CN111807591B - Method and system for curing mixed salt of high-salt wastewater of power plant - Google Patents
Method and system for curing mixed salt of high-salt wastewater of power plant Download PDFInfo
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- CN111807591B CN111807591B CN202010488021.8A CN202010488021A CN111807591B CN 111807591 B CN111807591 B CN 111807591B CN 202010488021 A CN202010488021 A CN 202010488021A CN 111807591 B CN111807591 B CN 111807591B
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- 239000002351 wastewater Substances 0.000 title claims abstract description 99
- 150000003839 salts Chemical class 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000001704 evaporation Methods 0.000 claims abstract description 104
- 230000008020 evaporation Effects 0.000 claims abstract description 102
- 238000001035 drying Methods 0.000 claims abstract description 59
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 56
- 239000012452 mother liquor Substances 0.000 claims abstract description 41
- 239000000428 dust Substances 0.000 claims abstract description 37
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000003546 flue gas Substances 0.000 claims abstract description 35
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 26
- 239000002245 particle Substances 0.000 claims abstract description 25
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 claims abstract description 25
- 235000019353 potassium silicate Nutrition 0.000 claims abstract description 24
- 239000010881 fly ash Substances 0.000 claims abstract description 18
- 239000000945 filler Substances 0.000 claims abstract description 15
- 239000002002 slurry Substances 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims abstract description 12
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 5
- 238000001723 curing Methods 0.000 claims description 54
- 239000003638 chemical reducing agent Substances 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 13
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 claims description 12
- 239000002893 slag Substances 0.000 claims description 12
- 229910001388 sodium aluminate Inorganic materials 0.000 claims description 12
- 238000005507 spraying Methods 0.000 claims description 11
- 238000000889 atomisation Methods 0.000 claims description 9
- 239000012717 electrostatic precipitator Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 8
- 239000011449 brick Substances 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 7
- 238000009287 sand filtration Methods 0.000 claims description 7
- 239000004576 sand Substances 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 2
- 238000000465 moulding Methods 0.000 abstract description 6
- 239000002918 waste heat Substances 0.000 abstract description 4
- 238000006477 desulfuration reaction Methods 0.000 description 13
- 230000023556 desulfurization Effects 0.000 description 13
- 230000008023 solidification Effects 0.000 description 6
- 238000007711 solidification Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 4
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- -1 Cl) - Corrosion) Chemical class 0.000 description 1
- 239000004115 Sodium Silicate Substances 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 229940059864 chlorine containing product ectoparasiticides Drugs 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 229920000876 geopolymer Polymers 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000000265 homogenisation Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910052911 sodium silicate Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
-
- 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
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B28/00—Compositions of mortars, concrete or artificial stone, containing inorganic binders or the reaction product of an inorganic and an organic binder, e.g. polycarboxylate cements
- C04B28/24—Compositions of mortars, concrete or artificial stone, containing inorganic binders or the reaction product of an inorganic and an organic binder, e.g. polycarboxylate cements containing alkyl, ammonium or metal silicates; containing silica sols
- C04B28/26—Silicates of the alkali metals
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
-
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Ceramic Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention provides a method and a system for solidifying high-salt wastewater and mixed salt of a power plant, wherein the method comprises a desulfurizing tower, a high-salt wastewater collecting tank, a flue heat exchange system, a flash evaporation mother liquor collecting box, a bypass flue drying system, a dust remover and an evaporation product solidifying system which are sequentially connected, wastewater discharged from the desulfurizing tower and reverse osmosis concentrated water of the power plant are filtered and heated and then enter the flash evaporation system, flash evaporation mother liquor A enters the bypass flue drying system to separate particles B and products C, a slurry F is formed by the flash evaporation mother liquor A, a filler D and a water glass solution E, and a solidified body is obtained after molding and curing. The invention designs a method and a system for solidifying high-salt wastewater mixed salt of a power plant for avoiding potential risks existing in flue evaporation, which fully utilize the waste heat of flue gas after a dust removal system, flash-gas the high-salt wastewater, exchange heat between flash-gas mother liquor and the flue gas in a drying tower, solidify products after dust removal, and avoid potential secondary pollution caused by entering mixed salt in the high-salt wastewater into fly ash.
Description
Technical Field
The invention relates to the technical field of industrial wastewater treatment, in particular to a method and a system for curing mixed salt of high-salt wastewater of a power plant.
Background
The high-salt wastewater of the coal-fired power plant mainly comes from tail end wastewater after cascade utilization, such as reverse osmosis concentrated water, circulating sewage, desulfurization wastewater and the like. High-salt wastewater has high salt content, high discharge capacity and corrosiveness to metals (such as Cl) - Corrosion), and the like, the direct discharge can cause serious harm to the ecological environment, the zero discharge becomes the focus of attention in the industry, and the treatment difficulty is higher than that of common industrial wastewater.
The prior desulfurization wastewater zero discharge method mainly comprises evaporation pond treatment, pretreatment, membrane concentration, evaporation crystallization, direct evaporation of a flue, evaporation of a bypass flue and the like. The evaporation pond has lower treatment cost, but the treatment effect is greatly limited by wind speed, wastewater concentration and water environment, and has wind loss and great influence on the surrounding environment. The pretreatment, membrane concentration and evaporative crystallization technology can realize the recycling of crystallized salt, but the treatment process is long, the one-time investment is large, and the pretreatment and dosing cost is high. The flue direct evaporation technology has the advantages that the content of smoke dust in the flue is large, so that fly ash deposition is caused, the atomized desulfurization wastewater needs a flue with a certain length for evaporation crystallization, the actual boiler flue is shorter, the flue cannot be completely evaporated, the flue is corroded, the pressure of a dust remover is greatly increased, and the boiler efficiency is affected to a certain extent. The flue gas bypass treatment device is extremely easy to cause wall sticking because high ash content flue gas is independently introduced as a evaporating heat source of desulfurization wastewater, so that the operation of a drying tower cannot be normally carried out, the service life of equipment is influenced, and if hot air of an air preheater is independently adopted as the evaporating heat source, compared with hot flue gas, the boiler efficiency is greatly influenced.
The flue gas evaporation zero emission technology directly utilizes the waste heat of flue gas to realize zero emission of desulfurization waste water, has simple technology and lower cost, is a favored zero emission technology at present, and is reported by the environmental protection agency of the United states, the potential risk caused by evaporation of the flue of the desulfurization waste water is that the characteristics of fly ash can be changed when evaporation products are mixed into the fly ash, and the comprehensive utilization of the fly ash is influenced; chlorine-containing products cannot be completely trapped by the dust remover, and corrosion of the dust remover and a flue can be increased, so that operation and maintenance costs are increased. Thus, there is a need for separate treatment of flue gas vaporization products that reduces the hazard to the overall system.
Disclosure of Invention
The invention designs a method and a system for solidifying mixed salt of high-salt wastewater in a power plant aiming at the treatment of a flue gas evaporation product, which fully utilize the waste heat of flue gas after a dust removal system, flash-gas the high-salt wastewater, exchange heat between flash-gas mother liquor and the flue gas in a drying tower, solidify the product after dust removal, and avoid potential secondary pollution caused by the mixed salt in the high-salt wastewater entering fly ash.
The invention provides a method for solidifying mixed salt of high-salt wastewater of a power plant, which comprises the following steps:
s1, wastewater discharged from a desulfurizing tower and reverse osmosis concentrated water of a power plant enter a high-salt wastewater collection tank and then enter a sand filtration system to be filtered to remove suspended matters;
s2, the filtered high-salt wastewater enters a flue heat exchange system, and the high-salt wastewater is heated to 70-80 ℃ through heat exchange with flue gas in a flue of a desulfurizing tower;
s3, the heated high-salt wastewater enters a flash evaporation system, is sprayed into a flash evaporation tank body through a spraying device, steam sequentially enters a liquid drop separation device and a steam condensing device through a steam outlet, and liquid which is not evaporated falls into a water tank to obtain flash evaporation mother liquor A and flows into a flash evaporation mother liquor collecting box;
s4, enabling flash evaporation mother liquor A flowing out of a flash evaporation mother liquor collecting box to enter a bypass flue drying system, spraying the flash evaporation mother liquor A into a drying tower through a rotary atomization device, fully exchanging heat with high-temperature flue gas in the drying tower to obtain a drying product and hot gas, separating particles B from the drying product through a cyclone separator, and capturing dust in the hot gas by a dust remover to obtain a product C;
s5, putting the particles B, the products C and the filler D into a homogenizing device, uniformly stirring, and then adding the water glass solution E to form slurry F;
s6, pouring the slurry F into a forming device for forming, and standing for 24-48 hours at room temperature to obtain a formed body;
s7, placing the formed body obtained in the S6 into a curing device for curing to obtain a cured body which can be used as a pavement brick.
The invention relates to a curing method for mixed salt of high-salt wastewater of a power plant, which is characterized in that the curing conditions in the step S7 are as follows: the temperature is 40-60 ℃, the humidity is 80-90%, and the curing time is 28 days.
According to the method for solidifying the mixed salt of the high-salt wastewater of the power plant, in the step S5, the filler D comprises blast furnace slag, fly ash, sodium aluminate and a water reducer, wherein the sum of the particles B and the product C, the blast furnace slag, the fly ash, the sodium aluminate and the water reducer are prepared by the following components in percentage by mass: 10% -20%, 40% -60%, 20% -30%, 8% -15% and 1% -5% of the components.
The invention relates to a method for curing mixed salt of high-salt wastewater in a power plant, which is characterized in that the water reducer is a polycarboxylic acid high-performance water reducer as an optimal mode.
According to the method for curing the mixed salt of the high-salt wastewater of the power plant, in the preferred mode, the mass percentage of the sum of the particles B, the products C and the filler D in the step S5 to the water glass solution E is 100: (20-40), the modulus of the water glass solution E is 1.2-1.8, and the SiO is 2 The mass fraction of (2) is 15-20%.
The invention provides a mixed salt solidifying system for high-salt wastewater of a power plant, which is used as a preferable mode and comprises a desulfurizing tower, a high-salt wastewater collecting tank, a flue heat exchange system, a flash evaporation mother liquor collecting box, a bypass flue drying system, a dust remover and an evaporation product solidifying system arranged at one side of an outlet of the dust remover, which are connected in sequence;
the bypass flue drying system comprises a drying tower, a rotary atomization device which is arranged at the inner top of the drying tower and connected with a flash evaporation mother liquor collecting box, a cyclone separator which is arranged at the bottom of the drying tower, and a high-temperature flue gas inlet which is arranged at the upper part of the drying tower, wherein an outlet of the cyclone separator is connected with a dust remover;
the evaporation product curing system comprises a homogenizing device, a forming device and a curing device which are sequentially arranged, and is used for homogenizing, forming and curing the granules B, the products C, the fillers D and the water glass solution E.
According to the high-salt wastewater mixed salt solidification system for the power plant, as an optimal mode, a sand filtering system is connected between a high-salt wastewater collection tank and a flue heat exchange system.
According to the high-salt wastewater mixed salt curing system for the power plant, as a preferable mode, the main flue at the front end of the desulfurizing tower is sequentially connected with the electrostatic precipitator and the air preheater, the flue heat exchange system is arranged on the main flue between the desulfurizing tower and the electrostatic precipitator, the high-temperature flue gas inlet is connected with the main flue at the front end of the air preheater, and the air outlet of the precipitator is connected with the main flue between the electrostatic precipitator and the air preheater.
The invention relates to a high-salt wastewater mixed salt curing system for a power plant, which is characterized in that a flue heat exchange system comprises a water inlet pipe, a heat exchange component and a water outlet pipe which are sequentially connected, wherein the water inlet pipe is connected with an outlet of a sand filtration system, the heat exchange component is arranged in a main flue of a desulfurizing tower, and the water outlet pipe is connected with an inlet of a flash evaporation system.
The invention relates to a high-salt wastewater mixed salt solidification system for a power plant, which is used for solving the problems that the high-salt wastewater mixed salt solidification system is difficult to realize and the like in the prior art.
The high-salt wastewater is filtered by a sand filtering system, then enters a flash evaporation system after being heated by a flue, and is recovered by a steam condensing device, the wastewater is sprayed into a flash evaporation tank in a mist or liquid drop state, the wastewater is evaporated and cooled in the process, the part which is not flashed falls into a bottom water tank, and flash evaporation mother liquor in the bottom water tank enters a mother liquor collecting box. The bypass flue drying system extracts high-temperature flue gas after denitration and before the air preheater, and the flue gas purification device comprises a drying tower and a dust remover, wherein the upper part of the drying tower is provided with a flue gas inlet, the lower part of the drying tower is provided with a flue gas outlet, the top end of the drying tower is provided with a rotary atomizing device, the bottom of the drying tower is provided with a cyclone separator, the flue gas outlet is connected with the dust remover, and the flue gas after dust removal returns to a main flue after the air preheater. The evaporated product collected by the dust collector enters a curing system, and the evaporated product curing system comprises a homogenizing device, a forming device and a curing device.
The compressive strength of the cured body obtained by the method is more than 30MPa, and the dissolution rate of chloride ions is less than 10 percent, so that the cured body is used for pavement bricks.
The invention has the following advantages:
(1) The waste heat of the flue gas after the dust removal system is fully utilized, the temperature of the flue gas entering the desulfurizing tower is reduced while the high-salt wastewater is heated, and the evaporation capacity of the desulfurizing system is reduced, so that the emission of the desulfurizing wastewater is reduced from the source;
(2) Sand filtering is carried out before the high-salt wastewater enters the flue heat exchange system, so that suspended matters in the high-salt wastewater are effectively removed, deposition and scaling of the high-salt wastewater on the surface of the heat exchanger are reduced, and stable operation of the heat exchange system is facilitated;
(3) The flash evaporation system is utilized to recycle precious fresh water resources, so that the waste of the water resources is reduced;
(4) The dry product of the bypass flue drying system is mainly mixed salt and heavy metal ions in high-salt wastewater, the mixed salt and heavy metal ions in the high-salt wastewater are solidified by adopting the principle of geopolymer, a stable solidified body is formed, secondary potential hazards of the mixed salt and the heavy metal ions can be effectively avoided, and the formed solidified body can be used as a pavement brick;
(5) In the whole high-salt wastewater zero-emission system, chemical adding treatment is not needed, and the cost of high-salt wastewater zero-emission is effectively reduced.
Drawings
FIG. 1 is a schematic diagram of a method for curing mixed salt in high-salt wastewater of a power plant;
FIG. 2 is a schematic diagram-1 of a system for curing mixed salt in high-salt wastewater of a power plant;
FIG. 3 is a schematic diagram-2 of a system for curing mixed salt in high-salt wastewater of a power plant;
FIG. 4 is a schematic diagram of a flue heat exchange system for a high salt wastewater salt-water curing system of a power plant;
FIG. 5 is a schematic diagram of a flash vaporization system for a high salt wastewater salt-rejection solidification system of a power plant;
FIG. 6 is a schematic diagram of a bypass flue drying system for a high salt wastewater salt-mixed curing system of a power plant;
FIG. 7 is a schematic diagram of an evaporation product curing system for a high salt wastewater salt-impurity curing system of a power plant.
Reference numerals:
1. a desulfurizing tower; 2. a high-salt wastewater collection tank; 3. a flue heat exchange system; 31. a water inlet pipe; 32. a heat exchange assembly; 33. a water outlet pipe; 4. a flash vaporization system; 41. a flash tank body; 42. A flash tank inlet; 43. a spraying device; 44. a steam outlet; 45. a droplet separator; 46. a steam condensing device; 47. a water tank; 5. flash evaporation mother liquor collecting box; 6. a bypass flue drying system; 61. a drying tower; 62. a rotary atomizing device; 63. a cyclone separator; 64. a high temperature flue gas inlet; 7. a dust remover; 8. an evaporation product curing system; 81. a homogenizing device; 82. a molding device; 83. a curing device; 9. a sand filtration system; 10. an electrostatic precipitator; 11. an air preheater.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments.
Example 1
As shown in FIG. 1, the invention provides a method for solidifying mixed salt of high-salt wastewater of a power plant, which comprises the following steps:
s1, wastewater discharged from a desulfurizing tower 1 and reverse osmosis concentrated water of a power plant enter a high-salt wastewater collection tank 2 and then enter a sand filtration system 9 to be filtered to remove suspended matters;
s2, the filtered high-salt wastewater enters a flue heat exchange system 3, and the high-salt wastewater is heated to 70-80 ℃ through heat exchange with flue gas in a flue of the desulfurizing tower 1;
s3, the heated high-salt wastewater enters a flash evaporation system 4, is sprayed into a flash evaporation tank body 41 through a spraying device 43, steam sequentially enters a liquid drop separation device 45 and a steam condensing device 46 through a steam outlet 44, liquid which is not evaporated falls into a water tank 47, the flash evaporation system 4 concentrates the high-salt wastewater by 3-5 times to obtain flash evaporation mother liquor A, and flows into a flash evaporation mother liquor collecting box 5;
s4, enabling flash evaporation mother liquor A flowing out of a flash evaporation mother liquor collecting box 5 to enter a bypass flue drying system 6, spraying the flash evaporation mother liquor A into a drying tower 61 through a rotary atomization device 62, and performing full heat exchange with high-temperature flue gas in the drying tower 61 to obtain a drying product and hot gas, separating particles B from the drying product through a cyclone separator 63, and collecting dust in the hot gas by a dust remover 7 to obtain a product C;
s5, putting the particles B, the product C and the filler D into a homogenizing device 81, uniformly stirring, and then adding a water glass solution E to form slurry F;
s6, pouring the slurry F into a forming device 82 for forming, and standing for 24-48 hours at room temperature to obtain a formed body;
s7, placing the formed body obtained in the S6 into a curing device 83 for curing to obtain a cured body which can be used as a pavement brick.
Example 2
The composition of desulfurization wastewater from a power plant is shown in the following table:
| project | Quantity of |
| Ca 2+ (mg/L) | 850 |
| Mg 2+ (mg/L) | 650 |
| Cl - (mg/L) | 13000 |
| SO 4 2- (mg/L) | 6700 |
As shown in FIG. 1, the invention provides a method for solidifying mixed salt of high-salt wastewater of a power plant, which comprises the following steps:
s1, wastewater discharged from a desulfurizing tower 1 enters a high-salt wastewater collecting tank 2 and then enters a sand filtering system 9 to be filtered to remove suspended matters;
s2, the filtered desulfurization wastewater enters a flue heat exchange system 3, and the desulfurization wastewater is heated to 70-80 ℃ through heat exchange with flue gas in a flue of the desulfurization tower 1;
s3, the heated desulfurization wastewater enters a flash evaporation system 4, the heated desulfurization wastewater is sprayed into a flash evaporation tank body 41 through a spraying device 43, steam sequentially enters a liquid drop separation device 45 and a steam condensing device 46 through a steam outlet 44, liquid which is not evaporated falls into a water tank 47, the desulfurization wastewater is concentrated by 3-5 times by the flash evaporation system 4, a flash evaporation mother liquor A is obtained, and the flash evaporation mother liquor A flows into a flash evaporation mother liquor collecting box 5;
s4, enabling flash evaporation mother liquor A flowing out of a flash evaporation mother liquor collecting box 5 to enter a bypass flue drying system 6, spraying the flash evaporation mother liquor A into a drying tower 61 through a rotary atomization device 62, enabling the atomization particle size of the rotary atomization device 62 to be 30-100 mu m, fully exchanging heat with high-temperature flue gas in the drying tower 61 to obtain a drying product and hot gas, separating particles B from the drying product through a cyclone separator 63, and capturing dust in the hot gas by a dust remover 7 to obtain a product C;
s5, putting the particles B, the product C and the filler D into a homogenizing device 81, uniformly stirring, and then adding a water glass solution E to form slurry F;
the filler D comprises blast furnace slag, fly ash, sodium aluminate and a water reducer, wherein the sum of the particles B and the product C, the blast furnace slag, the fly ash, the sodium aluminate and the water reducer are prepared according to the following mass percent: 10% -20%, 40% -60%, 20% -30%, 8% -15% and 1% -5% of blending;
the water reducer is a polycarboxylic acid high-performance water reducer;
the mass percentage of the sum of the particle B, the product C and the filler D to the water glass solution E is 100: (20-40), the modulus of the water glass solution E is 1.2-1.8, and the SiO is 2 The mass fraction of (2) is 15-20%.
S6, pouring the slurry F into a forming device 82 for forming, and standing for 24-48 hours at room temperature to obtain a formed body;
s7, placing the formed body obtained in the S6 into a curing device 83 for curing to obtain a cured body which can be used as a pavement brick.
The curing conditions in step S7 are: the temperature is 40-60 ℃, the humidity is 80-90%, and the curing time is 28 days.
Example 3
The method for curing the mixed salt of the high-salt wastewater of the power plant is as described in example 2, and the sum of the particles B and the products C, the blast furnace slag, the fly ash, the sodium aluminate and the water reducer are in mass percent: 15%, 50%, 25%, 8%, 2% of the total weight of the mixture are added into a homogenizing device 81, stirred for 3-5min, and then added with water glass solution E with a modulus of 1.4 and SiO 2 The mass fraction of the water glass solution E is 15%, the addition amount of the water glass solution E is 35% of the sum of the mass of the particles B, the mass of the product C, the mass of the blast furnace slag, the mass of the fly ash, the mass of the sodium aluminate and the mass of the water reducing agent, the mixture is stirred again to form uniform slurry F, and a solidified body is obtained after the slurry F is molded and cured, wherein the compressive strength of the solidified body is 40.5MPa, and the dissolution rate of chloride ions is less than 10% and is used for pavement bricks.
Example 4
The method for curing the mixed salt of the high-salt wastewater of the power plant is as described in example 2, and the sum of the particles B and the products C, the blast furnace slag, the fly ash, the sodium aluminate and the water reducer are in mass percent: adding 10%, 60%, 20%, 8%, 2% into homogenizing device 81, stirring for 3-5min, and adding water glassSolution E, sodium silicate solution E having a modulus of 1.8, siO 2 The mass fraction of the water glass solution E is 20 percent, the addition amount of the water glass solution E is 20 percent of the sum of the mass of the particles B, the product C, the blast furnace slag, the fly ash, the sodium aluminate and the water reducing agent, the mixture is stirred again to form uniform slurry F, and the slurry F is molded and cured to obtain a solidified body.
Example 5
The method for curing the mixed salt of the high-salt wastewater of the power plant is as described in example 2, and the sum of the particles B and the products C, the blast furnace slag, the fly ash, the sodium aluminate and the water reducer are in mass percent: adding 20%, 40%, 20%, 15%, 5% into homogenizing device 81, stirring for 3-5min, adding water glass solution E with modulus of 1.2 and SiO 2 The mass fraction of the water glass solution E is 15%, the addition amount of the water glass solution E is 40% of the sum of the mass of the particles B, the mass of the product C, the mass of the blast furnace slag, the mass of the fly ash, the mass of the sodium aluminate and the mass of the water reducer, the water glass solution E is stirred again to form uniform slurry F, and the slurry F is molded and cured to obtain a solidified body.
Example 6
As shown in fig. 2, the present invention provides a high-salt wastewater mixed salt solidification system for a power plant, which is characterized in that: the device comprises a desulfurizing tower 1, a high-salt wastewater collecting tank 2, a flue heat exchange system 3, a flash evaporation system 4, a flash evaporation mother liquor collecting box 5, a bypass flue drying system 6, a dust remover 7 and an evaporation product solidifying system 8 which are sequentially connected with each other, wherein the evaporation product solidifying system is arranged at one side of an outlet of the dust remover 7.
The bypass flue drying system 6 comprises a drying tower 61, a rotary atomization device 62 which is arranged at the inner top of the drying tower 61 and connected with the flash mother liquor collecting box 5, a cyclone separator 63 which is arranged at the bottom of the drying tower 61, and a high-temperature flue gas inlet 64 which is arranged at the upper part of the drying tower 61, wherein the outlet of the cyclone separator 63 is connected with a dust remover 7;
the evaporation product curing system 8 includes a homogenizing device 81, a molding device 82, and a curing device 83, which are placed in this order, and the evaporation product curing system 8 is used for homogenizing, molding, and curing the particles B, the product C, the filler D, and the water glass solution E.
Example 7
As shown in fig. 3, the present invention provides a high-salt wastewater mixed salt solidification system for a power plant, which is characterized in that: the device comprises a desulfurizing tower 1, a high-salt wastewater collecting tank 2, a flue heat exchange system 3, a flash evaporation system 4, a flash evaporation mother liquor collecting box 5, a bypass flue drying system 6, a dust remover 7 and an evaporation product solidifying system 8 which are sequentially connected with each other, wherein the evaporation product solidifying system is arranged at one side of an outlet of the dust remover 7.
Between the high-salt wastewater collection tank 2 and the flue heat exchange system 3, a sand filtration system 9 is connected.
As shown in fig. 4, the flue heat exchange system 3 comprises a water inlet pipe 31, a heat exchange component 32 and a water outlet pipe 33 which are sequentially connected, the water inlet pipe 31 is connected with the outlet of the sand filtration system 7, the heat exchange component 32 is arranged in the main flue of the desulfurizing tower 1, and the water outlet pipe 33 is connected with the inlet of the flash evaporation system 4.
As shown in fig. 5, the flash evaporation system 4 comprises a flash evaporation tank 41, a flash evaporation tank inlet 42 connected with the water outlet pipe 33 and arranged on the upper side surface of the flash evaporation tank 41, a spraying device 43 connected with the flash evaporation tank inlet 42 and arranged on the upper inner side of the flash evaporation tank 41, a steam outlet 44 arranged on the upper side surface of the flash evaporation tank 41, a liquid drop separation device 45 connected with the steam outlet 44, a steam condensing device 46 connected with the steam outlet of the liquid drop separation device 45 and a water tank 47 arranged at the inner bottom of the flash evaporation tank 41, wherein the water tank is used for containing flash evaporation mother liquor a, and the outlet of the water tank 47 is connected with the inlet of the flash evaporation mother liquor collecting box 5.
As shown in fig. 6, the bypass flue drying system 6 comprises a drying tower 61, a rotary atomizing device 62 arranged at the top of the drying tower 61 and connected with the flash mother liquor collecting box 5, a cyclone 63 arranged at the bottom of the drying tower 61, and a high-temperature flue gas inlet 64 arranged at the upper part of the drying tower 61, wherein the outlet of the cyclone 63 is connected with a dust remover 7;
as shown in fig. 7, the evaporation product curing system 8 includes a homogenizing device 81, a molding device 82, and a curing device 83 placed in this order, and the evaporation product curing system 8 is used for homogenization, molding, and curing of the particles B, the product C, the filler D, and the water glass solution E.
The main flue at the front end of the desulfurizing tower 1 is sequentially connected with the electrostatic precipitator 10 and the air preheater 11, the flue heat exchange system 3 is arranged on the main flue between the desulfurizing tower 1 and the electrostatic precipitator 10, the high-temperature flue gas inlet 64 is connected with the main flue at the front end of the air preheater 11, and the air outlet of the dust remover 7 is connected with the main flue between the electrostatic precipitator 10 and the air preheater 11.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (7)
1. A method for solidifying mixed salt of high-salt wastewater in a power plant is characterized by comprising the following steps: the method comprises the following steps:
s1, desulfurizing wastewater discharged by a desulfurizing tower (1) and reverse osmosis concentrated water of a power plant enter a high-salt wastewater collecting tank (2), and then enter a sand filtering system (9) for filtering to remove suspended matters;
s2, the filtered high-salt wastewater enters a flue heat exchange system (3), and the high-salt wastewater is heated to 70-80 ℃ through heat exchange with flue gas in a flue of the desulfurizing tower (1);
s3, the heated high-salt wastewater enters a flash evaporation system (4), is sprayed into a flash evaporation tank body (41) through a spraying device (43), and steam sequentially enters a liquid drop separation device (45) and a steam condensing device (46) through a steam outlet (44), and liquid which is not evaporated falls into a water tank (47) to obtain flash evaporation mother liquor A and flows into a flash evaporation mother liquor collecting box (5);
s4, enabling the flash evaporation mother liquor A flowing out of the flash evaporation mother liquor collecting box (5) to enter a bypass flue drying system (6), spraying the flash evaporation mother liquor A into a drying tower (61) through a rotary atomization device (62), fully exchanging heat with high-temperature flue gas in the drying tower (61) to obtain a drying product and hot gas, separating particles B from the drying product through a cyclone separator (63), and capturing dust in the hot gas by a dust remover (7) to obtain a product C;
s5, placing the particles B, the product C and the filler D into a homogenizing device (81), uniformly stirring, and then adding a water glass solution E to form slurry F;
the filler D comprises blast furnace slag, fly ash, sodium aluminate and a water reducer, wherein the sum of the particles B and the product C, the blast furnace slag, the fly ash, the sodium aluminate and the water reducer are prepared from the following components in percentage by mass: 10% -20%, 40% -60%, 20% -30%, 8% -15% and 1% -5% of blending;
the mass percentage of the sum of the mass of the particles B, the mass of the product C and the mass of the filler D to the mass percentage of the water glass solution E is 100: (20-40), the modulus of the water glass solution E is 1.2-1.8, siO 2 15-20% by mass;
s6, pouring the slurry F into a forming device (82) for forming, and standing for 24-48 hours at room temperature to obtain a formed body;
s7, placing the formed body obtained in the S6 into a curing device (83) for curing to obtain a cured body which can be used as a pavement brick;
the high-salt wastewater mixed salt curing system of the power plant comprises a desulfurizing tower (1), a high-salt wastewater collecting tank (2), a flue heat exchange system (3), a flash evaporation system (4), a flash evaporation mother liquor collecting box (5), a bypass flue drying system (6), a dust remover (7) and an evaporation product curing system (8) which are sequentially connected, wherein the evaporation product curing system is arranged at one side of an outlet of the dust remover (7);
the bypass flue drying system (6) comprises a drying tower (61), a rotary atomization device (62) which is arranged at the inner top of the drying tower (61) and connected with the flash evaporation mother liquor collecting box (5), a cyclone separator (63) which is arranged at the bottom of the drying tower (61) and a high-temperature flue gas inlet (64) which is arranged at the upper part of the drying tower (61), wherein an outlet of the cyclone separator (63) is connected with the dust remover (7);
the evaporation product curing system (8) comprises a homogenizing device (81), a forming device (82) and a curing device (83) which are sequentially arranged, and the evaporation product curing system (8) is used for homogenizing, forming and curing the particles B, the products C, the fillers D and the water glass solution E.
2. The method for solidifying mixed salt of high-salt wastewater in a power plant according to claim 1, which is characterized by comprising the following steps: the curing conditions in the step S7 are as follows: the temperature is 40-60 ℃, the humidity is 80-90%, and the curing time is 28 days.
3. The method for solidifying mixed salt of high-salt wastewater in a power plant according to claim 1, which is characterized by comprising the following steps: the water reducer is a polycarboxylic acid water reducer.
4. The method for solidifying mixed salt of high-salt wastewater in a power plant according to claim 1, which is characterized by comprising the following steps: a sand filtering system (9) is connected between the high-salt wastewater collecting tank (2) and the flue heat exchange system (3).
5. The method for solidifying mixed salt of high-salt wastewater in a power plant according to claim 4, which is characterized by comprising the following steps: the flue heat exchange system (3) is arranged on the main flue between the desulfurizing tower (1) and the electrostatic precipitator (10), the high-temperature flue gas inlet (64) is connected with the main flue at the front end of the air preheater (11), and the air outlet of the dust remover (7) is connected with the main flue between the electrostatic precipitator (10) and the air preheater (11).
6. The method for solidifying mixed salt of high-salt wastewater in a power plant according to claim 5, which is characterized in that: the flue heat exchange system (3) comprises a water inlet pipe (31), a heat exchange assembly (32) and a water outlet pipe (33) which are sequentially connected, wherein the water inlet pipe (31) is connected with an outlet of the sand filtration system (7), the heat exchange assembly (32) is arranged in a main flue of the desulfurizing tower (1), and the water outlet pipe (33) is connected with an inlet of the flash evaporation system (4).
7. The method for solidifying mixed salt of high-salt wastewater in a power plant according to claim 6, which is characterized in that: the flash evaporation system (4) comprises a flash evaporation tank body (41), a flash evaporation tank body inlet (42) which is connected with a water outlet pipe (33) and is arranged on the side surface of the upper portion of the flash evaporation tank body (41), a spraying device (43) which is connected with the flash evaporation tank body inlet (42) and is arranged on the inner upper portion of the flash evaporation tank body (41), a steam outlet (44) which is arranged on the side surface of the upper portion of the flash evaporation tank body (41), a liquid drop separation device (45) which is connected with the steam outlet (44), a steam condensing device (46) which is connected with the steam outlet of the liquid drop separation device (45) and a water tank (47) which is arranged at the inner bottom of the flash evaporation tank body (41), and the water tank (47) is used for containing flash evaporation mother liquor A, and the outlet of the water tank (47) is connected with an inlet of a flash evaporation mother liquor collecting box (5).
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