CN220812158U - Desalted water preparing system for power plant wastewater - Google Patents
Desalted water preparing system for power plant wastewater Download PDFInfo
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- CN220812158U CN220812158U CN202420580828.8U CN202420580828U CN220812158U CN 220812158 U CN220812158 U CN 220812158U CN 202420580828 U CN202420580828 U CN 202420580828U CN 220812158 U CN220812158 U CN 220812158U
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 349
- 239000002351 wastewater Substances 0.000 title claims abstract description 23
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 60
- 238000005261 decarburization Methods 0.000 claims abstract description 56
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 55
- 238000005342 ion exchange Methods 0.000 claims abstract description 34
- 239000004576 sand Substances 0.000 claims abstract description 26
- 238000001914 filtration Methods 0.000 claims abstract description 20
- 238000001556 precipitation Methods 0.000 claims abstract description 19
- 238000004140 cleaning Methods 0.000 claims description 21
- 239000012528 membrane Substances 0.000 claims description 20
- 238000005262 decarbonization Methods 0.000 claims description 17
- 238000006243 chemical reaction Methods 0.000 claims description 13
- 150000001768 cations Chemical class 0.000 claims description 12
- 238000007670 refining Methods 0.000 claims description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical group [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 11
- 239000003546 flue gas Substances 0.000 claims description 11
- 150000001450 anions Chemical class 0.000 claims description 10
- 238000004062 sedimentation Methods 0.000 claims description 9
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 238000005189 flocculation Methods 0.000 claims description 5
- 230000016615 flocculation Effects 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 239000007789 gas Substances 0.000 claims description 2
- 238000005498 polishing Methods 0.000 claims description 2
- 239000010908 plant waste Substances 0.000 claims 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 30
- 239000000498 cooling water Substances 0.000 abstract description 8
- 235000012239 silicon dioxide Nutrition 0.000 abstract description 5
- 239000000377 silicon dioxide Substances 0.000 abstract description 5
- 238000000034 method Methods 0.000 description 23
- 230000008569 process Effects 0.000 description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 12
- 238000010612 desalination reaction Methods 0.000 description 9
- 238000009287 sand filtration Methods 0.000 description 8
- 239000000126 substance Substances 0.000 description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 description 6
- 239000001569 carbon dioxide Substances 0.000 description 6
- 238000011033 desalting Methods 0.000 description 6
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 5
- 238000007664 blowing Methods 0.000 description 5
- 230000002035 prolonged effect Effects 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- 229910052710 silicon Inorganic materials 0.000 description 5
- 239000010703 silicon Substances 0.000 description 5
- 239000000084 colloidal system Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000011010 flushing procedure Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000000909 electrodialysis Methods 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- 239000013049 sediment Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000012958 reprocessing Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000002352 surface water Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000009296 electrodeionization Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000010287 polarization Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Abstract
The utility model discloses a desalted water preparing system for power plant wastewater, which comprises a raw water tank, wherein a water outlet of the raw water tank is connected with a high-density precipitation device, a water outlet of the high-density precipitation device is connected with a sand filtering device, a water outlet of the sand filtering device is connected with an ultrafiltration device, a water outlet of the ultrafiltration device is connected with a reverse osmosis device, a water outlet of the reverse osmosis device is connected with a decarburization device, a water outlet of the decarburization device is connected with an ion exchange device, and a water outlet of the ion exchange device is connected with a desalted water tank. The system utilizes the circulating cooling water drainage of the power plant and the concentrated water of the water converted from the power plant as raw water to prepare desalted water, so that the waste water resource can be effectively utilized, the resource is saved, and the cost is reduced; the conductivity of the desalted water prepared is less than or equal to 0.2 mu S/cm, the silicon dioxide content is less than or equal to 20 mu g/L, and the water quality requirement of the desalted water of the power plant is met.
Description
Technical Field
The utility model belongs to the technical field of water treatment, and particularly relates to a desalted water preparation system for power plant wastewater.
Background
In the production and operation process of a power plant, the desalted water treatment process is an important link, and in the desalted water treatment system of the power plant, the desalted water treatment system is required to ensure that the water quality of the produced water meets the standard while ensuring that the water yield is met, and the economic cost is reduced as much as possible.
Common desalination processes include electrodialysis, ion exchange, EDI electrodeionization, reverse osmosis, etc., and a desalination pretreatment step is provided before desalination. On the one hand, the traditional desalting pretreatment links such as multi-medium filtration, ultrafiltration and the like are simple to operate and stable in operation, but have poor water fluctuation resistance and cannot remove hardness and silicon dioxide. On the other hand, the conventional desalination process also has the following problems: the electrodialysis method has the advantages of simple process system and less equipment, can be used for preparing desalted water by being connected in series with the ion exchange method, but is easy to generate polarization scaling and has higher requirement on the quality of inlet water; the EDI electric desalting method is a process combining electrodialysis technology and ion exchange, has good water quality of produced water and low running cost, but has extremely strict requirement on water quality of inlet water and higher initial investment cost; the reverse osmosis method has the advantages of high desalination rate, simple operation and maintenance and stable equipment operation, but has certain requirements on the water temperature of the inlet water, the water production capacity of the reverse osmosis can be reduced when the water temperature is lower than 20 ℃, and when the reverse osmosis is operated in winter, the water temperature of the inlet water is heated by steam, a large amount of steam is consumed, and certain operation cost can be increased for cold areas.
Therefore, proper desalted water treatment process and equipment are selected, and the method has certain significance and value for preparing qualified desalted water and reducing running cost in winter.
Disclosure of utility model
The utility model aims to provide a system for preparing desalted water from power plant wastewater, which utilizes the power plant wastewater to prepare desalted water reaching the standard, realizes the resource utilization of the power plant and saves the cost.
The utility model is implemented by the following technical scheme.
The utility model provides a desalted water system is prepared to power plant's waste water, it includes the former water tank, the delivery port of former water tank is connected with high density sediment device through the raw water pump, the product water outlet of the concentrated pond of sediment of high density sediment device is connected with sand filtration device, the product water outlet connection of sand filtration device has ultrafiltration device, the delivery port of ultrafiltration product water tank of ultrafiltration device is connected with reverse osmosis unit, the product water outlet connection of reverse osmosis unit has decarbonization device, decarbonization device's the delivery port of product water tank is connected with ion exchange device, the product water outlet connection of ion exchange device's mixed bed has desalted water tank; the heat exchanger is also included; the water outlet of the sand filter device is communicated with the cold medium inlet of the heat exchanger, and the cold medium outlet of the heat exchanger is communicated with the water inlet of the ultrafiltration device.
The circulating cooling water drainage of the power plant and the concentrated water of the power plant are used as raw water, so that water resources can be effectively utilized, and energy conservation and emission reduction are realized; the raw water tank plays a role in buffering raw water supply, the raw water supply amount and the raw water pump input amount are coordinated, raw water is pressurized by the raw water pump and is sent to the high-density precipitation device after entering the raw water tank, silicon and hardness are removed, produced water enters the sand filtering device through the lifting pump to remove suspended matters and colloid, produced water of the sand filtering device enters the ultrafiltration device to remove suspended matters remained by sand filtering, and under the condition of colder winter, the produced water of the sand filtering device firstly rises in temperature through the heat exchanger and then enters the ultrafiltration device; the produced water of the ultrafiltration device enters the reverse osmosis device to realize high-efficiency desalination; the reverse osmosis produced water automatically flows into the decarbonization device to remove carbon dioxide, the decarbonized produced water enters the ion exchange device to further remove salt, and the conductivity of the produced water of the ion exchange device is less than or equal to 0.2 mu S/cm, so that the water quality requirement of desalted water of a power plant is met.
Further, the high-density sedimentation device comprises a slow reaction tank, a fast reaction tank, a flocculation tank and a sedimentation concentration tank which are communicated in sequence; the water outlet of the raw water pump is communicated with the water inlet of the slow reaction tank; and a water outlet of the sedimentation concentration tank is communicated with a water inlet of the sand filtering device through a lifting pump. Raw water entering the high-density precipitation device sequentially passes through the slow reaction tank, the fast reaction tank, the flocculation tank and the precipitation concentration tank, so that the hardness and silicon dioxide of the raw water can be effectively removed.
Further, a double-layer filter material is arranged in the sand filter device. Can be used for removing suspended matters and colloid. The high-density precipitation device and the sand filtration device can remove hard and impurities from raw water, so that the subsequent ultrafiltration device can smoothly run, and the service life of an ultrafiltration membrane is prolonged.
Further, the heat exchanger is a flue gas heat exchanger. The heat source adopts the flue gas of 140-160 ℃ behind the boiler dust remover of the power plant, and the heat of the flue gas is utilized to raise the temperature of water produced by the sand filter device, thereby being beneficial to the normal and stable operation of the ultrafiltration device and the reverse osmosis device, reducing the influence of seasonal temperature change on the water yield of the reverse osmosis process in the follow-up, and compared with the reverse osmosis method in the background art, a large amount of steam is utilized for heating in winter, and the method has the advantage of energy conservation. The raw water does not pass through the heat exchanger in summer.
Further, the ultrafiltration device comprises a self-cleaning filter, ultrafiltration membrane equipment and an ultrafiltration water producing tank; the water inlet of the self-cleaning filter is communicated with the produced water outlet of the sand filtering device, and the water inlet of the self-cleaning filter is communicated with the cold medium outlet of the heat exchanger; the water outlet of the self-cleaning filter is communicated with the water inlet of the ultrafiltration membrane equipment, and the water outlet of the ultrafiltration membrane equipment is communicated with the water inlet of the ultrafiltration water production tank. The ultrafiltration device can remove suspended matters, colloid, microorganisms and the like in water; the self-cleaning filter is arranged in the ultrafiltration device, so that the ultrafiltration device is protected, and the service life of the ultrafiltration membrane is prolonged due to the blockage or scratch damage of large particulate matters; the flushing water, the back flushing water and the concentrated water of the ultrafiltration membrane equipment of the self-cleaning filter can be returned to the original water tank for reprocessing.
Further, the reverse osmosis device comprises a cartridge filter and a reverse osmosis apparatus; the water outlet of the ultrafiltration water producing tank is communicated with the water inlet of the cartridge filter through a reverse osmosis booster pump, and the water producing outlet of the cartridge filter is communicated with the reverse osmosis equipment through a reverse osmosis high-pressure pump. The cartridge filter is arranged, so that large particles in the water of the ultrafiltration water production tank can be further intercepted, normal operation of reverse osmosis is ensured, and the cleaning period of a reverse osmosis membrane is prolonged; the reverse osmosis is arranged, so that salt in water can be efficiently removed, the salt in water is reserved on the concentrated water side of the reverse osmosis equipment and enters other working procedures for treatment and utilization, the salt in produced water is less, and the salt enters the decarburization device from a produced water outlet.
Further, the decarburization device comprises a primary decarburization tower, a secondary decarburization tower and the decarburization water producing tank; the water inlet of the primary decarburization tower is communicated with the water outlet of the reverse osmosis device, the air inlet of the primary decarburization tower is connected with an air blower, and the water outlet of the primary decarburization tower is communicated with the water inlet of the secondary decarburization tower through a decarburization booster pump; the gas outlet of the secondary decarburization tower is connected with a vacuumizing device, and the water outlet of the secondary decarburization tower is communicated with the water inlet of the decarburization water producing tank. And (3) adopting a two-stage decarburization tower with a blowing stripping and vacuum suction dual-tower in series to remove carbon dioxide, bicarbonate and the like in water, and allowing the decarbonized water to enter the decarbonized water production tank.
Further, the ion exchange device comprises a cation bed, a anion bed and a mixed bed; the water outlet of the decarburization water producing tank is communicated with the water inlet of the cation bed through an ion exchange booster pump, the water producing outlet of the cation bed is communicated with the water inlet of the anion bed, and the water producing outlet of the anion bed is communicated with the water inlet of the mixed bed. Setting the ion exchange booster pump, conveying the water in the decarburization water production tank to the cation bed, and sequentially passing the decarburized water through the cation bed, the anion bed and the mixed bed to further carry out desalination treatment so as to reduce the conductivity of the water; and a detector is arranged at a water outlet of the mixed bed, and when the water outlet reaches the standard, the produced water of the mixed bed is conveyed to the desalted water tank for use by a power plant.
Further, the ion exchange apparatus further comprises a polishing bed; the water outlet of the mixed bed is communicated with the water inlet of the refining bed, and the water outlet of the refining bed is communicated with the water inlet of the desalted water tank. And when the conductivity index of the produced water of the mixed bed is detected to be unqualified, the produced water of the mixed bed is conveyed to the refining bed for further desalination, and then enters the desalted water tank.
The beneficial effects are that: the utility model provides a system for preparing desalted water from power plant wastewater, which utilizes power plant circulating cooling water drainage and power plant chemical water concentrated water as raw water to prepare desalted water, and can effectively utilize wastewater resources, save resources and reduce cost.
Raw water is sequentially treated by a high-density precipitation device, a sand filtering device, an ultrafiltration device, a reverse osmosis device, a decarburization device, an ion exchange device and the like, the conductivity of the desalted water obtained by the method is less than or equal to 0.2 mu S/cm, the silicon dioxide content is less than or equal to 20 mu g/L, and the water quality requirement of the desalted water of a power plant is met.
The high-density precipitation device has strong water fluctuation resistance, can remove the hardness and silicon of raw water, and ensures the stable operation of subsequent equipment; a heat exchanger is arranged behind the sand filtering device, the temperature of raw water is heated by using a flue gas heat source at 140-160 ℃ after the dust removal of a power plant boiler, the smooth operation of an ultrafiltration device and a reverse osmosis device in winter is ensured, and the resource utilization of power plant flue gas is realized; compared with the conventional single decarbonization process, the decarbonization process with the blowing stripping and vacuum pumping double towers in series can efficiently remove carbon dioxide and bicarbonate; the ion exchange device is additionally provided with a refining bed, and the water outlet of the mixed bed can effectively ensure the water quality of the outlet water.
Drawings
In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the utility model, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram showing the connection of the system for producing desalted water from power plant wastewater in example 1.
FIG. 2 is a schematic diagram showing the connection between the high-density precipitation apparatus and the sand filtration apparatus in example 1.
FIG. 3 is a schematic diagram showing the connection between the ultrafiltration device and the reverse osmosis device in example 1.
FIG. 4 is a schematic diagram showing the connection of the decarburization unit, the ion exchange unit and the desalinated water tank in example 1.
The drawings are as follows: 1. a raw water tank; 1-1 raw water pump; 2. a high density precipitation device; 2-1 a slow reaction tank; 2-2 a rapid reaction tank; 2-3, a flocculation tank; 2-4, a sedimentation concentration tank; 2-5, lifting pump; 3. sand filtering device; 4. a heat exchanger; 5. an ultrafiltration device; 5-1, self-cleaning the filter; 5-2, ultrafiltration membrane equipment; 5-3, ultrafiltering to form a water tank; 6. a reverse osmosis device; 6-1, reverse osmosis booster pump; 6-2, a cartridge filter; 6-3, reverse osmosis high pressure pump; 6-4, reverse osmosis equipment; 7. a decarburization device; 7-1, a primary decarburization tower; 7-2, a blower; 7-3, decarburizing the booster pump; 7-4, a secondary decarburization tower; 7-5, vacuumizing equipment; 7-6, decarburizing a water producing tank; 8. an ion exchange device; 8-1, an ion exchange booster pump; 8-2, a cation bed; 8-3, a bed of yin; 8-4, mixing bed; 8-5, refining bed; 9. a desalting water tank.
Detailed Description
The following description of the embodiments of the present utility model 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 utility model, but not all embodiments. In the description of the present utility model, it should be noted that the terms "primary," "secondary," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
Example 1: a system for preparing desalted water from power plant wastewater is shown in fig. 1, and comprises a raw water tank 1, a high-density precipitation device 2, a sand filtering device 3, a heat exchanger 4, an ultrafiltration device 5, a reverse osmosis device 6, a decarburization device 7, an ion exchange device 8 and a desalted water tank 9.
The water outlet of the raw water tank 1 is connected with a high-density sedimentation device 2 through a raw water pump 1-1. As shown in fig. 1 and 2, the high-density sedimentation device 2 comprises a slow reaction tank 2-1, a fast reaction tank 2-2, a flocculation tank 2-3 and a sedimentation concentration tank 2-4 which are communicated in sequence; the water outlet of the raw water pump 1-1 is communicated with the water inlet of the slow reaction tank 2-1; the water outlet of the sedimentation and concentration tank 2-4 is communicated with the water inlet of the sand filtering device 3 through a lifting pump 2-5. The sand filter device 3 is internally provided with a double-layer filter material, and a produced water outlet of the sand filter device 3 is connected with an ultrafiltration device 5. As shown in fig. 3, the ultrafiltration device 5 comprises a self-cleaning filter 5-1, an ultrafiltration membrane device 5-2 and an ultrafiltration water producing tank 5-3; the water inlet of the self-cleaning filter 5-1 is communicated with the water outlet of the sand filter device 3, the water outlet of the self-cleaning filter 5-1 is communicated with the water inlet of the ultrafiltration membrane equipment 5-2, and the water outlet of the ultrafiltration membrane equipment 5-2 is communicated with the water inlet of the ultrafiltration water producing tank 5-3; the flushing water and the back flushing water from the cleaning filter 5-1 return to the front-end raw water tank 1 for reprocessing. The reverse osmosis device 6 comprises a cartridge filter 6-2 and a reverse osmosis equipment 6-4; the water outlet of the ultrafiltration water producing tank 5-3 is communicated with the water inlet of the cartridge filter 6-2 through the reverse osmosis booster pump 6-1, the water producing outlet of the cartridge filter 6-2 is communicated with the reverse osmosis equipment 6-4 through the reverse osmosis high pressure pump 6-3, and the concentrated water of the reverse osmosis equipment 6-4 can be discharged to the power plant desulfurization device, so that the water resource utilization is realized. As shown in fig. 1 and 4, the decarburization device 7 comprises a primary decarburization tower 7-1, a secondary decarburization tower 7-4 and a decarburization water producing tank 7-6; the water inlet of the first-stage decarburization tower 7-1 is communicated with the water outlet of the reverse osmosis equipment 6-4, the air inlet of the first-stage decarburization tower 7-1 is connected with a blower 7-2, and the water outlet of the first-stage decarburization tower 7-1 is communicated with the water inlet of the second-stage decarburization tower 7-4 through a decarburization booster pump 7-3; the air outlet of the secondary decarburization tower 7-4 is connected with a vacuumizing device 7-5, and the water outlet of the secondary decarburization tower 7-4 is communicated with the water inlet of the decarburization water producing tank 7-6. The ion exchange device 8 comprises a cation bed 8-2, a anion bed 8-3 and a mixed bed 8-4; the water outlet of the decarburization water producing tank 7-6 is communicated with the water inlet of the cation bed 8-2 through the ion exchange booster pump 8-1, the water producing outlet of the cation bed 8-2 is communicated with the water inlet of the anion bed 8-3, and the water producing outlet of the anion bed 8-3 is communicated with the water inlet of the mixed bed 8-4; the water outlet of the mixed bed 8-4 is communicated with the water inlet of the desalted water tank 9; the ion exchange device 8 also comprises a refining bed 8-5; the water outlet of the mixed bed 8-4 is communicated with the water inlet of the refining bed 8-5, and the water outlet of the refining bed 8-5 is communicated with the water inlet of the desalted water tank 9.
As shown in fig. 1, the system for preparing desalted water from the power plant wastewater also comprises a heat exchanger 4, wherein the heat exchanger 4 is a flue gas heat exchanger 4; the water outlet of the sand filter device 3 is communicated with the cold medium inlet of the heat exchanger 4, and the cold medium outlet of the heat exchanger 4 is communicated with the water inlet of the self-cleaning filter 5-1; the heat medium inlet of the heat exchanger 4 is communicated with a power plant boiler flue gas pipeline, and the heat source is power plant boiler flue gas.
The working principle is as follows: the circulating cooling water drainage of the power plant and the concentrated water of the power plant are used as raw water, so that water resources can be effectively utilized, and energy conservation and emission reduction are realized; the raw water tank 1 plays a role in buffering raw water supply, the raw water supply amount and the raw water pump 1-1 input amount are coordinated, raw water is pressurized by the raw water pump 1-1 and is sent into the high-density precipitation device 2 after entering the raw water tank 1, silicon and hardness are removed, produced water enters the sand filtration device 3 through the lifting pump 2-5, suspended matters and colloid are removed, produced water of the sand filtration device 3 enters the ultrafiltration device 5, residual suspended matters of sand filtration are removed, and under the condition of colder winter, the produced water of the sand filtration device 3 is heated by the heat exchanger 4 and then enters the ultrafiltration device 5; the produced water of the ultrafiltration device 5 enters the reverse osmosis device 6 to realize high-efficiency desalination; the reverse osmosis produced water automatically flows into a decarburization device 7, two-stage decarburization towers which are connected in series by blowing, stripping and vacuum suction are adopted to remove carbon dioxide, bicarbonate and the like in water, the produced water after decarburization enters an ion exchange device 8 and sequentially passes through a positive bed 8-2, a negative bed 8-3 and a mixed bed 8-4 to be further desalted, a detector is arranged at a produced water outlet of the mixed bed 8-4, when the produced water reaches the standard, the produced water of the mixed bed 8-4 is conveyed to a desalted water tank 9, and when the produced water does not reach the standard, the produced water of the mixed bed 8-4 is conveyed to a refined bed 8-5 to be further desalted, and then the produced water enters a desalted water tank 9. The conductivity of desalted water in the desalted water tank 9 is less than or equal to 0.2 mu S/cm, the silicon dioxide content is less than or equal to 20 mu g/L, and the water quality requirement of the desalted water of the power plant is met.
Example 2: a Power plant uses the power plant wastewater of the embodiment 1 to prepare desalted water, and uses the power plant circulating cooling water drainage and the power plant chemical water concentrated water as raw water to prepare desalted water.
The design water quantity of the desalted water treatment station of the power plant A is 200 m 3/h, and surface water is originally adopted as a water source; after the circulating cooling water drainage of the power plant and the concentrated water of the chemical water of the power plant are adopted, the annual working time is 8000 h according to the treatment cost of 2 yuan per ton, and the wastewater treatment cost can be effectively reduced by 320 ten thousand per year.
When the power plant A operates in winter, the saturated steam of 0.3 Mpa is used as a heat source, the temperature of the inlet water is heated to 5 ℃ by using a plate heat exchanger, and the steam consumption is 1.89 t/h in winter; the current transformation is to adopt the flue gas heat exchanger to heat the water temperature in winter, and the power plant can reduce 5468.73 t steam in winter, saves 109.37 ten thousand yuan (the steam price is 200 yuan/ton according to 120 days in winter).
The original desalting water pretreatment process adopts a multi-medium filtration and ultrafiltration system, has no hard removal and silicon removal functions, and when the quality of raw water is poor, the multi-medium filter is easy to be blocked by filter materials, the ultrafiltration and reverse osmosis chemical cleaning frequency is high, the membrane scaling is serious, and the desalting rate is reduced; the high-density precipitation device is changed into a pretreatment process, the reverse osmosis device runs stably, the cleaning frequency of the ultrafiltration membrane and the reverse osmosis membrane is reduced, and the service life is prolonged.
The original desalted water decarbonization process adopts a conventional blast decarbonization tower, the decarbonization efficiency is about 90%, when the quality of raw water is poor, the content of soluble carbon dioxide and bicarbonate in the effluent of the decarbonization tower is still high, and the operation load of the subsequent ion exchange process is increased; after the two decarburization towers of blowing stripping and vacuum suction are modified to be connected in series, the decarburization efficiency is up to more than 98%, and the operation load of the ion exchange device is effectively slowed down.
The original ion exchange device adopts a positive bed and a negative bed which are connected in series, the conductivity of the effluent fluctuates, and the conductivity of the effluent of the negative bed is more than 0.2 mu S/cm when the quality of the raw water is poor; the mixing bed and the refining bed are additionally arranged, and the conductivity of the effluent can continuously meet the requirement of less than or equal to 0.15 mu S/cm.
Example 3: and B, the power plant utilizes the power plant wastewater of the embodiment 1 to prepare desalted water, and the power plant circulating cooling water drainage and the power plant chemical water concentrated water are used as raw water to prepare desalted water.
B, designing water quantity of a desalted water treatment station of the power plant to be 400 m 3/h, and taking surface water as a water source; the method adopts the circulating cooling water of the power plant for drainage and the concentrated water of the chemical water of the power plant, and the annual working time is 8000 h according to the treatment cost of 2 yuan per ton, so that the wastewater treatment cost can be effectively reduced by 640 ten thousand per year.
When the energy-saving type solar energy heat pump unit runs in winter, the original energy-saving type solar energy heat pump unit adopts 0.3 Mpa saturated steam as a heat source, and utilizes a plate heat exchanger to heat inlet water at 4 ℃, and the steam consumption is 3.04t/h in winter; the flue gas heat exchanger is adopted to heat the water temperature in winter, 8755.20t of steam can be reduced by the power plant in winter, 175.10 ten thousand yuan (the steam price is 200 yuan/ton according to 120 days in winter).
The original desalting water pretreatment process adopts a multi-medium filtration and ultrafiltration system, has no hard removal and silicon removal functions, and when the raw water quality is poor, the multi-medium filter is easy to be blocked by filter materials, the ultrafiltration and reverse osmosis chemical cleaning frequency is high, and the membrane scaling is serious; after the high-density precipitation device is pretreated, the reverse osmosis device runs stably, the cleaning frequency of the ultrafiltration membrane and the reverse osmosis membrane is reduced, and the service life is prolonged.
The original desalted water decarbonization process adopts a conventional blast decarbonization tower, the decarbonization efficiency is about 91%, when the quality of raw water is poor, the content of soluble carbon dioxide and bicarbonate in the effluent of the decarbonization tower is still high, and the operation load of the subsequent ion exchange process is increased; after being modified into the series connection of the blowing stripping and vacuum suction double decarburization towers, the decarburization efficiency is as high as 98.5%, and the running load of the ion exchange process is effectively slowed down.
The original ion exchange device adopts the series connection of a positive bed, a negative bed and a mixed bed, the electric conductivity of the effluent is accidentally larger than 0.2 mu S/cm, a refining bed is additionally arranged, and the electric conductivity of the effluent can continuously meet the requirement of less than or equal to 0.15 mu S/cm.
The foregoing description of the preferred embodiments of the utility model is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the utility model.
Claims (9)
1. The desalted water preparing system for the power plant waste water comprises a raw water tank, and is characterized in that a water outlet of the raw water tank is connected with a high-density precipitation device through a raw water pump, a water outlet of a precipitation concentration tank of the high-density precipitation device is connected with a sand filtering device, a water outlet of the sand filtering device is connected with an ultrafiltration device, a water outlet of an ultrafiltration water tank of the ultrafiltration device is connected with a reverse osmosis device, a water outlet of reverse osmosis equipment of the reverse osmosis device is connected with a decarburization device, a water outlet of a decarburization water tank of the decarburization device is connected with an ion exchange device, and a water outlet of a mixed bed of the ion exchange device is connected with a desalted water tank;
The heat exchanger is also included; the water outlet of the sand filter device is communicated with the cold medium inlet of the heat exchanger, and the cold medium outlet of the heat exchanger is communicated with the water inlet of the ultrafiltration device.
2. The system for preparing desalted water from wastewater of power plant according to claim 1, wherein the high-density precipitation device comprises a slow reaction tank, a fast reaction tank, a flocculation tank and a precipitation concentration tank which are communicated in sequence; the water outlet of the raw water pump is communicated with the water inlet of the slow reaction tank; and a water outlet of the sedimentation concentration tank is communicated with a water inlet of the sand filtering device through a lifting pump.
3. The system for preparing desalted water from waste water of power plant according to claim 1, wherein a double-layer filter material is arranged in the sand filter device.
4. The system for producing desalinated water from wastewater of a power plant of claim 1, wherein the heat exchanger is a flue gas heat exchanger.
5. The system for preparing desalted water from wastewater of power plant according to claim 1, wherein said ultrafiltration device comprises a self-cleaning filter, an ultrafiltration membrane apparatus, said ultrafiltration water producing tank; the water inlet of the self-cleaning filter is communicated with the produced water outlet of the sand filtering device, and the water inlet of the self-cleaning filter is communicated with the cold medium outlet of the heat exchanger; the water outlet of the self-cleaning filter is communicated with the water inlet of the ultrafiltration membrane equipment, and the water outlet of the ultrafiltration membrane equipment is communicated with the water inlet of the ultrafiltration water production tank.
6. The system for producing desalinated water from wastewater of a power plant of claim 1, wherein the reverse osmosis apparatus includes a cartridge filter and a reverse osmosis device; the water outlet of the ultrafiltration water producing tank is communicated with the water inlet of the cartridge filter through a reverse osmosis booster pump, and the water producing outlet of the cartridge filter is communicated with the reverse osmosis equipment through a reverse osmosis high-pressure pump.
7. The system for preparing desalted water from waste water of power plant according to claim 1, wherein said decarbonization device comprises a primary decarbonization tower, a secondary decarbonization tower, and said decarbonization water producing tank; the water inlet of the primary decarburization tower is communicated with the water outlet of the reverse osmosis device, the air inlet of the primary decarburization tower is connected with an air blower, and the water outlet of the primary decarburization tower is communicated with the water inlet of the secondary decarburization tower through a decarburization booster pump; the gas outlet of the secondary decarburization tower is connected with a vacuumizing device, and the water outlet of the secondary decarburization tower is communicated with the water inlet of the decarburization water producing tank.
8. The system for preparing desalted water from wastewater of power plant according to claim 1, wherein said ion exchange means comprises a cation bed, a anion bed, a mixed bed; the water outlet of the decarburization water producing tank is communicated with the water inlet of the cation bed through an ion exchange booster pump, the water producing outlet of the cation bed is communicated with the water inlet of the anion bed, and the water producing outlet of the anion bed is communicated with the water inlet of the mixed bed.
9. The system for producing desalinated water from power plant wastewater of claim 8, wherein the ion exchange unit further includes a polishing bed; the water outlet of the mixed bed is communicated with the water inlet of the refining bed, and the water outlet of the refining bed is communicated with the water inlet of the desalted water tank.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202420580828.8U CN220812158U (en) | 2024-03-25 | 2024-03-25 | Desalted water preparing system for power plant wastewater |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202420580828.8U CN220812158U (en) | 2024-03-25 | 2024-03-25 | Desalted water preparing system for power plant wastewater |
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