CN117700008A - Zero-emission evaporating treatment process for desulfurization wastewater of coal-fired power plant - Google Patents
Zero-emission evaporating treatment process for desulfurization wastewater of coal-fired power plant Download PDFInfo
- Publication number
- CN117700008A CN117700008A CN202311614060.8A CN202311614060A CN117700008A CN 117700008 A CN117700008 A CN 117700008A CN 202311614060 A CN202311614060 A CN 202311614060A CN 117700008 A CN117700008 A CN 117700008A
- Authority
- CN
- China
- Prior art keywords
- coal
- power plant
- zero
- desulfurization wastewater
- fired power
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 69
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 54
- 230000023556 desulfurization Effects 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 29
- 230000008569 process Effects 0.000 title claims abstract description 27
- 238000001704 evaporation Methods 0.000 title claims abstract description 22
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000003546 flue gas Substances 0.000 claims abstract description 42
- 238000001035 drying Methods 0.000 claims abstract description 31
- 239000007787 solid Substances 0.000 claims abstract description 18
- 239000002245 particle Substances 0.000 claims abstract description 14
- 239000002002 slurry Substances 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 20
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 238000000889 atomisation Methods 0.000 claims description 12
- 150000003839 salts Chemical class 0.000 claims description 12
- 238000004140 cleaning Methods 0.000 claims description 10
- 238000001914 filtration Methods 0.000 claims description 7
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 6
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 6
- 238000011010 flushing procedure Methods 0.000 claims description 6
- 239000004571 lime Substances 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 5
- 239000000498 cooling water Substances 0.000 claims description 4
- 239000010802 sludge Substances 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 3
- 239000008394 flocculating agent Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 239000000701 coagulant Substances 0.000 claims description 2
- 230000007797 corrosion Effects 0.000 claims description 2
- 238000005260 corrosion Methods 0.000 claims description 2
- 239000004744 fabric Substances 0.000 claims description 2
- 229910000856 hastalloy Inorganic materials 0.000 claims description 2
- 238000006386 neutralization reaction Methods 0.000 claims description 2
- 125000001741 organic sulfur group Chemical group 0.000 claims description 2
- 238000001556 precipitation Methods 0.000 claims description 2
- 238000010926 purge Methods 0.000 claims description 2
- UONOETXJSWQNOL-UHFFFAOYSA-N tungsten carbide Chemical compound [W+]#[C-] UONOETXJSWQNOL-UHFFFAOYSA-N 0.000 claims description 2
- 230000008020 evaporation Effects 0.000 abstract description 15
- 239000000428 dust Substances 0.000 abstract description 12
- 230000000694 effects Effects 0.000 abstract description 6
- 239000010881 fly ash Substances 0.000 abstract description 6
- 239000002956 ash Substances 0.000 abstract description 2
- 230000005684 electric field Effects 0.000 abstract description 2
- 239000002893 slag Substances 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract 1
- 238000002425 crystallisation Methods 0.000 description 6
- 230000008025 crystallization Effects 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000012528 membrane Substances 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- 238000010276 construction Methods 0.000 description 3
- 230000007547 defect Effects 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 235000019738 Limestone Nutrition 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000007605 air drying Methods 0.000 description 1
- 229910001854 alkali hydroxide Inorganic materials 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010835 comparative analysis Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- -1 fluoride ions Chemical class 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 238000013139 quantization Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Abstract
The invention provides a zero-emission evaporating treatment process for desulfurization waste water of a coal-fired power plant, which utilizes the existing equipment to the maximum extent through adjusting the operation mode of the existing facilities of the coal-fired power plant, improves the stability of an evaporating system, and when a lifting pump is sent to an atomizing disk rotating at a high speed in a tower, waste liquid is stretched into a film or pulled into filaments (depending on the rotating speed and the slurry amount) due to the effect of centrifugal force, and is broken and dispersed into liquid drops at the edge of the atomizing disk to be fully mixed with hot flue gas of a boiler. The desulfurization wastewater containing soluble and suspended solid particles is evaporated under high-temperature flue gas, and the outlet temperature of an evaporation tower is 150-160 ℃. The evaporated solid entrainment matter part enters the front main flue of the electric dust collector together with the flue gas, is trapped by the electric dust collector, is mixed with fly ash of the whole plant, and part of the solid entrainment matter part flows into the bottom of the drying tower to be pumped into an ash pipe of a first electric field of the electric dust collector through a bin pump or is mixed with a slag system.
Description
Technical Field
The invention relates to a wastewater treatment system, in particular to a zero-emission evaporation-to-dry treatment process for desulfurization wastewater of a coal-fired power plant.
Background
The combustion power coal of the coal-fired power plant is converted into electric energy, sulfur dioxide in the coal-fired flue gas can pollute the atmosphere, the limestone wet desulfurization technology is mature, the desulfurization efficiency is high, and the application range is wide, so that the method becomes the main flow process of the current desulfurization. The limestone wet desulfurization system needs to discharge certain desulfurization wastewater at regular intervals, so that the normal and stable operation of the desulfurization system is ensured.
When the desulfurization system is constructed, a desulfurization wastewater treatment process of a triple box method is generally constructed in a matched mode, and the desulfurization wastewater is discharged after reaching the standard. With the improvement of environmental protection requirements, the current yellow river and Yangtze river basin are required to finish the zero discharge of desulfurization wastewater of the coal-fired power plant in a limited period, and the conditional power plant is encouraged to start to build the zero discharge of desulfurization wastewater.
The current desulfurization wastewater zero-emission evaporation-to-dryness treatment process route of the mainstream coal-fired power plant is as follows.
1) Pretreatment, membrane concentration and traditional evaporative crystallization
The desulfurization wastewater is pretreated by adding alkaline substances (sodium hydroxide or lime), flocculating agents, gravity sedimentation and the like, most suspended matters, heavy metals, fluoride ions, hardness, silicon dioxide and other scaling substances in the wastewater are removed, then membrane technology (DTRO/DT, NF+SWRO, FO and the like) is adopted to carry out concentration reduction quantization on the pretreated wastewater, fresh water is recycled, concentrated water enters a subsequent traditional evaporative crystallization system (MED & MVR), condensed water is recycled, and crystallized salt is additionally treated.
Defects: the technology pretreatment, membrane concentration and traditional evaporative crystallization are added with alkaline substances in the earlier pretreatment for softening treatment, lime is added cheaply, but the sludge is large, the softening effect is difficult to ensure the subsequent membrane technology treatment, for example, the cost for adding sodium hydroxide is high. The subsequent evaporative crystallization system consumes a large amount of energy, the final crystallized salt also has no good sales channel, and there is a risk of being defined as hazardous waste by the subsequent environmental regulations.
2) Flue gas waste heat concentration and secondary air drying
The flue gas after taking the induced draft fan enters the concentration tower, the flue gas enters the concentration tank from the lower part, the desulfurization waste water is sprayed from the upper part, the vaporization part of the desulfurization waste water and the flue gas return to the absorption tower together, after the concentration at the bottom of the tower is dried by secondary air, solid particles such as crystalline salt enter the front flue of the dust remover along with the secondary air, and the solid particles are collected by the dust remover so as to achieve the effect of removal.
Defects: the flue gas waste heat concentration carries out concentration decrement to desulfurization waste water, leads to the solid content in the desulfurization waste water to increase, and flue gas waste heat concentration system is difficult to stable operation, has also increased the dry jam risk of overgrate air.
3) Low temperature flash concentrating and bypass flue drying
The desulfurization waste water is directly overflowed and extracted from a desulfurization waste water cyclone without a pretreatment system, hot water at the outlet of the existing low-temperature economizer is used as a heat source for heating, after three-effect flash evaporation concentration, the concentration rate can reach 90%, 50% -90% of the concentrated waste water is automatically adjustable on line, concentrated liquor enters spray dryers of two units respectively for evaporation drying or rotary sprayers (the heat source of the dryer is from hot flue gas at 350 ℃ in a flue between the front air pre-separators after denitration), generated dust and steam are introduced into a flue before electric dust removal along with the flue gas, chloride ions, other solid particles and metal elements are captured by utilizing electric dust removal, and evaporated steam enters a desulfurization tower. The water vapor generated in the flash evaporation concentration process can be recovered to desulfurization process water or other use water after condensation. Defects: the low-temperature flash evaporation concentration is used for carrying out flash evaporation concentration on desulfurization wastewater, the inherent impurities are used as crystal nuclei for crystallization, the crystal particles are large, and a subsequent evaporating system is easy to block, so that a bypass flue is adopted for drying, but the problem of easy blocking cannot be solved.
In summary, the prior art has some technical problems to be solved, the stable operation is difficult, and special pretreatment process sections ((1) pretreatment, (2) flue gas waste heat concentration, (3) low-temperature flash evaporation concentration) are required to be arranged, so that the engineering cost is high and the investment is repeated.
Disclosure of Invention
In order to solve the problems, the invention discloses a zero-emission evaporation-drying treatment process for desulfurization wastewater of a coal-fired power plant, which reduces the turbidity of spray water on the premise of saving a certain medicament, removes residual hard particles by using a self-cleaning filter, thereby reducing the solid content of spray wastewater, and finally adopts a high-temperature flue gas bypass rotary atomization drying system to set necessary facilities so as to realize a desulfurization wastewater zero-emission system with low engineering cost, short construction period and stable operation.
The zero-emission evaporating treatment process for the desulfurization wastewater of the coal-fired power plant comprises a desulfurization wastewater cyclone, a neutralization tank, a settling tank, a slurry clarifying tank and a water outlet tank which are sequentially connected, wherein the discharge end of the water outlet tank is connected with a water outlet conveying pump; sludge in the slurry clarifying tank is discharged through a plate-and-frame filter press, and is characterized in that: the device also comprises a self-cleaning filter, a buffer tank, a wastewater conveying pump and a rotary atomizer; filtering by a self-cleaning filter to remove residual hard particles; the water outlet section filtered by the self-cleaning filter is connected with a buffer tank, the buffer tank is used for adding liquid alkali, and sodium hydroxide solution is adopted to reduce the generation of precipitated substances; one end of the buffer tank is connected with a waste water conveying pump, a stainless steel Y-shaped filter is arranged on the waste water conveying pump, high-temperature flue gas generated by the boiler air preheater is conveyed into the rotary atomizer, a bottom outlet of the rotary atomizer is connected with a flue gas outlet of the boiler air preheater, and a cold air inlet is arranged at the bottom of the boiler air preheater.
Further, the high-temperature flue gas bypass rotary atomization drying system is adopted, hot secondary air is not adopted, and the high-temperature flue gas is utilized to the present, so that the high-temperature flue gas bypass rotary atomization drying system is arranged as a bypass system, and the system is convenient to overhaul and maintain.
Furthermore, the atomizing disk is manufactured by hastelloy C276, wherein the part contacted with the wastewater is made of tungsten carbide, corrosion resistance and wear resistance in the actual operation process are considered, and impurities in the wastewater and dried salt are prevented from wearing the nozzle of the atomizing disk too fast; the wastewater forms tiny fog drops under the action of high-strength centrifugal force of the rotary atomizer. The atomizer adopts a high-speed motor, the connection mode is direct connection, the rotating speed of the rotary atomizer is more than 15000 revolutions per minute, when the desulfurization waste water is sent to an atomizing disk rotating at high speed, the waste water stretches into a film or is pulled into filaments (depending on the rotating speed and the slurry amount) due to the action of centrifugal force, and the waste water breaks up and disperses into liquid drops at the edge of the atomizing disk. The optimal atomization effect of the slurry is ensured, and the droplet size is reduced.
When the hot flue gas is dispersed and enters the drying tower, the fine fog drops atomized by the rotary atomizer are contacted with the hot flue gas, in the gas-liquid contact process, moisture is rapidly evaporated, and before the atomized fog drops reach the wall of the drying tower by controlling gas distribution, liquid flow rate, fog drop diameter and the like, the fog drops are dried, and salt in the waste water finally forms powdery products. Most of the dry products fall into the bottom end of the drying tower and then are collected and transported, and a small part of the dry products enter a dust remover along with the flue gas for treatment.
When the rotary atomizing nozzle technology is used in the practical application of bypass flue evaporation engineering, the bypass flue evaporation usually adopts a high-temperature bypass flue evaporation atomizing evaporation mode of 'dwarf', a single-machine single-tower design is adopted conventionally, a unit is provided with a dwarf bypass flue evaporation crystallizer, the size of the single evaporation crystallization tower is large, a foundation and a corresponding steel frame are arranged independently in the space to be pulled to the side of the tail flue, and a certain occupied area is needed.
Further, the high-temperature flue gas bypass rotary atomization drying system is provided with a flushing system, flushing before starting and flushing before stopping are completed.
Further, a rinse of about 2-10 minutes is performed every 4-8 hours of operation, as determined by the commissioning.
Further, the high-temperature flue gas bypass rotary atomization drying system is provided with a compressed air purging system, so that the blockage risk is reduced.
Further, the high-temperature flue gas bypass rotary atomization drying system is provided with an oil tank and an oil filtering device.
Furthermore, the high-temperature flue gas bypass rotary atomization drying system is provided with cooling water, and pure water (namely desalted water) is used as the cooling water.
Further, the rotating speed of the rotary high-speed rotary atomizer is more than 15000 revolutions/min.
Further, the flow rate of the wastewater entering the atomizer is more than or equal to 1.4m/s and less than or equal to 2.5m/s.
The specific flow of the improvement of the invention is as follows:
1. adjusting the desulfurization wastewater cyclone to reduce solid particles entering the existing triple box system, wherein the accumulated solid particles of the desulfurization system are taken away by gypsum;
2. the addition of lime slurry is canceled, the lime slurry is not added, the entry of solid impurities is greatly reduced, and the precipitation of salt substances, particularly substances such as magnesium hydroxide and the like, caused by the change of slurry from acidity to alkalinity can be avoided;
3. the organic sulfur dosing is canceled, and is used for removing heavy metal which is not thoroughly added by the removed heavy metal after the lime slurry is dosed, and no wastewater is discharged after zero emission, so that the addition is not needed;
4. according to the water quality condition, the adding amount of the flocculating agent and the coagulant aid is adjusted, so that the turbidity of the effluent is reduced.
5. In order to ensure the stable operation of the sludge system, the filter cloth of the frame filter press is forcedly replaced for 3 months, so that the filtering effect is improved;
6. in order to ensure the turbidity of the effluent, a self-cleaning filter is arranged for filtering to remove residual hard particles; liquid alkali dosing is arranged, and sodium hydroxide solution is adopted to reduce the generation of a precipitated substrate; the stainless steel Y-shaped filter of 2205 is arranged on the wastewater conveying pump, so that subsequent equipment is protected, and cleaning is convenient.
The invention has the beneficial effects that: according to the current situation of the coal-fired power plant, the built system of the power plant is utilized as much as possible to carry out system coupling, so that repeated investment is avoided, the stable operation is the first requirement, and the zero emission of desulfurization wastewater of the coal-fired power plant is realized according to local conditions.
Drawings
FIG. 1, a flow chart of the present invention;
Detailed Description
The present invention is further illustrated in the following drawings and detailed description, which are to be understood as being merely illustrative of the invention and not limiting the scope of the invention. It should be noted that the words "front", "rear", "left", "right", "upper" and "lower" used in the following description refer to directions in the drawings, and the words "inner" and "outer" refer to directions toward or away from, respectively, the geometric center of a particular component.
Comparison of three desulfurization wastewater comprehensive treatment processes
Note that: the price of standard coal is 1000 yuan/ton, and the electricity price is 0.4 yuan/kW
As can be seen from the comparative analysis of the table above: all three processes can meet the purpose of zero emission of desulfurization wastewater.
From the analysis of the disposable investment, the scheme has the lowest investment and the scheme has the highest investment; according to analysis of operation cost, the spray drying of the high-temperature flue gas is the highest, and the low-temperature flash evaporation is the lowest; the scheme is the simplest from the operation and maintenance; according to the influence analysis of solid salt entering the fly ash, the scheme II and the scheme I solidify salt entering the fly ash, so that the utilization and sales of the fly ash of a power plant can be influenced, the scheme I solid salt can be sold independently, the utilization and sales of the existing fly ash are not influenced, and the sales of the scheme I solid salt is difficult.
Desulfurization waste water such as 5m in average discharge amount is considered in consideration of low load rate of power plant 3 Considering/h, the scheme has 150w more than the two-year running cost of the scheme, and does not consider financial cost, and compared with the scheme, if the scheme is adopted for 10 years, the scheme can recover redundant investment and comprehensively consider, so that the scheme is very suitable for the built power plants, especially power plants with the power of 330MW and below, or has short construction period and rapidly influences the local environmental protection policy.
Specific construction parameters:
at full load, each furnace was charged with about 44000Nm from the inlet of the denitration outlet air preheater 3 And (3) flue gas/h, wherein an inlet baffle is arranged on the drying tower to adjust the flue gas amount, and the flue gas uniformly enters the tower through a tower top flue gas distributor in a rotational flow manner (the flue gas flow field can be flexibly adjusted according to the condition of the flow field in the tower to fill the whole drying tower, so that the contact time of the flue gas and liquid drops is increased, and the like). After the desulfurization wastewater is quenched and clarified by the triple box, the desulfurization wastewater enters a wastewater box for buffering, and when the desulfurization wastewater is sent to an atomizing disk rotating at a high speed in a tower by a lifting pump, the wastewater is stretched into a film or pulled into filaments (depending on the rotating speed and the slurry amount) due to the effect of centrifugal force, and the wastewater is broken and dispersed into liquid drops at the edge of the atomizing disk and is fully mixed with hot flue gas of a boiler. The desulfurization waste water containing soluble and suspended solid particles is evaporated under high-temperature flue gas, and the outlet temperature of the evaporation tower is 150-160 ℃. The evaporated solid entrainment matter part enters the front main flue of the electric dust collector together with the flue gas, is trapped by the electric dust collector, is mixed with fly ash of the whole plant, and part of the solid entrainment matter part flows into the bottom of the drying tower to be pumped into an ash pipe of a first electric field of the electric dust collector through a bin pump or is mixed with a slag system.
List of main devices:
the technical means disclosed by the scheme of the invention is not limited to the technical means disclosed by the embodiment, and also comprises the technical scheme formed by any combination of the technical features.
Claims (10)
1. The zero-emission evaporating treatment process for the desulfurization wastewater of the coal-fired power plant comprises a desulfurization wastewater cyclone, a neutralization tank, a settling tank, a slurry clarifying tank and a water outlet tank which are sequentially connected, wherein the discharge end of the water outlet tank is connected with a water outlet conveying pump; sludge in the slurry clarifying tank is discharged through a plate-and-frame filter press, and is characterized in that: the device also comprises a self-cleaning filter, a buffer tank, a wastewater conveying pump and a rotary atomizer; filtering by a self-cleaning filter to remove residual hard particles; the water outlet section filtered by the self-cleaning filter is connected with a buffer tank, the buffer tank is used for adding liquid alkali, and a sodium hydroxide solution is adopted to reduce the generation of suspended matters; one end of the buffer tank is connected with a waste water conveying pump, a stainless steel Y-shaped filter is arranged on the waste water conveying pump, high-temperature flue gas generated by the boiler air preheater is conveyed into the rotary atomizer, a bottom outlet of the rotary atomizer is connected with a flue gas outlet of the boiler air preheater, and a cold air inlet is arranged at the bottom of the boiler air preheater.
2. The zero-emission evaporation-drying treatment process for desulfurization wastewater of a coal-fired power plant according to claim 1, which is characterized in that: the existing triple box treatment equipment is utilized, the operation mode of the suspended matters is changed for the purpose of removing the suspended matters, the desulfurization wastewater cyclone is adjusted, and the entry of solid particles is reduced; the addition of lime slurry is canceled, and the entry of impurities and the precipitation of salts are reduced; the organic sulfur dosing is canceled; the adding amount of the flocculating agent and the coagulant aid is adjusted, so that the turbidity of the effluent is reduced; the filter cloth of the frame filter press is forcedly replaced every three months; and a self-cleaning filter is arranged for filtering to remove residual hard particles.
3. The zero-emission evaporation-drying treatment process for desulfurization wastewater of a coal-fired power plant according to claim 1, which is characterized in that: the atomizing disk is made of hastelloy C276, wherein the part contacted with the wastewater is made of tungsten carbide, corrosion resistance and wear resistance in the actual operation process are considered, and impurities in the wastewater and dried salt are prevented from wearing out the nozzle of the atomizing disk too fast.
4. The zero-emission evaporation-drying treatment process for desulfurization wastewater of a coal-fired power plant according to claim 1, which is characterized in that: the high-temperature flue gas bypass rotary atomization drying system is provided with a flushing system, flushing before starting and flushing before stopping are completed.
5. The zero-emission evaporation-drying treatment process for desulfurization wastewater of a coal-fired power plant according to claim 4, which is characterized in that: a rinse of about 2-10 minutes is performed every 4-8 hours of operation, as determined by the commissioning.
6. The zero-emission evaporation-drying treatment process for desulfurization wastewater of a coal-fired power plant according to claim 1, which is characterized in that: the high-temperature flue gas bypass rotary atomization drying system is provided with a compressed air purging system.
7. The zero-emission evaporation-drying treatment process for desulfurization wastewater of a coal-fired power plant according to claim 1, which is characterized in that: the high-temperature flue gas bypass rotary atomization drying system is provided with an oil tank and an oil filtering device.
8. The zero-emission evaporation-drying treatment process for desulfurization wastewater of a coal-fired power plant according to claim 1, which is characterized in that: the high-temperature flue gas bypass rotary atomization drying system is provided with cooling water, and pure water (namely desalted water) is used as the cooling water.
9. The zero-emission evaporation-drying treatment process for desulfurization wastewater of a coal-fired power plant according to claim 1, which is characterized in that: the rotating speed of the rotary high-speed rotary atomizer is more than 15000 revolutions/min.
10. The zero-emission evaporation-drying treatment process for desulfurization wastewater of a coal-fired power plant according to claim 1, which is characterized in that: the flow rate of the wastewater entering the atomizer is 1.4. 1.4 m/s.ltoreq.V.ltoreq.2.5 m/s.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311614060.8A CN117700008A (en) | 2023-11-29 | 2023-11-29 | Zero-emission evaporating treatment process for desulfurization wastewater of coal-fired power plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311614060.8A CN117700008A (en) | 2023-11-29 | 2023-11-29 | Zero-emission evaporating treatment process for desulfurization wastewater of coal-fired power plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN117700008A true CN117700008A (en) | 2024-03-15 |
Family
ID=90161517
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202311614060.8A Pending CN117700008A (en) | 2023-11-29 | 2023-11-29 | Zero-emission evaporating treatment process for desulfurization wastewater of coal-fired power plant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN117700008A (en) |
-
2023
- 2023-11-29 CN CN202311614060.8A patent/CN117700008A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107032428B (en) | System and method for zero emission treatment of undersaturated flue gas concentration crystallization desulfurization wastewater | |
| CN209974506U (en) | Wet flue gas desulfurization waste water concentration decrement system | |
| CN106630358A (en) | Zero-release coupling humidifying dust-removing synergizing system and method for desulfurization wastewater | |
| CN107129094A (en) | The Zero discharging system of desulfurization wastewater is evaporated based on multi-heat source | |
| CN110723858A (en) | Desulfurization wastewater zero-discharge treatment system and treatment process | |
| CN111908696A (en) | Zero-discharge system and method for flue gas and water co-treatment of desulfurization wastewater | |
| CN208008493U (en) | A kind of equipment that flue residue heat is used for Waste Water From Fire Power Plant zero discharge treatment | |
| CN107857321B (en) | Process for zero discharge treatment of wastewater of thermal power plant | |
| CN105668669A (en) | Desulfurization waste water treatment system and process for power plant | |
| CN206109121U (en) | Desulfurization waste water flue evaporation recovery processing device | |
| CN108529808A (en) | A kind of desulfurization wastewater treatment system and technique | |
| CN211367297U (en) | Desulfurization waste water zero release processing system | |
| CN109485114A (en) | A kind of processing unit and method of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling | |
| CN113501612A (en) | Energy-concerving and environment-protective type desulfurization waste water zero release processing system | |
| CN106517628A (en) | Desulfurization-wastewater zero discharging device for coal-fired power plant | |
| CN107176742A (en) | A kind of desulfurization wastewater rotational flow dust-removing method | |
| CN107827306A (en) | A kind of thermal power plant desulfurization wastewater zero-discharge treatment system | |
| CN108557930B (en) | The method comprises the following steps of: waste water from power plants processing device and method | |
| CN111320315A (en) | Desulfurization wastewater treatment system | |
| CN208857076U (en) | A kind of desulfurization wastewater treatment system | |
| CN112429901A (en) | Desulfurization waste water zero discharge system of low temperature flue gas concentration decrement and evaporation of double fluid bypass flue | |
| CN103482810B (en) | Novel system and method for zero emission treatment of high-salinity heavy metal wastewater | |
| CN207877490U (en) | A kind of thermal power plant desulfurization wastewater zero-discharge treatment system | |
| CN108793557B (en) | Desulfurization wastewater bypass flue evaporation treatment process and system | |
| CN117700008A (en) | Zero-emission evaporating treatment process for desulfurization wastewater of coal-fired power plant |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |