CN112705025A - Energy-saving ammonia desulphurization device with ultralow emission and desulphurization process - Google Patents
Energy-saving ammonia desulphurization device with ultralow emission and desulphurization process Download PDFInfo
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- CN112705025A CN112705025A CN202011588388.3A CN202011588388A CN112705025A CN 112705025 A CN112705025 A CN 112705025A CN 202011588388 A CN202011588388 A CN 202011588388A CN 112705025 A CN112705025 A CN 112705025A
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 122
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 61
- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 200
- 238000010521 absorption reaction Methods 0.000 claims abstract description 149
- 238000004140 cleaning Methods 0.000 claims abstract description 130
- 230000003647 oxidation Effects 0.000 claims abstract description 79
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 79
- 238000002425 crystallisation Methods 0.000 claims abstract description 59
- 230000008025 crystallization Effects 0.000 claims abstract description 59
- 238000005507 spraying Methods 0.000 claims abstract description 56
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 46
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 46
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 46
- 238000012856 packing Methods 0.000 claims abstract description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000012452 mother liquor Substances 0.000 claims abstract description 26
- 238000003756 stirring Methods 0.000 claims abstract description 24
- 230000008929 regeneration Effects 0.000 claims abstract description 6
- 238000011069 regeneration method Methods 0.000 claims abstract description 6
- 239000007921 spray Substances 0.000 claims description 87
- 239000003546 flue gas Substances 0.000 claims description 50
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 49
- 238000006477 desulfuration reaction Methods 0.000 claims description 40
- 230000023556 desulfurization Effects 0.000 claims description 40
- 230000003009 desulfurizing effect Effects 0.000 claims description 38
- 239000002002 slurry Substances 0.000 claims description 30
- 238000009826 distribution Methods 0.000 claims description 26
- 238000005406 washing Methods 0.000 claims description 23
- 239000000779 smoke Substances 0.000 claims description 21
- 238000011010 flushing procedure Methods 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 10
- 239000012141 concentrate Substances 0.000 claims description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 6
- 229910052717 sulfur Inorganic materials 0.000 claims description 6
- 239000011593 sulfur Substances 0.000 claims description 6
- 230000003197 catalytic effect Effects 0.000 claims description 5
- 238000005086 pumping Methods 0.000 claims description 5
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 4
- 230000001174 ascending effect Effects 0.000 claims description 3
- 238000013019 agitation Methods 0.000 claims 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 abstract description 18
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 abstract description 18
- 239000000428 dust Substances 0.000 abstract description 5
- 230000007613 environmental effect Effects 0.000 abstract description 5
- 238000010276 construction Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 230000005611 electricity Effects 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 6
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 description 3
- 239000000945 filler Substances 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- JZRWCGZRTZMZEH-UHFFFAOYSA-N Thiamine Natural products CC1=C(CCO)SC=[N+]1CC1=CN=C(C)N=C1N JZRWCGZRTZMZEH-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- KYMBYSLLVAOCFI-UHFFFAOYSA-N thiamine Chemical compound CC1=C(CCO)SCN1CC1=CN=C(C)N=C1N KYMBYSLLVAOCFI-UHFFFAOYSA-N 0.000 description 1
- 229960003495 thiamine Drugs 0.000 description 1
- 235000019157 thiamine Nutrition 0.000 description 1
- 239000011721 thiamine Substances 0.000 description 1
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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
- B01D53/46—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
- B01D53/75—Multi-step processes
-
- 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D53/77—Liquid phase processes
- B01D53/79—Injecting reactants
-
- 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
Abstract
The invention relates to an energy-saving ultra-low emission ammonia desulphurization device and a process, wherein the ammonia desulphurization device comprises a desulphurization tower, an oxidation tank, a mother liquor tank, a cyclone, a circulating pump and the like, and the desulphurization tower is sequentially divided into an ammonium sulfate crystallization section, a concentration spraying section, an SO (sulfur oxide) section and an SO (sulfur oxide) section from bottom to top2An absorption section, a cleaning section and a demisting section; the ammonium sulfate crystallization section adopts a flat-bottom and annular stirring pipe structure, so that the height of a crystallization tank is reduced; the concentration and spraying adopt a forward flow process, so that the tower pressure drop is reduced; the taking-out pump and the stirring pump are combined through the cyclone, so that the number of system equipment is reduced; the absorption section adopts regular packing and is arranged between sectionsThe linear regeneration structure design reduces the absorption circulation volume and the number of absorption pumps; the cleaning water tank is omitted, so that the lift of a cleaning pump is reduced, and the liquid capacity of the system is reduced; the high-efficiency demister eliminates wet electricity. The invention further perfects the process flow of the ammonia desulphurization device, realizes desulphurization and dust removal with low investment, low energy consumption and high efficiency, can reduce the construction cost and the operation cost of the device while ensuring ultralow emission, and realizes environmental protection and benefit.
Description
Technical Field
The invention relates to an ammonia desulphurization device, in particular to an energy-saving ammonia desulphurization device with ultralow emission and a desulphurization process.
Background
The ammonia desulphurization is one of high-efficiency wet desulphurization processes, and occupies a certain place in the popularization and application of China. The existing ultra-low emission ammonia desulphurization device achieves the purpose of ultra-low emission by reducing airspeed, increasing absorption circulation volume, adding a washing system and adding a wet electric demisting device. However, the device has the problems of high manufacturing cost, large occupied area and high running power consumption, so that the ammonia desulphurization method goes into an embarrassing situation that the environmental protection is passed but the economic is not passed.
Disclosure of Invention
One of the purposes of the invention is to provide an energy-saving ammonia desulphurization device with ultralow emission, so as to reduce the construction cost and the operation cost of the device while ensuring ultralow emission and realize both environmental protection and economic benefit.
The second purpose of the invention is to provide an energy-saving ammonia desulphurization process with ultralow emission so as to realize desulphurization and dust removal with low investment, low energy consumption and high efficiency.
One of the objects of the invention is achieved by: an energy-saving ammonia desulphurization device with ultralow emission comprises a desulphurization tower and an oxidation tank, wherein the desulphurization tower is sequentially divided into an ammonium sulfate crystallization section, a concentration spraying section and an SO (sulfur oxide) section from bottom to top2An absorption section, a cleaning section and a demisting section.
The ammonium sulfate crystallization section comprises a flat-bottom-shaped concentration crystallization tank serving as the bottom of the desulfurization tower and an annular stirrer arranged in the concentration crystallization tank; the liquid outlet pipe of the concentrated crystallization tank is connected with an external stirring discharge pump, the outlet pipe of the stirring discharge pump is connected to the inlet of the first cyclone, and the dilute liquid outlet pipe of the first cyclone is connected to the annular stirrer.
The concentration spray section comprises a smoke inlet pipe inserted on the tower wall of the desulfurization tower, a concentration section spray pipe arranged at the inner port of the smoke inlet pipe and a back flush spray pipe positioned above the smoke inlet pipe; the back flushing spray pipe is externally connected with an absorption liquid circulating pump, the concentration section spray pipe is externally connected with a concentration liquid circulating pump, and the liquid inlet end of the concentration liquid circulating pump is communicated with the ammonium sulfate crystallization section through a pipeline.
The SO2The absorption section comprises an absorption section liquid collecting disc arranged at the upper part of the concentration spraying section, three absorption section packing layers which are arranged above the absorption section liquid collecting disc at intervals up and down, and a spraying liquid distribution pipe arranged in the space above each absorption section packing layer. The inlet pipes of the three spraying liquid distribution pipes are connected in parallel outside the tower and then connected with an absorption liquid circulating pump, the inlet end of the absorption liquid circulating pump is connected to the absorption liquid outlet of the oxidation tank through a pipeline, and the absorption liquid inlet of the oxidation tank is connected with an absorption liquid return pipe arranged on a liquid collecting disc of an absorption section through a pipeline; and an ammonia adding pipe for providing ammonia water is connected to the inlet pipe of the spraying liquid distribution pipe arranged between the absorption section packing layers, and the ammonia adding pipe is externally connected with an ammonia supply main pipe.
The cleaning section comprises a first-stage cleaning section and a second-stage cleaning section.
The first-stage cleaning section comprises a cleaning zone arranged at SO2The device comprises a first-stage cleaning section liquid collecting disc at the upper part of an absorption section, a first-stage cleaning section packing layer at the upper part of the first-stage cleaning section liquid collecting disc and a first-stage cleaning section spray pipe at the upper part of the first-stage cleaning section packing layer; the spraying pipe of the first-stage cleaning section is externally connected with a first-stage cleaning circulating pump, and the inlet end of the first-stage cleaning circulating pump is connected with a cleaning liquid return pipe arranged on the liquid collecting disc of the first-stage cleaning section.
The secondary cleaning section comprises a secondary cleaning section liquid collecting disc arranged at the upper part of the primary cleaning section, a secondary cleaning section packing layer positioned at the upper part of the secondary cleaning section liquid collecting disc and a secondary cleaning section spray pipe positioned at the upper part of the secondary cleaning section packing layer; the spraying pipe of the second-stage cleaning section is externally connected with a second-stage cleaning circulating pump, and the inlet end of the second-stage cleaning circulating pump is connected with a cleaning liquid return pipe arranged on a liquid collecting disc of the second-stage cleaning section.
The demisting section comprises a primary demisting section and an ultra-clean demisting section.
The primary demisting section comprises two layers of baffle plate demisters and a first washing spray pipe, the two layers of baffle plate demisters are positioned at the upper part of the secondary cleaning section and are arranged at intervals from top to bottom, the first washing spray pipe is arranged between the two layers of baffle plate demisters, and the first washing spray pipe is connected with a process water main pipe.
The ultra-clean demisting section comprises two layers of screen demisters and a second washing spray pipe, wherein the two layers of screen demisters are arranged at an upper interval and a lower interval, the second washing spray pipe is arranged between the two layers of screen demisters, the screen demisters on the lower layer are arranged on the top surface of the baffle plate demister on the upper layer, and the second washing spray pipe is externally connected with a desalted water header pipe.
The concentrate outlet pipe of the first cyclone is connected to the inlet of the second cyclone, the concentrate outlet pipe of the second cyclone is connected to the centrifuge, and the dilute liquid outlet pipe of the second cyclone is connected to the mother liquid tank.
An accident spray pipe is also arranged in the smoke inlet pipe and is connected with the process water main pipe.
The ammonia supply main pipe is respectively connected to the stirring discharge pump inlet pipe, the first-stage cleaning circulating pump inlet pipe, the second-stage cleaning circulating pump inlet pipe and the absorption liquid circulating pump inlet pipe through ammonia adding pipes, and valves are respectively arranged on the ammonia adding pipes.
The oxidation tank comprises an absorption circulation section at the lower part and an oxidation section at the upper part; an absorption circulation liquid inlet and an absorption circulation liquid outlet are arranged on the absorption circulation section, and a filter is arranged in the absorption circulation liquid outlet; the oxidation section is provided with an oxidation air distribution pipe and an oxidation packing layer, and the upper part of the oxidation section is connected with an overflow pipe which is communicated with a concentration crystallization tank of the desulfurizing tower.
The second purpose of the invention is realized by the following steps: an energy-saving ammonia desulphurization process with ultralow emission comprises the following steps:
a. the ammonia desulphurization device is arranged; injecting desulfurization liquid into a concentration crystallization tank of the desulfurization tower, and stopping injecting liquid when the liquid level is close to the height of an overflow pipe;
b. introducing sulfur-containing high-temperature flue gas into a concentration spraying section of a desulfurizing tower through an air inlet pipe, circularly spraying a desulfurizing liquid to the sulfur-containing high-temperature flue gas by using a concentration section spraying pipe and a concentrated liquid circulating pump, and evaporating and concentrating the desulfurizing liquid while cooling the flue gas to obtain ammonium sulfate slurry; the back flushing spray pipe sprays absorption liquid through an absorption liquid circulating pump to back flush the absorption and collection liquid disc;
c. extracting ammonium sulfate slurry in the concentration and crystallization tank by using a stirring and discharging pump, injecting dilute solution concentrated by the first cyclone into an annular stirrer in the concentration and crystallization tank, and continuously stirring by using the annular stirrer to promote concentration and crystallization of ammonium sulfate in the concentration and crystallization tank; the ammonium sulfate slurry overflowing through an overflow pipe on the concentration crystallization tank flows into an oxidation tank, and an oxidation fan continuously blows oxidation air into the oxidation tank to enable the flowing ammonium sulfate slurry to be subjected to catalytic oxidation in the oxidation tank;
d. pumping the ammonium sulfate slurry in the concentrated crystallization tank into a first cyclone by a stirring discharge pump through a liquid outlet pipe at the lower part of the concentrated crystallization tank, concentrating the ammonium sulfate slurry by the first cyclone, injecting the concentrated ammonium sulfate slurry into a second cyclone, further concentrating the ammonium sulfate slurry by the second cyclone, separating the ammonium sulfate from the concentrated slurry by a centrifugal machine, sending separated mother liquor flowing out of the centrifugal machine into a mother liquor tank, pumping the separated mother liquor back into the concentrated crystallization tank of the desulfurizing tower by a mother liquor pump, and continuously participating in circulation;
e. the ascending flue gas treated by the concentration spraying section enters SO through a liquid collecting disc of the absorption section2The absorption section is characterized in that the three layers of spraying liquid distribution pipes are used for circularly spraying absorption liquid to the entering smoke through an absorption liquid circulating pump; the three layers of absorption section packing layers absorb the residual SO in the flue gas layer by layer2(ii) a The spraying liquid distribution pipe arranged between the three packing layers of the absorption section sprays the absorption liquid, and simultaneously, ammonia is uniformly added into the absorption liquid between the packing layers to perform online regeneration operation on the absorption liquid SO as to ensure that the absorption liquid recovers to absorb SO2The ability of (c); from SO2Absorbing section is receivedCollective absorption of SO2The absorption liquid enters an absorption circulation section at the lower part of the oxidation tank, most of the absorption liquid is circularly sprayed in the desulfurization tower through an absorption liquid circulating pump and a spraying liquid distribution pipe, a small part of the absorption liquid rises to enter an oxidation section and is oxidized by bubbling air, and after the oxidation rate of ammonium sulfite reaches more than 99%, liquid is supplemented to a concentrated spraying section of the desulfurization tower through an overflow pipe at the upper part of the oxidation tank;
f. via SO2The flue gas desulfurized in the absorption section enters a cleaning section, and the cleaning liquid collected from the absorption section is pumped to a spray pipe of the cleaning section by a cleaning circulating pump to circularly spray and clean the entering flue gas; the cleaned flue gas is cleaned again by the flushing spray pipe in the demisting section, fog drops in the desulfurized flue gas are eliminated by the multistage demisters, and finally the flue gas is discharged through a chimney on the upper part of the desulfurizing tower.
An accident spray pipe is arranged in a smoke inlet pipe of the desulfurizing tower and is connected with a process water main pipe so as to carry out early spray washing and cooling on the smoke passing through the air inlet pipe under the condition of overtemperature by utilizing process water.
The invention has the beneficial effects that:
1. set up concentrate mixing system in the desulfurizing tower, make concentrated crystallizer can adopt flat structure, under the same condition of thiamine crystallization section volume, compare with original awl end structure, can reduce the height of desulfurizing tower, the corresponding cost that has reduced the desulfurizing tower. The swirler is additionally arranged at the outlet of the stirring discharge pump, and the concentrated solution is used for discharging, so that the original discharge pump is omitted, the equipment quantity is reduced, the solid content of the discharged solution is increased through secondary concentration of the swirler, and the mother solution circulation volume is reduced.
2. The concentration spraying is arranged at the flue gas inlet, the overall height of the concentration spraying section is reduced, the manufacturing cost of the desulfurizing tower is correspondingly reduced, and meanwhile, the adverse effect of uneven cooling of the flue gas due to uneven distribution of the flue gas in the concentration spraying section is eliminated.
3、SO2The absorption section adopts a structure of a plurality of layers of packing layers, and the ammonia adding pipe is communicated with the spraying liquid distributing pipe among the packing layers for spraying, so that the absorption liquid can be regenerated between the packing layers without large circulation, therebyThe number of the absorption liquid circulating pumps is reduced, the power consumption is reduced, and the unfavorable conditions that the pH value is increased due to excessive ammonia addition at one position of the circulating liquid to cause ammonia escape and aerosol formation are avoided.
4. By adopting the catalytic oxidation process outside the tower, the volume of the oxidation tank is reduced, the manufacturing cost of the oxidation tank is reduced, the pressure of required oxidation air is reduced, and the manufacturing cost and the power consumption of the oxidation fan are reduced. The implementation of the catalytic oxidation process outside the tower can reduce SO of the desulfurizing tower2The setting height of the absorption section is increased, and the static pressure of the inlet of the absorption liquid circulating pump is increased by heightening the position of the oxidation tank, so that the setting height of the spray pipe of the absorption section is reduced; at the same time, SO2The absorption adopts a filler structure, the operation flexibility is large (30-120 percent), and the spray head on the spray liquid distribution pipe does not need backpressure more than 0.07MPa, thereby reducing the lift of the absorption liquid circulating pump and reducing SO2The working power consumption of the absorption section.
5. The invention cancels the configuration of the cleaning water tank, and utilizes the high potential energy of the return liquid of the liquid collecting tray of the cleaning section to improve the inlet pressure of the cleaning circulating pump, thereby reducing the lift of the cleaning circulating pump. In addition, a cleaning water tank is omitted, the liquid capacity of the whole desulfurization system is reduced, the capacity of an accident pool is correspondingly reduced, and the occupied area of the desulfurization system and the overall equipment investment are reduced.
6. The invention adopts the arrangement form of the high-efficiency baffle demister connected with the ultra-clean wire mesh demister in series and the dust removal process, so that the content of liquid drops at the flue gas outlet of the desulfurizing tower can be reduced to 50 My Ag/M3In the following, ultra-low emission is realized, so that a wet electric device of the traditional ammonia desulphurization system can be saved, and the aims of further reducing the investment and reducing the power consumption are fulfilled.
7. The invention eliminates the cleaning water tank and reduces the oxidation tank, so that the capacity of each liquid in the system is reduced, the volume of the accident tank can be reduced, and the investment is reduced.
In a word, the invention further perfects the ammonia desulphurization process of the ultra-low emission flue gas, adopts the energy-saving wet-electricity-free process of in-tower crystallization, outside-tower oxidation, regeneration between sections and multi-stage purification, reduces the overall cost of the ammonia desulphurization device by more than 30 percent, reduces the power consumption of the system by more than 60 percent, realizes the desulphurization and dust removal with low investment, low energy consumption and high efficiency, reduces the construction cost and the operation cost of the device while ensuring the ultra-low emission, and realizes the environmental protection and the economic benefit.
Drawings
Fig. 1 is a schematic structural view of the present invention.
In the figure: 1. a desulfurizing tower; 2. a second-stage cleaning circulating pump; 3. a first-stage cleaning circulating pump; 4. an absorption liquid circulating pump; 5. an oxidation fan; 6. an oxidation tank; 7. an annular agitator; 8. a concentrated solution circulating pump; 9. a stirring discharge pump; 10. a primary swirler; 11. a centrifuge; 12. a mother liquor tank; 13. a mother liquor pump; 14. a secondary cyclone; 15. a smoke inlet pipe; 16. an accident spray pipe; 17. a concentration section spray pipe; 18. backwashing the spray pipe; 19. an absorption section liquid collecting disc; 20. a filling layer of the absorption section; 21. a spraying liquid distribution pipe; 22. a liquid collecting disc of the primary cleaning section; 23. a first-stage cleaning section packing layer; 24. a first-stage cleaning section spray pipe; 25. a liquid collecting disc of the secondary cleaning section; 26. a second-stage cleaning section packing layer; 27. a secondary cleaning section spray pipe; 28. a baffle demister; 29. a first flushing shower; 30. a wire mesh demister; 31. the second flushing spray pipe 32, the overflow pipe 33, the liquid outlet pipe 34, the process water main pipe 35, the desalted water main pipe 36, the ammonia supply water main pipe 37 and the ammonia adding pipe.
Detailed Description
As shown in FIG. 1, the ultra-low emission ammonia desulfurization device of the present invention comprises a desulfurization tower 1, an oxidation tank 6, a mother liquor tank 12, a primary cyclone 10, a secondary cyclone 14, a centrifuge 11, a plurality of circulating pumps, and the like.
The desulfurizing tower 1 is divided into an ammonium sulfate crystallization section, a concentration spraying section and SO from bottom to top in sequence2The device comprises an absorption section, a primary cleaning section, a secondary cleaning section, a primary demisting section and an ultra-clean demisting section.
The ammonium sulfate crystallization section of the desulfurization tower 1 is located at the bottom of the desulfurization tower 1 and comprises a flat-bottom-shaped concentration crystallization tank as the bottom of the desulfurization tower and an annular stirrer 7 arranged in the concentration crystallization tank. A liquid outlet pipe 33 connected to the lower part of the concentrated crystallization tank is externally connected with a stirring discharge pump 9, the outlet pipe of the stirring discharge pump 9 is connected to the inlet of the first cyclone 10, and the dilute liquid outlet pipe of the first cyclone 10 is connected to the liquid injection port of the annular stirrer 7. The concentrated liquid outlet pipe of the first cyclone 10 is connected to the inlet of the second cyclone 14, the concentrated liquid outlet pipe of the second cyclone 14 is connected to the centrifuge 11, the dilute liquid outlet pipe of the second cyclone 14 is connected to the mother liquor tank 12, and the outlet pipe of the mother liquor tank 12 is communicated to the concentrated crystallization tank of the desulfurizing tower 1 through the mother liquor pump 13. The stirring discharge pump 9 and the first cyclone 10 continuously supply the circular stirrer 7 with circulating stirring liquid, so that the circular stirrer 7 continuously stirs to facilitate the concentration and crystallization of ammonium sulfate. The ammonium sulfate slurry concentrated by the primary cyclone 10 is sent to a secondary cyclone 14 for further concentration, and then sent to a centrifuge 11 for separating ammonium sulfate after concentration, and the separated mother liquor of the centrifuge is sent to a mother liquor tank 12. The mother liquor tank 12 collects the dilute liquid flowing out of the secondary cyclone and the mother liquor separated by the centrifuge, and the dilute liquid and the mother liquor are sent back to the concentration crystallization tank of the desulfurizing tower 1 by the mother liquor pump 13 to continue to participate in circulation.
The concentration spray section of the desulfurizing tower 1 is arranged at the upper part of the concentration crystallization tank, and comprises a smoke inlet pipe 15 inserted on the wall of the desulfurizing tower, a concentration section spray pipe 17 arranged at the inner port of the smoke inlet pipe, a back flush spray pipe 18 positioned above the smoke inlet pipe 15 and the like. The concentrated section spray pipe 17 is externally connected with a concentrated solution circulating pump 8, and concentrated slurry is circularly sprayed and the flue gas is cooled through the concentrated circulating pump 8. The liquid inlet end of the concentrated solution circulating pump 8 is communicated with the ammonium sulfate crystallization section through a pipeline, and the ammonium sulfate slurry in the ammonium sulfate crystallization section is used for water washing desulfurization of the flue gas entering the desulfurizing tower 1. The back-flushing spray pipe 18 is externally connected with an absorption liquid circulating pump 4 and is provided with a back-flushing valve, and the absorption liquid is used for carrying out back-flushing type secondary desulfurization and cooling on the flue gas. An accident spray pipe 16 is also arranged in the smoke inlet pipe 15, an accident valve is arranged on the accident spray pipe 16, and the accident spray pipe 16 is connected with a process water main pipe 34 so as to carry out early spray washing dust removal on the smoke passing through the smoke inlet pipe 15 by using process water when needed.
SO of desulfurizing tower 12The absorption section comprises an absorption section liquid collecting disc 19 arranged at the upper part of the concentrated spraying section, three absorption section packing layers 20 arranged above the absorption section liquid collecting disc 19 and a spraying liquid distribution pipe arranged in the space above each absorption section packing layer21. The packing layers 20 of the three absorption sections are arranged at intervals up and down, the inlet pipes of three spraying liquid distributing pipes 21 are connected in parallel with the inlet pipe of the back flushing spraying pipe 18 in the concentration spraying section outside the tower and then connected with the outlet end of the absorption liquid circulating pump 4, the inlet end of the absorption liquid circulating pump 4 is connected to the absorption liquid outlet of the oxidation tank 6 through a pipeline, the absorption liquid inlet of the oxidation tank 6 is connected with an absorption liquid return pipe arranged on the liquid collecting tray 19 of the absorption section through a pipeline, and the absorption liquid enters the absorption circulation section at the lower part of the oxidation tank 6. The inlet pipes of the spraying liquid distribution pipes 21 are respectively connected with a control valve, and the three spraying liquid distribution pipes 21 circularly spray the absorption liquid through the absorption liquid circulating pump 4. An ammonia adding pipe 37 (an ammonia adding mixer can also be arranged) for providing ammonia water is connected on the inlet pipe of the spraying liquid distribution pipe 21 arranged between the three layers of absorption section packing layers 20, and the ammonia adding pipe 37 is connected with the ammonia supply main pipe 36. Ammonia is uniformly added into the absorption liquid among the filler layers through the spraying liquid distribution pipes 21 arranged among the layers, and the absorption liquid is subjected to on-line regeneration operation SO that the absorption liquid can recover to absorb SO 2The ability of the cell to perform.
The first-stage cleaning section of the desulfurizing tower 1 is arranged at SO2A first-stage cleaning section liquid collecting disc 22 at the upper part of the absorption section, a first-stage cleaning section packing layer 23 at the upper part of the first-stage cleaning section liquid collecting disc, and a first-stage cleaning section spray pipe 24 at the upper part of the first-stage cleaning section packing layer 23. The first-stage cleaning section spray pipe 24 is connected to the outlet end of the first-stage cleaning circulating pump 3 through a pipeline, and the inlet end of the first-stage cleaning circulating pump 3 is connected with a cleaning liquid return pipe arranged on the first-stage cleaning section liquid collecting tray 22. The first-stage cleaning section spray pipe 24 carries out circulating spray cleaning through the first-stage cleaning circulating pump 3.
The second-stage cleaning section of the desulfurizing tower 1 comprises a second-stage cleaning section liquid collecting disc 25 arranged on the upper part of the first-stage cleaning section, a second-stage cleaning section packing layer 26 positioned on the upper part of the second-stage cleaning section liquid collecting disc, and a second-stage cleaning section spray pipe 27 positioned on the upper part of the second-stage cleaning section packing layer 26. The second-stage cleaning section spray pipe 27 is connected to the outlet end of the second-stage cleaning circulating pump 2 through a pipeline, and the inlet end of the second-stage cleaning circulating pump 2 is connected with a cleaning liquid return pipe arranged on the second-stage cleaning section liquid collecting tray 25. The second cleaning section spray pipe 27 performs circulating spray cleaning by the second cleaning circulating pump 2.
The primary demisting section of the desulfurizing tower 1 comprises two layers of baffle plate demisters 28 which are positioned at the upper part of the secondary cleaning section and are arranged at intervals up and down, and a first washing spray pipe 29 which is arranged between the two layers of baffle plate demisters. The first flushing spray pipe 29 is externally connected with a process water main pipe 34, and the desulfurized flue gas is flushed by the process water of the production system. The baffle demister 28 is used to remove moisture from the desulfurized flue gas.
The ultra-clean demisting section of the desulfurizing tower 1 comprises two layers of wire mesh demisters 30 arranged at an upper interval and a lower interval and a second flushing spray pipe 31 arranged between the two layers of wire mesh demisters 30. The second flushing spray pipe 31 is externally connected with a desalted water main pipe 35, and the desalted water of the production system is utilized to flush the desulfurized flue gas. The lower wire mesh demister 30 is arranged on the top surface of the upper baffle demister 28 to form a one-level combined demister, and the lower baffle demister 28 and the upper wire mesh demister 30 are matched to form a three-level demisting, so that the content of liquid drops at the flue gas outlet of the desulfurizing tower can be reduced to 50 Ag/M3The following.
In the ammonia desulfurization apparatus of the present invention, the ammonia supply header pipe 36 is connected to the stirring discharge pump inlet pipe, the primary cleaning circulation pump inlet pipe, the secondary cleaning circulation pump inlet pipe, and the absorption liquid circulation pump inlet pipe through the respective ammonia addition pipes, and the respective ammonia addition pipes are connected to the control valves.
In FIG. 1, the oxidation tank 6 in the ammonia desulfurization apparatus includes two sections, a lower absorption cycle section and an upper oxidation section. An absorption circulation section of the oxidation tank 6 is provided with an absorption circulation liquid inlet and an absorption circulation liquid outlet, and a built-in filter is arranged in the absorption circulation liquid outlet. An oxidation air distribution pipe and an oxidation filler layer are arranged in an oxidation section of the oxidation tank 6, an oxidation fan 5 is connected with the oxidation air distribution pipe inserted into the oxidation tank 6, and oxidation air is continuously blown into the oxidation tank 6, so that a small part of absorption circulating liquid entering the oxidation section is subjected to catalytic oxidation in the oxidation section. An overflow pipe 32 is connected to an upper part of the oxidation stage of the oxidation tank 6, and the overflow pipe 32 is connected to an upper part of the concentration crystallization tank of the desulfurization tower 1 to supplement the absorption circulation liquid overflowing the oxidation tank 6 into the concentration crystallization tank of the desulfurization tower 1.
The energy-saving ammonia desulphurization process with ultralow emission comprises the following steps:
1. the energy-saving ammonia desulfurization device with ultra-low discharge is arranged, the desulfurization liquid is injected into the concentration crystallization tank of the desulfurization tower 1, and the injection is stopped when the liquid level is close to the height of the overflow pipe 32.
2. Introducing sulfur-containing high-temperature flue gas into a concentration spraying section of a desulfurizing tower 1 through an air inlet pipe 15, circularly spraying a desulfurizing liquid to the sulfur-containing high-temperature flue gas by using a concentration section spraying pipe 17 and a concentrated liquid circulating pump 8, cooling the flue gas, and simultaneously cooling SO in the flue gas2Reacts with ammonia water in the desulfurization liquid to form ammonium sulfate slurry. The back flushing spray pipe 18 sprays SO through the absorption liquid circulating pump 42And the absorption liquid generated in the absorption section is used for carrying out back-flushing type secondary desulfurization and cooling on the entering flue gas.
An accident spray pipe 16 is also arranged in the smoke inlet pipe 15, an accident valve is arranged on the accident spray pipe 16, and the accident spray pipe 16 is connected with a process water main pipe 34 so as to carry out early spray washing cooling on the smoke passing through the gas inlet pipe 15 by using process water when needed.
3. Pumping ammonium sulfate slurry in the concentration and crystallization tank by using a stirring and discharging pump 9, injecting dilute solution concentrated by a first cyclone 10 into an annular stirrer 7 in the concentration and crystallization tank, and continuously stirring the annular stirrer 7 so as to facilitate concentration and crystallization of ammonium sulfate in the concentration and crystallization tank. The ammonium sulfate slurry overflowing through the overflow pipe 32 of the concentration and crystallization tank flows into the oxidation tank 6, and the oxidation fan 5 continuously blows oxidation air into the oxidation tank 6 to catalytically oxidize the ammonium sulfate slurry flowing into the oxidation tank 6.
4. The stirring discharge pump 9 pumps the ammonium sulfate slurry in the concentrated crystallization tank into the first cyclone 10 through a liquid outlet pipe 33 at the lower part of the concentrated crystallization tank, the first cyclone 10 concentrates the ammonium sulfate slurry and then injects the ammonium sulfate slurry into the second cyclone 14, the second cyclone 14 further concentrates the ammonium sulfate slurry, the concentrated slurry is separated into ammonium sulfate by the centrifuge 11, the separated mother liquor flowing out of the centrifuge is sent to the mother liquor tank 12, and the separated mother liquor is pumped back to the concentrated crystallization tank of the desulfurizing tower 1 through the mother liquor pump 13 to continue to participate in circulation.
5. The ascending flue gas treated by the concentration spraying section passes through the absorption section setThe liquid disk 19 enters SO2In the absorption section, the spraying liquid distribution pipes 21 arranged in three layers carry out circulating spraying of absorption liquid on the entering smoke through the absorption liquid circulating pump 4; the three layers of absorption section packing layers 20 absorb the residual SO in the flue gas layer by layer2. The spraying liquid distribution pipe 21 arranged between the three packing layers of the absorption section sprays the absorption liquid, and simultaneously, ammonia is uniformly added into the absorption liquid between the packing layers to perform online regeneration operation on the absorption liquid SO as to ensure that the absorption liquid recovers to absorb SO2The ability of the cell to perform.
From SO2Absorbed SO collected at the absorption stage2The absorption liquid enters an absorption circulation section at the lower part of the oxidation tank 6, and most of the absorption liquid is circularly sprayed in the desulfurizing tower through an absorption liquid circulating pump 4 and a spraying liquid distribution pipe 21; a small part of the ammonium sulfite rises to enter an oxidation section and is oxidized by the bubbling air, and after the oxidation rate of the ammonium sulfite reaches more than 99 percent, the liquid is supplemented to the concentration spray section of the desulfurizing tower 1 through an overflow pipe 32 at the upper part of the oxidation tank 6.
6. Via SO2The flue gas of absorption section desulfurization treatment gets into the one-level and washs the section through one-level washing section liquid collecting tray 22, washs the washing liquid that the section collecting pipe 24 pump sending was collected from the one-level from one-level by one-level washing circulating pump 3 to one-level, carries out the circulation to the flue gas that gets into and sprays the washing.
7. The flue gas cleaned in the first cleaning section enters the second cleaning section through the second cleaning section liquid collecting disc 25, and the cleaning liquid collected from the second cleaning section is pumped to the second cleaning section spray pipe 27 by the second cleaning circulating pump 2, so that the flue gas is circularly sprayed and cleaned.
8. The flue gas cleaned in the secondary cleaning section enters a demisting section, the moisture in the desulfurized flue gas is removed by a baffle plate demister 28 in the primary demisting section, and process water is sprayed by a first washing spray pipe 29 to wash the desulfurized flue gas; then the second flushing spray pipe 31 in the ultra-clean demisting section sprays desalted water, the wire mesh demister 30 eliminates the moisture in the desulfurized flue gas, and finally the clean gas meeting the environmental protection requirement is discharged from a chimney at the upper part of the desulfurizing tower 1.
Claims (9)
1. An energy-saving ultra-low emission ammonia desulphurization device,comprises a desulfurizing tower and an oxidation tank, and is characterized in that the desulfurizing tower is divided into an ammonium sulfate crystallization section, a concentration spraying section and SO from bottom to top in sequence2An absorption section, a cleaning section and a demisting section;
the ammonium sulfate crystallization section comprises a flat-bottom-shaped concentration crystallization tank serving as the bottom of the desulfurization tower and an annular stirrer arranged in the concentration crystallization tank; a liquid outlet pipe connected to the lower part of the concentrated crystallization tank is externally connected with a stirring discharge pump, the outlet pipe of the stirring discharge pump is connected to the inlet of a first cyclone, and the dilute liquid outlet pipe of the first cyclone is connected to the annular stirrer;
the concentration spray section comprises a smoke inlet pipe inserted on the tower wall of the desulfurization tower, a concentration section spray pipe arranged at the inner port of the smoke inlet pipe and a back flush spray pipe positioned above the smoke inlet pipe; the back flushing spray pipe is externally connected with an absorption liquid circulating pump, the concentration section spray pipe is externally connected with a concentration liquid circulating pump, and the liquid inlet end of the concentration liquid circulating pump is communicated with the ammonium sulfate crystallization section through a pipeline;
the SO2The absorption section comprises an absorption section liquid collecting disc arranged at the upper part of the concentration spraying section, three absorption section packing layers which are arranged above the absorption section liquid collecting disc at intervals up and down, and a spraying liquid distributing pipe arranged in the space above each absorption section packing layer; the inlet pipes of the three spraying liquid distribution pipes are connected in parallel outside the tower and then connected with an absorption liquid circulating pump, the inlet end of the absorption liquid circulating pump is connected to the absorption liquid outlet of the oxidation tank through a pipeline, and the absorption liquid inlet of the oxidation tank is connected with an absorption liquid return pipe arranged on a liquid collecting disc of an absorption section through a pipeline; and an ammonia adding pipe for providing ammonia water is connected to the inlet pipe of the spraying liquid distribution pipe arranged between the absorption section packing layers, and the ammonia adding pipe is externally connected with an ammonia supply main pipe.
2. The ammonia desulfurization apparatus of claim 1, wherein the cleaning section comprises a primary cleaning section and a secondary cleaning section;
the first-stage cleaning section comprises a cleaning zone arranged at SO2A first-stage cleaning section liquid collecting disc at the upper part of the absorption section, a first-stage cleaning section packing layer at the upper part of the first-stage cleaning section liquid collecting disc and a first-stage cleaning section packing layer at the upper part of the first-stage cleaning section packing layerThe first-stage cleaning section of the spray pipe; the first-stage cleaning section spray pipe is externally connected with a first-stage cleaning circulating pump, and the inlet end of the first-stage cleaning circulating pump is connected with a cleaning liquid return pipe arranged on a first-stage cleaning section liquid collecting disc;
the secondary cleaning section comprises a secondary cleaning section liquid collecting disc arranged at the upper part of the primary cleaning section, a secondary cleaning section packing layer positioned at the upper part of the secondary cleaning section liquid collecting disc and a secondary cleaning section spray pipe positioned at the upper part of the secondary cleaning section packing layer; the spraying pipe of the second-stage cleaning section is externally connected with a second-stage cleaning circulating pump, and the inlet end of the second-stage cleaning circulating pump is connected with a cleaning liquid return pipe arranged on a liquid collecting disc of the second-stage cleaning section.
3. The ammonia desulfurization apparatus of claim 2, wherein the demister section comprises a primary demister section and an ultra-clean demister section;
the primary demisting section comprises two layers of baffle plate demisters positioned at the upper part of the secondary cleaning section and arranged at intervals up and down and a first washing spray pipe arranged between the two layers of baffle plate demisters, and the first washing spray pipe is externally connected with a process water main pipe;
the ultra-clean demisting section comprises two layers of screen demisters and a second washing spray pipe, wherein the two layers of screen demisters are arranged at an upper interval and a lower interval, the second washing spray pipe is arranged between the two layers of screen demisters, the screen demisters on the lower layer are arranged on the top surface of the baffle plate demister on the upper layer, and the second washing spray pipe is externally connected with a desalted water header pipe.
4. The ammonia desulfurization apparatus of claim 1, wherein the concentrate outlet of the first cyclone is connected to the inlet of a second cyclone, the concentrate outlet of the second cyclone is connected to the centrifuge, and the dilute outlet of the second cyclone is connected to the mother liquor tank.
5. The ammonia desulfurization apparatus according to claim 1, wherein an emergency shower is further provided in the flue gas inlet pipe, and the emergency shower is connected to a process water main.
6. The ammonia desulfurization apparatus according to claim 1, wherein the ammonia supply header pipe is connected to the agitation discharge pump inlet pipe, the primary cleaning circulation pump inlet pipe, the secondary cleaning circulation pump inlet pipe, and the absorption liquid circulation pump inlet pipe through ammonia feed pipes, and valves are connected to the ammonia feed pipes.
7. The ammonia desulfurization apparatus of claim 1, wherein the oxidation tank comprises a lower absorption cycle section and an upper oxidation section; an absorption circulation liquid inlet and an absorption circulation liquid outlet are arranged on the absorption circulation section, and a filter is arranged in the absorption circulation liquid outlet; the oxidation section is provided with an oxidation air distribution pipe and an oxidation packing layer, and the upper part of the oxidation section is connected with an overflow pipe which is communicated with a concentration crystallization tank of the desulfurizing tower.
8. An energy-saving ultra-low emission ammonia desulphurization process is characterized by comprising the following steps:
a. setting up an ammonia desulfurization apparatus as defined in any one of claims 1 to 7; injecting desulfurization liquid into a concentration crystallization tank of the desulfurization tower, and stopping injecting liquid when the liquid level is close to the height of an overflow pipe;
b. introducing sulfur-containing high-temperature flue gas into a concentration spraying section of a desulfurization tower through a gas inlet pipe, circularly spraying desulfurization liquid to the sulfur-containing high-temperature flue gas by using a concentration section spraying pipe and a concentration liquid circulating pump, and cooling the flue gas while making an oxidation liquid into ammonium sulfate slurry; the back flushing spray pipe sprays by an absorption liquid circulating pump to flush the absorption and collection liquid disc;
c. extracting ammonium sulfate slurry in the concentration and crystallization tank by using a stirring and discharging pump, injecting dilute solution concentrated by the first cyclone into an annular stirrer in the concentration and crystallization tank, and continuously stirring by using the annular stirrer to promote concentration and crystallization of ammonium sulfate in the concentration and crystallization tank; the ammonium sulfate slurry overflowing through an overflow pipe on the concentration crystallization tank flows into an oxidation tank, and an oxidation fan continuously blows oxidation air into the oxidation tank to enable the flowing ammonium sulfate slurry to be subjected to catalytic oxidation in the oxidation tank;
d. pumping the ammonium sulfate slurry in the concentrated crystallization tank into a first cyclone by a stirring discharge pump through a liquid outlet pipe at the lower part of the concentrated crystallization tank, concentrating the ammonium sulfate slurry by the first cyclone, injecting the concentrated ammonium sulfate slurry into a second cyclone, further concentrating the ammonium sulfate slurry by the second cyclone, separating the ammonium sulfate from the concentrated slurry by a centrifugal machine, sending separated mother liquor flowing out of the centrifugal machine into a mother liquor tank, pumping the separated mother liquor back into the concentrated crystallization tank of the desulfurizing tower by a mother liquor pump, and continuously participating in circulation;
e. the ascending flue gas treated by the concentration spraying section enters SO through a liquid collecting disc of the absorption section2The absorption section is characterized in that the three layers of spraying liquid distribution pipes are used for circularly spraying absorption liquid to the entering smoke through an absorption liquid circulating pump; the three layers of absorption section packing layers absorb the residual SO in the flue gas layer by layer2(ii) a The spraying liquid distribution pipe arranged between the three packing layers of the absorption section sprays the absorption liquid, and simultaneously, ammonia is uniformly added into the absorption liquid between the packing layers to perform online regeneration operation on the absorption liquid SO as to ensure that the absorption liquid recovers to absorb SO2The ability of (c); from SO2Absorbed SO collected at the absorption stage2The absorption liquid enters an absorption circulation section at the lower part of the oxidation tank, and is circularly sprayed in the desulfurizing tower through an absorption liquid circulating pump and a spraying liquid distribution pipe;
f. via SO2The flue gas desulfurized in the absorption section enters a cleaning section, and the cleaning liquid collected from the absorption section is pumped to a spray pipe of the cleaning section by a cleaning circulating pump to circularly spray and clean the entering flue gas; the cleaned flue gas is cleaned again by the flushing spray pipe in the demisting section, fog drops in the desulfurized flue gas are eliminated by the multistage demisters, and finally the flue gas is discharged through a chimney on the upper part of the desulfurizing tower.
9. The ammonia desulfurization process of claim 8 wherein an emergency spray pipe is disposed in the flue gas inlet pipe of the desulfurization tower and connected to the process water header pipe to perform a preliminary spray water washing cooling of the flue gas passing through the gas inlet pipe with the process water.
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