CN110183024A - A kind of device using low-grade flue gas concentration waste water - Google Patents
A kind of device using low-grade flue gas concentration waste water Download PDFInfo
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- CN110183024A CN110183024A CN201910548941.1A CN201910548941A CN110183024A CN 110183024 A CN110183024 A CN 110183024A CN 201910548941 A CN201910548941 A CN 201910548941A CN 110183024 A CN110183024 A CN 110183024A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 131
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 85
- 239000003546 flue gas Substances 0.000 title claims abstract description 85
- 238000001704 evaporation Methods 0.000 claims abstract description 66
- 230000008020 evaporation Effects 0.000 claims abstract description 58
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 56
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 56
- 230000023556 desulfurization Effects 0.000 claims abstract description 54
- 239000000428 dust Substances 0.000 claims abstract description 35
- 238000001035 drying Methods 0.000 claims abstract description 33
- 238000004062 sedimentation Methods 0.000 claims description 40
- 239000007921 spray Substances 0.000 claims description 30
- 239000007789 gas Substances 0.000 claims description 22
- 238000009833 condensation Methods 0.000 claims description 21
- 230000005494 condensation Effects 0.000 claims description 21
- 238000011144 upstream manufacturing Methods 0.000 claims description 19
- 239000012716 precipitator Substances 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 11
- 230000003009 desulfurizing effect Effects 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 10
- 239000006228 supernatant Substances 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 8
- 230000008859 change Effects 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 6
- 238000000034 method Methods 0.000 abstract description 16
- 239000003517 fume Substances 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 230000008569 process Effects 0.000 abstract description 7
- 239000002918 waste heat Substances 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 5
- 238000004064 recycling Methods 0.000 abstract description 4
- 239000000779 smoke Substances 0.000 abstract description 3
- 238000011084 recovery Methods 0.000 description 6
- 238000000889 atomisation Methods 0.000 description 5
- 238000002425 crystallisation Methods 0.000 description 5
- 230000008025 crystallization Effects 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- 238000001694 spray drying Methods 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000003020 moisturizing effect Effects 0.000 description 4
- 230000002411 adverse Effects 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 238000003303 reheating Methods 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000002633 protecting effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000004069 wastewater sedimentation Methods 0.000 description 1
Classifications
-
- 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
- C02F1/06—Flash 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
- C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
- C02F1/12—Spray 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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- 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
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
- C02F2201/007—Modular design
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Treating Waste Gases (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a kind of devices using low-grade flue gas concentration waste water.The device is made of for solving the problems, such as the recycling of power-plant flue gas waste heat and Waste water concentrating dust removing units, desulfurization unit, economizer and Waste water concentrating system etc..The device carries out Waste water concentrating using coal-burning power plant or other industry fume afterheat, and concentration process influences very little to smoke moisture, waste water is become available water, finally by institute's recovered flue gas heat transfer to low adding system, realizes that thermal energy step utilizes.High-concentration waste water after concentration decrement can be sent to evaporation drying system, substantially reduce evaporation drying system institute calorific requirement, reduce the influence to unit, and whole system has the advantages that low energy consumption, small investment, operating cost are low etc..
Description
Technical field
The invention belongs to environmental technology fields, and in particular to a kind of device using low-grade flue gas concentration waste water, especially
It is related to a kind of for flue gas waste heat recovery association in thermal power plant flue gas waste heat recovery coordinated desulfurization wastewater treatment or other field
With the device of wastewater treatment.
Background technique
Wet desulphurization wastewater treatment mainly uses three header pretreatments+clarifying basin+dewaterer technology at present, can remove
Part heavy metal reduces part SS, turbidity, but cannot remove removing chloride, and treated, and waste water gets nowhere.Currently study
Technology has depth pretreatment+concentration decrement+evaporation drying.
Wherein, depth pretreatment includes dosing, clarification and filtering；Concentration decrement can using thermal method (MED, MVR, NED) and
Embrane method (UF/RO)；Evaporation drying is to be dried using steam or fume afterheat.Recyclable salt is generated using steam raising, it is real
Water reuse in existing waste water, the disadvantage is that the salt of recycling is low-grade salt, reuse is difficult, while evaporation process need to use higher quality
Steam, energy consumption is high, investment is big, and service requirement is high.Using fume afterheat evaporation measure have invest it is lower, operating cost compared with
It is low, while downstream efficiency of dust collection is improved, disadvantage is consumption high-quality fume afterheat, influences air preheater flue-gas temperature, causes
Unit efficiency reduces, while will increase cleaner load, if not carrying out concentration decrement, large quantity of moisture can be made to enter desulfurization system
System causes desulfurizing tower evaporation capacity to reduce, and influences desulfurization washing water quantity, and processing wastewater flow rate can also be limited by flue-gas temperature and load.
Therefore at present there is consumption high-quality heat energy in desulfurization wastewater concentration technique, and energy consumption is high, cost of investment is big, operation is wanted
Ask high, the problems such as adversely affecting to unit efficiency.
Summary of the invention
Therefore, the technical problem to be solved by the present invention is to existing desulfurization wastewater concentration techniques there is consumption high-quality heat energy,
And energy consumption is high, cost of investment is big, service requirement is high, the defects of adversely affecting to unit efficiency, to propose a kind of utilization
The device of low-grade flue gas concentration waste water.
For this purpose, technical solution provided by the present invention is as follows:
Device provided by the present invention using low-grade flue gas concentration waste water, including being connected to the dust removing units of setting and taking off
Sulphur unit further includes economizer, is set between the dust removing units and desulfurization unit or along flue gas circulating direction, setting
It further include Waste water concentrating system in the dust removing units upstream, the Waste water concentrating system includes,
First Heat Exchanger is connected to the economizer, by desulfurization wastewater and the first heat exchange in the economizer
Medium exchanges heat in the First Heat Exchanger；
Flash tank including shell and is set to the concentration wastewater outlet of the lower part of the housing, the shell and described first
Heat exchanger connection, is sent into the flash tank with the desulfurization wastewater after will heat up and is flashed；
Second heat exchanger is connected to the concentration wastewater outlet, and waste water will be concentrated in second heat exchanger with
The heat exchange of two heat transferring mediums；
Sedimentation device is connected to second heat exchanger, concentration waste water after cooling down be sent into the sedimentation device into
Row sedimentation.
Further, the sedimentation device includes at least two-stage sedimentation unit, so that the concentration waste water progress after cooling is more
Grade precipitating；
The top of the sedimentation device is connected to the First Heat Exchanger so that the supernatant in the sedimentation device and/
Or additional desulfurization wastewater enters in the First Heat Exchanger, and with the first heat transferring medium in the economizer described the
Heat exchange in one heat exchanger.
Further, further include evaporation drying unit, be connected to the lower part of the sedimentation device, by the sedimentation device
The dense desulfurization wastewater of lower part is sent into the evaporation drying unit；
Air preheater is set on the upstream flue of the dust removing units.
Further, the evaporation drying unit is flue spray evaporator, along the circulating direction of flue gas, the flue
Spray evaporator is set in the upstream flue of the dust removing units.
Further, the evaporation drying unit is rotary spray evaporation device, and the import of high temperature dry flue gas, edge is arranged in upper part
On the circulating direction of flue gas, the high temperature dry flue gas import is connected to the upstream flue of the air preheater, so that the air preheater
Upstream flue in high temperature dry flue gas enter the rotary spray evaporation device in dense desulfurization wastewater exchange heat；
The lower part of the rotary spray evaporation device is provided with the outlet of high temperature wet flue gas, high temperature wet flue gas outlet with it is described
The connectivity points of flue connection between air preheater and dust removing units, the sedimentation device and the rotary spray evaporation device are located at institute
State the top of rotary spray evaporation device.
It further, further include third heat exchanger, the secondary steam outlet with the upper part of the housing, the third is changed
Hot device is also connected to second heat exchanger, so that the second heat transferring medium after the heating in second heat exchanger enters
The third heat exchanger, and exchange heat again with the secondary steam from the flash tank.
Further, further include air preheater, be set on the upstream flue, the nozzle be set to the air preheater with
In upstream flue between the dust removing units, alternatively, high temperature dry flue gas outlet and the gas approach of the air preheater connect
It is logical.
Further, further include the first pump, be connected to the flash tank, for making in the flash tank in negative pressure state
And control its interior vacuum degree；
Second pump, is set on the pipeline between the sedimentation device and the First Heat Exchanger, by supernatant and/or
Additional desulfurization wastewater is sent into the First Heat Exchanger；
Third pump, is set on the pipeline between the sedimentation device and the evaporation drying unit.
4th pump, is set on the pipeline between the flash tank and the second heat exchanger；
5th pump, is set to the water return pipeline of low pressure condensation water or comes on waterpipe.
It further, further include chimney, the chimney is connected to the desulfurization unit；
The dust removing units are electric precipitator；The economizer is low low-level (stack-gas) economizer；The desulfurization unit is desulfurizing tower.
Further, first heat transferring medium is heat medium water；Second heat transferring medium is low pressure condensation water.
Technical solution of the present invention has the advantages that by the way that the dust removing units, economizer and the desulfurization list that are sequentially communicated is arranged
Member further includes Waste water concentrating system, and Waste water concentrating system includes First Heat Exchanger, is connected to economizer, by desulfurization wastewater with
The first heat transferring medium in economizer exchanges heat in First Heat Exchanger；Flash tank, including shell and it is set to lower part of the housing
Concentration wastewater outlet, shell is connected to First Heat Exchanger, is sent into flash tank and is flashed with the desulfurization wastewater after will heat up；
Second heat exchanger is connected to concentration wastewater outlet, and waste water will be concentrated and exchange heat in the second heat exchanger with the second heat transferring medium；It is heavy
Falling unit is connected to the second heat exchanger, and the concentration waste water after cooling is sent into sedimentation device and is settled.The device utilizes combustion
Coal-fired plant or other industry fume afterheat carry out Waste water concentrating, and concentration process not will cause significant change to smoke moisture, will give up
Water becomes available water, finally by institute's recovered flue gas heat transfer to low plus condensed water low adding system, realizes thermal energy step benefit
With.When high-concentration desulfurized waste water after concentration decrement carries out subsequent evaporation drying again, heat needed for substantially reducing evaporation drying system
Amount, reduces influence to unit, and whole system has the advantages that low energy consumption, small investment, operating cost are low etc..
Detailed description of the invention
It, below will be to specific in order to illustrate more clearly of the specific embodiment of the invention or technical solution in the prior art
Embodiment or attached drawing needed to be used in the description of the prior art be briefly described, it should be apparent that, it is described below
Attached drawing is some embodiments of the present invention, for those of ordinary skill in the art, before not making the creative labor
It puts, is also possible to obtain other drawings based on these drawings.
Fig. 1 is a kind of structural schematic diagram of the device in the embodiment of the present invention using low-grade flue gas concentration waste water；
Fig. 2 is another structural schematic diagram of the device in the embodiment of the present invention using low-grade flue gas concentration waste water；
Fig. 3 is the structural schematic diagram of Waste water concentrating system in the embodiment of the present invention；
Wherein appended drawing reference indicates are as follows:
0- air preheater；1- dust removing units；2- desulfurization unit；3- chimney；4- economizer；5- First Heat Exchanger；6- flash tank；
7- third heat exchanger；8- sedimentation device；The second heat exchanger of 9-；10- nozzle；11- first is pumped；12- second is pumped；13- third pump；
14- rotary spray evaporation device；15- the 4th is pumped；16- the 5th is pumped.
Specific embodiment
Technical solution of the present invention is clearly and completely described below, it is clear that described embodiment is the present invention
A part of the embodiment, instead of all the embodiments.Based on the embodiments of the present invention, those of ordinary skill in the art are not having
Every other embodiment obtained under the premise of creative work is made, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that term " center ", "upper", "lower", "left", "right", "vertical",
The orientation or positional relationship of the instructions such as "horizontal", "inner", "outside" be based on the orientation or positional relationship shown in the drawings, merely to
Convenient for description the present invention and simplify description, rather than the device or element of indication or suggestion meaning must have a particular orientation,
It is constructed and operated in a specific orientation, therefore is not considered as limiting the invention.In addition, term " first ", " second ",
" third " is used for descriptive purposes only and cannot be understood as indicating or suggesting relative importance.
In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, term " installation ", " phase
Even ", " connection " shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or be integrally connected；It can
To be mechanical connection, it is also possible to be electrically connected；It can be directly connected, can also can be indirectly connected through an intermediary
Connection inside two elements.For the ordinary skill in the art, above-mentioned term can be understood at this with concrete condition
Concrete meaning in invention.
As long as in addition, the non-structure each other of technical characteristic involved in invention described below different embodiments
It can be combined with each other at conflict.
Embodiment 1
A kind of device using low-grade flue gas concentration waste water is present embodiments provided, as shown in figs. 1 and 3, including connection
The dust removing units 1 and desulfurization unit 2 of setting, further include economizer 4, be set between dust removing units 1 and desulfurization unit 2 or
Along flue gas circulating direction, it is set to 1 upstream of dust removing units, in the present embodiment, dust removing units 1 are electric precipitator, and economizer 4 is
Low low-level (stack-gas) economizer, desulfurization unit 2 are desulfurizing tower, further include Waste water concentrating system, and Waste water concentrating system includes,
First Heat Exchanger 5 is connected to economizer 4, and desulfurization wastewater and the first heat transferring medium in economizer are existed
Heat exchange in First Heat Exchanger 5, specifically, the first heat transferring medium are the intermediate heat medium water obtained after high-temperature flue gas exchanges heat；
Flash tank 6 including shell and is set to the concentration wastewater outlet of lower part of the housing, and shell is connected to First Heat Exchanger 5,
It is sent into flash tank 6 and is flashed with the desulfurization wastewater after will heat up；
Second heat exchanger 9 is connected to concentration wastewater outlet, and waste water will be concentrated and exchange heat in the second heat exchanger 9 with second
Media for heat exchange, specifically, the second heat transferring medium are from extraneous low pressure condensation water；
Sedimentation device 8 is connected to the second heat exchanger 9, and the concentration waste water after cooling is sent into sedimentation device 8 and is sunk
Drop；Specifically, sedimentation device 8 includes at least two-stage sedimentation unit, so that the concentration waste water after cooling carries out multi stage precipitation；Sedimentation
The top of device 8 is connected to First Heat Exchanger 5, so that the supernatant and/or additional desulfurization wastewater in sedimentation device 8 enter first
In heat exchanger 5, and exchange heat in First Heat Exchanger 5 with the first heat transferring medium in economizer 4；More specifically, such as Fig. 3 institute
Show, sedimentation device 8 is the three-level sedimentation unit being sequentially communicated.Using multi stage precipitation form, after guaranteeing need to only be concentrated on a small quantity
Density wastewater be sent to evaporation drying system, to reduce influence to unit whole efficiency.
In above-mentioned apparatus, Waste water concentrating is carried out using coal-burning power plant or other industry fume afterheat, concentration process will not increase
Add smoke moisture, waste water is become into available water, finally by the low adding system of institute's recovered flue gas heat transfer to low plus condensed water,
Realize that thermal energy step utilizes.When high-concentration desulfurized waste water after concentration decrement carries out subsequent evaporation drying again, evaporation is substantially reduced
Drying system institute calorific requirement, reduces influence to unit, and whole system has the advantages that low energy consumption, small investment, operating cost are low etc..
As shown in Figure 1, further include third heat exchanger 7, the secondary steam outlet with upper part of the housing, third heat exchanger 7
It is also connected to the second heat exchanger 9, so that the second heat transferring medium after the heating in the second heat exchanger enters third heat exchanger
7, and exchange heat again with the secondary steam from flash tank 6, secondary steam becomes secondary steam condensate, and low pressure condensation water water becomes
At low pressure condensation water return water.
Further, further include evaporation drying unit, be connected to the lower part of sedimentation device 8, by 8 lower part of sedimentation device
Dense desulfurization wastewater is sent into evaporation drying unit；Specifically, evaporation drying unit is that flue spray evaporator (may be, for example, nozzle
10), along the circulating direction of flue gas, nozzle 10 is set in the upstream flue of dust removing units 1.
Further, further include air preheater 0, be set on the upstream flue of dust removing units 1, nozzle 10 is set to air preheater
In upstream flue between 0 and dust removing units 1；Chimney 3, chimney 3 are connected to desulfurization unit 2.
In order to control the chlorine ion concentration in effluent settling chamber, part density wastewater is sent to evaporation drying unit, and evaporation is dry
Flue sprayer (may be, for example, nozzle 10) can be used in dry unit, and flue sprayer is typically located at air preheater 0 and electric precipitator
Between flue inside, the concentrated water after atomization is evaporated to water vapour using the high-temperature residual heat flue gas in flue, steam is with dedusting
Flue gas afterwards enters desulfurizing tower, and evaporative crystallization object enters electric precipitator with grey outlet with dust.
The device is made of low low-level (stack-gas) economizer, the Waste water concentrating system of low temperature phase change and evaporation drying unit.Low-temperature phase
The Waste water concentrating system of change is mainly by First Heat Exchanger 5 (waste water heater), flash tank 6 (waste water flash tank), the second heat exchanger 9
(gaseous effluent cooler), third heat exchanger 7 (condenser), sedimentation device 8 (effluent settling chamber), vacuum pump (the first pump 11) and correlation
The equipment such as waste water delivery pump composition, evaporation drying unit are flue sprayer (may be, for example, nozzle 10) composition.Former flue gas system
If having installed low low-level (stack-gas) economizer, flue gas system does not need to be transformed, only need to be by the heating agent waterpipe of low low-level (stack-gas) economizer
It is transformed, the pipeline for the low adding system being routed directly to originally is truncated, the Waste water concentrating system of low temperature phase change is accessed.If flue gas
The non-cloth of system sets low low-level (stack-gas) economizer, then needs to increase newly low low-level (stack-gas) economizer to recycle former flue gas heat.General low temperature
The coolant-temperature gage that comes of intermediate heat medium water is 70 DEG C or more, in order to which maximum possible using fume afterheat and prevents low-temperature corrosion, intermediate heat
The coolant-temperature gage that comes of matchmaker's water is selected as 70 DEG C, through rising to 95 DEG C or so with its temperature after flue gas heat exchange.Intermediate heating agent after heating
Water is sent to waste water heater and desulfurization wastewater exchanges heat, and it is 35 DEG C or so that general waste water, which carrys out coolant-temperature gage, can heat desulfurization wastewater
To 65-75 DEG C, the waste water after heating enters waste water flash tank and carries out vacuum flash, and flash temperature is between 55-65 DEG C, concentrate
Density wastewater afterwards comes out from flash tank bottom and is sent to gaseous effluent cooler, is exchanged heat with low pressure condensation water with it, what is exchanged heat for the first time is low
Pressure condensation water and the secondary steam of waste water flash drum overhead exchange heat within the condenser, and secondary steam condensed water can be used for desulfurizing tower work
Skill moisturizing, the low pressure condensation water being heated are back to low adding system, complete the recycling of fume afterheat.Density wastewater quilt after cooling
It send to effluent settling chamber, by multi stage precipitation, supernatant, which with new desulfurization wastewater is sent to waste water heater and heats again, to be followed
Ring concentrate.
Embodiment 2
A kind of device using low-grade flue gas concentration waste water is present embodiments provided, as shown in Figures 2 and 3, in above-mentioned reality
On the basis of applying example 1, as the embodiment of changeable type, evaporation drying unit is rotary spray evaporation device 14, upper part setting
High temperature dry flue gas import, along the circulating direction of flue gas, the import of high temperature dry flue gas is connected to the upstream flue of air preheater 0, so that
High temperature dry flue gas in the upstream flue of air preheater 0 enters in rotary spray evaporation device to exchange heat with dense desulfurization wastewater；Specifically, high
Warm dry flue gas import is connected to the gas approach of air preheater 0；
The lower part of rotary spray evaporation device is provided with the outlet of high temperature wet flue gas, the outlet of high temperature wet flue gas with air preheater 0 and remove
Flue connection between dirt unit 1, specifically, the outlet of high temperature wet flue gas is connected to the gas approach of dust removing units 1, and relative to
The connectivity points of the connectivity points of the import of high temperature dry flue gas and upstream flue, the outlet of high temperature wet flue gas and upstream flue are close to dust removing units
1, the connectivity points of sedimentation device 8 and rotary spray evaporation device are located at the top of rotary spray evaporation device, specifically, sedimentation device 8
It is located at the top of rotary spray evaporation device with the connectivity points of rotary spray evaporation device.
In actual condition, the spray drying tower independently rotated is can be used in evaporation drying unit, the spray drying independently rotated
Tower is arranged in except flue gas system, and gas bypass is arranged, and is extracted denitration SCR and is exported small part flue gas to spray drying tower, desulfurization
Waste water sprays into spray drying tower and the concentrated water after atomization is evaporated to water vapour using the heat of flue gas in spray drying tower, sprays
Mist drying tower exiting flue gas enters dust removing units gas approach, and steam enters in desulfurizing tower with the flue gas after dedusting, evaporative crystallization
Object enters electric precipitator with dust and is captured with grey outlet.It is spray-dried the solid salt after tower bottom discharge is concentrated and dried.
Embodiment 3
A kind of device using low-grade flue gas concentration waste water is present embodiments provided, on the basis of above-described embodiment 1 or 2
On, further include the first pump 11, be connected to flash tank 6, for making to be in negative pressure state in flash tank 6 and controlling vacuum degree in it；
Also in order to guarantee waste water after heating can flash concentration, the concentration systems of low temperature phase change need matched with vacuum pump (namely the
One pump 11), connect with waste water flash tank and condenser by vacuum pump, is located at after condenser, and secondary steam is first carried out in condenser
Cooling, cooling procedure undergoes phase transition generation negative pressure, itself can maintain system negative pressure state, but system opens machine and keeps vacuum degree
Stablize, need to be arranged vacuum pump, vacuum pump is vacuumized when opening machine, in the process of running, it is solidifying need to only to extract secondary steam
The on-condensible gas that elutriation goes out reduces vacuum pump power consumption while guaranteeing that system vacuum is stablized；
Second pump 12, is set on the pipeline between sedimentation device 8 and First Heat Exchanger 5, by supernatant and/or additional
Desulfurization wastewater is sent into First Heat Exchanger 5；
Third pump 13, is set on the pipeline between sedimentation device 8 and evaporation drying unit.
4th pump 15, is set on the pipeline between flash tank 6 and the second heat exchanger 9；
5th pump 16, is set to the water return pipeline of low pressure condensation water or comes on waterpipe.
In addition, it should be noted that, the water quality and water characteristic of desulfurization wastewater and unit load, coal-fired ingredient, operation item
The many factors such as part, sulfur removal technology water water quality, lime stone ingredient are related, have the spies such as pollutant is complex in composition, fluctuation range is big
Point, pH value is lower, and in acidity, suspension content is high in water, salt content is high, there are the possibility of heavy metals exceeding standard, chloride contents
Very high, corrosivity is very strong, is the waste water that disposition is most difficult in power plant.Carrying out decrement concentration to desulfurization wastewater then needs a large amount of high-quality to steam
Hair or flue gas, energy consumption is again high, no matter using fume afterheat before unit steam extraction or air preheater can cause adverse effect to unit, be
Solve the problems, such as this, the present invention is using a kind of device of flue gas waste heat recovery collaboration Waste water concentrating, and the device is by being arranged in electricity
Low low-level (stack-gas) economizer before or after deduster recycles former flue gas heat, and recycled heat is sent to waste water by heat medium water and heated
Device, the waste water that effluent settling chamber is sent carry out heat temperature raising, and the waste water after heating enters waste water flash tank, and flash tank is negative pressure
State, vacuum degree are provided by vacuum pump, and vacuum pump is connected with condenser, are located at after condenser.Density wastewater after flash distillation from
Flash tank bottom enters gaseous effluent cooler, and entrained heat is used to heat low pressure condensation water for the first time, density wastewater after cooling into
Enter effluent settling chamber, by fractional precipitation, supernatant and new desulfurization wastewater are re-circulated to waste water heater, wastewater sedimentation
The a small amount of density wastewater of bottom of pond portion then send the flue sprayer to electric precipitator, after being atomized using the high-temperature residual heat flue gas in flue
Concentrated water be evaporated to water vapour, steam enters desulfurizing tower with the flue gas after dedusting, and evaporation drying object is removed with dust into electricity
Dirt device is with grey outlet；Or the evaporation drying into the spray evaporation tower independently rotated is sent, extract the outlet denitration SCR small part flue gas extremely
Evaporating column, desulfurization wastewater spray into evaporating column and the concentrated water after atomization are evaporated to water vapour using the heat of flue gas in evaporating column,
Evaporating column exiting flue gas enters deduster gas approach, and steam enters desulfuration absorbing tower with the flue gas after dedusting；Evaporative crystallization object
Enter electric precipitator with dust to be captured with grey outlet.Resulting secondary steam is flashed to come out from flash drum overhead into cold
Condenser, within the condenser to low pressure condensation water carry out reheating, by the low pressure condensation water after reheating be back to and its
The low plus circulation of temperature close, secondary steam condensed water are then used for desulphurization system technique moisturizing.It is low by the present apparatus
The flue gas heat that temperature is recycled first is used for desulfurization wastewater concentration, solves the disadvantage that regular course utilizes high-quality heat energy evaporation
End, meanwhile, heat transfer contained by it is given to low pressure condensation water system after Waste water concentrating, is made heat without outlet, is obtained adequately
Cascade utilization meets desulfurization and abolishes processing institute's calorific requirement and do not lose how many heat, most of heat is finally transmitted to low
Pressure condensation water, to reduce units consumption.
The present apparatus can make full use of the low low-level (stack-gas) economizer of the existing flue gas waste heat recovery equipment of power plant, if not carrying out more than flue gas
Recuperation of heat transformation, then need to increase low low-level (stack-gas) economizer newly before or after electric precipitator.Routine techniques is will by low low-level (stack-gas) economizer
Flue gas system waste heat is recycled for heating low pressure condensation water or steam air heater, and desulfurization wastewater concentration systems are added in the present apparatus, first
Concentrate is carried out to waste water using recycled heat, then is given density wastewater and secondary steam heat transfer by cooler and condenser
Low pressure condensation water, institute's recovered flue gas heat is in the process almost without loss, and only quality decreases.Concentration systems and evaporation knot
Crystallographic system system is that can be changed according to unit load and be adjusted independently of flue gas system.
The low low-level (stack-gas) economizer recycling by being arranged in front of or after electric precipitator is had the technical effect that achieved by the present invention
Fume afterheat can be improved the dust collection capacity of electric precipitator and reduce the moisturizing of desulfurizing tower process water.In Waste water concentrating system, utilize
For improving desulfurization wastewater temperature, the waste water after heating up is flashed the heat of off-gas recovery in waste water flash tank, thus
Realize the concentration of desulfurization wastewater, flash tank is negative pressure state, and vacuum degree is provided by vacuum pump, and institute's recovered flue gas heat is with concentration
Waste water and secondary steam are taken out of, recycle concentration waste water and condensation secondary steam institute heat content using low pressure condensation water, finally make this
Heat is back to low pressure condensation water system, in the case where almost not losing recycled heat, has expanded heat purposes, has realized heat
Energy cascade utilization, condensed secondary steam condensed water can be used for desulphurization system technique moisturizing.Concentration waste water is pumped to through waste water
Effluent settling chamber, after multi stage precipitation, supernatant is recycled to waste water heater with the desulfurization wastewater newly entered, a small amount of highly concentrated
The waste water of degree is sent to evaporation drying unit then to control the chlorine ion concentration of concentration systems waste water.It is sent to flue spray evaporation
When device, the concentrated water after atomization is evaporated to water vapour using the high-temperature residual heat flue gas in flue, steam with the flue gas after dedusting into
Enter desulfurizing tower, evaporative crystallization object enters electric precipitator with grey outlet with dust；Or it is sent to the spray evaporation independently rotated
Evaporation drying in tower extracts denitration SCR and exports small part flue gas to evaporating column, and it is sharp in evaporating column that desulfurization wastewater sprays into evaporating column
The concentrated water after atomization is evaporated to water vapour with the heat of flue gas, evaporating column exiting flue gas enters deduster gas approach, steam
Enter desulfuration absorbing tower with the flue gas after dedusting；Evaporative crystallization object enters electric precipitator with dust and is captured with grey outlet.
It solves coal-burning power plant or other industry flue gas waste heat recovery in the above manner, while realizing Waste water concentrating again.This is
System has that low energy consumption, small investment, operating cost are low, reaches the environment protectings such as efficient energy-saving and emission-reduction, have society well and
Economic impact.
Obviously, the above embodiments are merely examples for clarifying the description, and does not limit the embodiments.It is right
For those of ordinary skill in the art, can also make on the basis of the above description it is other it is various forms of variation or
It changes.There is no necessity and possibility to exhaust all the enbodiments.And it is extended from this it is obvious variation or
It changes still within the protection scope of the invention.
Claims (9)
1. a kind of device using low-grade flue gas concentration waste water, dust removing units and desulfurization unit including connection setting are also wrapped
Economizer is included, be set between the dust removing units and desulfurization unit or along flue gas circulating direction, is set to the dedusting
Unit upstream, which is characterized in that it further include Waste water concentrating system, the Waste water concentrating system includes,
First Heat Exchanger is connected to the economizer, by desulfurization wastewater and the first heat transferring medium in the economizer
It exchanges heat in the First Heat Exchanger；
Flash tank including shell and is set to the concentration wastewater outlet of the lower part of the housing, the shell and first heat exchange
Device connection, is sent into the flash tank with the desulfurization wastewater after will heat up and is flashed；
Second heat exchanger is connected to the concentration wastewater outlet, waste water will be concentrated and change in second heat exchanger with second
Thermal medium heat exchange；
Sedimentation device is connected to second heat exchanger, and the concentration waste water after cooling is sent into the sedimentation device and is sunk
Drop.
2. the apparatus according to claim 1, which is characterized in that the sedimentation device includes at least two-stage sedimentation unit, with
Concentration waste water after making cooling carries out multi stage precipitation；
The top of the sedimentation device is connected to the First Heat Exchanger, so that supernatant in the sedimentation device and/or outer
Add desulfurization wastewater to enter in the First Heat Exchanger, and is changed with the first heat transferring medium in the economizer described first
Heat exchange in hot device.
3. the apparatus of claim 2, which is characterized in that further include evaporation drying unit, with the sedimentation device
The dense desulfurization wastewater of the sedimentation device lower part is sent into the evaporation drying unit by lower part connection；
Air preheater is set on the upstream flue of the dust removing units.
4. device according to claim 3, which is characterized in that the evaporation drying unit is flue spray evaporator, edge
On the circulating direction of flue gas, the flue spray evaporator is set in the upstream flue of the dust removing units.
5. device according to claim 3, which is characterized in that the evaporation drying unit is rotary spray evaporation device,
The import of high temperature dry flue gas is arranged in top, and along the circulating direction of flue gas, the high temperature dry flue gas import is upper with the air preheater
Swim flue connection so that high temperature dry flue gas in the upstream flue of the air preheater enter in the rotary spray evaporation device with it is dense
Desulfurization wastewater heat exchange；
The lower part of the rotary spray evaporation device is provided with the outlet of high temperature wet flue gas, and the high temperature wet flue gas outlet and the sky are pre-
The connectivity points of flue connection between device and dust removing units, the sedimentation device and the rotary spray evaporation device are located at the rotation
Turn the top of spray evaporator.
6. device according to any one of claims 1-5, which is characterized in that further include,
Third heat exchanger, the secondary steam outlet with the upper part of the housing, the third heat exchanger are also changed with described second
Hot device connection, so that the second heat transferring medium after the heating in second heat exchanger enters the third heat exchanger, and
It exchanges heat again with the secondary steam from the flash tank.
7. the device according to any one of claim 2-6, which is characterized in that further include,
First pump, is connected to the flash tank, for making to be in negative pressure state in the flash tank and controlling vacuum degree in it；
Second pump, is set on the pipeline between the sedimentation device and the First Heat Exchanger, by supernatant and/or additional
Desulfurization wastewater is sent into the First Heat Exchanger；
Third pump, is set on the pipeline between the sedimentation device and the evaporation drying unit；
4th pump, is set on the pipeline between the flash tank and the second heat exchanger；
5th pump, is set to the water return pipeline of low pressure condensation water or comes on waterpipe.
8. device according to claim 7, which is characterized in that further include chimney, the chimney and the desulfurization unit connect
It is logical；
The dust removing units are electric precipitator；The economizer is low low-level (stack-gas) economizer；The desulfurization unit is desulfurizing tower.
9. device according to claim 1 to 8, which is characterized in that first heat transferring medium is heat medium water；
Second heat transferring medium is low pressure condensation water.
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