demister 7-4, a primary circulating spraying coil 7-5, a liquid collecting hopper 7-6, a secondary circulating spraying coil 7-7 and a double-cyclone tube array 7-8 from top to bottom in sequence.
The double-cyclone tube array 7-8 is composed of a plurality of double-cyclone tubes 7-8-1, each double-cyclone tube 7-8-1 comprises a tube body 7-8-1-1 and blades 7-8-1-2 located at two ends of the tube body and having opposite rotation directions, the elevation angle of the blades 7-8-1-2 is 20-25 degrees, the radial angle of the blades 7-8-1-2 is 16-18 degrees, and the number of the blades 7-8-1-2 is 20-24.
The double cyclone tube arrays 7-8 accelerate the mass transfer process of the WFGD desulfurization system 7, and greatly improve the desulfurization efficiency. The tube body 7-8-1-1 and the blades 7-8-1-2 are made of PP, polytetrafluoroethylene or C276, and the thickness of the blades 7-7-1-2 is set to be 6-12mm according to different materials.
The primary circulating water pump 7-9 and the secondary circulating slurry tank 7-10 are arranged outside the main spray tower 7-1.
A liquid inlet of the primary circulating water pump 7-9 is connected with a liquid outlet pipe 7-1-1 at the lower part of the main spray tower 7-1 through a pipeline, and a liquid outlet thereof is connected with the primary circulating spray coil pipe 7-7 through a pipeline.
The secondary circulating slurry pool 7-10 comprises a heating medium water heat exchange pipe 7-10-1 arranged on the inner wall, a stirrer 7-10-2 and a secondary circulating water pump 7-10-3 which are arranged on the secondary circulating slurry pool 7-10, a first liquid inlet of the secondary circulating slurry pool 7-10 is connected with a liquid collecting funnel 7-6 in the main spray tower 7-1 through a pipeline, a liquid inlet of the secondary circulating water pump 7-10-3 on the secondary circulating slurry pool 7-10 is connected with a pipeline 7-10-4, the pipeline 7-10-4 is inserted into the secondary circulating slurry pool 7-10, a liquid outlet of the secondary circulating water pump 7-10-3 is connected with a primary circulating spray coil pipe 7-5 through a pipeline, a second liquid inlet of the secondary circulating slurry pool 7-10 is connected with a return pipe 7-1 at the lower part of the main spray tower 7-1 through a pipeline 2, and a pipeline for connecting a second liquid inlet of the secondary circulating slurry tank 7-10 with a return pipe 7-1-2 at the lower part of the main spray tower 7-1 is provided with an electromagnetic valve 7-11.
The metal electric bag coupling device 8 comprises a shell 8-1, an insulator box 8-2, a blowing ash removal pipeline 8-3, a cathode wire fixing plate 8-4, a cathode wire 8-5, a sleeve mounting plate 8-6, a metal cloth bag 8-7, a sleeve 8-8 and a partition plate 8-9.
The insulator box 8-2 is arranged at the outer top of the shell 8-1. The blowing ash removal pipeline 8-3 is arranged at the upper part in the shell 8-1, one end of the blowing ash removal pipeline extends out of the shell 8-1 and is connected with the gas path pipeline, and a plurality of blowing valves 8-3-1 are arranged on the blowing ash removal pipeline 8-3. The cathode line fixing plate 8-4 is arranged below the blowing ash removal pipeline 8-3, the plurality of cathode lines 8-5 are uniformly and fixedly arranged below the cathode line fixing plate 8-4, the cathode lines 8-5 are composed of cathode line main pipes 8-5-1 and the felting needles 8-5-2, and the cathode line main pipes 8-5-1 and the felting needles 8-5-2 are made of 2205 duplex stainless steel materials. The felting needles 8-5-2 are spirally arranged along the axial direction of the cathode line main pipe 8-5-1, the corona starting voltage is low, and the discharging effect is good. The cathode wire fixing plate 8-4 is connected with an insulator box 8-2 with hot air blowing through a hot air pipe.
The sleeve mounting plate 8-6 is arranged below the cathode ray fixing plate 8-4, a plurality of sleeves 8-8 are uniformly and fixedly arranged on the sleeve mounting plate 8-6, a plurality of airflow holes are formed in the wall of each sleeve 8-8, the sleeves 8-8 and the cathode rays 8-5 on the cathode ray fixing plate 8-4 are arranged at intervals, the metal cloth bag 8-7 is fixedly sleeved on the sleeves 8-8, the sleeve mounting plate 8-6 is provided with a plurality of fan-shaped water distribution nozzles (not shown in the figure) with a fan-shaped angle of 120 degrees, the fan-shaped water distribution nozzles are externally connected with water pipes and used for uniformly distributing water on the outer surface of the metal cloth bag 8-7 and flushing dust, slurry, aerosol particles and other pollutants on the metal cloth bag 8-.
The metal cloth bag 8-7 is a cylindrical intermetallic compound, one end of the metal cloth bag is open, the other end of the metal cloth bag is closed, the main component of the intermetallic compound is iron-aluminum alloy, and the thickness of the metal cloth bag 8-7 cloth layer is 1 mm.
The baffle plate 8-9 is arranged below the cathode line 8-5 and the metal cloth bag 8-7, and a plurality of through holes 8-9-1 are arranged on the baffle plate 8-9.
The circulating water treatment device 9 is used for receiving the water flowing out of the metal electric bag coupling device 8, cleaning and filtering the water, adjusting the pH value of the water, precipitating and filtering the water, and recycling the treated water.
The heat medium water plate type rear heat exchanger 10 is used for heating low-temperature flue gas discharged by the metal electric bag coupling device 8, improving the temperature of the discharged flue gas and reducing chimney corrosion and white smoke at a chimney opening. The plates in the heat medium water plate type rear heat exchanger 10 are arranged perpendicular to the flue, so that the possibility of ash collection is avoided, and a circulating water pump (not shown in the figure) is arranged on a connecting pipeline of the heat medium water plate type rear heat exchanger 10.
The first heat medium water pipe type heat exchange device 11 and the second heat medium water pipe type heat exchange device 12 are both a light pipe without fins, the light pipe is made of polytetrafluoroethylene and has strong wear-resisting and corrosion-resisting properties, and the light pipe is perpendicular to a flue during installation.
The flue gas outlet end of the ammonia mixing device 1 is connected with the flue gas inlet end of the SCR denitration device 2 through a pipeline, the outlet end of the SCR denitration device 2 is connected with the first inlet of the air preheater 3 through a pipeline, the first outlet of the air preheater 3 is connected with the flue gas inlet end of the heat medium water plate type front heat exchanger 4 through a pipeline, the flue gas outlet end of the heat medium water plate type front heat exchanger 4 is connected with the flue gas inlet end of the electrostatic dust removal device 5 through a pipeline, the flue gas outlet end of the electrostatic dust removal device 5 is connected with the flue gas inlet end of the flue tube type heat exchanger 6 through a pipeline, the flue gas outlet end of the flue tube type heat exchanger 6 is connected with the flue gas inlet end of the WFGD desulfurization system 7 through a pipeline, the flue gas outlet end of the WFGD desulfurization system 7 is connected with the flue gas inlet end of the metal electric bag coupling device 8 through a pipeline, the flue gas outlet end, the water outlet of a shell 8-1 of the metal electric bag coupling device 8 is connected with a circulating water treatment device 9 through a pipeline, a heat medium water plate type front heat exchanger 4 is connected with a heat medium water plate type rear heat exchanger 10 through a pipeline, a first heat medium water pipe type heat exchanger 11 is connected with a flue pipe type heat exchanger 6 through a pipeline, and a second heat medium water pipe type heat exchanger 12 is connected with a heat medium water heat exchange pipe 7-10-1 on the inner wall of a secondary circulating slurry pool 7-10 through a pipeline.
The first heat medium water pipe type heat exchange device 11 is connected with the flue pipe type heat exchanger 6 through a pipeline, and heat absorbed by the flue pipe type heat exchanger 6 is subjected to heat exchange with flue gas in a chimney in the first heat medium water pipe type heat exchange device 11 by using water as a medium, so that the flue gas temperature of the chimney is improved.
The second heat medium water pipe type heat exchange device 12 is connected with a heat medium water heat exchange pipe 7-10-1 on the inner wall of the second-stage circulating slurry pool 7-10 through a pipeline, the heat medium water heat exchange pipe 7-10-1 adopts water as a medium to exchange heat with the second heat medium water pipe type heat exchange device 12, and slurry in the second-stage circulating slurry pool is cooled, so that the solubility of gas in the second-stage circulating slurry pool 7-10 is improved, the desulfurization efficiency is improved, and meanwhile, the flue gas temperature of a chimney is further improved.
The process of the high-temperature industrial flue gas comprehensive treatment system for treating the high-temperature flue gas of the industrial boiler comprises the following steps:
A. system connection: the flue gas outlet end of the boiler 14 is connected with the flue gas inlet end of the ammonia mixing device 1 through a pipeline, primary and secondary combustion-supporting air S of the boiler 14 is connected with a second inlet of the air preheater 3 through a pipeline, an air inlet of the boiler 14 is connected with a second outlet of the air preheater 3 through a pipeline, the flue gas outlet end of the heat medium water plate type rear heat exchange device 10 is connected with the flue gas inlet end of the chimney 13 through a pipeline, and the first heat medium water pipe type heat exchange device 11 and the second heat medium water pipe type heat exchange device 12 are installed at the upper end of the top of the chimney 13.
B. Denitration and cooling treatment: the system is started, high-temperature flue gas generated by the boiler 14 enters the ammonia mixing device 1 through a pipeline, the ammonia spraying amount of the ammonia spraying devices 1-6 is adjusted according to the concentration of NOx in the flue gas, the high-temperature flue gas and the ammonia are fully mixed and then enter the SCR denitration system 2 for denitration treatment, the denitrated flue gas is subjected to heat exchange with primary and secondary combustion air S of the boiler 14 through the air preheater 3 and is cooled to 150 ℃, and then enters the heat medium water plate type front heat exchanger 4 for heat exchange, and the temperature is reduced to 100 ℃.
The temperature of the high-temperature flue gas generated by the boiler 14 is 390 ℃, and the dust content in the flue gas is 25g/Nm3NOx content 430mg/Nm3The SOx content was 6000mg/Nm3。
C. And (3) dust removal treatment: the cooled flue gas enters an electrostatic dust collection device 5, and the dust content in the flue gas is reduced to 42mg/Nm after electrostatic dust collection3And the temperature of the dedusted flue gas entering the flue pipe type heat exchanger 6 is reduced to 70 ℃.
D. And (3) desulfurization treatment: after entering a WFGD desulfurization system 7, the cooled flue gas is sprayed in a two-stage circulating mode through a double-cyclone tube array 7-8, a first-stage circulating spray coil 7-7 and a second-stage circulating spray coil 7-5, and then large-particle gypsum slurry, large-particle liquid drops and aerosol particles carried in the flue gas are removed by a tubular demister 7-4, a plate demister 7-3 and a high-efficiency demister 7-2 respectively.
When primary circulating spraying is carried out, a primary circulating water pump 7-9 pumps the slurry containing the desulfurizer in the spraying main tower 7-1 into a primary circulating spraying coil 7-7 to carry out primary spraying on the flue gas; when the secondary circulating spraying is carried out, the slurry containing the desulfurizer in the secondary circulating slurry pool 7-10 is pumped into a secondary circulating spraying coil pipe 7-5 through a secondary circulating water pump 7-10-3 on the secondary circulating slurry pool 7-10 to carry out secondary spraying on the flue gas, the slurry after the secondary spraying flows into the secondary circulating slurry pool 7-10 through a liquid collecting funnel 7-6, and when the slurry in the secondary circulating slurry pool 7-10 is lacked, an electromagnetic valve 7-11 is opened to supplement the slurry in the main spraying tower 7-1 into the secondary circulating slurry pool 7-10.
The desulfurizer adopts calcium carbide to hydrolyze to obtain acetylene gas, and then the calcium carbide slag which takes calcium hydroxide as a main component is obtained, the pH value of slurry in the main spraying tower 7-1 is 5, and the pH value of slurry in the secondary circulating slurry tank 7-10 is 6.1.
E. Deep purification treatment: the desulfurized flue gas enters a metal electric bag coupling device 8, 110Kv direct-current high-voltage electricity is applied between a metal cloth bag 8-7 and a cathode wire 8-5, under the action of a strong electric field, dust particles, serous fluid, aerosol particles and other pollutants in the flue gas are gathered on the surface of the metal cloth bag 8-7, meanwhile, the flue gas is sprayed and washed by a water distribution nozzle on a sleeve mounting plate 8-6, the washed dust particles, serous fluid, aerosol particles and other pollutants are communicated with washing water and fall into the lower part of a shell 8-1 through a through hole 8-9-1 on a partition plate 8-9, the washing water enters a circulating water treatment device 9 from a water outlet at the bottom of the shell 8-1, and the circulating water treatment device 9 is used for cleaning and filtering, PH regulation and precipitation filtration, so that the treated water is recycled.
When the resistance in the metal electric bag coupling device 8 reaches a set value, compressed air is blown to clean the inside of the metal electric bag coupling device 8 by opening a blowing valve 8-3-1 on a blowing ash cleaning pipeline 8-3, and auxiliary water mist is added in the blowing ash cleaning pipeline 8-3 for blowing.
F. And (3) heating and discharging: the flue gas after deep purification treatment enters a heat medium water plate type rear heat exchanger 10, is heated and then enters a chimney 13 to be discharged, the top of the chimney 13 is further heated by a first heat medium water pipe type heat exchange device 11 and a second heat medium water pipe type heat exchange device 12, and the heated flue gas is discharged from the top end of the chimney 13. The dust emission of the flue gas discharged from the top of the chimney 13<4mg/m3、SOx<30mg/m3、NOx<40mg/m3Mercury emission<0.03mg/m3Moisture content of flue gas<8.5 percent, and meets the requirement of high-efficiency comprehensive treatment of the flue gas.
Claims (6)
1. High temperature industry flue gas comprehensive treatment system, characterized by: the system comprises an ammonia mixing device, an SCR denitration device, an air preheater, a heat medium water plate type front heat exchanger, an electrostatic dust removal device, a flue pipe type heat exchanger, a WFGD desulfurization system, a metal electric bag coupling device, a circulating water treatment device, a heat medium water plate type rear heat exchange device, a first heat medium water pipe type heat exchange device and a second heat medium water pipe type heat exchange device;
a double-blade fixed flow disturbing column, a central shaft seat, a four-blade rotating flow guide column, a flow guide light pipe and an ammonia spraying device are arranged in a box body of the ammonia mixing device; the included angle of two blades of the double-blade fixed turbulence column is 90 degrees, and a plurality of turbulence holes for smoke to pass through are formed in the blades according to the size of the smoke; four double-blade fixed flow disturbing columns, five central shaft seats and four flow guide light tubes are fixed on a bottom plate of the box body side by side through welding, five four-blade rotating flow guide columns are respectively arranged on shaft rods of the central shaft seats, an ammonia spraying device is arranged at the upper end of the box wall of the box body, and the position of the ammonia spraying device is higher than the heights of the double-blade fixed flow disturbing columns, the four-blade rotating flow guide columns and the flow guide light tubes;
the SCR denitration device comprises two layers of dust removal units with high-temperature injection valves for back blowing, and the dust removal units are arranged in a front flue of the denitration device;
the plate of the heat medium water plate type front heat exchanger is arranged perpendicular to the flue, and a circulating water pump is arranged on a connecting pipeline of the heat medium water plate type front heat exchanger;
the electrostatic dust removal device comprises a double-layer porous airflow uniform distribution plate arranged at an inlet and a plurality of layers of baffle plates arranged at an outlet;
the WFGD desulfurization system comprises a main spray tower, a primary circulating water pump and a secondary circulating slurry tank; the primary circulating water pump and the secondary circulating slurry tank are arranged outside the main spraying tower, a liquid inlet of the primary circulating water pump is connected with a liquid outlet pipe at the lower part of the main spraying tower through a pipeline, and a liquid outlet of the primary circulating water pump is connected with the primary circulating spraying coil pipe through a pipeline;
the high-efficiency demister, the plate-type demister, the tubular demister, the primary circulating spray coil, the liquid collecting hopper, the secondary circulating spray coil and the double-cyclone tube array are sequentially arranged in the main spray tower from top to bottom; the double-cyclone tube array is composed of a plurality of double-cyclone tubes, and each double-cyclone tube comprises a tube body and blades positioned at two ends of the tube body and having opposite rotation directions;
the second-stage circulating slurry pool comprises a heating medium water heat exchange pipe arranged on the inner wall, a stirrer and a second-stage circulating water pump, the stirrer and the second-stage circulating water pump are arranged on the second-stage circulating slurry pool, a first liquid inlet of the second-stage circulating slurry pool is connected with a liquid collecting hopper in the main spray tower through a pipeline, a liquid inlet of the second-stage circulating water pump on the second-stage circulating slurry pool is connected with a pipeline, the pipeline is inserted into the second-stage circulating slurry pool, a liquid outlet of the second-stage circulating water pump is connected with a first-stage circulating spray coil pipe through a pipeline, a second liquid inlet of the second-stage circulating slurry pool is connected with a return pipe at the lower part of the main spray tower through a pipeline;
the metal electric bag coupling device comprises a shell, an insulator box, a blowing ash removal pipeline, a cathode wire fixing plate, a cathode wire, a sleeve mounting plate, a metal cloth bag, a sleeve and a partition plate; the insulator box is arranged on the outer top of the shell; the blowing and dust removing pipeline is arranged at the upper part in the shell, one end of the blowing and dust removing pipeline extends out of the shell and is connected with the gas path pipeline, a plurality of blowing valves are arranged on the blowing and dust removing pipeline, a cathode wire fixing plate is arranged below the blowing and dust removing pipeline, a plurality of cathode wires are uniformly and fixedly arranged below the cathode wire fixing plate, each cathode wire consists of a cathode wire main pipe and a puncture needle, the puncture needles are spirally arranged along the axis direction of the cathode wire main pipe, and the cathode wire fixing plate is connected with an insulator box with hot air blowing function through a hot air pipe; the sleeve mounting plate is arranged below the cathode ray fixing plate, a plurality of sleeves are uniformly and fixedly arranged on the sleeve mounting plate, a plurality of airflow holes are formed in the wall of each sleeve, the sleeves and the cathode rays on the cathode ray fixing plate are arranged at intervals, the metal cloth bags are fixedly sleeved on the sleeves, the sleeve mounting plate is provided with a plurality of fan-shaped water distribution nozzles with fan-shaped angles of 120 degrees, and the fan-shaped water distribution nozzles are externally connected with water pipes; the partition board is arranged below the cathode wire and the metal cloth bag, and a plurality of through holes are formed in the partition board;
the plate pieces of the heat medium water plate type rear heat exchanger are arranged perpendicular to the flue, and a circulating water pump is arranged on a connecting pipeline of the heat medium water plate type rear heat exchanger;
the flue gas outlet end of the ammonia mixing device is connected with the flue gas inlet end of the SCR denitration device through a pipeline, the outlet end of the SCR denitration device is connected with the first inlet of the air preheater through a pipeline, the first outlet of the air preheater is connected with the flue gas inlet end of the heat medium water plate type front heat exchanger through a pipeline, the flue gas outlet end of the heat medium water plate type front heat exchanger is connected with the flue gas inlet end of the electrostatic dust removal device through a pipeline, the flue gas outlet end of the electrostatic dust removal device is connected with the flue gas inlet end of a flue tube type heat exchanger through a pipeline, the flue gas outlet end of the flue tube type heat exchanger is connected with the flue gas inlet end of the WFGD desulfurization system through a pipeline, the flue gas outlet end of the WFGD desulfurization system is connected with the flue gas inlet end of the metal electric bag coupling device through a pipeline, and the flue, the water outlet of the metal electric bag coupling device shell is connected with a circulating water treatment device through a pipeline, a heat medium water plate type front heat exchanger is connected with a heat medium water plate type rear heat exchanger through a pipeline, a first heat medium water pipe type heat exchange device is connected with a flue pipe type heat exchanger through a pipeline, and a second heat medium water pipe type heat exchange device is connected with a heat medium water heat exchange pipe on the inner wall of the secondary circulating slurry pool through a pipeline.
2. The high-temperature industrial flue gas comprehensive treatment system as claimed in claim 1, which is characterized in that: the electrostatic dust removal device is powered by a 100KV high-frequency high-voltage power supply, the anode is a 480C type plate made of carbon steel, the cathode is an RS bur line, and the cathode line of the last electric field is a stainless steel needle-prick line, so that the collection of fine dust is improved.
3. The high-temperature industrial flue gas comprehensive treatment system as claimed in claim 1, which is characterized in that: the elevation angle of the blades of the double cyclone tubes is 20-25 degrees, the radial angle of the blades is 16-18 degrees, the number of the blades is 20-24, the thickness of the blades is 6-12mm, and the tube body and the blades are made of PP, polytetrafluoroethylene or C276.
4. The high-temperature industrial flue gas comprehensive treatment system as claimed in claim 1, which is characterized in that: the flue pipe type heat exchanger is a light pipe without fins, and the light pipe is made of polytetrafluoroethylene; the first heat medium water pipe type heat exchange device and the second heat medium water pipe type heat exchange device are both return light pipes without fins, the return light pipes are made of polytetrafluoroethylene materials, and the return light pipes are perpendicular to the flue.
5. The high-temperature industrial flue gas comprehensive treatment system as claimed in claim 1, which is characterized in that: the cathode wire main pipe and the puncture needle are made of 2205 duplex stainless steel materials; the metal cloth bag is a cylindrical intermetallic compound, one end of the metal cloth bag is open, the other end of the metal cloth bag is closed, the main component of the intermetallic compound is iron-aluminum alloy, and the thickness of a cloth layer of the metal cloth bag is 1 mm.
6. The treatment method applied to the high-temperature industrial flue gas comprehensive treatment system of any one of claims 1 to 5 is characterized in that: comprises the following steps of,
A. system connection: the flue gas outlet end of the boiler is connected with the flue gas inlet end of the ammonia mixing device through a pipeline, primary and secondary combustion-supporting air S of the boiler is connected with a second inlet of the air preheater through a pipeline, the air inlet of the boiler is connected with a second outlet of the air preheater through a pipeline, the flue gas outlet end of the heat medium water plate type rear replacement heat device is connected with the flue gas inlet end of the chimney through a pipeline, and the first heat medium water pipe type heat exchange device and the second heat medium water pipe type heat exchange device are installed at the upper end of the top of the chimney;
B. denitration and cooling treatment: starting the system, feeding high-temperature flue gas generated by the boiler into an ammonia mixing device through a pipeline, adjusting the ammonia injection amount by an ammonia injection device according to the concentration of NOx in the flue gas, fully mixing the high-temperature flue gas and the ammonia, feeding the mixed gas into an SCR (selective catalytic reduction) denitration system for denitration treatment, carrying out heat exchange and cooling on the denitrified flue gas and primary and secondary combustion air S of the boiler through an air preheater, and feeding the denitrated flue gas into a heat medium water plate type front heat exchanger for further cooling through heat exchange;
C. and (3) dust removal treatment: the cooled flue gas enters an electrostatic dust removal device, dust content is reduced through electrostatic dust removal, and the dedusted flue gas enters a flue pipe type heat exchanger for further cooling;
D. and (3) desulfurization treatment: after entering a WFGD desulfurization system, the cooled flue gas is subjected to two-stage circulating spraying through a double-cyclone tube array, a primary circulating spraying coil and a secondary circulating spraying coil, and then a tubular demister, a plate demister and a high-efficiency demister are used for respectively removing large-particle gypsum slurry, large-particle liquid drops and aerosol particles carried in the flue gas; when primary circulating spraying is carried out, a primary circulating water pump pumps slurry containing a desulfurizer in the spraying main tower into a primary circulating spraying coil pipe to carry out primary spraying on the flue gas; when secondary circulating spraying is carried out, the slurry containing the desulfurizer in the secondary circulating slurry pool is pumped into a secondary circulating spraying coil pipe through a secondary circulating water pump on the secondary circulating slurry pool to carry out secondary spraying on the flue gas, the slurry after secondary spraying flows into the secondary circulating slurry pool through a liquid collecting funnel, and when the slurry in the secondary circulating slurry pool is lacked, an electromagnetic valve is opened to supplement the slurry in the spraying main tower into the secondary circulating slurry pool;
the desulfurizing agent is acetylene gas obtained by hydrolyzing calcium carbide to obtain calcium carbide slag which takes calcium hydroxide as a main component, the pH value of slurry in the spraying main tower is 5, and the pH value of slurry in the secondary circulating slurry tank is 6.1;
E. deep purification treatment: the desulfurized flue gas enters a metal electric bag coupling device, 110Kv direct-current high-voltage electricity is applied between a metal cloth bag and a cathode wire, under the action of a strong electric field, dust particles, slurry and aerosol particles in the flue gas are gathered to the surface of the metal cloth bag, are sprayed and washed by a water distribution nozzle on a sleeve mounting plate, fall into the lower part of a shell through a through hole on a partition plate, and enter a circulating water treatment device from a water outlet at the bottom of the shell;
when the resistance in the metal electric bag coupling device reaches a set value, a blowing valve on a blowing ash removal pipeline is opened to blow compressed air to remove ash in the metal electric bag coupling device, and auxiliary water mist in the blowing ash removal pipeline is opened to blow;
F. and (3) heating and discharging: the flue gas after deep purification treatment enters a heat medium water plate type rear heat exchanger to be heated and then enters a chimney to be discharged, the top of the chimney is further heated by a first heat medium water pipe type heat exchange device and a second heat medium water pipe type heat exchange device, and the heated flue gas is discharged from the top end of the chimney.
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| CN201911314999.6A CN111135704B (en) | 2019-12-19 | 2019-12-19 | Comprehensive treatment system and method for high-temperature industrial flue gas |
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