CN115124100A - High-efficient high salt waste water evaporative crystallization system - Google Patents
High-efficient high salt waste water evaporative crystallization system Download PDFInfo
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- CN115124100A CN115124100A CN202210741667.1A CN202210741667A CN115124100A CN 115124100 A CN115124100 A CN 115124100A CN 202210741667 A CN202210741667 A CN 202210741667A CN 115124100 A CN115124100 A CN 115124100A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 53
- 238000002425 crystallisation Methods 0.000 title claims abstract description 45
- 230000008025 crystallization Effects 0.000 title claims abstract description 45
- 150000003839 salts Chemical class 0.000 title description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 56
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 44
- 239000003546 flue gas Substances 0.000 claims abstract description 44
- 239000013078 crystal Substances 0.000 claims abstract description 36
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 29
- 230000023556 desulfurization Effects 0.000 claims abstract description 29
- 239000000428 dust Substances 0.000 claims abstract description 17
- 238000010438 heat treatment Methods 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 12
- 238000001704 evaporation Methods 0.000 claims description 47
- 230000008020 evaporation Effects 0.000 claims description 47
- 239000007788 liquid Substances 0.000 claims description 41
- 230000005611 electricity Effects 0.000 claims description 3
- 238000010531 catalytic reduction reaction Methods 0.000 abstract 1
- 239000002244 precipitate Substances 0.000 description 19
- 238000000034 method Methods 0.000 description 17
- 239000012141 concentrate Substances 0.000 description 11
- 239000007787 solid Substances 0.000 description 11
- 230000008569 process Effects 0.000 description 10
- 238000001556 precipitation Methods 0.000 description 8
- 230000009286 beneficial effect Effects 0.000 description 6
- 208000028659 discharge Diseases 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 230000009471 action Effects 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 239000007789 gas Substances 0.000 description 3
- 239000010440 gypsum Substances 0.000 description 3
- 229910052602 gypsum Inorganic materials 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 239000006228 supernatant Substances 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000009977 dual effect Effects 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000001737 promoting effect Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 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
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical class OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
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- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
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Classifications
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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
- C02F1/048—Purification of waste water by evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0011—Heating features
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0011—Heating features
- B01D1/0017—Use of electrical or wave energy
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/02—Crystallisation from solutions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D2009/0086—Processes or apparatus therefor
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
-
- 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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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to the field of treatment of desulfurization wastewater, and discloses a high-efficiency high-salinity wastewater evaporative crystallization system which comprises an SCR (selective catalytic reduction) module, an air preheater, a low-temperature economizer, a dust remover, an induced draft fan, a flue gas heat exchanger, a desulfurization island and a chimney, wherein the SCR module and the dust remover are sequentially connected, a high-temperature bypass evaporative crystallizer is arranged on a bypass between the SCR module and the dust remover, an evaporative concentration separation system is arranged on a bypass between the air preheater and the desulfurization island, the evaporative concentration separation system comprises a condenser, a vacuum pump, an evaporative concentration separator, a seed crystal circulating pump, a vacuum belt conveyor, a heater, a heating circulating pump and an atomizing water pump, and the evaporative concentration separator is used for evaporative concentration crystallization of heated wastewater.
Description
Technical Field
The invention relates to the field of desulfurization wastewater treatment, in particular to a high-efficiency high-salinity wastewater evaporative crystallization system.
Background
The desulfurization wastewater is mainly the discharge water of a desulfurization island in the wet desulfurization (limestone/gypsum method) process of boiler flue gas. In order to maintain the balance of the mass of the slurry circulation system of the desulfurization unit, prevent the soluble fraction of the flue gas, i.e., the chlorine concentration, from exceeding the specified value and ensure the quality of gypsum, a certain amount of waste water must be discharged from the system, which is mainly from the gypsum dewatering and cleaning system. The impurities contained in the wastewater mainly comprise suspended matters, supersaturated sulfite, sulfate and heavy metals, and many of the impurities are the first pollutants strictly controlled in the national environmental protection standard.
Since environmental protection laws of the people's republic of China and action plans for water pollution control (ten items of water) were issued in 2015, the overall requirements for wastewater treatment are improved, and treatment processes such as flue gas evaporation drying or evaporative crystallization are encouraged to be adopted in the feasible technical guidelines for pollution control of thermal power plants (HJ2301-2017), so that no desulfurization wastewater is discharged, and with the deep implementation of a pollution discharge approval system, the environmental evaluation of the project of not discharging the reclaimed wastewater faces the transformation condition, and zero discharge treatment becomes the current trend.
At present, the mainstream desulfurization wastewater zero-discharge process in the market is pretreatment, concentration and decrement and solidification drying, wherein the concentration and decrement technology mainly comprises a membrane method and a thermal method, the membrane method is harsh in cost and water inlet conditions, so the concentration technology which is applied and tried more at present is a concentration tower and a multi-effect flash evaporation technology, the multi-effect flash evaporation technology is often subjected to scaling blockage caused by overhigh local concentration multiple due to uneven vacuum degree control in the operation process, the maintenance frequency is high, the system stability is poor, and the problems of spray gun blockage caused by incoming water with high solid content and salt content at the front end and the like are often generated in a solidification and drying section.
Disclosure of Invention
Therefore, a high-efficiency high-salinity wastewater evaporative crystallization system is needed to be provided, and the problems of low treatment efficiency and poor system stability of the existing desulfurization wastewater zero-discharge system are solved.
In order to achieve the aim, the invention provides a high-efficiency high-salinity wastewater evaporative crystallization system which comprises an SCR module, an air preheater, a low-temperature economizer, a dust remover, an induced draft fan, a flue gas heat exchanger, a desulfurization island and a chimney which are sequentially connected, wherein a high-temperature bypass evaporative crystallizer is arranged on a bypass between the SCR module and the dust remover, an evaporative concentration separation system is arranged on a bypass between the air preheater and the desulfurization island,
the evaporative concentration separation system comprises a condenser, a vacuum pump, an evaporative concentration separator, a seed crystal circulating pump, a vacuum belt conveyor, a heater, a heating circulating pump and an atomizing water pump, wherein the heater is connected with a wastewater outlet of a desulfurization island, the evaporative concentration separator is used for heating evaporative concentration crystallization of wastewater, the side edge of the evaporative concentration separator is connected with the heater through the heating circulating pump, the side edge of the evaporative concentration separator is connected with a high-temperature bypass evaporative crystallizer through the atomizing water pump, the top of the evaporative concentration separator is connected with the condenser through the vacuum pump, a hot air outlet of the condenser is connected with an air preheater, the bottom edge of the evaporative concentration separator is connected with the seed crystal circulating pump, and the seed crystal circulating pump is connected with the vacuum belt conveyor.
Furthermore, an annular baffle plate is fixed on the inner side wall of the evaporation concentration separator, a liquid inlet groove with a closed bottom surface and an open top surface is formed between the baffle plate and the inner side wall of the evaporation concentration separator, a flow guide channel is formed in the middle of the annular baffle plate, the heater is communicated with the liquid inlet tank, the side surface of the evaporation concentration separator is provided with a circulating water outlet and a concentrated clear liquid outlet, the circulating water outlet and the concentrated clear liquid outlet are positioned below the baffle plate, the circulating water outlet is connected with the water inlet of the heater through a circulating pump, the concentrated clear liquid outlet is connected with the high-temperature bypass evaporative crystallizer through an atomizing water pump, the outlet of the seed crystal circulating pump is connected with a conveying pipe, the other end of the conveying pipe is connected with a vacuum belt conveyor, the other end of the conveying pipe is also connected with a return pipe in a branch way, the other end of the return pipe penetrates through the side wall of the evaporation concentration separator and extends into the flow guide channel.
Furthermore, a conical cover is fixed at the bottom of the flow guide channel, and the concentrated clear liquid outlet and the circulating water outlet are both positioned above the conical cover.
The export of water conservancy diversion passageway is enlarged to the toper cover, reduces the velocity of flow of concentrate after the crystallization, is favorable to the sediment of crystallization precipitate, and the toper cover can block the crystallization precipitate that the below billows simultaneously, effectively avoids on the crystallization precipitate moves concentrated clear liquid export and circulation delivery port, and the solid volume greatly reduced that contains of concentrated clear liquid export and circulation delivery port liquid can directly be carried extremely high temperature bypass evaporative crystallizer atomizing or heater need not to set up the concentrate baffle-box in addition, reduction equipment cost.
Further, the return pipe is positioned below the liquid level of the liquid inlet tank. The position that the back flow pipe refluxed sets up and spills over the liquid level below at the concentrate for can be mixed with the precipitate intensive of backward flow after the concentrate spills over, saturated salt material carries out the enrichment crystallization on the precipitate in the concentrate, prevents evaporation concentration separator wall and continuous pipeline inner wall from taking place scaling nature and blockking up.
Further, the bottom of the evaporation concentration separator is in a cone hopper shape. The bottom of the evaporation concentration separator is in a cone hopper shape, which is beneficial to crystallization and solid particle precipitation.
High temperature bypass evaporative crystallizer passes through atomizing water pump with the evaporative concentration separator and is connected the completion atomized water supply, quotes the high temperature flue gas that comes from the air heater front end and the atomized water that comes from the evaporative concentration separator and carries out the evaporative crystallization of heat exchange completion waste water, and produced crystallisate and vapor are carried along with the flue gas extremely the dust remover front end, atomizing water pump access connection evaporative concentration separator awl fill top position, under the dual function of water conservancy diversion passageway and seed crystal, the bottom that most crystallisate and solid particle deposit, the concentrated solution of evaporative crystallization atomized water interface horizontal position contains solid greatly reduced, can directly carry extremely high temperature bypass evaporative crystallizer atomizes, need not to set up the concentrated solution baffle-box in addition, reduce cost.
The evaporation concentration separator and the air preheater are sequentially connected through the vacuum pump and the condenser and are used for recovering mechanical energy and heat energy of steam generated in the evaporation concentration separator and controlling negative pressure conditions, evaporation crystallization of waste water in the evaporation concentration separator is facilitated, and meanwhile heating cost of pretreatment of the high-temperature flue gas treatment system is reduced.
Further, the number of the heaters is at least two, and at least two heaters are arranged in parallel.
A plurality of heaters are parallelly connected and are mutually standby, the valves can be switched in the operation process, one heater operates on line, the other heater quits the system to independently clean and overhaul, the normal operation of the system is not influenced, and the overall stability of the system is improved. When a plurality of heaters are used simultaneously, the treatment capacity of the desulfurized high-salinity wastewater can be increased.
Further, the heat source of the heater is one of the following heat sources: hot water or steam directly or indirectly generated from a flue gas heat exchanger, low-temperature economizers or other hot water from a power plant, steam generated from a power plant boiler, direct heating by electricity.
The heater has multiple heat source choices, and when the heater used the hot water or the steam that the gas heater produced as the heat source, realized the recycle to heat in the high temperature flue gas processing system, can effectively reduce the energy cost of whole device, reached the purpose that reduces the pollution simultaneously.
The technical scheme has the following beneficial effects:
the invention provides a high-efficiency high-salinity wastewater evaporative crystallization system which can fully utilize the waste heat of flue gas of a power plant and can realize zero-emission treatment of desulfurization wastewater. And concentrating and reducing the desulfurization wastewater through an evaporation concentration separator. The reduced wastewater can be atomized and dried by a high-temperature bypass evaporation crystallizer.
In the evaporation concentration separation system, a heater heats high-salinity wastewater, the desulfurization wastewater is heated by the heater and then is guided into a liquid inlet tank for evaporation concentration, the concentrated solution after evaporation concentration overflows from the top of the liquid inlet tank and flows into a flow guide channel, the concentrated wastewater is mixed with refluxing crystals in the flow guide channel, supersaturated wastewater solution generates crystal precipitation, the refluxing crystals play a role of seed crystals to facilitate the precipitation of the crystals, the crystals flow out of the flow guide channel along with the wastewater after precipitation, the flow area is increased, the flow rate is reduced, solid-liquid separation occurs, solid precipitates are deposited on a bottom layer, the upper concentrated solution is positioned on the upper layer of the precipitates, the concentrated solution containing a large amount of precipitates partially flows back into an evaporation concentration separator through a seed crystal circulating pump, and part of the concentrated solution is conveyed to a vacuum belt conveyor for disposal, the device is integrally designed for concentration and precipitation, and a precipitation pool is not additionally arranged, the process flow is simplified, the cost is saved, and the high-efficiency treatment of the desulfurization high-salinity wastewater is completed.
Drawings
FIG. 1 is a block diagram of a system according to an embodiment.
FIG. 2 is a block diagram of an evaporative concentration separator according to an embodiment.
Description of reference numerals:
11. an SCR module; 12. an air preheater; 13. a low-temperature economizer; 14. a dust remover; 15. an induced draft fan; 16. a flue gas heat exchanger; 17. a desulfurization island; 18. a chimney;
21. a high temperature bypass evaporative crystallizer; 22. an atomizing water pump; 23. a high-temperature flue gas inlet pipe; 24. atomizing a water inlet pipe; 25. a steam outlet pipe;
31. an evaporation concentration separator; 311. a concentrated clear liquid outlet; 312. a steam outlet; 32. a circulation pump; 321. a circulating water outlet; 33. a heater; 34. a seed crystal circulating pump; 341. a return pipe; 35. a baffle plate; 351. a liquid inlet tank; 352. a flow guide channel; 36. a conical cover; 37. a condenser; 38. and a vacuum pump.
Detailed Description
To explain technical contents, structural features, and objects and effects of the technical solutions in detail, the following detailed description is given with reference to the accompanying drawings in conjunction with the embodiments.
Referring to fig. 1-2, the present embodiment provides a high-efficiency high-salinity wastewater evaporative crystallization system, which includes an SCR module 11, an air preheater 12, a low-temperature economizer 13, a dust remover 14, an induced draft fan 15, a flue gas heat exchanger 16, a desulfurization island 17, and a chimney 18, which are sequentially connected by a pipeline.
A high-temperature bypass evaporative crystallizer 21 is arranged in a bypass between the SCR module 11 and the dust remover 14, and an evaporative concentration separation system is arranged in a bypass between the air preheater 12 and the desulfurization island 17.
The evaporation concentration separation system comprises an evaporation concentration separator 31, a circulating pump 32, a heater 33, a seed crystal circulating pump 34, a condenser 37 and a vacuum pump 38, wherein the condenser 37 is provided with a steam inlet, a cooling water outlet, a cold air inlet and a hot air outlet, the top of the evaporation concentration separator 31 is provided with a steam outlet 312, the steam inlet of the condenser 37 is connected with the steam outlet 312 through the vacuum pump 38, and the hot air outlet is connected with the air preheater 12. The evaporation concentration separator 31 and the air preheater 12 are sequentially connected through a vacuum pump 38 and a condenser 37 and used for recovering mechanical energy and heat energy of steam generated in the evaporation concentration separator 31 and controlling negative pressure conditions, thereby being beneficial to evaporation crystallization of waste water in the evaporation concentration separator 31 and simultaneously reducing the heating cost of pretreatment of a high-temperature flue gas treatment system.
An annular baffle plate 35 is fixed on the inner side wall of the evaporation concentration separator 31, a bottom surface is formed between the baffle plate 35 and the inner side wall of the evaporation concentration separator 31 to be closed, an open top surface liquid inlet tank 351, a flow guide channel 352 is formed in the middle of the annular baffle plate 35, a water inlet of a heater 33 is connected with a wastewater outlet of the desulfurization island 17, a water outlet of the heater 33 is communicated with the liquid inlet tank 351, a circulating water outlet 321 is formed in the side surface of the evaporation concentration separator 31, the circulating water outlet 321 is positioned below the baffle plate 35, the circulating water outlet 321 is connected with a water inlet of the heater 33 through a circulating pump 32, the bottom of the evaporation concentration separator 31 is connected with an inlet of a seed crystal circulating pump 34, an outlet of the seed crystal circulating pump 34 is connected with a conveying pipe, the other end of the conveying pipe is connected with a vacuum belt conveyor and a return pipe 341, and the other end of the return pipe 341 penetrates through the side wall of the evaporation concentration separator 31 and extends into the flow guide channel 352.
The return pipe 341 is located below the liquid level of the liquid inlet tank 351. The position that back flow pipe 341 flows back sets up in the concentrate spills over the liquid level below for can be mixed with the precipitate intensive mixing of backward flow after the concentrate spills over, and saturated salt matter carries out the enrichment crystallization on the precipitate in the concentrate, prevents that evaporation concentration separator 31 wall and continuous pipeline inner wall from taking place scaling nature and blockking up.
The bottom of the evaporation concentration separator 31 is cone-shaped. The bottom of the evaporation concentration separator 31 is in a cone hopper shape, which is beneficial to crystallization and solid particle precipitation. In this embodiment, the evaporation concentration separator 31 includes a straight cylinder section and a conical hopper section, and the conical hopper section is fixed below the straight cylinder section.
The side of evaporation concentration separator 31 is equipped with concentrated clear liquid export 311, and concentrated clear liquid export 311 is located feed liquor groove 351 below, is connected with high temperature flue gas intake pipe 23 on the high temperature bypass evaporation crystallizer 21, atomizing inlet tube 24 and crystal and steam outlet duct 25, and the gas outlet of SCR module 11 is connected to high temperature flue gas intake pipe 23, and atomizing inlet tube 24 passes through atomizing water pump 22 and connects concentrated clear liquid export 311, and crystal and steam outlet duct 25 connect the import of dust remover 14.
High temperature bypass evaporative crystallizer 21 is connected through atomizing water pump 22 with evaporative concentration separator 31 and is accomplished the atomized water supply, quote the high temperature flue gas that comes from air heater 12 front end and the atomized water that comes from evaporative concentration separator 31 and carry out the evaporation crystallization of heat exchange completion waste water, produced crystallization and vapor are carried to the dust remover 14 front end along with the flue gas, the evaporation water pump access connection evaporative concentration separator 31 awl fill top position, under the dual function of water conservancy diversion passageway 352 and seed crystal, the bottom that most crystallization and solid particle deposit, the concentrated solution of evaporative crystallization atomized water interface horizontal position contains solid greatly reduced, can directly carry to high temperature bypass evaporative crystallizer 21 atomizing, need not to set up the concentrated solution baffle-box in addition, reduce cost.
In this embodiment, the conical cover 36 is fixed to the bottom of the diversion channel 352, and the concentrated clear liquid outlet 311 and the circulation water outlet 321 are both located above the conical cover 36.
The export of diversion passageway 352 is enlargied to conical cover 36, reduce the velocity of flow of concentrate after the crystallization, be favorable to the sediment of crystallization precipitate, conical cover 36 can block the crystallization precipitate that the below turned over and gushes simultaneously, effectively avoid the crystallization precipitate to move on concentrated clear liquid export 311 and circulation delivery port 321, the solid matter volume greatly reduced that contains of concentrated clear liquid export 311 and circulation delivery port 321 liquid, can directly carry to high temperature bypass evaporation crystallizer 21 atomizing or heater 33, need not to set up the concentrate baffle-box in addition, reduce equipment cost.
In this embodiment, the evaporation concentration separation system includes two heaters 33 connected in parallel, the two heaters 33 are connected in parallel and are mutually standby, during operation, the two heaters 33 can be switched through a valve, one heater operates on line, the other heater exits from the system to perform cleaning and maintenance operation independently, normal operation of the system is not affected, and overall stability of the system is improved. When the plurality of heaters 33 are simultaneously used, the treatment amount of the desulfurized high-salinity wastewater can be increased.
The heat source of the heater 33 is one of the following heat sources: hot water or steam directly or indirectly generated from the flue gas heat exchanger 16, low-temperature coal economizer 13 or other hot water from the power plant, steam generated from the boiler of the power plant, and direct heating by electricity. The heater 33 has various heat source choices, and when the heater 33 uses hot water or steam generated by the flue gas heat exchanger 16 as a heat source, the heat in the high-temperature flue gas treatment system is recycled, so that the energy cost of the whole device can be effectively reduced, and the purpose of reducing pollution is achieved.
Specifically, in the invention, the heat source of the heater 33 is the waste heat generated by the flue gas heat exchanger 16 of the high-temperature flue gas treatment system, so that the heat of the high-temperature flue gas treatment system is recycled, the energy consumption of the whole system is reduced, and the economic benefit is improved.
The invention comprises the following steps:
high-temperature flue gas generated by a boiler sequentially passes through an SCR module 11, an air preheater 12, a low-temperature economizer 13, a dust remover 14, an induced draft fan 15, a flue gas heat exchanger 16, a desulfurization island 17 and a chimney 18, the temperature, the humidity, the particle content, the sulfur content and the nitrogen content of the high-temperature flue gas obtained after treatment all reach the environmental protection emission standard, the SCR module 11 is used for applying a denitration process to the high-temperature flue gas, and the dust remover 14 removes the particle content in the flue gas.
The flue gas is behind high temperature flue gas processing system's SCR module 11, part high temperature flue gas passes through high temperature flue gas intake pipe 23 and enters into high temperature bypass evaporative crystallizer 21 in, atomizing water pump 22 carries the high-temperature bypass evaporative crystallizer 21 in through atomizing inlet tube 24 after with the upper clear concentrate atomizing of evaporative concentration separator 31 internal concentration crystallization, high temperature flue gas heats concentrated wet steam, partial salinity is separated out the crystallization, crystal and vapor pass through crystal and vapor outlet duct 25 and carry to dust remover 14, the granule in the flue gas is got rid of to dust remover 14.
High-temperature flue gas is conveyed into a flue gas heat exchanger 16 through an induced draft fan 15, the high-temperature flue gas is cooled, a heat medium generated by the flue gas heat exchanger 16 is connected into a heater 33, the heater 33 is heated, the flue gas is desulfurized through a desulfurization island 17 to generate high-salt wastewater, the high-salt wastewater is heated through the heater 33 and conveyed into a liquid inlet tank 351 through a pipeline to be evaporated and concentrated in the liquid inlet tank 351 to form supersaturated solution, an evaporation concentration separator 31 provides low-pressure conditions through a vacuum pump 38 to be beneficial to evaporation and concentration of the wastewater, meanwhile, evaporated gas is conveyed into a condenser 37 through the vacuum pump 38 to heat cold air of the condenser 37, hot air generated by the condenser 37 is used as a heat source of an air preheater 12, so that heat energy is fully utilized, the supersaturated solution flows into a flow guide channel 352 after overflowing from the liquid inlet tank 351, the supersaturated solution is mixed with crystals output by a flow guide channel 352, the backflow crystals play a role of crystal seeds and are beneficial to promoting the precipitation of the crystals, the crystals flow out of the diversion channel 352 along with the wastewater after being precipitated, the flow area is increased, the flow rate is reduced, solid-liquid separation occurs, solid precipitates are deposited on the bottom layer, at the moment, even if part of the crystal precipitates are upwards rolled by impact, the conical cover 36 can block the crystals, the crystal precipitates are deposited on the lower layer below the baffle plate 35, the upper layer is supernatant concentrated solution, the temperature of the supernatant concentrated solution is controlled to be 60-100 ℃, the supernatant concentrated solution can be conveyed to the heater 33 through the circulating water outlet 321 by the circulating pump 32 for cyclic heating concentration, after certain time of treatment, high-salt part precipitates in the wastewater are discharged, the formed concentrated clear solution is conveyed to the high-temperature bypass evaporative crystallizer 21 through the atomizing water pump 22 for heating crystallization, the crystal precipitates deposited on the lower layer are directly output through the conveying part of the seed crystal circulating pump 34, and partially through the reflux pipe 341 to seed the crystallization of the supersaturated solution, thereby promoting the crystallization efficiency. In this embodiment, the seed circulation pump 34 conveys the crystallized precipitate to a vacuum belt conveyor through a pipeline, and the position of the vacuum belt conveyor is not shown in the figure.
In the high-efficiency high-salinity wastewater evaporative crystallization system provided by the invention, the waste heat of the flue gas of a power plant can be fully utilized, and zero discharge treatment of desulfurization wastewater can be realized. The desulfurization waste water is concentrated and reduced by an evaporation concentration separator 31. Further, the reduced wastewater may be subjected to an atomization drying process through the high-temperature bypass evaporator-crystallizer 21.
It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or terminal that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or terminal. Without further limitation, an element defined by the phrases "comprising … …" or "comprising … …" does not exclude the presence of additional elements in a process, method, article, or terminal that comprises the element. Further, herein, "greater than," "less than," "more than," and the like are understood to exclude the present numbers; the terms "above", "below", "within" and the like are to be understood as including the number.
Although the embodiments have been described, other variations and modifications of the embodiments may occur to those skilled in the art once they learn of the basic inventive concepts, so that the above description is only for the embodiments of the present invention, and is not intended to limit the scope of the invention, which is intended to be covered by the present invention.
Claims (7)
1. A high-efficiency high-salinity wastewater evaporative crystallization system is characterized by comprising an SCR module, an air preheater, a low-temperature economizer, a dust remover, an induced draft fan, a flue gas heat exchanger, a desulfurization island and a chimney which are sequentially connected, wherein a high-temperature bypass evaporative crystallizer is arranged on a bypass between the SCR module and the dust remover, an evaporative concentration separation system is arranged on a bypass between the air preheater and the desulfurization island,
the evaporative concentration separation system comprises a condenser, a vacuum pump, an evaporative concentration separator, a seed crystal circulating pump, a vacuum belt conveyor, a heater, a heating circulating pump and an atomizing water pump, wherein the heater is connected with a wastewater outlet of a desulfurization island, the evaporative concentration separator is used for heating evaporative concentration crystallization of wastewater, the side edge of the evaporative concentration separator is connected with the heater through the heating circulating pump, the side edge of the evaporative concentration separator is connected with a high-temperature bypass evaporative crystallizer through the atomizing water pump, the top of the evaporative concentration separator is connected with the condenser through the vacuum pump, a hot air outlet of the condenser is connected with an air preheater, the bottom edge of the evaporative concentration separator is connected with the seed crystal circulating pump, and the seed crystal circulating pump is connected with the vacuum belt conveyor.
2. The high-efficiency high-salinity wastewater evaporative crystallization system according to claim 1, wherein an annular baffle plate is fixed on the inner side wall of the evaporative concentration separator, a liquid inlet tank with a closed bottom surface and an open top surface is formed between the baffle plate and the inner side wall of the evaporative concentration separator, a flow guide channel is formed in the middle of the annular baffle plate, the heater is communicated with the liquid inlet tank, a circulation water outlet and a concentrated clear liquid outlet are formed in the side surface of the evaporative concentration separator, the circulation water outlet and the concentrated clear liquid outlet are positioned below the baffle plate, the circulation water outlet is connected with the water inlet of the heater through a circulation pump, the concentrated clear liquid outlet is connected with the high-temperature bypass evaporative crystallizer through an atomizing water pump, the outlet of the seed crystal circulation pump is connected with a delivery pipe, the other end of the delivery pipe is connected with a vacuum belt conveyor, and the other end of the delivery pipe is further connected with a return pipe by a branch, the other end of the return pipe penetrates through the side wall of the evaporation concentration separator and extends into the flow guide channel.
3. The efficient high-salinity wastewater evaporative crystallization system of claim 2, wherein a conical cover is fixed at the bottom of the diversion channel, and the concentrated clear liquid outlet and the circulating water outlet are both positioned above the conical cover.
4. The high-efficiency high-salinity wastewater evaporative crystallization system according to claim 2, wherein the return pipe is positioned below the liquid level of the liquid inlet tank.
5. The high-efficiency high-salinity wastewater evaporative crystallization system according to claim 2, wherein the bottom of the evaporative concentration separator is cone-hopper shaped.
6. The high-efficiency high-salinity wastewater evaporative crystallization system according to claim 1, wherein the number of the heaters is at least two, and at least two heaters are arranged in parallel.
7. The high-efficiency high-salinity wastewater evaporative crystallization system according to claim 1, wherein the heat source of the heater is one of the following heat sources: hot water or steam directly or indirectly generated from a flue gas heat exchanger, low-temperature economizers or other hot water from a power plant, steam generated from a power plant boiler, direct heating by electricity.
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