CN210620491U - System for zero release of flue gas desulfurization waste water - Google Patents
System for zero release of flue gas desulfurization waste water Download PDFInfo
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- CN210620491U CN210620491U CN201921318991.2U CN201921318991U CN210620491U CN 210620491 U CN210620491 U CN 210620491U CN 201921318991 U CN201921318991 U CN 201921318991U CN 210620491 U CN210620491 U CN 210620491U
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Abstract
The utility model discloses a system of flue gas desulfurization waste water zero release, include through the buffering that the pipeline links to each other in order subsides unit, multiple-effect circulation evaporation unit, concentrate collection unit and dry unit, multiple-effect circulation evaporation unit includes the circulation evaporation subelement that two effects establish ties and set up at least. The utility model is suitable for a coal fired generating set's flue gas desulfurization waste water treatment can realize that zero liquid of flue gas desulfurization waste water discharges and the system flow is short, need not traditional three headers and handles, also need not traditional chemistry and softens the processing, and make full use of coal fired power plant waste heat simultaneously, with low costs just can the long-term steady operation of assurance system.
Description
Technical Field
The utility model relates to a desulfurization waste water treatment's technical field, more specifically say, relate to a system of flue gas desulfurization waste water zero release.
Background
At present, the environment protection situation is severe, and particularly, after the comprehensive control of the discharge of water pollution sources is emphasized by the action plan of water pollution prevention and control (ten items of water) issued by the state academy in 2015, the discharge standard of wastewater in various industries is more and more strict, the pollution to the environment needs to be reduced to the maximum extent, and high-salt concentrated water in various industries also needs to reach zero liquid discharge. Limestone gypsum wet desulphurization is adopted for most coal-fired power generating sets, and the terminal wastewater is high-salinity wastewater after flue gas desulphurization. Desulfurization waste water concentration is high and the composition is complicated, and the salinity of waste water can not be handled to traditional triplex case, if the triplex case goes out the direct discharge and will cause very big harm to the environment. With the continuous improvement of the water treatment requirement, the realization of zero discharge of the desulfurization wastewater of the coal-fired power plant is imperative.
The desulfurization wastewater is the terminal wastewater of a coal-fired power plant, has high salt concentration (TDS: 30000-60000 mg/L), contains various heavy metal ions and contains CaSO4Tends to be saturated, belongs to typical high-salt wastewater which is difficult to treat and is difficult to treat by the traditional water treatment technology.
The main treatment technology of desulfurization waste water treatment at present is triple box precipitation filtration treatment, can not satisfy new emission requirement, and traditional triple box complex operation, the running cost is high. The current zero discharge technology of desulfurization waste water after passing through a triple box is mainly divided into a membrane method technology and a thermal method technology.
The technical route adopted by the membrane method technology is as follows: softening>Salt separation>Membrane concentration>And (4) crystallizing. The technical route has long flow, high investment and operation cost (the investment cost is more than 200 ten thousand per ton of water according to the water amount per hour, the treatment cost per ton of water is more than 80 yuan), poor overall economy, difficult later maintenance of the membrane and finally prepared NaCl and Na2SO4The salt economy is poor. In addition, there is also a small amount of miscellaneous salts that ultimately need to be handled separately in this route. With the increasing environmental protection requirement, the part of miscellaneous salt needs to be treated according to the danger waste, and the treatment cost is high.
Thermal methods are divided into multiple-effect evaporation and flue gas evaporation. The multi-effect evaporation is that the wastewater is softened and then the desulfurized wastewater is concentrated or evaporated into mixed salt by adopting steam. Flue gas evaporationThe desulfurization waste water is directly dried into miscellaneous salt by adopting high-temperature (the smoke gas is above 300 ℃ in front of an air preheater) or low-temperature (the smoke gas is about 150 ℃ at the inlet of a dust remover). The subsequent treatment of the miscellaneous salt finally obtained by multi-effect evaporation is difficult, and the CaSO4The heat exchange tube is easy to be blocked due to scaling in the evaporation process, and generally needs to be cleaned once in 2-3 months. The flue gas evaporation has certain influence on a flue gas system, and if the extracted flue gas amount is too large, a series of problems of unit heat efficiency reduction, unstable combustion, aggravation of cold end corrosion of an air preheater and the like can be caused. Multiple effect evaporation to avoid CaSO4Scaling, requiring a perfect softening pretreatment, the overall operating cost will be higher than 60 yuan/ton water. The heat efficiency of the unit is reduced by the evaporation of the flue gas, if the heat efficiency of the unit is kept unchanged, the coal consumption needs to be increased properly, and the overall operation cost is about 40 yuan/ton of water on the basis of considering the coal consumption.
SUMMERY OF THE UTILITY MODEL
To the problem that exists among the prior art, the utility model provides a flue gas desulfurization waste water zero discharge system of optimization is applicable to coal-fired generating set's flue gas desulfurization waste water treatment, can realize that zero liquid of flue gas desulfurization waste water discharges and the system flow is short.
The utility model provides a system for zero discharge of flue gas desulfurization wastewater, which comprises a buffering sedimentation unit, a multiple-effect circulating evaporation unit, a concentrated solution collecting unit and a drying unit which are sequentially connected through a pipeline, wherein the multiple-effect circulating evaporation unit at least comprises a circulating evaporation subunit which is provided with two effects in series connection, wherein,
the water inlet of the buffering sedimentation unit is connected with a flue gas desulfurization waste water pipeline, the water outlet of the buffering sedimentation unit is connected with the water inlet of the multi-effect circulating evaporation unit, and the concentrated water outlet of the multi-effect circulating evaporation unit is connected with the water inlet of the concentrated solution collection unit;
the concentrated solution collection unit is characterized in that a water outlet of the concentrated solution collection unit is connected with a water inlet of the drying unit, the drying unit is further connected with an upstream pipeline of the high-temperature flue gas supply flue through an inlet flue and is connected with a downstream pipeline of the high-temperature flue gas supply flue through an outlet flue, the downstream pipeline of the high-temperature flue gas supply flue is connected with the dust removal unit, and a drying heat source of the drying unit is the high-temperature flue gas from the high-temperature flue gas supply flue.
According to an embodiment of the system for zero emission of flue gas desulfurization wastewater of the present invention, each effect circulating evaporation sub-unit of the multiple effect circulating evaporation unit comprises a separation chamber, a heater, a concentrated water pump and a circulating pump;
the circulation concentration part at the lower part of the separation chamber is connected with a water inlet of the heater through a circulation pump, the circulation concentration part at the lower part of the separation chamber is also connected with a water inlet of the heater in the next effective circulation evaporation subunit or a water inlet of the concentrated solution collection unit through a concentrated water pump, a steam outlet of the heater is connected with a steam-water separation part at the upper part of the separation chamber, and a steam inlet is connected with a heat source pipeline or the steam-water separation part at the upper part of the separation chamber in the previous effective circulation evaporation subunit;
and the water outlet of the buffer sedimentation unit is connected with a circulating concentration part at the lower part of a separation chamber in a primary circulating evaporation subunit of the multi-effect circulating evaporation unit.
According to the utility model discloses an embodiment of the system of flue gas desulfurization waste water zero release, each effect circulation evaporation subelement of multiple effect circulation evaporation unit is still including setting up the swirler between heater or concentrate collection unit in concentrated water pump and next effect circulation evaporation subelement, the top of swirler links to each other and the bottom links to each other with the seed crystal jar with the water inlet of the heater in the next effect circulation evaporation system or the water inlet of concentrate collection unit, the seed crystal jar passes through the seed crystal pump and links to each other with the concentrated part of circulation of separating chamber lower part in each effect circulation evaporation subelement, still is provided with the seed crystal on the seed crystal jar and adds the mouth of throwing into in advance.
According to the utility model discloses an embodiment of the system of flue gas desulfurization waste water zero release, the heater lower part among each effect circulation evaporation subelement of multiple-effect circulation evaporation unit still is provided with the distilled water and draws forth the mouth, and wherein, the steam-water separation part on separation chamber upper portion links to each other with the condenser that is provided with the vacuum pump in the last effect circulation evaporation subelement.
According to the utility model discloses an embodiment of the system of flue gas desulfurization waste water zero release, drying unit is including setting up desicator and the atomizer in a plurality of unit, the female pipe between concentrate collection unit and each desicator adopts the backward flow setting of high flow, big pipe diameter and unnecessary concentrate backward flow to concentrate collection unit, wherein, spout in each desicator after the concentrate atomization from concentrate collection unit.
According to the utility model discloses an embodiment of the system of flue gas desulfurization waste water zero release, buffering subsides the unit and includes buffering setting tank and the sludge pump and the intake pump that link to each other with buffering setting tank, concentrate collection unit includes concentrate jar and concentrate pump.
According to the utility model discloses an embodiment of the system of flue gas desulfurization waste water zero release, the upper reaches pipeline that the flue was supplied with to the high temperature flue gas links to each other with air heater's flue gas entry and the low reaches pipeline that the flue was supplied with to the high temperature flue gas links to each other with air heater's exhanst gas outlet, air heater sets up the low reaches at SCR denitrification facility. .
Compared with the prior art, the utility model provides a flue gas desulfurization waste water zero discharge system who optimizes is applicable to coal-fired generating set's flue gas desulfurization waste water treatment, can realize that zero liquid of flue gas desulfurization waste water discharges and system flow is short. The flue gas desulfurization wastewater does not need the traditional triple box treatment and the traditional chemical softening treatment, simultaneously makes full use of the waste heat (low-parameter steam, flue gas waste heat and the like) of the coal-fired power plant, has low overall investment and operation cost, and can ensure the long-term stable operation of the system.
Drawings
Fig. 1 shows a schematic structural diagram of a system for zero emission of flue gas desulfurization wastewater according to an exemplary embodiment of the present invention.
Description of reference numerals:
1-buffer settling tank, 2-water inlet pump, 3-sludge pump, 41-first effect separation chamber, 51-first effect heater, 61-first effect circulating pump, 71-first effect cyclone, 81-first effect concentrated water pump, 42-last effect separation chamber, 52-last effect heater, 62-last effect circulating pump, 72-last effect cyclone, 82-last effect concentrated water pump, 9-crystal seed tank, 91-crystal seed, 10-crystal seed pump, 11-concentrated liquid tank, 12-concentrated liquid pump, 13-condenser, 14-vacuum pump, 15-dryer, 16-SCR denitration device, 17-air preheater, 18-dust remover, 19-inlet flue of dryer, 20-outlet flue of dryer.
Detailed Description
All of the features disclosed in this specification, or all of the steps in any method or process so disclosed, may be combined in any combination, except combinations of features and/or steps that are mutually exclusive.
Any feature disclosed in this specification may be replaced by alternative features serving equivalent or similar purposes, unless expressly stated otherwise. That is, unless expressly stated otherwise, each feature is only an example of a generic series of equivalent or similar features.
The following specifically explains the concept of zero discharge of flue gas desulfurization wastewater.
The technical idea of the utility model specifically is that after carrying out simple gravity settlement with the waste water that flue gas desulfurization system (not containing the three-way box) produced, carry out multiple-effect circulation evaporation treatment and obtain the concentrate after the concentration, utilize the complete evaporation to dryness of the concentrate after high temperature flue gas will concentrate, the miscellaneous salt after the evaporation to dryness returns the dust remover along with the flue gas in the waste water, evenly sneak into at last and realize the zero release in the fly ash.
According to the technical idea above, the utility model provides a system of flue gas desulfurization waste water zero release.
Fig. 1 shows a schematic structural diagram of a system for zero emission of flue gas desulfurization wastewater according to an exemplary embodiment of the present invention.
As shown in fig. 1, according to the exemplary embodiment of the present invention, the system for zero discharge of flue gas desulfurization wastewater includes a buffer settling unit, a multiple-effect circulation evaporation unit, a concentrated solution collecting unit and a drying unit which are connected in sequence through a pipeline, wherein the multiple-effect circulation evaporation unit includes at least a circulation evaporation subunit which is provided in a two-effect series connection manner.
The following describes each part separately.
The utility model discloses a water inlet of unit is subsided in buffering links to each other with flue gas desulfurization waste water pipeline and the delivery port links to each other with the water inlet of multiple-effect circulation evaporation unit. Wherein, the buffering settlement unit mainly realizes simple gravity buffering settlement of the flue gas desulfurization waste water which is not treated by the triple box, and removes part of suspended matters. Preferably, the buffering and settling unit comprises a buffering and settling tank 1, and a sludge pump 3 and a water inlet pump 2 which are connected with the buffering and settling tank 1, sludge settled at the bottom is intermittently discharged through the sludge pump 3, and raw water at the upper part is pumped out through the water inlet pump 2 and pumped into the multi-effect circulating evaporation unit.
The utility model discloses a multiple-effect circulation evaporation unit carries out multiple-effect circulation evaporation concentration to the raw water and handles, and its dense water export links to each other with the water inlet of concentrate collecting unit. The effect number of the multiple-effect circulating evaporation unit is determined according to the specific water quantity and the water quality, and the utility model discloses a zero discharge system of flue gas desulfurization waste water is generally set up to two ~ three effects.
Specifically, the utility model discloses each effect circulation evaporation subunit of multiple-effect circulation evaporation unit includes separation chamber, heater, dense water pump and circulating pump, and for example one effect circulation evaporation subunit includes one and imitates separation chamber 41, one imitates heater 51, one imitates circulating pump 61 and one imitates dense water pump 81, and last effect circulation evaporation subunit includes last effect separation chamber 42, last effect heater 52, last effect circulating pump 62 and last effect dense water pump 82.
Wherein, the flash evaporation of the concentrated water and/or the raw water is realized after the separation chamber is heated, part of water forms secondary steam, and the concentrated water and/or the raw water are concentrated. The separating chamber comprises a lower circulating concentration part and an upper steam-water separation part. The heater heats the concentrated water and/or the raw water, the concentrated water pump is used for outputting the concentrated water, and the circulating pump is used for circulating the concentrated water and/or the raw water.
The water outlet of the buffer sedimentation unit is connected with the circulating concentration part at the lower part of the separation chamber in the one-effect circulating evaporation subunit of the multi-effect circulating evaporation unit so as to supply the raw water to the multi-effect circulating evaporation unit for multi-effect circulating evaporation concentration.
The circulation concentration part at the lower part of the separation chamber is connected with a water inlet of the heater through a circulation pump, the circulation concentration part at the lower part of the separation chamber is also connected with a water inlet of the heater in the next effective circulation evaporation subunit or a water inlet of the concentrated solution collection unit through a concentrated water pump, a steam outlet of the heater is connected with a steam-water separation part at the upper part of the separation chamber, and a steam inlet is connected with a heat source pipeline or the steam-water separation part at the upper part of the separation chamber in the last effective circulation evaporation subunit.
In order to avoid scaling, the multiple-effect circulation evaporation sub-unit of the utility model further comprises a cyclone arranged between the heater or the concentrated solution collecting unit in the concentrated water pump and the next-effect circulation evaporation sub-unit, for example, the one-effect circulation evaporation sub-unit comprises a first-effect cyclone 71, and the last-effect circulation evaporation sub-unit comprises a last-effect cyclone 72. The top of the cyclone is connected with the water inlet of a heater in the next-effect circulating evaporation system or the water inlet of the concentrated solution collecting unit, the bottom of the cyclone is connected with the seed crystal tank 9, and the seed crystal tank 9 is connected with the circulating and concentrating part at the lower part of the separation chamber in each effect circulating evaporation subunit through the seed crystal pump 10, so that the liquid flows back to each effect circulating evaporation subunit. In addition, the seed tank 9 may be provided with a pre-seeding inlet, and a small amount of seed crystals 91 may be manually added directly to the seed tank 9 when the system is started.
The multiple-effect circulating evaporation unit is in a forced circulating evaporation mode, raw water is heated by the heater in the circulating process and then enters the separation chamber for flash evaporation, secondary steam obtained by flash evaporation enters the next-effect heater for continuous heating, and therefore heat of the secondary steam is recycled. And continuously circulating, evaporating and concentrating part of the flash evaporated concentrated water by a circulating pump, allowing part of the concentrated water to enter a cyclone by a concentrated water pump for cyclone separation, allowing the concentrated water at the top of the cyclone to enter a next effect for continuous evaporation, and collecting a solid-liquid mixture at the bottom of the cyclone in a seed crystal tank 9.
In addition, the lower part of the heater in each effect circulating evaporation subunit of the multi-effect circulating evaporation unit is also provided with a distilled water outlet, and the steam-water separation part at the upper part of the separation chamber in the last effect circulating evaporation subunit is connected with a condenser 13 provided with a vacuum pump. That is, the secondary steam discharged from the last-effect separation chamber 42 is condensed into distilled water by the condenser 13. The multi-effect circulating evaporation unit operates in a micro-negative pressure state, and the vacuum degree is maintained through the vacuum pump 14.
The concentrated solution collecting unit is used for collecting concentrated water concentrated by the multi-effect circulation evaporation unit, and preferably comprises a concentrated solution tank 11 and a concentrated solution pump 12. The water outlet of the concentrated solution collecting unit is connected with the water inlet of the drying unit, and the concentrated solution pump 12 sends the concentrated solution in the concentrated solution tank 11 to the drying unit for evaporation.
The drying unit is connected with an upstream pipeline of the high-temperature flue gas supply flue through an inlet flue 19 and is connected with a downstream pipeline of the high-temperature flue gas supply flue through an outlet flue 20, the downstream pipeline of the high-temperature flue gas supply flue is connected with the dust removal unit, and a drying heat source of the drying unit is the high-temperature flue gas from the high-temperature flue gas supply flue. That is, the utility model discloses a drying unit adopts the bypass form to supply with the flue parallelly connected with the high temperature flue gas, and the flue gas volume of extraction is little, has avoided the influence to former flue gas system.
Preferably, the drying unit comprises dryers 15 and atomizers (not shown) arranged in several trains, and the main pipe between the concentrate collecting unit and each dryer 15 is provided with a high-flow, large-pipe-diameter backflow arrangement and the excess concentrate flows back into the concentrate collecting unit, wherein the concentrate from the concentrate collecting unit is atomized and sprayed into each dryer.
An upstream pipe of the high-temperature flue gas supply flue is connected with a flue gas inlet of the air preheater 17 and a downstream pipe of the high-temperature flue gas supply flue is connected with a flue gas outlet of the air preheater 17 and is located downstream of the SCR denitration device 16.
In the dryer 15, the concentrated solution is atomized and then fully mixed with the high-temperature flue gas from the inlet flue 19 of the dryer, and then is quickly evaporated to dryness, and the dried mixed salt and the flue gas return to the inlet of the dust remover 18 through the outlet flue 20 of the dryer. The high-temperature flue gas adopts flue gas between an SCR denitration device 16 and an air preheater 17, and miscellaneous salts are uniformly mixed with the flue gas in a flue, collected by a dust remover 18 and then uniformly mixed into fly ash.
Therefore, the utility model discloses reduced traditional three headers, equipment such as chemical softening, the system is simple and effectively solved present other desulfurization waste water treatment technique ubiquitous investment running cost height, miscellaneous salt can't handle, easy scale deposit and to boiler and flue influence a great deal of problem such as big.
When the system is used, the flue gas desulfurization wastewater is firstly subjected to buffering and settling treatment and separated to obtain raw water. Preferably, the suspended matter in the raw water is controlled below 1000 mg/L. The system is simpler by omitting the triple box and adopting simple sedimentation to preliminarily control suspended matters in the flue gas desulfurization wastewater.
Then the raw water is subject to multi-effect circulating evaporation treatment to at least obtain concentrated solution. Preferably, the raw water concentration multiplying power is controlled to be 5-10 times, and the flow rate of the multi-effect circulating evaporation treatment is controlled to be more than 2.8 m/s. The energy consumption of an evaporation system can be reduced by adopting multi-effect circulating evaporation treatment, at least two-effect circulating evaporation treatment is recommended to be adopted according to the water quality characteristics of the flue gas desulfurization wastewater, and 2-3-effect circulating evaporation treatment is preferred.
To prevent fouling, it is preferred to employ a cyclonic separation process to reflux the seeds during the effective cyclic evaporation process, whereby fresh seed addition is not required during normal operation. Specifically, each effect concentrated water obtained by the multi-effect cyclic evaporation treatment is subjected to cyclone separation treatment to obtain top concentrated water and bottom solid-liquid mixture, wherein the top concentrated water is subjected to next effect cyclic evaporation, the last effect concentrated water is used as a concentrated solution to be subjected to subsequent drying treatment, and the bottom solid-liquid mixture is used as a seed crystal or is mixed with a pre-seed crystal and then flows back to continue the multi-effect cyclic evaporation treatment. Wherein, the newly added crystal seeds adopt anhydrous calcium sulfate powder, and then the newly generated crystals in the concentration process of the raw water can be attached to the surface of the crystal seeds with the same crystal form to grow, thereby avoiding the scaling on the inner wall of the pipeline.
And then extracting high-temperature flue gas to dry the concentrated solution to obtain the miscellaneous salt. The high-temperature flue gas extracted in the step is preferably flue gas which comes from the front of an air preheater and has the temperature of 300-350 ℃, the amount of the extracted high-temperature flue gas is controlled to be not higher than 2% of the total amount of the flue gas so as to avoid adverse effects on an original flue gas system, and the high-temperature flue gas can ensure that a concentrated solution is completely evaporated to dryness to obtain miscellaneous salts. Moreover, the drying treatment preferably adopts a bypass mode of being connected with the flue gas pipeline in parallel to lead out high-temperature flue gas, so that the required flue gas amount is small, and the influence on an original flue gas system can be avoided.
And finally, mixing the miscellaneous salt with the subsequent flue gas, then performing dust removal and collection, and mixing the miscellaneous salt into the fly ash. The miscellaneous salt evaporated to dryness in the concentrated solution returns to an inlet flue of a dust remover along with the flue gas, and is finally uniformly mixed into the fly ash after being subjected to dust removal and collection in the dust remover.
The present invention will be described with reference to the following embodiments.
As shown in FIG. 1, in the embodiment, after the flue gas desulfurization wastewater before the triple box is precipitated by the buffer settling tank 1, suspended matters are below 1000mg/L, and then the raw water enters the multi-effect circulating evaporation unit.
The multi-effect circulating evaporation unit adopts a forced circulation evaporation mode, the wastewater is heated by the first-effect heater 51 and enters the first-effect separation chamber 41 for flash evaporation, part of the flash-evaporated concentrated water returns to the first-effect heater 51 for circulating evaporation by the first-effect circulating pump 61, and the flash-evaporated secondary steam is used as an evaporation heat source of the next effect to continuously evaporate the next-effect concentrated water. The flow rate of the pipeline is controlled to be more than 2.8m/s, and raw water is concentrated by 5-10 times in the multi-effect circulating evaporation unit.
And after the concentrated water in each effect in the multi-effect circulating evaporation unit passes through the cyclones 71-72 respectively, collecting the solid-liquid mixture at the bottom in the seed crystal tank 9, and then returning the solid-liquid mixture to each effect circulating evaporation subunit through the seed crystal pump 10. And enabling concentrated water at the tops of the cyclones 71-72 to enter the next effect for continuous circulating evaporation. The system is started up by manually adding a small amount of seed crystal 91 to maintain the proper amount of seed crystal for the system.
The concentrated solution after evaporation concentration is collected in a concentrated solution tank 11, and then is conveyed to a dryer 15 through a concentrated solution pump 12, wherein a conveying pipeline between the concentrated solution tank 11 and the dryer 15 is of a main pipe type, the flow is 2-4 times of the actually required flow, and the flow speed of the pipeline is controlled to be more than 2.5 m/s.
The dryer 15 adopts the high temperature flue gas of about 350 ℃ before the air heater 17 to evaporate the concentrate, and the dense water volume that the dryer 15 was handled is designed according to the demand of high temperature flue gas, in order to reduce a series of influences such as boiler efficiency, combustor stability and air preheater cold junction corruption, the high temperature flue gas volume that the dryer 15 extracted is not higher than the total amount of flue gas 2%.
The concentrated water is atomized and then sprayed into the dryer 15, a double-fluid spray gun or a high-speed rotary atomizer can be adopted as the atomization form, the particle size of the atomized concentrated solution is 50-100 um, and the pressure drop of the dryer 15 is within the range of 400-800 Pa.
The concentrated solution is dried to obtain miscellaneous salt, and finally enters a dust remover 18 through a flue. The miscellaneous salt and the smoke dust are mixed evenly in the dust remover 18 and then mixed into the fly ash.
The utility model provides a flue gas desulfurization waste water zero release treatment technology route has really realized the waste water zero release, and the system is simple and investment cost saves more than 20%, and the running cost is below 20 yuan/ton water, can effectively prevent system scale deposit and long-term steady operation, and the heat exchange tube cleaning cycle is more than 6 months.
The present invention is not limited to the foregoing embodiments. The invention extends to any novel feature or any novel combination of features disclosed in this specification, and to any novel method or process steps or any novel combination of features disclosed.
Claims (7)
1. A system for zero discharge of flue gas desulfurization wastewater is characterized by comprising a buffer sedimentation unit, a multi-effect circulating evaporation unit, a concentrated solution collection unit and a drying unit which are sequentially connected through a pipeline, wherein the multi-effect circulating evaporation unit at least comprises a circulating evaporation subunit formed by connecting two effects in series, wherein,
the water inlet of the buffering sedimentation unit is connected with a flue gas desulfurization waste water pipeline, the water outlet of the buffering sedimentation unit is connected with the water inlet of the multi-effect circulating evaporation unit, and the concentrated water outlet of the multi-effect circulating evaporation unit is connected with the water inlet of the concentrated solution collection unit;
the concentrated solution collection unit is characterized in that a water outlet of the concentrated solution collection unit is connected with a water inlet of the drying unit, the drying unit is further connected with an upstream pipeline of the high-temperature flue gas supply flue through an inlet flue and is connected with a downstream pipeline of the high-temperature flue gas supply flue through an outlet flue, the downstream pipeline of the high-temperature flue gas supply flue is connected with the dust removal unit, and a drying heat source of the drying unit is the high-temperature flue gas from the high-temperature flue gas supply flue.
2. The system for zero emission of flue gas desulfurization wastewater of claim 1, wherein each effect circulation evaporation sub-unit of the multi-effect circulation evaporation unit comprises a separation chamber, a heater, a concentrated water pump and a circulating pump;
the circulation concentration part at the lower part of the separation chamber is connected with a water inlet of the heater through a circulation pump, the circulation concentration part at the lower part of the separation chamber is also connected with a water inlet of the heater in the next effective circulation evaporation subunit or a water inlet of the concentrated solution collection unit through a concentrated water pump, a steam outlet of the heater is connected with a steam-water separation part at the upper part of the separation chamber, and a steam inlet is connected with a heat source pipeline or the steam-water separation part at the upper part of the separation chamber in the previous effective circulation evaporation subunit;
and the water outlet of the buffer sedimentation unit is connected with a circulating concentration part at the lower part of a separation chamber in a primary circulating evaporation subunit of the multi-effect circulating evaporation unit.
3. The system for zero emission of flue gas desulfurization wastewater according to claim 2, wherein each of the multiple-effect circulating evaporation sub-units further comprises a cyclone disposed between the concentrate pump and the heater or the concentrate collection unit in the next-effect circulating evaporation sub-unit, the top of the cyclone is connected to the water inlet of the heater or the concentrate collection unit in the next-effect circulating evaporation sub-unit, the bottom of the cyclone is connected to the seed crystal tank, the seed crystal tank is connected to the circulating and concentrating part at the lower part of the separation chamber in each of the multiple-effect circulating evaporation sub-units through the seed crystal pump, and the seed crystal tank is further provided with a seed crystal pre-adding inlet.
4. The system for zero emission of flue gas desulfurization wastewater as recited in claim 2, wherein a distilled water outlet is further provided at a lower portion of the heater in each effect circulating evaporation subunit of the multiple effect circulating evaporation unit, and wherein a steam-water separation portion at an upper portion of a separation chamber in the last effect circulating evaporation subunit is connected to a condenser provided with a vacuum pump.
5. The system for zero emission of wastewater generated by flue gas desulfurization according to claim 1, wherein the drying unit comprises dryers and atomizers arranged in a plurality of units, a main pipe between the concentrated solution collecting unit and each dryer is provided with a high-flow and large-pipe-diameter backflow device, and redundant concentrated solution flows back to the concentrated solution collecting unit, wherein the concentrated solution from the concentrated solution collecting unit is atomized and then sprayed into each dryer.
6. The system for zero emission of wastewater generated by flue gas desulfurization according to claim 1, wherein the buffer settling unit comprises a buffer settling tank/pond, a sludge pump and a water inlet pump which are connected with the buffer settling tank/pond, and the concentrated solution collecting unit comprises a concentrated solution tank and a concentrated solution pump.
7. The system for zero emission of wastewater generated by flue gas desulfurization according to claim 1, wherein an upstream pipe of the high-temperature flue gas supply flue is connected to a flue gas inlet of an air preheater and a downstream pipe of the high-temperature flue gas supply flue is connected to a flue gas outlet of the air preheater, and the air preheater is disposed downstream of the SCR denitration device.
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Cited By (2)
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| CN111892112A (en) * | 2020-08-31 | 2020-11-06 | 中电华创电力技术研究有限公司 | Treatment system for zero discharge of desulfurization wastewater of coal-fired power plant |
| CN112194298A (en) * | 2020-08-07 | 2021-01-08 | 东方电气集团东方锅炉股份有限公司 | System and method for recycling wastewater of whole power plant |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112194298A (en) * | 2020-08-07 | 2021-01-08 | 东方电气集团东方锅炉股份有限公司 | System and method for recycling wastewater of whole power plant |
| CN111892112A (en) * | 2020-08-31 | 2020-11-06 | 中电华创电力技术研究有限公司 | Treatment system for zero discharge of desulfurization wastewater of coal-fired power plant |
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