CN102642883B - System for desalinating seawater by waste heat from power plant - Google Patents
System for desalinating seawater by waste heat from power plant Download PDFInfo
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- 239000013505 freshwater Substances 0.000 claims abstract description 60
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 40
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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Abstract
The invention discloses a system for desalinating seawater by waste heat from a power plant. The system comprises a condenser circulating seawater taking branch system, a seawater multi-stage fresh evaporation branch system and a boiler smoke waste heat heating seawater circulating branch system which are divided according to the flow direction of seawater to be desalinated, and also comprises a vacuum pumping branch system, and a fresh water and seawater pollution discharge branch system, wherein the vacuum pumping branch system and the fresh water and seawater pollution discharge branch system are used as auxiliary systems connected with the seawater multi-stage fresh evaporation branch system. A multi-stage fresh evaporation method is adopted by the system. Because the waste heat of a condenser and boiler smoke of a power plant is utilized, energy sources needed for desalinating the seawater in a conventional distillation method are omitted, the operating cost in desalinating the seawater in a distillation method is reduced, and simultaneously the prepared fresh water is distilled water which can be partially used as supplementing water for the boiler of the power plant, the treatment cost for softening water in the power plant is saved, energy is saved, and the environment is protected.
Description
Technical field
The present invention relates to sea water desaltination field, particularly a kind of system of utilizing residual heat of electric power plant to desalinize seawater.
Background technology
The method of sea water desaltination is a lot, and that can accomplish maximization and industrialization is mainly embrane method and Re Fa.Embrane method is called again reverse osmosis method, and it is the principle of having utilized osmotic pressure.This method utilizes semi-permeable membranes to reach the fresh water object separated with salt.Under normal conditions, semi-permeable membranes allows the solvent in solution to pass through, and does not allow solute to see through.Because seawater saliferous is high, if seawater and freshwater is separated with semi-permeable membranes, fresh water can be diffused into by semi-permeable membranes a side of seawater, thereby the liquid level of seawater one side is raise, until certain height produces pressure, fresh water is no longer spread.This process is infiltration.If acted in a diametrically opposite way, obtain fresh water, as long as the seawater in semi-permeable membranes is pressed, will make the fresh water in seawater be penetrated into outside semi-permeable membranes, and salt tunicle is blocked in seawater, Here it is reverse osmosis method.Its major advantage is for saving the energy.
Hot method is conventional is divided into again distillation method and flash method.Distillation method is generally low temperature multiple-effect distillation, and its primary device is called vaporizer.In vaporizer, seawater is steam heated to temperature of saturation, and evaporates part water vapor, is fresh water after water recovery.Flash method is the principle by flash distillation, and seawater can flash off a part of steam from high environment to the low environment of pressure of pressure, will after this part vapor condenses, be fresh water.It compares advantage with reverse osmosis method be that the water quality of gained fresh water is higher, shortcoming for the energy consuming larger.
China's Coastal Areas is populous, and industry is flourishing, and the convenient transportation of bunker coal and a large amount of waters are considered in a lot of fuel-burning power plant, and a lot of addressings are near seashore.A large amount of waters in fuel-burning power plant comprise two parts, and a part is needed pure water and system self water that burns till steam of boiler, the fresh water of this part for processing; Another part is the recirculated water of cooling exhaust steam in steam turbine, and this part can be river or seawater; In the condenser of recirculated water after steam turbine, the exhaust steam in steam turbine after acting is condensed into water, the latent heat that exhaust steam condensation is emitted is taken away by this part recirculated water, fuel-burning power plant for seashore, recirculated water after this part intensification directly enters marine, cause very large energy dissipation, yet at present for the utilization of this low-temperature heat source, also there is no fine, feasible method.
The about 40 ℃ of left and right of condenser seawater recirculated water out, if temperature is carried out flash distillation preparing fresh thus, output and your efficiency are all very low, suppose to utilize 10 ℃ of temperature difference to carry out flash distillation preparing fresh, its enthalpy drop is only 42kj/kg, therefore every kilogram of 40 ℃ of seawater come flash distillation fresh water amount to be only about 0.017kg, if consider its power consumption cost, uneconomic beyond doubt with this preparing fresh again.
Condenser waste heat compared to above-mentioned power plant, the waste heat of boiler of power plant, although amount does not have condenser waste heat many, but the grade of energy is high, we know in boiler smoke contains sour gas, and when cigarette temperature is high, they can flow through each heating surface of boiler until be removed in thionizer with the form of gaseous state.When cigarette temperature is during lower than a certain temperature, their can with flue gas in water vapour be combined into sulfuric acid and corrode heat-exchange equipment; For avoiding the acid of heated surface at the end of boiler to reveal corrosion, exhaust gas temperature design is higher conventionally, and approximately 140 ℃ of left and right of discharge smoke temperature of power station boiler, if this part of heat energy can coordinate condenser to carry out sea water desaltination, must improve the efficiency of sea water desaltination.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of residual heat of electric power plant system that desalinizes seawater of utilizing, and utilizes the used heat of plant condenser recirculated water and residual heat from boiler fume to carry out flash distillation preparing fresh, can reduce like this cost of preparing fresh, saves the energy.
The present invention is by the following technical solutions:
Utilize the residual heat of electric power plant system that desalinizes seawater, comprising:
Condenser circulating seawer water intaking sub-system, the water outlet hydroecium of join aggregation condenser water outlet;
Seawater multistage flash evaporation sub-system, comprise a plurality of flash tanks, be respectively first step flash tank, second stage flash tank ... N level flash tank, the seawater that is gathered in described condenser water outlet hydroecium enters the condensation tube bank of the condensation tube bank of N-1 level flash tank, N-2 level flash tank ... the condensation tube bank of first step flash tank; The another final stage cooling system that connects of condensation tube bank of N level flash tank;
Residual heat from boiler fume heating cycle seawater sub-system, comprise flue gas waste heat recovery apparatus, described flue gas waste heat recovery apparatus is located in flue, seawater from first step flash tank condensation tube bank enters first step flash tank tank body, second stage flash tank tank body after described flue gas waste heat recovery apparatus ... until N level flash tank tank body, seawater flash distillation in each flash tank, forms fresh water after contacting with the condensation tube bank of each flash tank;
Vacuumize sub-system, described in vacuumize sub-system and comprise vaccum-pumping equipment, described vaccum-pumping equipment is connected with each flash tank tank body;
Fresh water and seawater blowdown sub-system, comprise fresh water pipeline and blowdown seawater pipeline, and described fresh water pipeline is connected with the water outlet of each flash tank, and the seawater of flash distillation does not enter blowdown seawater pipeline after by N level flash tank tank body.
Condenser circulating seawer water intaking sub-system of the present invention, wherein need the seawater of desalination from the recirculated water of fuel-burning power plant condenser, condenser circulating seawer water intake system comprises: Condenser Top tube bank, dividing plate, water outlet collector, filter screen, sea water preprocessing device, water pump; Described Condenser Top tube bank is positioned at the top of condenser, and the leaving water temperature(LWT) of recirculated water wants high compared to the temperature of the tube bank at other position of condenser here; Dividing plate and water outlet collector are separated recirculated water and other recirculated water that will take out, and make it enter water outlet collector; Water outlet collector is connected with filter screen, sea water preprocessing device, water pump successively, makes the seawater after heating enter multistage flash evaporation system.
Seawater multistage flash evaporation sub-system of the present invention comprises one or more sea water flash steaming pots (being illustrated as Pyatyi), wherein each flash tank is connected in series, the need that sea water preprocessing device comes desalinize seawater and are pressurizeed and flowed into successively fourth stage flash tank condensation tube bank, third stage flash tank condensation tube bank, second stage flash tank condensation tube bank, the condensation of first step flash tank and restrain by water pump, then remove boiler smoke-gas residual-heat recovering device; Seawater after heating goes flash distillation in flash tank again, flows to first step flash tank, check valve, second stage flash tank, check valve, third stage flash tank, check valve, fourth stage flash tank, check valve, level V flash tank successively by check valve; Fresh water water outlets at different levels are also connected successively;
The flash tank of seawater multistage flash evaporation sub-system of the present invention comprises flash tank condensation tube bank, balanced ventilation mouth, fresh water water outlet, flash tank tank body, steam purifier, between double flash evaporation tank, is connected with check valve;
Level V flash tank of the present invention is connected with and vacuumizes sub-system, fresh water and seawater blowdown sub-system, final stage cooling system; Pumped vacuum systems comprises a vacuum pumping pump, and vacuum meter maintains the vacuum tightness in flash tank, and pumped vacuum systems is connected with the balanced ventilation mouth on level V flash tank.Fresh water and seawater blowdown sub-system comprise fresh water transfer pump, seawater residual sea water pump, and fresh water transfer pump is connected with fresh water water outlet on level V flash tank, and seawater residual sea water pump is connected with the check valve on level V flash tank; Final stage cooling system is connected with level V flash tank condensation tube bank, and the water coolant of final stage cooling system is that recirculated water enters, the female pipe of backwater internal recycle seawater.
Residual heat from boiler fume heating cycle seawater sub-system of the present invention, while adopting corrosion-resistant flue gas waste heat recoverer form, thermal source is boiler exhaust gas waste heat, and corrosion-resistant flue gas waste heat recoverer is taked boiler economizer structure formation, and material adopts acid-resistant corrosion material.
Its material of corrosion-resistant flue gas waste heat recoverer of residual heat from boiler fume heating cycle seawater sub-system of the present invention also can be plain carbon stool material, specifically according to boiler smoke acid dew point height, determines;
Residual heat from boiler fume heating cycle seawater sub-system of the present invention, boiler smoke-gas residual-heat recovering device can also be divided into residual heat from boiler fume and reclaim heat release section and two parts of residual heat from boiler fume recovery endotherm section, and thermal source is residual heat from boiler fume; Between two parts of flue gas waste heat recovery heat release section and flue gas waste heat recovery endotherm section, circulatory mediator is the saturation steam of high temperature circulation water or natural circulation.
The present invention can be according to the processing power of sea water desaltination, and the high temperature section that extracts part recirculated water coordinates the waste heat recovery of boiler smoke, carries out multistage flash evaporation, preparing fresh, supplement the required fresh water of power plant self, simultaneously because the fresh water of obtaining is simple distillation water, save the cost of water treatment of power-plant makeup; Reclaim residual heat of electric power plant, energy-saving and emission-reduction.
The present invention or can be by the following technical solutions:
Utilize the residual heat of electric power plant system that desalinizes seawater, comprising:
Condenser circulating seawer water intaking sub-system, the water outlet hydroecium of join aggregation condenser water outlet;
Seawater flash distillation sub-system, comprises flash tank, and the seawater that is gathered in described condenser water outlet hydroecium enters flash tank tank body, the another cooling system that connects of condensation tube bank of described flash tank, and seawater is flash distillation in flash tank, after contacting, forms fresh water with the condensation tube bank of flash tank;
Vacuumize sub-system, described in vacuumize sub-system and comprise vaccum-pumping equipment, described vaccum-pumping equipment is connected with flash tank tank body;
Fresh water and seawater blowdown sub-system, comprise fresh water pipeline and blowdown seawater pipeline, and described fresh water pipeline is connected with the vapor-recovery unit on flash tank top, and the seawater of flash distillation does not enter blowdown seawater pipeline.
The present invention also can utilize separately plant condenser waste heat to desalinize seawater, and comprises the condenser in fuel-burning power plant and is attached thereto the water intake system connecing; Also comprise a flash tank and coupled pumped vacuum systems, steam and condensate system and drainage; Condenser and being attached thereto on the water intake system pipeline connecing, can also install (also can not installing additional) auxiliary heating system additional, and thermal source is the other forms of used heat of power plant, and condenser hot sea water is out heated, and facilitates preparing fresh; Flash tank also comprises the utility appliance such as flap and drainage, and flap act as separates the seawater of not flash distillation and the good fresh water of condensation; When the seawater of not flash distillation reaches certain liquid level, seawater is drained from drainage.Flash tank and coupled steam and condensate system, steam and condensate system mainly comprises water coolant tube bank, the low-temperature circulating water that water coolant is power plant.
Accompanying drawing explanation
Fig. 1 be the present invention relates to utilize the desalinize seawater schematic diagram of system of residual heat of electric power plant.
Fig. 2 the present invention relates to the desalinize seawater schematic diagram of single flash tank in system of residual heat of electric power plant for land productivity.
Fig. 3 is the schematic diagram that utilizes the condenser recirculated water sub-system that the residual heat of electric power plant system of desalinizing seawater comprises the present invention relates to.
Fig. 4 be the present invention relates to utilize the desalinize seawater schematic diagram of a kind of embodiment of flue gas waste heat recovery apparatus 1 of system of residual heat of electric power plant.
Fig. 5 be the present invention relates to utilize the desalinize seawater schematic diagram of another kind of embodiment of flue gas waste heat recovery apparatus 1 of system of residual heat of electric power plant.
Fig. 6 be the present invention relates to utilize the desalinize seawater part schematic diagram of condenser circulating seawer water intaking sub-system of system of residual heat of electric power plant.
Fig. 7 is utilize residual heat of electric power plant the to desalinize seawater systematic schematic diagram that single condenser waste heat of system desalinizes seawater the present invention relates to.
Fig. 8 be the present invention relates to utilize the desalinize seawater schematic diagram of auxiliary heating system 30 of system of residual heat of electric power plant.
Embodiment
Referring to Fig. 1, for what the present invention relates to, utilize the desalinize seawater schematic diagram of system of residual heat of electric power plant.Utilize the residual heat of electric power plant system that desalinizes seawater, comprise the water intaking of condenser circulating seawer sub-system, seawater multistage flash evaporation sub-system, residual heat from boiler fume heating cycle seawater sub-system, vacuumize sub-system, fresh water and seawater blowdown sub-system.
The water outlet hydroecium 22 of described condenser circulating seawer water intaking sub-system join aggregation condenser water outlet.Described seawater multistage flash evaporation sub-system comprises a plurality of flash tanks, is respectively first step flash tank 3, second stage flash tank 4 ... N level flash tank.Referring to Fig. 2, for the present invention relates to the desalinize seawater schematic diagram of single flash tank in system of residual heat of electric power plant for land productivity.In conjunction with Fig. 1, the seawater that is gathered in described condenser water outlet hydroecium 22 enters the condensation tube bank 15 of the condensation tube bank 15 of N-1 level flash tank, N-2 level flash tank ... the condensation tube bank 15 of first step flash tank 3; The another final stage cooling system that connects of condensation tube bank 15 of N level flash tank.In the present embodiment, Multi-stage flash steaming pot has Pyatyi, and seawater enters from the condensation tube bank 15 of fourth stage flash tank 6, successively through the 3rd, second, the condensation tube bank 15 of first step flash tank 5,4,3.Described residual heat from boiler fume heating cycle seawater sub-system, comprise flue gas waste heat recovery apparatus 1, described flue gas waste heat recovery apparatus 1 is located in flue gas flue, seawater from the 3 condensation tube banks 15 of first step flash tank enters first step flash tank tank body 18, second stage flash tank tank body 18 after described flue gas waste heat recovery apparatus 1 ... until N level flash tank tank body 18, in the present embodiment, seawater enters first, second successively ... level V flash tank tank body 18.Seawater flash distillation in each flash tank, forms fresh water after contacting with the condensation tube bank of each flash tank.
The described sub-system that vacuumizes comprises vaccum-pumping equipment, and described vaccum-pumping equipment is connected with each flash tank tank body 18.Preferably, vaccum-pumping equipment comprises vacuum pumping pump 10 and a plurality of vacuum meter 13, and described vacuum pumping pump 10 is connected with N level flash tank, and described vacuum meter 13 is located in each flash tank.On described each flash tank, be all provided with balanced ventilation mouth 16, described vacuum pumping pump 10 is connected with the balanced ventilation mouth 16 of N level flash tank, and the balanced ventilation mouth 16 of other flash tank is located between adjacent flash tank.
Described fresh water and seawater blowdown sub-system comprise fresh water pipeline and blowdown seawater pipeline, and described fresh water pipeline is connected with the water outlet of each flash tank, and the seawater of flash distillation does not enter blowdown seawater pipeline after by N level flash tank tank body 18.
The residual heat of electric power plant system that desalinizes seawater of utilizing the present invention relates to also comprises condenser recirculated water sub-system, referring to Fig. 3, described condenser recirculated water sub-system comprises the female pipe of recirculated water water inlet, the female pipe of recirculated water backwater, the female pipe of described recirculated water water inlet connects respectively the import (water inlet hydroecium 21) of described condenser 23, and the import of described final stage cooling system, the female pipe of described recirculated water backwater connects respectively answer back (the backwater hydroecium 20) of described condenser 23, the outlet of the outlet of described final stage cooling system and described blowdown seawater pipeline.
Referring to Fig. 4, for what the present invention relates to, utilize the desalinize seawater schematic diagram of a kind of embodiment of flue gas waste heat recovery apparatus 1 of system of residual heat of electric power plant.Described flue gas waste heat recovery apparatus 1 is tube bank, from the seawater of first step flash tank 3 condensations tube banks 15, from the tube bank import of flue 101, enters, and after tube bank, from the tube bank of flue 103, exports out.The material of the tube bank of described flue gas waste heat recovery apparatus 1 is acid-resistant corrosion material or common charcoal steel.
Flue gas waste heat recovery apparatus 1 can be also another kind of form, referring to Fig. 5, for what the present invention relates to, utilizes the desalinize seawater schematic diagram of another kind of embodiment of flue gas waste heat recovery apparatus 1 of system of residual heat of electric power plant.Described flue gas waste heat recovery apparatus 1 comprises heat release section 105 and endotherm section 104, described heat release section 105 is connected with endotherm section 104, form circulation line, in pipeline, there is circulatory mediator to flow, described endotherm section 104 is located in flue, from the seawater of first step flash tank 3 condensations tube banks 15, enters first step flash tank tank body 18 after described heat release section 105 is heated.Circulatory mediator is the saturation steam of high temperature circulation water or natural circulation.
Referring to Fig. 6, for what the present invention relates to, utilize the desalinize seawater part schematic diagram of condenser circulating seawer water intaking sub-system of system of residual heat of electric power plant.In the water outlet hydroecium 22 of described condenser circulating seawer water intaking sub-system, be provided with dividing plate 222, and described dividing plate 222 is located at the top of described water outlet hydroecium 22, the bank of condenser pipes that described dividing plate 222 isolates is connected with described seawater multistage flash evaporation sub-system by water outlet collector 221, the bank of condenser pipes of other water outlet concentrates on backwater hydroecium 20, by the female pipe of recirculated water main water outlet pipe and recirculated water backwater, is connected.
Get back to Fig. 3, described condenser circulating seawer water intaking sub-system also comprises filter screen 19 and sea water preprocessing device 11, and the sea water filter net 19 of described pass-out water hydroecium 22, sea water preprocessing device 11 enter described seawater multistage flash evaporation sub-system.
Now, according to the flow process from seawater to fresh water, set forth embodiment of the present invention:
As shown in Figure 3, condenser 23 is comprised of a large amount of tube banks, the intake low temperature seawater of female Guan Lai of recirculated water is walked in tube bank, the exhaust steam that steam turbine comes is walked outside pipe, when cryogenic tube bundle is passed through in the exhaust steam when steam turbine, waste heat is emitted in condensation rapidly, self become the water of condensation well that reduces phlegm and internal heat, and recirculated water is intake, the recirculated water of female Guan Lai has absorbed exhaust steam condensation and has emitted waste heat, temperature raises, and for general big-and-middle-sized Power Plant, temperature generally approaches 40 ℃ of left and right, this part water is directly drained by recirculated water main water outlet pipe, causes very large waste; The present invention is at water outlet hydroecium 22 tops, by dividing plate 222, separate the recirculated water of some Condenser Top tube banks 231, by water outlet collector 221, draw seawater multistage flash evaporation sub-system, dividing plate 222 radians are large as much as possible, without dead angle, guarantee that the glueballs of cleaning condenser 23 can freely be come in and gone out.
The seawater recirculated water of water outlet collector 221, first passes through filter screen 19, this filter screen 19 on the one hand can filtration cycle water in impurity, can collect the glueballs that cleans condenser 23 on the one hand, when plant condenser 23 carries out after glueballs flushing, this filter screen 19 should be opened taking-up glueballs, rinses.
Seawater is introduced into sea water preprocessing device 11, at this, remove the impurity such as silt, and then in water pump 12 input multistage flash evaporation sub-systems, the circulating seawer of 40 ℃ of left and right, is introduced into the flash tank condensation tube bank 15 in fourth stage flash tank 6, and circulating seawer is now as the water coolant of fourth stage flash tank 6, the steam of condensation fourth stage flash tank 6 flash distillations, absorb heat, self temperature raises, and suppose that rising is 45 ℃; And then remove the steam of third stage flash tank 5 condensation third stage flash tank 5 flash distillations, and it is 50 ℃ that temperature raises, and flows successively, when from the 3 condensations tube banks 15 of first step flash tank out time, the temperature that now needs to desalinate circulating seawer is 60 ℃.
The circulating seawer temperature that multistage flash evaporation is come is 60 ℃, now enters boiler smoke-gas residual-heat recovering device 1 heating again; Boiler smoke-gas residual-heat recovering device 1 of the present invention can be two kinds of structure formations, and one is corrosion-resistant flue gas waste heat recoverer 102 forms; In boiler of power plant flue gas, contain sour gas and have corrodibility, so flue gas waste heat recovery apparatus 1 selects corrosion-resistant material manufacture, corrosion-resistant flue gas waste heat recoverer 102 is economizer form structure, and its import connects flue 101, and outlet connects flue 103; Flue gas, through corrosion-resistant flue gas waste heat recoverer 102, passes to the waste heat of flue gas in the seawater coming from condenser 23 tube banks; From technical background data, the funnel temperature of boiler is about 140 ℃ of left and right, and according to the desalination output of seawater and concrete boiler smoke tolerance, now our hypothesis is heated to 80 ℃ of left and right circulating seawer.
If we calculate the characteristic of boiler smoke, we can obtain different smoke components, the temperature of its flue gas acid dew point, now again according to the desalination output of seawater and concrete boiler smoke tolerance, arrange the temperature of the suitable seawater that enters boiler smoke-gas residual-heat recovering device 1, now corrosion-resistant flue gas waste heat recoverer 102 can be selected common material manufacture and can not revealed corrosion by boiler smoke acid.
Be similarly and avoid boiler smoke acid to reveal corrosion, flue gas waste heat recovery apparatus 1 can also be Fig. 5 form, be divided into residual heat from boiler fume and reclaim heat release section 105 and 104 two parts of residual heat from boiler fume recovery endotherm section, boiler smoke reclaims endotherm section 104 through residual heat from boiler fume, fume afterheat is passed to circulatory mediator---the saturation steam of high temperature circulation water or natural circulation, high temperature circulation water reclaims in heat release section 105 heat is passed to the seawater that will heat at residual heat from boiler fume again, after high temperature circulation water cooling, getting back to again flue gas waste heat recovery endotherm section 104 reheats, so circulation, realize boiler of power plant fume afterheat is passed to the seawater that multistage flash evaporation system is come, by the temperature of controlled circulation medium, can prevent the acid dew corrosion of flue gas waste heat recovery endotherm section 104.
80 ℃, seawater after boiler smoke-gas residual-heat recovering device 1 heating, now by check valve 2, enter first step flash tank 3 and carry out flash distillation, the steam producing is met flash tank condensation tube bank 15 and is condensed into distilled water after steam purifier 14, by fresh water water outlet 17, flow to next stage flash tank, finally at level V flash tank 7, by fresh water transfer pump 9, taken away; The seawater of flash distillation does not flow to next stage flash tank through check valve 2 and continues flash distillation, until level V flash tank 7, because of seawater temperature temperature is now lower, for obtaining more fresh water, now with the water coolant that recirculated water enters backwater mother pipe, carrys out the steam of condensation flash distillation.
For seawater flash distillation, Multi-stage flash steaming pot need to maintain certain vacuum tightness, this seawater desalination system is furnished with pumped vacuum systems, pumped vacuum systems comprises a vacuum pumping pump 10, a plurality of vacuum meters 13, maintain the vacuum tightness in each flash tank, pumped vacuum systems is connected with the balanced ventilation mouth 16 on level V flash tank 7.Other balanced ventilation mouths 16, between every double flash evaporation tank, hold together Multi-stage flash steaming pot.
Owing to being negative pressure with respect to external atmosphere pressure in Multi-stage flash steaming pot, the fresh water of therefore producing and the last not seawater of flash distillation all need to be extracted by pump additional pressure, and the present invention is furnished with fresh water transfer pump 9, seawater residual sea water pump 8.
The power consumption of each pump of energy consumption that whole system is total, other do not need the extra energy to carry out heating seawater, so energy-conserving and environment-protective, reduce the processing cost of sea water desaltination.It shown in Fig. 1 of the present invention, is only the sea water desaltination of part recirculated water, for maximizing and industrialization, the recirculated water of whole water outlet hydroecium 22 can be drawn and desalinated, its principle, system flow are the same with figure mono-, the present invention is only Pyatyi flash system, in implementation process, according to fresh water treatment amount, residual heat of electric power plant reclaims scale, can be designed to a certain progression that needs.
The residual heat of electric power plant system of desalinizing seawater of utilizing the present invention relates to can also be utilized separately the enforcement that desalinizes seawater of condenser waste heat.Referring to Fig. 7, the systematic schematic diagram desalinizing seawater for single condenser waste heat.Comprise the water intaking of condenser circulating seawer sub-system, seawater flash distillation sub-system, vacuumize sub-system, fresh water and seawater blowdown sub-system.Water outlet hydroecium 22, the filter screen of 23 water outlets of described condenser circulating seawer water intaking sub-system join aggregation condenser.Described seawater flash distillation sub-system comprises flash tank, in the present embodiment, flash tank can be single, the seawater that is gathered in described condenser 23 water outlet hydroeciums 22 enters flash tank tank body by filter screen, the another cooling system that connects of condensation tube bank 26 of described flash tank, the circulatory mediator in described cooling system is low-temperature circulating water or boiler low-temperature supplementary feed.Seawater, in the interior flash distillation of flash tank 27, forms fresh water after contacting with the condensation tube bank 26 of flash tank 27.The described sub-system that vacuumizes comprises vaccum-pumping equipment, and described vaccum-pumping equipment is connected with flash tank 27 tank bodies.Preferably, described in vacuumize sub-system vaccum-pumping equipment comprise vacuum pumping pump 25, described vacuum pumping pump 25 is connected with the top of flash tank 27.Described fresh water and seawater blowdown sub-system comprise fresh water pipeline and blowdown seawater pipeline, and described fresh water pipeline is connected with the vapor-recovery unit on flash tank 27 tops, and the seawater of flash distillation does not enter blowdown seawater pipeline by residual sea water pump 31.
This form also comprises condenser recirculated water sub-system, described condenser recirculated water sub-system comprises the female pipe of recirculated water water inlet, the female pipe of recirculated water backwater, the female pipe of described recirculated water water inlet connects the import of described cooling system by valve 24, the female pipe of described recirculated water backwater connects the outlet of cooling system by valve 24.
In the water outlet hydroecium 22 of condenser circulating seawer water intaking sub-system, be provided with dividing plate 222, and described dividing plate 222 is located at the top of described water outlet hydroecium 22, the bank of condenser pipes that described dividing plate 222 isolates is connected with described seawater flash distillation sub-system, and other water outlet bank of condenser pipes is connected by the female pipe of recirculated water main water outlet pipe and recirculated water backwater.
In addition, described condenser circulating seawer water intaking sub-system also comprises boosting sub-system, described boosting sub-system comprises tube still heater 301, the seawater of described water outlet hydroecium 22 enters described flash tank 27, the waste hot steam that the thermal source of described tube still heater 301 is power plant after described tube still heater 301 heating.
In the circulating seawer access flash tank 27 of 40 ℃ that the present invention can carry out steam trap, the circulating seawer of 40 ℃ of left and right, in flash tank 27, because pressure sharply reduces, flash distillation rapidly; Steam upwards, through condensation tube bank 26, is condensed into fresh water, reaches the fresh water object separated with salinity; Water of condensation falls into the vapour-condensing equipment for recovering 28 on flash tank 27 tops, then is drawn by pipeline, can, as the supplementary feed of thermal power plant self feedwater, also can make other purposes; In circulating seawer, the unevaporated seawater of part directly enters in the female pipe of recirculated water backwater; Low temperature cold source as condensed steam can be a fraction of low-temperature circulating water, also can be for boiler low-temperature supplementary feed, its temperature should be lower than the flash vaporization point of circulating seawer.
In order to make circulating seawer flash distillation, the interior needs of flash tank 27 maintain certain vacuum tightness, and the circulating seawer temperature of supposing to enter flash tank 27 is 40 ℃, and the pressure of its corresponding saturation water is P
40, therefore, now the absolute pressure in flash tank 27 should be less than P
40, make circulating seawer explosive evaporatoin.Vacuum tightness in flash tank 27 is provided by vacuum pump and maintains, and for the incondensable gas being mixed with in flash tank 27, also by vacuum pump, siphons away in the lump discharge.
In water intake system, can also increase by an auxiliary heating system 30, the seawater recirculated water coming from condenser 23 tube banks is reheated; Auxiliary heating system 30 can be structure shown in Fig. 8: comprise tubular heat exchange, the seawater that water fetching device comes is sent in flash tank 27 by water pump 29 after tube still heater 301 heating again, the thermal source of tube still heater 301 is the waste hot steam of power plant, seawater after heating is for preventing fouling, temperature is unsuitable too high, generally lower than 100 ℃.
The total energy consumption of whole system is the power consumption that vacuum pump adds water pump, and other do not need the extra energy to carry out heating seawater, so energy-conserving and environment-protective, reduces the processing cost of sea water desaltination.
The fresh water of producing is distilled water, and as the moisturizing of boiler, better than the soft water of water treatment of power plant, the present invention can replace the water treatment device of power plant, improves economy of power plant benefit.
Claims (15)
1. utilize the residual heat of electric power plant system that desalinizes seawater, it is characterized in that comprising:
Condenser (23) circulating seawer water intaking sub-system, the water outlet hydroecium (22) of join aggregation condenser (23) water outlet;
Seawater multistage flash evaporation sub-system, comprise a plurality of flash tanks, be respectively first step flash tank (3), second stage flash tank (4) ... N level flash tank, the seawater that is gathered in described condenser (23) water outlet hydroecium (22) enters the condensation tube bank (15) of the condensation tube bank (15) of N-1 level flash tank, N-2 level flash tank ... the condensation tube bank (15) of first step flash tank (3); The condensation tube bank (15) of N level flash tank separately connects final stage cooling system, is equipped with refining plant (14) in described flash tank; Also comprise condenser recirculated water sub-system, described condenser recirculated water sub-system comprises the female pipe of recirculated water water inlet, the female pipe of recirculated water backwater, the female pipe of described recirculated water water inlet connects respectively the import of described condenser (23), and the import of described final stage cooling system, the female pipe of described recirculated water backwater connects respectively answering back of described condenser (23), and the outlet of described final stage cooling system;
Residual heat from boiler fume heating cycle seawater sub-system, comprise flue gas waste heat recovery apparatus (1), seawater from first step flash tank (3) condensation tube bank (15) enters first step flash tank tank body (18), second stage flash tank tank body (18) after described flue gas waste heat recovery apparatus (1) ... until N level flash tank tank body (18), seawater flash distillation in each flash tank, forms fresh water after contacting with the condensation tube bank (15) of each flash tank;
Vacuumize sub-system, described in vacuumize sub-system and comprise vaccum-pumping equipment, described vaccum-pumping equipment is connected with each flash tank tank body (18);
Fresh water and seawater blowdown sub-system, comprise fresh water pipeline and blowdown seawater pipeline, and described fresh water pipeline is connected with the water outlet of each flash tank, and the seawater of flash distillation does not enter blowdown seawater pipeline after by N level flash tank tank body (18).
2. the residual heat of electric power plant system that desalinizes seawater of utilizing according to claim 1, it is characterized in that: also comprise condenser recirculated water sub-system, described condenser recirculated water sub-system comprises the female pipe of recirculated water water inlet, the female pipe of recirculated water backwater, the female pipe of described recirculated water water inlet connects the import of described condenser (23), the female pipe of described recirculated water backwater connects respectively answering back of described condenser (23), and the outlet of described blowdown seawater pipeline.
3. the residual heat of electric power plant system that desalinizes seawater of utilizing according to claim 1, it is characterized in that: described in vacuumize sub-system vaccum-pumping equipment comprise vacuum pumping pump (10) and a plurality of vacuum meter (13), described vacuum pumping pump (10) is connected with N level flash tank, and described vacuum meter (13) is located in each flash tank.
4. the residual heat of electric power plant system that desalinizes seawater of utilizing according to claim 3, it is characterized in that: on described each flash tank, be all provided with balanced ventilation mouth (16), described vacuum pumping pump (10) is connected with the balanced ventilation mouth (16) of N level flash tank, and the balanced ventilation mouth (16) of other flash tank is located between adjacent flash tank.
5. the residual heat of electric power plant system that desalinizes seawater of utilizing according to claim 1, it is characterized in that: described flue gas waste heat recovery apparatus (1) is tube bank, seawater from first step flash tank (3) condensation tube bank (15) enters from the tube bank import of flue gas flue (103), after tube bank, from the tube bank of flue gas flue (101), export out.
6. the residual heat of electric power plant system that desalinizes seawater of utilizing according to claim 5, is characterized in that: the material of the tube bank of described flue gas waste heat recovery apparatus (1) is acid-resistant corrosion material or common charcoal steel.
7. the residual heat of electric power plant system that desalinizes seawater of utilizing according to claim 1, it is characterized in that: described flue gas waste heat recovery apparatus (1) comprises heat release section (105) and endotherm section (104), described heat release section (105) is connected with endotherm section (104), form circulation line, in pipeline, there is circulatory mediator to flow, described endotherm section (104) is located in flue, and the seawater of restraining (15) from first step flash tank (3) condensation enters first step flash tank tank body (18) after described heat release section (105) is heated.
8. the residual heat of electric power plant system that desalinizes seawater of utilizing according to claim 7, is characterized in that: circulatory mediator is the saturation steam of high temperature circulation water or natural circulation.
9. according to utilizing the residual heat of electric power plant system that desalinizes seawater described in any one in claim 1-2, it is characterized in that: in the water outlet hydroecium (22) that condenser circulating seawer water intaking sub-system connects, be provided with dividing plate (222), and described dividing plate (222) is located at the top of described water outlet hydroecium (22), the bank of condenser pipes that described dividing plate (222) isolates is connected with described seawater multistage flash evaporation sub-system by water outlet collector (221), and other water outlet bank of condenser pipes is connected by the female pipe of recirculated water main water outlet pipe and recirculated water backwater.
10. the residual heat of electric power plant system that desalinizes seawater of utilizing according to claim 9, it is characterized in that: described condenser circulating seawer water intaking sub-system also comprises filter screen (19) and sea water preprocessing device (11), and the seawater of described water outlet hydroecium (22) enters described seawater multistage flash evaporation sub-system by filter screen (19), sea water preprocessing device (11).
11. 1 kinds are utilized the residual heat of electric power plant system that desalinizes seawater, it is characterized in that comprising:
Condenser circulating seawer water intaking sub-system, the water outlet hydroecium (22) of join aggregation condenser (23) water outlet, in the water outlet hydroecium (22) that described condenser circulating seawer water intaking sub-system connects, be provided with dividing plate (222), and described dividing plate (222) is located at the top of described water outlet hydroecium (22), the bank of condenser pipes that described dividing plate (222) isolates is connected with described seawater flash distillation sub-system, and other water outlet bank of condenser pipes is connected by the female pipe of recirculated water main water outlet pipe and recirculated water backwater;
Seawater flash distillation sub-system, comprise flash tank (27), the seawater that is gathered in described condenser water outlet hydroecium (22) enters flash tank tank body, the condensation tube bank (26) of described flash tank (27) separately connects cooling system, seawater flash distillation in flash tank (27), forms fresh water after contacting with the condensation tube bank (26) of flash tank (27); Described condenser circulating seawer water intaking sub-system also comprises boosting sub-system, described boosting sub-system comprises tube still heater (301), the seawater of described water outlet hydroecium (22) enters described flash tank (27), the waste hot steam that the thermal source of described tube still heater (301) is power plant after described tube still heater (301) heating;
Vacuumize sub-system, described in vacuumize sub-system and comprise vaccum-pumping equipment, described vaccum-pumping equipment is connected with flash tank tank body;
Fresh water and seawater blowdown sub-system, comprise fresh water pipeline and blowdown seawater pipeline, and described fresh water pipeline is connected with the vapor-recovery unit on flash tank (27) top, and the seawater of flash distillation does not enter blowdown seawater pipeline.
The 12. residual heat of electric power plant systems that desalinize seawater of utilizing according to claim 11, it is characterized in that: also comprise condenser recirculated water sub-system, described condenser recirculated water sub-system comprises the female pipe of recirculated water water inlet, the female pipe of recirculated water backwater, the female pipe of described recirculated water water inlet connects the import of described cooling system, and the female pipe of described recirculated water backwater connects the outlet of cooling system.
The 13. residual heat of electric power plant systems that desalinize seawater of utilizing according to claim 11, is characterized in that: described in vacuumize sub-system vaccum-pumping equipment comprise vacuum pumping pump (25), described vacuum pumping pump (25) is connected with the top of flash tank (27).
The 14. residual heat of electric power plant systems that desalinize seawater of utilizing according to claim 11, is characterized in that: the circulatory mediator in described cooling system is low-temperature circulating water or boiler low-temperature supplementary feed.
The 15. residual heat of electric power plant systems that desalinize seawater of utilizing according to claim 11, is characterized in that: described condenser circulating seawer water intaking sub-system also comprises filter screen, and the seawater of described water outlet hydroecium (22) enters described seawater flash distillation sub-system by filter screen.
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| CN201210138159.0A CN102642883B (en) | 2012-05-07 | 2012-05-07 | System for desalinating seawater by waste heat from power plant |
| PCT/CN2013/072511 WO2013166882A1 (en) | 2012-05-07 | 2013-03-13 | System for desalination of seawater by using waste heat from power plant |
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| CN201210138159.0A CN102642883B (en) | 2012-05-07 | 2012-05-07 | System for desalinating seawater by waste heat from power plant |
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Families Citing this family (17)
| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2013166882A1 (en) * | 2012-05-07 | 2013-11-14 | 上海伏波环保设备有限公司 | System for desalination of seawater by using waste heat from power plant |
| CN102877902B (en) * | 2012-10-12 | 2014-07-23 | 凤阳海泰科能源环境管理服务有限公司 | Electricity-water co-production system implemented through waste heat recovery |
| CN104089276A (en) * | 2014-06-24 | 2014-10-08 | 首钢京唐钢铁联合有限责任公司 | Multistage flash evaporation treatment system utilizing dead steam and circulating cooling water |
| CN104030385B (en) * | 2014-06-30 | 2016-10-19 | 上海伏波环保设备有限公司 | Utilize the indirect low temperature multi-effect seawater desalting system of engine of boat and ship exhaust heat |
| CN104193062B (en) * | 2014-09-02 | 2018-08-28 | 集美大学 | Utilize the more technology coupling seawater desalination plants and its method of low-temperature heat source |
| CN104402159B (en) * | 2014-11-28 | 2016-01-27 | 浙江大学 | A kind of board-like multistage flash evaporation desulfurization wastewater disposal and recovery devices and methods therefor |
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| CN107128993B (en) * | 2017-05-04 | 2020-08-07 | 国家海洋局天津海水淡化与综合利用研究所 | Power plant flue gas waste heat direct evaporation type desalination system with flue gas reheating function |
| CN107854858B (en) * | 2017-10-27 | 2020-04-17 | 中石化宁波工程有限公司 | Multi-stage flash tank |
| CN107676842B (en) * | 2017-11-02 | 2019-09-27 | 清华大学 | The system of hydro-thermal alliance and the regulation method of the system are realized using residual heat of electric power plant |
| CN110713219A (en) * | 2019-10-12 | 2020-01-21 | 申杰涛 | Multistage flash evaporation technology and device for flash evaporation of flow flash evaporation surface |
| CN110759405B (en) * | 2019-11-06 | 2021-02-05 | 山东大学 | Waste heat utilization process and system for seawater direct-flow cooling water of power plant |
| CN212403523U (en) * | 2020-06-19 | 2021-01-26 | 北京清建能源技术有限公司 | Preparation device of hot purified water |
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