CN103663589B - Seawater desalinization method and seawater desalinization device - Google Patents
Seawater desalinization method and seawater desalinization device Download PDFInfo
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- CN103663589B CN103663589B CN201310686162.0A CN201310686162A CN103663589B CN 103663589 B CN103663589 B CN 103663589B CN 201310686162 A CN201310686162 A CN 201310686162A CN 103663589 B CN103663589 B CN 103663589B
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- 239000013535 sea water Substances 0.000 title claims abstract description 146
- 238000000034 method Methods 0.000 title claims abstract description 49
- 239000013505 freshwater Substances 0.000 claims abstract description 184
- 238000009833 condensation Methods 0.000 claims abstract description 94
- 230000005494 condensation Effects 0.000 claims abstract description 94
- 238000001704 evaporation Methods 0.000 claims abstract description 73
- 230000008020 evaporation Effects 0.000 claims abstract description 58
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 55
- 239000012267 brine Substances 0.000 claims abstract description 32
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 32
- 239000006200 vaporizer Substances 0.000 claims description 133
- 238000002347 injection Methods 0.000 claims description 34
- 239000007924 injection Substances 0.000 claims description 34
- 238000005507 spraying Methods 0.000 claims description 24
- 238000011033 desalting Methods 0.000 claims description 21
- 238000010521 absorption reaction Methods 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims description 8
- 230000008569 process Effects 0.000 claims description 7
- 239000003643 water by type Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 4
- 238000012546 transfer Methods 0.000 claims description 4
- 238000010276 construction Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 abstract description 3
- 230000003134 recirculating effect Effects 0.000 abstract 1
- 239000012530 fluid Substances 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 10
- 238000009834 vaporization Methods 0.000 description 10
- 230000008016 vaporization Effects 0.000 description 10
- 238000005265 energy consumption Methods 0.000 description 7
- 238000001223 reverse osmosis Methods 0.000 description 7
- 239000007921 spray Substances 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000010865 sewage Substances 0.000 description 5
- 238000010612 desalination reaction Methods 0.000 description 4
- 230000002829 reductive effect Effects 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 3
- 238000011161 development Methods 0.000 description 3
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- 230000008859 change Effects 0.000 description 2
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- 230000007547 defect Effects 0.000 description 2
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- 238000012423 maintenance Methods 0.000 description 2
- 230000036961 partial effect Effects 0.000 description 2
- 230000002093 peripheral effect Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000001055 chewing effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
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- 238000011835 investigation Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
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- 230000009347 mechanical transmission Effects 0.000 description 1
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- 239000012266 salt solution Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009923 sugaring Methods 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
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- 239000002699 waste material Substances 0.000 description 1
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Classifications
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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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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides to a seawater desalinization method and a seawater desalinization device. The method comprises the steps as follows: firstly, introducing seawater passing through a heat exchanger into an evaporator directly, or running seawater in a fresh water circulation box containing another built-in heat exchanger, absorbing heat from the fresh water inside the fresh water circulation box and then introducing the seawater into the evaporator; secondly, evaporating the seawater in the evaporator; thirdly, condensing the water vapor generated from the seawater inside the evaporator in a condensation ejector, feeding back the latent heat of the water vapor to the fresh water to increase the temperature of the fresh water, sucking the water vapor into the evaporator by an ejection recirculating pump to exchange heat with the seawater and further lower the temperature of the fresh water, and receiving the latent heat fed back by the water vapor generated from the evaporation of seawater at the condensation ejector; fourthly, discharging strong brine generated from evaporation of the seawater through a strong brine discharge pump. The invention further provides a device for conducting the seawater desalinization method. The device is small in size and in space usage, stable and reliable in operation, high in work efficiency and large in evaporation capacity, low in power source consumption and good in quality of the fresh water produced by the device, and no air-suction device is required.
Description
Technical field
The present invention relates to a kind of method for desalting seawater and device.
Background technology
" water " is a very large problem.Statesman says " war of world's contention in future resource will be caused by water "; Scientist says " water is irreplaceable ", " water can not complete science proposition forever "; Economist foretells " after energy dilemma, next crisis will take turns to water crisis ".Great mass of data and treatise show, if the mankind also fetch water as it is and use water, will produce a series of serious consequence; Resource is once exhaust, and expanding economy, the various ecosystem and human health and existence all will be on the hazard.Estimate in 21st century, water to the importance of the mankind by with oil 20th century importance to the mankind the same, water will become a kind of scarce commodity determining national wealth.Water industry will be 21st century maximum industries.In tellurian gross amount of water resources, fresh water only accounts for 2. 5 %, and seawater accounts for 97. 5 %, and in a sense, seawater is only inexhaustible, nexhaustible main water source.Therefore, development desalination technology, wants fresh water to be solve the most effective means of Freshwater resources imbalance between supply and demand to ocean.China be a water resources extremely shortage country.Gross amount of water resources only has 2. 81 tcms, occupies the 6th, the world, but water resources is the 108th, the world per capita, is one of 21 poor-waters country in the world.Special is one of most water-deficient area of China in Northern Coastal Provinces.Consider the factors such as Northern Coastal Provinces population growth, industrial structure change, agricultural development and Eco-environmental Water Consumption demand, predict nearly ten years, coastal 4 provinces (city) of northern China per capita comprehensive water-using amount will reach 325 ~ 365 M respectively
3with 350 ~ 400 M
3, lack of water total amount will reach 166 ~ 25,500,000,000 M respectively
3with 273 ~ 39,300,000,000 M
3; Meanwhile, consider the poor and resources water shortage situation of the water quality of southern coastal some areas, the lack of water situation of coastland will be severeer.Sea water desaltination is one of fundamental way solving coastland water scarcity, the Freshwater resources bottleneck having become the development of restriction Chinese national economy and living standards of the people raising in short supply.
Existing method for desalting seawater mainly contains distillation method, high pressure reverse osmosis method, low-temperature multi-effect method, cold method, multistage flash vaporization, electroosmose process, ion exchange method etc.All there is certain defect in these methods.The apparatus structure used is more complicated, and manufacturing cost is higher, and operation energy consumption is high.Current main stream approach is: these three kinds of methods of low-temperature multi-effect method, multistage flash vaporization, high pressure reverse osmosis method.Situation according to 2007 annual sea water desaltination markets is added up, in Middle East, the share of market of multistage flash vaporization (MSF) has exceeded 70 %, and low-temperature multi-effect method (MED) remains basically stable with the share of market of reverse osmosis method (RO); And in other each continents, the share of market of reverse osmosis method (RO) is all the highest.Because the Middle East market share occupies 74 % of world market, so the proportion of multistage flash vaporization (MSF) in three kinds of mainstream technologys or maximum.Multistage flash evaporation (MSF) and low-temperature multi-effect (MED) also have the main technical characteristics of reverse osmosis method (RO) to be: multistage flash evaporation (MSF) current consumption 4. 0 ~ 5. 5 kWh/ ton, its scale and capacity are maximum now, also lower to raw material water quality requirement, fouling of heat exchangers is medium, running top temperature is at 90 ~ 112 DEG C, but equipment cost is higher.Low-temperature multi-effect method (MED) current consumption is 2. 5 ~ 3. 5kWh/ tons, and industrial scale and capacity can only be medium, and fouling of heat exchangers degree is lower, medium to raw material water quality requirement, and operating temperature reaches about 70 DEG C.The current consumption of reverse osmosis method (RO) is 4.5 ~ 5.5kWh/ ton, and fresh water production scale and capacity can only be medium, and equipment scaling degree is medium, very high to raw material water quality requirement, and running cost is also very high, can carry out at normal temperatures.
Multiple-effect and multistage seawater desalting technology all need vapor jet pump, and energy consumption is high, and induction efficiency is lower, and mostly need set up suction air device and set up the condensation that special condenser is specifically designed to steam, and working efficiency is lower.Use more multistage flash vaporization sea water desalting equipment, also need to set up suction air device, and aspiration is less, vacuum tightness is lower, steam output is also low, energy consumption is high, and vacuum duration state is poor.At present, China's sea water desaltination cost is approximately about 5 yuan/ton, far away higher than tap water cost.In the world today, extensive sea water desalinating plant adopts multistage flash vaporization exactly, although technology is carried out in the decompression of this Technology application, but need to inject more heat energy, go the temperature of cooling water of condensing water vapor substantially similar with envrionment temperature, its freshwater product temperature is out generally higher than envrionment temperature, and its strong brine temperature of discharging is also more than 43 DEG C.And use more desalination technology to be high pressure reverse osmosis technology at present, though this technical costs declines to some extent, still will consume more electric energy, also will consume other material, its cost also can not be despised, and the fresh water quality of making is also not ideal enough.Chinese patent 201210276447.2 discloses " a kind of heat pump improves the device and method of sea water desaltination efficiency ", its apparatus structure more complicated, manufacture maintenance cost also relatively high, operation energy consumption is high, although cost decreases compared with current three large main flow desalination technologies, but be not still very desirable, heat energy recycling is lower.
Summary of the invention
The technical problem to be solved in the present invention is, overcome the above-mentioned defect that prior art exists, provide a kind of heat energy recycling rate high, operation energy consumption is low, and working efficiency is high, the method for desalting seawater that cost is low and device.
The technical scheme that the present invention solves the employing of its technical problem is:
The method for desalting seawater of the present invention is:
Seawater, after interchanger, directly enters vaporizer, or flows through the fresh water circulating box being built-in with another interchanger, after the fresh water heat absorption in fresh water circulating box, enter vaporizer again, the evaporation work of seawater in vaporizer divides two sections, front and back to complete: the leading portion evaporation work of seawater is, seawater mainly relies on the heat of self in vaporizer, to realize evaporation (when seawater flows through the fresh water circulating box being built-in with interchanger, when entering vaporizer again after the fresh water heat absorption in fresh water circulating box, the heat of the leading portion evaporation work of seawater also comprises the heat absorbed from the fresh water in fresh water circulating box), the back segment evaporation work of seawater: seawater absorbs fresh water latent heat that vaporizer internal recycling and evaporates that (namely seawater absorbs the latent heat of the fresh water circulated in fresh water circulation loop in the first vaporizer in the first vaporizer, described fresh water circulation loop is made up of spraying cycle pump, condensation injector, fresh water circulating box and vaporizer), in vaporizer, fresh water reduces latent heat to seawater, realizes extra large evaporation of water, the steam that the evaporation of vaporizer maritime interior waters produces, condensation is carried out at condensation injector place, steam gives fresh water Feedback of latent heating again at condensation injector place, fresh water temperature is raised, fresh water after intensification is ejected in fresh water circulating box by condensation injector, fresh water after intensification carries out heat exchange with seawater in fresh water circulating box again injected recycle pump suction vaporizer, fresh water temperature after heat exchange reduces, fresh water after temperature reduces receives at condensation injector place and evaporates by vaporizer maritime interior waters the steam feedback and next latent heat that produce, heat circulation and transfer is realized by condensation and evaporation mode, while mass transfer process, also pass again thermal property by condensation injector and realize desalting process, the strong brine produced after the evaporation of vaporizer maritime interior waters is discharged by strong brine overboard pump, be injected into the fresh water in fresh water circulating box by condensation injector, collect after cooling.
When fresh water enters before condensation injector, temperature only has about 25 degree, like this, be conducive to the efficiency improving injection and condensing water vapor, realize injecting heat to vaporizer continually, injecting the fluid that heat relies on is exactly jetting fluid (i.e. fresh water), spray liquid flow body heat content inherently from absorbed by injection the steam of coming the latent heat that discharges.Evaporation of seawater inhale latent heat major part from the fresh water in working cycle, and the latent heat that fresh water heat energy discharges at condensation injector place from steam, because the mode of fresh water circulation has to flow through vaporizer.Vaporizer, by forming this kind of countercurrent heat exchange method, and by arranging condenser in vaporizer, make the fresh water entering vaporizer be the circulation fresh water of comparatively high temps, and the fresh water flowing out vaporizer is the fresh water that temperature is lower.The strong brine of discharging from vaporizer can be carried out again double evaporation-cooling by strong brine overboard pump and be concentrated, evaporate for three times and concentrate, evaporate for four times with concentrated, even evaporates and concentrates for five times.
The sea water desalinating plant of the present invention comprises the first spraying cycle pump, the first condensation injector, the first fresh water circulating box and the first vaporizer; First fresh water circulating box bottom is connected by the inlet end of pipeline with the first vaporizer, the exit end of the first vaporizer is connected by the inlet end of pipeline with the first spraying cycle pump, first spraying cycle pump outlet end is connected by the inlet end of pipeline with the first condensation injector, the exit end of the first condensation injector is provided with the mouth of pipe and stretches into pipeline in the first fresh water circulating box, and the injection end interface of the first condensation injector is connected to the vacuum chamber of the first vaporizer by pipeline; First fresh water circulating box inside is equipped with the 3rd interchanger; The exit end of the 3rd interchanger is connected to the first vaporizer by pipeline, the exit end of First Heat Exchanger is connected by the inlet end of pipeline with the second interchanger, the exit end of the second interchanger is connected by the inlet end of pipeline with the 3rd interchanger being placed in the first fresh water circulating box inside, the inlet end of First Heat Exchanger is that seawater flows into end, and the exit end of the second interchanger is also connected to the first vaporizer by pipeline; Described first vaporizer is connected by pipeline strong brine overboard pump.
Further, described first fresh water circulating box bottom is connected with another inlet end of First Heat Exchanger by pipeline, and another exit end of First Heat Exchanger is fresh water collecting end.
Further, the pipeline that the exit end of described second interchanger is connected with the first vaporizer is provided with the first valve.
Further, the pipeline that the exit end of described second interchanger is connected with the inlet end of the 3rd interchanger being placed in the first fresh water circulating box inside is provided with the second valve.
Further, the pipeline that described first fresh water circulating box bottom is connected with another inlet end of First Heat Exchanger is provided with the 3rd valve.
Further, the present invention also comprises at least one circulating and evaporating concentration systems again, and strong brine overboard pump output terminal is connected with circulating and evaporating concentration systems again.
Further, the described concentration systems of circulating and evaporating again comprises the 4th interchanger, a strong brine is discharged delivery side of pump and is connected by the inlet end of pipeline with the 4th interchanger, the exit end of the 4th interchanger is connected by the inlet end of pipeline with the 5th interchanger be placed in the second fresh water circulating box, the exit end of the 5th interchanger is connected to the second vaporizer by pipeline, the vacuum chamber of the second vaporizer is connected to the injection end interface of the second condensation injector by pipeline, the exit end of the second condensation injector is provided with the mouth of pipe and stretches into pipeline road in the second fresh water circulating box, second fresh water circulating box bottom is connected by the inlet end of pipeline with the second vaporizer, the exit end of the second vaporizer is connected with the inlet end of the second condensation injector by the second spraying cycle pump, second vaporizer is connected with secondary strong brine overboard pump by pipeline.
Further, described second fresh water circulating box bottom is also connected with another inlet end of First Heat Exchanger by pipeline.
Further, the pipeline that described second fresh water circulating box is connected with another inlet end of First Heat Exchanger is provided with the 4th valve.Described 3rd valve is a fresh water output variable valve, and the 4th valve is secondary fresh water output variable valve.
Further, described first vaporizer the 3rd vaporizer that is built-in with condenser substitutes.
Further, the inlet end of the condenser in described 3rd vaporizer is that seawater flows into end, the exit end of the condenser in the 3rd vaporizer is connected with the inlet end of well heater by pipeline, condensed water suction pump is provided with below condenser in 3rd vaporizer, the exit end of well heater is connected to the 3rd vaporizer by pipeline, 3rd vaporizer is connected with the inlet end of recycle pump by pipeline, the exit end of recycle pump is connected with the inlet end by pipeline the 3rd condensation injector, the exit end of the 3rd condensation injector is provided with the mouth of pipe and stretches into pipeline in the 3rd fresh water circulating box, 3rd fresh water circulating box bottom is connected to the 3rd vaporizer by pipeline, the injection end interface of the 3rd condensation injector is connected to the 3rd vaporizer by pipeline.
Further, described 3rd vaporizer and condenser are one-piece construction.
Further, described 3rd vaporizer is by the external strong brine discharge line of another strong brine overboard pump.
Further, described 3rd fresh water circulating box is by the external fresh water outlet pipe of check valve.
The present invention utilizes condensation injector to make vaporizer inside form relative vacuum, makes the seawater entered in vaporizer under relative vacuum environment, carry out the evaporation of lesser temps.We know, condensation injector has been widely used in the vacuum-evaporation of the industry such as food, chemical industry, light industry, pharmacy, dyestuff, sugaring, deodorization, vacuum distilling, vacuum concentration, vacuum crystallization, the various explained hereafter occasion such as vacuum-drying.Condensation injector mainly contains following feature: 1. make water and vapour contact area greatly with multi-nozzle structure formation, be conducive to energy exchange, vapour can be made fully to condense into water and discharge latent heat to spraying fluid; 2. condensation injector volume is little, compact construction, and working efficiency is high, and current consumption is low; 3. use easy and simple to handle, easy to maintenance, mechanical transmission, and noise is low; 4. floor space is little, can install by indoor low level, saves floor area of building and installation costs; 5. Large Towers class, still class, oil-sealed rotary pump and condensing equipment can be replaced.But, the working efficiency of condensation injector be improved, because the performance of condensation injector and efficiency change comparatively large, it is both relevant with workmanship with the structural shape of complete assembly, size, also have much relations with working conditions.Need further investigation and grasp relevant rule, high efficiency operation could be realized.The working efficiency of complete assembly not only depends on condensation injector design optimization degree, also depend on the size of each significant parameter point in this device workflow, as by injection medium fluid temperature, the temperature of spraying fluid, also have and spray the flow velocity of fluid and the size etc. of pressure; The PLB2000 model parameter of producing from Hu Jiang ejector vacuum pump factory is seen: institute's adapted impeller pump power is 22kw, and the work water yield is 80m
3/ h, the Inlet and outlet water temperature difference is 18 DEG C, work water temperature is 25 DEG C, when in driven fluid volume, vacuum tightness is 660mmHg, this condensation injector suction secondary steam amount is 2000kg/h, along with vacuum tightness be reduced to 200mmHg gradually time, its aspiration has increased to 20000kg/h, but must maintaining more than 91 DEG C temperature in evaporation cavity, just can to make in evaporation cavity that absolute pressure reaches 560mmHg(vacuum tightness be 200mmHg), this just needs to injecting more heat energy in evaporation cavity.What model was PSB-500 is joined circulation pump power is equally also 22kw, and when vacuum tightness is 710mmHg, its rate of air sucked in required is 5 m
3/ h, if when vacuum tightness is reduced to 525mmHg, this condensation injector rate of air sucked in required can reach 50 m
3/ h, when can find out vacuum tightness decline about 73%, its aspiration increase by 1000%.Compared with it should be pointed out that the condensation of chewing with single spraying sprays, although the condensation injector efficiency of high-order many nozzles is high, under conventional higher vacuum tightness (as 84 ~ 89kpa i.e. 630 ~ 670mmhg), its efficiency or obviously reduce.Therefore, vacuumize with condensation injector under a high vacuum and will consume larger power.The kind of condensation injector is a lot, mode of operation with have many uses general, its structure is simple, easy to manufacture, bookkeeping convenient.In fact, sea water desaltination does not need very high vacuum environment, in order to acquire fresh water, instead of seawater concentrate after salt solution, we only need seawater to be concentrated into about 6% just enough.Condensation injector is used for sea water desaltination and is also of great significance, this drawn based on comparing with other various desalination technologies, even if vacuum tightness is reduced to below 14Kpa, evaporation of seawater problem can be realized very well, realize by constantly injecting heat energy to seawater, this heat energy can adopt Recycle design to realize.Reduce injection stream temperature and raise driven fluid temperature and can improve induction efficiency, but considering to heat to driven fluid to consume more heat energy, and reduce injection stream temperature and also will consume more electric energy, therefore not calculate.But, the present invention is condensed into liquid state injection injection steam out at condensation injector place and discharges latent heat, this part latent heat again feeds back to and sprays operating fresh water, this part latent heat is made fully to obtain recycle, and again this partial heat energy is sucked in vaporizer by spraying cycle pump, allow Absorption by Sea Water circulate in fresh water latent heat and evaporated, so this part heat energy reduces again to seawater, so become lower from the fresh water temperature of vaporizer outflow, like this, be conducive to the efficiency improving injection and condensing water vapor, seawater is evaporated after obtaining this latent heat, and this partial heat energy is fed back to fresh water again at condensation injector, like this, circulate again and again, and inject more heat need not to the seawater flowing into vaporizer, also need not lower the temperature to the fresh water entering condensation injector, the low temperature fresh water for spraying wanted can be obtained, the vaporization heat that should possess when simultaneously also can obtain evaporation of seawater, thus realize the circulation of most of heat energy, we only need disposable injection heat energy, evaporate in vaporizer, condensation in injector, realize the working cycle that heat energy goes round and begins again.And the heat interchanging area of interchanger can be saved with the heat exchange that condensation and evaporation mode carry out.Existing condensation injector is not by heat energy recycling, and just heating to required dry thing simply, or opposing jet body carries out water cooling tower cooling, also can be air-cooled.This efficient sea water desalting and waste disposal plant and method, it comprises vaporizer, condensation injector, spraying cycle pump, heat exchanger, fresh water circulating box, strong brine extractor pump.
The present invention also can be used for sewage disposal, needs water constituent major part to be evaporated, so just can realize the zero release of sewage, make most water in sewage obtain recycle during sewage disposal.So cost of sewage disposal is higher than sea water desaltination cost, because concentration is higher, water-absorbent is higher, and water evaporation difficulty just strengthens, and due to concentration of wastewater larger, block interchanger possibility larger.
Device volume of the present invention is little, occupies little space, stable and reliable operation, and without the need to configuring suction air device, working efficiency is high, and steam output is also large, to consume power source few, vacuum duration state is good, output fresh water quality better.Use the present invention, not only can reduce device fabrication cost, also sea water desaltination energy consumption can be down to below 1.5 degree of electricity/tons simultaneously, more energy-conservation; Not only proper scale preparing fresh, is also specially adapted to submarine, steamer, the western water quality of island and China poor etc. local for producing the fresh water drunk, applied widely.
Accompanying drawing explanation
Fig. 1 is the sea water desalinating plant structural representation of the embodiment of the present invention 1;
Fig. 2 is the sea water desalinating plant structural representation of the embodiment of the present invention 2;
Fig. 3 is the sea water desalinating plant structural representation of the embodiment of the present invention 3.
Embodiment
Below in conjunction with drawings and Examples, the invention will be further described.
Embodiment 1:
With reference to Fig. 1, the present embodiment sea water desalinating plant comprises the first spraying cycle pump 2, first condensation injector 3, first fresh water circulating box 4 and the first vaporizer 1; First fresh water circulating box 4 bottom is connected by the inlet end of pipeline with the first vaporizer 1, the exit end of the first vaporizer 1 is connected by the inlet end of pipeline with the first spraying cycle pump 2, the exit end of the first spraying cycle pump 2 is connected by the inlet end of pipeline with the first condensation injector 3, the exit end of the first condensation injector 3 is provided with the mouth of pipe and stretches into pipeline in the first fresh water circulating box 4, and the injection end interface of the first condensation injector 3 is connected to the vacuum chamber of the first vaporizer 1 by pipeline; First fresh water circulating box 4 inside is equipped with the 3rd interchanger; The exit end of the 3rd interchanger is connected to the first vaporizer 1 by pipeline, the exit end of First Heat Exchanger 7 is connected by the inlet end of pipeline with the second interchanger 6, the exit end of the second interchanger 6 is connected by the inlet end of pipeline with the 3rd interchanger being placed in the first fresh water circulating box 4 inside, the inlet end of First Heat Exchanger 7 is that the exit end that seawater flows into end 9, second interchanger 6 is also connected to the first vaporizer 1 by pipeline;
Described first vaporizer 1 is connected by pipeline strong brine overboard pump 5.
Described first fresh water circulating box 4 bottom is connected with another inlet end of First Heat Exchanger 7 by pipeline, and another exit end of First Heat Exchanger 7 is fresh water collecting end 8.
The pipeline that the exit end of described second interchanger 6 is connected with the first vaporizer 1 is provided with the first valve 10.
The pipeline that the exit end of described second interchanger 6 is connected with the inlet end of the 3rd interchanger being placed in the first fresh water circulating box 4 inside is provided with the second valve 11.
The pipeline that described first fresh water circulating box 4 bottom is connected with another inlet end of First Heat Exchanger 7 is provided with the 3rd valve 12.
Described first spraying cycle pump 2, first condensation injector 3, first fresh water circulating box 4 and the first vaporizer 1 form fresh water circulation loop.
The efficient sea water desalting method of the present invention: the seawater after filtration flows into end 9 from seawater and flows into First Heat Exchanger 7, after seawater tentatively heats up in First Heat Exchanger 7, flow into the second interchanger 6 again, second interchanger 6 is mainly used in as seawater injects heat, seawater is by there being two current available through route after the second interchanger 6: Article 1 seawater flows through route and is, when circulation fresh water temperature is too high, first valve 10 is closed, second valve 11 is opened, when seawater passes through the interchanger of the first fresh water circulating box 4 inside, its most of heat is passed to seawater by the fresh water in the first fresh water circulating box 4, seawater relies on the heat of self and obtains heat from fresh water, enter in the first vaporizer 1 and realize evaporation, seawater own temperature declines, complete the leading portion evaporation work of seawater thus, complete after leading portion evaporation work until seawater, seawater absorbs the latent heat of the fresh water circulated in fresh water circulation loop in the first vaporizer, realizes extra large evaporation of water, completes the back segment evaporation work of seawater thus.Another seawater flows through route, first valve 10 is opened, second valve 11 is closed, seawater directly enters evaporation in the first vaporizer 1 by the first valve 10 and produces steam, now, seawater equally also divides two sections, front and back to complete (the leading portion evaporation work of seawater: seawater relies on the heat of self to realize evaporation in the first vaporizer 1 in the evaporation work of the first vaporizer 1; The back segment evaporation work of seawater: seawater absorbs the latent heat of the fresh water circulated in fresh water circulation loop in the first vaporizer, realizes extra large evaporation of water).The power that first condensation injector 3 is provided by the first spraying cycle pump 2, after the fresh water sucking-off in the first fresh water circulating box 4, when flowing through the first vaporizer 1, the latent heat of the thermal energy of fresh water needed for evaporation of seawater (namely above in mention " latent heat that seawater absorbs the fresh water circulated in fresh water circulation loop in the first vaporizer "), fresh water temperature is reduced and squeezes in the first condensation injector 3 to carry out condensation injection, be injected into the first fresh water circulating box 4 by the first condensation injector 3; Meanwhile, the steam of the first vaporizer 1 inside is carried out condensation by injection to the first condensation injector 3, thus makes steam latent heat feed back to fresh water again.The seawater be concentrated is discharged (now, also this part strong brine can will be carried out again second time evaporation with concentrated, detailed in Example 2) by the strong brine overboard pump 5 be connected with the first vaporizer 1.Be injected into the fresh water of the first fresh water circulating box 4 by the first condensation injector 3, flow to First Heat Exchanger 7 through the 3rd valve 12, flowed out by fresh water collecting end 8 after fresh water temperature being declined by First Heat Exchanger 7, collected by peripheral equipment fresh water standby pool.First Heat Exchanger 7 is when lowering the temperature to fresh water, and the heat of fresh water output for the Absorption by Sea Water flowing into end 9 inflow from seawater, can realize the preliminary intensification to flowing into the seawater that end 9 flows into from seawater.
Embodiment 2:
The difference of the present embodiment device and embodiment 1 device is: also comprise at least one circulating and evaporating concentration systems again, and strong brine overboard pump 5 output terminal is connected with circulating and evaporating concentration systems again.
The present embodiment for one again circulating and evaporating concentration systems be described.
With reference to Fig. 2, the described concentration systems of circulating and evaporating again comprises the 4th interchanger 18, the output terminal of a strong brine overboard pump 5 is connected by the inlet end of pipeline with the 4th interchanger 18, the exit end of the 4th interchanger 18 is connected by the inlet end of pipeline with the 5th interchanger be placed in the second fresh water circulating box 16, the exit end of the 5th interchanger is connected to the second vaporizer 13 by pipeline, the vacuum chamber of the second vaporizer 13 is connected to the injection end interface of the second condensation injector 15 by pipeline, the exit end of the second condensation injector 15 is provided with the mouth of pipe and stretches into pipeline in the second fresh water circulating box 16, second fresh water circulating box 16 bottom is connected by the inlet end of pipeline with the second vaporizer 13, the exit end of the second vaporizer 13 is connected with the inlet end of the second condensation injector 15 by the second spraying cycle pump 14, second vaporizer 13 is connected with secondary strong brine overboard pump 19 by pipeline.
Described second fresh water circulating box 16 bottom is connected with another inlet end of First Heat Exchanger 7 by pipeline.
The pipeline that described second fresh water circulating box 16 is connected with another inlet end of First Heat Exchanger 7 is provided with the 4th valve 17.Described 3rd valve 12 is a fresh water output variable valve, and the 4th valve 17 is secondary fresh water output variable valve.
Strong brine overboard pump 5 is squeezed into the concentrated seawater that first time evaporation is discharged after the 4th interchanger 18 heats, heat balance is carried out in the second fresh water circulating box 16, and then flow in the second vaporizer 13 and carry out second time evaporation with concentrated, vaporized steam is by entering in the second fresh water circulating box 16 after the second condensation injector 15 injection condensation, major part fresh water flows out the second fresh water circulating box 16 and sucks release latent heat in the second vaporizer 13 by the second spraying cycle pump 14, after cooling again from the second vaporizer 13 out, and be pressed in the second condensation injector 15 by the second spraying cycle pump 14 and carry out work, remove injection and steam in condensation second vaporizer 13, like this, complete working cycle again and again, finally, by secondary strong brine overboard pump 19 in the seawater discharge again concentrated or press-in the 3rd circulating and evaporating concentration systems.
First time evaporation concentration concentration of seawater out generally can reach about 6%, generally adopt single vaporization with concentrated just enough for producing fresh water, if need highly enriched further, user can arrange the identical concentration systems of circulating and evaporating again of multiple structure as required, and the quantity of circulating and evaporating concentration systems is determined according to demand by user again.
Each fresh water circulating box not only has water storage function, with provide respective spray recycle pump can fresh water outside, the effect carrying out heat exchange with seawater can also be played, and each fresh water circulating box position is higher than corresponding evaporator, like this, gas can not be there is in vaporizer block up, also be convenient to spraying cycle pump and can not produce cavitation erosion situation.
Fresh water in described first vaporizer 1, second vaporizer 13 therein loop direction must and seawater formed adverse current, and seawater sprays on corresponding evaporator top has evaporating space, fall warm seawater and fall into the latent heat that can obtain circulation fresh water further and continue evaporation after a part of steam of evaporation, like this, just can guarantee that seawater has enough vaporization heats, and make in vaporizer, there is enough pressure (referring to absolute pressure), to diminish with the difference of injection pressure, thus be conducive to the efficiency improving corresponding condensation injector work.
All the other are with embodiment 1.
Embodiment 3:
The difference of the present embodiment device and embodiment 1 device is: described first vaporizer the 3rd vaporizer 28 that is built-in with condenser substitutes.
The present embodiment by arranging condenser in the 3rd vaporizer 28, the inlet end of the condenser in the 3rd vaporizer 28 is that seawater flows into end, the exit end of the condenser in the 3rd vaporizer 28 is connected by the inlet end of pipeline with well heater 30, condensed water suction pump 24 is provided with below condenser in 3rd vaporizer 28, the exit end of well heater 30 is connected to the 3rd vaporizer 28 by pipeline, 3rd vaporizer 28 is connected by the inlet end of pipeline with recycle pump 20, the exit end of recycle pump 20 is connected with the inlet end by pipeline the 3rd condensation injector 21, the exit end of the 3rd condensation injector 21 is provided with the mouth of pipe and stretches into pipeline in the 3rd fresh water circulating box 22, 3rd fresh water circulating box 22 bottom is connected to the 3rd vaporizer 28 by pipeline, the injection end interface of the 3rd condensation injector 21 is connected to the 3rd vaporizer 28 by pipeline.
3rd vaporizer 28 is by the external strong brine discharge line 26 of another strong brine overboard pump 25.
3rd fresh water circulating box 22 is by the external fresh water outlet pipe 27 of check valve 23.
Seawater 29 directly enters the condenser in vaporizer 28, condensing water vapor, thus seawater temperature is raised, and the steam be condensed is extracted out by condensed water suction pump 24, well heater 30 is for the further intensification before evaporation of seawater, when seawater is successively by the condenser in the 3rd vaporizer 28, after well heater 30 carries out twice intensification in front and back, evaporate in vaporizer 28, evaporative process is divided into two steps, the first step is that seawater allows a part of water evaporate in relative vacuum situation by self heat, second step is evaporated by the latent heat of Absorption by Sea Water the 3rd vaporizer 28 internal recycling fresh water, the steam that evaporation of seawater produces by the 3rd condensation injector 21 by recycle pump 20 the power injection that provides in the 3rd fresh water circulating box 22, fresh water in fresh water circulating box 22 is divided into two parts, sub-fraction flows into fresh water reserve tank by pipeline and check valve 23 by fresh water outlet pipe 27, another part then continues to suck injection fluid as the 3rd condensation injector 21 after release latent heat in the 3rd vaporizer 28 by recycle pump 20.The seawater be concentrated then is discharged by strong brine discharge line 26 by another strong brine overboard pump 25.
What the present embodiment adopted is another kind of heat energy recycling mode, and the recycle of a part of heat energy realizes by seawater preheating in vaporizer.
The present invention utilizes condensation injector condensing water vapor, and utilize the latent heat of fresh water in Absorption by Sea Water working cycle to realize evaporation, seawater after filtration is after the disposable injection heat energy of interchanger, in the enough situations of guarantee circulated heat, the seawater of follow-up inflow just need not inject so much heat, just make up the part heat energy lost in working cycle just passable, in fact, the heat energy injecting seawater is all transferred to the fresh water of circulation, and the fresh water heat of output is by carrying out thermal exchange with the seawater just flowing into whole device, fresh water temperature is lowered, just can flow into peripheral equipment fresh water standby pool.Evaporation and condensation are modes the most efficiently of conducting heat, like this, not only can save many heat exchanger areas, reduce facility investment expense, thermodynamic cycle can also be accelerated, save energy, play the dual function of condensation injector injection and condensing water vapor, evaporation of seawater steam out in corresponding condensation injector under rapid condensation, meanwhile, the latent heat that condensation discharges constantly enters into again in the fresh water of working cycle, like this, again for evaporation of seawater provides enough latent heat, heat energy is allowed to obtain recycle.Use the present invention, the temperature that each vaporizer internal flow is enough can not only be ensured, make there are enough vaporization heats during evaporation of seawater, and can also ensure that there is enough pressure (this refers to relative atmospheric to press as the absolute pressure under vacuum condition) vaporizer inside, ensure that the pressure of condensation injector institute injection is unlikely to too low and affects injector induction efficiency.Highly effective sea-water fresh water implementation procedure must be that fresh water internal circulating load is greater than seawater influx, like this, excessive seawater flow just can be avoided to slattern seawater circulation pump horsepower and inject the heat energy of seawater, and sea water desaltination rate is about 30% to be advisable, seawater flow is that fresh water internal circulating load about 75% is advisable.
In prior art, condensation injector is only for carrying out drying and suction steam, because its injection pressure (in vaporizer absolute pressure) is too low and cannot realize high injection ratio, because condensation injector leading portion working efficiency can be very high, but when vacuum tightness declines a lot, its efficiency is just corresponding reduction also, and can take away by the many heats of injection thing in injection process, so that temperature is too low, cause vacuum tightness too high, and spray pressure reduction will be excessive, like this, injection flow velocity will be strengthened, and consume many powers of motor, only having carries out heating to driven fluid just can make evaporation chamber pressure be brought up, and injection ratio is improved, but this will consume more multi-energy undoubtedly.And the present invention is by getting up heat energy recycling, while vaporizer inner fluid temperature is ensured, make vacuum tightness lower accordingly, injection volume is guaranteed.
Device volume of the present invention is little, occupies little space, stable and reliable operation, and without the need to configuring suction air device, working efficiency is high, and steam output is also large, to consume power source few, vacuum duration state is good, output fresh water quality better.Use the present invention, not only can reduce device fabrication cost, also sea water desaltination energy consumption can be down to below 1.5 degree of electricity/tons simultaneously; Not only proper scale preparing fresh, is also specially adapted to submarine, steamer, the western water quality of island and China poor etc. local as producing the fresh water drunk, applied widely.
Claims (10)
1. a method for desalting seawater, is characterized in that, seawater, after interchanger, directly enters vaporizer, or flows through the fresh water circulating box being built-in with another interchanger, after the fresh water heat absorption in fresh water circulating box, enter vaporizer again, the evaporation work of seawater in vaporizer divides two sections, front and back to complete: the leading portion evaporation work of seawater is that seawater mainly relies on the heat of self in vaporizer, realize evaporation, when seawater flows through the fresh water circulating box being built-in with interchanger, and when entering vaporizer again after the fresh water heat absorption in fresh water circulating box, the heat of the leading portion evaporation work of seawater also comprises the heat absorbed from the fresh water in fresh water circulating box, the back segment evaporation work of seawater: seawater absorbs fresh water latent heat that vaporizer internal recycling and evaporates in the first vaporizer, and in vaporizer, fresh water reduces latent heat to seawater, realizes extra large evaporation of water, the steam that the evaporation of vaporizer maritime interior waters produces, condensation is carried out at condensation injector place, steam gives fresh water Feedback of latent heating again at condensation injector place, fresh water temperature is raised, fresh water after intensification is ejected in fresh water circulating box by condensation injector, fresh water after intensification carries out heat exchange with seawater in fresh water circulating box again injected recycle pump suction vaporizer, fresh water temperature after heat exchange reduces, fresh water after temperature reduces is at condensation injector place, receive and evaporate by vaporizer maritime interior waters the steam feedback and next latent heat that produce, heat circulation and transfer is realized by condensation and evaporation mode, while mass transfer process, also pass again thermal property by condensation injector and realize desalting process, the strong brine produced after the evaporation of vaporizer maritime interior waters is discharged by strong brine overboard pump, is injected into the fresh water in fresh water circulating box, collects after cooling by condensation injector.
2. implement a device for method for desalting seawater as claimed in claim 1, it is characterized in that, comprise the first spraying cycle pump, the first condensation injector, the first fresh water circulating box and the first vaporizer; First fresh water circulating box bottom is connected by the inlet end of pipeline with the first vaporizer, the exit end of the first vaporizer is connected by the inlet end of pipeline with the first spraying cycle pump, first spraying cycle pump outlet end is connected by the inlet end of pipeline with the first condensation injector, the exit end of the first condensation injector is provided with the mouth of pipe and stretches into pipeline in the first fresh water circulating box, and the injection end interface of the first condensation injector is connected to the vacuum chamber of the first vaporizer by pipeline; First fresh water circulating box inside is equipped with the 3rd interchanger; The exit end of the 3rd interchanger is connected to the first vaporizer by pipeline, the exit end of First Heat Exchanger is connected by the inlet end of pipeline with the second interchanger, the exit end of the second interchanger is connected by the inlet end of pipeline with the 3rd interchanger being placed in the first fresh water circulating box inside, the inlet end of First Heat Exchanger is that seawater flows into end, and the exit end of the second interchanger is also connected to the first vaporizer by pipeline; Described first vaporizer is connected with a strong brine overboard pump by pipeline.
3. implement the device of method for desalting seawater according to claim 2, it is characterized in that, described first fresh water circulating box bottom is connected with another inlet end of First Heat Exchanger by pipeline, and another exit end of First Heat Exchanger is fresh water collecting end.
4. according to Claims 2 or 3, implement the device of method for desalting seawater, it is characterized in that, the pipeline that the exit end of described second interchanger is connected with the first vaporizer is provided with the first valve.
5. according to Claims 2 or 3, implement the device of method for desalting seawater, it is characterized in that, the pipeline that the exit end of described second interchanger is connected with the inlet end of the 3rd interchanger being placed in the first fresh water circulating box inside is provided with the second valve.
6. implement the device of method for desalting seawater according to claim 3, it is characterized in that, the pipeline that described first fresh water circulating box bottom is connected with another inlet end of First Heat Exchanger is provided with the 3rd valve.
7. implement the device of method for desalting seawater according to claim 2, it is characterized in that, also comprise at least one circulating and evaporating concentration systems again, strong brine overboard pump output terminal is connected with circulating and evaporating concentration systems again, the described concentration systems of circulating and evaporating again comprises the 4th interchanger, a strong brine is discharged delivery side of pump and is connected by the inlet end of pipeline with the 4th interchanger, the exit end of the 4th interchanger is connected by the inlet end of pipeline with the 5th interchanger be placed in the second fresh water circulating box, the exit end of the 5th interchanger is connected to the second vaporizer by pipeline, the vacuum chamber of the second vaporizer is connected to the injection end interface of the second condensation injector by pipeline, the exit end of the second condensation injector is provided with the mouth of pipe and stretches into pipeline in the second fresh water circulating box, second fresh water circulating box bottom is connected by the inlet end of pipeline with the second vaporizer, the exit end of the second vaporizer is connected with the inlet end of the second condensation injector by the second spraying cycle pump, second vaporizer is connected with secondary strong brine overboard pump by pipeline.
8. implement the device of method for desalting seawater according to claim 7, it is characterized in that, described second fresh water circulating box bottom is also connected with another inlet end of First Heat Exchanger by pipeline; The pipeline that described second fresh water circulating box is connected with another inlet end of First Heat Exchanger is provided with the 4th valve.
9. implement the device of method for desalting seawater according to claim 2, it is characterized in that, described first vaporizer the 3rd vaporizer that is built-in with condenser substitutes.
10. implement the device of method for desalting seawater according to claim 9, it is characterized in that, described 3rd vaporizer and condenser are one-piece construction.
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| CN111544913A (en) * | 2020-04-27 | 2020-08-18 | 广东中科光年数智科技有限公司 | Heat pump evaporation concentration system |
| CN113716799A (en) * | 2021-08-24 | 2021-11-30 | 长江生态环保集团有限公司 | System for garden water system and energy coupling are administered |
| CN114014399B (en) * | 2021-11-06 | 2023-03-24 | 海南月壤科技控股有限公司 | Almost zero energy consumption seawater desalination method and system |
| CN115520935B (en) * | 2022-09-29 | 2024-09-03 | 中冶焦耐(大连)工程技术有限公司 | A method and system for recovering high-temperature condensate from a coking plant |
| CN117534155B (en) * | 2023-12-20 | 2024-06-07 | 江苏聚德环保科技有限公司 | Seawater desalination equipment and method with high desalination rate |
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| CN101708871B (en) * | 2009-12-03 | 2011-06-29 | 招玉春 | Gradient preheating multistage evaporation-type seawater desalination power generation system |
| CN101948148B (en) * | 2010-10-22 | 2012-06-27 | 河北宏润重工股份有限公司 | Energy-saving low-temperature multiple-effect seawater desalting device |
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