CN106219855A - Direct Air-cooled Unit recuperation of heat and water treatment facilities and recuperation of heat and method for treating water - Google Patents
Direct Air-cooled Unit recuperation of heat and water treatment facilities and recuperation of heat and method for treating water Download PDFInfo
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- CN106219855A CN106219855A CN201610806054.6A CN201610806054A CN106219855A CN 106219855 A CN106219855 A CN 106219855A CN 201610806054 A CN201610806054 A CN 201610806054A CN 106219855 A CN106219855 A CN 106219855A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 260
- 238000011282 treatment Methods 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 18
- 239000012528 membrane Substances 0.000 claims abstract description 126
- 238000004821 distillation Methods 0.000 claims abstract description 124
- 238000010438 heat treatment Methods 0.000 claims abstract description 123
- 238000001816 cooling Methods 0.000 claims abstract description 41
- 239000013535 sea water Substances 0.000 claims description 31
- 238000011084 recovery Methods 0.000 claims description 26
- 238000003756 stirring Methods 0.000 claims description 15
- 238000004519 manufacturing process Methods 0.000 claims description 14
- 230000009471 action Effects 0.000 claims description 10
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 238000005086 pumping Methods 0.000 claims description 8
- 238000010992 reflux Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 7
- 230000003647 oxidation Effects 0.000 claims description 6
- 238000007254 oxidation reaction Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000002351 wastewater Substances 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 5
- 238000010248 power generation Methods 0.000 claims description 5
- 238000001556 precipitation Methods 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 4
- 238000004062 sedimentation Methods 0.000 claims description 3
- 239000010865 sewage Substances 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 239000002352 surface water Substances 0.000 claims description 3
- 239000003673 groundwater Substances 0.000 claims 1
- 230000009286 beneficial effect Effects 0.000 abstract description 3
- 239000013505 freshwater Substances 0.000 abstract description 2
- 239000000463 material Substances 0.000 abstract 1
- 230000006872 improvement Effects 0.000 description 9
- 230000008569 process Effects 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 230000002349 favourable effect Effects 0.000 description 4
- 238000010612 desalination reaction Methods 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 230000004907 flux Effects 0.000 description 3
- 230000002209 hydrophobic effect Effects 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 238000011033 desalting Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000005189 flocculation Methods 0.000 description 2
- 230000016615 flocculation Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000035515 penetration Effects 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000010408 sweeping Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000012982 microporous membrane Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
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- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/364—Membrane distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/368—Accessories; Auxiliary operations
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D1/00—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators
- F28D1/02—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid
- F28D1/04—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits
- F28D1/047—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits the conduits being bent, e.g. in a serpentine or zig-zag
- F28D1/0477—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits the conduits being bent, e.g. in a serpentine or zig-zag the conduits being bent in a serpentine or zig-zag
-
- 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
- C02F2103/06—Contaminated groundwater or leachate
-
- 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
- C02F2103/08—Seawater, e.g. for desalination
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
Landscapes
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a kind of Direct Air-cooled Unit recuperation of heat and water treatment facilities, former water enters pretreatment unit water inlet end, pretreatment unit water side is connected with heating bath water inlet end, and heating bath water side is connected with distillation device water inlet end, and distillation device water side is connected with producing pond；Water pump is positioned at distillation device water side, and heating bath water outlet is aspirated into distillation device by water pump, and distillation device water outlet flows back into heating bath by water pump；Or water pump is positioned at distillation device water inlet end, heating bath water outlet enters distillation device by pressure, and distillation device water outlet flows back into heating bath by water pump；Exhaust steam enters heating bath by air pump, in condensate return to boiler.Present invention also offers a kind of Direct Air-cooled Unit recuperation of heat and method for treating water.Beneficial effects of the present invention: make full use of exhaust steam residual heat, by Membrane Materials system condensing, saves the energy and air cooling system power consumption, produces high-quality freshwater resources, energy-conserving and environment-protective.
Description
Technical Field
The invention relates to the technical field of energy conservation and environmental protection, in particular to a heat recovery and water treatment device and a heat recovery and water treatment method for a direct air cooling unit.
Background
In water-deficient areas of China, some coal-fired power plants adopt air cooling units for power generation, and the air cooling units are generally divided into direct air cooling units and indirect air cooling units. In the direct air-cooling unit, exhaust steam is firstly led to an air-cooling condenser, surface heat exchange and cooling are carried out on the exhaust steam in the air-cooling condenser (an air-cooling island) by an axial flow fan, and the exhaust steam returns to a hot well (or a condensation water tank) after being condensed into water and then enters a thermodynamic system. Therefore, the direct air cooling unit does not need circulating cold water, a large amount of water resources can be saved, and power consumption is high due to the fact that the large-scale axial flow fan is required to purge. In addition, a large amount of heat in the exhaust steam enters the atmosphere, which not only causes energy waste, but also causes atmospheric environmental problems. Therefore, how to recycle the heat in the exhaust steam is always a key research field in the field of energy conservation.
The Membrane Distillation (MD) technology is an efficient membrane separation technology, the wastewater temperature is controlled, a hydrophobic microporous membrane is used as a separation medium, the steam pressure difference between two sides of the membrane is used as a mass transfer driving force, the processes of wastewater concentration and pure water recovery are realized, and compared with the traditional membrane separation technology, the MD technology has numerous advantages, such as extremely high salt interception efficiency, nearly 100% interception efficiency on most non-volatile substances, low requirement on the quality of inlet water, mild operation conditions (no need of high-pressure equipment), convenient operation and maintenance, difficult occurrence of membrane pollution, low energy consumption compared with the traditional evaporation and the like. In addition, the membrane distillation has strong adaptability to the change of the salt content in the wastewater, and theoretically, the membrane module can normally operate as long as solute is unsaturated and separated out. Since membrane distillation requires heating of raw water, energy consumption is relatively high, which is also one of the important factors limiting large-scale application of MD process.
Disclosure of Invention
In order to solve the above problems, the present invention provides a heat recovery and water treatment apparatus for a direct air cooling unit and a heat recovery and water treatment method, which combines a membrane distillation technology with a cooling system of the direct air cooling unit, thereby reducing or even avoiding waste of steam exhaust heat in the direct air cooling unit and recovering energy.
The invention provides a heat recovery and water treatment device of a direct air cooling unit, which comprises a pretreatment device, a heating pool, an air suction pump, a first heat exchanger, a first stirring device, a boiler, a membrane distillation device, a water pump and a water production pool, wherein the first heat exchanger and the first stirring device are arranged in the heating pool;
raw water to be treated enters the water inlet end of the pretreatment device, the water outlet end of the pretreatment device is connected with the water inlet end of the heating pool, the water outlet end of the heating pool is connected with the water inlet end of the membrane distillation device, and the water outlet end of the membrane distillation device is connected with the water production pool;
the water pump is positioned at the water outlet end of the membrane distillation device, the outlet water of the heating pool is pumped into the membrane distillation device through the water pump, and the outlet water of the membrane distillation device flows back into the heating pool through the water pump; or the water pump is positioned at the water inlet end of the membrane distillation device, the outlet water of the heating pool enters the membrane distillation device through pressure, and the outlet water of the membrane distillation device flows back to the heating pool through the water pump;
and the exhaust steam enters the heating pool through the air extraction pump, and condensed water generated after the exhaust steam is condensed flows back to the boiler.
As a further improvement of the invention, the system also comprises an auxiliary heating pool, an air pump, a second heat exchanger and a second stirring device, wherein the second heat exchanger and the second stirring device are arranged in the auxiliary heating pool;
raw water to be treated enters the water inlet end of the pretreatment device, the water outlet end of the pretreatment device is connected with the water inlet end of the heating pool, the water outlet end of the heating pool is connected with the water inlet end of the auxiliary heating pool, the water outlet end of the auxiliary heating pool is connected with the water inlet end of the water film distillation device, and the water outlet end of the water film distillation device is connected with the water production pool;
the water pump is positioned at the water outlet end of the membrane distillation device, the outlet water of the auxiliary heating tank is pumped into the membrane distillation device through the water pump, and the outlet water of the membrane distillation device flows back into the heating tank through the water pump; or the water pump is positioned at the water inlet end of the membrane distillation device, the outlet water of the auxiliary heating pool enters the membrane distillation device through pressure, and the outlet water of the membrane distillation device flows back to the heating pool through the water pump;
high-temperature steam enters the auxiliary heating tank through the air suction pump, exhaust steam enters the heating tank through the air suction pump, condensate water generated after the exhaust steam is condensed flows back into the boiler, and meanwhile, the condensate water generated after the high-temperature steam is condensed flows back into the boiler.
As a further improvement of the invention, the pretreatment device is one or a combination of several of a sedimentation tank, an oil separation tank, an oxidation tank, a softening tank, a filter and a biochemical tank.
As a further improvement of the invention, the direction of the steam flow of the dead steam in the first heat exchanger is opposite to the direction of the water flow in the heating pool.
As a further improvement of the invention, the membrane distillation device adopts one or a combination of a plurality of air gap type membrane distillation devices, air sweeping type membrane distillation devices, vacuum air gap type membrane distillation devices and direct contact type membrane distillation devices.
As a further improvement of the invention, the high-temperature steam is high-temperature steam with the temperature higher than 80 ℃ after power generation in the steam turbine.
The invention also provides a heat recovery and water treatment method for the direct air cooling unit, which comprises the following steps:
step 1, raw water to be treated enters a heating pool after being pretreated by a pretreatment device;
step 2, the exhaust pump pumps exhausted steam at 55-65 ℃ discharged by a steam turbine of the direct air cooling unit into the heating pool, the pretreated raw water is heated to 45-60 ℃ through the first heat exchanger, and condensed water generated after heat exchange and condensation of the exhausted steam flows back to the boiler;
step 3, after the water in the heating pool is heated, the water is pumped into the membrane distillation device under the pumping action of the water pump to carry out membrane distillation concentration treatment; or, after being heated, the water in the heating pool enters the membrane distillation device through pressure to carry out membrane distillation concentration treatment;
step 4, refluxing concentrated water generated by membrane distillation to the heating pool under the action of the water pump, and repeating the step 2 and the step 3;
and 5, collecting the produced water of the membrane distillation device by the water producing pool for production or life.
As a further improvement of the invention, step 3 is replaced by:
heating water in the heating pool and then feeding the water into an auxiliary heating pool, pumping high-temperature steam with the temperature higher than 80 ℃ generated in a steam turbine into the auxiliary heating pool by using an air pump, heating the water in the auxiliary heating pool to 70-95 ℃ by using a second heat exchanger, and refluxing the high-temperature steam into the boiler after heat exchange and condensation; meanwhile, after being heated, the water in the auxiliary heating pool is pumped into the membrane distillation device under the pumping action of the water pump to carry out membrane distillation concentration treatment, or after being heated, the water in the auxiliary heating pool enters the membrane distillation device under pressure to carry out membrane distillation concentration treatment.
As a further improvement of the invention, the pretreatment in the step 1 is one or more of chemical bottom precipitation, chemical oxidation, biological treatment, filtration and adsorption.
As a further improvement of the invention, in step 1, the raw water is power plant wastewater or domestic sewage or seawater or surface water or underground water.
The invention has the beneficial effects that:
1. the waste steam and the waste heat of the direct air cooling unit are fully utilized, so that the energy and the power consumption of an air cooling system are saved, a large amount of high-quality fresh water resources can be produced, the win-win effect of energy conservation and environmental protection is realized, and the maximization of the heat efficiency of the whole power plant is facilitated;
2. a membrane distillation auxiliary steam heating system (an auxiliary heating pool, an air suction pump, a second heat exchanger and a second stirring device) can be arranged according to actual needs so as to meet the requirements of the membrane distillation system on different water inlet temperatures, thus being beneficial to saving the floor area of a power plant and being convenient for the reconstruction of the existing system;
3. is suitable for pure water production or other solution desalination treatments such as wastewater treatment and seawater desalination.
Drawings
Fig. 1 is a schematic structural diagram of a heat recovery and water treatment device of a direct air cooling unit according to a first embodiment of the invention;
fig. 2 is a schematic structural diagram of a heat recovery and water treatment device of a direct air cooling unit according to a second embodiment of the present invention.
In the figure, the position of the upper end of the main shaft,
1. a pretreatment device; 2. a heating tank; 3. an air pump; 4. a first heat exchanger; 5. a boiler; 6. an auxiliary heating tank; 7. an air pump; 8. a second heat exchanger; 9. a membrane distillation device; 10. a water pump; 11. a water producing pool.
Detailed Description
The present invention will be described in further detail below with reference to specific embodiments and with reference to the attached drawings.
Embodiment 1, as shown in fig. 1, a heat recovery and water treatment device of a direct air cooling unit according to a first embodiment of the present invention includes a pretreatment device 1, a heating tank 2, an air pump 3, a first heat exchanger 4, a first stirring device, a boiler 5, a membrane distillation device 9, a water pump 10, and a water production tank 11, wherein the heating tank 2 is internally provided with the first heat exchanger 4 and the first stirring device. Raw water to be treated enters the water inlet end of the pretreatment device 1, the water outlet end of the pretreatment device 1 is connected with the water inlet end of the heating pool 2, the water outlet end of the heating pool 2 is connected with the water inlet end of the membrane distillation device 9, and the water outlet end of the membrane distillation device 9 is connected with the water production pool 11. The water pump 10 is positioned at the water outlet end of the membrane distillation device 9, the outlet water of the heating pool 2 is pumped into the membrane distillation device 9 through the water pump 10, and the outlet water of the membrane distillation device 9 flows back into the heating pool 2 through the water pump 10; or the water pump 10 is positioned at the water inlet end of the membrane distillation device 9, the outlet water of the heating pool 2 enters the membrane distillation device 9 through pressure, and the outlet water of the membrane distillation device 9 flows back to the heating pool 2 through the water pump 10. The exhaust steam enters the heating pool 2 through the air pump 3, and condensed water generated after the exhaust steam is condensed flows back to the boiler 5.
Wherein,
the pretreatment device 1 is one or a combination of a plurality of sedimentation tanks, oil separation tanks, oxidation tanks, softening tanks, filters and biochemical tanks.
The direction of the steam flow of the dead steam in the first heat exchanger 4 is opposite to the direction of the water flow in the heating pool 2.
The membrane distillation device 9 adopts one or a combination of a plurality of air gap type membrane distillation devices, air sweeping type membrane distillation devices, vacuum air gap type membrane distillation devices and direct contact type membrane distillation devices.
The method for desalting seawater by using the heat recovery and water treatment device of the direct air cooling unit by taking seawater as a treatment object comprises the following steps:
step 1, removing suspended matters, hardness and other pollutants in seawater after the seawater with the salt content of about 3.2% is subjected to softening, flocculation, precipitation, filtration and other pretreatment of a pretreatment device 1, and feeding the pretreated seawater into a heating pool 2.
And 2, extracting exhaust steam of 65 ℃ discharged by a steam turbine of the direct air cooling unit into the heating pool 2 by using the air extracting pump 3, heating the seawater to 60 ℃ by using the first heat exchanger 4, and refluxing condensate water generated after heat exchange and condensation of the exhaust steam into the boiler 5 after heat regeneration and deoxidization treatment.
Step 3, pumping the heated seawater into a membrane distillation device 9 under the pumping action of a water pump 10 for membrane distillation concentration treatment; or the heated seawater enters the membrane distillation device 9 through pressure to carry out membrane distillation concentration treatment.
And 4, refluxing concentrated water generated by membrane distillation into the heating pool 2 under the action of the water pump 10, and performing heating and membrane distillation concentration treatment.
And 5, collecting the produced water of the membrane distillation device 9 by a water producing pool 11, and recycling the produced water for the production of a power plant, the life of residents and the like.
The adoption of the water inlet mode of suction is favorable for reducing the seawater pressure in the membrane component and avoiding the penetration of a hydrophobic membrane, and meanwhile, the steam pressure difference on two sides of the membrane can be increased under the same operation condition, thereby being favorable for improving the water flux of the membrane.
In this embodiment, because the space in the power plant is sufficient, there is enough space for constructing the membrane distillation system, and in order not to affect the power generation efficiency of the main machine, the arrangement of the seawater auxiliary heating system (the auxiliary heating tank, the air suction pump, the second heat exchanger and the second stirring device) is cancelled. When the salt content of the seawater in the heating pool 2 reaches 20%, the seawater is discharged out of the heating pool 2 for subsequent treatment, and the heating and concentration processes are repeated.
Embodiment 2, as shown in fig. 2, a direct air cooling unit heat recovery and water treatment apparatus according to a second embodiment of the present invention is different from embodiment 1 in that the apparatus further includes an auxiliary heating tank 6, an air pump 7, a second heat exchanger 8, and a second stirring device, and the second heat exchanger 8 and the second stirring device are disposed in the auxiliary heating tank 6. Raw water to be treated enters the water inlet end of the pretreatment device 1, the water outlet end of the pretreatment device 1 is connected with the water inlet end of the heating pool 2, the water outlet end of the heating pool 2 is connected with the water inlet end of the auxiliary heating pool 6, the water outlet end of the auxiliary heating pool 6 is connected with the water inlet end of the water film distillation device 9, and the water outlet end of the water film distillation device 9 is connected with the water production pool 11. The water pump 10 is positioned at the water outlet end of the membrane distillation device 9, the outlet water of the auxiliary heating pool 6 is pumped into the membrane distillation device 9 through the water pump 10, and the outlet water of the membrane distillation device 9 flows back into the heating pool 2 through the water pump 10; or the water pump 10 is positioned at the water inlet end of the membrane distillation device 9, the outlet water of the auxiliary heating pool 6 enters the membrane distillation device 9 through pressure, and the outlet water of the membrane distillation device 9 flows back to the heating pool 2 through the water pump 10. High-temperature steam enters the auxiliary heating pool 6 through the air extracting pump 7, exhaust steam enters the heating pool 2 through the air extracting pump 3, condensate water generated after the exhaust steam is condensed flows back to the boiler 5, and meanwhile, the condensate water generated after the high-temperature steam is condensed flows back to the boiler 5.
Wherein the high-temperature steam is the high-temperature steam with the temperature higher than 80 ℃ after power generation in the steam turbine.
The method for desalting seawater by using the heat recovery and water treatment device of the direct air cooling unit by taking seawater as a treatment object comprises the following steps:
step 1, removing suspended matters, hardness and other pollutants in seawater after the seawater with the salt content of about 2.8% is subjected to softening, flocculation, precipitation, filtration and other pretreatment of a pretreatment device 1, and feeding the pretreated seawater into a heating pool 2.
And 2, extracting exhaust steam of 55 ℃ discharged by a steam turbine of the direct air cooling unit into the heating pool 2 by using the air extracting pump 3, heating the seawater to 45 ℃ by using the first heat exchanger 4, and refluxing condensate water generated after heat exchange and condensation of the exhaust steam into the boiler 5 after heat regeneration and deoxidization treatment.
Step 3, the heated seawater enters an auxiliary heating pool 6, high-temperature steam at 90 ℃ generated in a steam turbine is extracted into the auxiliary heating pool 6 by an air extraction pump 7, the seawater is heated to 80 ℃ by a second heat exchanger 8, and the high-temperature steam flows back to a boiler 5 after heat exchange and condensation; meanwhile, the heated seawater is pumped into the membrane distillation device 9 for membrane distillation concentration treatment under the pumping action of the water pump 10, or the heated seawater enters the membrane distillation device 9 for membrane distillation concentration treatment through pressure.
And 4, refluxing concentrated water generated by membrane distillation into the heating pool 2 under the action of the water pump 10, and performing heating and membrane distillation concentration treatment.
And 5, collecting the produced water of the membrane distillation device 9 by a water producing pool 11, and recycling the produced water for the production of a power plant, the life of residents and the like.
The adoption of the water inlet mode of suction is favorable for reducing the seawater pressure in the membrane component and avoiding the penetration of a hydrophobic membrane, and meanwhile, the steam pressure difference on two sides of the membrane can be increased under the same operation condition, thereby being favorable for improving the water flux of the membrane.
In this embodiment, the layout is compact, the area available for construction is limited, and in order to reduce the floor area of the membrane distillation system, the water flux per membrane area of the membrane distillation system needs to be increased as much as possible so as to reduce the amount of membrane modules and finally save the site area, so that the membrane distillation inlet water needs to be controlled at a higher temperature, and an auxiliary seawater heating system (an auxiliary heating tank, an air suction pump, a second heat exchanger and a second stirring device) is added. When the salt content of the seawater in the heating pool 2 reaches 20%, the seawater is discharged out of the heating pool 2 for subsequent treatment, and the heating and concentration processes are repeated.
The invention aims at the defects of large energy consumption and serious heat loss of an air cooling system in a power plant of a direct air cooling unit, combines the waste heat utilization of the power plant with a membrane distillation process, replaces the direct air cooling system with the membrane distillation system, and carries out membrane distillation seawater desalination or other membrane distillation water treatment processes by using the waste heat in exhaust steam as a heat source of the membrane distillation system. The pretreatment process can be one or more of chemical bottom precipitation, chemical oxidation, biological treatment, filtration and adsorption. Wherein the raw water for treatment is power plant wastewater or domestic sewage or seawater or surface water or underground water.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The heat recovery and water treatment device of the direct air cooling unit is characterized by comprising a pretreatment device (1), a heating pool (2), an air pump (3), a first heat exchanger (4), a first stirring device, a boiler (5), a membrane distillation device (9), a water pump (10) and a water production pool (11), wherein the first heat exchanger (4) and the first stirring device are arranged in the heating pool (2);
raw water to be treated enters the water inlet end of the pretreatment device (1), the water outlet end of the pretreatment device (1) is connected with the water inlet end of the heating pool (2), the water outlet end of the heating pool (2) is connected with the water inlet end of the membrane distillation device (9), and the water outlet end of the membrane distillation device (9) is connected with the water production pool (11);
the water pump (10) is positioned at the water outlet end of the membrane distillation device (9), the outlet water of the heating pool (2) is pumped into the membrane distillation device (9) through the water pump (10), and the outlet water of the membrane distillation device (9) flows back into the heating pool (2) through the water pump (10); or the water pump (10) is positioned at the water inlet end of the membrane distillation device (9), the outlet water of the heating pool (2) enters the membrane distillation device (9) through pressure, and the outlet water of the membrane distillation device (9) flows back to the heating pool (2) through the water pump (10);
and the exhaust steam enters the heating pool (2) through the air extraction pump (3), and condensed water generated after the exhaust steam is condensed flows back to the boiler (5).
2. The heat recovery and water treatment device of the direct air cooling unit according to claim 1, further comprising an auxiliary heating tank (6), an air pump (7), a second heat exchanger (8) and a second stirring device, wherein the second heat exchanger (8) and the second stirring device are arranged in the auxiliary heating tank (6);
raw water to be treated enters the water inlet end of the pretreatment device (1), the water outlet end of the pretreatment device (1) is connected with the water inlet end of the heating pool (2), the water outlet end of the heating pool (2) is connected with the water inlet end of the auxiliary heating pool (6), the water outlet end of the auxiliary heating pool (6) is connected with the water inlet end of the water film distillation device (9), and the water outlet end of the film distillation device (9) is connected with the water production pool (11);
the water pump (10) is positioned at the water outlet end of the membrane distillation device (9), the outlet water of the auxiliary heating tank (6) is pumped into the membrane distillation device (9) through the water pump (10), and the outlet water of the membrane distillation device (9) flows back into the heating tank (2) through the water pump (10); or the water pump (10) is positioned at the water inlet end of the membrane distillation device (9), the outlet water of the auxiliary heating tank (6) enters the membrane distillation device (9) through pressure, and the outlet water of the membrane distillation device (9) flows back to the heating tank (2) through the water pump (10);
high-temperature steam enters the auxiliary heating pool (6) through the air extracting pump (7), exhaust steam enters the heating pool (2) through the air extracting pump (3), condensate water generated after the exhaust steam is condensed flows back into the boiler (5), and meanwhile, the condensate water generated after the high-temperature steam is condensed flows back into the boiler (5).
3. The heat recovery and water treatment device of the direct air cooling unit according to claim 1 or 2, characterized in that the pretreatment device (1) is one or a combination of several of a sedimentation tank, an oil separation tank, an oxidation tank, a softening tank, a filter and a biochemical tank.
4. The direct air cooling unit heat recovery and water treatment device according to claim 1 or 2, characterized in that the direction of the dead steam in the first heat exchanger (4) is opposite to the direction of the water flow in the heating tank (2).
5. The heat recovery and water treatment device of the direct air cooling unit according to claim 1 or 2, characterized in that the membrane distillation device (9) is one or more of an air gap type membrane distillation device, a gas swept type membrane distillation device, a vacuum air gap type membrane distillation device and a direct contact type membrane distillation device.
6. The heat recovery and water treatment device of the direct air cooling unit according to claim 2, wherein the high-temperature steam is the high-temperature steam with the temperature higher than 80 ℃ after power generation in the steam turbine.
7. A heat recovery and water treatment method using the heat recovery and water treatment device of the direct air cooling unit according to claim 1, characterized by comprising the following steps:
step 1, raw water to be treated enters a heating pool (2) after being pretreated by a pretreatment device (1);
step 2, the exhaust pump (3) pumps exhaust steam at 55-65 ℃ discharged by a steam turbine of the direct air cooling unit into the heating pool (2), the pretreated raw water is heated to 45-60 ℃ through the first heat exchanger (4), and condensed water generated after heat exchange and condensation of the exhaust steam flows back into the boiler (5);
step 3, after the water in the heating pool (2) is heated, the water is pumped into the membrane distillation device (9) under the pumping action of the water pump (10) to carry out membrane distillation concentration treatment; or, after being heated, the water in the heating pool (2) enters the membrane distillation device (9) through pressure to carry out membrane distillation concentration treatment;
step 4, refluxing concentrated water generated by membrane distillation into the heating pool (2) under the action of the water pump (10), and repeating the step 2 and the step 3;
and 5, collecting the water produced by the membrane distillation device (9) by the water producing pool (11) for production or life.
8. The heat recovery and water treatment method of claim 7, wherein step 3 is replaced with:
the water in the heating pool (2) is heated and then enters an auxiliary heating pool (6), high-temperature steam with the temperature higher than 80 ℃ generated in a steam turbine is extracted into the auxiliary heating pool (6) by an air extraction pump (7), the water in the auxiliary heating pool (6) is heated to 70-95 ℃ by a second heat exchanger (8), and the high-temperature steam flows back into the boiler (5) after heat exchange and condensation; meanwhile, after being heated, the water in the auxiliary heating tank (6) is pumped into the membrane distillation device (9) under the pumping action of the water pump (10) to carry out membrane distillation concentration treatment, or after being heated, the water in the auxiliary heating tank (6) enters the membrane distillation device (9) through pressure to carry out membrane distillation concentration treatment.
9. The heat recovery and water treatment method according to claim 7 or 8, wherein the pretreatment in step 1 is one or more of chemical bottom precipitation, chemical oxidation, biological treatment, filtration and adsorption.
10. The heat recovery and water treatment method according to claim 7 or 8, wherein in step 1, the raw water is power plant wastewater or domestic sewage or seawater or surface water or groundwater.
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