CN113003637A - System for flue gas waste heat utilization and desulfurization waste water zero release coupling - Google Patents
System for flue gas waste heat utilization and desulfurization waste water zero release coupling Download PDFInfo
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- CN113003637A CN113003637A CN202110487752.5A CN202110487752A CN113003637A CN 113003637 A CN113003637 A CN 113003637A CN 202110487752 A CN202110487752 A CN 202110487752A CN 113003637 A CN113003637 A CN 113003637A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 130
- 239000003546 flue gas Substances 0.000 title claims abstract description 128
- 239000002351 wastewater Substances 0.000 title claims abstract description 104
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 94
- 230000023556 desulfurization Effects 0.000 title claims abstract description 94
- 239000002918 waste heat Substances 0.000 title claims abstract description 37
- 230000008878 coupling Effects 0.000 title claims abstract description 16
- 238000010168 coupling process Methods 0.000 title claims abstract description 16
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 160
- 239000000428 dust Substances 0.000 claims abstract description 34
- 238000011282 treatment Methods 0.000 claims abstract description 26
- 238000001704 evaporation Methods 0.000 claims abstract description 17
- 230000008020 evaporation Effects 0.000 claims abstract description 17
- 238000004065 wastewater treatment Methods 0.000 claims abstract description 11
- 239000012141 concentrate Substances 0.000 claims description 15
- 238000002156 mixing Methods 0.000 claims description 12
- 239000002893 slag Substances 0.000 claims description 6
- 239000003245 coal Substances 0.000 claims description 5
- 239000002699 waste material Substances 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 3
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims 2
- 241000242583 Scyphozoa Species 0.000 claims 1
- 230000001172 regenerating effect Effects 0.000 abstract description 8
- 230000007613 environmental effect Effects 0.000 abstract description 6
- 238000004134 energy conservation Methods 0.000 abstract description 4
- 238000010586 diagram Methods 0.000 description 11
- 239000012535 impurity Substances 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 229910001385 heavy metal Inorganic materials 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000010129 solution processing Methods 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 239000002956 ash Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 239000010881 fly ash Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical class OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- -1 chloride ions Chemical class 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to a system for coupling flue gas waste heat utilization and zero emission of desulfurization wastewater, which comprises a condensate water regenerative system, a desulfurization wastewater treatment system and a flue gas waste heat utilization system; the condensate water backheating system sequentially comprises a cold water outlet, a hot water outlet and a water return port on a condensate water main pipe, and the three are connected with a condensate water pipeline; the flue gas waste heat utilization system comprises an SCR system and an FGD system which are connected through a flue gas pipeline; an air preheater, a dust remover and an induced draft fan are sequentially arranged on the flue gas pipeline; the desulfurization wastewater treatment system comprises a steam generator, a desulfurization wastewater evaporation and concentration system and a desulfurization wastewater concentrated solution treatment system; the flue gas pipeline is also provided with at least 1 low-temperature economizer. The system for coupling the flue gas waste heat utilization with the desulfurization wastewater zero discharge realizes the mutual coupling and coordination of the flue gas waste heat utilization system and the desulfurization wastewater zero discharge system, and achieves multiple benefits of energy conservation, water conservation and environmental protection.
Description
Technical Field
The invention relates to the field of energy conservation and environmental protection, in particular to a system for coupling flue gas waste heat utilization and desulfurization wastewater zero discharge.
Background
In the wet desulphurization process of the boiler flue gas, in order to prevent the concentration of soluble chloride ions and fine dust particles in the slurry from being too high, a certain amount of desulphurization wastewater needs to be discharged from the absorption tower at regular time so as to maintain the material balance in the desulphurization device. The impurities of the wet desulphurization waste water mainly come from flue gas, a desulfurizer and desulphurization process water, the impurities of the flue gas come from the combustion of coal, and the impurities of the desulfurizer come from the dissolution of limestone. The coal contains various elements including heavy metals, the elements generate various compounds after combustion, one part of the compounds are discharged out of a hearth along with slag, the other part of the compounds enter an absorption tower of the desulfurization device along with flue gas, are dissolved in absorption slurry and are continuously concentrated in the circulation process of the absorption slurry, and therefore the impurity content in the desulfurization wastewater is high. The impurities contained in the desulfurization wastewater are mainly solid suspended matters, supersaturated sulfite, sulfate, chloride and trace heavy metals, wherein the heavy metals are first pollutants which are strictly controlled in the national environmental protection standard. At present, the conventional desulfurization wastewater treatment process comprises neutralization, reaction, flocculation and precipitation treatment, and heavy metals and other suspended impurities in the desulfurization wastewater are precipitated by adding a medicament and are removed. The precipitated sludge is dewatered to form a sludge cake and is transported to the outside of the plant.
The conventional desulfurization wastewater treatment process can only remove heavy metals and other suspended impurities contained in the desulfurization wastewater, but cannot remove soluble ions such as chloride ions, sodium ions and the like in water. The high salt content of the power plant desulfurization wastewater leads to the treatment of the wastewater which can only be reused in a coal ash system. Therefore, most of the desulfurization waste water of the thermal power plant can be recycled to a coal and ash system to achieve zero emission. The reuse of the desulfurization waste water is limited because a part of power plants adopt a dry ash removal mode for water conservation and comprehensive utilization of ash; and the limitation of the water consumption for spraying in a coal yard causes that the desulfurization wastewater is difficult to be completely recycled in a factory.
With the improvement of national requirements on environmental protection, newly-built coal-fired power plants gradually require the achievement of zero emission of desulfurization wastewater. In recent years, some domestic research institutions and power plants try and apply different desulfurization wastewater zero emission technical routes, including a technical route of pretreatment, membrane concentration and an evaporative crystallizer, a technical route of concentration and evaporation by using waste heat of flue gas, a technical route of direct evaporation of a main flue or a bypass flue, mixed evaporation of flue gas and the like. The technical route of 'concentration and evaporation by using the waste heat of flue gas' has the advantages of moderate investment, low operation cost, small occupied area and the like, and becomes a key technical route concerned in the industry, but the key point is the process of desulfurizing waste water and the requirement for an external heat source.
At present, most thermal power plants are provided with flue gas waste heat utilization systems, and flue gas waste heat is heated into condensed water through a low-temperature economizer, so that the heat economy of a unit is improved. The technical route of 'concentration and evaporation by using the waste heat of the flue gas' also needs the waste heat of the flue gas. However, the overall consideration of a flue gas waste heat utilization system and a desulfurization wastewater zero-emission system, the mutual coordination among the systems and the like are not achieved at present, and the problems are also urgently needed to be solved by people.
Disclosure of Invention
In order to solve the problems, the invention provides a system for coupling flue gas waste heat utilization and desulfurization wastewater zero emission, wherein the flue gas waste heat is utilized to heat condensed water led out from a main condensed water pipeline of a regenerative system, the heated condensed water enters a steam generator, closed circulating water with a certain flow and a certain pressure is heated into steam, and the cooled condensed water returns to the main condensed water of the regenerative system. And steam that steam generator produced gets into desulfurization waste water evaporation concentration system and is used for concentrated desulfurization waste water, returns steam generator after the steam condensation, forms closed circulation, and the concentrated waste water that desulfurization waste water evaporation concentration system produced gets into desulfurization waste water concentrate processing system and handles. The mutual coupling and coordination of the flue gas waste heat utilization system and the desulfurization wastewater zero discharge system are realized, and multiple benefits of energy conservation, water conservation and environmental protection are achieved.
The technical means adopted by the invention are as follows.
The invention relates to a system for coupling flue gas waste heat utilization and zero emission of desulfurization wastewater, which comprises a condensation water regenerative system, a desulfurization wastewater treatment system and a flue gas waste heat utilization system;
the condensate water backheating system sequentially comprises a cold water outlet, a hot water outlet and a backwater port on a condensate water main pipe, the cold water outlet, the hot water outlet and the backwater port are all connected with a condensate water pipeline, the condensate water pipelines respectively connected with the cold water outlet and the hot water outlet are converged at a water outlet mixing port, and a backwater inlet is arranged on the condensate water pipeline connected with the water outlet mixing port of the low-temperature economizer;
the flue gas waste heat utilization system comprises an SCR system and an FGD system; the SCR system is connected with the FGD system through a flue gas pipeline from the SCR system to the FGD system; the flue gas pipeline is sequentially provided with the air preheater and the dust remover;
the desulfurization wastewater treatment system comprises a steam generator, a desulfurization wastewater evaporation and concentration system and a desulfurization wastewater concentrated solution treatment system; the steam generator is connected with the desulfurization wastewater evaporation concentration system through a circulating water pipeline; a concentrated wastewater outlet of the desulfurization wastewater evaporation and concentration system is connected with a concentrated wastewater inlet of the desulfurization wastewater concentrated solution treatment system; the waste water inlet of the desulfurization waste water evaporation and concentration system is connected with a waste water pipeline; the desulfurization wastewater concentrated solution treatment system is arranged on a flue gas branch pipeline of the flue gas pipeline; the desulfurization waste water concentrated solution treatment system is at least connected with the air preheater in parallel; a flue gas branch pipeline connected with the desulfurization wastewater concentrated solution treatment system and a flue gas pipeline are connected with a flue gas merging port;
the flue gas pipeline is also provided with at least 1 low-temperature economizer which is arranged at the inlet and/or the outlet of the dust remover 32, the condensed water pipeline sequentially passes through the low-temperature economizer and the steam generator and then returns to the water return port, and the condensed water pipeline exchanges heat with the flue gas pipeline in the low-temperature economizer; the condensed water pipeline exchanges heat with the circulating water pipeline in the steam generator.
Preferably, a return water outlet is formed in a condensed water pipeline connected with the steam generator and the return water port; the backwater outlet is connected with the backwater inlet through a backwater pipeline.
Preferably, a high-temperature condensed water outlet of the low-temperature economizer is connected with a water return port through a condensed water pipeline; the low-temperature economizer and the water return port are additionally provided with a branch pipeline, and the branch pipeline is connected with the water return inlet after passing through the steam generator.
Preferably, a second low-temperature economizer is arranged on a condensed water pipeline between the low-temperature economizer and the steam generator, and the second low-temperature economizer is also arranged on the flue gas pipeline between the low-temperature economizer and the flue gas merging port; the condensed water pipe exchanges heat with the flue gas pipe in the second low-temperature economizer.
Preferably, a dust remover is arranged on a flue gas pipeline between the air preheater and the flue gas merging port, and a second dust remover is arranged on a flue gas branch pipeline between the desulfurization wastewater concentrated solution treatment system and the flue gas merging port.
Preferably, the desulfurization wastewater concentrated solution treatment system is provided with a waste residue outlet; the waste residue outlet is connected with the residue bin through a pipeline.
Preferably, the flue gas waste heat utilization system further comprises an induced draft fan, and when the low-temperature economizer is arranged at the outlet of the dust remover, the induced draft fan is arranged on a flue gas pipeline between the dust remover and the low-temperature economizer; when the low-temperature economizer is arranged at the inlet of the dust remover, the induced draft fan is arranged on the flue gas pipeline at the outlet of the dust remover.
The invention has the following beneficial effects:
1. the flue gas waste heat utilization system and the desulfurization wastewater zero discharge system are coupled with each other, so that the coordination is good and the adjustment is convenient;
2. the desulfurization waste water zero discharge system utilizes a part of flue gas waste heat, and the rest flue gas heat is returned to the regenerative system through condensed water, so that the heat economy of the unit is improved; meanwhile, the temperature of the raw flue gas entering the desulfurization system is further reduced, the water consumption for desulfurization is reduced, and multiple benefits of energy conservation, water conservation and environmental protection are achieved.
3. The desulfurization waste water is concentrated and then is evaporated by using high-temperature flue gas, so that the consumption of the high-temperature flue gas and the influence on the efficiency of a boiler are greatly reduced.
4. The treatment mode of the high-temperature flue gas after utilization is determined according to the comprehensive utilization condition of the fly ash, and the form is flexible. The part of high-temperature dust-containing flue gas can be independently dedusted after being utilized and then returns to the main flue, thereby avoiding the influence on the comprehensive utilization of the fly ash.
Drawings
Fig. 1 is a schematic system structure according to a first embodiment of the present invention.
Fig. 2 is a schematic system structure diagram of a second embodiment of the present invention.
Fig. 3 is a schematic system structure diagram of a third embodiment of the present invention.
Fig. 4 is a schematic system structure diagram of a fourth embodiment of the present invention.
Fig. 5 is a schematic system structure diagram of a fifth embodiment of the present invention.
Fig. 6 is a schematic system structure diagram of a sixth embodiment of the present invention.
Description of the figure numbers: the system comprises a condensate water regenerative system 1, a desulfurization wastewater treatment system 2, a flue gas waste heat utilization system 3, a condensate water pipeline 4, a circulating water pipeline 5, a wastewater pipeline 6, a flue gas pipeline 7, a water return pipeline 8, a cold water outlet 11, a hot water outlet 12, a water return port 13, a steam generator 21, a desulfurization wastewater evaporation concentration system 22, a desulfurization wastewater concentrate treatment system 23, an air preheater 31, a dust remover 32, a low-temperature economizer 33, a second low-temperature economizer 34, a second dust remover 35, an induced draft fan 36, a water return outlet 41, a water return inlet 42, a water outlet mixing port 43, a flue gas branch pipeline 71, a flue gas merging port 72, a flue gas merging port 73, a concentrated wastewater outlet 221, a wastewater inlet 222, a concentrated wastewater inlet 231, a waste residue outlet 232 and a high-temperature condensate outlet 331.
Detailed Description
Fig. 1 is a schematic structural diagram of a system according to a first embodiment of the present invention, which includes a condensate heat recovery system 1, a desulfurization wastewater treatment system 2, and a flue gas waste heat utilization system 3.
The condensate water regenerative system 1 sequentially comprises a cold water outlet 11, a hot water outlet 12 and a water return port 13 on a condensate water main pipe, wherein the cold water outlet 11, the hot water outlet 12 and the water return port 13 are all connected with the condensate water pipe 4, the condensate water pipe 4 connected with the cold water outlet 11 and the hot water outlet 12 is converged at a water outlet mixing port 43, cold water and hot water from the cold water outlet 11 and the hot water outlet 12 are mixed at the water outlet mixing port 43, the water outlet amount of the cold water and the hot water is controlled by adjusting water outlet valves of the cold water outlet 11 and the hot water outlet 12, so that the purpose of controlling the water outlet temperature at the water outlet mixing port 43 is achieved, and the condensate water from the water outlet mixing port 43 returns to the water return port 13 after passing through a steam generator 21 and a low-temperature economizer 33.
This flue gas waste heat utilization system 3 contains the SCR system, the FGD system, be connected through flue gas pipeline 7 by SCR system to FGD system flue gas trend between this SCR system and the FGD system, this air heater 31 has set gradually on this flue gas pipeline 7, this dust remover 32, draught fan 36 and low temperature economizer 33, this air heater 31 and this dust remover 32 further heat the inside flue gas of flue gas pipeline 7, the dust removal is handled, then in low temperature economizer 33, this flue gas pipeline 7 carries out the heat transfer with this condensate pipe 4, further heat the condensate water in the condensate pipe 4, and cool down the flue gas in the flue gas pipeline 7, and the flue gas after the cooling gets into the FGD system and handles.
This desulfurization wastewater treatment system 2 contains steam generator 21, desulfurization wastewater evaporative concentration system 22, desulfurization wastewater concentrate processing system 23, is connected through circulating water pipeline 5 between this steam generator 21 and this desulfurization wastewater evaporative concentration system 22, and the condensate water through the heating carries out the heat transfer through condensate water pipeline 4 in this steam generator 21 with the closed circulating water in this circulating water pipeline 5, and the closed circulating water heating of certain flow, certain pressure becomes steam. The condensed water pipe 4 of the steam generator 21 connected with the return water port 13 is provided with a return water outlet 41, the condensed water pipe 4 of the low-temperature economizer 33 connected with the outlet water mixing port 43 is provided with a return water inlet 42, the return water outlet 41 is connected with the return water inlet 42 through a return water pipe 8, the condensed water cooled after passing through the steam generator 21 is divided into two flow directions before returning to the return water port 13, one flow direction directly returns to the return water port 13, the other flow direction flows to the condensed water pipe 4 between the outlet water mixing port 43 and the low-temperature economizer 33 through the return water pipe 8 and is mixed with the condensed water in the condensed water pipe, and the flow is controlled through a valve according to actual requirements, so that the temperature of the condensed water can be further adjusted.
The concentrated wastewater outlet 221 of the desulfurization wastewater evaporative concentration system 22 is connected to the concentrated wastewater inlet 231 of the desulfurization wastewater concentrated solution treatment system 23, the wastewater inlet 222 of the desulfurization wastewater evaporative concentration system 22 is connected to the wastewater pipe 6, wastewater enters the desulfurization wastewater evaporative concentration system 22 through the wastewater pipe 6 to be treated, steam formed by circulating water in the circulating water pipe 5 in the steam generator 21 is used for wastewater concentration and desulfurization in the desulfurization wastewater evaporative concentration system 22, then the steam is cooled and liquefied into liquid, the liquid returns to the steam generator 21 through the circulating water pipe 5 to be heated into steam again, and the concentrated wastewater enters the desulfurization wastewater concentrated solution treatment system 23. The desulfurization waste water concentrated solution processing system 23 is arranged on a flue gas branch pipeline 71 of the flue gas pipeline 7, the desulfurization waste water concentrated solution processing system 23 is connected with the air preheater 31 in parallel, the flue gas branch pipeline 71 connected with the desulfurization waste water concentrated solution processing system 23 is connected with the flue gas pipeline 7 and is connected with a flue gas merging port 72, the desulfurization waste water concentrated solution processing system 23 utilizes the heat of high-temperature flue gas generated by an SCR system to evaporate the concentrated waste water, and the flue gas in the flue gas branch pipeline 71 is mixed with the high-temperature flue gas in the flue gas pipeline 7 at the flue gas merging port 72.
Fig. 2 is a schematic diagram showing a system structure of a second embodiment of the present invention, and fig. 2 is compared with fig. 1, and the same parts thereof are not described herein, except that a high-temperature condensed water outlet 331 of the low-temperature economizer 33 is connected to the return water port 13 through a condensed water pipe 4, a branch pipe is further provided on the condensed water pipe 4 between the low-temperature economizer 33 and the return water port 13, the branch pipe is connected to the return water inlet 42 after passing through the steam generator 21, and after heat exchange in the steam generator 21, the condensed water in the branch pipe is returned to the condensed water pipe 4 between the outlet water mixing port 43 and the low-temperature economizer 33 to be mixed with the condensed water in the condensed water pipe 4. Second embodiment compared to the first embodiment, the temperature of the condensate returning to the condensate regenerative system 1 is slightly higher than that of the first embodiment, but the control logic is slightly complicated
Fig. 3 is a schematic diagram of a system structure of a third embodiment of the present invention, which is different from the first embodiment in that the low-temperature economizer 33 is disposed at the inlet of the dust remover 32 on the flue gas duct 7. In the third embodiment, the temperature of the flue gas entering the dust remover 32 is reduced, which is beneficial to collecting the smoke dust, and simultaneously, the flue gas amount of the induced draft fan 36 is reduced, and the power consumption of the induced draft fan 36 is reduced. But can not utilize the residual heat of the flue gas generated by the temperature rise of the induced draft fan 36.
Fig. 4 is a schematic diagram of a system structure according to a fourth embodiment of the present invention, which is different from the first embodiment in that a second low-temperature economizer 34 is disposed on the condensed water pipe 4 between the low-temperature economizer 33 and the steam generator 21, the second low-temperature economizer 34 is also disposed on the flue gas pipe 7 between the low-temperature economizer 33 and the flue gas merging opening 72, and the condensed water pipe 4 exchanges heat with the flue gas pipe 7 in the second low-temperature economizer 34. In the third embodiment, the condensed water is subjected to two heating treatments and then enters the steam generator 21 to exchange heat with the circulating water, and in this embodiment, the temperature of the flue gas entering the dust remover 32 is reduced, which is beneficial to collecting the flue gas, meanwhile, the flue gas amount of the induced draft fan 36 is reduced, the power consumption of the induced draft fan 36 is reduced, the residual heat of the flue gas generated by the temperature rise of the induced draft fan 36 can be utilized, and the heat economy of the unit is further improved.
Fig. 5 is a schematic diagram of the system structure of the fifth embodiment of the present invention, which is different in that a dust remover 32 is disposed on the flue gas pipe 7 between the air preheater 31 and the flue gas merging port 72, and a second dust remover 35 is disposed on the flue gas branch pipe 71 between the desulfurization wastewater concentrate treatment system 23 and the flue gas merging port 72. In this embodiment, the salt-containing dust passing through the desulfurization wastewater concentrate treatment system 23 is separately collected by the second dust remover 35, and does not enter the dust remover 32, so that the comprehensive utilization of the fly ash collected by the dust remover 32 is not affected.
Fig. 6 is a schematic system structure diagram of a sixth embodiment of the present invention, which is different from the sixth embodiment in that the desulfurization waste water concentrate treatment system 23 is provided with a slag outlet 232, and the slag outlet 232 is connected with a slag bin through a pipeline. In this embodiment, the desulfurization waste water concentrate treatment system 23 can recover the filter cake by using the desulfurization system filter press, and the desulfurization waste water concentrate is discharged to the slag bin by using the high-temperature flue gas evaporation process.
Claims (7)
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Cited By (2)
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| CN114229935A (en) * | 2021-12-16 | 2022-03-25 | 河南科达东大国际工程有限公司 | Concentrated desulfurization waste water device of electrolytic aluminum flue gas waste heat |
| CN117073305A (en) * | 2023-07-12 | 2023-11-17 | 中国葛洲坝集团勘测设计有限公司 | A kind of concrete temperature control and water flow integrated machine and control method |
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