CN215570471U - High-salinity wastewater treatment system for deacidification tower of rotary kiln incineration system - Google Patents
High-salinity wastewater treatment system for deacidification tower of rotary kiln incineration system Download PDFInfo
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- CN215570471U CN215570471U CN202121454041.XU CN202121454041U CN215570471U CN 215570471 U CN215570471 U CN 215570471U CN 202121454041 U CN202121454041 U CN 202121454041U CN 215570471 U CN215570471 U CN 215570471U
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- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 10
- 238000000926 separation method Methods 0.000 claims abstract description 85
- 238000001704 evaporation Methods 0.000 claims abstract description 83
- 230000008020 evaporation Effects 0.000 claims abstract description 81
- 239000012452 mother liquor Substances 0.000 claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 238000010791 quenching Methods 0.000 claims abstract description 26
- 150000003839 salts Chemical class 0.000 claims abstract description 13
- 239000002562 thickening agent Substances 0.000 claims abstract description 13
- 208000028659 discharge Diseases 0.000 claims description 19
- 230000000171 quenching effect Effects 0.000 claims description 13
- 239000007788 liquid Substances 0.000 abstract description 10
- 125000004122 cyclic group Chemical group 0.000 abstract description 6
- 239000002351 wastewater Substances 0.000 abstract description 6
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 239000007787 solid Substances 0.000 abstract description 2
- 230000009466 transformation Effects 0.000 abstract description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 8
- 239000003546 flue gas Substances 0.000 description 8
- 239000002920 hazardous waste Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000000889 atomisation Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 239000012153 distilled water Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The utility model relates to a high-salt water treatment system of a deacidification tower of a rotary kiln incineration system, belonging to the technical field of high-salt wastewater treatment. The technical scheme is as follows: before entering a quench tower, high-salt wastewater generated by a deacidification tower of a rotary kiln incineration system is treated by a triple-effect evaporator, the recovered condensate water with low salt content enters the quench tower (20) for reuse, and the condensate water with high salt content returns to a three-stage separation chamber (9) for cyclic separation; the high-concentration mother liquor generated at the bottom of the triple-effect evaporator is subjected to concentration increase through the thickener (13), solid-liquid separation is carried out through the centrifuge (14), a solid strong salt product (21) is obtained, and the separated mother liquor enters the mother liquor tank (17) and then returns to the triple-effect evaporator for circulating evaporation. The utility model has the beneficial effects that: the water demand of quench tower equipment is satisfied completely to the comdenstion water, improves the utilization ratio of water resource, reduces the running cost, reduces to discharge secondary pollution, and the transformation investment is little, and the processing cost is low, has realized the zero release and has used multipurposely.
Description
Technical Field
The utility model relates to a high-salinity wastewater treatment system for a deacidification tower of a rotary kiln incineration system, and belongs to the technical field of high-salinity wastewater treatment.
Background
The safety and harmless treatment of the hazardous waste are very important, and the national requirement for the concentrated harmless treatment of the hazardous waste has important significance for effectively controlling pollution sources and strictly preventing secondary pollution. The rotary kiln incineration is one of important means, the in-furnace incineratable hazardous wastes enter the rotary kiln for incineration through different feeding channels, the generated flue gas enters a secondary combustion chamber for secondary incineration, the slag enters a water seal slag conveyor for cooling and then is discharged, and the flue gas enters the secondary combustion chamber for secondary incineration. Flue gas purification processing system includes "exhaust-heat boiler + SNCR denitration + quench tower + dry process deacidification + active carbon adsorption + sack dust removal + wet process deacidification + flue gas heater + draught fan + on-line monitoring system", and the strong brine of discharge not only need handle the back emission in the deacidification system of follow wet process, still can cause the water waste. The prior art adopts a high-salt water treatment mode for a deacidification tower of a rotary kiln incineration system as follows: the quenching tower is used as an evaporator to evaporate high-salinity water, and the following problems are caused: after the high-salt wastewater is sprayed into the quenching tower, water is evaporated instantly, crystals generated by salt in the water are attached to the wall or the bottom of the quenching tower, and a thick layer of salt scale is formed on the wall of the quenching tower for a long time, so that the effective inner diameter of the quenching tower is reduced, the atomization area of the flue gas is reduced, the flow rate of the flue gas is increased, the atomization residence time of the flue gas is reduced, and the flue gas quenching effect is reduced rapidly; because salt crystals and fly ash are mixed and attached to the bottom of the tower to form scale, the difficulty of ash removal and maintenance of equipment is increased.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a high-salinity wastewater treatment system for a deacidification tower of a rotary kiln incineration system, wherein before entering a quenching tower, high-salinity wastewater is treated and recovered by a triple-effect evaporator, condensed water of the triple-effect evaporator is recycled by the quenching tower, so that the water demand of quenching tower equipment can be completely met, the utilization rate of water resources is improved, the operation cost is reduced, the secondary pollution discharge is reduced, the improvement investment is low, the treatment cost is low, and the problems in the background art are solved.
The technical scheme of the utility model is as follows:
a high-salinity wastewater treatment system for a deacidification tower of a rotary kiln incineration system comprises a primary separation chamber, a primary evaporation chamber, a secondary separation chamber, a secondary evaporation chamber, a tertiary separation chamber, a tertiary evaporation chamber, a thickener, a centrifuge, a condenser, a vacuum pump, a mother liquor tank, a mother liquor circulating pump and a quench tower; the high-salt water pipeline is connected with the primary separation chamber, the top of the primary separation chamber is connected with the primary evaporation chamber, the top of the primary evaporation chamber is connected with the secondary separation chamber, and the bottom of the primary evaporation chamber and the bottom of the primary separation chamber are connected with the secondary evaporation chamber together; the top of the second-stage separation chamber is connected with the second-stage evaporation chamber, the top of the second-stage evaporation chamber is connected with the third-stage separation chamber, and the bottom of the second-stage evaporation chamber and the bottom of the second-stage separation chamber are connected with the third-stage evaporation chamber together; the top of the third-stage separation chamber is connected with a third-stage evaporation chamber, and the top of the third-stage evaporation chamber is connected with a quenching tower through a condenser and a vacuum pump; the bottom of the third-stage evaporation chamber and the bottom of the third-stage separation chamber are sequentially connected with the thickener, the centrifuge and the mother liquor tank together, and the mother liquor tank is connected with the third-stage evaporation chamber through a mother liquor circulating pump.
The lower parts of the second-stage separation chamber and the third-stage separation chamber are connected with a condensate tank through pipelines, the bottom of the condenser is also connected with the condensate tank, and the top of the condensate tank is connected with the third-stage separation chamber.
The bottom of the primary evaporation chamber is connected with the bottom of the primary separation chamber through a primary axial-flow pump, and is connected with the secondary evaporation chamber through a primary discharge pump; the bottom of the second-stage evaporation chamber is connected with the bottom of the second-stage separation chamber through a second-stage axial flow pump, and is connected with the third-stage evaporation chamber through a second-stage discharge pump; the bottom of the third-stage evaporation chamber is connected with the bottom of the third-stage separation chamber through a third-stage axial flow pump, and the bottom of the third-stage evaporation chamber is connected with the bottom of the third-stage separation chamber through a third-stage discharge pump.
The separation chamber, the evaporation chamber, the axial-flow pump, the discharge pump, the thickener, the centrifuge, the condenser, the vacuum pump, the mother liquor circulating pump, the quench tower and the like which are related to the utility model are all common equipment known in the field. The separating chamber is a device for separating the mixed substance into two or more different substances, the evaporating chamber is heated under the negative pressure state for gas-liquid separation, and the three evaporating chambers of the utility model form a triple-effect evaporator together.
Before entering a quench tower, high-salinity wastewater generated by a deacidification tower of a rotary kiln incineration system is treated by a three-effect evaporator, the recovered condensate water with low salt content enters the quench tower for recycling, and the condensate water with high salt content returns to a three-stage separation chamber for cyclic separation; the high-concentration mother liquor generated at the bottom of the triple-effect evaporator is subjected to concentration increase through the thickener, solid-liquid separation is performed through the centrifuge to obtain a solid strong salt product, and the separated mother liquor enters the mother liquor tank and then returns to the triple-effect evaporator for cyclic evaporation, so that zero-emission comprehensive utilization is realized.
The utility model has the beneficial effects that: adopt the triple effect evaporimeter to handle the recovery before high salt waste water gets into the quench tower, the comdenstion water of the triple effect evaporimeter of quench tower retrieval and utilization can satisfy the water demand of quench tower equipment completely, improves the utilization ratio of water resource, reduces the running cost, reduces and discharges secondary pollution, and the transformation investment is little, and processing cost is low, has realized the zero release and has used multipurposely.
Drawings
FIG. 1 is a schematic diagram of the system architecture for carrying out the present invention;
in the figure: the device comprises a primary separation chamber 1, a primary evaporation chamber 2, a primary axial-flow pump 3, a primary discharge pump 4, a secondary separation chamber 5, a secondary evaporation chamber 6, a secondary axial-flow pump 7, a secondary discharge pump 8, a tertiary separation chamber 9, a tertiary evaporation chamber 10, a tertiary axial-flow pump 11, a tertiary discharge pump 12, a thickener 13, a centrifuge 14, a condenser 15, a vacuum pump 16, a mother liquor tank 17, a condensate tank 18, a mother liquor circulating pump 19, a quench tower 20 and a strong salt product 21.
Detailed Description
The utility model is further illustrated by the following examples in conjunction with the accompanying drawings.
A high-salinity wastewater treatment system for a deacidification tower of a rotary kiln incineration system comprises a primary separation chamber 1, a primary evaporation chamber 2, a secondary separation chamber 5, a secondary evaporation chamber 6, a tertiary separation chamber 9, a tertiary evaporation chamber 10, a thickener 13, a centrifuge 14, a condenser 15, a vacuum pump 16, a mother liquor tank 17, a mother liquor circulating pump 19 and a quench tower 20; the high-salt water pipeline is connected with the primary separation chamber 1, the top of the primary separation chamber 1 is connected with the primary evaporation chamber 2, the top of the primary evaporation chamber 2 is connected with the secondary separation chamber 5, and the bottom of the primary evaporation chamber 2 and the bottom of the primary separation chamber 1 are connected with the secondary evaporation chamber 6; the top of the secondary separation chamber 5 is connected with a secondary evaporation chamber 6, the top of the secondary evaporation chamber 6 is connected with a tertiary separation chamber 9, and the bottom of the secondary evaporation chamber 6 and the bottom of the secondary separation chamber 5 are connected with a tertiary evaporation chamber 10; the top of the third-stage separation chamber 9 is connected with a third-stage evaporation chamber 10, and the top of the third-stage evaporation chamber 10 is connected with a quenching tower 20 through a condenser 15 and a vacuum pump 16; the bottom of the third-stage evaporation chamber 10 and the bottom of the third-stage separation chamber 9 are sequentially connected with a thickener 13, a centrifuge 14 and a mother liquor tank 17 together, and the mother liquor tank 17 is connected with the third-stage evaporation chamber 10 through a mother liquor circulating pump 19.
The lower parts of the second-stage separation chamber 5 and the third-stage separation chamber 9 are connected with a condensate tank 18 through pipelines, the bottom of the condenser 15 is also connected with the condensate tank 18, and the top of the condensate tank 18 is connected with the third-stage separation chamber 9.
The bottom of the primary evaporation chamber 2 is connected with the bottom of the primary separation chamber 1 through a primary axial-flow pump 3, and is connected with a secondary evaporation chamber 6 through a primary discharge pump 4.
The bottom of the second-stage evaporation chamber 6 is connected with the bottom of the second-stage separation chamber 5 through a second-stage axial flow pump 7, and is connected with a third-stage evaporation chamber 10 through a second-stage discharge pump 8.
The bottom of the third-stage evaporation chamber 10 is connected with the bottom of the third-stage separation chamber 9 through a third-stage axial flow pump 11, and is connected with a thickener 13 through a third-stage discharge pump 12.
The specific process of the embodiment is as follows:
the high-salinity wastewater of the wet deacidification tower enters a primary separation chamber 1 for primary separation, part of mother liquor exchanges heat with steam outside the pipe through a heat exchange pipe at the speed of 1.5-3.5 m per second by a primary axial-flow pump 3, enters a primary evaporation chamber 2 for evaporation, and the other part of the mother liquor in the primary separation chamber 1 directly enters a secondary evaporation chamber 6 for evaporation by a primary discharge pump 4; the gas-liquid part generated in the first-stage evaporation chamber 2 flows back to the first-stage separation chamber 1 to be circularly heated, so that the mother liquor in the first-stage separation chamber is preheated, and the other part of the generated gas-liquid enters the second-stage separation chamber 5 to be subjected to gas-liquid separation. A part of the mother liquor generated by the secondary separation chamber 5 enters a secondary evaporation chamber 6 through a secondary axial-flow pump 7 for further mother liquor concentration, and the other part of the mother liquor directly enters a tertiary evaporation chamber 10 through a secondary discharge pump 8 for evaporation; gas-liquid part generated in the secondary evaporation chamber 6 flows back to the secondary separation chamber 5 for cyclic heating so that the mother liquor in the secondary separation chamber is preheated; and the other part of the generated gas-liquid enters the third-stage separation chamber 9 for gas-liquid separation. A part of mother liquor generated by the third-stage separation chamber 9 enters a third-stage evaporation chamber 10 through a third-stage axial-flow pump 11 for further mother liquor concentration, the other part of mother liquor enters a thickener 13 through a third-stage discharge pump 12 for thickening, and then enters a centrifuge 14 for centrifugation to obtain a strong salt product 21, and the third part of mother liquor returns to the second-stage separation chamber 5 in the third-stage separation chamber 9 for circulating evaporation; the water produced in the tertiary separation chamber 9 flows directly into the condensate tank 18 as condensate. A part of gas-liquid generated in the third-stage separation chamber 9 flows back to the third-stage separation chamber 9 through a condensate tank 18 for cyclic heating; the mother liquor in the mother liquor tank 17 enters the three-stage evaporation chamber 10 through a mother liquor circulating pump 19 for circulating evaporation. A part of steam generated by the three-stage evaporator 10 is condensed by a condenser 15 to generate distilled water, the distilled water flows into a condensing tank 18 and then flows back to the three-stage separation chamber 9 for cyclic evaporation, and the other part of condensed water is pumped into a quenching tower system 20 through a vacuum pump 16.
Claims (3)
1. The utility model provides a high salt effluent disposal system of rotary kiln system of burning deacidification tower which characterized in that: comprises a primary separation chamber (1), a primary evaporation chamber (2), a secondary separation chamber (5), a secondary evaporation chamber (6), a tertiary separation chamber (9), a tertiary evaporation chamber (10), a thickener (13), a centrifuge (14), a condenser (15), a vacuum pump (16), a mother liquor tank (17), a mother liquor circulating pump (19) and a quench tower (20); the high-salt water pipeline is connected with the primary separation chamber (1), the top of the primary separation chamber (1) is connected with the primary evaporation chamber (2), the top of the primary evaporation chamber (2) is connected with the secondary separation chamber (5), and the bottom of the primary evaporation chamber (2) and the bottom of the primary separation chamber (1) are connected with the secondary evaporation chamber (6) together; the top of the secondary separation chamber (5) is connected with a secondary evaporation chamber (6), the top of the secondary evaporation chamber (6) is connected with a tertiary separation chamber (9), and the bottom of the secondary evaporation chamber (6) and the bottom of the secondary separation chamber (5) are connected with a tertiary evaporation chamber (10) together; the top of the third-stage separation chamber (9) is connected with a third-stage evaporation chamber (10), and the top of the third-stage evaporation chamber (10) is connected with a quenching tower (20) through a condenser (15) and a vacuum pump (16); the bottom of the three-stage evaporation chamber (10) and the bottom of the three-stage separation chamber (9) are sequentially connected with a thickener (13), a centrifuge (14) and a mother liquor tank (17) together, and the mother liquor tank (17) is connected with the three-stage evaporation chamber (10) through a mother liquor circulating pump (19).
2. The rotary kiln incineration system deacidification tower high-salinity wastewater treatment system according to claim 1, characterized in that: the lower parts of the second-stage separation chamber (5) and the third-stage separation chamber (9) are connected with a condensate tank (18) through a pipeline, the bottom of the condenser (15) is also connected with the condensate tank (18), and the top of the condensate tank (18) is connected with the third-stage separation chamber (9).
3. The high-salinity wastewater treatment system for the deacidification tower of the rotary kiln incineration system as claimed in claim 1 or 2, wherein: the bottom of the primary evaporation chamber (2) is connected with the bottom of the primary separation chamber (1) through a primary axial-flow pump (3), and is connected with a secondary evaporation chamber (6) through a primary discharge pump (4); the bottom of the secondary evaporation chamber (6) is connected with the bottom of the secondary separation chamber (5) through a secondary axial-flow pump (7), and is commonly connected with a tertiary evaporation chamber (10) through a secondary discharge pump (8); the bottom of the three-stage evaporation chamber (10) is connected with the bottom of the three-stage separation chamber (9) through a three-stage axial flow pump (11), and is connected with a thickener (13) through a three-stage discharge pump (12).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121454041.XU CN215570471U (en) | 2021-06-29 | 2021-06-29 | High-salinity wastewater treatment system for deacidification tower of rotary kiln incineration system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121454041.XU CN215570471U (en) | 2021-06-29 | 2021-06-29 | High-salinity wastewater treatment system for deacidification tower of rotary kiln incineration system |
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| CN215570471U true CN215570471U (en) | 2022-01-18 |
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| CN202121454041.XU Active CN215570471U (en) | 2021-06-29 | 2021-06-29 | High-salinity wastewater treatment system for deacidification tower of rotary kiln incineration system |
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| CN (1) | CN215570471U (en) |
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- 2021-06-29 CN CN202121454041.XU patent/CN215570471U/en active Active
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